CN218494769U - Analytic gas and flash distillation gas communication recovery system - Google Patents
Analytic gas and flash distillation gas communication recovery system Download PDFInfo
- Publication number
- CN218494769U CN218494769U CN202222604492.8U CN202222604492U CN218494769U CN 218494769 U CN218494769 U CN 218494769U CN 202222604492 U CN202222604492 U CN 202222604492U CN 218494769 U CN218494769 U CN 218494769U
- Authority
- CN
- China
- Prior art keywords
- gas
- pipeline
- flash
- recovery
- communicated
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model discloses a desorption gas and flash evaporation gas intercommunication recovery system, including cryrogenic separation system, PSA hydrogen manufacturing system, hydrogenation compressor, carbonylation reactor, desorption gas compressor, flash evaporation gas compressor, decarbonization system, decarbonization pipeline, cryrogenic separation pipeline, hydrogen manufacturing pipeline, desorption gas recovery pipeline, flash evaporation gas recovery pipeline; the first gas outlet of the PSA hydrogen production system is communicated with the gas inlet of the desorption gas compressor through a desorption gas pipeline; the gas outlet of the desorption gas compressor is communicated with the second gas inlet of the cryogenic separation system through a desorption gas recovery pipeline; the second gas outlet of the cryogenic separation is communicated with a gas inlet of a flash gas compressor through a flash gas pipeline; the gas outlet of the flash evaporation gas compressor is connected into a decarburization pipeline through a flash evaporation gas recovery pipeline; the flash evaporation gas pipeline is communicated with the analysis gas recovery pipeline through a partial pressure pipeline; the pressure division pipeline is provided with an adjusting valve.
Description
Technical Field
The utility model relates to an ethylene glycol preparation system technical field, concretely relates to analytic gas and flash distillation gas intercommunication recovery system.
Background
Ethylene glycol is a strategic and large-scale chemical basic raw material and is mainly used for producing polyethylene terephthalate, unsaturated polyester resin, an antifreezing agent and the like.
The prior ethylene glycol production has two modes, one is that petroleum is used as a raw material, ethylene oxide is obtained by catalysis of ethylene, and ethylene glycol is synthesized by hydration of the ethylene oxide. Secondly, the dimethyl oxalate is prepared by taking coal-based synthesis gas as a raw material through an oxidative coupling reaction, and then the ethylene glycol is synthesized. Because of the contradiction between the supply and demand of petroleum in China, the preparation of the ethylene glycol is mostly carried out by adopting a second mode; when the ethylene glycol is prepared by the second mode, cryogenic separation needs to be carried out under low temperature, and hydrogen provided by a PSA (pressure swing adsorption) hydrogen production system is utilized to react with dimethyl oxalate formed after carbon monoxide compression to finally generate the ethylene glycol.
In the PSA purification production process of the existing preparation process, the gas components coming out of the desorption gas are carbon monoxide and hydrogen, and the desorption gas compressor is used for returning the desorption gas in the PSA to the cryogenic separation system by utilizing the desorption gas channel. In the production process, because the pressure difference of the analysis gas channel is high, when the pressure of an outlet is adjusted, part of analysis gas needs to be discharged to a torch; the adjustment mode can ensure that the recovery rate of the desorption gas is low, the desorption gas is wasted seriously, and the cost of cryogenic separation and PSA purification is increased.
The utility model has the following contents:
according to prior art not enough, the utility model provides a gas analysis and flash distillation gas intercommunication recovery system fully retrieves gas analysis and flash distillation gas through this system to bring the intra-system into and circulate, reduced the consumption to the feed gas.
In order to achieve the above purpose, the utility model discloses a following technical scheme realizes:
a recovery system for communicating analysis gas with flash gas comprises a cryogenic separation system, a PSA hydrogen production system, a hydrogenation compressor, a carbonylation reactor, an analysis gas compressor, a flash gas compressor, a decarburization system, a decarburization pipeline, a cryogenic separation pipeline, a hydrogen production pipeline, an analysis gas recovery pipeline, a flash gas pipeline and a flash gas recovery pipeline;
the gas inlet of the decarburization system is connected with a decarburization pipeline, and raw gas is introduced into the decarburization system through the decarburization pipeline; the gas outlet of the decarburization system is connected to a first gas inlet of the cryogenic separation system through a cryogenic separation pipeline; the first gas outlet of the cryogenic separation system is communicated with the gas inlet of the PSA hydrogen production system through a hydrogen production pipeline; the first gas outlet of the PSA hydrogen production system is communicated with the gas inlet of the desorption gas compressor through a desorption gas pipeline; the gas outlet of the desorption gas compressor is communicated with the second gas inlet of the cryogenic separation system through a desorption gas recovery pipeline;
the second gas outlet of the cryogenic separation is communicated with a gas inlet of a flash gas compressor through a flash gas pipeline; the gas outlet of the flash evaporation gas compressor is connected into a decarburization pipeline through a flash evaporation gas recovery pipeline; the flash evaporation gas pipeline is communicated with the analysis gas recovery pipeline through a partial pressure pipeline; the pressure division pipeline is provided with an adjusting valve.
Preferably, the third gas outlet of the cryogenic separation system is communicated with the gas inlet of the carbonylation reactor through a gas discharge pipeline; and a second gas outlet of the PSA hydrogen production system is communicated with a gas inlet of the hydrogenation compressor through a hydrogen discharge pipeline.
Preferably, the analysis gas recovery pipeline is communicated with a first flare pipeline, and the flare pipeline is provided with a regulating valve.
Preferably, a second flare pipeline is communicated with the flash gas recovery pipeline and is connected with the first flare pipeline in series; and the second flare pipeline is provided with a regulating valve.
Preferably, the flash evaporation gas pipeline, the analysis gas recovery pipeline and the flash evaporation gas recovery pipeline are provided with regulating valves.
The utility model provides a solution gas and flash distillation gas intercommunication recovery system the utility model discloses beneficial effect has following several:
1. when the system is used for recovering the analysis gas and the cryogenic separation treatment capacity reaches the upper limit, part of the analysis gas is mixed into the flash evaporation gas through the partial pressure pipeline and returns to the decarburization system through the flash evaporation gas pipeline again. The aim of temporarily reducing the treatment capacity of the cryogenic separation system is achieved.
2. When the system recycles the flash evaporation gas and the compressed gas, a torch pipeline is reserved, and when the flash evaporation gas and the compressed gas need to be discharged to a torch, the regulating valve can be opened for discharging.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the description below are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
Fig. 1 is a schematic diagram of the connection relationship of the pipelines of the whole equipment of the present invention.
In the figure, a cryogenic separation system 1, a PSA hydrogen production system 2, a hydrogenation compressor 3, a carbonylation reactor 4, a desorption gas compressor 5, a flash gas compressor 6, a decarbonization system 7, a decarbonization pipeline 8, a carbon discharge pipeline 9, a cryogenic separation pipeline 10, a hydrogen production pipeline 11, a hydrogen discharge pipeline 12, a desorption gas pipeline 13, a desorption gas recovery pipeline 14, a flash gas pipeline 15, a flash gas recovery pipeline 16, a first torch pipeline 17, a second torch pipeline 18 and a regulating valve 19.
The specific implementation mode is as follows:
as shown in the figure, the recovery system for communicating the desorbed gas with the flash gas mainly comprises: the system comprises a cryogenic separation system 1, a PSA hydrogen production system 2, a hydrogenation compressor 3, a carbonylation reactor 4, a desorption gas compressor 5, a flash gas compressor 6, a decarburization system 7, a decarburization pipeline 8, a cryogenic separation pipeline 10, a hydrogen production pipeline 11, a desorption gas pipeline 13, a desorption gas recovery pipeline 14, a flash gas pipeline 15 and a flash gas recovery pipeline 16; the above-mentioned lines are connected to the equipment as follows: firstly, an air inlet of a decarburization system 7 is connected with a decarburization pipeline 8, raw material gas is introduced into the decarburization system 7 through the decarburization pipeline 8, the raw material gas mainly comprises carbon monoxide and hydrogen and is doped with a small amount of carbon dioxide, after passing through the decarburization system 7, the content of the carbon dioxide can be greatly reduced, and the content of the carbon dioxide is less than or equal to 0.1ppm; the pressure value in the decarburization line 8 was 5.3mpa.
The gas outlet of the decarburization system 7 is connected to the first gas inlet of the cryogenic separation system 1 through the cryogenic separation pipeline 10, after the raw gas enters the cryogenic separation system 1, carbon monoxide is separated from hydrogen, the cryogenic separation system 1 is the existing equipment, the equipment itself is not improved, details are not provided, and the pressure value of the cryogenic separation pipeline 10 is 5.3mpa. A third gas outlet of the cryogenic separation system 1 is communicated with a gas inlet of the carbonylation reactor 4 through a carbon discharge pipeline 9; the separated carbon monoxide enters the carbonylation reactor 4 from the carbon discharge tube line 9, the carbon monoxide is compressed to synthesize dimethyl oxalate, and the pressure value of the carbon discharge tube line 9 is 0.6mpa.
The first gas outlet of the cryogenic separation system 1 is communicated with the gas inlet of the PSA hydrogen production system 2 through a hydrogen production pipeline 11; the PSA hydrogen production system 2 is an existing apparatus for purification. A first gas outlet of the PSA hydrogen production system 2 is communicated with a gas inlet of the desorption gas compressor 5 through a desorption gas pipeline 13, and the pressure value of the desorption gas pipeline 13 is 0.13mpa; the second gas outlet of the PSA hydrogen production system 2 is communicated with the gas inlet of the hydrogenation compressor 3 through a hydrogen discharge pipeline 12, and the pressure value of the hydrogen discharge pipeline 12 is 3.2mpa. The hydrogen is compressed and then mixed with dimethyl oxalate to generate ethylene glycol. The gas outlet of the desorption gas compressor 5 is communicated with the second gas inlet of the cryogenic separation system 1 through a desorption gas recovery pipeline 14, and the pressure value of the desorption gas recovery pipeline 14 is 0.63mpa.
As shown in the figure, the second gas outlet of the cryogenic separation is communicated with the gas inlet of the flash gas compressor 6 through a flash gas pipeline 15, and the pressure value of the flash gas pipeline 15 is 0.4mpa; the gas outlet of the flash evaporation gas compressor 6 is connected into the decarburization pipeline 8 through a flash evaporation gas recovery pipeline 16, and the pressure value of the flash evaporation gas recovery pipeline 16 is 6.5mpa; the flash evaporation gas pipeline 15 is communicated with the analysis gas recovery pipeline 14 through a partial pressure pipeline; the pressure-dividing pipeline is provided with a regulating valve 19. The first flare pipeline 17 is communicated with the analysis gas recovery pipeline 14, and the flare pipeline is provided with a regulating valve 19. The flash evaporation gas recovery pipeline 16 is communicated with a second flare pipeline 18, and the second flare pipeline 18 is connected with the first flare pipeline 17 in series; the second flare line 18 is provided with a regulating valve 19. The flash gas line 15, the analysis gas recovery line 14, and the flash gas recovery line 16 are provided with regulating valves 19. The above-mentioned fixing methods are all welded or screwed by means of the common technical means of those skilled in the art, if they are not separately described.
The working principle is as follows:
the raw material gas enters a decarburization system 7 through a decarburization pipeline 8 to decarbonize part of carbon dioxide, so that the content of the carbon dioxide in the raw material gas is reduced; then introducing the raw material gas subjected to decarburization treatment into a cryogenic separation system 1, separating carbon monoxide from hydrogen in the raw material gas, then introducing the carbon monoxide into a hydrogenation compressor 3 for compression treatment, and introducing the hydrogen into a PSA hydrogen production system 2 for purification; due to the limitation of purification efficiency, the desorbed gas is still remained in the PSA hydrogen production system 2, and is a part which cannot be purified; therefore, the resolved gas passes through the resolving gas compressor 5 and then is pumped into the cryogenic separation system 1 again. Similarly, the deep cooling separation system 1 also has a part of flash steam which cannot be separated, and the flash steam is recycled into the decarburization system 7 through a flash steam recycling pipeline 16; prevent flash evaporation gas and desorption gas which can not participate in separation or purification from being directly discharged into a torch to cause waste. Because the treatment capacity of the cryogenic separation system 1 is large, the flash vapor pipeline 15 and the analysis gas recovery pipeline 14 are directly connected with a partial pressure pipeline, the partial pressure pipeline can mix analysis gas into the flash vapor, the analysis gas enters the decarburization system 7 through the flash vapor pipeline 15, and the treatment capacity of the cryogenic gas system is temporarily reduced.
The above, only be the embodiment of the preferred of the present invention, but the protection scope of the present invention is not limited thereto, and any person skilled in the art is in the technical scope of the present invention, according to the technical solution of the present invention and the utility model, which are designed to be replaced or changed equally, all should be covered within the protection scope of the present invention.
Claims (5)
1. A recovery system for communicating analysis gas and flash gas comprises a cryogenic separation system, a PSA hydrogen production system, a hydrogenation compressor, a carbonylation reactor, an analysis gas compressor, a flash gas compressor, a decarburization system, a decarburization pipeline, a cryogenic separation pipeline, a hydrogen production pipeline, an analysis gas recovery pipeline, a flash gas pipeline and a flash gas recovery pipeline;
the method is characterized in that: the gas inlet of the decarburization system is connected with a decarburization pipeline, and raw gas is introduced into the decarburization system through the decarburization pipeline; the gas outlet of the decarburization system is connected to a first gas inlet of the cryogenic separation system through a cryogenic separation pipeline; the first gas outlet of the cryogenic separation system is communicated with the gas inlet of the PSA hydrogen production system through a hydrogen production pipeline; a first gas outlet of the PSA hydrogen production system is communicated with a gas inlet of a desorption gas compressor through a desorption gas pipeline; the gas outlet of the desorption gas compressor is communicated with the second gas inlet of the cryogenic separation system through a desorption gas recovery pipeline;
the second gas outlet of the cryogenic separation is communicated with a gas inlet of a flash gas compressor through a flash gas pipeline; the gas outlet of the flash evaporation gas compressor is connected into a decarburization pipeline through a flash evaporation gas recovery pipeline; the flash evaporation gas pipeline is communicated with the analysis gas recovery pipeline through a partial pressure pipeline; the pressure division pipeline is provided with an adjusting valve.
2. A system for recovery of stripping gas in communication with flash gas as claimed in claim 1, wherein: the third gas outlet of the cryogenic separation system is communicated with the gas inlet of the carbonylation reactor through a gas exhaust pipeline; and a second gas outlet of the PSA hydrogen production system is communicated with a gas inlet of the hydrogenation compressor through a hydrogen discharge pipeline.
3. A system for recovery of stripping gas in communication with flash gas as claimed in claim 1, wherein: the desorption gas recycling pipeline is communicated with a first flare pipeline, and the flare pipeline is provided with a regulating valve.
4. A system for recovery of stripping gas in communication with flash gas as claimed in claim 3, wherein: the flash evaporation gas recovery pipeline is communicated with a second flare pipeline which is connected with the first flare pipeline in series; and the second torch pipeline is provided with a regulating valve.
5. The system for recovering the desorption gas and the flash gas in a communication manner according to claim 2, which is characterized in that: and regulating valves are arranged on the flash evaporation gas pipeline, the analysis gas recovery pipeline and the flash evaporation gas recovery pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222604492.8U CN218494769U (en) | 2022-09-29 | 2022-09-29 | Analytic gas and flash distillation gas communication recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222604492.8U CN218494769U (en) | 2022-09-29 | 2022-09-29 | Analytic gas and flash distillation gas communication recovery system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN218494769U true CN218494769U (en) | 2023-02-17 |
Family
ID=85192190
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202222604492.8U Active CN218494769U (en) | 2022-09-29 | 2022-09-29 | Analytic gas and flash distillation gas communication recovery system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN218494769U (en) |
-
2022
- 2022-09-29 CN CN202222604492.8U patent/CN218494769U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN210340328U (en) | Integrated continuous oxygen and nitrogen making device | |
| CN111270036A (en) | System and process method for producing sponge iron by direct reduction of hydrogen energy | |
| CN104709877A (en) | Device and method for recovering nitrogen and hydrogen in synthetic ammonia purge gas | |
| CN206996207U (en) | The device of hydrogen is reclaimed in a kind of butanediol device hydrogenation synthesis emptying end gas from Isosorbide-5-Nitrae | |
| CN112374459B (en) | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery | |
| CN104190200B (en) | A kind of waste gas in synthesizing ammonia recycle device | |
| CN218494769U (en) | Analytic gas and flash distillation gas communication recovery system | |
| CN115970438A (en) | Method and device for producing hydrogen for fuel cell vehicle from ethylbenzene dehydrogenation tail gas | |
| CN101898069A (en) | Pressure swing adsorption pressured regeneration method for preparing methanol synthesis gas | |
| CN111422830A (en) | Sewage treatment plant biogas hydrogen production system and method | |
| CN108046986B (en) | Recycling system and recycling method for effective gas in coal-to-ethylene glycol process | |
| CN216662494U (en) | Pure hydrogen production synthetic ammonia system | |
| CN214653658U (en) | Nitrogen-rich gas recycling system of pressure swing adsorption nitrogen making machine | |
| CN112361715B (en) | Cryogenic ethylene recovery process | |
| CN212102909U (en) | System for producing sponge iron by direct reduction of hydrogen energy | |
| CN211896032U (en) | Pressure swing absorption separation system for supercritical water gasification hydrogen production gas phase product | |
| CN107311173A (en) | A kind of preparation method of high pressure vapor carbon dioxide for coal gasification unit | |
| CN203971683U (en) | A kind of waste gas in synthesizing ammonia recycle device | |
| CN109847555B (en) | Device and method for recovering multiple gases in catalytic dry gas based on hydrate method | |
| CN107118818B (en) | Process for synthesizing LNG (liquefied Natural gas) by using methanol purge gas | |
| CN1508064A (en) | Method for preparing high-purity nitrogen gas | |
| CN104357118B (en) | Method for increasing recycling rate of liquefied natural gas | |
| CN201473331U (en) | Equal high pressure liquid ammonia reclaiming system device for high pressure vent gas in synthetic ammonia section | |
| CN221822122U (en) | System for preparing methanol and acetic acid and coproducing LNG (liquefied Natural gas) by using blast furnace gas and coke oven gas | |
| CN210595253U (en) | Hydrogen recovery device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |