CN110947280A - System and method for purifying carbon dioxide acid gas containing impurities - Google Patents
System and method for purifying carbon dioxide acid gas containing impurities Download PDFInfo
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- CN110947280A CN110947280A CN201911299087.6A CN201911299087A CN110947280A CN 110947280 A CN110947280 A CN 110947280A CN 201911299087 A CN201911299087 A CN 201911299087A CN 110947280 A CN110947280 A CN 110947280A
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- carbon dioxide
- acid gas
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- hydrogen sulfide
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 269
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 141
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 134
- 239000002253 acid Substances 0.000 title claims abstract description 92
- 239000012535 impurity Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 27
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 62
- 238000010521 absorption reaction Methods 0.000 claims abstract description 50
- 238000005507 spraying Methods 0.000 claims abstract description 47
- 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
- 238000001179 sorption measurement Methods 0.000 claims abstract description 36
- 238000001914 filtration Methods 0.000 claims abstract description 28
- 238000000746 purification Methods 0.000 claims abstract description 27
- 239000002002 slurry Substances 0.000 claims abstract description 21
- 238000002309 gasification Methods 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 137
- -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 55
- 230000008929 regeneration Effects 0.000 claims description 47
- 238000011069 regeneration method Methods 0.000 claims description 47
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 229910001868 water Inorganic materials 0.000 claims description 31
- 239000007788 liquid Substances 0.000 claims description 21
- 230000018044 dehydration Effects 0.000 claims description 19
- 238000006297 dehydration reaction Methods 0.000 claims description 19
- 238000010992 reflux Methods 0.000 claims description 16
- 239000007921 spray Substances 0.000 claims description 15
- 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 8
- 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 6
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 230000009286 beneficial effect Effects 0.000 description 10
- 238000006073 displacement reaction Methods 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- 239000000428 dust Substances 0.000 description 3
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 2
- 235000011941 Tilia x europaea Nutrition 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 239000004571 lime Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 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
- 239000002274 desiccant Substances 0.000 description 1
- 238000003795 desorption Methods 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
- 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
- 238000011084 recovery Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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Classifications
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- 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
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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
- 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
Abstract
The invention relates to a purification system and a purification method for carbon dioxide acid gas containing impurities, wherein the purification system comprises a carbon dioxide acid gas absorption device, a spraying stirrer, a constant pressure container and a molecular sieve adsorption filtering device, a first input end of the carbon dioxide acid gas absorption device is connected with an associated gas pipeline containing carbon dioxide, an output end of the carbon dioxide acid gas absorption device is connected with the spraying stirrer, the absorbed carbon dioxide acid gas containing impurities is conveyed to the spraying stirrer to generate hydrate slurry and methane gas, the spraying stirrer is connected with the constant pressure container and conveys the hydrate slurry to the constant pressure container for gasification, the constant pressure container is connected with the molecular sieve adsorption filtering device and conveys a gasification product to the molecular sieve adsorption filtering device for adsorption filtering to obtain pure carbon dioxide dry gas. The carbon dioxide acid gas containing impurities is sprayed and continuously stirred by the spraying stirrer to generate hydrate slurry and methane gas, and the methane gas is directly separated out in a gas phase state, so that the aim of separating and removing the methane is fulfilled.
Description
Technical Field
The invention relates to the technical field of carbon dioxide purification, in particular to a method for realizing high-efficiency H removal in a carbon dioxide flooding ground process system2O、H2S and CH4CO of2Acid gas impurity purification process system and method.
Background
CO2Oil displacement and geological sequestration technology is an effective means for improving oil recovery rate and reducing greenhouse gas emission of oil fields, but with CO2Breakthrough in oil well and high CO content2Deacidification of associated gas and impure CO2The process optimization problem of acid gas purification. Generally speaking, if the alcohol amine method is selected to remove high CO content2CO in associated gas2Acid gas, which can cause CO2The main impurity contained in the acid gas is H2O, with a small amount of residual CH4And a certain amount ofH2S and the like. Due to CO2Demand for reinjection concentration and CO2The requirement of pipeline transportation safety is urgent to need an efficient method for realizing CO containing impurities2Acid gas purification process. However, the purification of carbon dioxide sour gas by conventional methods is difficult to ensure in the removal of H2O and H2Removing CH while allowing the content of S to be allowable4. Thus, for large scale CO2For an oil displacement ground process system, efficient CO-containing research and development2The acid gas impurity purification process has important theoretical and practical significance.
Disclosure of Invention
The invention aims to solve the technical problems that the existing purification method can not remove methane in carbon dioxide acid gas, and the existing purification 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 and filtration device, carbon dioxide sour gas absorbing device's first input and the associated gas line connection who contains carbon dioxide, carbon dioxide sour gas absorbing device's output with it connects to spray the agitator, carries the absorptive carbon dioxide sour gas that contains impurity to spray the agitator and generate hydrate slurry and methane gas, spray the agitator with the constant voltage container is connected and carries the hydrate slurry to the gasification of constant voltage container, the constant voltage container with the molecular sieve adsorption and filtration device is connected and carries the gasification result extremely the molecular sieve adsorption and filtration device carries out the adsorption and filters and obtain pure carbon dioxide dry gas.
The invention has the beneficial effects that: the invention firstly absorbs the acid gas with high carbon dioxide content by the carbon dioxide acid gas absorption 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 removed in a gas phase state, thereby achieving the purpose of separating and removing the methane. 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 further improved as follows.
Furthermore, the temperature in the spraying stirrer needs to be 275.15-275.20K, and the pressure in the spraying stirrer needs to be 1.80-1.81 MPa.
The beneficial effect of adopting the further scheme is that: under the conditions of temperature and pressure, hydrate slurry is generated.
Further, 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 of the bottom of the spraying stirrer, a water outlet is formed in the bottom of the constant pressure container, and the top of the constant pressure container is communicated with the molecular sieve adsorption and filtration device through a pipeline.
The beneficial effect of adopting the further scheme is that: the constant pressure container can maintain normal pressure and normal temperature to ensure the decomposition of hydrate slurry.
Further, carbon dioxide sour gas absorbing device includes absorption tower, regenerator, alcohol amine rich and lean liquid heat exchanger, the first input of absorption tower with contain carbon dioxide associated gas pipe connection, the absorption tower top is equipped with the purification gas discharge port, the absorption tower bottom is passed through alcohol amine rich and lean liquid heat exchanger tube side with the first input intercommunication of regenerator, the second input of absorption tower pass through alcohol amine rich and lean liquid heat exchanger shell side with the first output intercommunication in regenerator bottom, the second output at regenerator top with spray agitator top intercommunication.
The beneficial effect of adopting the further scheme is that: the absorption tower, 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 exchange heat, and the alcohol amine rich liquid can be regenerated to resolve carbon dioxide acid gas to form the alcohol amine lean liquid for recycling.
Furthermore, 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 at a position, close to an inlet, inside the condensate reflux separator.
The beneficial effect of adopting the further scheme is that: the arrangement of the condensate reflux separator can condense the water vapor carried by the gas output by the second output end at the top of the regeneration tower into liquid to reflux to the condensate reflux separator by utilizing the condenser, thereby improving the regeneration efficiency and obtaining the carbon dioxide acid gas containing a small amount of water, hydrogen sulfide, methane and other impurities.
Further, an alcohol amine barren liquor booster pump is arranged between the alcohol amine barren liquor and rich liquor heat exchanger and the first output end at the bottom of the regeneration tower.
The beneficial effect of adopting the further scheme is that: the arrangement of the alcohol amine barren liquor booster pump is used for boosting the alcohol amine barren liquor input into the alcohol amine barren liquor heat exchanger, so that subsequent heat exchange and cyclic utilization are realized.
Furthermore, a reboiler is connected between the alcohol amine barren liquor booster pump and the first output end at the bottom of the regeneration tower, and the reboiler is communicated with the regeneration tower at a position close to the first output end at the bottom of the regeneration tower.
The beneficial effect of adopting the further scheme is that: due to the arrangement of the reboiler, the acid gas dissolved in the alcohol amine barren solution output by the first output end of the regeneration tower can be further desorbed by the reboiler and then flows back to the bottom of the regeneration tower, so that the regeneration efficiency is improved, and the alcohol amine barren solution with the absorption capacity recovered is obtained from the first output end at the bottom of the regeneration tower.
Furthermore, the molecular sieve adsorption and 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 effect of adopting the further scheme is that: the water and the hydrogen sulfide in the carbon dioxide acid gas can be removed by utilizing the dehydration adsorber and the hydrogen sulfide removal adsorber, and the dust generated by the molecular sieve cracking can be filtered by utilizing the filter to obtain the 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 effect of adopting the further scheme is that: the 3A molecular sieve is adopted, and only water is adsorbed and hydrogen sulfide and carbon dioxide are not adsorbed by utilizing the characteristic of small pore diameter of the 3A molecular sieve; and adopting RK-38 molecular sieve for removing hydrogen sulfide.
A method for purifying carbon dioxide acid gas containing impurities comprises the following steps:
s1, checking that the carbon dioxide acid gas absorption device, the spraying stirrer, the constant pressure container and the molecular sieve adsorption filtering device are in normal operation state;
s2, allowing 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, allowing alcohol amine lean solution in the carbon dioxide acid gas absorption device to absorb the carbon dioxide acid gas in a countercurrent manner, discharging purified gas from the top of the carbon dioxide acid gas absorption device, regenerating alcohol amine rich solution after absorbing the acid gas and reusing the regenerated alcohol amine rich solution, allowing the carbon dioxide acid gas containing impurities resolved in the regeneration process to enter a spraying stirrer, and allowing the impurities in the carbon dioxide acid gas containing impurities to be water, hydrogen sulfide and methane;
s3, setting the temperature of the spraying stirrer to be 275.16-275.20K, setting the pressure to be 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 that carbon dioxide, water and hydrogen sulfide in carbon dioxide acid gas are sprayed and continuously stirred, discharging methane from the top of the spraying stirrer in a gas phase state, and gravity-automatically introducing the carbon dioxide hydrate and the hydrogen sulfide hydrate into a constant-pressure container from the bottom of the spraying 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 allowing the obtained gaseous carbon dioxide, water and hydrogen sulfide to enter a molecular sieve adsorption filtering device from the top of the constant pressure container;
and S5, adsorbing and filtering the carbon dioxide acid gas flow containing water and hydrogen sulfide by the molecular sieve adsorption and filtration device to obtain dry pure carbon dioxide dry gas.
The invention has the beneficial effects that: the method can absorb the acid gas with high carbon dioxide content through the carbon dioxide acid gas absorption device, and the regenerated and desorbed 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 desorbed in a gas phase state, so that the aim of separating and desorbing the methane is fulfilled. 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 components represented by the respective reference numerals are listed below:
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. an alcohol amine barren liquor booster pump; 7. a reboiler; 8. a spray agitator; 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 this invention are described below in conjunction with the following drawings, which are set forth to illustrate, but are not to be construed to limit the scope of the invention.
Example 1
As shown in fig. 1, the purification system for carbon dioxide acid gas containing impurities of this embodiment includes a carbon dioxide acid gas absorption device, a spraying stirrer 8, a constant pressure container 9 and a molecular sieve adsorption filter device, a first input end of the carbon dioxide acid gas absorption device is connected to an associated gas pipeline 4 containing carbon dioxide, an output end of the carbon dioxide acid gas absorption device is connected to the spraying stirrer 8, the absorbed carbon dioxide acid gas containing impurities is delivered to the spraying stirrer 8 to generate hydrate slurry and methane gas, the spraying stirrer 8 is connected to the constant pressure container 9 and delivers the hydrate slurry to the constant pressure container 9 for gasification, and the constant pressure container 9 is connected to the molecular sieve adsorption filter device and delivers the gasification product to the molecular sieve adsorption filter device for adsorption filtration to obtain pure carbon dioxide dry gas. The carbon dioxide acid gas absorption device of the embodiment is used for removing acid gas from associated gas with high carbon dioxide content to obtain carbon dioxide acid gas containing impurities such as water, hydrogen sulfide and methane. In the embodiment, a spraying stirrer and a constant pressure container are used for removing the impurity methane in the carbon dioxide acid gas to obtain the carbon dioxide acid gas containing water and hydrogen sulfide impurities.
The embodiment is mainly used for the carbon dioxide acid gas impurity purification process system for efficiently removing water, hydrogen sulfide and methane in the carbon dioxide flooding ground process system. According to the embodiment, the acid gas with high carbon dioxide content is firstly absorbed by the carbon dioxide acid gas absorption 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 from the gas phase state, so that the purpose of separating and separating the methane is achieved. The purification system of the embodiment 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 preferred embodiment of the present invention, the temperature in the spraying stirrer 8 is required to be 275.15-275.20K, and the pressure is required to be 1.80-1.81 MPa. Under the conditions of temperature and pressure, hydrate slurry is generated.
As shown in fig. 1, the pressure in the constant pressure container 9 of this embodiment is maintained at 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 agitator 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 maintain normal pressure and normal temperature to ensure the decomposition of hydrate slurry. Both carbon dioxide hydrate and hydrogen sulfide hydrate are decomposed in this apparatus, and carbon dioxide at the gas phase outlet at the top of the apparatus will carry a portion of water vapor and a small amount of hydrogen sulfide, which subsequently needs to be subjected to molecular sieve dehydration and hydrogen sulfide removal treatment.
As shown in fig. 1, the carbon dioxide acid gas absorption device of this embodiment includes an absorption tower 1, a regeneration tower 2, an alcohol amine lean and rich liquid heat exchanger 3, a first input end of the absorption tower 1 is connected to a carbon dioxide associated gas pipeline 4, a purified gas discharge port is disposed at the top of the absorption tower 1, a first input end of the regeneration tower 2 is communicated with the bottom of the absorption tower 1 through a tube pass of the alcohol amine lean and rich liquid heat exchanger 3, a second input end of the absorption tower 1 is communicated with a first output end of the bottom of the regeneration tower 2 through a shell pass of the alcohol amine lean and rich liquid heat exchanger 3, and a second output end of the top of the regeneration tower 2 is communicated with the top of the spray stirrer 8. The alcohol amine lean solution and the alcohol amine rich solution can exchange heat by adopting the alcohol amine lean solution heat exchanger, and the alcohol amine rich solution output by the absorption tower can be regenerated by the regeneration tower to resolve carbon dioxide acid gas to become the alcohol amine lean solution for recycling. Wherein, the absorption tower 1 is a packed tower to ensure that gas is fully contacted with the adsorbent. The tower 2 type of the regeneration tower is a plate tower with reboiling equipment at the bottom, the plate tower is simple in structure and high in efficiency, and the bottom reboiling can improve the regeneration efficiency. A shell-and-tube heat exchanger is adopted, and the alcohol amine rich solution passes through a tube pass, so that the corrosion of equipment and the desorption of acid gas components in the alcohol amine rich solution are reduced.
As shown in fig. 1, a condensate reflux separator 5 is connected to a pipeline between the second output end of 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 the second input end of the regeneration tower 2, and a condenser is disposed inside the condensate reflux separator 5 and near the inlet thereof. The setting of lime set backward flow separator, usable condenser make by the gaseous vapor condensation that carries of regenerator top second output become liquid reflux to lime set backward flow separator in, improve regeneration efficiency, obtain the carbon dioxide sour gas that contains impurity such as water, hydrogen sulfide and methane.
As shown in fig. 1, an alcohol amine lean solution booster pump 6 is disposed between the alcohol amine lean solution heat exchanger 3 and the first output end of the bottom of the regeneration tower 2. The arrangement of the alcohol amine barren liquor booster pump is used for boosting the alcohol amine barren liquor input into the alcohol amine barren liquor 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 is communicated with the regeneration tower 2 at a position close to the first output end of the bottom of the regeneration tower. The arrangement of the reboiler can ensure that the acid gas is further desorbed, so that the alcohol amine rich solution is completely regenerated into the alcohol amine barren 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, and the constant pressure vessel 9 is communicated with the dehydration adsorber 10. The water and the hydrogen sulfide in the carbon dioxide acid gas can be removed by utilizing the dehydration adsorber and the hydrogen sulfide removal adsorber, and the dust generated by the molecular sieve cracking can be filtered by utilizing the filter to obtain the pure carbon dioxide dry gas. The molecular sieve dehydration process of this embodiment is a desiccant dehydration hydrogen sulfide removal process, and according to the adsorption force of the adsorbent surface, dehydration is performed first, and then hydrogen sulfide is removed.
In the embodiment, the dehydration adsorber 10 adopts a 3A molecular sieve, and the hydrogen sulfide removal adsorber 11 adopts an RK-38 molecular sieve. The 3A molecular sieve is adopted, and only water is adsorbed and hydrogen sulfide and carbon dioxide are not adsorbed by utilizing the characteristic of small pore diameter of the 3A molecular sieve; and adopting RK-38 molecular sieve for removing hydrogen sulfide.
According to the embodiment, firstly, the absorption tower absorbs the acid gas with high carbon dioxide content, the regeneration tower is used for regenerating the absorbent, then the carbon dioxide acid gas enters the spraying stirrer to generate carbon dioxide hydrate and hydrogen sulfide hydrate in a low-temperature and high-pressure environment, the slurry of the carbon dioxide hydrate and the hydrogen sulfide hydrate is introduced into the constant-temperature container for gasification, and finally the mixed gas is dehydrated and dehydrogenated through the molecular sieve adsorption filtering device to obtain pure carbon dioxide dry gas.
Example 2
The method for purifying the carbon dioxide acid gas containing the impurities comprises the following steps:
s1, checking that the carbon dioxide acid gas absorption device, the spraying stirrer 8, the constant pressure container 9 and the molecular sieve adsorption filtering device are in normal operation state; the method comprises the following steps: checking whether the absorption tower and the regeneration tower work normally; checking whether the temperature and pressure control of the spraying stirrer meets the requirements or not; checking whether the pressure control of the constant pressure container is stable; monitoring whether the pump operates normally; checking whether various valves of the dehydration adsorber 10, the hydrogen sulfide removal adsorber 11 and the filter are switched on or off as required; then, temperature control is performed: starting a low-temperature control and constant-temperature circulator to control the temperature of the spraying stirrer according to preset experimental conditions until the temperature is constant to a set value; setting a constant pressure container to be stable at room temperature, and setting the constant pressure container to be stable at normal pressure;
s2, the associated gas containing carbon dioxide generated from a carbon dioxide driving well head enters an absorption tower of a carbon dioxide acid gas absorption device from the bottom and flows from bottom to top, meanwhile, alcohol amine barren solution in the carbon dioxide acid gas absorption device is in countercurrent contact with the associated gas, purified gas is discharged from the top of the carbon dioxide acid gas absorption device after the carbon dioxide acid gas is absorbed, alcohol amine rich solution after the acid gas is absorbed flows out from the bottom of the absorption tower, the alcohol amine rich solution enters the upper part of a regeneration tower after the temperature of the alcohol amine rich solution is raised to about 82-94 ℃ after passing through an alcohol amine barren solution heat exchanger, the alcohol amine rich solution is in countercurrent contact with high-temperature water vapor of a reboiler downwards along the regeneration tower, most of the acid gas is analyzed, the alcohol amine barren solution which recovers the absorption capacity after regeneration flows out from the bottom of the regeneration tower, the alcohol amine rich solution exchanges heat with cold alcohol. Condensing the gas flowing out of the top of the regeneration tower through a condensate reflux separator to obtain carried liquid water, and introducing carbon dioxide acid gas containing impurities such as water, hydrogen sulfide and methane into a spraying stirrer;
s3, setting the temperature of the spraying stirrer 8 to be 275.15-275.20K, setting the pressure to be 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 that carbon dioxide, water and hydrogen sulfide in carbon dioxide acid gas are sprayed and continuously stirred, discharging methane from the top of the spraying stirrer 8 in a gas phase state, and gravity-flowing the carbon dioxide hydrate and the hydrogen sulfide hydrate from the bottom of the spraying stirrer 8 into a constant-pressure container 9;
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, and enabling the obtained gaseous carbon dioxide, water and hydrogen sulfide to enter a molecular sieve adsorption filtering device from the top of the constant pressure container 9;
and S5, allowing 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, allowing the dehydrated carbon dioxide acid gas containing hydrogen sulfide impurities to flow out of the bottom of the dehydration adsorption tower and enter the hydrogen sulfide removal adsorption tower for hydrogen sulfide adsorption, and finally performing dust removal through a filter to obtain dry pure carbon dioxide dry gas.
According to the purification method of the carbon dioxide acid gas containing impurities, the carbon dioxide acid gas with high carbon dioxide content can be absorbed through the carbon dioxide acid gas absorption device, the regenerated and desorbed carbon dioxide acid gas containing impurities 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 directly desorbed in a gas phase state, and the purpose of separating and desorbing the 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 is to be understood that the terms "central," "longitudinal," "lateral," "length," "width," "thickness," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," "clockwise," "counterclockwise," "axial," "radial," "circumferential," and the like are used in the orientations and positional relationships indicated in the drawings for convenience in describing the invention and to simplify the description, and are not intended to indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality" means at least two, e.g., two, three, etc., unless specifically limited otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; they may be directly connected or indirectly connected through intervening media, or they may be connected internally or in any other suitable relationship, unless expressly stated otherwise. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the present invention, unless otherwise expressly stated or limited, the first feature "on" or "under" the second feature may be directly contacting the first and second features or indirectly contacting the first and second features through an intermediate. Also, a first feature "on," "over," and "above" a second feature may be directly or diagonally above the second feature, or may simply indicate that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature may be directly under or obliquely under the first feature, or may simply mean that the first feature is at a lesser elevation than the second feature.
In the description herein, references to the description of the term "one embodiment," "some embodiments," "an example," "a specific example," or "some examples," etc., mean 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 invention. In this specification, the schematic representations of the terms used above are not necessarily intended to refer 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, various embodiments or examples and features of different embodiments or examples described in this specification can be combined and combined by one skilled in the art without contradiction.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (10)
1. The utility model provides a carbon dioxide sour gas clean system who contains impurity, its characterized in that includes carbon dioxide sour gas absorbing device, sprays agitator, constant voltage container and molecular sieve adsorption and filtration device, carbon dioxide sour gas absorbing device's first input and the associated gas pipeline connection who contains carbon dioxide, carbon dioxide sour gas absorbing device's output with it connects to spray the agitator, carries the carbon dioxide sour gas that contains impurity that absorbs to spraying the agitator and generating hydrate slurry and methane gas, spray the agitator with constant voltage container is connected and carry the hydrate slurry to the gasification of constant voltage container, constant voltage container with molecular sieve adsorption and filtration device is connected and carry the gasification result to molecular sieve adsorption and filtration device adsorbs and filters and obtains pure carbon dioxide dry gas.
2. The system for purifying the carbon dioxide sour gas containing the impurities as claimed in claim 1, wherein the spraying stirrer is required to simultaneously meet the temperature of 275.15-275.20K and the pressure of 1.80-1.81 MPa.
3. The carbon dioxide acid gas purification system containing impurities as claimed in claim 1, wherein the pressure in the constant pressure container is maintained at normal pressure and 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 filtration device through a pipeline.
4. The carbon dioxide acid gas purification system containing impurities as claimed in claim 1, wherein the carbon dioxide acid gas absorption device comprises an absorption tower, a regeneration tower and an alcohol amine lean-rich liquid heat exchanger, a first input end of the absorption tower is connected with the carbon dioxide associated gas pipeline, a purified gas discharge port is arranged at the top of the absorption tower, the bottom of the absorption tower is communicated with a first input end of the regeneration tower through the alcohol amine lean-rich liquid heat exchanger tube pass, a second input end of the absorption tower is communicated with a first output end at the bottom of the regeneration tower through the alcohol amine lean-rich liquid heat exchanger shell pass, and a second output end at the top of the regeneration tower is communicated with the top of the spray stirrer.
5. The carbon dioxide acid gas purification system containing impurities as claimed in claim 4, 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 spraying stirrer, the condensate reflux separator is communicated with the second input end of the regeneration tower, and a condenser is arranged inside the condensate reflux separator and close to the inlet of the condensate reflux separator.
6. The carbon dioxide acid gas purification system containing impurities as claimed in claim 4, wherein an alcohol amine lean solution booster pump is arranged between the alcohol amine lean solution heat exchanger and the first output end of the bottom of the regeneration tower.
7. The carbon dioxide acid gas purification system containing impurities as claimed in claim 6, wherein 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.
8. The acid gas purification system for carbon dioxide containing impurities as claimed in claim 1, wherein the molecular sieve adsorption filtration device comprises a dehydration adsorber, a hydrogen sulfide removal adsorber and a filter connected in series, and the constant pressure vessel is communicated with the dehydration adsorber.
9. The acid gas purification system for carbon dioxide containing impurities as claimed in claim 8, wherein the dehydration adsorber uses 3A molecular sieve and the hydrogen sulfide removal adsorber uses RK-38 molecular sieve.
10. The method for purifying the carbon dioxide acid gas containing the impurities is characterized by comprising the following steps:
s1, checking that the carbon dioxide acid gas absorption device, the spraying stirrer, the constant pressure container and the molecular sieve adsorption filtering device are in normal operation state;
s2, allowing 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, allowing alcohol amine lean solution in the carbon dioxide acid gas absorption device to absorb the carbon dioxide acid gas in a countercurrent manner, discharging purified gas from the top of the carbon dioxide acid gas absorption device, regenerating alcohol amine rich solution after absorbing the acid gas and reusing the regenerated alcohol amine rich solution, allowing the carbon dioxide acid gas containing impurities resolved in the regeneration process to enter a spraying stirrer, and allowing the impurities in the carbon dioxide acid gas containing impurities to be water, hydrogen sulfide and methane;
s3, setting the temperature of the spraying stirrer to be 275.15-275.20K, setting the pressure to be 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 that carbon dioxide, water and hydrogen sulfide in carbon dioxide acid gas are sprayed and continuously stirred, discharging methane from the top of the spraying stirrer in a gas phase state, and gravity-automatically introducing the carbon dioxide hydrate and the hydrogen sulfide hydrate into a constant-pressure container from the bottom of the spraying 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 allowing the obtained gaseous carbon dioxide, water and hydrogen sulfide to enter a molecular sieve adsorption filtering device from the top of the constant pressure container;
and S5, adsorbing and filtering the carbon dioxide acid gas flow containing water and hydrogen sulfide by the molecular sieve adsorption and filtration device to obtain dry pure carbon dioxide dry gas.
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101177267A (en) * | 2007-10-31 | 2008-05-14 | 武汉凯迪电力环保有限公司 | Method for preparing food-grade carbon-dioxide by using power station smoke gas and system thereof |
| CN102329672A (en) * | 2011-09-06 | 2012-01-25 | 北京昊业怡生科技有限公司 | Method for separating and producing methane and carbon dioxide from marsh gas |
| CN103203174A (en) * | 2013-03-27 | 2013-07-17 | 华北电力大学（保定） | Method for collecting SO2 and CO2 in flue gas from coal-fired power plant and producing chemical products |
| CN106890545A (en) * | 2017-04-05 | 2017-06-27 | 安徽宣城金宏化工有限公司 | The separating technology and equipment of hydrogen sulfide in a kind of carbon disulphide production tail gas |
| CN207811623U (en) * | 2018-01-09 | 2018-09-04 | 中国石油工程建设有限公司 | A kind of device of the carbon dioxide removal from ethane gas |
| CN108722161A (en) * | 2018-08-16 | 2018-11-02 | 盘锦道博尔环保科技股份有限公司 | A kind of system and method removing hydrogen sulfide in oil field companion, secondary anger |
| CN109929638A (en) * | 2019-04-08 | 2019-06-25 | 常州大学 | A kind of method and apparatus for integrating hydrate and combining acid gas in removing natural gas with hydramine method |
| CN109929637A (en) * | 2019-04-08 | 2019-06-25 | 常州大学 | A kind of method and device based on hydrate gas separation principle purifying gas |
| CN211513994U (en) * | 2019-12-17 | 2020-09-18 | 中国石油集团工程股份有限公司 | Carbon dioxide acid gas purification system containing impurities |
-
2019
- 2019-12-17 CN CN201911299087.6A patent/CN110947280A/en active Pending
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101177267A (en) * | 2007-10-31 | 2008-05-14 | 武汉凯迪电力环保有限公司 | Method for preparing food-grade carbon-dioxide by using power station smoke gas and system thereof |
| CN102329672A (en) * | 2011-09-06 | 2012-01-25 | 北京昊业怡生科技有限公司 | Method for separating and producing methane and carbon dioxide from marsh gas |
| CN103203174A (en) * | 2013-03-27 | 2013-07-17 | 华北电力大学（保定） | Method for collecting SO2 and CO2 in flue gas from coal-fired power plant and producing chemical products |
| CN106890545A (en) * | 2017-04-05 | 2017-06-27 | 安徽宣城金宏化工有限公司 | The separating technology and equipment of hydrogen sulfide in a kind of carbon disulphide production tail gas |
| CN207811623U (en) * | 2018-01-09 | 2018-09-04 | 中国石油工程建设有限公司 | A kind of device of the carbon dioxide removal from ethane gas |
| CN108722161A (en) * | 2018-08-16 | 2018-11-02 | 盘锦道博尔环保科技股份有限公司 | A kind of system and method removing hydrogen sulfide in oil field companion, secondary anger |
| CN109929638A (en) * | 2019-04-08 | 2019-06-25 | 常州大学 | A kind of method and apparatus for integrating hydrate and combining acid gas in removing natural gas with hydramine method |
| CN109929637A (en) * | 2019-04-08 | 2019-06-25 | 常州大学 | A kind of method and device based on hydrate gas separation principle purifying gas |
| CN211513994U (en) * | 2019-12-17 | 2020-09-18 | 中国石油集团工程股份有限公司 | Carbon dioxide acid gas purification system containing impurities |
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