CN204891549U - Natural gas desulfurization decarbonization system of coupling sour gas concentration - Google Patents
Natural gas desulfurization decarbonization system of coupling sour gas concentration Download PDFInfo
- Publication number
- CN204891549U CN204891549U CN201520594307.9U CN201520594307U CN204891549U CN 204891549 U CN204891549 U CN 204891549U CN 201520594307 U CN201520594307 U CN 201520594307U CN 204891549 U CN204891549 U CN 204891549U
- Authority
- CN
- China
- Prior art keywords
- solution
- lean solution
- lean
- pump
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Abstract
The utility model discloses a natural gas desulfurization decarbonization system of coupling sour gas concentration, including natural gas filtering separation system, solution absorption system, flash distillation concentration system and the solution regeneration system who connects gradually, still be provided with solution stable system and solution filtration system. The utility model is suitable for a problem that the operation is unstable, solvent loss volume is big that natural gas desulfurization decarbonization device maximized and arouses had both been solved to large -scale natural gas desulfurization decarbonization device and contain the direct LNG liquefied desulfurization decarbonization preprocessing device of the sulphur raw materials natural gas, had also solved sulphur recovery unit equipment oversize's after the natural gas desulfurization decarbonization problem. Compare with aMDEA technology, MDEAmax technology, the utility model discloses the sour gas volume reduces by 20-45% when reaching like products gas index, and corresponding low reaches sulphur recovery unit equipment and pipeline can reduce 20-45%, have obvious advantage and extensive application prospect.
Description
Technical field
The utility model belongs to natural gas processing technical field, is specifically related to a kind of selexol process decarbonization system of the acid gas concentrate that is coupled.
Background technology
Because China's energy demand grows with each passing day, environmental requirement is simultaneously more strict, and natural gas is as a kind of high-quality, efficient, the clean energy, and the ratio in primary energy consumption improves day by day.Along with China's natural gas exploitation is on the increase, no matter be the natural gas processing plant for the purpose of pipe gas transmission or the sulfur-containing gas pretreatment unit for the purpose of LNG liquefaction, natural gas treatment plant scale is increasing.The single-row treating capacity of natural gas treatment plant of current China design and construction is all lower than foreign level, and the increase for the treatment of scale realizes mainly through increasing complexes columns.Foreign natural gas process is overall towards maximization future development, adopts single cover maximization device technique to realize High-efficiency Gas process, increase economic efficiency, but maximization natural gas processing technology still rests in offshore company's hand.
Desulfurization and decarburization device is agent set in sulfur-containing gas process, in order to remove raw natural gas overwhelming majority H
2s, CO
2, the foreign gas such as organic sulfur.Large desulfurization decarburization technique faces that device operation fluctuation is large, solvent loss is many and the problem such as downstream unit processing load is large.Therefore, breaking through maximization desulfurization and decarburization technology is the key solving maximization natural gas processing technology.
The current whole world widely used large-scale natural gas desulfurization and decarburization technique is all the improvement carried out based on conventional amine desulfurization decarbonization process.The improved though of offshore company is mainly divided into two kinds: one reduces equipment size, as aMDEA technique under adopting high-efficiency desulfurization decarbonization solvent to realize same treatment scale situation; Another kind adopts improving technique flow process, and the device stability requirement after making desulfurization and decarburization device meet maximization, as MDEAmax technique.Two kinds of typical techniques above will be introduced respectively below:
(1) aMDEA technique adopts and utilizes aMDEA patent solvent to H
2s has high selective, particularly H in unstripped gas
2the very low and CO of S content
2the occasion that dividing potential drop is high, uses lower solution circulation amount to realize at guarantee gas product CO in large desulfurization decarbonization device
2efficient removal overwhelming majority H when content is qualified
2s.Due to the chemistry of aMDEA solvent and heat endurance relatively good, selective desulfurization efficiency is higher than common MDEA solvent, and solvent load is less, can to a certain degree reduce appliance arrangement scale.Although this technique utilizes aMDEA to H
2s has high selective, has decreased solution to CO
2absorption, but CO higher in unstripped gas to be ensured
2relatively low level can be removed to, still have the CO of considerable amount
2be dissolved in aMDEA solution, the H removed along with solution reclaiming process
2s and CO
2enter in acid gas, and deliver to downstream sulfur recovery facility or other acid gas processing devices, the effect of these downstream units is H poisonous in process acid gas
2s, realizes sulfur highly effective and reclaims and tail gas qualified discharge, CO in acid gas processing procedure
2only do not participate in any reaction as inert gas.AMDEA technique do not consider the equipment size of sulfur recovery facility and acid gas total amount proportional, and CO in acid gas
2existence the equipment size of sulfur recovery facility is had waste significantly, this wasting phenomenon will be more outstanding in maximization natural gas processing process, likely as CO in acid gas
2concentration height to a certain extent, makes sulfur recovery facility equipment size super large, and becomes design new in large-scale natural gas treating apparatus whole process, manufacture or transportation bottleneck.
(2) MDEAmax process characteristic is mainly by selecting MDEA solution (concentration is 50wt%) the reinforcing desulfuration decarburization effect of high concentration, and the high concentration amine liquid of unit volume can absorb more H
2s and CO
2, thus reduce solution circulation amount, reduce the equipment size under same treatment scale condition.But it is higher that high concentration MDEA solution also exists viscosity, the problems such as solution foaming tendency increases, fluctuation of service, and wet purification natural gas entrained solution amount increases, and solution losses is high.This technique problem such as fluctuation of service, solvent loss height in large desulfurization decarbonization device will be amplified further, in order to address these problems, MDEAmax technique is on conventional amine desulfurization decarburization process base, increase a lean solution surge tank in the lean solution section of solution circulation backflow, the solution reserves utilizing lean solution surge tank huge balance the big ups and downs of liquid level in each equipment; Meanwhile, water scrubber is set before absorption tower top wet purification natural gas goes out device, wet purification natural gas normal temperature deaerated water is carried out wash the amine liquid reclaiming wet purification gas and carry secretly, and amine liquid is delivered in desulfurization and decarburization unit flashing tank, thus reduce solution losses.Although MDEAmax technique solves large desulfurization decarbonization device operational stability and solvent loss problem well, but still do not notice that MDEA is to H
2s and CO
2common suction act on impact excessive on downstream sulfur recovery facility equipment size in maximization process.MDEA is to H
2s and CO
2common suction effect H when causing regeneration acid gas to enter downstream sulfur recovery facility
2s concentration is on the low side, affects by molecular balance, and Recovery ratio is on the low side, if when C/S is higher in unstripped gas, may cause H in desulfurization acid gas
2s concentration is lower, forces recovery technology of sulfur to adopt shunting, and adopts fuel gas combustion-supporting, affect Recovery ratio further.In order to avoid recovery technology of sulfur adopts shunting, be everlasting in engineering and acid gas concentration unit (technological principle and device category and desulfurization and decarburization device similar) is set between desulfurization and decarburization device and sulfur recovery facility, utilize this device to carry out concentrate to the acid gas that desulfurization and decarburization device produces, remove most of CO
2, improve the H entering sulfur recovery facility acid gas
2s concentration, can avoid adopting shunting, can reduce again the acid gas amount entering sulfur recovery facility, and then reduce sulfur recovery facility equipment and line size.But this scheme needs to increase a whole set of acid gas concentration unit, and construction investment is high, and floor space is large.
Utility model content
The utility model overcomes shortcoming of the prior art, and provide a kind of selexol process decarbonization system of the acid gas concentrate that is coupled, this system can either complete conventional gas desulfurization and decarburization function, can utilize H again simultaneously
2s and CO
2flash evaporation characteristic and be that the amine liquid of matrix is to H with MDEA
2the selective absorbing characteristic of S is to H in rich solution
2s content concentrate, and mate high-pressure natural gas desulfurization and decarburization and low pressure sour gas extracting and concentrating technology condition respectively, complete acid gas concentrate process.The utility model is applicable to the desulfurization and decarburization pretreatment unit of large-scale natural gas desulfurization and decarburization device and the direct LNG liquefaction of sulfur-bearing raw natural gas, selexol process decarbonization device maximization Problems existing can be solved, significantly reduce downstream sulfur recovery facility equipment size and energy consumption simultaneously.
The technical solution of the utility model is: a kind of selexol process decarburization coupling acid gas upgrading system, comprises the natural gas filtering piece-rate system, solution absorption system, flash distillation upgrading system and the solution regeneration system that connect successively, wherein:
Described natural gas filtering piece-rate system comprises the gravity separator and filter separator that connect successively;
Described solution absorption system comprises the absorption tower and wet purification gas water scrubber that connect successively;
Described flash distillation upgrading system comprises the primary flash device, poor rich liquid heat exchanger, rich solution heater and the two-stage flash device that connect successively; Described primary flash device comprises primary flash tank and primary flash tower, and described two-stage flash device comprises two-stage flash tank, two-stage flash Gas Cooler and the two-stage flash tower that state successively connects successively;
Described solution regeneration system comprises regenerator, regeneration overhead return tank and regenerator reboiler; Described regenerator top gas vent is connected with regeneration overhead return tank by regeneration overhead condensate cooler, and the liquid outlet of regeneration overhead return tank is connected with regenerator upper liquid entrance through regenerator reflux pump.
Further, between described desulfurization and decarburization absorption tower and regenerator, be provided with solution-stabilized system, described solution-stabilized system comprises the hot lean pump, lean solution air cooler, lean solution aftercooler, lean solution surge tank, lean solution booster and the lean solution cooler that connect successively; Described hot lean pump is connected with poor rich liquid heat exchanger, and the liquid outlet of described lean solution cooler is connected with the upper liquid entrance of primary flash tower and two-stage flash tower respectively.
Further, solution filtration system is provided with in described solution-stabilized system, described solution filtration system comprises the lean solution filter pump, lean solution prefilter, active carbon filter and the lean solution after-filter that connect successively, and the liquid outlet of described lean solution after-filter is connected with the upper entrance of lean solution surge tank; The lower part outlet of described lean solution surge tank is connected with the entrance of lean solution filter pump.
Compared with prior art, the utility model has the advantages that: both solved selexol process decarbonization device and to have maximized the fluctuation of service caused, the problem that solvent loss amount is large, also solve the problem that sulfur recovery facility equipment size after selexol process decarburization is excessive.Concrete manifestation is as follows:
(1) under identical operating mode, compared with aMDEA technique, MDEAmax technique, when the utility model reaches like products gas index, acid gas amount reduces by 20 ~ 45%, respective downstream sulfur recovery facility equipment and pipeline can reduce 20 ~ 45%, effectively can reduce capital equipment and line size, saving equipment investment, there is obvious advantage and application prospect widely.
(2) under identical operating mode, connect compared with acid gas concentration unit with conventional desulfurization decarbonization device, the utility model takes into account desulfurization and decarburization and acid gas concentrate function, reduce the most equipment of the acid gas concentration unit arranged separately simultaneously, overall energy consumption reduces by 10 ~ 20%, and significantly reduces investment outlay and equipment occupation of land.
Accompanying drawing explanation
The utility model illustrates by example and with reference to the mode of accompanying drawing, wherein:
Fig. 1 is systematic schematic diagram of the present utility model.
Detailed description of the invention
A kind of selexol process decarbonization system of the acid gas concentrate that is coupled, as shown in Figure 1, comprise: gravity separator 1, filter separator 2, absorption tower 3, primary flash tank 4, primary flash tower 5, poor rich liquid heat exchanger 6, rich solution heater 7, two-stage flash tank 8, two-stage flash Gas Cooler 9, two-stage flash tower 10, two-stage flash column bottoms pump 11, pump 12 at the bottom of two-stage flash tank, regenerator 13, regeneration overhead condensate cooler 14, return tank 15, regenerator reflux pump 16, regenerator reboiler 17, hot lean pump 18, lean solution air cooler 19, lean solution surge tank 20, lean solution booster 21, lean solution aftercooler 22, lean solution circulating pump 23, wet purification gas water scrubber 24, washing pump 25, lean solution cooler 26, lean solution filter pump 27, lean solution prefilter 28, the equipment such as active carbon filter 29 and lean solution after-filter 30.
The utility model is provided with solution-stabilized system, flash distillation upgrading system (double flash evaporation concentrate) and wet purification gas water wash system in conventional amine desulfurization decarbonization device, defines the device adapting to the decarburization of maximization selexol process, utilizes H simultaneously
2s and CO
2flash evaporation characteristic and be that the amine liquid of matrix is to H with MDEA
2the selective absorbing characteristic of S is to H in rich solution
2s content concentrate, and mate high-pressure natural gas desulfurization and decarburization and low pressure sour gas extracting and concentrating technology condition respectively, effectively improve large desulfurization decarbonization device operational stability, significantly reduce downstream acid gas processing device (as sulfur recovery facility) equipment size.The utility model defines five major function systems, natural gas filtering piece-rate system (comprising gravity separator 1 and filter separator 2) successively, solution absorption system (comprises absorption tower 3, lean solution circulating pump 23, lean solution booster 21, wet purification gas water scrubber 24, washing pump 25), flash distillation upgrading system (comprises primary flash tank 4, primary flash tower 5, poor rich liquid heat exchanger 6, rich solution heater 7, two-stage flash tank 8, two-stage flash Gas Cooler 9, two-stage flash tower 10), solution regeneration system (comprises regenerator 13, regeneration overhead condensate cooler 14, regeneration overhead return tank 15, regenerator reflux pump 16, regenerator reboiler 17), solution-stabilized and filtration system (hot lean pump 18, lean solution air cooler 19, lean solution aftercooler 22, lean solution surge tank 20, lean solution filter pump 27, lean solution prefilter 28, active carbon filter 29 and lean solution after-filter 30), the concrete connected mode of native system is as follows:
Gravity separator 1 top exit connects with filter separator 2 entrance, filter separator 2 outlet connects with absorption tower 3 lower gas entrance, absorption tower 3 top gas outlet connects with wet purification gas water scrubber 24, the import and export of washing pump 25 are connected to wet purification gas water scrubber 24 tower bottom and tower top respectively, and the outlet of wet purification gas water scrubber 24 top gas is connected with downstream unit, absorption tower 3 bottom liquid outlet connects with primary flash tank 4 top entry, primary flash tank 4 is directly connected with primary flash tower 5, primary flash tank 4 bottom liquid outlet connects poor rich liquid heat exchanger 6 successively, rich solution heater 7, two-stage flash tank 8, the outlet of two-stage flash tank 8 top gas connects two-stage flash Gas Cooler 9 successively, two-stage flash tower 10, two-stage flash tower 10 bottom liquid outlet and two-stage flash tank 8 bottom liquid outlet are respectively through two-stage flash column bottoms pump 11, pump 12 at the bottom of two-stage flash tank is connected to regenerator 13 upper liquid entrance, the outlet of regenerator 13 top gas connects regeneration overhead condensate cooler 14 successively, downstream acid gas processing device is connected again after return tank 15, the liquid outlet of return tank 15 is connected with regenerator 13 upper liquid entrance through regenerator reflux pump 16, regenerator 13 bottom is connected with regenerator reboiler 17, regenerator 13 bottom liquid outlet successively with poor rich liquid heat exchanger 6, hot lean pump 18, lean solution air cooler 19, lean solution aftercooler 22, lean solution surge tank 20 is connected, lean solution surge tank 20 bottom liquid outlet successively with lean solution filter pump 27, lean solution prefilter 28, active carbon filter 29 is connected with lean solution after-filter 30, final lean solution after-filter 30 liquid outlet is connected with lean solution surge tank 20, lean solution surge tank 20 lower liquid outlet after lean solution booster 21 respectively with lean solution circulating pump 23, lean solution cooler 26 is connected, lean solution circulating pump 23 is connected with absorption tower 3 upper liquid entrance, lean solution cooler 26 liquid outlet is connected with the upper liquid entrance of two-stage flash tower 10 with primary flash tower 5 respectively.
Primary flash tower adopts packed tower, and two-stage flash tower adopts plate column, and water scrubber is plate column.
Operation principle of the present utility model is:
(1) two-stage flash facility is set at conventional amine desulfurization decarbonization device flash tank and flash column flow process downstream, form rich solution double flash evaporation upgrading system, primary flash tank and flash column, as lighter hydrocarbons flash distillation facility, flash off most of lighter hydrocarbons and a small amount of CO in rich solution
2and H
2s, requires H in the primary flash gas after process
2s concentration≤100ppm, flashed vapour can be used as full factory fuel gas and uses; Two-stage flash tank and flash column, as acid gas flash distillation facility, flash off a large amount of CO
2with a small amount of H
2s, closely reaches H in concentrate rich solution
2the object of S concentration, reduction acid gas amount, requires H in the two-stage flash gas after process
2s concentration≤50ppm, flashed vapour can be used as full factory fuel gas and uses.The outlet of poor rich liquid heat exchanger 6 rich solution arranges a rich solution heater 7, low-pressure steam (144 ~ 152 DEG C) or conduction oil (160 ~ 220 DEG C) can be adopted as thermal medium, the rich solution outlet of rich solution heater 7 connects two-stage flash tank 8 entrance, two-stage flash tank gaseous phase outlet connects two-stage flash Gas Cooler 9 entrance, two-stage flash Gas Cooler 9 exports and is connected with flashed vapour entrance bottom two-stage flash tower 10, enter in tower through the cooled lean solution of lean solution cooler 26 (lean solution temperature is lower than cooled rich solution flashed vapour 10 ~ 30 DEG C) from two-stage flash tower 10 top, with the rich solution flashed vapour counter current contacting entered by two-stage flash tower bottom, two-stage flash tower 10 bottom liquid outlet and two-stage flash tank 8 bottom liquid outlet respectively at the bottom of two-stage flash column bottoms pump 11, two-stage flash tank pump 12 be connected to regenerator 13 top rich solution entrance.
(2) hot lean pump 18, lean solution air cooler 19, lean solution surge tank 20, lean solution booster 21, lean solution aftercooler 22, flash distillation lean solution cooler 26 are set, form solution-stabilized system.The outlet of poor rich liquid heat exchanger 6 lean solution and hot lean pump 18, lean solution air cooler 19 entrance is connected, lean solution air cooler 19, lean solution aftercooler 22 is connected successively with lean solution surge tank 20, the lean solution outlet of lean solution surge tank is connected with lean solution booster 21, lean solution booster 21 outlet is divided into two branch roads, wherein one is connected to lean solution circulating pump 23 entrance, lean solution circulating pump 23 exports and is connected with top, absorption tower 3 lean solution entrance, other one is connected to flash distillation lean solution cooler 26 lean solution side entrance, lean solution cooler lean solution side outlet is connected to primary flash tower 5 top lean solution entrance and two-stage flash tower 10 top lean solution entrance respectively.Lean solution surge tank 20 connects lean solution filter pump 27, lean solution prefilter 28, active carbon filter 29 and lean solution after-filter 30 successively, and the outlet of lean solution after-filter 30 lean solution is connected to lean solution surge tank 20.
(3) wet purification gas water scrubber 24, washing pump 25 are set.The wet purification gas outlet at top, absorption tower 3 is connected with the wet purification gas entrance of wet purification gas water scrubber 24 bottom, washing pump 25 entrance and exit connects wet purification gas water scrubber 24 bottom water out and upper water entrance respectively, in addition, bottom wet purification gas water scrubber 24, leakage fluid dram is connected with primary flash tank.
Solvent loss through desulfurization and decarburization device of the present utility model reduces by 40%, and regenerated acid tolerance reduces 42%, and downstream sulfur recovery facility equipment and line size reduce about 42%.
Claims (7)
1. a selexol process decarbonization system for the acid gas concentrate that is coupled, is characterized in that: comprise the natural gas filtering piece-rate system, solution absorption system, flash distillation upgrading system and the solution regeneration system that connect successively, wherein:
Described natural gas filtering piece-rate system comprises the gravity separator and filter separator that connect successively;
Described solution absorption system comprises the absorption tower and wet purification gas water scrubber that connect successively;
Described flash distillation upgrading system comprises the primary flash device, poor rich liquid heat exchanger, rich solution heater and the two-stage flash device that connect successively; Described primary flash device comprises primary flash tank and primary flash tower, and described two-stage flash device comprises two-stage flash tank, two-stage flash Gas Cooler and the two-stage flash tower that state successively connects successively;
Described solution regeneration system comprises regenerator, regeneration overhead return tank and regenerator reboiler, described regenerator top gas vent is connected with regeneration overhead return tank by regeneration overhead condensate cooler, and the liquid outlet of regeneration overhead return tank is connected with regenerator upper liquid entrance through regenerator reflux pump.
2. the selexol process decarbonization system of a kind of acid gas concentrate that is coupled according to claim 1, it is characterized in that: between described desulfurization and decarburization absorption tower and regenerator, be provided with solution-stabilized system, described solution-stabilized system comprises the hot lean pump, lean solution air cooler, lean solution aftercooler, lean solution surge tank, lean solution booster and the lean solution cooler that connect successively; Described hot lean pump is connected with poor rich liquid heat exchanger, and the liquid outlet of described lean solution cooler is connected with the upper liquid entrance of primary flash tower and two-stage flash tower respectively.
3. the selexol process decarbonization system of a kind of acid gas concentrate that is coupled according to claim 2, it is characterized in that: in described solution-stabilized system, be provided with solution filtration system, described solution filtration system comprises the lean solution filter pump, lean solution prefilter, active carbon filter and the lean solution after-filter that connect successively, and the liquid outlet of described lean solution after-filter is connected with the upper entrance of lean solution surge tank; The lower part outlet of described lean solution surge tank is connected with the entrance of lean solution filter pump.
4. the selexol process decarbonization system of a kind of acid gas concentrate that is coupled according to claim 2, is characterized in that: described lean solution booster is connected with absorption tower upper liquid entrance by lean solution circulating pump.
5. the selexol process decarbonization system of a kind of acid gas concentrate that is coupled according to claim 1, is characterized in that: bottom water out and the upper water entrance of described wet purification gas water scrubber are connected import and the outlet of washing pump respectively.
6. the selexol process decarbonization system of a kind of acid gas concentrate that is coupled according to claim 1, is characterized in that: described two-stage flash tower bottom liquid outlet and two-stage flash pot bottom liquid outlet respectively at the bottom of two-stage flash column bottoms pump, two-stage flash tank pump be connected to regenerator top rich solution entrance.
7. the selexol process decarbonization system of a kind of acid gas concentrate that is coupled according to claim 1, is characterized in that: described primary flash tower adopts packed tower, and two-stage flash tower adopts plate column, and wet purification gas water scrubber is plate column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520594307.9U CN204891549U (en) | 2015-08-10 | 2015-08-10 | Natural gas desulfurization decarbonization system of coupling sour gas concentration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520594307.9U CN204891549U (en) | 2015-08-10 | 2015-08-10 | Natural gas desulfurization decarbonization system of coupling sour gas concentration |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204891549U true CN204891549U (en) | 2015-12-23 |
Family
ID=54913766
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520594307.9U Active CN204891549U (en) | 2015-08-10 | 2015-08-10 | Natural gas desulfurization decarbonization system of coupling sour gas concentration |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN204891549U (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105013296A (en) * | 2015-08-10 | 2015-11-04 | 中国石油集团工程设计有限责任公司 | Natural gas desulfuration and decarbonization system and method coupling acid gas concentration |
| RU2621754C1 (en) * | 2016-08-15 | 2017-06-07 | Игорь Анатольевич Мнушкин | Method of absorption cleaning of hydrocarbon gas from acid components |
| CN113337322A (en) * | 2020-03-03 | 2021-09-03 | 中国石油化工股份有限公司 | Efficient natural gas dechlorinating device and process |
-
2015
- 2015-08-10 CN CN201520594307.9U patent/CN204891549U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105013296A (en) * | 2015-08-10 | 2015-11-04 | 中国石油集团工程设计有限责任公司 | Natural gas desulfuration and decarbonization system and method coupling acid gas concentration |
| CN105013296B (en) * | 2015-08-10 | 2017-06-06 | 中国石油集团工程设计有限责任公司 | A kind of selexol process decarbonization system and method for coupling acid gas concentrate |
| RU2621754C1 (en) * | 2016-08-15 | 2017-06-07 | Игорь Анатольевич Мнушкин | Method of absorption cleaning of hydrocarbon gas from acid components |
| CN113337322A (en) * | 2020-03-03 | 2021-09-03 | 中国石油化工股份有限公司 | Efficient natural gas dechlorinating device and process |
| CN113337322B (en) * | 2020-03-03 | 2022-12-02 | 中国石油化工股份有限公司 | Efficient natural gas dechlorination device and process |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105013296B (en) | A kind of selexol process decarbonization system and method for coupling acid gas concentrate | |
| CN104445272B (en) | A kind of conversion gas phlegma comprehensive reutilization method containing ammonia, carbonic acid gas | |
| CN102806000B (en) | Energy-saving one-step rectisol method | |
| CN202751942U (en) | Sulphur tail gas absorption and purification combined device | |
| CN105038882B (en) | A kind of saturated aqueous oil field gas reclaims the comprehensive smart dewatering process of LNG/LPG/NGL products | |
| CN202808741U (en) | Deep purification system for natural gas desulfuration and decarburization | |
| CN204891549U (en) | Natural gas desulfurization decarbonization system of coupling sour gas concentration | |
| CN109569193A (en) | It is a kind of to absorb the sulfur method synchronous with regeneration | |
| CN102489120B (en) | Low temperature methanol wash method and equipment | |
| CN104087358B (en) | Natural gas purification is equipped | |
| CN210826085U (en) | Blast furnace gas catalytic desulfurization device | |
| CN203429147U (en) | Methane purifying system | |
| CN202355997U (en) | CO2 absorption tower and low-temperature methanol washing equipment comprising same | |
| CN205011721U (en) | Smart dewatering system of synthesis of LNGLPGNGL product is retrieved to saturation wet oil associated gas | |
| CN106477577B (en) | A kind of device and production method of heat pump distillation production ultra-high purity carbon dioxide | |
| CN104624022A (en) | Double-absorption and double-desorption hydrogen gas and light hydrocarbon comprehensive recovery system | |
| CN202912906U (en) | Skid-mounted type natural gas purifying and recycling device | |
| CN202751934U (en) | Sulfur tail gas absorption purification combination device with circulated absorbents | |
| CN203833908U (en) | Natural gas deacidifying device | |
| CN216125432U (en) | Amine liquid regenerating device for removing coke powder in regenerated amine liquid | |
| CN204093274U (en) | Flue gas desulphurization system | |
| CN105833680A (en) | Amine desulphurization method for refinery plant | |
| CN109929638A (en) | A kind of method and apparatus for integrating hydrate and combining acid gas in removing natural gas with hydramine method | |
| CN205164444U (en) | Flue gas recirculation desulfurization system | |
| CN210855897U (en) | For high content of CO2Ethane gas deep purification device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180115 Address after: 610041 Chengdu high tech Zone, Sichuan province sublimation Road No. 6 Patentee after: China Petroleum Engineering Construction Co Ltd Address before: 610041 Chengdu high tech Zone, Sichuan province sublimation Road No. 6 Patentee before: Engineering Design Co., Ltd., China Petroleum Group |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20210220 Address after: 100007 No. 9 North Main Street, Dongcheng District, Beijing, Dongzhimen Patentee after: CHINA NATIONAL PETROLEUM Corp. Patentee after: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. Address before: No. 6, Sichuan hi tech Zone, sublime Road, Chengdu, Sichuan Patentee before: CHINA PETROLEUM ENGINEERING & CONSTRUCTION Corp. |
|
| TR01 | Transfer of patent right |