CN218321242U - Residual oil hydrogenation system - Google Patents
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- CN218321242U CN218321242U CN202222617869.3U CN202222617869U CN218321242U CN 218321242 U CN218321242 U CN 218321242U CN 202222617869 U CN202222617869 U CN 202222617869U CN 218321242 U CN218321242 U CN 218321242U
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Abstract
A system for residual oil hydrogenation comprises a first heat exchanger with a first cold and hot medium channel, a second heat exchanger with a second cold and hot medium channel, a first hydrogenation reactor, a second hydrogenation reactor, a third heat exchanger with a third cold and hot medium channel and a fourth heat exchanger, wherein the inlet of the first cold medium channel is connected with a feeding pipeline; the inlet of the second cold medium channel is communicated with the outlet of the first cold medium channel; the inlet of the first hydrogenation reactor is communicated with the outlet of the second cold medium channel through a first pipeline, and a feeding heating furnace is arranged on the first pipeline; the inlet of the second hydrogenation reactor is communicated with the outlet of the first hydrogenation reactor through a second pipeline, and the outlet is communicated with the inlet of the second heat medium channel; the inlet of the third heat medium passage communicates with the outlet of the second heat medium passage, and the outlet of the third cold medium passage communicates with the second line. The method and the device can reduce the risk of scaling or coking and can also improve the temperature of the raw oil after heat exchange.
Description
Technical Field
The utility model belongs to the technical field of oil refining device and technology, concretely relates to a system for residual oil hydrogenation.
Background
Sources of resid: mainly from atmospheric and vacuum bottoms in atmospheric and vacuum units, the higher the metals, sulfur, nitrogen, etc. content in the residue, the higher its propensity and rate of coke formation during heating, as the distillation range is higher.
The existing residual oil hydrogenation process mostly adopts a fixed bed reactor or a fluidized bed reactor. The normal fixed bed reactor is mainly used for processing the residual oil in the atmospheric tower, the operation period is short, and the problems of coking or scaling can occur on a tube pass and a shell pass of a reaction charging and discharging heat exchanger; and the hydrogenation process adopting the fixed bed reactor is mostly a hydrogen mixing process in front of the furnace (namely mixing hydrogen and residual oil in front of a heating furnace), and one heating furnace is adopted for heating.
In the residual oil hydrogenation process adopting the fluidized bed reactor, because of the limitation of the process route, a process of mixing hydrogen after the furnace (namely mixing hydrogen and residual oil after the heating furnace) heated by two heating furnaces is adopted; meanwhile, the temperature of the raw oil after heat exchange is not too high, and the temperature required by the reaction is compensated mainly by the temperature of heating hydrogen; and the boiling bed reactor has no reaction product and only has hot high-pressure separation gas.
Therefore, the hydrogenation process using a fixed bed reactor or an ebullated bed reactor has respective advantages and disadvantages.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the technical problem that to prior art's current situation, provide a system for residual oil hydrogenation to when reducing scale deposit or coking risk, can also improve the temperature behind the raw oil heat transfer.
The utility model provides a technical scheme that above-mentioned technical problem adopted does: a system for hydrogenating residua, comprising:
the first heat exchanger is provided with a first heat medium channel and a first cold medium channel, and the inlet of the first cold medium channel is connected with a feed pipeline for conveying reaction feed;
the second heat exchanger is provided with a second heat medium channel and a second cold medium channel, and the inlet of the second cold medium channel is communicated with the outlet of the first cold medium channel;
the inlet of the first hydrogenation reactor is communicated with the outlet of the second cold medium channel through a first pipeline, and a feeding heating furnace is arranged on the first pipeline;
the inlet of the second hydrogenation reactor is communicated with the outlet of the first hydrogenation reactor through a second pipeline, and the outlet of the second hydrogenation reactor is communicated with the inlet of the second heat medium channel;
a third heat exchanger having a third heat medium passage and a third cooling medium passage, an inlet of the third heat medium passage being communicated with an outlet of the second heat medium passage, and an outlet of the third cooling medium passage being communicated with the second line;
a hot high-pressure separation tank, an inlet of which is communicated with an outlet of the third heat medium channel, and a hot high-pressure gas outlet at the top of which is communicated with an inlet of the first heat medium channel;
and the fourth heat exchanger is provided with a fourth heat medium channel and a fourth cold medium channel, the inlet of the fourth heat medium channel is communicated with the outlet of the first heat medium channel, the outlet of the fourth heat medium channel is connected to downstream equipment, the inlet of the fourth cold medium channel is connected with a hydrogen pipeline for conveying hydrogen, and the outlet of the fourth cold medium channel is simultaneously communicated with the inlet of the third cold medium channel and the feeding pipeline.
In order to better utilize the heat of the hot high-pressure gas, preferably, the fourth heat exchanger is a multi-stream wound tube heat exchanger having one tube pass and three shell passes, an inlet of the tube pass is an inlet of the fourth heat medium channel, an outlet of the tube pass is an outlet of the fourth heat medium channel, the three shell passes are denoted as a first shell pass, a second shell pass and a third shell pass, the first shell pass, the second shell pass and the third shell pass are sequentially arranged along the direction from the inlet of the tube pass to the outlet of the tube pass, the first shell pass is the fourth cold medium channel, the inlet of the second shell pass is connected with a low-pressure oil distribution pipeline for conveying cold low-pressure oil, the outlet of the second shell pass is used for outputting the cold low-pressure oil after heat exchange, the inlet of the third shell pass is connected with a water supply pipeline for conveying water, and the outlet of the third shell pass is used for outputting the water after heat exchange. Therefore, the hot high-pressure gas output from the hot high-pressure separation tank is sequentially subjected to heat exchange and cooling with hydrogen, cold low-pressure oil and water, and then enters downstream equipment, and the heat of the hot high-pressure gas can be fully utilized in the process. And the heated water can be used for heating in the life of residents. And the hot high-pressure gas exchanges heat with hydrogen firstly, then exchanges heat with cold low-pressure oil, and finally exchanges heat with water, and the heat exchange sequence has the following effects:
1. the temperature of the hydrogen is preferentially increased by utilizing high-temperature heat Gao Fenqi, which is beneficial to increasing the temperature of reaction feeding materials in a feeding pipeline; 2. compared with hydrogen, the temperature of cold low-temperature oil is lower, and heat exchange after the hydrogen is favorable for graded utilization of heat; 3. the outlet temperature of the water used as the refrigerant for heat recovery is determined according to the temperature of the hot high-pressure gas, and the temperature of the hot high-pressure gas can be further reduced. In conclusion, the heat exchange sequence realizes the gradual utilization of the temperature of the heat source, can effectively utilize the heat of the hot high-pressure gas to heat materials, has smaller area of heat exchange equipment, and can reduce the investment of the heat exchange equipment.
In the above solution, the water supply line may be a line for conveying low-pressure water or high-pressure water, and in order to reduce the risk of water pollution caused by medium leakage in the pipe pass and ensure normal water heating, preferably, the water supply line is a high-pressure water line for conveying high-pressure water;
the heat exchanger further comprises a fifth heat exchanger which is provided with a fifth heat medium channel and a fifth cold medium channel, wherein an inlet of the fifth heat medium channel is communicated with an outlet of the third shell side, an outlet of the fifth heat medium channel is connected to the downstream equipment, an inlet of the fifth cold medium channel is connected with a low-pressure water pipeline used for conveying low-pressure water, and an outlet of the fifth cold medium channel is used for outputting the low-pressure water after heat exchange. Therefore, the high-pressure water exchanges heat with the heat Gao Fenqi (in a high-pressure state) in the tube pass of the fourth heat exchanger, so that the pressure in the fourth heat exchanger is balanced, and the risk of water pollution caused by pressure unbalance and heat high-pressure gas leakage into water is reduced. The fifth heat exchanger can heat low-pressure water, and the heated low-pressure water can be used for household heat supply and the like; and even if high-pressure water leaks to low-pressure water in the fifth heat exchanger, the medium of the fifth heat exchanger and the medium of the fifth heat exchanger are both water, so that the problem of pollution does not exist.
Preferably, the outlet of the fifth heat medium channel is communicated with a connecting pipe on the fourth heat exchanger through a first bypass pipeline, and the connecting pipe is communicated with a part, located between the second shell side and the third shell side, of the tube side of the fourth heat exchanger. Therefore, water can be injected into the tube pass without additionally arranging a water injection pipeline, and water can dissolve partial media such as hydrogen sulfide and ammonium salt in the high-temperature gas so as to reduce the phenomenon that the partial media in the high-temperature gas corrodes the heat exchanger.
Also preferably, the high-pressure water line is communicated with a connecting pipe on the fourth heat exchanger through a second bypass line, and the connecting pipe is communicated with a part, located between the second shell side and the third shell side, of the tube side of the fourth heat exchanger.
In the above scheme, preferably, the first hydrogenation reactor is a boiling bed reactor, and the second hydrogenation reactor is four fixed bed reactors connected in series.
Preferably, the first heat exchanger, the second heat exchanger and the third heat exchanger are single-flow wound tube heat exchangers with a single tube pass and a single shell pass, a first heat medium channel of the first heat exchanger is a single tube pass, and a first cold medium channel is a single shell pass; a second heat medium channel of the second heat exchanger is a single shell pass, and a second cold medium channel of the second heat exchanger is a single tube pass; and a third heat medium channel of the third heat exchanger is a single shell pass, and a third cold medium channel of the third heat exchanger is a single tube pass.
In each of the above aspects, preferably, the downstream equipment includes an air cooler and a cold high-pressure separation tank, an inlet of the air cooler is communicated with an outlet of the fourth heat medium passage, and an outlet of the air cooler is communicated with an inlet of the cold high-pressure separation tank.
The air cooler generally divide into dry-type air cooler and wet-type air cooler according to the cooling method difference, and dry-type air cooler relies on the fan to supply air in succession and realizes the cooling, and it has resistance to reduce greatly and equipment size big, needs many parallel operation to can occupy the defect in great space, dry-type air cooler's heat transfer effect is unsatisfactory simultaneously, and energy consumptions such as metal are big, and the piping is complicated. The wet air cooler enhances heat exchange by means of spraying or atomizing of cooling liquid (generally water), the heat exchange effect of the wet air cooler is superior to that of a dry air cooler, but the pressure and the large scale borne by the wet air cooler are limited, and the wet air cooler is difficult to be applied to the high-pressure fields of hydrogenation, hydrocracking and the like; in addition, high-pressure hot high-pressure gas has certain corrosivity, and in order to prevent the corrosion of ammonium salt in the wet air cooler, a nickel-based alloy material with high price is generally adopted, so that the manufacturing cost is high. Simultaneously, wet-type air cooler is mostly the top water spray, has that the water spray is inhomogeneous, the water spray volume is big and do not realize the effective pervaporation of heat exchange tube to lead to heat exchange efficiency not high, and the water consumption is big.
Compared with the prior art, the utility model has the advantages of: through arranging the first and second hydrogenation reactors and the first, second, third and fourth heat exchangers, residual oil firstly enters the first hydrogenation reactor and then enters the second hydrogenation reactor for reaction, the first hydrogenation reactor can be a boiling bed reactor, the second hydrogenation reactor can be a fixed bed reactor, the residual oil firstly enters the first hydrogenation reactor, the catalyst is discharged, regenerated and added, the reaction activity can be maintained, the operation period is prolonged, and after part of coke-forming impurities are removed from the first hydrogenation reactor, the risk of coking of the second hydrogenation reactor can be reduced, so that the operation period of the second hydrogenation reactor can be prolonged. Meanwhile, the four heat exchangers are arranged in the application, the temperature of the raw oil can be increased, and residual oil hydrogenation can be performed only by combining one heating furnace with the four heat exchangers.
Drawings
Fig. 1 is a schematic structural diagram of a first embodiment of the present invention;
fig. 2 is a schematic structural diagram of a second embodiment of the present invention;
fig. 3 is a schematic structural diagram of a third embodiment of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the following embodiments.
The first embodiment is as follows:
as shown in fig. 1, which is a first preferred embodiment of the system for hydrogenating residual oil according to the present invention, the system includes a first heat exchanger 100, a second heat exchanger 200, a first hydrogenation reactor 300, a second hydrogenation reactor 400, a third heat exchanger 500, a hot high-pressure separation tank 600, and a fourth heat exchanger 700.
The first heat exchanger 100 is a single-flow wound tube heat exchanger, and has a first hot medium channel 110 (which is a tube side), a first cold medium channel 120 (which is a shell side), and an inlet of the first cold medium channel 120 is connected to a feed line 130 for conveying a reaction feed.
The second heat exchanger 200 is a single-flow wound tube heat exchanger, and has a second heat medium channel 210 (shell side) and a second cold medium channel 220 (tube side), and an inlet of the second cold medium channel 220 communicates with an outlet of the first cold medium channel 120.
The inlet of the first hydrogenation reactor 300 is communicated with the outlet of the second cooling medium channel 220 through a first pipeline 310, and a feeding heating furnace 320 is arranged on the first pipeline 310. In this embodiment, the first hydrogenation reactor 300 is an ebullated bed reactor.
The inlet of the second hydrogenation reactor 400 is communicated with the outlet of the first hydrogenation reactor 300 through a second pipeline phase 410, and the outlet of the second hydrogenation reactor 400 is communicated with the inlet of the second heat medium channel 210. In this embodiment, the second hydrogenation reactor 400 is four fixed bed reactors connected in series.
The third heat exchanger 500 is a single-flow-wound tube heat exchanger, and has a third heat medium path 510 (which is a shell side) and a third cooling medium path 520 (which is a tube side), an inlet of the third heat medium path 510 is communicated with an outlet of the second heat medium path 210, and an outlet of the third cooling medium path 520 is communicated with the second line.
An inlet of the hot high pressure separation tank 600 is communicated with an outlet of the third heat medium path 510, an outlet of hot high pressure separation gas at the top of the hot high pressure separation tank 600 is communicated with an inlet of the first heat medium path 110, and an outlet at the bottom of the hot high pressure separation tank 600 is connected to the downstream.
The fourth heat exchanger 700 is a single-flow-wound tube heat exchanger, and has a fourth heat medium channel 710 (for a tube side) and a fourth cold medium channel 720 (for a shell side), an inlet of the fourth heat medium channel 710 is connected to an outlet of the first heat medium channel 110, an outlet of the fourth heat medium channel 710 is connected to a downstream device, an inlet of the fourth cold medium channel 720 is connected to a hydrogen line 730 for delivering hydrogen, and an outlet of the fourth cold medium channel 720 is simultaneously connected to an inlet of the third cold medium channel 520 and the feed line 130.
In this embodiment, the downstream equipment includes an air cooler 900 and a cold high-pressure knockout drum 901, the air cooler 900 is an existing high-pressure air cooler, an inlet of the air cooler 900 is communicated with an outlet of the fourth heat medium channel 710 through a third pipeline 903, a water injection pipeline 904 is connected to the third pipeline 903, and an outlet of the air cooler 900 is communicated with an inlet of the cold high-pressure knockout drum 901.
The residue hydrogenation process of this example was as follows:
the reaction feed (the temperature is 260 ℃) mixed with the hydrogen enters the shell side of the first heat exchanger 100 to exchange heat with a tube side medium, the reaction feed (the temperature is 301 ℃) output from the shell side of the first heat exchanger 100 is input into the tube side of the second heat exchanger 200 to exchange heat with the shell side medium in the second heat exchanger 200, the reaction feed (the temperature is 364 ℃) output from the tube side of the second heat exchanger 200 is heated by a feed heating furnace 320 and then enters the first hydrogenation reactor 300 to carry out hydrogenation reaction, a section of reaction product output from the top of the first hydrogenation reactor 300 enters the second hydrogenation reactor 400 to carry out hydrogenation reaction, a section of reaction product (the temperature is 413 ℃) output from the bottom of the second hydrogenation reactor 400 is input into the shell side of the second heat exchanger 200 as the shell side medium, inputting a second-stage reaction product (with the temperature of 366 ℃) output from the shell side of the second heat exchanger 200 into the shell side of the third heat exchanger 500, exchanging heat with a tube side medium of the third heat exchanger 500, inputting a second-stage reaction product (with the temperature of 360 ℃) output from the shell side of the third heat exchanger 500 into the hot high-pressure separation tank 600 for separation, inputting separated heat Gao Fenqi (with the temperature of 360 ℃) into the tube side of the first heat exchanger 100 as the tube side medium, inputting heat Gao Fenqi (with the temperature of 280-300 ℃) output from the tube side of the first heat exchanger 100 into the tube side of the fourth heat exchanger 700, exchanging heat with the shell side medium in the fourth heat exchanger 700, and inputting heat Gao Fenqi (with the temperature of 173.7 ℃) output from the tube side of the fourth heat exchanger 700 into downstream equipment for further separation;
meanwhile, hydrogen (the temperature is 99.7 ℃) is used as a shell side medium and is input into the shell side of the fourth heat exchanger 700, the hydrogen (the temperature is 280 ℃) output from the shell side of the fourth heat exchanger 700 is divided into two paths, the first path is used as a tube side medium and is input into the tube side of the third heat exchanger 500, and the hydrogen (the temperature is 320 ℃) output from the tube side of the third heat exchanger 500 is added into a first section of reaction product; the second pass is conveyed to feed line 130.
In this embodiment, two paths for conveying hydrogen are provided with valves (not shown in the figure) to control the flow of each path of hydrogen according to actual working conditions.
Example two:
as shown in fig. 2, a second preferred embodiment of the system for hydrogenating residual oil according to the present invention is substantially the same as the first preferred embodiment, except that in the second preferred embodiment, the fourth heat exchanger 700 is a multi-stream wound tube heat exchanger having one tube pass and three shell passes, the inlet of the tube pass is the inlet of the fourth heat medium channel 710, the outlet of the tube pass is the outlet of the fourth heat medium channel 710, the three shell passes are denoted as a first shell pass 740, a second shell pass 750, and a third shell pass 760, the first shell pass 740, the second shell pass 750, and the third shell pass are sequentially arranged along the direction from the inlet of the tube pass to the outlet of the tube pass, the first shell pass 740 is the fourth cold medium channel 720, the inlet of the second shell pass 750 is connected with a low oil distribution pipeline 751 for conveying cold low oil distribution, the outlet of the second shell pass 750 is used for outputting cold low oil after heat exchange, the inlet of the third shell pass 760 is connected with a water supply pipeline 761 for conveying water, and the outlet of the third shell pass 760 is used for outputting water after heat exchange.
In this embodiment, the water supply line 761 is a high-pressure water line for conveying high-pressure water; the heat exchanger further comprises a fifth heat exchanger 800, the fifth heat exchanger 800 is a single-flow wound tube heat exchanger, and is provided with a fifth heat medium channel 810 (which is a tube side) and a fifth cold medium channel 820 (which is a shell side), an inlet of the fifth heat medium channel 810 is communicated with an outlet of the third shell side 760, an outlet of the fifth heat medium channel 810 is connected to the downstream equipment, an inlet of the fifth cold medium channel 820 is connected with a low-pressure water pipeline 821 for conveying low-pressure water, and an outlet of the fifth cold medium channel 820 is used for outputting the low-pressure water after heat exchange.
Meanwhile, the outlet of the fifth heat medium channel 810 is communicated with a connecting pipe on the fourth heat exchanger 700 through a first bypass pipeline 701, and the connecting pipe is communicated with a part, located between the second shell side and the third shell side, of the tube side of the fourth heat exchanger 700.
The residue hydrogenation process of this example is as follows:
the reaction feed (the temperature is 260 ℃) mixed with the hydrogen enters the shell side of the first heat exchanger 100 to exchange heat with a tube side medium, the reaction feed (the temperature is 301 ℃) output from the shell side of the first heat exchanger 100 is input into the tube side of the second heat exchanger 200 to exchange heat with the shell side medium in the second heat exchanger 200, the reaction feed (the temperature is 364 ℃) output from the tube side of the second heat exchanger 200 is heated by a feed heating furnace 320 and then enters the first hydrogenation reactor 300 to carry out hydrogenation reaction, a section of reaction product output from the top of the first hydrogenation reactor 300 enters the second hydrogenation reactor 400 to carry out hydrogenation reaction, a section of reaction product (the temperature is 413 ℃) output from the bottom of the second hydrogenation reactor 400 is input into the shell side of the second heat exchanger 200 as the shell side medium, inputting a second-stage reaction product (with the temperature of 366 ℃) output from the shell side of the second heat exchanger 200 into the shell side of the third heat exchanger 500, exchanging heat with a tube side medium of the third heat exchanger 500, inputting a second-stage reaction product (with the temperature of 360 ℃) output from the shell side of the third heat exchanger 500 into the hot high-pressure separation tank 600 for separation, inputting separated hot Gao Fenqi (with the temperature of 360 ℃) as a tube side medium into the tube side of the first heat exchanger 100, inputting hot Gao Fenqi (with the temperature of 280-300 ℃) output from the tube side of the first heat exchanger 100 into the tube side of the fourth heat exchanger 700, exchanging heat with the shell side medium in the fourth heat exchanger 700, and inputting hot Gao Fenqi (with the temperature of 70 ℃) output from the tube side of the fourth heat exchanger 700 into downstream equipment for further separation;
meanwhile, hydrogen (with the temperature of 99.7 ℃) is input into the first shell side 740 of the fourth heat exchanger 700 as a shell side medium, the hydrogen (with the temperature of 280 ℃) output from the first shell side 740 of the fourth heat exchanger 700 is divided into two paths, the first path is input into the tube side of the third heat exchanger 500 as a tube side medium, and the hydrogen (with the temperature of 320 ℃) output from the tube side of the third heat exchanger 500 is added into a first-stage reaction product; the second pass is conveyed to feed line 130.
Cold low-fraction oil (at 50 ℃) is input into the second shell side 750 of the fourth heat exchanger 700 as a shell side medium, and the temperature of the cold low-fraction oil output from the second shell side 750 of the fourth heat exchanger 700 is 185 ℃.
High-pressure water is input into a third shell pass 760 of the fourth heat exchanger 700 as a shell pass medium, high-pressure water output from the third shell pass 760 of the fourth heat exchanger 700 is input into a tube pass of the fifth heat exchanger 800 as a tube pass medium, low-pressure water is input into the shell pass of the fifth heat exchanger 800 as a shell pass medium to exchange heat with the high-pressure water, the low-pressure water output from the shell pass of the fifth heat exchanger 800 can be used for heating in family life, the high-pressure water output from the tube pass of the fifth heat exchanger 800 is divided into two paths, one path returns to the tube pass of the fourth heat exchanger 700 through a first bypass pipeline 701, and the other path is conveyed to downstream equipment.
Example three:
as shown in fig. 3, this embodiment is substantially the same as the second embodiment except that the second bypass line 702 is provided instead of the first bypass line 701 in the second embodiment, specifically: the high-pressure water line is communicated with a connecting pipe on the fourth heat exchanger 700 through a second bypass line 702, and the connecting pipe is communicated with a part, located between the second shell side and the third shell side, of the tube side of the fourth heat exchanger 700.
Claims (8)
1. A system for hydrogenating residua, comprising:
the first heat exchanger (100) is provided with a first heat medium channel (110) and a first cold medium channel (120), and the inlet of the first cold medium channel (120) is connected with a feed line (130) for conveying reaction feed;
a second heat exchanger (200) having a second heat medium passage (210) and a second cooling medium passage (220), wherein an inlet of the second cooling medium passage (220) communicates with an outlet of the first cooling medium passage (120);
the inlet of the first hydrogenation reactor (300) is communicated with the outlet of the second cold medium channel (220) through a first pipeline (310), and a feeding heating furnace (320) is arranged on the first pipeline (310);
a second hydrogenation reactor (400) having an inlet connected to the outlet of the first hydrogenation reactor (300) through a second line (410), and having an outlet connected to the inlet of the second heat medium passage (210);
a third heat exchanger (500) having a third heat medium path (510) and a third cooling medium path (520), an inlet of the third heat medium path (510) being communicated with an outlet of the second heat medium path (210), and an outlet of the third cooling medium path (520) being communicated with the second line (410);
a hot high-pressure separation tank (600) having an inlet connected to the outlet of the third heat medium passage (510) and a hot high-pressure gas outlet at the top connected to the inlet of the first heat medium passage (110);
and the fourth heat exchanger (700) is provided with a fourth heat medium channel (710) and a fourth cold medium channel (720), the inlet of the fourth heat medium channel (710) is communicated with the outlet of the first heat medium channel (110), the outlet of the fourth heat medium channel (710) is connected to downstream equipment, the inlet of the fourth cold medium channel (720) is connected with a hydrogen pipeline (730) used for conveying hydrogen, and the outlet of the fourth cold medium channel (720) is simultaneously communicated with the inlet of the third cold medium channel (520) and the feeding pipeline (130).
2. The system of claim 1, wherein: the fourth heat exchanger (700) is a multi-flow wound tube heat exchanger having one tube pass and three shell passes, an inlet of the tube pass is an inlet of the fourth heat medium channel (710), an outlet of the tube pass is an outlet of the fourth heat medium channel (710), the three shell passes are marked as a first shell pass (740), a second shell pass (750) and a third shell pass (760), the first shell pass (740), the second shell pass (750) and the third shell pass are sequentially arranged along a direction from the inlet of the tube pass to the outlet of the tube pass, the first shell pass (740) is the fourth cold medium channel (720), an inlet of the second shell pass (750) is connected with a low oil distribution pipe line (751) for conveying cold low oil distribution, an outlet of the second shell pass (750) is used for outputting cold low oil distribution after heat exchange, an inlet of the third shell pass (760) is connected with a water supply pipe line (761) for conveying water, and an outlet of the third shell pass (760) is used for outputting water after heat exchange.
3. The system of claim 2, wherein: the water supply line (761) is a high-pressure water line for transporting high-pressure water;
the heat exchanger further comprises a fifth heat exchanger (800) which is provided with a fifth heat medium channel (810) and a fifth cold medium channel (820), wherein an inlet of the fifth heat medium channel (810) is communicated with an outlet of the third shell pass (760), an outlet of the fifth heat medium channel (810) is connected to downstream equipment, an inlet of the fifth cold medium channel (820) is connected with a low-pressure water pipeline (821) used for conveying low-pressure water, and an outlet of the fifth cold medium channel (820) is used for outputting the low-pressure water after heat exchange.
4. The system of claim 3, wherein: the outlet of the fifth heat medium channel (810) is communicated with a connecting pipe on the fourth heat exchanger (700) through a first bypass pipeline (701), and the connecting pipe is communicated with the part, located between the second shell side and the third shell side, of the tube side of the fourth heat exchanger (700).
5. The system of claim 3, wherein: the high-pressure water pipeline is communicated with a connecting pipe on the fourth heat exchanger (700) through a second bypass pipeline (702), and the connecting pipe is communicated with a part, located between the second shell pass and the third shell pass, of the tube pass of the fourth heat exchanger (700).
6. The system of claim 1, wherein: the first hydrogenation reactor (300) is a boiling bed reactor, and the second hydrogenation reactor (400) is four fixed bed reactors connected in series.
7. The system of claim 1, wherein: the first heat exchanger (100), the second heat exchanger (200) and the third heat exchanger (500) are all single-flow wound tube type heat exchangers with a single tube pass and a single shell pass, a first heat medium channel (110) of the first heat exchanger (100) is the single tube pass, and a first cold medium channel (120) is the single shell pass; a second heat medium channel (210) of the second heat exchanger (200) is a single shell pass, and a second cold medium channel (220) of the second heat exchanger is a single tube pass; the third heat medium channel (510) of the third heat exchanger (500) is a single shell pass, and the third cold medium channel (520) is a single tube pass.
8. The system according to any one of claims 1 to 7, wherein: the downstream equipment comprises an air cooler (900) and a cold high-pressure separation tank (901), wherein the inlet of the air cooler (900) is communicated with the outlet of the fourth heat medium channel (710), and the outlet of the air cooler (900) is communicated with the inlet of the cold high-pressure separation tank (901).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222617869.3U CN218321242U (en) | 2022-09-30 | 2022-09-30 | Residual oil hydrogenation system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222617869.3U CN218321242U (en) | 2022-09-30 | 2022-09-30 | Residual oil hydrogenation system |
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| Publication Number | Publication Date |
|---|---|
| CN218321242U true CN218321242U (en) | 2023-01-17 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222617869.3U Active CN218321242U (en) | 2022-09-30 | 2022-09-30 | Residual oil hydrogenation system |
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|---|---|
| CN (1) | CN218321242U (en) |
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- 2022-09-30 CN CN202222617869.3U patent/CN218321242U/en active Active
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