Self-adaptive three-cycle pressurized carbon-containing material step conversion system and method
阅读说明：本技术 一种自适应三循环加压含碳物料梯级转化系统及方法 (Self-adaptive three-cycle pressurized carbon-containing material step conversion system and method ) 是由 李大鹏 刘国海 于 2018-08-24 设计创作，主要内容包括：本发明公开了一种自适应三循环加压含碳物料梯级转化装置系统及方法,其中一种自适应三循环加压含碳物料梯级转化装置系统包括含碳物料备料系统、含碳物料加压热化学转化系统、富碳颗粒化学链转化系统、多相流分离系统、本发明所公开的装置系统及方法以石油焦、重质油砂岩、生物质、低阶煤炭资源等含碳物料为原料,可实现含碳物料的高效清洁转化与梯级利用,用于生产高品质轻质油品及合成气,基于该发明所公开的含碳物料梯级转化装置系统可构建新型煤、油、化、电多联产模式。(The invention discloses a self-adaptive three-cycle pressurized carbon-containing material step conversion device system and a method, wherein the self-adaptive three-cycle pressurized carbon-containing material step conversion device system comprises a carbon-containing material preparation system, a carbon-containing material pressurized thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multiphase flow separation system.)
1. A self-adaptive three-cycle pressurized carbon-containing material step conversion system is characterized by comprising a carbon-containing material preparation system, a carbon-containing material pressurized thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multiphase flow diversion system;
the carbon-containing material preparation system comprises a carbon-containing material pretreatment sub-device (10), a carbon-containing material conveying device (11), a material conveying control device (12) and a carbon-containing material steady-state conveying feedback device (13) which are sequentially connected;
the multi-phase flow diversion system comprises a multi-phase flow dry diversion unit, a multi-phase flow quenching settler (60) and a multi-phase flow wet diversion device (63);
the multiphase flow dry-method flow dividing unit comprises a multi-attribute particle flow divider (22), a first-stage multiphase flow divider (32), a second-stage multiphase flow divider (40) and a third-stage multiphase flow divider (50);
the carbon-containing material pressurized thermochemical conversion system comprises a carbon-containing material pressurized thermochemical reaction unit (30), a carbon-containing material feeding port (301) connected with a carbon-containing material steady-state conveying feedback device (13) and a porous active particle inlet (302) connected with a porous active particle return unit (310) are respectively formed in a mixed material reinforced transfer region (30-3) in the middle of the carbon-containing material pressurized thermochemical reaction unit (30), an outlet of a multiphase flow rectifying region (30-1) at the bottom of the carbon-containing material pressurized thermochemical reaction unit (30) is connected with a heat capacity/bed density regulation and fluidization circulation unit (27) through a refractory lining, the top of the carbon-containing material pressurized thermochemical reaction unit (30) is further connected with a first-stage multiphase flow splitter (32), and carbon-poor particles obtained by splitting of the first-stage multiphase flow splitter (32) flow downwards and sequentially pass through a first-stage multiphase flow splitter fluidization leg (33), The carbon-poor particle sealing return feeder (34) is connected with a multiphase flow temperature regulation and control area (30-2) of the carbon-containing material pressurization thermochemical reaction unit (30), high-temperature gas-solid mixed fluid output from the top of the first-stage multiphase flow diverter (32) enters the second-stage multiphase flow diverter (40) through a lining pipeline (35), carbon-rich coarse particles obtained by diversion of the second-stage multiphase flow diverter (40) sequentially flow downwards through a fluidization dipleg (41) of the second-stage multiphase flow diverter and a carbon-rich coarse particle sealing return feeder (42) and circularly return to a circulating particle strengthening and transferring area (20-1) at the bottom of a carbon-rich particle chemical chain reaction unit (20) of the carbon-rich particle chemical chain conversion system, high-temperature gas-solid mixed fluid output from the top of the second-stage multiphase flow diverter (40) enters the third-stage multiphase flow diverter (50) through a second-stage lining pipeline (43), and carbon-rich fine particles obtained by diversion of the multiphase flow The slurry is made into stable suspension and then enters a suspension slurry storage tank (105) after entering a graded slurry preparation unit (53) connected with a compound pulping agent (104) and being made into stable suspension, the suspension slurry storage tank (105) is connected with a chemical chain initial reaction area (20-3) of a carbon-rich particle chemical chain reaction unit (20) through an active carbon-rich fine particle circulating material returning unit (210), and gas-solid mixed fluid containing ultrafine particles obtained by shunting of a three-level multiphase flow diverter (50) is mixed with a quenching agent (103) in a drawing quenching pipe (54) and then enters a multiphase flow quenching settler (60) of a multiphase flow splitting system;
the carbon-rich particle chemical chain conversion system comprises a carbon-rich particle chemical chain reaction unit (20), an inert particle discharge pipe (25) is arranged at an outlet at the lower end of the carbon-rich particle chemical-looping reaction unit (20), high-temperature inert particles discharged through the inert particle discharge pipe (25) downwards enter an inert particle discharge and heat energy recovery unit (80), an outlet at the upper end of the carbon-rich particle chemical-looping reaction unit (20) is connected with a multi-attribute particle diverter (22) through a lining pipeline (21), the upper end of the multi-attribute particle diverter (22) is connected with a multiphase rectifying region at the lower end of a carbonaceous material pressurization thermochemical reaction unit (30) through a diverter lining pipeline (26), and the lower end of the multi-attribute particle diverter (22) is respectively connected with a porous particle sealing return feeder (24) and a heat capacity/bed density regulation and fluidization circulation unit (27) through a multi-attribute particle diverter fluidization dipleg (23);
the multiphase flow quenching settler (60) of the multiphase flow separation system is characterized in that the upper end of the multiphase flow quenching settler (60) is provided with a gas-phase product outlet (106), the lower end of the multiphase flow quenching settler is respectively connected with inlets of a first cross processor (61 a) and a second cross processor (61 b), outlets of the first cross processor (61 a) and the second cross processor (61 b) are connected with a multiphase flow wet diverter (63) through a light-distillate multi-effect recovery tower (62), heavy distillate oil separated by the multiphase flow wet diverter (63) is output through a heavy-distillate outlet (107), heavy components obtained after diversion descend to enter a colloid particle diverter (64), carbon-rich colloid particles obtained by separation enter a colloid particle modification activation tower (65), porous active particles obtained by the colloid particle modification activation tower (65) pass through a porous active particle conveyor (109) and circularly return to a carbon-containing material pressurization thermochemical reaction unit (30), the side wall of the colloidal particle modification activation tower (65) is also provided with an inlet connected with a modifier conveyor (108).
2. The adaptive three-cycle pressurized carbonaceous material stepped conversion system according to claim 1, wherein the carbon-rich particle chemical-looping reaction unit (20) comprises a bottom-up circulating particle reinforced transfer area (20-1), a carbon-rich particle activation area (20-2), a chemical-looping initiation reaction area (20-3), a chemical-looping depth reaction area (20-4) and a transition regulation and control area (20-5), the side wall of the circulating particle reinforced transfer area (20-1), the side wall of the carbon-rich particle activation area (20-2) and the side wall of the chemical-looping initiation reaction area (20-3) are respectively provided with 1-10 activator inlets connected with an activator (200) through flow control valves from bottom to top, and the suspension slurry storage tank (105) is in phase with the chemical-looping initiation reaction area (20-3) of the carbon-rich particle chemical-looping reaction unit (20) through an activated carbon-rich fine particle circulating material returning unit (210) And (4) connecting.
3. The adaptive three-cycle pressurized carbonaceous material step conversion system according to claim 1, wherein the carbonaceous material pressurized thermochemical reaction unit (30) comprises a multiphase flow rectifying region (30-1), a multiphase flow temperature regulating region (30-2), a mixed material strengthening and transferring region (30-3) and a hydrocracking reaction region (30-4) from bottom to top, the carbonaceous material inlet (301), the porous active particle sealing material returning unit (310) and the mixed material strengthening and transferring region (30-3) are communicated, and the bottom of the multi-attribute particle diverter fluidization dipleg (23) is connected with the multiphase flow rectifying region (30-1) at the bottom of the carbonaceous material pressurized thermochemical reaction unit (30) through a heat capacity/bed density regulating fluidization circulation unit (27).
4. The adaptive three-cycle pressurized carbonaceous material staged conversion system of claim 1, wherein the porous active particulate recycle unit (310) comprises a colloidal particle splitter (64), a colloidal particle modification activation tower (65), and a modifier conveyor (108) and a porous active particulate conveyor (109) connected to the colloidal particle modification activation tower (65).
5. The adaptive three-cycle pressurized carbonaceous material step conversion system according to claim 1, wherein the carbon-rich particle chemical-looping reaction unit (20) is connected with the multi-attribute particle diverter (22) through a lining pipeline (21), the multi-attribute particle diverter fluidization dipleg (23) is connected with an inlet of the circulating particle enhanced transfer zone (20-1) at the bottom of the carbon-rich particle chemical-looping reaction unit (20) through a porous particle sealing return feeder (24), and the axial included angles of the carbon-rich particle chemical-looping reaction unit (20) and the porous particle sealing return feeder (24) and the carbon-rich particle sealing return feeder (42) are respectively 40-90 °.
6. The adaptive three-cycle pressurized carbonaceous material step conversion system according to claim 1, wherein the carbonaceous material pressurized thermochemical reaction unit (30) is connected with the primary multiphase flow splitter (32) through a lining pipe (31), the primary multiphase flow splitter fluidization dipleg (33) is connected with the multiphase flow temperature control region (30-2) of the carbonaceous material pressurized thermochemical reaction unit (30) through a carbon-poor particle sealing return feeder (34), and the axial included angles of the carbonaceous material pressurized thermochemical reaction unit (30) and the lining pipe (31) and the carbon-poor particle sealing return feeder (34) are 40-90 degrees.
7. The adaptive three-cycle pressurized carbonaceous material cascade conversion system according to claim 1, wherein the outlet end of the extraction quenching pipe (54) at the middle-lower part of the three-stage multiphase flow splitter (50) is connected with the inlet at the top of the multiphase flow quenching settler (60), the inlet end of the extraction quenching pipe (54) is composed of a reducing joint (54-1) and an extraction throat pipe (54-2) sleeved therein, an annular cavity (54-3) is formed between the reducing joint (54-1) and the extraction throat pipe (54-2), the quenching medium (103) enters the extraction quenching pipe (54) from the reducing joint (54-1) and is mixed with the high-temperature gas-solid mixed fluid output by the three-stage multiphase flow splitter (50) through the annular cavity (54-3), and the extraction quenching pipe (54) is located at 1/5-2/3 of the vertical height of the three-stage multiphase flow splitter (50), the included angle between the central line and the vertical line is 30-65 degrees.
8. The adaptive three-cycle pressurized carbonaceous material cascade conversion system according to claim 1, wherein the bottom of the multiphase flow quenching settler (60) is provided with crossed discharge ports, each discharge port is respectively connected with a first crossed processor (61 a) and a second crossed processor (61 b) through a shut-off valve, and the outlets of the first crossed processor (61 a) and the second crossed processors (61 b) are combined and then connected with the inlet of a light distillate oil multi-effect recovery tower (62).
9. The adaptive three-cycle pressurized carbonaceous material staged conversion system of claim 1, wherein: the flow divider lining pipeline (26) is connected with the secondary lining pipeline (43) through a thermal capacitance coupling compensation regulator (70).
10. A self-adaptive three-cycle pressurized carbon-containing material step conversion method is characterized by mainly comprising the following steps:
a) the method comprises the following steps that a carbon-containing material (100) firstly enters a carbon-containing material pretreatment device (10) of a carbon-containing material feeding system to prepare powder particles with the water content of less than or equal to 4.0 wt% and the particle size range of 100-1000 mu m, then enters a mixed material reinforced transfer area (30-3) of a carbon-containing material pressurization thermochemical reaction unit (30) through a carbon-containing material conveying device (11) and a material conveying control device (12) connected with a conveying medium (101), and a high-temperature gas-solid mixed fluid generated after thermochemical conversion ascends from a hydro-thermal cracking reaction area (30-4) at the top of the carbon-containing material pressurization thermochemical reaction unit (30) to enter a first-stage multiphase flow divider (32);
b) the carbon-poor particles with the carbon content of 1.00-10.00 wt% obtained by the flow of the primary multi-phase flow diverter (32) downwards enter a fluidization dipleg (33) of the primary multi-phase flow diverter, circularly return to a multi-phase flow temperature regulation and control area (30-2) at the middle lower part of the carbon-containing material pressurization thermochemical reaction unit (30) through a carbon-poor particle sealing return feeder (34), and high-temperature gas-solid mixed fluid output from the top of the primary multi-phase flow diverter (32) enters a secondary multi-phase flow diverter (40) through a lining pipeline (35);
c) the carbon-rich coarse particles with the particle size range larger than or equal to 50 mu m and the carbon content of 50.00-85.00 wt% captured by the second-stage multiphase flow diverter (40) downwards enter a fluidization dipleg (41) of the second-stage multiphase flow diverter, circularly return to a circulating particle reinforced transfer area (20-1) at the bottom of a carbon-rich particle chemical chain reaction unit (20) through a carbon-rich coarse particle sealed return feeder (42), and high-temperature gas-solid mixed fluid output from the top of the second-stage multiphase flow diverter (40) enters a third-stage multiphase flow diverter (50) through a lining pipeline (43);
d) the carbon-rich fine particles with the particle size range of 1-50 microns captured by the third-stage multiphase flow splitter (50) downwards enter a fluidization dipleg (51) of the third-stage multiphase flow splitter, the carbon-rich particles flowing downwards in the fluidization dipleg (51) of the third-stage multiphase flow splitter enter a stage batching slurry preparation unit (53) through a fluidization energy dissipater (52) to prepare stable suspension, the stable suspension is transferred into a suspension slurry storage tank (105), the stable suspension enters a chemical chain initial reaction zone (20-3) in the middle of a carbon-rich particle chemical chain reaction unit (20) through an active carbon-rich fine particle circulation material returning unit (210), and gas-solid mixed fluid output from the top of the third-stage multiphase flow splitter (50) enters a multiphase flow quenching settler (60) after being mixed with quenching agent (103) through a pumping quenching pipe (54);
e) the gas-liquid-solid mixed fluid entering the multiphase flow quenching settler (60) is subjected to high-efficiency flow splitting, a gas phase product (106) is output from the top of the multiphase flow quenching settler (60) and enters the downstream for deep separation, the obtained liquid-solid mixed fluid is divided into two flows downwards and enters a first cross processor (61 a) and a second cross processor (61 b) and then enters a light distillate oil multi-effect recovery tower (62) after being converged, and finally enters a multiphase flow wet flow diverter (63) for high-efficiency multiphase flow separation, the heavy component obtained after the flow splitting enters a colloidal particle diverter (64) downwards, the carbon-rich colloidal particles obtained by the separation enter a colloidal particle modification activation tower (65) for modification activation treatment, the obtained porous active particles are circulated back to a mixed material reinforced transfer area (30-3) at the lower part of the carbon-containing material pressurized thermochemical reaction unit (30) through a porous active particle conveyor (109);
f) the carbon-rich coarse particles circularly returned to the bottom circulating particle reinforced transfer area (20-1) of the carbon-rich particle chemical chain reaction unit (20) through the carbon-rich coarse particle sealing return feeder (42) go upward to pass through a carbon-rich particle activation area (20-2) and then are converged with the stable suspension liquid entering the chemical chain initial reaction area (20-3) through the activated carbon-rich fine particle circulating return unit (210) in the step d) and then sequentially go upward to pass through a chemical chain deep reaction area (20-4) and a transition regulation and control area (20-5), the high-temperature gas-solid mixed fluid containing the multi-attribute particles generated after deep chemical chain conversion enters a multi-attribute particle flow divider (22) through a lining pipeline (21), inert coarse particles obtained by flow division of the multi-attribute particle flow divider (22) downwards enter a multi-attribute particle flow divider fluidization dipleg (23), and then the high-temperature gas-solid mixed fluid is divided into two paths: one path of the gas flow passes through a porous particle sealing return feeder (24) and circularly returns to a circulating particle reinforced transfer zone (20-1) at the bottom of a carbon-rich particle chemical chain reaction unit (20), and the other path of the gas flow passes through a heat capacity/bed density control fluidization circulation unit (27) and ascends to enter a multiphase flow rectification zone (30-1) of a carbon-containing material pressurization thermochemical reaction unit (30); inert coarse particles generated by the carbon-rich particle chemical-looping reaction unit (20) enter an inert particle discharging and heat energy recovery unit (80) from a bottom outlet through a discharging lining pipeline (25);
g) the high-temperature gas-solid mixed fluid obtained by shunting through the multi-attribute particle shunt (22) enters a multiphase flow rectifying area (30-1) at the bottommost end of a carbon-containing material pressurizing thermochemical reaction unit (30) through a shunt lining pipeline (26), firstly is rectified with multi-property particles from a heat capacity/bed density regulating and fluidizing circulation unit (27) and then ascends to enter a multiphase flow temperature regulating and controlling area (30-2), then is mixed with carbon-poor particles from a carbon-poor particle sealing return feeder (34) and ascends to enter a mixed material reinforced transfer area (30-3), and finally is mixed with qualified powder particles from a carbon-containing material feeding system and then enters a hydrogen thermal cracking reaction area (30-4) for thermal cracking reaction, so that the closed-loop process circulation from the step a) to the step g) is completed.
11. The adaptive three-cycle pressurized carbonaceous material staged conversion method according to claim 10, wherein the carbonaceous material (100) is a carbonaceous material with a volatile content of 20.00 wt% to 45.00 wt%, and the transport medium (101) is CO2、N2One or more than two of fuel combustion flue gas with the oxygen content less than or equal to 5.0 vol% or circulating synthesis gas, a carbon-containing material steady-state conveying feedback device (13) is connected with a mixed material reinforced transfer area (30-3) of a carbon-containing material pressurizing thermochemical reaction unit (30), and overheating protection steam with the internal apparent flow rate of 20-50 m/s is arranged at a carbon-containing material feeding port (301).
12. The self-adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein the heavy components output from the bottom of the multiphase flow wet splitter (63) enter the colloid particle splitter (64) to obtain colloid particles with a solid content of 40 wt% -60 wt%, and if the volatile components of the colloid particles are a low aromatic intermediate phase with a content of more than or equal to 40 wt%, the colloid particles are directly heated to more than or equal to 200 ℃ and then are conveyed to the carbonaceous material pressurized thermochemical reaction unit (30) through the colloid particle feeder (310) for deep conversion.
13. The self-adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein a particle circulation factor of a multi-channel carbon-poor circulation material returning system constructed by the carbonaceous material pressurized thermochemical reaction unit (30), the primary multiphase flow splitter (32), the primary multiphase flow splitter fluidization dipleg (33) and the carbon-poor particle sealing material returning device (34) is regulated within 50-300.
14. The adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein the activating agent (200) enters the discharge liner pipeline (25) and the carbon-rich particle activation zone (20-2) and the chemical chain initiation reaction zone (20-3) of the carbon-rich particle chemical chain reaction unit (20) respectively to participate in the thermochemical chain conversion reaction of the carbonaceous material, wherein the H in the activating agent entering the carbon-rich particle activation zone (20-2)2O (g) partial pressure and O2Partial pressure ratio [ (PH)2O)/PO2]Not less than 1.0, H in the activator entering the chemical chain initiation reaction zone (20-3)2O (g) partial pressure and O2Partial pressure ratio [ (PH)2O)/PO2]≤1.0。
15. The adaptive three-cycle pressurized carbonaceous material staged conversion method as claimed in claim 10, wherein the internal diameters of the different regions of the carbon-rich particle chemical-looping reaction unit (20) are numbered D1, D2 and D3, the height of the circulating particle enhanced transfer region (20-1) at the lowest end is 0.5D 1-1.5D 1, the height of the carbon-rich particle activation region (20-2) at the upper end of the circulating particle enhanced transfer region (20-1) is 0.5D 1-1.5D 1, the height of the chemical-looping initiation reaction region (20-3) at the upper end of the carbon-rich particle activation region (20-2) is 0.05D 2-D2, the height of the chemical-looping depth reaction region (20-4) at the upper end of the chemical-looping initiation reaction region (20-3) is 0.5D 2-4D 2, and the height of the transition control region (20-5) at the top end is 0.5D 3-3D.
16. The adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein the carbon-rich particle chemical-looping reaction unit (20) has an operating temperature of 950-1200 ℃, an operating pressure of 0.5-5 MPa, and an internal mixed fluid superficial velocity of 0.8-5.0 m/s.
17. The self-adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein the operating temperature of the carbonaceous material pressurized thermochemical reaction unit (30) is 500 to 650 ℃, the operating pressure is 0.5 to 5MPa, and the superficial velocity of the internal mixed fluid is 0.8 to 5.0 m/s.
18. The self-adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein the operating temperature of the multiphase flow dry-method flow splitting unit is 480-630 ℃, and the operating pressure is 0.5-5 MPa.
19. The adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein the operating temperature of the multiphase flow quench settler (60) is 280-380 ℃ and the operating pressure is 0.5-5 MPa.
20. The adaptive three-cycle pressurized carbonaceous material step conversion method according to claim 10, wherein the multiphase flow wet splitter (63) has an operating temperature of 80-120 ℃ and an operating pressure of 0.1-0.5 MPa.
Technical Field
The invention belongs to the field of energy and chemical engineering integration technology and process systems, and particularly relates to a self-adaptive three-cycle pressurized carbon-containing material step conversion system and method.
Background
The clean and efficient conversion technology for carbon-containing materials such as coal, biomass, petroleum coke, semicoke, oil shale, oil sand asphalt, heavy asphalt and the like is a key technology, a common technology and a pilot technology for process industries such as a multi-industry cross-coupling industrial mode for realizing diversification of industrial hydrogen production raw materials, development of liquid fuel synthesis, bulk energy product synthesis, fuel cells, IGCC clean gas power generation and the like. In the method, the development of large-scale high-efficiency and clean conversion integrated devices and process systems of the carbon-containing materials, which are easy to realize industrial popularization and application, is an important basic stone and a prerequisite for the development of the technical system, around the aims of large-scale device, strong adaptability of raw materials, intensification of technological process, high carbon conversion rate, reasonable hydrogen-carbon ratio of gas-phase products, high light components and aromatic hydrocarbon content of liquid-phase products, low device specific investment strength, high energy efficiency level, near-zero pollutant discharge and the like.
Patent document CN108179030A discloses a biomass gasification furnace and a biomass gasification method, wherein opposed nozzles and angled nozzles are provided, so that the temperature distribution of the cross section of the throat section is uniform, the high temperature can be maintained, and further tar can be oxidized and pyrolyzed, so that the tar removal efficiency in the furnace is further improved. Patent document CN108003902A discloses a system and a method for fast pyrolysis of biomass, in which pyrolysis gas generated by biomass itself is used as a heat carrier and fuel gas for fast pyrolysis. Pyrolysis gas generated by biomass decomposition is divided into two parts, one part is used as fuel of a heat carrier heating furnace and used for heating a heat carrier after combustion, and the other part of pyrolysis gas is directly used as the heat carrier and directly introduced into the pyrolysis furnace to heat biomass materials.
Patent document CN105712295A discloses a method for preparing porous carbon by co-pyrolysis of petroleum coke and oily sludge, which utilizes the co-pyrolysis of petroleum coke and oily sludge to prepare porous carbon, and exerts the synergistic effect of petroleum coke and oily solid waste, thereby realizing the resource and harmless utilization of petroleum coke and oily solid waste, and simultaneously preparing a porous carbon material with a large comparative area and narrow pore size distribution. Patent document CN105712295A discloses a method for preparing a hydrogen-rich gas by catalytic gasification of petroleum coke, in which a catalyst and petroleum coke are fully mixed, a catalytic gasification reaction is performed under the conditions that the gasification temperature is 700-900 ℃, the water vapor partial pressure is 40-70%, and the gasification reaction time is 10-120 min, and the hydrogen-rich gas is finally obtained by removing water vapor through condensation after gas generated by catalytic gasification is discharged.
Patent document CN106010613A discloses a method and equipment for directly obtaining light oil by pyrolyzing small-particle oil sand, in which crude ore is crushed and dried, directly cracked at high temperature, pyrolysis time, temperature and the like are controlled to obtain tailings and light components in different proportions, and the light components are fractionated to obtain dry gas, gasoline and diesel components, heavy fuel oil and water. Patent document CN106010613A discloses a method and a device for preparing clean fuel oil by pyrolyzing oil sand, in which the oil sand and pulverized coal are crushed, dried, mixed with a high-temperature heat carrier and lime, and subjected to pyrolysis reaction to generate oil gas and semicoke; the generated oil gas is cooled, collected by dust and fractionated, and then oil slurry, distillate oil and coke oven gas are discharged; each distillate oil is clean fuel oil; burning the generated semicoke and coke oven gas together with combustion air to generate high-temperature solid particles and high-temperature flue gas; and a part of the high-temperature solid particles are used as a high-temperature heat carrier and enter the dry distillation furnace for pyrolysis reaction.
As basic energy and strategic resources in China, the research on coal gasification and pyrolysis technology is most extensive and intensive, the traditional coal conversion is mainly gasification conversion, a coal gasification device is taken as a 'leading', and downstream industrial chains are expanded to coal-to-olefin, coal-to-natural gas and coal-to-ethylene glycol, fuel oil products and high-end fine chemical products through F-T synthesis and the like. Although the coal gasification process converts coal into simple and stable CO and H2、CO2And the like, but the inorganic micromolecules have the defects of excessive splitting of coal molecules, high energy consumption level, low energy utilization efficiency and the like, the chemical energy contained in the coal resources cannot be fully utilized, and the quality classification and classification of the coal resources and the gradient utilization of the energy resources are not realized. The modern coal resource quality-divided high-efficiency conversion process technology taking the coal pyrolysis and coal carbonization technologies as the core can realize the comprehensive utilization of coal resources, realize the diversification and high added value of terminal coal chemical products and further widen the downstream industrial chain distribution. Since 1805 years ago, from the beginning of the production of semi-coke by using bituminous coal as a raw material through a medium-low temperature pyrolysis method in the united kingdom, dozens of different coal pyrolysis processes have appeared at home and abroad, the foreign research and development are mainly concentrated in the last 60-70 years, the processes mainly comprise the ETCH pulverized coal pyrolysis process of the former Soviet Union, the Lurgi-Ruhrgas process of Germany, the Toscoal, COED, the Garrent process of America, the Australian CSIRO process, the Japanese fast pyrolysis process and the like, the autonomous research and development of the coal pyrolysis technology of China begin in the last 50 years, and the typical coal pyrolysis process startsThe method comprises a DG process of the university of the major continental engineering, a ZNLZ pyrolysis technology of the Anshan heat energy institute, an SJ pyrolysis technology of Sanjiang Shenmu, a belt furnace modification upgrading technology developed by Beijing Corlinsida company, a GG-I coal upgrading technology developed by Beijing Counton Futong, a heat accumulation type non-heat carrier rotating bed technology developed by Beijing Shengou group, a low-temperature dry distillation technology developed by Henan Longcheng group and Longcheng group, a gasification-pyrolysis integrated technology developed by Shaanxi coal industry chemical group and the like. However, the above-mentioned conversion technologies including coal, biomass, petroleum coke, semicoke, oil shale, oil sand bitumen, heavy bitumen and other carbon-containing materials all have the disadvantages of low device system integration degree, low energy efficiency level, strong raw material selectivity and poor product quality, and most importantly, the product conversion is not thorough, and it is difficult to convert the carbon-containing materials into high-added-value terminal functionalized products with high yield, and the comprehensive coupling integration of the pyrolysis and gasification processes of the carbon-containing materials in the processes of material, energy and process is not really realized.
Disclosure of Invention
The invention aims to provide a self-adaptive three-cycle pressurized carbon-containing material step conversion system and a method for performing efficient clean conversion and step utilization on carbon-containing materials by using carbon-containing materials such as petroleum coke, heavy oil sandstone, biomass, low-rank coal resources and the like as raw materials.
In order to achieve the aim, the system comprises a carbon-containing material preparation system, a carbon-containing material pressurization thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multi-phase flow diversion system;
the carbonaceous material preparation system comprises a carbonaceous material pretreatment sub-device, a carbonaceous material conveying device, a material conveying control device and a carbonaceous material steady-state conveying feedback device which are sequentially connected;
the multi-phase flow diversion system comprises a multi-phase flow dry diversion unit, a multi-phase flow quenching settler and a multi-phase flow wet diverter;
the multiphase flow dry-method flow dividing unit comprises a multi-attribute particle flow divider, a first-stage multiphase flow divider, a second-stage multiphase flow divider and a third-stage multiphase flow divider;
the carbon-containing material pressurized thermochemical conversion system comprises a carbon-containing material pressurized thermochemical reaction unit, a carbon-containing material feeding port connected with a carbon-containing material steady-state conveying feedback device and a porous active particle inlet connected with a porous active particle return unit are respectively arranged on a mixed material reinforced transfer region in the middle of the carbon-containing material pressurized thermochemical reaction unit, an outlet of a multiphase flow rectifying region at the bottom of the carbon-containing material pressurized thermochemical reaction unit is connected with a heat capacity/bed density regulation and control fluidization circulation unit through a refractory lining, the top of the carbon-containing material pressurized thermochemical reaction unit is also connected with a first-stage multiphase flow splitter, carbon-poor particles obtained by splitting through the first-stage multiphase flow splitter flow legs and a carbon-poor particle sealing return device sequentially flow downwards and are connected with a multiphase flow temperature regulation and control region of the carbon-containing material pressurized thermochemical reaction unit, high-temperature gas-solid mixed fluid output from the top of the first-stage multiphase flow splitter enters a second-stage multiphase flow splitter through a lining pipeline, carbon-rich coarse particles obtained by splitting of the second-stage multiphase flow splitter flow downwards sequentially pass through a second-stage multiphase flow splitter fluidization dipleg and a carbon-rich coarse particle sealing return feeder to circularly return to a circulating particle reinforced transfer area at the bottom of a carbon-rich particle chemical chain reaction unit of the carbon-rich particle chemical chain conversion system, high-temperature gas-solid mixed fluid output from the top of the second-stage multiphase flow splitter enters a third-stage multiphase flow splitter through the second-stage lining pipeline, carbon-rich fine particles obtained by splitting of the third-stage multiphase flow splitter flow downwards sequentially enter a third-stage multiphase flow splitter fluidization dipleg and a fluidization energy dissipater and then enter a stage slurry preparation unit connected with a compound slurrying agent to form stable suspension, the stable suspension is pumped into a suspension slurry storage tank, and the suspension slurry storage tank passes through an active carbon- The reaction zones are connected, and gas-solid mixed fluid containing ultrafine particles obtained by shunting of the three-stage multiphase flow diverter is mixed with quenching medium in the pumping quenching pipe and then enters a multiphase flow quenching settler of the multiphase flow splitting system;
the carbon-rich particle chemical chain conversion system comprises a carbon-rich particle chemical chain reaction unit, wherein an inert particle discharge pipe is arranged at an outlet at the lower end of the carbon-rich particle chemical chain reaction unit, high-temperature inert particles discharged by the inert particle discharge pipe downwards enter an inert particle discharge and heat energy recovery unit, an outlet at the upper end of the carbon-rich particle chemical chain reaction unit is connected with a multi-attribute particle flow divider through a lining pipeline, the upper end of the multi-attribute particle flow divider is connected with a multiphase rectifying area at the lower end of a carbon-containing material pressurization thermochemical reaction unit through the lining pipeline, and the lower end of the multi-attribute particle flow divider is respectively connected with a porous particle sealing return feeder and a heat capacity/bed density regulation and fluidization circulation unit through a multi-;
the multi-phase flow quenching settler of the multi-phase flow separation system is characterized in that a gas-phase product outlet is formed in the upper end of the multi-phase flow quenching settler, the lower end of the multi-phase flow quenching settler is connected with inlets of a first cross processor and a second cross processor respectively, the outlets of the first cross processor and the second cross processor are connected with a multi-effect light distillate oil recovery tower and a multi-phase flow wet diverter, heavy distillate oil separated by the multi-phase flow wet diverter is output from a heavy distillate oil outlet, heavy components obtained after diversion downwards enter a colloidal particle diverter, carbon-rich colloidal particles obtained after separation enter a colloidal particle modification activation tower, porous active particles obtained by the colloidal particle modification activation tower circularly return to a carbon-containing material pressurization thermochemical reaction unit through a porous active particle conveyor, and an inlet connected with a modifier conveyor is formed in the side wall of the colloidal particle modification activation tower.
The carbon-rich particle chemical chain reaction unit comprises a circulating particle reinforced transfer area, a carbon-rich particle activation area, a chemical chain initial reaction area, a chemical chain deep reaction area and a transition regulation and control area from bottom to top, 1-10 activator inlets connected with activators through flow control valves are respectively formed in the side wall of the circulating particle reinforced transfer area, the side wall of the carbon-rich particle activation area and the side wall of the chemical chain initial reaction area from bottom to top, and the suspension slurry storage tank is connected with the chemical chain initial reaction area of the carbon-rich particle chemical chain reaction unit through an active carbon-rich fine particle circulating material returning unit.
The carbon-containing material pressurized thermochemical reaction unit comprises a multiphase flow rectifying area, a multiphase flow temperature regulating and controlling area, a mixed material strengthening and transferring area and a hydrogen thermal cracking reaction area from bottom to top, a carbon-containing material inlet, a porous active particle sealing material returning unit and the mixed material strengthening and transferring area are communicated, and the bottom of a fluidization leg of the multi-attribute particle flow divider is connected with the multiphase flow rectifying area at the bottom of the carbon-containing material pressurized thermochemical reaction unit through a heat capacity/bed density regulating and controlling fluidization circulation unit.
The porous active particle returning unit comprises a colloidal particle splitter, a colloidal particle modification activation tower, a modifier conveyor and a porous active particle conveyor, wherein the modifier conveyor and the porous active particle conveyor are connected with the colloidal particle modification activation tower.
The carbon-rich particle chemical chain reaction unit is connected with the multi-attribute particle diverter through a lining pipeline, the fluidization dipleg of the multi-attribute particle diverter is connected with the inlet of the circulating particle reinforced transfer area at the bottom of the carbon-rich particle chemical chain reaction unit through the porous particle sealed return feeder, and the axial included angles of the axial direction of the carbon-rich particle chemical chain reaction unit and the axial direction of the porous particle sealed return feeder and the carbon-rich particle sealed return feeder are respectively 40-90 degrees.
The carbon-containing material pressurized thermochemical reaction unit is connected with the primary multiphase flow splitter through a lining pipeline, the fluidized dipleg of the primary multiphase flow splitter is connected with the multiphase flow temperature regulation and control area of the carbon-containing material pressurized thermochemical reaction unit through a carbon-poor particle sealing return feeder, and the axial included angles of the carbon-containing material pressurized thermochemical reaction unit and the lining pipeline and the carbon-poor particle sealing return feeder are 40-90 degrees.
The outlet end of a pumping quenching pipe at the middle lower part of the three-stage multiphase flow diverter is connected with the inlet at the top of the multiphase flow quenching settler, the inlet end of the pumping quenching pipe is composed of a pumping throat pipe sleeved in a reducing joint, an annular cavity is formed between the reducing joint and the pumping throat pipe, quenching medium enters the pumping quenching pipe from the reducing joint and is mixed with high-temperature gas-solid mixed fluid output by the three-stage multiphase flow diverter through the annular cavity, the pumping quenching pipe is positioned at 1/5-2/3 of the vertical height of the conical part of the three-stage multiphase flow diverter, and the included angle between the central line and the vertical line is 30-65 degrees.
The bottom of the multiphase flow quenching settler is provided with crossed discharge ports, each discharge port is respectively connected with a first crossed processor and a second crossed processor through a stop valve, and the outlets of the first crossed processor and the second crossed processor are merged and then connected with the inlet of a light distillate oil multi-effect recovery tower.
The flow divider lining pipeline is connected with the secondary lining pipeline through a thermal capacitance coupling compensation regulator.
The method of the invention comprises the following steps: a) the carbon-containing material firstly enters a carbon-containing material pretreatment device of a carbon-containing material feeding system) to prepare powder particles with the water content of less than or equal to 4.0 wt% and the particle size range of 100-1000 mu m, then enters a mixed material reinforced transfer region of a carbon-containing material pressurized thermochemical reaction unit through a carbon-containing material conveying device and a material conveying control device connected with a conveying medium, and high-temperature gas-solid mixed fluid generated after thermochemical conversion ascends from a hydrogen thermal cracking reaction region at the top of the carbon-containing material pressurized thermochemical reaction unit and enters a primary multiphase flow splitter;
b) the carbon-poor particles with the carbon content of 1.00-10.00 wt% obtained by the flow division of the primary multi-phase flow divider downwards enter a fluidization dipleg of the primary multi-phase flow divider, and circularly return to a multi-phase flow temperature regulation and control area at the middle lower part of the carbon-containing material pressurization thermochemical reaction unit through a carbon-poor particle sealing return feeder, and high-temperature gas-solid mixed fluid output from the top of the primary multi-phase flow divider enters the secondary multi-phase flow divider through a lining pipeline;
c) the carbon-rich coarse particles with the particle size range larger than or equal to 50 mu m and the carbon content of 50.00-85.00 wt% captured by the second-stage multiphase flow diverter downwards enter a fluidization dipleg of the second-stage multiphase flow diverter, the carbon-rich coarse particles are circularly returned to a circulating particle reinforced transfer area at the bottom of the carbon-rich particle chemical chain reaction unit through a carbon-rich coarse particle sealing return feeder, and high-temperature gas-solid mixed fluid output from the top of the second-stage multiphase flow diverter enters the third-stage multiphase flow diverter through a lining pipeline;
d) the carbon-rich fine particles with the particle size range of 1-50 microns captured by the third-stage multiphase flow diverter downwards enter a fluidization dipleg of the third-stage multiphase flow diverter, the carbon-rich particles flowing downwards in the fluidization dipleg of the third-stage multiphase flow diverter pass through a fluidization energy dissipater and then enter a stage batching slurry preparation unit to prepare stable suspension, then the stable suspension is transferred into a suspension slurry storage tank and enters a chemical chain initial reaction area in the middle of a carbon-rich particle chemical chain reaction unit through an active carbon-rich fine particle circulation material returning unit, and gas-solid mixed fluid output from the top of the third-stage multiphase flow diverter is mixed with quenching agent through a pumping quenching pipe and then enters a multiphase flow quenching settler;
e) the gas-liquid-solid mixed fluid entering the multi-phase flow quenching settler is subjected to high-efficiency flow splitting, a gas-phase product is output from the top of the multi-phase flow quenching settler and enters the downstream for deep separation, the obtained liquid-solid mixed fluid is divided into two flows downwards and enters a first cross processor and a second cross processor, then the two flows are converged and enter a light distillate oil multi-effect recovery tower, finally the two flows enter a multi-phase flow wet-method flow divider for multi-phase flow high-efficiency separation, the heavy component obtained after flow splitting enters a colloidal particle flow divider downwards, the carbon-rich colloidal particles obtained after separation enter a colloidal particle modification activation tower for modification activation treatment, and the obtained porous active particles are circulated by a porous active particle conveyor and return to a mixed material reinforced transfer area at the lower part of a carbon-containing material pressurized thermochemical reaction;
f) the carbon-rich coarse particles circularly returned to the carbon-rich particle chemical chain reaction unit bottom circulating particle reinforced transfer area by the carbon-rich coarse particle sealing return feeder pass through a carbon-rich particle activation area upwards and then are converged with the stable suspension entering the chemical chain initial reaction area by the active carbon-rich fine particle circulating return unit in the step d), then sequentially pass through a chemical chain deep reaction area and a transition regulation and control area upwards, the high-temperature gas-solid mixed fluid containing the multi-attribute particles generated after deep chemical chain conversion enters a multi-attribute particle splitter through a lining pipeline, the inert coarse particles obtained by splitting of the multi-attribute particle splitter flow downwards enter a multi-attribute particle splitter fluidization dipleg, and then are divided into two paths: one path is returned to the circulating particle reinforced transfer area at the bottom of the carbon-rich particle chemical chain reaction unit by a porous particle sealing return feeder) in a circulating way, and the other path is ascended to enter a multiphase flow rectifying area of the carbon-containing material pressurized thermochemical reaction unit by a heat capacity/bed density control fluidization circulating unit; inert coarse particles generated by the carbon-rich particle chemical chain reaction unit enter the inert particle discharging and heat energy recovery unit from a bottom outlet through a discharging lining pipeline;
g) the high-temperature gas-solid mixed fluid obtained by shunting of the multi-attribute particle flow divider enters a multiphase flow rectification area at the bottommost end of a carbon-containing material pressurization thermochemical reaction unit through a lining pipeline, is rectified with the multi-property particles from the heat capacity/bed density regulation and fluidization circulation unit and then flows upwards to enter a multiphase flow temperature regulation and control area, is mixed with the carbon-poor particles from the carbon-poor particle sealing return feeder and then flows upwards to enter a mixed material reinforced transmission area, and is finally mixed with qualified powder particles from a carbon-containing material feeding system and then enters a hydrogen thermal cracking reaction area for thermal cracking reaction, so that the closed-loop process circulation from the step a) to the step g) is completed.
The carbon-containing material is carbon-containing material with 20.00-45.00 wt% of volatile component content, and the conveying medium (101) adopts CO2、N2And the oxygen content is less than or equal to 5.0 vol%, one or more than two of fuel combustion flue gas or circulating synthesis gas, the carbon-containing material stable-state conveying feedback device is connected with a mixed material reinforced transfer area of the carbon-containing material pressurizing thermochemical reaction unit, and an internal apparent flow rate of 20-50 m/s of overheat protection steam is arranged at a feeding port of the carbon-containing material.
The heavy component output from the bottom of the multiphase flow wet-process flow divider enters the colloid particle flow divider to obtain colloid particles with solid content of 40-60 wt%, and if the volatile content of the colloid particles is more than or equal to 40 wt%, the low-aromaticity intermediate phase is directly heated to more than or equal to 200 ℃, and then is conveyed to the carbon-containing material pressurization thermochemical reaction unit through the colloid particle feeder to carry out deep conversion.
The particle circulation factor of the multi-channel carbon-poor circulation material returning system constructed by the carbon-containing material pressurization thermochemical reaction unit, the primary multi-phase flow splitter fluidization dipleg and the carbon-poor particle sealing material returning device is regulated and controlled within 50-300.
The activating agent respectively enters a carbon-rich particle activation zone and a chemical chain initial reaction zone of the carbon-rich particle chemical chain reaction unit of the discharge lining pipeline and participates in the thermochemical chain conversion reaction of the carbon-containing material, wherein the activating agent enters the carbon-rich particle activation zoneIn agent H2O (g) partial pressure and O2Partial pressure ratio [ (PH)2O)/PO2]Not less than 1.0, H in the activator entering the chemical chain initiation reaction zone2O (g) partial pressure and O2Partial pressure ratio [ (PH)2O)/PO2]≤1.0。
The inner diameter codes of different areas of the carbon-rich particle chemical chain reaction unit are D1, D2 and D3, the height of the circulating particle strengthening transfer area at the lowest end is 0.5D 1-1.5D 1, the height of the carbon-rich particle activation area at the upper end of the circulating particle strengthening transfer area is 0.5D 1-1.5D 1, the height of the chemical chain starting reaction area at the upper end of the carbon-rich particle activation area is 0.05D 2-D2, the height of the chemical chain depth reaction area at the upper end of the chemical chain starting reaction area is 0.5D 2-
The operating temperature of the carbon-rich particle chemical chain reaction unit is 950-1200 ℃, the operating pressure is 0.5-5 MPa, and the apparent velocity of the internal mixed fluid is 0.8-5.0 m/s.
The operating temperature of the carbon-containing material pressurization thermochemical reaction unit is 500-650 ℃, the operating pressure is 0.5-5 MPa, and the apparent velocity of the internal mixed fluid is 0.8-5.0 m/s.
The operating temperature of the multiphase flow dry-method flow dividing unit is 480-630 ℃, and the operating pressure is 0.5-5 MPa.
The operating temperature of the multiphase flow quenching settler is 280-380 ℃, and the operating pressure is 0.5-5 MPa.
The multiphase flow wet-method flow divider has the operating temperature of 80-120 ℃ and the operating pressure of 0.1-0.5 MPa.
The invention adopts high-efficiency clean conversion and gradient utilization of different carbon-containing materials, can produce high-quality light oil products with high added value based on the core integrated process technology of the invention, and constructs a high-end energy chemical product synthetic chemical industry chain based on deep processing of light oil products and conversion of synthesis gas.
The novel coal, oil, chemical and electricity poly-generation mode can be constructed based on the carbon-containing material step conversion device system disclosed by the invention.
Drawings
FIG. 1 is a schematic view of the overall structure of the present invention;
FIG. 2 is a flow diagram of a pressurized thermochemical conversion system for carbonaceous materials in accordance with the invention;
FIG. 3 is a schematic diagram of a carbon-rich particle chemical looping reaction unit according to the present invention;
FIG. 4 is a schematic view of a pressurized thermochemical reaction unit for carbonaceous materials in accordance with the invention;
FIG. 5 is a schematic cross-sectional view of a drawn quench tube according to the present invention.
DETAILED DESCRIPTION OF EMBODIMENT (S) OF INVENTION
The system and method of the present invention are described in further detail below with reference to the accompanying drawings.
The system comprises a carbonaceous material preparation system, a carbonaceous material pressurization thermochemical conversion system, a carbon-rich particle chemical chain conversion system and a multiphase flow diversion system;
referring to fig. 1 and 2, the carbonaceous material preparation system comprises a carbonaceous
the multi-phase flow diversion system comprises a multi-phase flow dry diversion unit, a multi-phase flow quenching settler 60 and a multi-phase flow
the multiphase flow dry diversion unit comprises a multi-attribute particle diverter 22, a first-stage
the carbon-containing material pressurized thermochemical conversion system comprises a carbon-containing material pressurized thermochemical reaction unit 30, a carbon-containing material feeding port 301 connected with a carbon-containing material steady-state conveying feedback device 13 and a porous active particle inlet 302 connected with a porous active particle return unit 310 are respectively arranged on a mixed material reinforced transfer region 30-3 in the middle of the carbon-containing material pressurized thermochemical reaction unit 30, an outlet of a multiphase flow rectification region 30-1 at the bottom of the carbon-containing material pressurized thermochemical reaction unit 30 is connected with a heat capacity/bed density regulation and control fluidization circulation unit 27 through a refractory lining, the top of the carbon-containing material pressurized thermochemical reaction unit 30 is also connected with a first-stage multiphase flow diverter 32, and carbon-poor particles obtained by diversion of the first-stage multiphase flow diverter 32 flow downwards pass through a first-stage multiphase flow diverter fluidization leg 33, a carbon-poor particle sealing return feeder 34 and the multiphase flow temperature regulation and control region 30 of the carbon-containing material 2, the high-temperature gas-solid mixed fluid output from the top of the first-stage multiphase flow splitter 32 enters a second-stage multiphase flow splitter 40 through a lining pipeline 35, carbon-rich coarse particles obtained by splitting of the second-stage multiphase flow splitter 40 descend, sequentially pass through a second-stage multiphase flow splitter fluidization leg 41 and a carbon-rich coarse particle sealing return feeder 42, and circularly return to a circulating particle reinforced transfer area 20-1 at the bottom of a carbon-rich particle chemical chain reaction unit 20 of the carbon-rich particle chemical chain conversion system, the high-temperature gas-solid mixed fluid output from the top of the second-stage multiphase flow splitter 40 enters a third-stage multiphase flow splitter 50 through a second-stage lining pipeline 43, carbon-rich fine particles obtained by splitting of the third-stage multiphase flow splitter 50 descend, sequentially enter a third-stage multiphase flow splitter fluidization leg 51 and a fluidization energy dissipater 52, and then enter a stage slurry preparation unit 53 connected, after a stable suspension is prepared, the suspension is pumped into a suspension slurry storage tank 105, the suspension slurry storage tank 105 is connected with a chemical chain initial reaction area 20-3 of a carbon-rich particle chemical chain reaction unit 20 through an active carbon-rich fine particle circulating material returning unit 210, and gas-solid mixed fluid containing ultrafine particles obtained by shunting of a three-stage multiphase flow diverter 50 is mixed with quenching medium 103 in a drawing quenching pipe 54 and then enters a multiphase flow quenching settler 60 of a multiphase flow splitting system;
the carbon-rich particle chemical chain conversion system comprises a carbon-rich particle chemical
in the multiphase flow quenching settler 60 of the multiphase flow separation system, the upper end of the multiphase flow quenching settler 60 is provided with a gas phase product outlet 106, and the lower end is respectively connected with inlets of a first cross processor 61a and a second cross processor 61b, wherein the first cross processor, the outlets of the two cross processors 61a and 61b are connected with a multiphase flow
Referring to fig. 3, the carbon-rich particle chemical-looping
Referring to fig. 4, the carbon-containing material pressurized
The porous active
Referring to fig. 5, the outlet end of the
The bottom of the multiphase flow quenching settler 60 is provided with crossed discharge ports, each discharge port is respectively connected with a first crossed processor 61a and a second crossed processor 61b through a stop valve, and the outlets of the first crossed processor 61a and the second crossed processor 61b are combined and then connected with the inlet of a light distillate oil
The splitter liner conduit 26 is connected to the secondary liner conduit 43 by a thermally coupled compensated regulator 70.
Referring to fig. 1, the self-adaptive three-cycle pressurized carbonaceous material step conversion method of the invention comprises the following steps:
a) the carbon-containing
b) the carbon-poor particles with the carbon content of 1.00 wt% -10.00 wt% obtained by the flow division of the primary
c) the carbon-rich coarse particles with the particle size range larger than or equal to 50 microns and the carbon content of 50.00-85.00 wt% captured by the second-stage
d) the carbon-rich fine particles with the particle size range of 1-50 microns captured by the third-stage
e) the gas-liquid-solid mixed fluid entering the multiphase flow quenching settler 60 is subjected to high-efficiency flow splitting, a gas phase product 106 is output from the top of the multiphase flow quenching settler 60 and enters the downstream for deep separation, the obtained liquid-solid multiphase product is divided into two downward flows into a first cross processor 61a and a second cross processor 61b and then enters a light distillate oil
f) the carbon-rich particles circularly returned to the circulating particle reinforced transfer area 20-1 at the bottom of the carbon-rich particle chemical chain reaction unit 20 by the carbon-rich coarse particle sealing return feeder 42 go upward to pass through the carbon-rich particle activation area 20-2 and then are combined with the stable suspension 105 entering the chemical chain initial reaction area 20-3 by the activated carbon-rich fine particle circulating return unit 210 in the step d), then the combined suspension goes upward in sequence to pass through the chemical chain deep reaction area 20-4 and the transition regulation area 20-5, the high-temperature gas-solid mixed fluid containing the multi-attribute particles generated after the deep chemical chain conversion enters the multi-attribute particle splitter 22 through the lining pipeline 21, the inert coarse particles obtained by splitting by the multi-attribute particle splitter 22 go downward to enter the multi-attribute particle splitter fluidization dipleg 23 and then are divided into two paths: one path is circularly returned to a circulating particle reinforced transfer area 20-1 at the bottom of the carbon-rich particle chemical chain reaction unit 20 through a porous particle sealing return feeder 24, and the other path is ascended to enter a multiphase flow rectification area 30-1 of a carbon-containing material pressurized thermochemical reaction unit 30 through a heat capacity/bed density control fluidization circulation unit 27; inert coarse particles generated by the carbon particle-rich chemical looping reaction unit 20 enter the inert particle discharging and heat energy recovery unit 80 from a bottom outlet through the discharge lining pipeline 25;
g) the high-temperature gas-solid mixed fluid obtained by the shunting of the multi-attribute particle flow divider 22 enters a multiphase flow rectification area 30-1 at the bottom end of a carbon-containing material pressurization
Wherein the carbon-containing
If the colloid particles with the solid content of 40 wt% -60 wt% obtained after the heavy components output from the bottom of the multiphase flow
The particle circulation factor of the multi-channel carbon-poor circulation material returning system constructed by the carbon-containing material pressurization
The activating agent respectively enters the
The inner diameter of different areas of the carbon-rich particle chemical
The operating temperature range of the carbon-rich particle chemical chain reaction unit (20) is 950-1200 ℃, the operating pressure is 0.5-5 MPa, and the apparent velocity of the internal mixed fluid is 0.8-5.0 m/s.
The operating temperature range of the carbon-containing material pressurization thermochemical reaction unit (30) is 500-650 ℃, the operating pressure is 0.5-5 MPa, and the apparent velocity of the internal mixed fluid is 0.8-5.0 m/s.
The operating temperature range of the multiphase flow dry-method flow dividing system is 480-630 ℃, and the operating pressure range is 0.5-5 MPa.
The operating temperature range of the multiphase flow quenching settler 60 is 280-380 ℃, and the operating pressure is 0.5-5 MPa.
The multiphase flow wet-
The low-rank coal is converted by the self-adaptive three-cycle pressurized carbonaceous material step conversion device system and the method disclosed by the invention, and the obtained medium-low temperature coal tar is subjected to dust removal, dehydration, desalination and purification in the subsequent coal tar pretreatment process in sequence and then enters a fractionation and cutting system to cut the purified coal tar into light distillate, medium distillate and heavy distillate; and (3) the distillate oil with different distillation ranges enters a subsequent distillate oil deep conversion device system to be finally converted into a clean fuel oil product with high added value, wherein the light distillate oil is extracted to obtain a phenol product, the dephenolized oil and the middle distillate oil enter a fixed bed hydrogenation unit together, the heavy distillate oil enters a suspended bed hydrocracking unit to be converted, and the liquid product obtained by conversion also enters the fixed bed hydrogenation device system. Liquid products produced after the middle distillate oil and the heavy distillate oil are subjected to suspension bed hydrogenation and fixed bed hydrogenation enter a hydrogenation product separation and recovery device system, and finally, LPG, hydrogen and liquid oiling products such as naphtha, diesel oil, wax oil, kerosene, high-octane gasoline and the like can be obtained respectively. The high hydrogen-carbon ratio synthetic gas generated by the device system can be used as raw material gas of a coal-based C1 chemical industry chain for synthesizing methanol, ethanol, SNG, F-T synthesis energy products and the like, and can also be used as fuel gas for IGCC clean gas power generation.
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