CN110947280B - Impurity-containing carbon dioxide acid gas purification system and method - Google Patents
Impurity-containing carbon dioxide acid gas purification system and method Download PDFInfo
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- CN110947280B CN110947280B CN201911299087.6A CN201911299087A CN110947280B CN 110947280 B CN110947280 B CN 110947280B CN 201911299087 A CN201911299087 A CN 201911299087A CN 110947280 B CN110947280 B CN 110947280B
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 265
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 132
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 132
- 239000002253 acid Substances 0.000 title claims abstract description 94
- 239000012535 impurity Substances 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 27
- 238000000746 purification Methods 0.000 title claims abstract description 22
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000007921 spray Substances 0.000 claims abstract description 44
- 238000001179 sorption measurement Methods 0.000 claims abstract description 38
- 239000002808 molecular sieve Substances 0.000 claims abstract description 36
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000001914 filtration Methods 0.000 claims abstract description 34
- 238000010521 absorption reaction Methods 0.000 claims abstract description 32
- 238000005507 spraying Methods 0.000 claims abstract description 21
- 239000002002 slurry Substances 0.000 claims abstract description 20
- 238000002309 gasification Methods 0.000 claims abstract description 9
- 238000003756 stirring Methods 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 140
- -1 alcohol amine Chemical class 0.000 claims description 57
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 49
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 38
- 230000008929 regeneration Effects 0.000 claims description 36
- 238000011069 regeneration method Methods 0.000 claims description 36
- 239000007788 liquid Substances 0.000 claims description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 229910001868 water Inorganic materials 0.000 claims description 27
- 230000018044 dehydration Effects 0.000 claims description 19
- 238000006297 dehydration reaction Methods 0.000 claims description 19
- 238000010992 reflux Methods 0.000 claims description 19
- 230000001172 regenerating effect Effects 0.000 claims description 13
- VTVVPPOHYJJIJR-UHFFFAOYSA-N carbon dioxide;hydrate Chemical compound O.O=C=O VTVVPPOHYJJIJR-UHFFFAOYSA-N 0.000 claims description 12
- LPSWFOCTMJQJIS-UHFFFAOYSA-N sulfanium;hydroxide Chemical compound [OH-].[SH3+] LPSWFOCTMJQJIS-UHFFFAOYSA-N 0.000 claims description 12
- 238000007599 discharging Methods 0.000 claims description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 7
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims description 7
- 238000004891 communication Methods 0.000 claims description 3
- 230000005484 gravity Effects 0.000 claims description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims 1
- 230000009286 beneficial effect Effects 0.000 description 10
- 239000006096 absorbing agent Substances 0.000 description 7
- 238000006073 displacement reaction Methods 0.000 description 6
- 239000000428 dust Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000011358 absorbing material Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 239000002274 desiccant Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000003129 oil well Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7022—Aliphatic hydrocarbons
- B01D2257/7025—Methane
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/20—Capture or disposal of greenhouse gases of methane
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention relates to a carbon dioxide acid gas purification system and method containing impurities, wherein the purification system comprises a carbon dioxide acid gas absorption device, a spray stirrer, a constant pressure container and a molecular sieve adsorption and filtration device, a first input end of the carbon dioxide acid gas absorption device is connected with a carbon dioxide-containing associated gas pipeline, an output end of the carbon dioxide acid gas absorption device is connected with the spray stirrer, the absorbed carbon dioxide acid gas containing impurities is conveyed to the spray stirrer to generate hydrate slurry and methane gas, the spray stirrer is connected with the constant pressure container and conveys the hydrate slurry to the constant pressure container for gasification, and the constant pressure container is connected with the molecular sieve adsorption and filtration device and conveys gasification products to the molecular sieve adsorption and filtration device for adsorption and filtration to obtain pure carbon dioxide dry gas. The carbon dioxide acid gas containing impurities generates hydrate slurry and methane gas under the spraying and continuous stirring of the spraying stirrer, and the methane gas is directly separated out in a gas phase state, so that the purpose of separating and separating methane is achieved.
Description
Technical Field
The invention relates to the technical field of carbon dioxide purification, in particular to a CO 2 acid gas impurity purification process system and method for realizing efficient removal of H 2O、H2 S and CH 4 in a carbon dioxide flooding ground process system.
Background
The CO 2 oil displacement and geological storage technology is an effective means for improving the recovery ratio and reducing the emission of greenhouse gases in an oil field, but with the breakthrough of CO 2 in an oil well, the problems of deacidification of associated gas with high content of CO 2 and process optimization of purifying acid gas with impurity CO 2 are faced. Generally, if the alcohol amine method is adopted to remove the CO 2 acid gas in the associated gas with high content of CO 2, the main impurity contained in the CO 2 acid gas is H 2 O, and a small amount of residual CH 4, a certain amount of H 2 S and the like are also involved. Because of the need for CO 2 reinjection concentration and the need for CO 2 pipeline transportation safety, there is a need for an efficient method to achieve a CO 2 sour gas purification process containing impurities. However, the purification of carbon dioxide acid gas by conventional methods has difficulty in ensuring the removal of CH 4 while removing H 2 O and H 2 S to the allowable levels. Therefore, for a large-scale CO 2 oil displacement ground process system, the development of an efficient CO 2 acid gas impurity purification process has important theoretical and practical significance.
Disclosure of Invention
The invention aims to solve the technical problems that the prior purifying method can not remove methane in the carbon dioxide acid gas, and the prior purifying system has low efficiency and can not meet the requirement of a large-scale carbon dioxide oil displacement ground process system.
The technical scheme for solving the technical problems is as follows: the utility model provides a carbon dioxide sour gas clean system who contains impurity, includes carbon dioxide sour gas absorbing device, sprays agitator, constant voltage container and molecular sieve adsorption filtration device, carbon dioxide sour gas absorbing device's first input with contain the associated gas pipeline connection of carbon dioxide, carbon dioxide sour gas absorbing device's output with spray the agitator is connected, carries the impurity carbon dioxide sour gas that contains the absorption to spray the agitator and generates hydrate slurry and methane gas, spray the agitator with constant voltage container is connected and carries the hydrate slurry to constant voltage container gasification, constant voltage container with molecular sieve adsorption filtration device is connected and carries the gasification result to molecular sieve adsorption filtration device carries out the absorption and filters and obtains pure carbon dioxide dry gas.
The beneficial effects of the invention are as follows: the invention firstly absorbs the acid gas with high carbon dioxide content through the carbon dioxide acid gas absorbing device, the carbon dioxide acid gas with impurities enters the spraying stirrer, hydrate slurry and methane gas are generated under the spraying and continuous stirring of the spraying stirrer, and the methane gas is directly separated out in a gas phase state, so that the purpose of separating and separating methane is achieved. The purification system can realize production continuity and improve efficiency, and has important theoretical and practical significance for a large-scale carbon dioxide oil displacement ground process system.
On the basis of the technical scheme, the invention can be improved as follows.
Furthermore, the temperature of 275.15-275.20K and the pressure of 1.80-1.81 MPa are required to be met in the spray stirrer.
The beneficial effects of adopting the further scheme are as follows: under these temperature and pressure conditions, the formation of a hydrate slurry is favored.
Further, the pressure in the constant pressure container maintains normal pressure normal atmospheric temperature, constant pressure container input with the thick liquids output of spray agitator bottom communicates, constant pressure container bottom is equipped with the outlet, the top through the pipeline with molecular sieve adsorption filtration device communicates.
The beneficial effects of adopting the further scheme are as follows: the constant pressure container can ensure the decomposition of the hydrate slurry after maintaining normal pressure and normal temperature.
Further, the carbon dioxide acid gas absorbing device comprises an absorbing tower, a regenerating tower and an alcohol amine lean-rich liquid heat exchanger, wherein a first input end of the absorbing tower is connected with a carbon dioxide-containing associated gas pipeline, a purified gas discharge port is formed in the top of the absorbing tower, the bottom of the absorbing tower is communicated with the first input end of the regenerating tower through an alcohol amine lean-rich liquid heat exchanger tube pass, a second input end of the absorbing tower is communicated with the first output end of the bottom of the regenerating tower through an alcohol amine lean-rich liquid heat exchanger shell pass, and a second output end of the top of the regenerating tower is communicated with the top of the spraying stirrer.
The beneficial effects of adopting the further scheme are as follows: the absorber, the regeneration tower and the alcohol amine lean and rich liquid heat exchanger are adopted, so that the alcohol amine lean liquid and the alcohol amine rich liquid can be subjected to heat exchange, and the alcohol amine rich liquid can be regenerated and resolved to form carbon dioxide acid gas and then become the alcohol amine lean liquid for recycling.
Further, a condensate reflux separator is connected to a pipeline between the second output end of the top of the regeneration tower and the top of the spray stirrer, the condensate reflux separator is communicated with the second input end of the regeneration tower, and a condenser is arranged in the condensate reflux separator and close to the inlet of the condensate reflux separator.
The beneficial effects of adopting the further scheme are as follows: the setting of condensate reflux separator can utilize the condenser to make the vapor carried by the gas output by the second output end at the top of the regeneration tower condense into liquid reflux to the condensate reflux separator, thereby improving the regeneration efficiency and obtaining the carbon dioxide acid gas containing a small amount of impurities such as water, hydrogen sulfide, methane and the like.
Further, an alcohol amine lean and rich liquid booster pump is arranged between the alcohol amine lean and rich liquid heat exchanger and the first output end at the bottom of the regeneration tower.
The beneficial effects of adopting the further scheme are as follows: and the alcohol amine lean solution booster pump is used for boosting the alcohol amine lean solution input into the alcohol amine lean solution heat exchanger, so that subsequent heat exchange and cyclic utilization are realized.
Further, a reboiler is connected between the alcohol amine lean solution booster pump and the first output end of the bottom of the regeneration tower, and the reboiler is communicated with the regeneration tower at a position close to the first output end of the bottom of the regeneration tower.
The beneficial effects of adopting the further scheme are as follows: and the reboiler is used for further desorbing acid gas dissolved in the alcohol amine lean solution output by the first output end of the regeneration tower and then refluxing the acid gas to the bottom of the regeneration tower, so that the regeneration efficiency is improved, and the alcohol amine lean solution with the recovery absorption capacity is obtained from the first output end of the bottom of the regeneration tower.
Further, the molecular sieve adsorption filtration device comprises a dehydration adsorber, a hydrogen sulfide removal adsorber and a filter which are sequentially connected in series, and the constant pressure container is communicated with the dehydration adsorber.
The beneficial effects of adopting the further scheme are as follows: the dehydration absorber and the hydrogen sulfide removal absorber can be used for removing water and hydrogen sulfide in the carbon dioxide acid gas, and the filter can be used for filtering dust generated by molecular sieve breakage to obtain pure carbon dioxide dry gas.
Further, the dehydration adsorber adopts a 3A molecular sieve, and the hydrogen sulfide removal adsorber adopts an RK-38 molecular sieve.
The beneficial effects of adopting the further scheme are as follows: the 3A molecular sieve is adopted, and only moisture is adsorbed by utilizing the characteristic of small aperture of the 3A molecular sieve, and hydrogen sulfide and carbon dioxide are not adsorbed; RK-38 molecular sieves were used for hydrogen sulfide removal.
A method for purifying carbon dioxide acid gas containing impurities, comprising the following steps:
S1, checking that a carbon dioxide acid gas absorption device, a spray stirrer, a constant pressure container and a molecular sieve adsorption filtration device are in a normal operation state;
S2, enabling associated gas containing carbon dioxide generated from a carbon dioxide flooding wellhead to enter a carbon dioxide acid gas absorption device from the bottom and flow from bottom to top, and simultaneously discharging purified gas from the top of the carbon dioxide acid gas absorption device after alcohol amine lean solution in the carbon dioxide acid gas absorption device absorbs the carbon dioxide acid gas in a countercurrent mode, wherein alcohol amine rich solution after absorbing the acid gas is regenerated and reused, impurity-containing carbon dioxide acid gas analyzed in the regeneration process enters a spray stirrer, and impurities in the impurity-containing carbon dioxide acid gas are water, hydrogen sulfide and methane;
s3, setting the temperature of the spray stirrer to 275.16-275.20K and the pressure to 1.80-1.81 MPa, under the conditions of the temperature and the pressure, generating carbon dioxide hydrate and hydrogen sulfide hydrate under the condition of spraying and continuously stirring carbon dioxide, water and hydrogen sulfide in the carbon dioxide acid gas, discharging methane from the top of the spray stirrer in a gas phase state, and leading the carbon dioxide hydrate and the hydrogen sulfide hydrate into a constant-pressure container by gravity self-flow from the bottom of the spray stirrer;
s4, decomposing and gasifying the carbon dioxide hydrate and the hydrogen sulfide hydrate in the constant-pressure container, discharging the generated liquid water from the bottom of the constant-pressure container, and enabling the obtained gaseous carbon dioxide, water and hydrogen sulfide to enter the molecular sieve adsorption filtering device from the top of the constant-pressure container;
s5, carrying out adsorption filtration on the carbon dioxide acid gas containing water and hydrogen sulfide by the molecular sieve adsorption filtration device to obtain dry pure carbon dioxide dry gas.
The beneficial effects of the invention are as follows: according to the method, the acid gas with high carbon dioxide content can be absorbed through the carbon dioxide acid gas absorbing device, the regenerated and parsed carbon dioxide acid gas with impurities enters the spraying stirrer, hydrate slurry and methane gas are generated under the spraying and continuous stirring of the spraying stirrer, and the methane gas is directly separated out in a gas phase state, so that the purpose of separating and separating methane is achieved. The purification system can realize production continuity and improve efficiency, and has important theoretical and practical significance for a large-scale carbon dioxide oil displacement ground process system.
Drawings
FIG. 1 is a process flow diagram of the purification system of the present invention.
In the drawings, the list of components represented by the various numbers is as follows:
1. An absorption tower; 2. a regeneration tower; 3. an alcohol amine lean rich liquid heat exchanger; 4. a carbon dioxide-containing associated gas line; 5. a condensate reflux separator; 6. alcohol amine lean solution booster pump; 7. a reboiler; 8. a spray stirrer; 9. a constant pressure vessel; 10. a dehydration adsorber; 11. a hydrogen sulfide removal adsorber; 12. and (3) a filter.
Detailed Description
The principles and features of the present invention are described below with reference to the drawings, the illustrated embodiments are provided for illustration only and are not intended to limit the scope of the present invention.
Example 1
As shown in fig. 1, the carbon dioxide acid gas purification system containing impurities in this embodiment includes a carbon dioxide acid gas absorption device, a spray stirrer 8, a constant pressure container 9 and a molecular sieve adsorption filtration device, a first input end of the carbon dioxide acid gas absorption device is connected with a carbon dioxide-containing associated gas pipeline 4, an output end of the carbon dioxide acid gas absorption device is connected with the spray stirrer 8, the absorbed carbon dioxide acid gas containing impurities is conveyed to the spray stirrer 8 to generate hydrate slurry and methane gas, the spray stirrer 8 is connected with the constant pressure container 9 and conveys the hydrate slurry to the constant pressure container 9 for gasification, and the constant pressure container 9 is connected with the molecular sieve adsorption filtration device and conveys gasification products to the molecular sieve adsorption filtration device for adsorption filtration to obtain pure carbon dioxide dry gas. The carbon dioxide acid gas absorption device is used for removing acid gas in associated gas with high carbon dioxide content to obtain carbon dioxide acid gas containing water, hydrogen sulfide, methane and other impurities. In the embodiment, the impurity methane in the carbon dioxide acid gas is removed by using a spray stirrer and a constant pressure container, so that the carbon dioxide acid gas containing water and hydrogen sulfide impurities is obtained.
The embodiment is mainly used for realizing a carbon dioxide acid gas impurity purification process system for efficiently removing water, hydrogen sulfide and methane in a carbon dioxide flooding ground process system. In the embodiment, the acid gas with high carbon dioxide content is absorbed by the carbon dioxide acid gas absorbing device, the carbon dioxide acid gas with impurities enters the spraying stirrer, hydrate slurry and methane gas are generated under the spraying and continuous stirring of the spraying stirrer, and the methane gas is directly separated out in a gas phase state, so that the purpose of separating and separating methane is achieved. The purification system of the embodiment can realize continuous production and improve efficiency, and has important theoretical and practical significance for a large-scale carbon dioxide flooding ground process system.
In this embodiment, the temperature of 275.15-275.20K and the pressure of 1.80-1.81 MPa are required to be satisfied in the spray stirrer 8. Under these temperature and pressure conditions, the formation of a hydrate slurry is favored.
As shown in fig. 1, the pressure in the constant pressure container 9 in this embodiment maintains normal pressure and normal temperature, the input end of the constant pressure container 9 is communicated with the slurry output end at the bottom of the spray mixer 8, the bottom of the constant pressure container 9 is provided with a water outlet, and the top is communicated with the molecular sieve adsorption filtration device through a pipeline. The constant pressure container can ensure the decomposition of the hydrate slurry after maintaining normal pressure and normal temperature. Both the carbon dioxide hydrate and the hydrogen sulfide hydrate decompose in this apparatus, and the carbon dioxide at the gas phase outlet at the top of the apparatus will carry a portion of the water vapor and a small amount of hydrogen sulfide, which then requires molecular sieve dehydration and dehydro-sulfide treatment.
As shown in fig. 1, the carbon dioxide acid gas absorbing device in this embodiment includes an absorbing tower 1, a regenerating tower 2, an alcohol amine lean-rich liquid heat exchanger 3, a first input end of the absorbing tower 1 is connected with a carbon dioxide associated gas containing pipeline 4, a purified gas discharging port is arranged at the top of the absorbing tower 1, the bottom of the absorbing tower 1 is communicated with the first input end of the regenerating tower 2 through a tube pass of the alcohol amine lean-rich liquid heat exchanger 3, a second input end of the absorbing tower 1 is communicated with the first output end at the bottom of the regenerating tower 2 through a shell pass of the alcohol amine lean-rich liquid heat exchanger 3, and a second output end at the top of the regenerating tower 2 is communicated with the top of a spray stirrer 8. The alcohol amine lean-rich liquid heat exchanger is adopted, so that the alcohol amine lean liquid and the alcohol amine rich liquid can exchange heat, and the alcohol amine rich liquid output by the absorption tower can be recycled after the carbon dioxide acid gas is regenerated and resolved by the regeneration tower to become the alcohol amine lean liquid. Wherein the absorption tower 1 is a packed tower to ensure that the gas and the adsorbent are fully contacted. The regeneration tower 2 tower type is a plate type tower with reboiling equipment at the bottom, the plate type tower is simple in structure and high in passing efficiency, and the bottom reboiling can improve the regeneration efficiency. And a shell-and-tube heat exchanger is adopted, and the alcohol amine rich liquid passes through a tube pass so as to reduce equipment corrosion and desorption of acid gas components in the alcohol amine rich liquid.
As shown in fig. 1, a condensate reflux separator 5 is connected to a pipeline between a second output end at the top of the regeneration tower 2 and the top of the spray stirrer 8 in this embodiment, the condensate reflux separator 5 is communicated with a second input end of the regeneration tower 2, and a condenser is disposed in the condensate reflux separator 5 near the inlet thereof. The setting of the condensate reflux separator can utilize the condenser to enable the water vapor carried by the gas output by the second output end at the top of the regenerator to be condensed into liquid to flow back to the condensate reflux separator, thereby improving the regeneration efficiency and obtaining the carbon dioxide acid gas containing water, hydrogen sulfide, methane and other impurities.
As shown in fig. 1, an alcohol amine lean and rich liquid booster pump 6 is disposed between the alcohol amine lean and rich liquid heat exchanger 3 and the first output end at the bottom of the regeneration tower 2 in this embodiment. And the alcohol amine lean solution booster pump is used for boosting the alcohol amine lean solution input into the alcohol amine lean solution heat exchanger, so that subsequent heat exchange and cyclic utilization are realized.
As shown in fig. 1, a reboiler 7 is connected between the alcohol amine lean solution booster pump 6 and the first output end of the bottom of the regeneration tower 2, and the reboiler communicates with the regeneration tower 2 at a position close to the first output end of the bottom of the regeneration tower. The reboiler can ensure that the acid gas is further desorbed, so that the alcohol amine rich solution is completely regenerated into alcohol amine lean solution.
As shown in fig. 1, the molecular sieve adsorption filtration device of the present embodiment includes a dehydration adsorber 10, a hydrogen sulfide removal adsorber 11, and a filter 12 connected in series in this order, and the constant pressure vessel 9 is in communication with the dehydration adsorber 10. The dehydration absorber and the hydrogen sulfide removal absorber can be used for removing water and hydrogen sulfide in the carbon dioxide acid gas, and the filter can be used for filtering dust generated by molecular sieve breakage to obtain pure carbon dioxide dry gas. The molecular sieve dehydration process of the embodiment is set as a drying agent dehydration and hydrogen sulfide removal process, and dehydration is performed firstly and then hydrogen sulfide is removed according to the adsorption force of the surface of the adsorbent.
Wherein, the dehydration absorber 10 of the present embodiment adopts a 3A molecular sieve, and the hydrogen sulfide removal absorber 11 adopts an RK-38 molecular sieve. The 3A molecular sieve is adopted, and only moisture is adsorbed by utilizing the characteristic of small aperture of the 3A molecular sieve, and hydrogen sulfide and carbon dioxide are not adsorbed; RK-38 molecular sieves were used for hydrogen sulfide removal.
The method comprises the steps of firstly absorbing acid gas with high carbon dioxide content through an absorption tower, regenerating an absorbing material through a regeneration tower, then enabling the carbon dioxide acid gas to enter a spraying stirrer to generate carbon dioxide hydrate and hydrogen sulfide hydrate under a low-temperature high-pressure environment, introducing the carbon dioxide hydrate and hydrogen sulfide hydrate slurry into a constant-temperature container for gasification, and finally dehydrating and removing hydrogen sulfide from the mixed gas through a molecular sieve adsorption and filtration device to obtain pure carbon dioxide dry gas.
Example 2
The method for purifying carbon dioxide acid gas containing impurities in the embodiment comprises the following steps:
s1, checking that a carbon dioxide acid gas absorption device, a spray stirrer 8, a constant pressure container 9 and a molecular sieve adsorption filtration device are in a normal operation state; comprising the following steps: checking whether the absorption tower and the regeneration tower work normally; checking whether the temperature and pressure control of the spray stirrer meets the requirements; checking whether the pressure control of the constant pressure container is stable; monitoring whether the pump is operating normally; checking whether various valves of the dehydration adsorber 10, the hydrogen sulfide removal adsorber 11 and the filter are opened and closed as required, etc.; then, temperature control is performed: according to preset experimental conditions, starting a low-temperature control and constant-temperature circulator to control the temperature of the spray stirrer until the temperature is constant to a set value; setting a constant pressure container to be stable at room temperature, wherein the constant pressure container is stable at normal pressure;
S2, enabling associated gas containing carbon dioxide generated from a carbon dioxide flooding wellhead to enter an absorption tower of a carbon dioxide acid gas absorption device from the bottom and flow upwards from the bottom, enabling alcohol amine lean solution in the carbon dioxide acid gas absorption device to contact with the associated gas in a countercurrent mode, absorbing carbon dioxide acid gas, discharging purified gas from the top of the carbon dioxide acid gas absorption device, enabling alcohol amine rich solution after absorbing the acid gas to flow out of the bottom of the absorption tower, enabling the alcohol amine rich solution to pass through an alcohol amine lean-rich solution heat exchanger, enabling the alcohol amine rich solution to rise to about 82-94 ℃ and then enter the upper portion of a regeneration tower, enabling the alcohol amine rich solution to contact with high-temperature steam of a reboiler in a countercurrent mode along the regeneration tower, enabling most of acid gas to be resolved, enabling alcohol amine lean solution with absorption capacity recovered after regeneration to flow out of the bottom of the regeneration tower, enabling the alcohol amine lean solution to exchange heat with cold alcohol amine rich solution in the alcohol amine rich solution heat exchanger and be cooled, and then circulating back into the absorption tower. The gas flowing out from the top of the regeneration tower is condensed to carry liquid water through a condensate reflux separator, and then carbon dioxide acid gas containing water, hydrogen sulfide, methane and other impurities enters a spray stirrer;
S3, setting the temperature of the spray stirrer 8 to 275.15-275.20K and the pressure to 1.80-1.81 MPa, under the conditions of the temperature and the pressure, generating carbon dioxide hydrate and hydrogen sulfide hydrate under the condition of spraying and continuously stirring carbon dioxide, water and hydrogen sulfide in the carbon dioxide acid gas, discharging methane from the top of the spray stirrer 8 in a gas phase state, and leading the carbon dioxide hydrate and the hydrogen sulfide hydrate into a constant pressure container 9 by gravity flow from the bottom of the spray stirrer 8;
S4, decomposing and gasifying the carbon dioxide hydrate and the hydrogen sulfide hydrate in the constant-pressure container 9, discharging the generated liquid water from the bottom of the constant-pressure container 9 to obtain gaseous carbon dioxide, water and hydrogen sulfide, and enabling the gaseous carbon dioxide, water and hydrogen sulfide to enter a molecular sieve adsorption and filtration device from the top of the constant-pressure container 9;
S5, enabling the carbon dioxide acid gas containing water and hydrogen sulfide to flow through a dehydration adsorption tower from top to bottom for water molecule adsorption, enabling the dehydrated carbon dioxide acid gas containing hydrogen sulfide impurities to flow out of the bottom of the dehydration adsorption tower and enter the dehydrogenation adsorption tower for hydrogen sulfide adsorption, and finally removing dust through a filter to obtain dry pure carbon dioxide dry gas.
According to the impurity-containing carbon dioxide acid gas purification method, the high carbon dioxide-containing acid gas can be absorbed through the carbon dioxide acid gas absorption device, the regenerated and analyzed impurity-containing carbon dioxide acid gas enters the spraying stirrer, hydrate slurry and methane gas are generated under the spraying and continuous stirring of the spraying stirrer, the methane gas is kept in a gas phase state to be directly separated, and the purpose of separating and separating methane is achieved. The purification system can realize production continuity and improve efficiency, and has important theoretical and practical significance for a large-scale carbon dioxide oil displacement ground process system.
In the description of the present invention, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present invention and simplifying the description, and do not indicate or imply that the device or element being referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present invention.
Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first" or "a second" may explicitly or implicitly include at least one such feature. In the description of the present invention, the meaning of "plurality" means at least two, for example, two, three, etc., unless specifically defined otherwise.
In the present invention, unless explicitly specified and limited otherwise, the terms "mounted," "connected," "secured," and the like are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly, through intermediaries, or both, may be in communication with each other or in interaction with each other, unless expressly defined otherwise. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
In the present invention, unless expressly stated or limited otherwise, a first feature "up" or "down" a second feature may be the first and second features in direct contact, or the first and second features in indirect contact via an intervening medium. Moreover, a first feature being "above," "over" and "on" a second feature may be a first feature being directly above or obliquely above the second feature, or simply indicating that the first feature is level higher than the second feature. The first feature being "under", "below" and "beneath" the second feature may be the first feature being directly under or obliquely below the second feature, or simply indicating that the first feature is less level than the second feature.
In the description of the present specification, a description referring to terms "one embodiment," "some embodiments," "examples," "specific examples," or "some examples," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the present invention. In this specification, schematic representations of the above terms are not necessarily directed to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples. Furthermore, the different embodiments or examples described in this specification and the features of the different embodiments or examples may be combined and combined by those skilled in the art without contradiction.
While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention.
Claims (7)
1. The utility model provides a carbon dioxide sour gas clean system who contains impurity, its characterized in that is used for CO 2 to drive a motor vehicle ground process system, including carbon dioxide sour gas absorbing device, spray agitator, constant pressure container and molecular sieve adsorption filtration device, carbon dioxide sour gas absorbing device's first input is connected with the associated gas pipeline that contains carbon dioxide, carbon dioxide sour gas absorbing device's output is connected with spray agitator, carries the impurity carbon dioxide sour gas that absorbs to spray agitator and produces hydrate slurry and methane gas, spray agitator with constant pressure container connection and carry the hydrate slurry to constant pressure container gasification, constant pressure container with molecular sieve adsorption filtration device connects and carries gasification product to molecular sieve adsorption filtration device carries out adsorption filtration and obtains pure carbon dioxide dry gas;
the spraying stirrer needs to meet the conditions that the temperature is 275.15-275.20K and the pressure is 1.80-1.81 MPa;
The pressure in the constant pressure container maintains normal pressure and normal temperature, the input end of the constant pressure container is communicated with the slurry output end at the bottom of the spray stirrer, the bottom of the constant pressure container is provided with a water outlet, and the top of the constant pressure container is communicated with the molecular sieve adsorption and filtration device through a pipeline;
The carbon dioxide acid gas absorbing device comprises an absorbing tower, a regenerating tower and an alcohol amine lean rich liquid heat exchanger, wherein a first input end of the absorbing tower is connected with a carbon dioxide-containing associated gas pipeline, a purified gas discharge port is formed in the top of the absorbing tower, the bottom of the absorbing tower is communicated with the first input end of the regenerating tower through an alcohol amine lean rich liquid heat exchanger tube pass, a second input end of the absorbing tower is communicated with the first output end of the bottom of the regenerating tower through an alcohol amine lean rich liquid heat exchanger shell pass, and the second output end of the top of the regenerating tower is communicated with the top of the spraying stirrer.
2. The carbon dioxide and acid gas purification system containing impurities according to claim 1, wherein a condensate reflux separator is connected to a pipeline between the second output end of the top of the regeneration tower and the top of the spray stirrer, the condensate reflux separator is communicated with the second input end of the regeneration tower, and a condenser is arranged in the condensate reflux separator and near the inlet of the condensate reflux separator.
3. The impurity-containing carbon dioxide acid gas purification system according to claim 1, wherein an alcohol amine lean-rich liquid booster pump is arranged between the alcohol amine lean-rich liquid heat exchanger and the first output end of the bottom of the regeneration tower.
4. A carbon dioxide acid gas purification system containing impurities according to claim 3, wherein a reboiler is connected between said alcohol amine lean solution booster pump and said first output end of said bottom of said regenerator, said reboiler being in communication with said regenerator at a location near said first output end of said bottom of said regenerator.
5. The carbon dioxide acid gas purification system containing impurities according to claim 1, wherein the molecular sieve adsorption filtration device comprises a dehydration adsorber, a dehydro-sulfide adsorber and a filter which are sequentially connected in series, and the constant pressure vessel is communicated with the dehydration adsorber.
6. The impurity containing carbon dioxide acid gas purification system of claim 5, wherein said dehydration adsorber comprises a 3A molecular sieve and said dehydro sulfide adsorber comprises an RK-38 molecular sieve.
7. A method for purifying carbon dioxide acid gas containing impurities, which is realized by the carbon dioxide acid gas purifying system according to any one of claims 1 to 6, comprising the steps of:
S1, checking that a carbon dioxide acid gas absorption device, a spray stirrer, a constant pressure container and a molecular sieve adsorption filtration device are in a normal operation state;
S2, enabling associated gas containing carbon dioxide generated from a carbon dioxide flooding wellhead to enter a carbon dioxide acid gas absorption device from the bottom and flow from bottom to top, and simultaneously discharging purified gas from the top of the carbon dioxide acid gas absorption device after alcohol amine lean solution in the carbon dioxide acid gas absorption device absorbs the carbon dioxide acid gas in a countercurrent mode, wherein alcohol amine rich solution after absorbing the acid gas is regenerated and reused, impurity-containing carbon dioxide acid gas analyzed in the regeneration process enters a spray stirrer, and impurities in the impurity-containing carbon dioxide acid gas are water, hydrogen sulfide and methane;
S3, setting the temperature of the spray stirrer to 275.15-275.20K and the pressure to 1.80-1.81 MPa, under the conditions of the temperature and the pressure, generating carbon dioxide hydrate and hydrogen sulfide hydrate under the condition of spraying and continuously stirring carbon dioxide, water and hydrogen sulfide in the carbon dioxide acid gas, discharging methane from the top of the spray stirrer in a gas phase state, and leading the carbon dioxide hydrate and the hydrogen sulfide hydrate into a constant-pressure container by gravity self-flow from the bottom of the spray stirrer;
s4, decomposing and gasifying the carbon dioxide hydrate and the hydrogen sulfide hydrate in the constant-pressure container, discharging the generated liquid water from the bottom of the constant-pressure container, and enabling the obtained gaseous carbon dioxide, water and hydrogen sulfide to enter the molecular sieve adsorption filtering device from the top of the constant-pressure container;
s5, carrying out adsorption filtration on the carbon dioxide acid gas containing water and hydrogen sulfide by the molecular sieve adsorption filtration device to obtain dry pure carbon dioxide dry gas.
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