Circulating liquid pump relay conveying method in two-stage or multi-stage hydrocarbon material expansion bed hydrogenation process

文档序号：1553466 发布日期：2020-01-21 浏览：22次中文

阅读说明：本技术 两级或多级碳氢料膨胀床氢化过程循环液泵接力输送方法 (Circulating liquid pump relay conveying method in two-stage or multi-stage hydrocarbon material expansion bed hydrogenation process ) 是由何巨堂于 2019-09-03 设计创作，主要内容包括：两级或多级碳氢料膨胀床氢化过程循环液泵接力输送方法,碳氢料可为重油和或煤,碳氢料膨胀床加氢反应过程UR包含液料串联反应的上游反应区R3、下游反应区R9,分离R9加氢反应产物得到的至少部分液体LOOPL返回R3进行循环反应,在R9设置液料加压泵PUMP9、R3设置液料3KL循环泵PUMP3时,LOOPL经过PUMP9升压后与液料3KL混合再进入PUMP3升压进入R3；本发明可将长程循环液的升压过程借助2个短程循环液升压泵完成,不需要设置长程循环液的专用升压泵,从而具有大幅度节省投资、节省能耗、节省安装空间、减少维修工作量的优点；高温高压含固体颗粒的循环反应浆液的接力输送过程常使用湿定子泵。(A circulating liquid PUMP relay conveying method in a two-stage or multi-stage hydrocarbon material expanded bed hydrogenation process is disclosed, a hydrocarbon material can be heavy oil or coal, a hydrocarbon material expanded bed hydrogenation reaction process UR comprises an upstream reaction zone R3 and a downstream reaction zone R9 of liquid material series reaction, at least part of liquid LOOPL obtained by separating a hydrogenation reaction product of R9 returns to R3 for circular reaction, when a liquid material pressure PUMP PUMP9 is arranged at R9 and a liquid material 3KL circulating PUMP PUMP3 is arranged at R3, the LOOPL is subjected to pressure boosting through PUMP9, then mixed with liquid material 3KL and enters into the PUMP3 to be boosted to enter into R3; the invention can complete the boosting process of the long-range circulating liquid by means of 2 short-range circulating liquid booster pumps without arranging a special booster pump of the long-range circulating liquid, thereby having the advantages of greatly saving investment, energy consumption, installation space and maintenance workload; the relay conveying process of the high-temperature high-pressure circulating reaction slurry containing the solid particles usually uses a wet stator pump.)

1. The relay conveying method of the circulating liquid pump in the two-stage or multi-stage hydrocarbon material expansion bed hydrogenation process comprises the following steps:

in the process of hydrogenation of a hydrocarbon material in an expanded bed UR, under the condition that hydrogen and liquid-phase hydrocarbon exist and a mixed-phase material of solid particles possibly exists at the same time, a first raw material URF at least containing carbon element and hydrogen element is subjected to an expanded bed hydrogenation URR to obtain a hydrogenation reaction product BASE-URP, a hydrogenation reaction effluent URP-X is discharged, and a net product URP in the hydrogenation reaction process is discharged;

a first raw material URF comprising a liquid raw material URFL and, if present, a solid particulate raw material URFs;

a liquid feedstock URFL comprising a hydrocarbon component composition having a conventional boiling point > 350 ℃ and possibly comprising a hydrocarbon component having a conventional boiling point > 530 ℃;

expanded bed hydroprocessing reactions URR comprising at least a part of the hydrorefining reactions of the liquid feedstock URFL, comprising at least a part of the hydro-thermal cracking reactions of the liquid feedstock URFL, possibly comprising at least a part of the hydro-thermal cracking reactions of the solid material URFS that may be present, possibly comprising at least a part of the hydro-stabilizing reactions of the thermally cracked radicals;

in the process UR of the hydrogenation reaction of the hydrocarbon material expanded bed, a hydrogenation catalyst URC may be used, and the hydrogenation catalyst URC may contain molybdenum element and/or iron element;

the hydrogenation reaction product BASE-URP is a mixed phase material which contains hydrogen and liquid phase hydrocarbon and possibly contains solid particles;

a material based on the BASE-URP of the hydrogenation reaction product is used as the URP-X of the hydrogenation reaction effluent; the hydrogenation reaction effluent URP-X appears in the form of 1 or 2 or more paths of materials, and is a gas phase or a liquid phase or a gas-liquid mixed phase or a gas-liquid-solid three-phase material flow;

the liquid stream URP-L, which is the effluent URP-X of the hydrogenation, may contain solid particles;

the gas-liquid mixed phase stream URP-M belonging to the hydrogenation reaction effluent URP-X may contain solid particles;

the hydrogenation reaction stage refers to a flow path section from the beginning of a hydrogenation reaction process of a hydrocarbon raw material containing liquid hydrocarbon to the gas-liquid separation process of a hydrogenation product of the hydrocarbon raw material to obtain at least one liquid-phase product consisting of at least one part of generated oil, and comprises the hydrogenation reaction process of the hydrogenation reaction stage and the gas-liquid separation process of at least one part of the hydrogenation reaction product of the hydrogenation reaction stage;

the hydrogenation reaction level RK with the forced circulation reaction of the liquid product of the reaction level RK refers to that in a separation step RKP-S of the reaction level RK, liquid RKP-SL obtained by separating the liquid RKP product of the hydrogenation reaction level RKP is forced to be pressurized by a circulating PUMP RKP-SL-PUMP and then returns to a reaction area of the hydrogenation reaction level RK for circulation reaction without passing through an upstream hydrogenation reaction level, and at least a part of the liquid reaction product of the liquid RKP-SL enters the product RKP;

the hydrogenation reaction process UR of the hydrocarbon material expanded bed uses 2 or more liquid material serial reaction stages, wherein the 2 adjacent reaction stages refer to that liquid material RSP-L99 containing liquid phase based on the product RSP of the upstream reaction stage RS enters a reaction zone of the adjacent downstream reaction stage RT for hydrogenation reaction, and no other hydrogenation reaction stage exists between the 2 adjacent reaction stages RS and RT;

when a plurality of liquid materials are used in the hydrogenation reaction process UR of the hydrocarbon material expansion bed, the 2 non-adjacent reaction stages RJ and RT refer to that liquid-phase-containing material RMP-X based on an upstream reaction stage RJP passes through at least 1 intermediate reaction stage RM to obtain a hydrogenation reaction product RSP of an RT adjacent upstream reaction stage RS, the liquid-phase-containing material RSP-L99 based on the hydrogenation reaction product RSP of the adjacent upstream reaction stage RS enters a reaction zone of the downstream reaction stage RT for hydrogenation reaction, and when only one intermediate reaction stage RM exists, the reaction stage RM is the adjacent upstream reaction stage RS of the reaction stage RT;

the hydrocarbon material expanded bed hydrogenation reaction process UR comprises 2 or more hydrogenation reaction stages of liquid material serial hydrogenation reaction, wherein each hydrogenation reaction stage uses at least 1 hydrogenation reactor, and each hydrogenation reaction stage uses at least 1 expanded bed hydrogenation reactor;

in the hydrogenation reaction process UR of the hydrocarbon material expanded bed, the liquid material serial hydrogenation reaction process comprises 2 or more hydrogenation reaction stages, and two adjacent upstream reaction stages RS and two adjacent downstream reaction stages RT exist;

in the process of hydrogenation of the hydrocarbon material expanded bed UR, when the liquid material serial hydrogenation reaction process comprises a plurality of hydrogenation reaction stages, an upstream reaction stage RJ and a downstream reaction stage RT which are not adjacent exist;

the hydrocarbon material expanded bed hydrogenation reaction process UR comprises 2 or more hydrogenation reaction stages of liquid material serial hydrogenation reaction, wherein at least 2 hydrogenation reaction stages, namely an upstream reaction stage RX and a downstream reaction stage RT belong to the hydrogenation reaction stage of the forced circulation reaction of liquid products in the reaction stage;

the flow relation between the upstream reaction stage RX and the downstream reaction stage RT is the adjacent reaction stages or the non-adjacent reaction stages;

in the hydrogenation reaction process UR of the hydrocarbon material expansion bed, a long-range circulating liquid RTTORX-RL exists, the long-range circulating liquid RTTORX-RL is a liquid material which is from a downstream reaction stage RT and has the same composition with the feeding of a downstream reaction stage RT circulating PUMP RKP-SL-PUMP, and the long-range circulating liquid RTTORX-RL circularly returns to a hydrogenation reaction zone of an upstream reaction stage RX for hydrogenation reaction;

the conveying process of the long-range circulating liquid RTTORX-RL is characterized in that:

① the long-range circulating liquid RTTORX-RL from the downstream reaction stage RT is mixed with the forced circulating reaction liquid RT-RL of the downstream reaction stage RT which is conveyed by the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT, and is separated into at least 2 paths after being pressurized by the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT:

the first path is used as pressurized circulating reaction liquid RT-RL of the reaction stage and enters a reaction area of a downstream reaction stage RT for at least partial hydrogenation reaction, and the second path is used as long-range circulating liquid RTTORX-RL-DP1 after primary pressurization;

② the circulating reaction liquid RXT-RL of the upstream reaction stage RX enters the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX and enters the reaction area of the upstream reaction stage RX for at least partial hydrogenation reaction after being pressurized;

meanwhile, the long-range circulating liquid RTTORX-RL-DP1 after primary pressurization is mixed with the circulating PUMP RXP-SL-PUMP feeding RX-RL of the upstream reaction stage RX, and is pressurized by the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX, and part or all of the liquid material discharged by the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX enters a reaction area of the upstream reaction stage RX to carry out at least part of hydrogenation reaction.

2. The method of claim 1, wherein:

the hydrocarbon material expanded bed hydrogenation reaction process UR comprises 2 or more hydrogenation reaction stages of liquid material serial hydrogenation reaction, and liquid-phase material RSP-L99 based on the reaction effluent RSP of the upstream hydrogenation reaction stage RS enters a reaction zone of the adjacent downstream hydrogenation reaction stage RT of the upstream hydrogenation reaction stage RS to carry out at least part of hydrogenation reaction;

liquid phase containing material RSP-L99 selected from one or more of the following streams:

① part or all of the reaction effluent RSP is used as liquid phase containing material RSP-L99;

② part or all of the reaction effluent RSP enters into a thermal high-pressure separation process RSP-HS to be separated into thermal high-oil-content RSP-HSO and thermal high-gas-content RSP-HSV, and at least a part of the thermal high-oil-content RSP-HSO is used as liquid-phase-containing material RSP-L99;

③ partial or all reaction effluents RSP enter a thermal high-pressure separation process RSP-HS to be separated into thermal high-oil-content RSP-HSO and thermal high-gas-content RSP-HSV, at least one part of the thermal high-oil-content RSP-HSO is depressurized, and liquid RSP-HSOA obtained after degassing is used as liquid-phase-containing material RSP-L99;

④ part or all of the reaction effluent RSP enters a cold high-pressure separation process RSP-CS to be separated into cold high-oil content RSP-CSO and cold high-gas content RSP-CSV, and at least a part of the cold high-oil content RSP-CSO is used as liquid-phase material RSP-L99;

⑤ separating partial or all reaction effluent RSP to obtain hydrogenated oil RSPPO and hydrogen-rich gas;

in the fractionation part of the hydrogenated oil RSPPO, separating a hydrocarbon liquid stream obtained by the hydrogenated oil RSPPO to be used as a liquid-phase-containing material RSP-L99;

⑥ separating partial or all reaction effluent RSP to obtain hydrogenated oil RSPPO and hydrogen-rich gas;

in the hydrogenation product oil RSPPO fractionation part, separating a stream which is obtained by hydrogenation product oil RSPPO and mainly consists of hydrocarbon components with the conventional boiling point higher than 350 ℃ and using the stream as a liquid-phase-containing material RSP-L99;

⑦ separating partial or all reaction effluent RSP to obtain hydrogenated oil RSPPO and hydrogen-rich gas;

in the fractionation section of hydrogenated oil RSPPO, a stream composed mainly of hydrocarbon components having a conventional boiling point of more than 530 ℃ and obtained by separating hydrogenated oil RSPPO is used as a liquid-phase-containing material RSP-L99.

3. The method of claim 1, wherein:

expanded bed hydrogenation process for hydrocarbon feedstock UR, the first feedstock URF comprising a liquid feedstock URFL and a solid particulate feedstock URFs;

the solid particle raw material URFS is selected from 1 or more of the following materials:

① pulverized coal;

② plastic powder;

③ powdered rubber;

④ the process of coal hydrogenation direct liquefaction RU blending other carbon hydrogen powder.

4. The method of claim 1, wherein:

expanded bed hydrogenation process for hydrocarbon feedstock UR, the first feedstock URF comprising a liquid feedstock URFL and a solid particulate feedstock URFs;

the solid particle raw material URFS is selected from 1 or more of the following materials:

① pulverized coal;

② solid particles of catalyst;

③ Sulfur powder;

④ semi-coke particles carried by hydrocarbon oil coke;

⑤ plastic powder;

⑥ powdered rubber;

⑦ hydrogenation of hydrocarbon powder to directly liquefy RU other solid powder needed to be input.

5. The method of claim 1, wherein:

the hydrogenation process UR of the hydrocarbon material expanded bed is a direct coal hydrogenation liquefaction reaction process and is selected from 1 or more of the following process flows:

① direct coal liquefaction oil production process using hydrogen donor solvent oil;

② direct coal hydrogenation liquefaction oil-making process without using hydrogen-supplying solvent oil;

③ kerosene refining process;

④ A process for hydrothermally dissolving coal.

6. The method of claim 1, further comprising:

expanded bed hydrogenation process of hydrocarbon feedstock UR, the first feedstock URF comprising a liquid feedstock URFL and possibly a solid particulate feedstock URFs;

liquid feedstock URFL consisting essentially of hydrocarbon components having a conventional boiling point > 350 ℃ and containing hydrocarbon components having a conventional boiling point > 530 ℃;

the liquid raw material URFL is selected from one or more of the following materials:

① low temperature coal tar or distillate oil thereof or oil obtained from thermal processing process thereof, wherein the thermal processing process is distillation process or thermal cracking process or coking process or catalytic cracking process;

② the medium temperature coal tar or distillate oil thereof or oil obtained from the thermal processing process thereof, the thermal processing process is distillation process or thermal cracking process or coking process or catalytic cracking process;

③ high temperature coal tar or distillate oil thereof or oil obtained from thermal processing process thereof, the thermal processing process is distillation process or thermal cracking process or coking process or catalytic cracking process;

④ the process of preparing oil by directly liquefying coal by hydrogenation or the process of thermal processing comprises the process of preparing oil by directly liquefying coal by hydrogenation without using hydrogen-supplying solvent oil, the process of preparing oil by directly liquefying coal by hydrogenation with hydrogen-supplying solvent oil, the process of co-refining oil and coal, and the process of hydro-thermal solution of coal, wherein the thermal processing process is a distillation process or a thermal cracking process or a coking process or a catalytic cracking process;

⑤ petroleum-based heavy oil or distillate oil thereof or oil obtained from thermal processing process thereof, wherein the thermal processing process is distillation process, thermal cracking process, coking process, catalytic cracking process or catalytic cracking process;

⑥ shale oil or its distillate or oil obtained from its thermal processing, wherein the thermal processing is distillation, thermal cracking, coking, catalytic cracking, or catalytic cracking;

⑦ petroleum sand-based heavy oil or distillate oil thereof or oil obtained by thermal processing, wherein the thermal processing is distillation process, thermal cracking process, coking process, catalytic cracking process or catalytic cracking process;

⑧ other hydrocarbon oils having a gum weight content of greater than 15% and or an asphaltene weight content of greater than 5.0%.

7. The method of claim 1, wherein:

in the process UR of the hydrogenation in the expanded hydrocarbon bed, the operating mode of the hydrogenation reactor in the expanded hydrocarbon bed is selected from 1 or more of the following modes:

① suspension bed reactor, namely slurry bed reactor;

② ebullated bed reactors;

③ combined suspended bed and ebullated bed reactor;

④ micro-expanded bed reactor.

8. The method of claim 1, wherein:

option 1, in a reactor XRUE, a reverse-flow reactor with a pure countercurrent working mode is adopted for liquid materials and gas materials;

option 2, in the reactor XRUE, the collected liquid of which the top is provided with a liquid collecting cup is pressurized by a circulating pump and then forcibly circulated and returned to the fluidized bed reactor of the XRUE raw material inlet;

option 3, in the reactor XRUE, the collected liquid of which the top is provided with a liquid collecting cup is pressurized by a circulating pump and then forcibly circulated and returned to the suspended bed reactor of the XRUE raw material inlet;

option 4, in the reactor XRUE, the collected liquid of which the top is provided with a liquid collecting cup is pressurized by a circulating pump and then forcibly circulated and returned to the fluidized bed reactor at the raw material inlet of the reactor XRUE, and the circulating pump conveys the circulating liquid and simultaneously conveys liquid material products to the downstream;

option 5, in the reactor XRUE, the collected liquid of which the top is provided with a liquid collecting cup is pressurized by a circulating pump and then forcibly circulated and returned to the suspended bed reactor at the raw material inlet of the reactor XRUE, and the circulating pump conveys the circulating liquid and simultaneously conveys liquid material products to the downstream;

option 6, in the reactor XRUE, the collected liquid with the liquid collecting cup arranged at the top is pressurized by a circulating pump and then forcibly circulated and returned to the fluidized bed reactor at the raw material inlet of the reactor XRUE, and meanwhile, other collected liquids discharged by the collecting cup are conveyed to the downstream by other special feeding pumps to obtain liquid material products;

option 7, in the reactor XRUE, the collected liquid with the liquid collecting cup arranged at the top is pressurized by a circulating pump and then forcibly circulated and returned to the suspended bed reactor at the raw material inlet of the reactor XRUE, and meanwhile, other collected liquids discharged by the collecting cup are conveyed to the downstream by other special feeding pumps to obtain liquid material products;

option 8, in the reactor XRUE, a liquid collecting cup is arranged at the top of the reactor, liquid products are discharged by the liquid collecting cup and conveyed to the downstream by a special feeding pump, and a fluidized bed reactor system for forced circulation of the liquid products is not arranged;

option 9, in the reactor XRUE, a liquid collecting cup is arranged at the top of the reactor, liquid products are discharged by the liquid collecting cup and conveyed to the downstream by a special feeding pump, and a suspension bed reactor system for forced circulation of the liquid products is not arranged;

option 10, in the reactor XRUE, the collected liquid of the liquid collecting cup arranged at the top is pressurized by a circulating pump and then forcibly circulated and returned to the combined reactor of the boiling bed and the fluidized bed at the raw material inlet of the reactor XRUE;

option 11, in the reactor XRUE, the collected liquid of which the top is provided with a liquid collecting cup is pressurized by a circulating pump and then forcibly circulated and returned to a combined reactor of a boiling bed and a boiling bed at the raw material inlet of the reactor XRUE, and the circulating pump conveys the circulating liquid and simultaneously conveys liquid material products to the downstream;

option 12, in the reactor XRUE, the collected liquid of which the top is provided with a liquid collecting cup is pressurized by a circulating pump and then forcibly circulated and returned to a combined reactor of a boiling bed and a boiling bed at a raw material inlet of the reactor XRUE, and meanwhile, other collected liquid discharged by the collecting cup is conveyed to the downstream by other special feeding pumps to obtain liquid material products;

option 13, reactor XRUE, a suspended bed reactor system with a central up-flow and peripheral down-flow pattern with internal draft tubes;

option 14, reactor XRUE, a suspended bed reactor system with a central down-flow and peripheral up-flow pattern with internal draft tubes;

option 15, reactor XRUE, an empty-tube bubbling bed suspended bed reactor system;

option 16, reactor XRUE, using external reactor circulation tubes, provides an external reactor loop flow from the liquid phase downflow of the upper reactor zone back to the lower reactor zone.

9. The method of claim 1, wherein:

the way of obtaining liquid product possibly containing solid from the reaction stage in the process of hydrogenation of hydrocarbon material expanded bed UR is selected from 1 or several of the following ways:

① the liquid material discharged from the gas-liquid separation process of the reaction product of the reaction level is used as the reaction product of the liquid material of the reaction level;

② the last reactor of the reaction stage uses a pure countercurrent reactor, and the liquid material discharged from the bottom liquid phase zone of the last reactor of the reaction stage is used as the liquid material product of the reaction stage;

③ a liquid collecting cup at the top is arranged in the last reactor of the reaction stage, and the liquid material discharged from the liquid collecting cup in the last reactor of the reaction stage through the flow guide pipe is used as the liquid material product of the reaction stage;

④ a liquid collecting cup at the top is arranged in the last reactor of the reaction stage, and the liquid material discharged from the liquid collecting cup in the last reactor of the reaction stage through the flow guide pipe is used as the liquid material to be degassed;

separating the liquid material to be degassed into a path of liquid flow rich in bubbles and a path of liquid flow poor in bubbles through a cyclone separation step;

a gas bubble-depleted liquid stream is used as a reaction grade liquid feed product.

10. The method of claim 1, wherein:

in the process UR of the hydrogenation reaction of the hydrocarbon material expanded bed, the last hydrogenation reactor R19 of the first reaction stage is a reactor with a partial liquid removal function, the top of the reactor is provided with a liquid collecting cup R19-DL, and a collecting liquid R19-DL-L led out by the liquid collecting cup R19-DL is taken as a liquid material product of the first reaction stage and is led to one or more of the following components:

① go to the second effect;

② removing the first reaction stage liquid product, separating into degassed liquid and gas;

③ recycling to the first reaction stage;

④ part of the collected liquid R19-DL-L is depressurized by a pressure reducing valve and then sent to a separation and recovery system.

11. The method of claim 1, wherein:

expanded bed hydrogenation process of hydrocarbon feedstock UR, the first feedstock URF comprising a liquid feedstock URFL and possibly a solid particulate feedstock URFs;

the liquid feed URFL consists essentially of hydrocarbon components with a conventional boiling point > 530 ℃.

12. The method of claim 1, further comprising:

in the hydrocarbon material expanded bed hydrogenation process UR, the ratio of the weight flow rate RTTORX-RL-W of the long-range circulating liquid RTTORX-RL to the weight flow rate URF-W of the first raw material URF is FK100, FK100 is (RTTORX-RL-W)/(URF-W), FK100 is selected from 1 of the following:

① is 0.001-0.30;

② is 0.30-0.60;

③ is 0.60 to 1.00;

④ is 1.00 to 2.00.

13. The method of claim 1, further comprising:

in the hydrocarbon material expanded bed hydrogenation reaction process UR, the ratio of the weight flow rate RTTORX-RL-W of the long-range circulating liquid RTTORX-RL to the weight flow rate RT-RL-W of the forced circulation reaction liquid RT-RL of the downstream reaction stage RT is FK500, FK500 ═ RTTORX-RL-W)/(RT-RL-W), FK500 is selected from 1 of the following:

① is 0.001-0.06;

② is 0.06-0.12;

③ is 0.12-0.20;

④ is 0.20 to 0.40.

14. The method of claim 1, further comprising:

the pressure of the long-range circulating liquid RTTORX-RL increased by a downstream reaction stage RT circulating PUMP RTP-SL-PUMP is 0.05-0.8 MPa;

the pressure of the long-range circulating liquid RTTORX-RL increased by a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX is 0.05-0.8 MPa.

15. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, and the working mode is selected from one of the following modes:

① conveying high temperature liquid;

② delivering high pressure liquid;

③ delivering high temperature and high pressure liquid;

④ delivering liquid material containing toxic components;

⑤ conveying liquid material containing corrosive components;

⑤ delivering volatile component-containing liquid;

⑥ delivering liquid material containing easily coagulating component;

⑦ conveying a material containing a solid component;

⑧ carry a portion of the bubble-containing material.

16. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, liquid materials conveyed by the PUMPs are high-temperature and high-pressure coal liquefaction intermediate product slurry or final product slurry in the coal hydrogenation direct liquefaction reaction process, and the operation conditions are as follows: the liquid material has a solid concentration of 5 to 55 wt%, a temperature of 390 to 480 ℃ and a pressure of 4.0 to 38.0 MPa.

17. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, liquid materials conveyed by the PUMPs are high-temperature and high-pressure intermediate product liquid materials or final product liquid materials in the heavy oil expanded bed hydrogenation reaction process, and the operation conditions are as follows: the liquid material has a solid concentration of 0.001 to 35 wt%, a temperature of 350 to 480 ℃ and a pressure of 4.0 to 38.0 MPa.

18. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, and the operating conditions of the inlet process medium of the PUMP cavity of the PUMPs are as follows: the temperature is-150 to 650 ℃, the pressure is 0.1 to 40.0MPa, and the volume flow rate of liquid at the inlet of the pump cavity is 0.1 to 10000m³H; the pump impeller applies energy to the process medium to increase the pressure of the process medium by 0.01-5.0 MPa; the pump impeller set uses 2-20 impellers operated in series.

19. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, the process medium conveyed in the PUMP shells of the PUMPs is high-temperature and high-pressure slurry in the direct coal hydrogenation liquefaction reaction process, and the operation conditions are as follows: the temperature is 370-500 ℃, the pressure is 4.0-38.0 MPa, the solid concentration is 5-55%, and the volume flow rate of liquid at the inlet of the pump cavity is 5.0-10000 m³H; the pump impeller applies energy to the process fluid to increase the pressure of the process fluid by 0.10-1.5 MPa; the pump impeller set uses 2-5 impellers operated in series.

20. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT and the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are both single-stage impeller centrifugal PUMPs.

21. The method of claim 1, further comprising:

the downstream reaction stage RT circulating PUMP RTP-SL-PUMP is a centrifugal PUMP, and can use 1 impeller or serially connect 2 impellers or serially connect a plurality of impellers;

the circulation PUMP RXP-SL-PUMP of the upstream effect RX is a centrifugal PUMP, possibly using 1 impeller or 2 impellers in series or a plurality of impellers in series.

22. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, and the arrangement modes of the PUMPs are selected from 1 mode of the following modes:

① horizontal arrangement, motor rotor shaft horizontal arrangement;

② is obliquely arranged, the rotor of the motor is obliquely arranged, and the elevation of the side of the motor is higher than that of the side of the pump cavity;

③, the motor rotor is arranged obliquely, and the elevation of the motor side is lower than that of the pump cavity side;

④ vertical arrangement, the motor rotor is vertical arrangement, the motor is above the pump cavity;

⑤ is arranged vertically, the rotor of the motor is arranged vertically, and the motor is arranged under the pump cavity.

23. The method of claim 1, further comprising:

the circulation PUMPs RTP-SL-PUMP of the downstream reaction stage RT or the circulation PUMPs RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, the use of these PUMPs to arrange a lining of the PUMP chamber wall in the PUMP chamber, selected from 1 or several of the following:

① erosion and abrasion resistant liner;

② corrosion resistant liner;

③ heat resistant bushings;

④ low temperature resistant bushings;

⑤ locating other parts.

24. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, and the purpose of arranging a lining on the inner wall of a liquid inlet connecting pipe and/or a lining on the inner wall of a liquid outlet connecting pipe in a PUMP cavity of the PUMPs is selected from 1 or more of the following PUMPs:

① erosion and abrasion resistant liner;

② corrosion resistant liner;

③ heat resistant bushings;

④ low temperature resistant bushings;

⑤ locating other parts.

25. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, 2-stage or multi-stage impellers are arranged in PUMP cavities of the PUMPs, and at least one stage of impeller is provided with an inducer.

26. The method of claim 1, further comprising:

the circulation PUMPs RTP-SL-PUMP of the downstream effect RT or RXP-SL-PUMP of the upstream effect RX are centrifugal PUMPs which are arranged in a way that 2 or more stages of impellers are arranged in the PUMP cavity, selected from 1 of the following ways:

① single-sided cantilevered arrangement of 2-stage or multi-stage impellers;

② a 2-stage or multi-stage impeller is arranged on one side of the impeller, the support part is composed of a bearing and a bearing sleeve, and the bearing sleeve is fixed and positioned;

③ 2 cantilever-type 2-stage or multi-stage impeller;

④ arranging 2-stage or multi-stage impellers in a single-side opposite mode;

⑤ double-sided opposed arrangement of 2 or more stage impellers.

27. The method of claim 1, further comprising:

28. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are gland-free centrifugal PUMPs which are shielded electric centrifugal PUMPs.

29. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are shaft seal-free centrifugal PUMPs, and the motors matched with the PUMPs are motors with heat screens or motors without heat screens.

30. The method of claim 1, further comprising:

a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are shaft seal-free centrifugal PUMPs which are provided with auxiliary liquid FZL input systems; the auxiliary liquid FZL is used as a flushing liquid and is used for preventing the process fluid in the pump shell from flowing into the cavity of the canned motor pump in a serial mode, the operating pressure of the auxiliary liquid input system is larger than the operating pressure of the process fluid in the pump shell, and at least one part of the auxiliary liquid FZL enters the pump shell through the flow channel to be mixed with the process fluid and is discharged out of the pump cavity along with the process fluid;

the used motor is provided with an injection interface E-K1 of the lubricating liquid and/or the cooling liquid EL of a motor cavity; the lubricating liquid and/or the cooling liquid EL is used for cooling and lubricating a rotor and a cavity of the motor;

and the discharge of the lubricating liquid andor the cooling liquid EL of the motor cavity is used for preventing the auxiliary liquid FZL andor the liquid in the pump cavity from flowing into the shielding motor cavity.

31. The method of claim 1, further comprising:

a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are shaft seal-free centrifugal PUMPs which are provided with auxiliary liquid FZL input systems; the auxiliary liquid FZL is used as a flushing liquid and is used for preventing the process fluid in the pump shell from flowing into the cavity of the electric pump in series, the operating pressure of the auxiliary liquid input system is greater than the operating pressure of the process fluid in the pump shell, and at least one part of the auxiliary liquid FZL enters the pump shell through the flow channel to be mixed with the process fluid and is discharged out of the pump cavity along with the process fluid;

the discharge of the lubricating liquid andor the cooling liquid EL of the motor cavity is used for preventing the auxiliary liquid FZL andor the liquid in the pump cavity from flowing into the motor cavity;

when the motor works normally, the operating pressure of a liquid existing area in the cavity of the motor is greater than the operating pressure of process fluid in the pump shell and is also greater than the operating pressure of fluid in the auxiliary liquid FZL of the electric pump, so that at least a part of EL enters the auxiliary liquid system through the flow channel and is mixed with the auxiliary liquid FZL to form mixed liquid EL-FZL, and at least a part of the mixed liquid EL-FZL enters the pump shell through the flow channel and is mixed with the process fluid to realize the replacement of the liquid in the cavity of the motor;

when the electric pump works, the process fluid enters the pump cavity of the electric pump from the process fluid inlet, flows through the impeller to receive the energy transmitted by the impeller, and then leaves the pump cavity of the electric pump from the process fluid outlet to become the boosted process fluid; the boosted process fluid comprises at least a portion of the auxiliary liquid FZL.

32. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are shaft seal-free centrifugal PUMPs, at least comprise a first basic assembly PUMP body and a second basic assembly shielding motor, and a third basic assembly connector is possibly used;

when the connecting body is used, one end of the connecting body is in butt joint with a pump shell, the other end of the connecting body is in butt joint with a motor, and a shaft of a motor rotor penetrates through the connecting body and then enters the front end part in the pump shell to be used as a shaft for mounting a pump impeller.

33. The method of claim 1, further comprising:

the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are non-shaft seal centrifugal PUMPs, at least one part of cooling and lubricating liquid DJL flowing through the gap between a motor stator and a motor rotor in the motor shell and the other part of cooling and lubricating liquid DJL flowing through the half-stroke external cooling chamber of the motor stator in the motor cavity;

inside the high temperature section of the motor shell, an overflowing gap of a circulating flow loop of cooling and lubricating liquid DJL for the motor rotor is formed and is used as a half-stroke external cooling chamber of a motor stator and an internal cooling chamber of the high temperature section of the motor shell.

Technical Field

The invention relates to a circulating liquid PUMP relay conveying method in a two-stage or multistage hydrocarbon material expanded bed hydrogenation process, wherein a hydrocarbon material can be heavy oil or coal, a hydrocarbon material expanded bed hydrogenation reaction process UR comprises an upstream reaction zone R3 and a downstream reaction zone R9 of liquid material series reaction, at least part of liquid LOOPL obtained by separating a R9 hydrogenation reaction product returns to R3 for circular reaction, and when a liquid material pressure PUMP PUMP9 is arranged at R9 and a liquid material 3KL circulating PUMP PUMP3 is arranged at R3, the LOOPL is subjected to pressure boosting through PUMP9, then is mixed with a liquid material 3KL 3 and then enters R3 after being subjected to pressure boosting; the invention can complete the boosting process of the long-range circulating liquid by means of 2 short-range circulating liquid booster pumps without arranging a special booster pump of the long-range circulating liquid, thereby having the advantages of greatly saving investment, energy consumption, installation space and maintenance workload; the relay conveying process of the high-temperature high-pressure circulating reaction slurry containing the solid particles usually uses a wet stator pump.

Background

With the progress of the technology of the hydrocarbon material expanded bed hydrogenation reaction process, a 'one-to-two or one-to-many' conveying requirement occurs in the pressurized conveying process of the intermediate slurry product or the final slurry product of the reaction process, for example, in the 3-stage coal hydrogenation direct liquefaction reaction process CTL using 3 reactors or the suspension bed hydrocracking reaction process of petroleum-based vacuum residue, the slurry product of the second hydrogenation reactor R2 needs to be conveyed and divided into three outgoing branch materials: the first path returns to the first hydrogenation reactor R1 as long-circulating slurry, the second path returns to the second hydrogenation reactor R2 as short-circulating slurry, and the third path is sent to the third reactor as 3-stage reaction raw material slurry.

Based on the above description, the circulating reaction liquid transferred across the reaction zone in the two-stage or multi-stage hydrocarbon material expanded bed hydrogenation reaction process has the following conventional transfer modes:

the scheme I adopts a one-to-one conveying scheme, namely a centrifugal pump is independently arranged to convey the circulating reaction liquid across the reaction zone, and the scheme has the advantages of adding a set of pump set, having huge investment, increasing installation space, being complex in system, increasing a fault point, and increasing the workload and cost of maintenance;

② scheme II, based on the downstream reaction zone R9 circulating liquid material pressure PUMP PUMP9, because the high-pressure high-temperature shielding electric PUMP is expensive, in order to save investment, a PUMP can be used to carry out a pressure mode of carrying out the same lift in a combined manner of 'pressurizing the circulating liquid material of the downstream reaction zone R9 by itself and pressurizing the circulating liquid material of the downstream reaction zone R9 to the upstream reaction zone R3 across the reaction zones', after pressurization, the pipeline system is divided into 2 paths to respectively remove 2 flow positions with different operating pressures, so that the 2 paths of discharged materials have the same lift and only can be the path 1 path meeting the maximum lift, namely meeting the lift required by pressurizing the circulating liquid material across the reaction zones, therefore, the PUMP PUMP9 has a complex structure and high energy consumption, and the lift of the short-path circulating slurry has a large residue, and the residual lift is used as a part with throttling effect in a slurry flow channel, is eroded and abraded power, and is usually consumed on throttling elements such as flow control valves, and the solid concentration of the slurry is high, therefore, the service life of the control valve core is very short, thereby influencing the accuracy, and the safety and stability of the production and stability;

the scheme makes the lift of the short circulating liquid material increased inefficiently, does not need to reduce the impeller stage number and the rotating speed of the pump, can increase the manufacturing difficulty of the pump set, obviously increases the power of a motor, increases the size of equipment, increases the weight of the equipment, increases the heat productivity of a stator and a rotor, finally obviously increases the manufacturing cost, increases the operation energy consumption, increases the installation difficulty, increases the installation space, and is also not beneficial to the transportation and the maintenance;

③ according to the third embodiment, based on the downstream reaction region R9 circulating liquid material pressurizing PUMP9, in order to save investment, a PUMP is adopted to perform pressurization of circulating liquid material in the downstream reaction region R9 and pressurization of circulating liquid material in the downstream reaction region R9 to the upstream reaction region R3 across the reaction regions in a combined manner of different lifts, such as a shielded electric centrifugal PUMP for conveying high-temperature and high-pressure coal slurry in the coal hydrogenation direct liquefaction reaction process, a shielded electric PUMP provided with 2 stages or multi-stage impellers is used to pressurize one inlet liquid material in 2018, and then convey slurry containing solids to at least 2 flow points with different operating pressures, the centrifugal PUMP has to be provided with 2 stages or multi-stage impellers in order to achieve the purpose of realizing at least 2 different lift liquid materials, so that the impeller has to be provided with 2 stages or multi-stage impellers, which has to cause the centrifugal PUMP to have complicated structure and enlarged PUMP cavity, and the PUMP shell has to increase the difficulty of manufacturing of the impeller PUMP, increase the difficulty of manufacturing the PUMP casing, increase the difficulty of the axial separation of solid slurry containing liquid particles, and the difficulty of the slurry containing solid particles in the PUMP, and the maintenance of the PUMP, and the difficulty of the slurry containing solid particles in the PUMP, and the maintenance of the slurry containing the slurry containing particles in the impeller PUMP, the dynamic slurry containing the impeller has to cause the high-stage impeller to deviate from the high-level of the slurry containing slurry.

In order to eliminate the drawbacks of the 3 solutions described above, the invention envisages: a circulating liquid PUMP relay conveying method in a two-stage or multi-stage hydrocarbon material expanded bed hydrogenation process is disclosed, a hydrocarbon material can be heavy oil or coal, a hydrocarbon material expanded bed hydrogenation reaction process UR comprises an upstream reaction zone R3 and a downstream reaction zone R9, liquid materials are reacted in series, at least part of liquid LOOPL obtained by separating a hydrogenation reaction product of R9 is returned to R3 for a circulating reaction, when a self liquid material pressurizing PUMP PUMP9 is arranged in R9, and a liquid material 3KL circulating PUMP PUMP3 is arranged in R3, the LOOPL is subjected to pressure boosting through PUMP9, then mixed with liquid material 3KL, and enters R3 after being subjected to pressure boosting through PUMP 3.

The invention has the advantages or characteristics that:

① the pressure increasing process of the long-range circulating liquid is completed by 2 existing short-range circulating liquid pressure increasing pumps, no special pressure increasing pump for the long-range circulating liquid is needed, the number of circulating pumps is reduced, the investment can be greatly saved, the installation space can be saved, and the maintenance workload can be reduced;

②, the manufacturing difficulty of the circulating liquid material pressure PUMP PUMP9 of the downstream reaction zone R9 can be reduced, the motor power, the equipment size, the equipment weight and the rotor heating value are reduced, the manufacturing cost and the operation energy consumption are finally obviously reduced, the installation difficulty is reduced, the installation space is saved, and the transportation and the maintenance are convenient;

③ the relay transportation process of the circulating reaction slurry containing solid particles at high temperature and high pressure usually uses a wet stator pump, and can also use a shield pump or other forms of centrifugal pumps.

The invention provides a two-stage or multi-stage circulating liquid pump relay conveying method in the hydrogenation process of a hydrocarbon material expansion bed, and similar technologies are not reported.

The invention aims to provide a relay conveying method for a circulating liquid pump in a two-stage or multi-stage hydrocarbon material expansion bed hydrogenation process, wherein a wet stator pump is generally used in the relay conveying process of high-temperature and high-pressure circulating reaction slurry containing solid particles, and a shield pump or other centrifugal pumps can also be used.

Disclosure of Invention

The invention relates to a two-stage or multi-stage circulating liquid pump relay conveying method in a hydrogenation process of a hydrocarbon material expansion bed, which comprises the following steps:

a first raw material URF comprising a liquid raw material URFL and, if present, a solid particulate raw material URFs;

the hydrogenation reaction product BASE-URP is a mixed phase material which contains hydrogen and liquid phase hydrocarbon and possibly contains solid particles;

the liquid stream URP-L, which is the effluent URP-X of the hydrogenation, may contain solid particles;

the gas-liquid mixed phase stream URP-M belonging to the hydrogenation reaction effluent URP-X may contain solid particles;

the hydrocarbon material expanded bed hydrogenation reaction process UR comprises 2 or more hydrogenation reaction stages of liquid material serial hydrogenation reaction, wherein at least 2 hydrogenation reaction stages, namely an upstream reaction stage RX and a downstream reaction stage RT belong to the hydrogenation reaction stage of the forced circulation reaction of liquid products in the reaction stage;

the flow relation between the upstream reaction stage RX and the downstream reaction stage RT is the adjacent reaction stages or the non-adjacent reaction stages;

the conveying process of the long-range circulating liquid RTTORX-RL is characterized in that:

According to the invention, a hydrogenation reaction process UR of a hydrocarbon material expanded bed comprises 2 or more hydrogenation reaction stages of liquid material serial hydrogenation reaction, and liquid-phase-containing material RSP-L99 based on reaction effluent RSP of an upstream hydrogenation reaction stage RS enters a reaction zone of an adjacent downstream hydrogenation reaction stage RT of the upstream hydrogenation reaction stage RS to carry out at least part of hydrogenation reaction;

the liquid phase containing material RSP-L99 can be selected from one or more of the following streams:

① part or all of the reaction effluent RSP is used as liquid phase containing material RSP-L99;

⑤ separating partial or all reaction effluent RSP to obtain hydrogenated oil RSPPO and hydrogen-rich gas;

in the fractionation part of the hydrogenated oil RSPPO, separating a hydrocarbon liquid stream obtained by the hydrogenated oil RSPPO to be used as a liquid-phase-containing material RSP-L99;

⑥ separating partial or all reaction effluent RSP to obtain hydrogenated oil RSPPO and hydrogen-rich gas;

⑦ separating partial or all reaction effluent RSP to obtain hydrogenated oil RSPPO and hydrogen-rich gas;

According to the present invention, generally, the hydrocarbon feedstock expanded bed hydrogenation process UR, the first feedstock URF comprises a liquid feedstock URFL and a solid particulate feedstock URFs;

the solid particulate raw material URFS may be selected from 1 or several of the following:

① pulverized coal;

② plastic powder;

③ powdered rubber;

④ the process of coal hydrogenation direct liquefaction RU blending other carbon hydrogen powder.

the solid particulate raw material URFS may be selected from 1 or several of the following:

① pulverized coal;

② solid particles of catalyst;

③ Sulfur powder;

④ semi-coke particles carried by hydrocarbon oil coke;

⑤ plastic powder;

⑥ powdered rubber;

⑦ hydrogenation of hydrocarbon powder to directly liquefy RU other solid powder needed to be input.

In the invention, when the hydrogenation process UR of the hydrocarbon material expanded bed is a direct coal hydrogenation liquefaction reaction process, 1 or more of the following processes can be selected:

① direct coal liquefaction oil production process using hydrogen donor solvent oil;

② direct coal hydrogenation liquefaction oil-making process without using hydrogen-supplying solvent oil;

③ kerosene refining process;

④ A process for hydrothermally dissolving coal.

According to the invention, in general, the hydrocarbon feedstock expanded bed hydrogenation process UR, the first feedstock URF comprises a liquid feedstock URFL and, if present, a solid particulate feedstock URFs;

the liquid raw material URFL can be selected from one or more of the following materials:

⑥ shale oil or its distillate or oil obtained from its thermal processing, wherein the thermal processing is distillation, thermal cracking, coking, catalytic cracking, or catalytic cracking;

⑧ other hydrocarbon oils having a gum weight content of greater than 15% and or an asphaltene weight content of greater than 5.0%.

In the present invention, generally, the hydrocarbon material expanded bed hydrogenation process UR uses a hydrocarbon material expanded bed hydrogenation reactor operating in a mode selected from 1 or more of the following:

① suspension bed reactor, namely slurry bed reactor;

② ebullated bed reactors;

③ combined suspended bed and ebullated bed reactor;

④ micro-expanded bed reactor.

option 1, in a reactor XRUE, a reverse-flow reactor with a pure countercurrent working mode is adopted for liquid materials and gas materials;

option 13, reactor XRUE, a suspended bed reactor system with a central up-flow and peripheral down-flow pattern with internal draft tubes;

option 14, reactor XRUE, a suspended bed reactor system with a central down-flow and peripheral up-flow pattern with internal draft tubes;

option 15, reactor XRUE, an empty-tube bubbling bed suspended bed reactor system;

option 16, reactor XRUE, using external reactor circulation tubes, provides an external reactor loop flow from the liquid phase downflow of the upper reactor zone back to the lower reactor zone.

In the present invention, generally, the manner in which the reaction stage obtains a liquid product that may contain solids in the expanded-bed hydrogenation process UR of the hydrocarbon feedstock is selected from 1 or more of the following manners:

① the liquid material discharged from the gas-liquid separation process of the reaction product of the reaction level is used as the reaction product of the liquid material of the reaction level;

separating the liquid material to be degassed into a path of liquid flow rich in bubbles and a path of liquid flow poor in bubbles through a cyclone separation step;

a gas bubble-depleted liquid stream is used as a reaction grade liquid feed product.

In the invention, in general, in the hydrocarbon material expanded bed hydrogenation process UR, the last hydrogenation reactor R19 of the first reaction stage is a reactor with a partial liquid removal function and provided with a liquid collecting cup R19-DL at the top, and a collected liquid R19-DL-L led out of the liquid collecting cup R19-DL is taken as a liquid material product of the first reaction stage and is directed to one or more selected from the following components:

① go to the second effect;

② removing the first reaction stage liquid product, separating into degassed liquid and gas;

③ recycling to the first reaction stage;

④ part of the collected liquid R19-DL-L is depressurized by a pressure reducing valve and then sent to a separation and recovery system.

the liquid feed URFL consists essentially of hydrocarbon components with a conventional boiling point > 530 ℃.

According to the invention, in the hydrogenation process UR of the hydrocarbon material expanded bed, the ratio of the weight flow rate RTTORX-RL-W of the long-range circulating liquid RTTORX-RL to the weight flow rate URF-W of the first raw material URF is FK100, FK100 is (RTTORX-RL-W)/(URF-W), FK100 is usually selected from 1 of the following:

① is 0.001-0.30;

② is 0.30-0.60;

③ is 0.60 to 1.00;

④ is 1.00 to 2.00.

In the invention, in the hydrocarbon material expanded bed hydrogenation reaction process UR, the ratio of the weight flow rate RTTORX-RL-W of the long-range circulating liquid RTTORX-RL to the weight flow rate RT-RL-W of the forced circulating reaction liquid RT-RL of the downstream reaction stage RT is FK500, FK500 ═ (RTTORX-RL-W)/(RT-RL-W), FK500 is generally selected from 1 of the following:

① is 0.001-0.06;

② is 0.06-0.12;

③ is 0.12-0.20;

④ is 0.20 to 0.40.

In the invention, generally, the pressure of the long-range circulating liquid RTTORX-RL increased by a downstream reaction stage RT circulating PUMP RTP-SL-PUMP is 0.05-0.8 MPa;

the pressure of the long-range circulating liquid RTTORX-RL increased by a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX is 0.05-0.8 MPa.

In the present invention, the circulation PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulation PUMP RXP-SL-PUMP of the upstream reaction stage RX is generally a centrifugal PUMP, and the operation mode is selected from one of the following:

① conveying high temperature liquid;

② delivering high pressure liquid;

③ delivering high temperature and high pressure liquid;

④ delivering liquid material containing toxic components;

⑤ conveying liquid material containing corrosive components;

⑤ delivering volatile component-containing liquid;

⑥ delivering liquid material containing easily coagulating component;

⑦ conveying a material containing a solid component;

⑧ carry a portion of the bubble-containing material.

In the invention, generally, the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, the liquid material delivered by the PUMPs is high-temperature and high-pressure coal liquefaction intermediate product slurry or final product slurry in the coal hydrogenation direct liquefaction reaction process, and the operation conditions are as follows: the liquid material has a solid concentration of 5 to 55 wt%, a temperature of 390 to 480 ℃ and a pressure of 4.0 to 38.0 MPa.

In the invention, a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are centrifugal PUMPs, liquid materials delivered by the PUMPs are high-temperature and high-pressure intermediate product liquid materials or final product liquid materials in the hydrogenation reaction process of a heavy oil expanded bed, and the operating conditions are as follows: the liquid material has a solid concentration of 0.001 to 35 wt%, a temperature of 350 to 480 ℃ and a pressure of 4.0 to 38.0 MPa.

In the present invention, the circulation PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulation PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, and the operating conditions of the inlet process medium of the PUMP chambers of these PUMPs are usually: the temperature is-150 to 650 ℃, the pressure is 0.1 to 40.0MPa, and the volume flow rate of liquid at the inlet of the pump cavity is 0.1 to 10000m³H; the pump impeller applies energy to the process medium to increase the pressure of the process medium by 0.01-5.0 MPa; the pump impeller set uses 2-20 impellers operated in series.

In the invention, a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are centrifugal PUMPs, a process medium conveyed in PUMP shells of the PUMPs is high-temperature and high-pressure slurry in a coal hydrogenation direct liquefaction reaction process, and the operation conditions are as follows: the temperature is 370-500 ℃, the pressure is 4.0-38.0 MPa, the solid concentration is 5-55%, and the volume flow rate of liquid at the inlet of the pump cavity is 5.0-10000 m³H; the pump impeller applies energy to the process fluid to increase the pressure of the process fluid by 0.10-1.5 MPa; the pump impeller set uses 2-5 impellers operated in series.

In general, a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT and a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are centrifugal PUMPs with single-stage impellers.

In the invention, generally, the downstream reaction stage RT circulating PUMP RTP-SL-PUMP is a centrifugal PUMP, and 1 impeller or 2 impellers in series or a plurality of impellers in series can be used;

the circulation PUMP RXP-SL-PUMP of the upstream effect RX is a centrifugal PUMP, possibly using 1 impeller or 2 impellers in series or a plurality of impellers in series.

According to the invention, the circulation PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulation PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, the arrangement of which is generally selected from 1 of the following ways:

① horizontal arrangement, motor rotor shaft horizontal arrangement;

② is obliquely arranged, the rotor of the motor is obliquely arranged, and the elevation of the side of the motor is higher than that of the side of the pump cavity;

③, the motor rotor is arranged obliquely, and the elevation of the motor side is lower than that of the pump cavity side;

④ vertical arrangement, the motor rotor is vertical arrangement, the motor is above the pump cavity;

⑤ is arranged vertically, the rotor of the motor is arranged vertically, and the motor is arranged under the pump cavity.

In the present invention, the circulation PUMPs RTP-SL-PUMP of the downstream reaction stage RT or the circulation PUMPs RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, the use of these PUMPs to arrange a lining of the PUMP cavity wall in the PUMP cavity is generally selected from 1 or several of the following:

① erosion and abrasion resistant bushings;

② corrosion resistant liner;

③ heat resistant bushings;

④ low temperature resistant bushings;

⑤ locating other parts.

According to the invention, the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, and the purpose of the PUMPs to arrange a lining on the inner wall of a liquid inlet connecting pipe and/or a lining on the inner wall of a liquid outlet connecting pipe in a PUMP cavity is generally selected from 1 or more of the following:

① erosion and abrasion resistant bushings;

② corrosion resistant liner;

③ heat resistant bushings;

④ low temperature resistant bushings;

⑤ locating other parts.

In the invention, generally, the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are centrifugal PUMPs, 2 or more stages of impellers are arranged in a PUMP cavity of the PUMPs, and at least one stage of impeller is provided with an inducer.

In general, the circulation PUMP RTP-SL-PUMP of the downstream effect RT or the circulation PUMP RXP-SL-PUMP of the upstream effect RX are centrifugal PUMPs, and the arrangement of these PUMPs in the PUMP chamber with 2 or more stages of impellers may be selected from 1 of the following ways:

① single-sided cantilevered arrangement of 2-stage or multi-stage impellers;

② a 2-stage or multi-stage impeller is arranged on one side of the impeller, the support part is composed of a bearing and a bearing sleeve, and the bearing sleeve is fixed and positioned;

③ 2 cantilever-type 2-stage or multi-stage impeller;

④ arranging 2-stage or multi-stage impellers in a single-side opposite mode;

⑤ double-sided opposed arrangement of 2 or more stage impellers.

In the invention, the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are non-shaft seal centrifugal PUMPs which can be wet stator non-shaft seal centrifugal PUMPs.

In the invention, the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are shaft seal-free centrifugal PUMPs which can be shielded electric centrifugal PUMPs.

In the invention, the circulating PUMP RTP-SL-PUMP of the downstream reaction stage RT or the circulating PUMP RXP-SL-PUMP of the upstream reaction stage RX are gland-seal-free centrifugal PUMPs, and the matching motors of the PUMPs can be motors with heat shields or motors without heat shields.

In the invention, a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are shaft-seal-free centrifugal PUMPs which can be provided with an auxiliary liquid FZL input system; the auxiliary liquid FZL is used as a flushing liquid and is used for preventing the process fluid in the pump shell from flowing into the cavity of the canned motor pump in a serial mode, the operating pressure of the auxiliary liquid input system is larger than the operating pressure of the process fluid in the pump shell, and at least one part of the auxiliary liquid FZL enters the pump shell through the flow channel to be mixed with the process fluid and is discharged out of the pump cavity along with the process fluid;

In the invention, a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are shaft-seal-free centrifugal PUMPs which can be provided with an auxiliary liquid FZL input system; the auxiliary liquid FZL is used as a flushing liquid and is used for preventing the process fluid in the pump shell from flowing into the cavity of the electric pump in series, the operating pressure of the auxiliary liquid input system is greater than the operating pressure of the process fluid in the pump shell, and at least one part of the auxiliary liquid FZL enters the pump shell through the flow channel to be mixed with the process fluid and is discharged out of the pump cavity along with the process fluid;

According to the invention, a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX is a shaft seal-free centrifugal PUMP, and generally at least comprises a first basic assembly PUMP body and a second basic assembly shielding motor, and a third basic assembly connector is possibly used;

In the invention, generally, a circulating PUMP RTP-SL-PUMP of a downstream reaction stage RT or a circulating PUMP RXP-SL-PUMP of an upstream reaction stage RX are shaft-seal-free centrifugal PUMPs, and in a cavity of a motor, at least a part of cooling lubricating liquid DJL flowing through a gap between a motor stator and a motor rotor in a motor shell also flows through a half-way external cooling chamber of the motor stator;

Detailed Description

The present invention is described in detail below.

The pressure in the present invention refers to absolute pressure.

The concentrations of the components described in the present invention, when not particularly specified, are weight concentrations, i.e., mass concentrations.

The hydrogenation process of the hydrocarbon material refers to a hydrogenation reaction process of the hydrocarbon material.

The hydrocarbon material in the invention refers to liquid and/or solid containing carbon and hydrogen elements, such as oil and/or coal.

The hydrogenation process UR of the expanded bed of hydrocarbon material in the present invention refers to a hydrogenation process using a hydrocarbon material as a raw material, and includes a hydrorefining reaction of a hydrocarbon material, and/or a catalytic hydrocracking reaction, and/or a hydrogenation stabilization reaction of thermal cracking radical fragments, and the like, and may be accompanied by a thermal condensation reaction of thermal cracking radicals.

The hydrogenation reaction process of the hydrocarbon material expanded bed can be a direct coal hydrogenation liquefaction reaction process, an inferior heavy oil hydrogenation reaction process and a kerosene co-hydrogenation reaction process.

The process for directly liquefying the carbon-hydrogen powder by hydrogenation mainly refers to the process for directly liquefying coal by hydrogenation, but can comprise other carbon-hydrogen powder which is combined with pulverized coal for liquefaction and mainly consists of carbon elements and hydrogen elements, such as powder which is prepared from waste plastics, waste rubber and other solids and can be used for liquefaction. Generally, in order to accelerate hydrogen supply speed, inhibit thermal condensation reaction, reduce reaction heat and improve reaction operability, hydrogen supply solvent oil is used in the efficient direct liquefaction process of hydrogenation of hydrocarbon powder.

The heavy oil in the invention refers to heavy hydrocarbon oil mainly composed of hydrocarbons with the conventional boiling point higher than 350 ℃, preferably mainly composed of hydrocarbons with the conventional boiling point higher than 450 ℃, preferably mainly composed of hydrocarbons with the conventional boiling point higher than 530 ℃, particularly preferably inferior heavy oil mainly composed of heavy hydrocarbons with low hydrogen content and rich in aromatic structural units, with the conventional boiling point higher than 530 ℃; for the hydrogenation reaction process of the inferior heavy oil, particularly the hydrogenation thermal cracking reaction process, in order to accelerate the hydrogen supply speed, inhibit the thermal condensation reaction, reduce the reaction heat and improve the reaction operability, the hydrogen supply solvent oil is needed in the high-efficiency hydrogenation reaction process of the inferior heavy oil.

The medium hydrocarbon refers to hydrocarbon with a conventional boiling range of 230-400 ℃, and the hydrogen donor hydrocarbon in the boiling range is usually an ideal hydrogen donor solvent component.

The hydrorefining reaction of the hydrocarbon material can be hydrogenation impurity removal reaction such as hydrogenation demetallization reaction, hydrogenation organic oxygen removal reaction, hydrogenation organic sulfur removal reaction, hydrogenation organic oxygen removal reaction, hydrogenation organic chlorine removal reaction and hydrogenation organic fluorine removal reaction, can be hydrogenation saturation reaction of unsaturated carbon-carbon bond such as olefin hydrogenation saturation reaction, alkyne hydrogenation saturation reaction and aromatic hydrocarbon hydrogenation saturation reaction, and can be one or more of the reactions. The hydro-thermal cracking reaction of the hydrocarbon material and the hydro-stabilization reaction of the thermal cracking free radical fragments always occur concomitantly, and are generally existed in the high-temperature hydro-thermal cracking reaction process of coal and/or heavy oil, such as a coal hydrogenation direct liquefaction reaction process, a hydrogenation reaction process of kerosene co-refining, a heavy oil hydro-thermal cracking reaction process and a heavy oil hydrogenation reaction process.

Therefore, the hydrogenation reaction process of the hydrocarbon material expanded bed can be a high-temperature hydrogenation reaction process of coal and/or inferior heavy oil, even can be a super heavy oil hydrodemetallization reaction process, a hydrodesulfurization reaction process and a hydrodenitrogenation reaction process, and can be a front hydrogenation refining reaction section of a super heavy oil hydrocracking reaction process, such as a hydrodemetallization reaction section, a hydrodesulfurization reaction section and/or a hydrodenitrogenation reaction section.

The hydrogenation process of the hydrocarbon material expanded bed of the invention generally uses an upflow expanded bed hydrogenation reactor

The expanded bed reactor is a vertical up-flow reactor, and belongs to an expanded bed reactor when a catalyst is used; the vertical type means that the central axis of the reactor is vertical to the ground in a working state after installation; the upflow means that the material main body flows in the reaction process from bottom to top to pass through the reaction space or the catalyst bed layer or flow in the same direction with the upward catalyst; the expanded bed means that a catalyst bed layer is in an expanded state in a working state, the expansion ratio of the catalyst bed layer is defined as the ratio KBED of the maximum height CWH of the working state when a reaction material passes through the catalyst bed layer and the height CUH of an empty bed standing state of the catalyst bed layer, generally, when the KBED is lower than 1.10, the bed is called a micro-expanded bed, when the KBED is between 1.25 and 1.55, the bed is called an ebullated bed, and a suspended bed is considered as the most extreme form of the expanded bed.

The back-mixing flow expanded bed reaction zone refers to the operation mode of the reaction zone of the expanded bed reactor, wherein liquid flow back mixing or circulating liquid exists; the return flow or the circulating liquid refers to at least one part of liquid phase XK-L in the intermediate product XK or the final product XK at the flow point K as a circulating liquid flow XK-LR to return to a reaction area at the upstream of the XK, and the reaction product of the circulating liquid flow XK-LR flows through the point K and exists in the XK. The mode of forming the back mixed flow can be any suitable mode, such as a reactor provided with a built-in inner circulation tube, a built-in outer circulation tube, a built-in liquid collecting cup, a diversion tube, a circulating pump, an external circulating tube and the like. Under the working condition, due to the repeated circulating operation of the liquid phase product or the intermediate liquid phase product, the hydrogen-supplying solvent oil in the gas phase product undergoes less thermal reaction compared with the hydrogen-supplying solvent oil in the liquid phase, so that more hydrogen-supplying capacity is remained, and the method is more suitable for being used.

The liquid collecting cup or the liquid collector arranged in the reactor refers to a container which is arranged in the reactor and is used for collecting liquid, the upper part or the upper part of the container is usually provided with an opening on the side surface, and a guide pipe is arranged on the bottom part or the lower part of the container for conveying or discharging the collected liquid; the top liquid collector of the expansion bed reactor is usually arranged in a liquid removal area of gas-liquid materials to obtain a mixed phase material flow of liquid and gas-liquid containing a small amount of bubbles or obtain liquid and gas. A typical example is the heavy OIL ebullated bed hydrogenation reactor used in the H-OIL process.

The thermal high separator refers to a gas-liquid separation device for separating intermediate products or final products of hydrogenation reaction.

The two-stage or multi-stage hydrogenation process of the present invention refers to a hydrogenation process comprising two reaction stages or a plurality of reaction stages.

The hydrogenation reaction section refers to a flow section from the beginning of a hydrogenation reaction process of a hydrocarbon raw material to the gas-liquid separation of a hydrogenation product of the hydrocarbon raw material to obtain at least one liquid-phase product consisting of at least part of generated oil, and comprises the hydrogenation reaction process of the hydrogenation reaction section and the gas-liquid separation process of the hydrogenation reaction product of the hydrogenation reaction section. Therefore, a single-stage hydrogenation method generally refers to a flow process mode in which the processing process of an initial hydrocarbon feedstock only comprises a hydrogenation reaction stage and a hydrogenation product gas-liquid separation process, wherein the hydrogenation reaction stage can use 1 or 2 or more hydrogenation reactors operated in series according to needs, so that the number and the form of the reactors are not the basis for determining the reaction stage, and a reaction step consisting of one or more reactors in series can be combined with a product separator to form a complete hydrogenation reaction stage.

The two-stage hydrogenation method refers to a flow mode that the processing flow of an initial hydrocarbon raw material comprises a liquid material processing flow and is operated in series and comprises two different hydrogenation reaction processes and a hydrogenation product gas-liquid separation process, wherein at least one part of material flow formed by the oil generated by the first-stage hydrogenation enters the two-stage hydrogenation reaction process.

The three-stage hydrogenation method refers to a flow mode that the processing process of the initial hydrocarbon raw material comprises a liquid material processing flow which is operated in series and consists of three different hydrogenation reaction processes and a hydrogenation product gas-liquid separation process, wherein at least one part of a material flow formed by the oil generated by the first-stage hydrogenation enters the second-stage hydrogenation reaction process, and at least one part of a material flow formed by the oil generated by the second-stage hydrogenation enters the third-stage hydrogenation reaction process. The flow structure of the hydrogenation method with more stages can be analogized according to the principle. The multistage hydrogenation method refers to a flow mode that the processing process of the initial hydrocarbon raw material comprises a liquid material processing flow and is operated in series, wherein the flow mode comprises three or more different hydrogenation reaction processes and hydrogenation product gas-liquid separation processes.

The three-stage hydrogenation method refers to a flow mode that the processing flow of the initial hydrocarbon raw material comprises a liquid material processing flow which is operated in series and consists of three different hydrogenation reaction processes and hydrogenation product gas-liquid separation processes.

The invention relates to a two-stage-like hydrogenation method, which is similar to a two-stage hydrogenation method and is regarded as the two-stage hydrogenation method when the ratio of the flow of a back-mixing liquid phase of a feeding and back-mixing flow expansion bed reactor on the rear stage to the flow of a liquid phase in the feeding on the upper stage tends to infinity.

The hydrogenation reaction of hydrocarbon material refers to the hydrogenation reaction of liquid and/or solid containing carbon and hydrogen elements such as oil and/or coal in the presence of hydrogen and under a pressurized condition, the raw material oil of the hydrogenation process of hydrocarbon oil is subjected to hydrofining and/or hydro-thermal cracking reaction to generate at least a part of products with lower molecular weight, and the raw material coal of the hydrogenation process of coal oil is subjected to thermal swelling, primary pyrolysis, secondary thermal cracking of intermediate products, free radical hydrogenation stabilization, thermal condensation and other reactions to generate at least a part of hydrocarbon products with conventional boiling points lower than 450 ℃.

Typical examples of the hydrogenation process of the hydrocarbon material in the expanded bed of the invention are a high-temperature coal tar suspension bed hydrogenation deep refining reaction process, a medium-low temperature coal tar suspension bed hydrogenation thermal cracking reaction process, a coal hydrogenation direct liquefaction reaction process, an oil-coal co-refining hydrogenation reaction process, and a petroleum-based heavy oil suspension bed or fluidized bed hydrocracking reaction process.

The reaction product BASE-URP of the hydrogenation reaction of the hydrocarbon material is at least gas-liquid two-phase material flow, and most of the material flow belongs to gas-liquid-solid three-phase material flow. The hydrogenation reaction effluent URP-X is used for discharging a hydrogenation reaction product BASE-URP, appears in the form of 1-path or 2-path or multi-path materials, and is a gas phase or liquid phase or gas-liquid mixed phase or gas-liquid-solid three-phase material flow.

The following description is made in conjunction with the hydrogenation reaction process of medium-low temperature coal tar feedstock hydrocarbon URF and the hydrogenation reaction process of coal-to-liquid.

The invention relates to a hydrogenation process UR of a hydrocarbon material, which comprises a shallow hydrogenation process AR and a deep hydrogenation process BR, and a two-stage hydrogenation method provided by the invention mainly relates to the deep hydrogenation process BR of the hydrocarbon material, in particular to a deep hydrogenation mode of high-boiling-point liquid-phase hydrocarbon components in the BR process and/or a deep hydrogenation mode of a coal tissue which is not deeply liquefied, and the key point relates to optimization of thermodynamic conditions in the deep hydrogenation reaction process, and relates to improvement of hydrogen partial pressure, hydrogenation selectivity, high-boiling-point hydrocarbon concentration in a liquid phase, catalyst concentration in the liquid phase, active hydrogen supply speed and target reaction speed, namely thermal reaction time shortening, and the like, and further relates to change of the whole hydrogenation reaction process.

The medium-low temperature coal tar has a conventional boiling point higher than 350 ℃ and consists of heavy fraction raw material hydrocarbon AR1F, and the suitable hydrogenation method is a hydrogenation reaction process UR using an upflow expanded bed because of containing coal pitch; the hydrogenation process UR may be a process in which a hydrorefining reaction is dominant, that is, a large amount of hydrorefining reaction and a relatively small amount of hydrocracking reaction occur; the hydrogenation process UR may also be a hydrocracking process, i.e. a large number of hydrorefining reactions and a large number of hydrocracking reactions occur.

In the coal-to-liquid hydrogenation reaction process, due to the coal powder and the circulating oil residue, the proper hydrogenation method is the hydrogenation reaction process UR using an upflow type expanded bed; the hydrogenation process UR is generally a reaction process mainly including a swelling reaction, a pyrolysis reaction, a hydro-thermal cracking reaction, and a radical hydrogenation stabilization reaction, but also a thermal condensation reaction of a pyrolysis intermediate heavy hydrocarbon occurs to generate asphaltenes and preasphaltenes, and a secondary thermal cracking reaction of a pyrolysis intermediate hydrocarbon product occurs to generate small-molecule hydrocarbons and gases.

No matter in the hydrogenation thermal cracking process of raw material hydrocarbon AR1F composed of heavy fraction with the conventional boiling point of medium-low temperature coal tar higher than 350 ℃, or in the hydrogenation reaction process of coal-to-liquid, the optimized operation scheme usually uses at least 2 upflow type expanded bed reactors, at the moment, the roughly front hydrogenation reactor carries out the shallow hydrogenation process AR, and the rear hydrogenation reactor carries out the deep hydrogenation process BR; the operation temperature of the shallow hydrogenation process AR is usually higher, usually as high as 350-430 ℃, and usually as high as 380-415 ℃, but the reaction temperature value is usually lower than that of the deep hydrogenation process BR, for example, the reaction temperature value is usually lower than that of the deep hydrogenation process BR by 15-50 ℃; the operating temperature of the BR in the deep hydrogenation process is usually higher, usually as high as 410-470 ℃, usually as high as 425-455 ℃, and the reaction temperature is usually higher than that of the AR in the shallow hydrogenation process, for example, usually higher than 15-50 ℃ or higher.

Heavy fraction raw material hydrocarbon AR1F with the normal boiling point of medium and low temperature coal tar higher than 350 ℃, wherein the low boiling point hydrocarbon fraction, namely the hydrocarbon component with the normal boiling point lower than 330 ℃, has lower impurity element content and lower residual carbon content, and in the hydrofining reaction process UR using an upflow expansion bed such as a suspension bed, the impurity elements in the low boiling point hydrocarbon fraction are easier to hydrogenolyze and remove residual carbon than the high boiling point hydrocarbon fraction, and colloid in the low boiling point hydrocarbon fraction is easier to hydrogenolyze and remove residual carbon, so the hydrodeimpurity removal and hydrodecabon removal tasks of the low boiling point hydrocarbon fraction are firstly completed as the hydrogenation degree is increased, but the hydrodeimpurity removal and hydrodecabon removal tasks of the high boiling point hydrocarbon fraction are not completed, if the deep hydrogenation is continued, excessive hydrogenation and excessive thermal cracking of the low boiling point hydrocarbon fraction are inevitably caused, in order to improve the selectivity of the hydrogenation process of the high boiling point hydrocarbon, it is desired to discharge the low boiling point intermediate products such as impurity gases, normal gaseous hydrocarbons, naphtha components and the like out of the reaction process in time and continuously carry out deep hydrogenation refining reaction or circular hydrogenation refining on the high boiling point intermediate products; the hydrorefining can accelerate the hydrogenation reaction by utilizing the advantages of greatly reducing the viscosity of the overall liquid phase and accelerating the diffusion speed of the high-boiling point component under the condition of existence of the low-boiling point raw material component, and the quality of the hydrogenated final product of the high-boiling point hydrocarbon component can be controlled by flexibly adjusting the circulation ratio, the reaction temperature and the like, in other words, the hydrorefined circulating oil formed by the heavy fraction unconverted oil is inevitably existed at the time.

In a single-stage single-pass hydrocracking reaction process UR using an upflow expansion bed such as a suspension bed, the raw material hydrocarbon AR1F composed of heavy fractions with the conventional boiling point of medium-low temperature coal tar being higher than 350 ℃ cannot achieve 100% full conversion generally, because the excessively high hydrocracking single-pass conversion rate causes excessive cracking of low-boiling-point hydrocarbons in the raw material and intermediate hydrogenation products to produce gas, excessive thermal condensation of high-boiling-point hydrocarbons to produce coke, severe deterioration of product distribution, and shortening of a continuous operation period.

In the coal-to-liquids hydrogenation reaction process, in order to improve the liquefaction rate of coal, that is, to improve the liquid yield, it is generally desirable that the active components (minor component and chitin component) in the coal are nearly completely liquefied, and the inert components (inert component) are moderately liquefied, but since the active components (minor component and chitin component) in the coal are easily liquefied and the inert components (inert component) are difficult to liquefy, the latter reaction stage of moderate liquefaction of the inert components (inert component) is the secondary pyrolysis reaction of the liquefied product of the active components, which inevitably results in excessive cracking of the raw material hydrogen supply agent and the intermediate product hydrocarbon, excessive thermal condensation of the high boiling point hydrocarbon and excessive coke generation, which seriously deteriorates the product distribution and shortens the continuous operation period, in other words, the coal liquefaction hydrogenation process inevitably has an undesirable deep hydrocracking process.

On the premise of existence of a deep hydrogenation process, the component concentrations (hydrogen, impurity gases, low-boiling-point hydrocarbons and high-boiling-point hydrocarbons) in the raw materials in the deep hydrogenation process greatly influence the hydrogen partial pressure, the catalyst concentration in the liquid phase and the high-boiling-point hydrocarbon concentration in the liquid phase, further directly and strongly influence the hydrogenation reaction selectivity, the active hydrogen supply speed, the target reaction time and the like, further directly and strongly influence the quantity of thermal condensation reactions and the quantity of secondary pyrolysis reactions, and determine the quality of the technological process.

In the hydrogenation reaction process UR of the medium-low temperature coal tar raw material hydrocarbon AR1F or the hydrogenation reaction process UR of the coal-to-liquid, a large amount of low molecular weight and low boiling point gas components can be generated in the shallow hydrogenation process AR, and the sources are as follows:

① A portion of the organic impurities O, S, N in the feed AR1F is converted to a lower boiling impurity gas component H₂O、H₂S、NH₃Exists in gas phase, and has high yield of impurity gas due to high content of organic impurity O, S, N in raw materials;

② conversion of part of the oxygen-containing functional groups in the raw material AR1F into the gas components with low boiling point, CO₂Present in the gas phase;

③ of raw material AR1F or of intermediate products with a part of paraffins and naphthenesSide chains of aromatic hydrocarbons, cracking to form the conventional gas component C with low boiling point₁～C₄Present in the gas phase;

④ the side chains of some paraffins, naphthenes and aromatics in the raw material AR1FL or intermediate product are cracked and cracked to form a naphtha component C with lower boiling point₅NBP200, partially in the gas phase at the reactor operating conditions; NBP200 represents a fraction with a normal boiling point of 200 ℃, and the pure components thereof can be components with a normal boiling point of 195-205 ℃, such as undecane with a normal boiling point of 196 ℃, pentamethylbenzofuran with a normal boiling point of 196 ℃, tetramethylbenzene with a normal boiling point of 198.4 ℃, toluidine with a normal boiling point of 200 ℃, dihexaxylphenol with a normal boiling point of 201 ℃, 4 methylhydroindene with a normal boiling point of 203 ℃ and the like.

In the hydrogenation process UR, heavy hydrocarbons and light reformate in the front hydrogenation process product enter a subsequent hydrotreating process such as deep hydrofinishing or hydrocracking, and the presence of the above-mentioned gas phase components will have the following effects:

① impurity gas component H₂O、H₂S、NH₃、CO、CO₂The hydrogen concentration can be obviously reduced, namely the hydrogen gas partial pressure value is obviously reduced, and the gas phase concentration is very high, such as 7-13%;

H₂O、H₂S、NH₃the hetero atom (non-hydrogen atom) has a lone electron pair which is an electron donor and can be adsorbed on the active center on the surface of the hydrogenation catalyst in the gas phase to reduce the activity of the catalyst;

oxygen and carbon in the CO have a lone electron pair which is an electron donor and can be adsorbed on an active center on the surface of the hydrogenation catalyst in the gas phase, so that the activity of the catalyst is reduced;

CO₂the oxygen in the catalyst has a lone electron pair which is an electron donor and can be adsorbed on an active center on the surface of the hydrogenation catalyst in a gas phase to reduce the activity of the catalyst;

CO、CO₂can also consume active hydrogen atoms to convert into H₂O、CH₄；

② conventional gas groupIs divided into C₁～C₄The gas phase concentration is 2.0-5.0%, and the hydrogen concentration can be reduced, namely the partial pressure value of the hydrogen gas phase is reduced;

③ naphtha component C₅The NBP200 component, the NBP200 to NBP330 component, the unsaturated bond of the unsaturated component can consume active hydrogen atoms to be converted into saturated bonds, and part of the components generate thermal cracking reaction to consume active hydrogen atoms to generate hydrocarbon components with lower carbon number, which is generally a process for reducing the value of the hydrocarbon components.

Thus, avoiding or eliminating the low boiling components produced by the shallow hydrogenation process AR of the hydrogenation process UR from entering the subsequent deep hydrogenation process BR will have the following direct and indirect effects:

① the hydrogen concentration is obviously increased, namely the hydrogen gas phase partial pressure value is obviously increased;

② reducing the gas phase partial pressure of impurity components, increasing the catalyst activity, or reducing the catalyst amount;

③, the amount of low boiling point hydrocarbon in the raw material hydrocarbon in the subsequent hydrogenation treatment process is reduced, which avoids the secondary hydrogenation of the low boiling point hydrocarbon, and the newly added hydrogen raw material has the gas stripping effect, which makes part of the low boiling point hydrocarbon in the raw material hydrocarbon in the subsequent hydrogenation treatment process change from liquid phase to gas phase, thus making the low boiling point hydrocarbon pass through the subsequent reaction zone once and avoid multiple reflux processing in the reaction zone, the subsequent reaction zone can carry out deep hydrogenation of the high boiling point component with the expected temperature, the expected cycle number and the expected time, which obviously improves the catalyst reaction selectivity, shortens the target reaction time, inhibits the side reaction and increases the target product yield;

④ inhibiting negative reaction, mainly inhibiting thermal condensation reaction, prolonging catalyst life or increasing continuous service life or decreasing deactivated catalyst discharge rate, reducing catalyst consumption, improving operability of high pressure reaction system (reducing liquid viscosity, reducing deposition rate of organic condensate, and reducing solid content, i.e. decreasing solid abrasion rate), i.e. prolonging continuous operation period;

⑤ the selectivity of active hydrogen atoms to target reaction is improved, and the consumption of hydrogen is reduced;

⑥ increasing the yield of higher carbon number hydrocarbon components;

⑦ as an indirect effect, the thermal cracking rate of heavy components such as colloidal asphaltenes can be increased and the thermal condensation rate of high heavy components such as colloidal asphaltenes can be reduced by increasing the hydrogen partial pressure;

⑧ as an indirect effect, the reaction temperature can be lowered or the space velocity increased, i.e. the operating severity is lowered or the work-up is increased, by increasing the hydrogen partial pressure;

⑨ because the concentration of catalyst solids is achieved, i.e., the catalyst concentration is increased, the amount of fresh catalyst added can be reduced;

⑩ the amount of newly added catalyst is reduced, namely the discharge amount of deactivated catalyst is reduced, the amount of non-distillable heavy oil discharged along with the deactivated catalyst is reduced, namely the liquid yield is increased;

(11) because the hydrogen partial pressure and/or the catalyst concentration are improved, and the concentration of active hydrogen atoms in a liquid phase can be improved, on the premise of ensuring the operability, the subsequent deep hydrogenation process BR can be allowed to operate under more severe conditions, such as improving the hydrofining depth and/or improving the once-through thermal cracking rate, so that the quantity of circulating slurry oil consisting of circulating hydrogenation materials such as unconverted oil can be reduced, namely the circulation ratio is reduced, and the liquid processing amount and the solid flow of a thermal high-pressure separator, a pressure reducing valve at the bottom of the thermal high-pressure separator and a subsequent fractionation system are reduced;

(12) because the liquid phase in the subsequent hydrotreating process mainly consists of high-boiling-point hydrocarbons and the operation temperature is high, the concentration of free radicals in the thermal cracking process is higher, and the fresh hydrogen supply solvent is added in the BR in the subsequent deep hydrogenation process, the liquid-phase hydrogen transfer speed can be obviously improved, the hydrogen supply function of the fresh hydrogen supply solvent can be fully exerted, the hydrogenation stable reaction speed of the free radicals can be obviously accelerated, the macromolecular thermal condensation reaction is obviously inhibited, the secondary cracking reaction of an intermediate product is obviously inhibited, the properties of a thermal cracking product are improved, and the yield of cracked liquid oil is improved.

Generally, the method for preventing the gas phase components generated by the shallow hydrogenation process AR of the hydrogenation reaction process UR from entering the subsequent deep hydrogenation process BR is to arrange a separation process for the reaction products of the upstream reaction stage, such as arranging a hot high-pressure separator between the reaction stages, i.e. introducing the hot high-pressure oil of the hot high-pressure separator between the reactors into the adjacent downstream reactor, thereby avoiding the disadvantages of the previous flow.

As mentioned above, whether it is a coal hydrogenation direct liquefaction reaction process, or a hydrogenation thermal cracking reaction process of macromolecule inferior heavy oil, wherein the process of converting macromolecule fracture into medium hydrocarbon and light hydrocarbon with suitable molecular weight is a multi-step series reaction process, therefore, the process of converting macromolecule fracture into medium hydrocarbon and light hydrocarbon with suitable small molecular weight is also a long thermal cracking reaction process, in the later stage reaction process of gradual thermal cracking of the initial macromolecule component, the medium hydrocarbon and light hydrocarbon generated in the early stage thermal cracking reaction process of the initial macromolecule component and the reaction conversion substances accompanied with reaction components (such as wax oil and hydrogen supply solvent of diesel oil component) will generate undesirable excessive thermal cracking reaction, consume hydrogen to generate normal gas hydrocarbon and light naphtha, and reduce the yield of liquid hydrocarbon; while the gas such as H is generated in the early reaction process₂S、NH3、H₂O、CO、CO₂、CH₄、C₂H₆In the latter reaction process, the hydrogenation catalyst is poisoned or the catalytic activity of the hydrogenation catalyst is inhibited, and the hydrogen partial pressure is reduced, so that from the viewpoint of optimizing the process operation, the whole reaction process is divided into two liquid-phase reaction zones (such as a first reaction zone and a second reaction zone) connected in series or three liquid-phase reaction zones (such as a front reaction zone, a middle reaction zone and a rear reaction zone) connected in series or more liquid-phase reaction zones (such as a first reaction zone, a second reaction zone, a third reaction zone and a fourth reaction zone) connected in series, a step-by-step or step-by-step reaction mode is formed, and the following 1 or more operations are implemented:

① the upstream reaction zone product can be separated so that at least part of the separated gas phase product does not pass through at least one downstream reaction zone, thereby preventing excessive thermal cracking of the low boiling point hydrocarbons of the intermediate product and preventing the polar component H of the intermediate product₂S、NH₃、H₂O、CO、CO₂The activity of the catalyst is reduced, the gas phase volume of a downstream reaction zone is reduced, the liquid phase fraction of the downstream reaction zone is improved, and the volume and the weight of a reactor of the downstream reaction zone are reduced;

② separating the products in the upstream reaction zone, and circulating at least part of the separated liquid phase gas phase products back to 1 or more upstream reaction zones, compared with fresh hydrocarbon raw material, returning the intermediate hydrogenation products with lower viscosity, higher hydrogen supply hydrocarbon concentration and higher temperature to the first hydrogenation reaction zone, so as to reduce the viscosity of the liquid phase in the first hydrogenation reaction zone and improve the hydrogen supply hydrocarbon concentration, thereby significantly improving the hydrogenation efficiency of the first hydrogenation reaction zone;

③ the downstream reaction zone can use high-purity hydrogen flow to form high hydrogen partial pressure under the same total pressure, the added hydrogen will strip the lower boiling point component in the liquid phase feed, and make it pass once and discharge from the reaction zone, to prevent the repeated thermal cracking of the lower boiling point heavy hydrocarbon component;

④ can separate the products in the downstream reaction zone, at least part of the separated liquid phase and gas phase products can be recycled to 1 or more upstream reaction zones, compared with the expanded bed hydrogenation reaction products which are separated by high pressure separation, oil fractionation process to separate vacuum residue and finally recycled to the first hydrogenation reaction zone, the final hydrogenation product liquid phase with high temperature mainly comprising vacuum residue and wax oil is recycled to the first hydrogenation reaction zone, more reaction heat can be recovered, the load of the high pressure separation and oil fractionation process of the expanded bed hydrogenation reaction products can be reduced, and the investment and energy consumption of the system can be reduced.

The invention relates to a hydrogenation reaction level RK with forced circulation reaction of liquid products of the reaction level RK, which is characterized in that in a separation step RKP-S of the reaction level RK, liquid RKP-SL obtained by separating the liquid RKP products of the hydrogenation reaction level RK is forced to be pressurized by a circulating PUMP RKP-SL-PUMP and then returns to a reaction area of the hydrogenation reaction level RK for circulation reaction without passing through an upstream hydrogenation reaction level, and at least a part of liquid reaction products of the liquid RKP-SL enter the products RKP.

The device RKP-SE performing the reaction-level RK separation step RKP-S may be a separator independent of the reaction-level RK reaction process device RKE.

The device RKP-SE for completing the RKP-S separation step of the reaction level RK can be combined with the RKE reaction process device RKE, for example, a liquid collecting cup is arranged at the top in the reactor RKP-SE, so that the RKP product of the reaction level RK is separated into a liquid material and a gas-liquid mixed phase material in a separation space formed by the liquid collecting cup at the top and a shell at the top of the reactor RKP-SE.

The invention relates to a circulating pump of intermediate reaction product liquid or final reaction product liquid, wherein a shaftless centrifugal pump such as a wet stator pump, a shield pump and a magnetic pump is often used in the relay conveying process of high-temperature and high-pressure circulating reaction slurry containing solid particles, and a shaftless pump with mechanical seal of a special structure can also be used.

An example of the wet stator centrifugal pump is a German KSB furnace water circulating pump used for a circulating water circulating pump of a power station boiler, and the circulating water circulating pump of the power station boiler manufactured by China Hefei Anhui motor technology development Limited liability company.

Taking a circulating water circulating pump of a power station boiler as an example, the wet stator centrifugal pump is characterized in that the wet stator centrifugal pump is free of a shielding sleeve, a stator winding is directly soaked in a medium, eddy loss caused by the shielding sleeve is avoided, and the pump set efficiency is improved by about 8 to 10 percent. The winding of the wet stator centrifugal pump is wound by adopting a specially designed and airtight multilayer polyethylene insulated copper conductor, the polyethylene layer plays a role of electrical insulation, and the outer layer is covered with Polyamide (PA) to improve the corrosion resistance. The winding of wet stator main pump submerges in the coolant, and cooling medium directly cools off the winding wire to there is not inside high temperature region, consequently, the cooling performance of wet stator main pump motor winding is obviously better than shielding the main pump. However, the winding of the wet stator main pump is immersed in radioactive reactor coolant for a long time, the reliability and durability of the insulating layer of the wet stator main pump are highly concerned, the aging and corrosion of the insulating layer are comprehensively analyzed and identified according to the maximum radiation intensity and medium condition possible in actual operation, and the reliability of the insulating layer in the design period of the main pump is ensured, because the maintenance and shutdown caused by the shielding sleeve or the insulating layer of the main pump motor have great influence on the benefit of a power plant.

The centrifugal canned motor pump of the invention refers to a canned motor driven centrifugal pump.

The invention relates to a canned motor pump, which is a sealless pump, wherein an impeller is sealed in a pressure container which is filled with pumped media and drives a motor rotor to be sealed in a special cooling and lubricating medium, the operation pressure of the pressure container is similar, the pressure container essentially belongs to a communicating vessel, the pressure container is only statically sealed, and the motor stator provides a rotating magnetic field to drive the rotor. The structure cancels a dynamic sealing device of a rotating shaft of the traditional centrifugal pump to the environment, so the leakage is completely avoided, and the used shielding motor can be a wet shielding motor or a dry shielding motor and is widely applied to the fields of refrigeration, air conditioning, medicine, chemical industry, petroleum and the like.

In the centrifugal canned motor pump of the present invention, generally, the impeller is installed at the outward extending end of the motor shaft (in the pump impeller cavity), and the impeller, the pump shaft and the motor rotor jointly form a rotating part. The impeller in the pump shell of the canned motor pump is coaxial with the canned motor rotor, and the basic components of the canned motor pump at least comprise a pump body, a canned motor and a connecting body for manufacturing, assembling and maintaining; when the connecting body is used, one end of the connecting body is in butt joint with a pump shell, the other end of the connecting body is in butt joint with a shielding motor, and a shaft of a rotor of the shielding motor penetrates through the connecting body and then enters the front end part in the pump shell to be used as a shaft for mounting a pump impeller.

Canned motor pumps are available from FLOWSERVE, USA, from the slag boiling bed hydrogenation unit, HAYWARD TYLER electric canned motor pumps, Hefei Hu canned motor pumps, and Dalian Imperial canned motor pumps.

The dry canned motor pump of the present invention, which is generally considered to be developed after the advent of the wet motor pump, differs from the wet motor pump in that a dry canned motor is used. Generally, the inner surface of a dry type shielded motor stator is isolated by a non-magnetic corrosion-resistant sheet sleeve to form a stator shielded sleeve, the outer surface of a dry type shielded motor rotor is isolated by a non-magnetic corrosion-resistant sheet sleeve to form a rotor shielded sleeve, and power (torque between the stator and the rotor) is transmitted from the stator to the rotor through a magnetic force field; the stator shielding sleeve and the rotor shielding sleeve are pressure containers in nature, the ends of the shields are statically sealed by flanges or welded structures, and are separated from the conveyed liquid, so that the stator winding iron core and the rotor iron core are not corroded, and the stator shielding sleeve and the rotor shielding sleeve are filled with resin possibly. The shield is made of a non-magnetic, corrosion resistant, high strength metal material, typically hastelloy (hastelloy c) alloy. At present, manufacturers of dry canned motor pumps in China include Hefei Hu canned motor pump company, Dalian empire Gum canned motor pump company, HAYWARD TYLER electric canned motor pump company, and so on.

The wet electric pump for conveying high-pressure fluid uses the liquid-immersed stator winding group of wet electric machine, so that the fixing component of the stator winding group can be non-pressure-bearing component, so that it is light in weight, small in volume and easy to assemble, so that in the interior of pressure-bearing shell body of wet electric machine the internal and external cooling gaps of stator can be conveniently formed, or called cooling chamber or cooling channel, and the external cooling chamber of stator can simultaneously bear the main cooling task of motor shell body and heat shield, and the internal cooling chamber of stator can simultaneously cool and lubricate motor and rotor of pump. The wet type canned motor pump is convenient for conveying high-temperature fluid because the cooling function is ideal.

The stator winding group of the dry type canned motor used for conveying high-pressure fluid is positioned in a pressure-resistant canned cover, so that the fixing component of the stator winding group is a pressure-bearing part and must be processed and manufactured by adopting a metal plate with thicker thickness, and therefore, the dry type canned motor has large weight and volume and is not easy to assemble, and thus, the inside of the pressure-bearing shell of the dry type canned motor can form an inner cooling gap and an outer cooling gap of a stator, but is not convenient. Generally, the dry type canned motor pump is not provided with a stator external cooling chamber, but is provided with a heat shield for limiting the heat transfer quantity from a pump shell to a motor shell, the cooling liquid in the stator internal cooling chamber transfers the heat transferred by the heat shield at the position, close to the motor end, of the heat shield to realize the cooling of the motor shell, obviously, compared with a wet type electric pump, the dry type canned motor pump has poor cooling function, and thus the high-temperature range of the fluid conveyed by the dry type canned motor pump is limited to a certain extent.

The following description will be given of some structural features and auxiliary system operation of the seal-less pump, taking the canned motor pump as an example.

The shielding electric pump has various structural main part arrangement schemes due to the requirements of manufacturing, assembling and maintaining, and at least comprises the following 2 typical schemes:

① scheme of three main parts, pump cover, shield motor body, shield motor back cover, pump body part radial subdivision structure, independent circulating pump body part including pump cover, installation scheme is that the outlet and inlet of pump cover are butt jointed with process pipeline, the structure part of shield motor shell near one end of pump body is used as the rest structure parts of pump shell;

② A pump cover, a connector, a shielding motor body, a shielding motor back cover, and a pump body part radial subdivision structure, wherein one end of the connector is butted with the pump cover, and the other end is butted with the shielding motor body.

The canned motor pump of the present invention may also include other auxiliary components such as an integrated cooler, as desired.

The shielding electric pump can be provided with a cooling component or a cooling system of the shielding electric pump body.

The canned motor pump, the motor and the pump body can share one integral engine base.

The shielded electric pump and the auxiliary liquid FZL input system can be arranged at any suitable position of any suitable main part and at any suitable position in a pump body (generally not a pump cover part) and/or a connecting body and/or a motor shielding body.

The location of the lubricant and/or coolant EL input system of the canned motor cavity of the canned motor pump of the present invention may be at any suitable location on any suitable main component, typically at a suitable location in the canned motor body and typically at the end of the canned motor body remote from the pump body.

The shielding electric pump can add blades on the back of the main impeller for medium containing particles, and has the function of timely discharging solid particles to prevent the solid particles from accumulating; meanwhile, the axial unbalanced force can be reduced, the abrasion damage speed of the arranged thrust bearing is favorably reduced, and the service life of the thrust bearing is favorably prolonged.

When the overflowing medium of the shielding electric pump is the liquid of the high-concentration solid, a wear-resistant bushing or a wear-resistant shell can be used for prolonging the service life of the overflowing part of the cavity of the pump.

The canned motor pump can be provided with the auxiliary impeller on the motor part to drive the cooling liquid in the motor cavity to circularly work, and the axial force generated by the auxiliary impeller can be used for balancing the axial force generated by part of the pump impeller because the auxiliary impeller is coaxial with the main impeller.

The installation mode of the canned motor pump can be vertical arrangement or horizontal arrangement.

The vertical canned motor pump can be installed in a mode that the motor is positioned above and the pump body is positioned below, or in a mode that the motor is positioned below and the pump body is positioned above.

According to the installation mode of the vertical canned motor pump, the motor is positioned below the pump body, and the pump body is positioned above the motor, so that the gas in the cavity of the motor and the cavity of the pump can be discharged, and the accumulation of the gas can be prevented.

The impeller of the canned motor pump is mainly in the form of a centrifugal pump impeller, the impeller can generate cavitation under certain working conditions, an inducer can be additionally arranged in front of the centrifugal impeller, and the cavitation erosion resistance of the pump is improved.

The canned motor pump of the invention can reduce the energy consumption of the motor, reduce the effective non-magnetic gap between the stator and the rotor, reduce the excitation current of the motor, thereby reducing the power consumption and improving the efficiency and the power factor of the canned motor pump motor. One method that can be used is that the metallic shielding sleeve is made of a regional magnetoelectric anisotropy material or different regions of the shielding sleeve are subjected to magnetoelectric anisotropy regulation and control treatment, magnetic permeability anisotropy regulation and control and electric conductivity anisotropy regulation and control.

For an oil-coal slurry circulating pump used in a coal slurry suspension bed hydrogenation reactor of a CTL (direct liquefaction) process of coal hydrogenation, the online operation dynamic measurement is very important, as the rotor of a canned motor pump is completely shielded by a pump shell, the displacement of the rotor cannot be measured, and whether the rotor is eccentric or bent or even worn cannot be directly judged, as faults of grinding of an across ring, bearing abrasion, wearing of a shielding sleeve, locking of the rotor and the like occur in the canned motor pump, the faults cause component damage and even cause incapability of operation of the pump set, and if the occurrence process of an event can be found in real time, unnecessary excessive damage or expansion accidents can be avoided. The method for monitoring the operation fault of the canned motor pump of the nuclear reactor disclosed in the Chinese patent ZL201010516186.8 and the monitoring system thereof are provided by the Chinese nuclear power research and design institute, and can be used for monitoring the operation state of the canned motor pump of the nuclear reactor on line, extracting the fault characteristic quantity of the canned motor pump and giving a fault alarm in the abnormal state of the canned motor pump. The method and the system for monitoring the operation fault of the canned motor pump can be combined with the invention for application.

The electric pump without shaft seal used in the invention can be used in combination with the following patent applications: a canned motor pump with two auxiliary fluid inlet systems is provided, which is disclosed in patent application No. 201710063971.4 and published in patent application No. CN 108317086A.

The shaft seal-free electric pump can use the first auxiliary liquid FZL, and the first auxiliary liquid FZL is used as a flushing liquid for preventing a process medium in a pump shell from being connected into a cavity of a shielding electric pump in series, so that the operating pressure of an input system of the first auxiliary liquid FZL is certainly greater than the operating pressure of the process medium in the pump shell; certainly, the first auxiliary liquid FZL is also a lubricating liquid and a cooling liquid of the bearing flowing downstream of the first auxiliary liquid FZL and is used for lubricating and cooling, so that the boiling range, viscosity-temperature characteristics, stability, corrosivity, solid impurity content, solid impurity particle size and the like of the components of the first auxiliary liquid need to meet the long-term operation requirements of the use occasions. The centrifugal pump with at least 2 different-lift liquid discharge ports can form a flushing system BWS and a shielding motor circulating cooling system ALS which flow to a pump impeller cavity relatively independently; when the circulating pump for the oil-coal slurry reactor is used for a CTL (direct liquid) coal hydrogenation direct liquefaction process, the coupling system of a motor circulating cooling system of the traditional canned motor pump and a flushing system flowing to a pump impeller cavity is decoupled, the consumption of lubricating oil can be reduced by 70-95%, and the running cost of a single circulating pump for a 100 ten thousand ton/year CTL reactor is saved by about 500 ten thousand yuan/year; the BWS may be fed with relatively large amounts of inexpensive flushing oil from the factory into the pumped process fluid in the pump impeller cavity, the ALS lubricating oil may be independently circulated in large volumes to increase cooling capacity while maintaining a low level of safe discharge into the BWS and ultimately into the pump impeller cavity, and the dual auxiliary fluid feed system may economically achieve the cooling, lubricating, flushing, sealing requirements needed for long term safe operation of the canned motor pump assembly. BWS can use the washing oil which is produced by the factory and has low price, for example, distillate oil with the conventional boiling range of 260-330 ℃ or distillate oil with the conventional boiling range of 300-360 ℃ or distillate oil with the conventional boiling range of 360-420 ℃ from the hydrogenation upgrading process of coal liquefied oil, the BWS has lower dust content and better thermal stability, and is more suitable for being used as the washing oil, and the washing oil is divided into groups to undergo thermal cracking hydrogenation reaction to be converted into light diesel oil and naphtha with high aromatic hydrocarbon potential after entering the reaction process of the direct coal liquefaction suspension bed.

The shaft seal-free electric pump of the invention can use the first auxiliary liquid FZL which is used as a flushing liquid,

the electric pump without shaft seal used in the invention can be used in combination with the following patent applications: the patent application No. 201710451303.9 and the patent application publication No. CN109038957A are applied to a shield motor of a half-stroke external cooling chamber for an inner stator of a motor shell and a shield electric pump thereof.

According to the canned motor pump, the canned motor of the half-stroke outer cooling chamber and the canned motor pump thereof can be used as the stator in the motor shell, and compared with a stator whole-course outer cooling chamber structure, the canned motor pump keeps the good tight assembly function and the deformation-resistant integral rigidity of the stator piece in the structure without the stator outer cooling chamber on the premise of keeping the cooling function of the inner cooling chamber at the high temperature section of the motor shell; compared with a stator structure without an external cooling chamber, the cooling function of the internal cooling chamber at the high-temperature section of the motor shell is added, and a cooling liquid opening arranged at the high-temperature section of the motor shell is transferred to the low-temperature section of the motor shell, so that the safety of the motor shell is improved; an overall optimized structure which gives consideration to multiple indexes of cooling, tight assembly and deformation-resistant integral rigidity of motor parts is formed, and the temperature and vibration application range of the canned motor pump is favorably expanded; the canned motor pump can be used as a slurry circulating pump with high temperature, high pressure and high solid concentration of a high-temperature liquid phase product reflux system of a gas-liquid material up-flow type coal hydrogenation direct liquefaction reactor.

The electric pump without shaft seal used in the invention can be used in combination with the following patent applications: the patent application number is 201710588184.1, and the patent application publication number is CN 109253090A.

The shielding electric pump is particularly suitable for an oil-coal slurry circulating pump used by a coal slurry suspension bed hydrogenation reactor in a coal hydrogenation direct liquefaction process CTL, a solid-containing washing liquid circulating pump of a gas phase dust removal system used by a heat high-pressure separator or a heat high-pressure fractionating tower of a coal slurry suspension bed hydrogenation reactor product in the coal hydrogenation direct liquefaction process CTL, a pressurizing pump or a circulating pump of liquid at the bottom of a heat high-pressure separator of a gas phase of the heat high-pressure separator of the coal slurry suspension bed hydrogenation reactor product in the coal hydrogenation direct liquefaction process CTL, a solid-containing circulating pump used by a solvent oil boiling bed or an up-flow micro-expansion bed hydrogenation reactor in the coal hydrogenation direct liquefaction process CTL, and a high-pressure high-temperature solid particle-containing oil pump is used as a feeding material in other hydrogenation processes.

The guide vane can be arranged on the outer side of the impeller of the shaft seal-free electric pump.

The balance ring can be fixed at the back of the final stage impeller of the electric pump without the shaft seal.

The pump cavity of the electric pump without the shaft seal refers to a functional space for mounting an impeller, a guide vane, a flow passage and a liquid discharge buffer space for overflowing in the process of boosting process fluid, can be a cavity in an integrated pump cover and pump base structural part, and can be a cavity of a combined part formed by the pump cover, the pump base and an intermediate pump cavity assembled between the pump cover and the pump base.

The shaft seal-free electric pump comprises a pump cavity base, and in most cases, the pump cavity base is also the front end of a motor chamber or the front end of a connecting body.

The characteristic parts of the present invention are described below.