阅读说明：本技术 一种馏分油回收装置及回收方法 (Distillate oil recovery device and recovery method ) 是由 刘哲 昝大鑫 吕云飞 王鑫 邓宏达 于 2020-08-03 设计创作，主要内容包括：本申请公开了一种馏分油回收装置,涉及碳物质加工技术领域。所述的馏分油回收装置包括：螺杆挤出机,螺杆挤出机具有一减压蒸发区,减压蒸发区对加氢残渣进行减压蒸馏,螺杆挤出机包括：螺杆,螺杆用于输送加氢残渣；加热夹套,加热夹套罩设在螺杆外侧,加热夹套对加氢残渣进行加热；减压管道,减压管道与减压蒸发区连接,减压管道对减压蒸发区抽气,使减压蒸发区保持负压状态；其中,物料一包括非挥发性液相产品及加氢残渣。本申请通过对物料一在螺杆挤出机中进行减压蒸馏,可以有效回收馏分油。(The application discloses distillate oil recovery unit relates to carbon material processing technology field. The distillate oil recovery device comprises: a screw extruder having a reduced pressure evaporation zone for reduced pressure distillation of hydrogenation residue, the screw extruder comprising: the screw is used for conveying hydrogenation residues; the heating jacket is covered on the outer side of the screw rod and heats the hydrogenation residue; the pressure reducing pipeline is connected with the pressure reducing evaporation area, and the pressure reducing pipeline is used for exhausting air to the pressure reducing evaporation area so that the pressure reducing evaporation area is kept in a negative pressure state; wherein, the first material comprises non-volatile liquid phase products and hydrogenation residues. This application is through carrying out the vacuum distillation to material one in screw extruder, can effectively retrieve the distillate oil.)

1. A distillate recovery apparatus, comprising:

the screw extruder is provided with a decompression evaporation area which is used for decompressing and distilling a first material, and comprises:

a screw for conveying the hydrogenation residue;

the heating jacket covers the outer side of the screw rod and heats the first material;

the pressure reducing pipeline is connected with the pressure reducing evaporation area, and the pressure reducing pipeline exhausts air from the pressure reducing evaporation area to keep the pressure reducing evaporation area in a negative pressure state;

wherein, the first material comprises a nonvolatile liquid phase product and hydrogenation residues.

2. The distillate oil recovery apparatus according to claim 1, wherein a heat transfer medium is introduced into the heating jacket, and the heat transfer medium is superheated steam or heat transfer oil.

3. The distillate oil recovery apparatus according to claim 1, wherein a first collecting pipe is provided in the reduced pressure evaporation zone for collecting volatile substances distilled from the first material.

4. A distillate oil recovery apparatus according to claim 3, wherein the collection conduit is connected to a separation tank, the top of the separation tank is connected to the pressure reduction conduit, and the bottom of the separation tank is provided with a wax oil recovery conduit.

5. A distillate recovery unit according to claim 4, characterized in that the collecting duct has a plurality of branch ducts, and a plurality of openings are correspondingly arranged above the reduced pressure evaporation zone, and a plurality of said openings are arranged side by side and connected to a plurality of said branch ducts.

6. The distillate oil recovery apparatus according to claim 1, wherein an inlet is provided at a bottom of an end of the screw extruder, and the inlet is connected to the thermal separation tank and receives the first material separated by the thermal separator.

7. The distillate recovery apparatus according to claim 1, wherein the screw extruder further comprises a low-temperature carbonization zone disposed after the vacuum distillation zone, and the low-temperature carbonization zone is mechanically sealed with the vacuum distillation zone.

8. The distillate recovery apparatus according to claim 1, wherein the screw of the screw extruder extends to the low-temperature carbonization zone, and a heating jacket is provided outside the screw extending to the low-temperature carbonization zone.

9. The distillate recovery apparatus according to claim 8, wherein a second collecting line is disposed above the low temperature carbonization zone.

10. A distillate recovery apparatus in accordance with claim 8, wherein an outlet is provided below the end of the low temperature carbonization zone.

11. A distillate oil recovery method is characterized by comprising the following steps:

and (3) carrying out reduced pressure distillation, namely carrying out reduced pressure distillation on a material I in a screw extruder, wherein the material I comprises a nonvolatile liquid phase product and hydrogenation residues, the pressure in the screw extruder is 0.01-0.6barg, and the distillation temperature is 200-400 ℃.

12. A distillate oil recovery process according to claim 11, characterized in that the pressure in the screw extruder is gradually reduced from the inlet of the first material until the first material is subjected to reduced pressure distillation.

13. A distillate recovery process according to claim 11, characterized in that the screw extruder is maintained at a constant temperature by means of a heating jacket during the vacuum distillation step.

14. A distillate oil recovery process in accordance with claim 11, characterized by that the volatile substances distilled off under reduced pressure are drawn out of the screw extruder and the residue remaining is material two.

15. The distillate recovery process according to claim 14, wherein the second material is carbonized at normal pressure and the carbonization temperature is 350-600 ℃.

Technical Field

The application relates to the technical field of carbon substance processing, in particular to a distillate oil recovery device and a recovery method.

Background

Currently, slurry bed hydrogenation is a common process for treating heavy oil, bitumen, tar, shale oil, oil sand or the like, and the hydrogenation reaction is generally carried out on the raw materials at a reaction temperature of 250-550 ℃ and a reaction pressure of 50-300 barg. Optionally, a catalyst may be added during the reaction. The hydrogenated products obtained after the reaction comprise gas-phase products, high-viscosity or solid hydrogenation residues, and low-boiling-point liquid hydrocarbon products of gasoline and medium-oil distillation range.

The existing suspension bed hydrogenation process is characterized in that hydrogenation residues are separated from gas-phase and liquid-phase products in a thermal separator, the temperature and the pressure of the thermal separator are equal to or slightly lower than the hydrogenation reaction temperature and pressure, and the generated hydrogenation residues are difficult to further treat. In addition to the solids (e.g., catalyst) and non-volatile liquids or high viscosity intermediates such as pitch, these residues also contain valuable distillates, such as wax oils, which need to be further recovered for obvious economic reasons.

In the prior art, there are many methods such as filtration, centrifugation, distillation under reduced pressure or the like for recovering these distillate oil components. The distillate recovered by these processes can be converted to economically high low boiling products by processes such as further hydrogenation. However, the wax oil recovered by filtration and/or centrifugation is costly and the equipment is complicated.

Alternatively, the valuable wax oil component can also be recovered by distilling the hydrogenation residue under reduced pressure. The oil recovered by vacuum distillation can be hydrogenated under relatively mild conditions to obtain more valuable products. However, when the hydrogenation residue is treated by using the vacuum tower, the hydrogenation residue has a high viscosity and poor fluidity, and thus it is difficult to transport the hydrogenation residue from the vacuum tower to the next treatment apparatus.

Disclosure of Invention

The application aims to provide a distillate oil recovery device and a distillate oil recovery method, and the problem that in the prior art, the mobility is poor when a vacuum tower is used for distilling hydrogenation residues is solved.

In order to achieve the above purpose, the embodiments of the present application adopt the following technical solutions: a distillate recovery apparatus comprising: a screw extruder having a reduced pressure evaporation zone for reduced pressure distillation of hydrogenation residue, the screw extruder comprising: the screw is used for conveying hydrogenation residues; the heating jacket is covered on the outer side of the screw rod and heats the hydrogenation residue; the pressure reducing pipeline is connected with the pressure reducing evaporation area, and the pressure reducing pipeline is used for exhausting air to the pressure reducing evaporation area so that the pressure reducing evaporation area is kept in a negative pressure state; wherein, the first material comprises non-volatile liquid phase products and hydrogenation residues.

In the technical scheme, the first material is subjected to reduced pressure distillation in the screw extruder, so that distillate oil can be effectively recovered. During distillation, the continuously rotating screw enables the first material to flow in the reduced pressure evaporation zone, the viscosity of the hydrogenation residue can be gradually increased along with the evaporation of the distillate oil, and the fluidity is reduced.

Further, according to the embodiment of the application, a heat conducting medium is introduced into the heating jacket, and the heat conducting medium is superheated steam or heat conducting oil.

Further, according to the embodiment of the application, a first collecting pipeline is arranged on the reduced-pressure evaporation area and used for collecting volatile substances distilled out of the first material.

Further, according to this application embodiment, wherein, collection pipe connection knockout drum, the top and the pressure reduction pipe connection of knockout drum, the knockout drum bottom is provided with the wax oil recovery pipeline.

Further, according to the embodiment of the present application, the first collecting pipe has a plurality of branch pipes, and a plurality of openings are correspondingly disposed above the reduced-pressure evaporation zone, and the plurality of openings are disposed side by side and connected to the plurality of branch pipes.

Further, according to the embodiment of the application, an inlet is arranged at the bottom of one end of the screw extruder, and the inlet is connected with the thermal separation tank and receives the first material separated by the thermal separator.

Further, according to the embodiment of the application, the screw extruder is also provided with a low-temperature carbonization zone, the low-temperature carbonization zone is arranged behind the reduced-pressure distillation zone, and the low-temperature carbonization zone and the reduced-pressure distillation zone are connected through mechanical sealing.

Further, according to the embodiment of the application, the screw of the screw extruder extends to the low-temperature carbonization zone, and the outer side of the screw extending to the low-temperature carbonization zone is provided with the heating jacket.

Further, according to the embodiment of the application, a second collecting pipeline is arranged above the low-temperature carbonization area.

Further, according to the embodiment of the application, an outlet is arranged below the tail end of the low-temperature carbonization zone.

In order to achieve the above object, the embodiment of the present application further discloses a distillate oil recovery method, comprising the following steps:

and (3) carrying out reduced pressure distillation, namely carrying out reduced pressure distillation on a material I in a screw extruder, wherein the material I comprises a nonvolatile liquid phase product and hydrogenation residues, the pressure in the screw extruder is 0.01-0.6barg, and the distillation temperature is 200-400 ℃.

Further, according to the embodiment of the present application, the pressure in the screw extruder is gradually reduced from the inlet of the first material until the first material is distilled under reduced pressure.

Further, according to the examples of the present application, wherein the reduced pressure distillation step is carried out, the temperature inside the screw extruder is kept constant by a heating jacket.

Further, according to the examples of the present application, wherein volatile substances distilled out under reduced pressure were extracted out of the screw extruder, the residue remained material two.

Further, according to the embodiment of the application, the second material is carbonized under normal pressure, and the carbonization temperature is 350-600 ℃.

Compared with the prior art, the method has the following beneficial effects: this application is through carrying out the vacuum distillation to material one in screw extruder, can effectively retrieve the distillate oil. During distillation, the continuously rotating screw enables the first material to flow in the reduced pressure evaporation zone, the viscosity of the hydrogenation residue can be gradually increased along with the evaporation of the distillate oil, and the fluidity is reduced.

Drawings

The present application is further described below with reference to the drawings and examples.

FIG. 1 is a schematic structural diagram of a distillate recovery apparatus of the present application.

In the attached drawings

1. A heat separator 2, a screw extruder 21, a reduced pressure evaporation zone

22. Low temperature carbonization zone 23, mechanical seal 24, inlet

25. Outlet 3, separating tank 4 and collecting pipeline I

5. A second collecting pipeline 6, a pressure reducing valve 7 and a first cooler

8. A second cooler 9, a pressure reducing pipeline 10 and a wax oil recovery pipeline

Detailed Description

In order to make the objects, technical solutions and advantages of the present invention clear and fully described, embodiments of the present invention are further described in detail below with reference to the accompanying drawings. It is to be understood that the specific embodiments described herein are merely illustrative of some embodiments of the invention and are not limiting of the invention, and that all other embodiments obtained by those of ordinary skill in the art without the exercise of inventive faculty are within the scope of the invention.

In the description of the present invention, it should be noted that the terms "center", "middle", "upper", "lower", "left", "right", "inner", "outer", "top", "bottom", "side", "vertical", "horizontal", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention. Furthermore, the terms "a," "an," "first," "second," "third," "fourth," "fifth," and "sixth" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

For the purposes of simplicity and explanation, the principles of the embodiments are described by referring mainly to examples. In the following description, numerous specific details are set forth in order to provide a thorough understanding of the embodiments. It will be apparent, however, to one skilled in the art that the embodiments may be practiced without these specific details. In some instances, well-known methods and structures have not been described in detail so as not to unnecessarily obscure the embodiments. In addition, all embodiments may be used in combination with each other.

Fig. 1 shows a distillate oil recovery apparatus, mainly used for recovering distillate oil from hydrogenation residue, comprising a screw extruder 2 and a pressure reducing pipeline 9, wherein the screw extruder 2 is communicated with the bottom of a hot separator 1, and the pressure reducing pipeline 9 is communicated with the screw extruder. The hot separator 1 receives the hydrogenation product from the hydrogenation reactor, which generally includes gas phase product, hydrogenation residue, and low boiling liquid hydrocarbon products of gasoline and medium oil boiling range, and the pressure and temperature of the hot separator 1 are the same as the reaction pressure and reaction temperature of the hydrogenation reaction. The hydrogenation product is separated in a hot separator 1 from the gaseous products and volatile influencing products and is discharged from the top of the hot separator 1 and may be further processed as required, the remaining material being conveyed from the bottom of the hot separator 1 to a screw extruder 2. The material comprises non-volatile liquid phase products and hydrogenation residues, for example, 80 wt% of oil, 18 wt% of residues and 2 wt% of inorganic solids, the distillation range of the oil is 300 ℃ and 510 ℃, and the boiling point of the residues is over 510 ℃ under normal pressure.

A pressure reducing valve 6 and a cooler I7 can be arranged between the screw extruder 2 and the thermal separator 1, and the material enters the screw extruder 2 after being reduced in pressure by the pressure reducing valve 6 and cooled by the cooler I7.

The screw extruder 2 has a reduced-pressure evaporation zone 21, and the reduced-pressure evaporation zone 21 is communicated with the reduced-pressure pipe 9. The vacuum device is arranged at the downstream of the pressure reducing pipeline 9, and the pressure reducing evaporation area 21 is kept in a negative pressure state through continuous air suction of the hollow device. The vacuum device is specifically a water ring vacuum pump followed by a steam jet pump, so that the pressure in the reduced-pressure evaporation zone 21 is from 0.01 to 0.6barg, preferably from 0.02 to 0.1 barg.

Specifically, the screw extruder 2 includes at least one screw, and one end of the screw is provided with a power device, which drives the screw to rotate. The outer side of the screw is sleeved with a heating jacket, and a heat-conducting medium can be introduced into the heating jacket. After the first material enters the screw extruder 2, the first material flows in the screw extruder 2 through the conveying of the rotating screw, and the first material is heated and distilled by the heat-conducting medium in the heating jacket. Wherein, the heat-conducting medium can be superheated steam, heat-conducting oil, etc.

In the technical scheme, the distillate oil can be effectively recovered by carrying out reduced pressure distillation on the first material in the screw extruder 2. During distillation, the screw which continuously rotates enables the first material to flow in the reduced pressure evaporation area 21, the viscosity of the hydrogenation residue can be gradually increased along with the evaporation of the distillate oil, and the mobility is reduced.

On this basis, a first collecting line 4 is provided above the reduced-pressure evaporation zone 21 of the screw extruder 2 for collecting the distilled volatile substances, which generally comprise fractions such as wax oil. The first collecting pipeline 4 is connected with the separating tank 3, a second cooler 8 is arranged between the first collecting pipeline 4 and the separating tank 3, and the collected volatile substances are cooled and then separated. The top of the separation tank 3 is connected with a pressure reducing pipeline 9, and the pressure reducing pipeline 9 sucks air from the separation tank 3 to maintain the negative pressure transition state of the pressure reducing evaporation area 21. The separating tank 3 is used for separating the distillate oil, discharging from a wax oil recovery pipeline 10 arranged at the bottom of the separating tank 3, and also directly returning to the inlet of the gas phase reactor for hydrogenation of the suspension bed to perform hydrogenation reaction to further generate light oil products, such as gasoline, diesel oil and the like.

Further, an inlet 24 is provided at the bottom of one end of the screw extruder 2, and the bottom of the thermal separator 1 communicates with the inlet 24. The material enters the screw extruder 2 through the inlet 24 from the bottom of the screw extruder 24. Set up like this, the feed position that can make material one is located screw extruder 2 under the liquid level, can make the feeding not influenced by the negative pressure in screw extruder 2, can not cause the feeding to contact the negative pressure environment in advance, leads to the feeding to begin the flash distillation in the pipeline. If the material is fed from the top, namely the material is directly connected with a negative pressure environment through a pipe orifice, firstly, the pressure difference is overlarge, the gas phase is flashed in advance, so that gas-liquid-solid three phases appear in a feeding pipeline, the volume flow rate of fluid is increased due to the appearance of the gas phase, and the abrasion of an equipment pipeline is greatly increased if the flow rate of the fluid is increased due to the solid contained in the fluid; secondly, unstable plug flow is easily formed, and vibration of pipelines and equipment is caused. In addition, the occurrence of negative pressure also increases the upstream valve differential pressure, and the wear on the valve element of the valve is also greatly increased.

In addition, the collecting pipe one 4 has a plurality of branch pipes, and a plurality of openings are correspondingly arranged above the reduced-pressure evaporation zone 21, and the plurality of openings are arranged side by side and connected with the plurality of branch pipes. Wherein the branch line remote from the inlet 24 is closest to the pressure relief line 9 and is most affected by the pressure relief line 9, resulting in a minimum pressure in that branch line, whereas the pressure is greatest at the branch line close to the inlet 24. With this arrangement, the pressure in the reduced-pressure evaporation zone 21 can be gradually reduced from the inlet 24 to the end of the reduced-pressure evaporation zone 21, which is advantageous in reducing the fluctuation of the feed due to the fluctuation of the front-end distillation process during the operation of the screw extruder. In particular, the pressure may be reduced from 0.6 to 0.01barg, preferably from 0.1 to 0.02 barg.

Next, the remaining material after distillation in the reduced pressure evaporation zone 21 is a second material, which generally comprises unseparated distillate, hydrogenation residue and inorganic solid components, and may comprise, for example, 32 wt% of oil component and 11 wt% of residue, and most preferably 2 wt% of inorganic solid components, based on the first material fed originally, wherein the oil component has an atmospheric boiling point of 450 ℃ to 510 ℃ and the residue has an atmospheric boiling point of over 510 ℃.

The second material may be further carbonized, so the screw extruder 2 may further have a low-temperature carbonization zone 22, and the low-temperature carbonization zone 22 is disposed after the reduced-pressure distillation zone 21 and connected to the reduced-pressure distillation zone 21 through a mechanical seal 23. The screw of the screw extruder 2 extends to the end of the low-temperature carbonization zone 22, and conveys the second material into the low-temperature carbonization zone 22. The outer side of the screw rod of the low-temperature carbonization zone 22 is also provided with a heating jacket, and the heat-conducting medium in the heating jacket can be flue gas. In the low-temperature carbonization zone 22, the second material is heated under normal pressure, and the heating temperature is gradually increased along the flowing direction of the second material, preferably gradually increased from 350 ℃ to 600 ℃.

In contrast, a second collecting pipeline 5 is arranged above the low-temperature carbonization zone 22 and is used for collecting the gas generated in the low-temperature carbonization zone 22 and recovering the distillate oil after cooling. Below the end of the low temperature carbonization zone 22, an outlet 25 is provided for discharging the remaining material out of the screw extruder 2. The remaining material is feed three, which includes coke charge product and inorganic solid components, which may include, for example, 3 wt% coke-like product and 2 wt% inorganic solid components based on the original feed of feed one.

In the low-temperature carbonization zone 22, the carbonization temperature is basically maintained at 350-500 ℃, which belongs to low-temperature carbonization. The required carbonization effect can be achieved at different carbonization temperatures, but the required carbonization (retention) time is different, and the quality of the obtained coke is different. Considering the problems of actual operation conditions, heating medium cost, high-temperature-resistant materials and the like of equipment, the carbonization is performed under the low-temperature condition, the carbonization time is relatively long, the operability is high, the economy is realized, and the cost is low.

The embodiment of the application also discloses a distillate oil recovery method, which comprises the following steps:

and (3) reduced pressure distillation, wherein the reduced pressure distillation is carried out on a first material 2 in a screw extruder, the first material comprises a nonvolatile liquid phase product and hydrogenation residues, the pressure in the screw extruder is 0.01-0.6barg, preferably 0.02-0.1barg, the distillation temperature is 200-400 ℃, and preferably 250-350 ℃.

In the technical scheme, the first material flows in the reduced-pressure evaporation area 21 through the continuously rotating screw, the viscosity of the hydrogenation residue can be gradually increased along with the evaporation of the distillate oil, the mobility is reduced, the flow of the hydrogenation residue is not influenced due to the conveying of the screw, and the problem of poor mobility when the reduced-pressure tower is used for distilling the hydrogenation residue in the prior art is solved.

In this regard, the pressure within the screw extruder is gradually reduced from the inlet 24 of the first material until the first material completes the reduced pressure distillation wherein the pressure is reduced from 0.6barg to 0.01barg, preferably from 0.1barg to 0.02 barg. By doing so, it is possible to reduce the fluctuation of the feed due to the fluctuation of the front-end distillation process when the screw extruder is operated.

Further, in conducting the reduced pressure distillation step, the inside of the screw extruder 2 is kept at a constant temperature by a heating jacket. The heat-conducting medium in the heating jacket can be superheated steam or heat-conducting oil.

In addition, volatile substances distilled out under reduced pressure are pumped out of the screw extruder, the volatile substances generally comprise fractions such as wax oil and the like, and the volatile substances can be directly returned to the inlet of the gas phase reactor for hydrogenation of the suspended bed to perform hydrogenation reaction to further generate light oil products such as gasoline, diesel oil and the like.

When the volatile substances are removed by the screw extruder, the residue is material two, and can be sent to a cooling and granulating device for solidification. This form of material is convenient to store and transport and can be used as a solid fuel or as a feedstock for a gasification process to produce synthesis gas.

Secondly, the second material can be further heated to a higher temperature, and carbonization treatment is carried out at normal pressure, wherein the carbonization temperature is preferably 350-600 ℃. The gas generated in the process can be extracted from the equipment and cooled, and then the distillate oil is recovered. The coke thus produced can ultimately be used as a fuel.

Although the illustrative embodiments of the present application have been described above to enable those skilled in the art to understand the present application, the present application is not limited to the scope of the embodiments, and various modifications within the spirit and scope of the present application defined and determined by the appended claims will be apparent to those skilled in the art from this disclosure.