CN204174126U - One removes CO, CO in ethylene glycol hydrogenation circulation gas 2device - Google Patents
One removes CO, CO in ethylene glycol hydrogenation circulation gas 2device Download PDFInfo
- Publication number
- CN204174126U CN204174126U CN201420613487.6U CN201420613487U CN204174126U CN 204174126 U CN204174126 U CN 204174126U CN 201420613487 U CN201420613487 U CN 201420613487U CN 204174126 U CN204174126 U CN 204174126U
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- CN
- China
- Prior art keywords
- pipeline
- tourie
- tank
- ethylene glycol
- hydrogen compressor
- Prior art date
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- Expired - Fee Related
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Gas Separation By Absorption (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The utility model provides one and removes CO, CO in ethylene glycol hydrogenation circulation gas
2device, comprise well heater, hydrogenator, condenser, separating tank, receiving tank, hydrogen compressor, mixing tank, also comprise absorption unit, mixing tank is connected with the bottom inlet of well heater, the top exit of well heater is connected with the top entry of hydrogenator, the outlet at bottom of hydrogenator is connected with the top of condenser, the outlet at bottom of condenser is connected with receiving tank, condenser overhead is connected with separating tank entrance, the top exit of separating tank is connected with one end of hydrogen compressor, the hydrogen compressor the other end is connected with the entrance of described mixing tank, the top of absorption unit is connected with one end of hydrogen compressor, the bottom of absorption unit is connected with separating tank top exit.The utility model device, is effectively stripped of carbon monoxide obnoxious flavour in hydrogenation reaction circulation gas, ensure that the activity of catalyst for hydrogenation, improve the productive rate of ethylene glycol, reduces the separating difficulty that thick second two is refining.
Description
Technical field
The utility model relates to chemical field, especially relates to one and removes CO, CO in ethylene glycol hydrogenation circulation gas
2device.
Background technology
(chemical formula is (CH to ethylene glycol
2oH)
2) preparation be by carbonylation unit come dimethyl oxalate (chemical formula is (COOCH
3)
2) and H
2being blended in temperature is 190-210 DEG C, and under the effect of the working pressure of 3.0MPa, 215 DEG C of temperature of reaction and hydrogenation catalyst, hydrogenation reaction occurs, and reaction formula is as follows:
(COOCH
3)
2+4H
2—→(CH
2OH)
2+2CH
3OH
The process unit of the hydrogenation unit of synthetic gas preparing ethylene glycol in prior art, as shown in Figure 1, comprise well heater 1 ', hydrogenator 2 ', condenser 3 ', separating tank 4 ', receiving tank 5 ', hydrogen compressor 6 ' and mixing tank 7 ', mixing tank 7 ' by pipeline with carry out dimethyl oxalate input channel from carbonylation unit and be connected, mixing tank 7 ' outlet is connected with the bottom inlet of well heater 1 ', the top exit of well heater 1 ' is connected by pipeline with the top entry of hydrogenator 2 ', the outlet at bottom of hydrogenator 2 ' is connected with the top of condenser 3 ' by pipeline, the outlet at bottom of condenser 3 ' is connected with receiving tank 5 ' by pipeline, the outlet of receiving tank 5 ' goes refining system to be connected by pipeline with thick ethylene glycol, condenser 3 ' top is connected with separating tank 4 ' entrance by pipeline, the top exit of separating tank 4 ' is connected with one end of hydrogen compressor 6 ' by pipeline, hydrogen compressor 6 ' the other end is connected with the entrance of mixing tank 7 ' by pipeline.
Owing to containing a small amount of oxalic acid in the dimethyl oxalate that carbonylation unit comes, while hydrogenator 2 ' medium-height grass acid esters and hydrogen generation hydrogenation reaction generating glycol, also oxalic acid decomposes be can there is and carbon monoxide and carbonic acid gas side reaction generated, carbon monoxide and carbon dioxide certainly will be caused so constantly to assemble in hydrogenation circulation gas, along with constantly increasing of carbon monoxide concentration in circulation gas, the activity of hydrogenation catalyst can be made to reduce gradually, poisoning of catalyst can be caused time serious, be forced to stop and carry out the reduction of catalyzer, seriously have impact on normally carrying out of production.
Utility model content
For above-mentioned technical problem, the purpose of this utility model is to provide one and removes CO, CO in ethylene glycol hydrogenation circulation gas
2device.
The technical solution adopted in the utility model is:
One removes CO, CO in ethylene glycol hydrogenation circulation gas
2device, comprise well heater, hydrogenator, condenser, separating tank, receiving tank, hydrogen compressor, mixing tank, also comprise absorption unit, described mixing tank by pipeline with carry out dimethyl oxalate input channel from carbonylation unit and be connected, the outlet of described mixing tank is connected with the bottom inlet of described well heater, the top exit of described well heater is connected by pipeline with the top entry of described hydrogenator, the outlet at bottom of described hydrogenator is connected by the top of pipeline with described condenser, the outlet at bottom of described condenser is connected with described receiving tank by pipeline, the outlet of described receiving tank goes refining system to be connected by pipeline with thick ethylene glycol, the top of described condenser is connected with described separating tank entrance by pipeline, the top exit of described separating tank is connected by pipeline one end with described hydrogen compressor, the described hydrogen compressor the other end is connected by the entrance of pipeline with described mixing tank, described absorption unit top is connected by pipeline one end with described hydrogen compressor, the bottom of described absorption unit is connected by the top exit of pipeline with described separating tank, the two ends of described absorption unit respectively by pipeline and hot nitrogen with go CO separation system and be connected, molecular sieve is provided with in described absorption unit.
Described in the utility modelly remove CO, CO in ethylene glycol hydrogenation circulation gas
2device, wherein, described absorption unit is tourie one and tourie two, described tourie one and tourie two being connected with is put, described tourie one is connected with one end of hydrogen compressor by pipeline with the top of tourie two, and described tourie one is connected with separating tank by pipeline with the bottom of tourie two; The top of described tourie one and tourie two is by pipeline and hot nitrogen feed system, and described tourie one is connected with going CO separation system by pipeline with the bottom of tourie two.
Described in the utility modelly remove CO, CO in ethylene glycol hydrogenation circulation gas
2device, wherein, in described tourie one and tourie two, be respectively equipped with 13X molecular sieve or 5A molecular sieve.
The utility model beneficial effect:
What the utility model provided removes CO, CO in ethylene glycol hydrogenation circulation gas
2device, effectively be stripped of the carbon monoxide obnoxious flavour causing poisoning of catalyst in hydrogenation reaction circulation gas, ensure that the activity of catalyst for hydrogenation, decrease the generation of side reaction, improve the productive rate of ethylene glycol, reduce the separating difficulty that thick second two is refining, also extend the work-ing life of catalyzer in addition, guarantee the long period safe operation of producing simultaneously.
Accompanying drawing explanation
Fig. 1 is the structural representation of the device of the hydrogenation unit of synthetic gas preparing ethylene glycol in prior art;
Fig. 2 is that the utility model removes CO, CO in ethylene glycol hydrogenation circulation gas
2the structural representation of device.
In figure: 1, well heater; 2, hydrogenator; 3, condenser; 4, separating tank; 5, receiving tank; 6, hydrogen compressor; 7, mixing tank; 8, tourie one; 9, tourie two.
Below with reference to drawings and Examples, the utility model is described in detail.
Embodiment
Embodiment 1
As shown in Figure 2, one removes CO, CO in ethylene glycol hydrogenation circulation gas
2device, comprise well heater 1, hydrogenator 2, condenser 3, separating tank 4, receiving tank 5, hydrogen compressor 6, mixing tank 7, also comprise absorption unit, mixing tank 7 by pipeline with carry out dimethyl oxalate input channel from carbonylation unit and be connected, the outlet of mixing tank 7 is connected with the bottom inlet of well heater 1, the top exit of well heater 1 is connected by pipeline with the top entry of hydrogenator 2, the outlet at bottom of hydrogenator 2 is connected by the top of pipeline with condenser 3, the outlet at bottom of condenser 3 is connected with receiving tank 5 by pipeline, the outlet of receiving tank 5 goes refining system to be connected by pipeline with thick ethylene glycol, the top of condenser 3 is connected with separating tank 4 entrance by pipeline, the top exit of separating tank 4 is connected by pipeline one end with hydrogen compressor 6, hydrogen compressor 6 the other end is connected by the entrance of pipeline with mixing tank 7, the top of absorption unit is connected by pipeline one end with hydrogen compressor 6, the bottom of absorption unit is connected by the top exit of pipeline with separating tank 4, the two ends of absorption unit respectively by pipeline and hot nitrogen with go CO separation system and be connected, absorption unit is tourie 1 and tourie 29, tourie 1 and tourie 29 being connected with is put, tourie 1 is connected by pipeline one end with hydrogen compressor 6 with the top of tourie 29, tourie 1 is connected with separating tank 4 by pipeline with the bottom of tourie 29, the top of tourie 1 and tourie 29 is by pipeline and hot nitrogen feed system, and tourie 1 is connected with going CO separation system by pipeline with the bottom of tourie 29, 13X molecular sieve is respectively equipped with in tourie 1 and tourie 29.
Adopt technical scheme provided by the utility model, circulation gas after hydrogenation reaction is caused in newly-increased gas absorbing device, after utilizing the molecular sieve be equipped with in absorption unit to carry out adsorbing and removing to the carbon monoxide in circulation gas and carbon dioxide, be back to the recycle that system is carried out in hydrogen compressor import again, the hot nitrogen out-of-bounds come is utilized to purge absorption unit, resolve, alternate run, the carbon monoxide parsed, carbonic acid gas deliver to carbon monoxide separation system.
Absorption unit is tourie 1 and tourie 29, tourie 1 and tourie 29 being connected with is put, tourie 1 is connected by pipeline one end with hydrogen compressor 6 with the top of tourie 29, adsorption tanks 1 and adsorption tanks 29 hocket use, tourie 1 is when adsorbing, tourie 29 is exactly regeneration, utilizes hot nitrogen to purge, makes to adsorb saturated CO and CO in molecular sieve
2therefrom desorption out, carries out recycle like this; The aperture 10A of 13X type molecular sieve, absorption is less than any molecule of 10A, can be used for CO absorption and CO
2gas.
Embodiment 2
Be with the difference of embodiment 1: be respectively equipped with 5A molecular sieve in tourie 1 and tourie 29, the adsorbable any molecule being less than this aperture of 5A molecular sieve, can be applicable to CO absorption and CO
2gas.
Above-described embodiment is only be described preferred implementation of the present utility model; not scope of the present utility model is limited; under the prerequisite not departing from the utility model design spirit; the various distortion that those of ordinary skill in the art make the technical solution of the utility model and improvement, all should fall in protection domain that the utility model claims determine.
Claims (3)
1. one kind removes CO, CO in ethylene glycol hydrogenation circulation gas
2device, comprise well heater (1), hydrogenator (2), condenser (3), separating tank (4), receiving tank (5), hydrogen compressor (6), mixing tank (7), it is characterized in that: also comprise absorption unit, described mixing tank (7) by pipeline with carry out dimethyl oxalate input channel from carbonylation unit and be connected, the outlet of described mixing tank (7) is connected with the bottom inlet of described well heater (1), the top exit of described well heater (1) is connected by pipeline with the top entry of described hydrogenator (2), the outlet at bottom of described hydrogenator (2) is connected by the top of pipeline with described condenser (3), the outlet at bottom of described condenser (3) is connected with described receiving tank (5) by pipeline, the outlet of described receiving tank (5) goes refining system to be connected by pipeline with thick ethylene glycol, the top of described condenser (3) is connected with described separating tank (4) entrance by pipeline, described separating tank (4) top exit is connected by pipeline one end with described hydrogen compressor (6), described hydrogen compressor (6) the other end is connected by the entrance of pipeline with described mixing tank (7), the top of described absorption unit is connected by pipeline one end with described hydrogen compressor (6), the bottom of described absorption unit is connected with described separating tank (4) top exit by pipeline, the two ends of described absorption unit respectively by pipeline and hot nitrogen with go CO separation system and be connected, molecular sieve is provided with in described absorption unit.
2. according to claim 1ly remove CO, CO in ethylene glycol hydrogenation circulation gas
2device, it is characterized in that: described absorption unit is tourie one (8) and tourie two (9), described tourie one (8) and tourie two (9) being connected with is put, described tourie one (8) is connected by pipeline one end with hydrogen compressor (6) with the top of tourie two (9), and described tourie one (8) is connected with separating tank (4) by pipeline with the bottom of tourie two (9); The top of described tourie one (8) and tourie two (9) is by pipeline and hot nitrogen feed system, and described tourie one (8) is connected with going CO separation system by pipeline with the bottom of tourie two (9).
3. according to claim 1 and 2ly remove CO, CO in ethylene glycol hydrogenation circulation gas
2device, it is characterized in that: in described tourie one (8) and tourie two (9), be respectively equipped with 13X molecular sieve or 5A molecular sieve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420613487.6U CN204174126U (en) | 2014-10-22 | 2014-10-22 | One removes CO, CO in ethylene glycol hydrogenation circulation gas 2device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420613487.6U CN204174126U (en) | 2014-10-22 | 2014-10-22 | One removes CO, CO in ethylene glycol hydrogenation circulation gas 2device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204174126U true CN204174126U (en) | 2015-02-25 |
Family
ID=52562953
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420613487.6U Expired - Fee Related CN204174126U (en) | 2014-10-22 | 2014-10-22 | One removes CO, CO in ethylene glycol hydrogenation circulation gas 2device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204174126U (en) |
-
2014
- 2014-10-22 CN CN201420613487.6U patent/CN204174126U/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150225 Termination date: 20161022 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |