CN103691250B - The method for purifying and recovering of time anger in a kind of steam drive oil production - Google Patents
The method for purifying and recovering of time anger in a kind of steam drive oil production Download PDFInfo
- Publication number
- CN103691250B CN103691250B CN201310504760.1A CN201310504760A CN103691250B CN 103691250 B CN103691250 B CN 103691250B CN 201310504760 A CN201310504760 A CN 201310504760A CN 103691250 B CN103691250 B CN 103691250B
- Authority
- CN
- China
- Prior art keywords
- gas
- pressure
- adsorption
- tower
- adsorption 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
- 238000000034 method Methods 0.000 title claims abstract description 85
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 15
- 238000010795 Steam Flooding Methods 0.000 title claims abstract description 14
- 239000007789 gas Substances 0.000 claims abstract description 59
- 238000001179 sorption measurement Methods 0.000 claims abstract description 54
- 239000007788 liquid Substances 0.000 claims abstract description 19
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000000746 purification Methods 0.000 claims abstract description 10
- 239000003345 natural gas Substances 0.000 claims abstract description 5
- 230000008569 process Effects 0.000 claims description 64
- 238000010521 absorption reaction Methods 0.000 claims description 23
- 239000003463 adsorbent Substances 0.000 claims description 15
- 230000003009 desulfurizing effect Effects 0.000 claims description 14
- 239000003795 chemical substances by application Substances 0.000 claims description 12
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 229910052717 sulfur Inorganic materials 0.000 claims description 7
- 239000011593 sulfur Substances 0.000 claims description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 claims description 6
- 239000002156 adsorbate Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 238000011069 regeneration method Methods 0.000 claims description 6
- 230000008439 repair process Effects 0.000 claims description 6
- 238000000926 separation method Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 239000012535 impurity Substances 0.000 claims description 5
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 4
- 238000006477 desulfuration reaction Methods 0.000 claims description 4
- 230000023556 desulfurization Effects 0.000 claims description 4
- 125000001741 organic sulfur group Chemical group 0.000 claims description 4
- 238000011084 recovery Methods 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- 229910002588 FeOOH Inorganic materials 0.000 claims description 3
- 230000000274 adsorptive effect Effects 0.000 claims description 3
- 238000007605 air drying Methods 0.000 claims description 3
- 239000012752 auxiliary agent Substances 0.000 claims description 3
- 150000001721 carbon Chemical class 0.000 claims description 3
- 239000000356 contaminant Substances 0.000 claims description 3
- 238000005262 decarbonization Methods 0.000 claims description 3
- 230000018044 dehydration Effects 0.000 claims description 3
- 238000006297 dehydration reaction Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 239000002737 fuel gas Substances 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 3
- 238000002203 pretreatment Methods 0.000 claims description 3
- 230000009467 reduction Effects 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 230000008929 regeneration Effects 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- 239000011787 zinc oxide Substances 0.000 claims description 3
- 238000005516 engineering process Methods 0.000 abstract description 3
- 230000035800 maturation Effects 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000006378 damage Effects 0.000 description 2
- 239000003129 oil well Substances 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 208000027418 Wounds and injury Diseases 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 208000014674 injury Diseases 0.000 description 1
- 230000000505 pernicious effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
The present invention relates to tail gas disposal technique field, particularly secondary angry method for purifying and recovering in a kind of steam drive oil production.The method can by the H in secondary anger
2s, CO
2and CH
4effectively be separated, to CO
2and CH
4carry out purifying and reclaiming.The present invention adopts low pressure pressure-variable adsorption, purification, low-pressure liquefied technique purified steam drives time anger of recovering the oil, and reclaims natural gas, produces liquid CO 2.This technique is advanced, and technology maturation is reliable, and product purity is high, and production cost is low.
Description
Technical field
The present invention relates to tail gas disposal technique field, particularly secondary angry method for purifying and recovering in a kind of steam drive oil production.
Background technology
Viscous crude field when adopting steam drive oil production, in oil well time anger hydrogen sulfide and carbon dioxide content more and more serious.The rising of hydrogen sulfide content and the concentrated outer row of secondary anger, cause oil well and wellsite working environment to worsen, cause certain injury, there is severe compromise to the health of employee and the periphery village common people; The rising of carbon dioxide content, causes time anger to utilize.Therefore control carries out to the secondary anger produced in steam drive oil production process very urgent.
Summary of the invention
The invention provides the method for purifying and recovering of time anger in a kind of steam drive oil production, the method can by the H in secondary anger
2s, CO
2and CH
4effectively be separated, to CO
2and CH
4carry out purifying and reclaiming.
For solving problems of the prior art, the present invention is achieved through the following technical solutions.
In steam drive oil production, a method for purifying and recovering for time anger, mainly comprises H in described anger
2s, CO
2and CH
4gas and other impurity, described method mainly comprises the following steps:
1) secondary air drying desulfurized step
In steam drive oil production, time anger removes liquid through gas-liquid separator, then after air cooler cooling, the desulfurizing agent that sulfur-bearing time anger enters in desulfurizing tower and tower reflects, removes the H in time anger
2s.
The weight ratio of described desulfurizing agent consists of: FeOOH 85-90%, zinc oxide 8-12%, auxiliary agent 2-3%.
2) secondary angry supercharging pre-treatment step
Time anger after desulfurization enters into unstripped gas surge tank as unstripped gas, after compressor boost to 0.3MPa, unstrpped gas enters pretreatment adsorption tower at the bottom of the pretreatment adsorption tower of pretreatment system, under the selective absorption of active carbon class adsorbent, and the most of C in removing unstripped gas
5 +heavy hydrocarbons impurity.
3) unstripped gas pressure-variable adsorption CH
4/ CO
2separating step
Unstripped gas through previous step enters pressure swing adsorption decarbonization system, the CO in adsorption tower Raw gas
2got off by silica type adsorbent adsorption selection, separation of C O
2purified gas to deoil field fuel gas system as gas product.
When the mass-transfer zone forward position (be called absorption forward position) of adsorbing contaminant in adsorption tower arrives a certain position of the reserved section of bed outlet, stop absorption, proceed to regenerative process.
The regenerative process of adsorbent is as follows successively:
A. drop pressure process
This is after adsorption process terminates, and along absorption direction, the gas of the elevated pressures in tower is put into the process that other has completed the lower pressure adsorption tower of regeneration, and this process is not only pressure reduction CH in recovery tower especially
4, improve CH
4the process of yield, this flow process includes three continuous print drop pressure processes altogether.
B. inverse put process
All press end, absorption forward position reached bed outlet after, against absorption direction adsorption column pressure is down to close to normal pressure, now by the CO adsorbed
2start to desorb in a large number from adsorbent, and enter CO
2storage tank.
C. vacuum process
After inverse put terminates, for making adsorbent be regenerated thoroughly, with vavuum pump, bed being vacuumized, reducing the dividing potential drop of adsorbate component further, and adsorbate is desorbed, and entering CO
2storage tank.
D. boost pressure process
After vacuum process completes, successively this adsorption tower is boosted with the elevated pressures gas from other adsorption tower, this process is corresponding with drop pressure process, be not only boost process, and be the process of the bed dead space gas reclaiming other tower, this flow process includes continuous three boost pressure processes altogether.
F. gas product boost process
After three boost pressure processes complete, can switch to reposefully to make adsorption tower and adsorb next time and ensure that product purity does not fluctuate in this course, need slowly and reposefully to use rich CH by boost adjusted valve
4gas rises to adsorptive pressure to adsorption column pressure.
After this process, adsorption tower just completes complete " adsorption-regeneration " circulation, again for absorption is next time got ready.
Multiple adsorption tower hockets above absorption, regenerative operation, has 1 adsorption tower to be in adsorbed state all the time, can realize being continuously separated and purification of secondary gas.
4) organic sulfur removal step
Activated carbon desulphurization agent is utilized to remove separation of C H
4after CO
2organic sulfur in gas.
5) liquid CO
2preparation process
CO after organic sulfide removal
2gas is pressurized to after 2.8MPa through overcompression and carries out de-hydrocarbon purification, then makes it liquefaction for liquid CO by cooling
2, drying dehydration, rectified purified after obtain industrial liquid CO
2product.
The present invention adopts low pressure pressure-variable adsorption, purification, low-pressure liquefied technique purified steam drives time anger of recovering the oil, and reclaims natural gas, produces liquid CO 2.This technique is advanced, and technology maturation is reliable, and product purity is high, and production cost is low.
Accompanying drawing explanation
Fig. 1 double tower dry desulfurizing process flow chart
Fig. 2 angry CO
2reclaiming clean process chart
Detailed description of the invention
Align 40 pieces angry employing recovery and purification methods of the present invention.The feature of neat 40 pieces anger is dispersions, and in each small station tolerance, secondary anger, hydrogen sulfide content difference is comparatively large, simultaneously CO in time anger
2content is up to 80%-90%.
Process mainly comprises the following steps:
1) secondary air drying desulfurized step
In steam drive oil production, time anger removes liquid through gas-liquid separator, then after air cooler cooling, the desulfurizing agent that sulfur-bearing time anger enters in desulfurizing tower and tower reflects, removes the H in time anger
2s.
The weight ratio of described desulfurizing agent consists of: FeOOH 85-90%, zinc oxide 8-12%, auxiliary agent 2-3%.
In order to make full use of desulfurizing agent, to ensure in each tower that desulfurizing agent can reach capacity Sulfur capacity, the desulfurization flow process adopting connection in series-parallel to combine, takes into full account technique in design, makes each tower can as first and last tower.Establish two beds in each desulfurizing tower, be convenient to the handling of desulfurizing agent.On average the cycle of changing dressings is half a year to desulfurizing agent.Hydrogen sulfide content≤10mg/m in natural gas after de-
3.
2) secondary angry supercharging pre-treatment step
Time anger after desulfurization enters into unstripped gas surge tank as unstripped gas, after compressor boost to 0.3MPa, unstrpped gas enters pretreatment adsorption tower at the bottom of the pretreatment adsorption tower of pretreatment system, under the selective absorption of active carbon class adsorbent, and the most of C in removing unstripped gas
5 +heavy hydrocarbons impurity.
3) unstripped gas pressure-variable adsorption CH
4/ CO
2separating step
Unstripped gas after oil removing enters pressure swing adsorption decarbonization system, the CO in adsorption tower Raw gas
2got off by silica type adsorbent adsorption selection, separation of C O
2purified gas to deoil field fuel gas system as gas product.
When the mass-transfer zone forward position (be called absorption forward position) of adsorbing contaminant in adsorption tower arrives a certain position of the reserved section of bed outlet, stop absorption, proceed to regenerative process.
The regenerative process of adsorbent is as follows successively:
A. drop pressure process
This is after adsorption process terminates, and along absorption direction, the gas of the elevated pressures in tower is put into the process that other has completed the lower pressure adsorption tower of regeneration, and this process is not only pressure reduction CH in recovery tower especially
4, improve CH
4the process of yield, this flow process includes three continuous print drop pressure processes altogether.
B. inverse put process
All press end, absorption forward position reached bed outlet after, against absorption direction adsorption column pressure is down to close to normal pressure, now by the CO adsorbed
2start to desorb in a large number from adsorbent, and enter CO
2storage tank.
C. vacuum process
After inverse put terminates, for making adsorbent be regenerated thoroughly, with vavuum pump, bed being vacuumized, reducing the dividing potential drop of adsorbate component further, and adsorbate is desorbed, and entering CO
2storage tank.
D. boost pressure process
After vacuum process completes, successively this adsorption tower is boosted with the elevated pressures gas from other adsorption tower, this process is corresponding with drop pressure process, be not only boost process, and be the process of the bed dead space gas reclaiming other tower, this flow process includes continuous three boost pressure processes altogether.
F. gas product boost process
After three boost pressure processes complete, can switch to reposefully to make adsorption tower and adsorb next time and ensure that product purity does not fluctuate in this course, need slowly and reposefully to rise to adsorptive pressure with rich CH4 gas to adsorption column pressure by boost adjusted valve.
After this process, adsorption tower just completes complete " adsorption-regeneration " circulation, again for absorption is next time got ready.
Multiple adsorption tower hockets above absorption, regenerative operation, has 1 adsorption tower to be in adsorbed state all the time, can realize being continuously separated and purification of secondary gas.
4) organic sulfur removal step
Activated carbon desulphurization agent is utilized to remove separation of C H
4after CO
2organic sulfur in gas.
The content (ppm) of table 1 organic sulfur
5) liquid CO
2preparation process
CO after organic sulfide removal
2gas is pressurized to after 2.8MPa through overcompression and carries out de-hydrocarbon purification, then makes it liquefaction for liquid CO by cooling
2, drying dehydration, rectified purified after obtain industrial liquid CO
2product.
With neat 40 pieces of oil fields time anger for unstripped gas, produce the purified gas and the liquid CO 2 that are rich in methane.Neat 40 pieces of oil fields time anger is all utilized, reclaims natural gas, reduce energy waste; Gas purification organic sulfide removal, reduces the pollution of pernicious gas to environment and the harm to human body; Liquid CO 2 is produced, and reduces greenhouse gas emission.This project not only meets the requirement of national recycling economy, cleaner production, and is environmental protection project.
Claims (3)
1. a secondary angry method for purifying and recovering in steam drive oil production, mainly comprises H in described anger
2s, CO
2and CH
4gas and other impurity, is characterized in that, described method mainly comprises the following steps:
1) secondary air drying desulfurized step
In steam drive oil production, time anger removes liquid through gas-liquid separator, then after air cooler cooling, the desulfurizing agent that sulfur-bearing time anger enters in desulfurizing tower and tower reacts, and removes the H in time anger
2s;
2) secondary angry supercharging pre-treatment step
Time anger after desulfurization enters into unstripped gas surge tank as unstripped gas, after compressor boost to 0.3MPa, unstrpped gas enters pretreatment adsorption tower at the bottom of the pretreatment adsorption tower of pretreatment system, under the selective absorption of active carbon class adsorbent, and the most of C in removing unstripped gas
5 +heavy hydrocarbons impurity;
3) unstripped gas pressure-variable adsorption CH
4/ CO
2separating step
Unstripped gas through previous step enters pressure swing adsorption decarbonization system, the CO in adsorption tower Raw gas
2got off by silica type adsorbent adsorption selection, separation of C O
2purified gas is as natural gas CH
4product deoils field fuel gas system;
4) organic sulfur removal step
Activated carbon desulphurization agent is utilized to remove separation of C H
4after CO
2organic sulfur in gas;
5) liquid CO
2preparation process
CO after organic sulfide removal
2gas is pressurized to after 2.8MPa through overcompression and carries out de-hydrocarbon purification, then makes it liquefaction for liquid CO by cooling
2, drying dehydration, rectified purified after obtain industrial liquid CO
2product.
2. method for purifying and recovering as claimed in claim 1, is characterized in that, at unstripped gas pressure-variable adsorption CH
4/ CO
2in separating step, when the mass-transfer zone forward position of adsorbing contaminant in adsorption tower arrives a certain position of the reserved section of bed outlet, stop absorption, proceed to regenerative process,
The regenerative process of adsorbent is as follows successively:
A. drop pressure process
This is after adsorption process terminates, and along absorption direction, the gas of the elevated pressures in tower is put into the process that other has completed the lower pressure adsorption tower of regeneration, and this process is not only pressure reduction CH in recovery tower especially
4, improve CH
4the process of yield, this flow process includes three continuous print drop pressure processes altogether;
B. inverse put process
All press end, absorption forward position reached bed outlet after, against absorption direction adsorption column pressure is down to close to normal pressure, now by the CO adsorbed
2start to desorb in a large number from adsorbent, and enter CO
2storage tank;
C. vacuum process
After inverse put terminates, for making adsorbent be regenerated thoroughly, with vavuum pump, bed being vacuumized, reducing the dividing potential drop of adsorbate component further, and adsorbate is desorbed, and entering CO
2storage tank;
D. boost pressure process
After vacuum process completes, successively this adsorption tower is boosted with the elevated pressures gas from other adsorption tower, this process is corresponding with drop pressure process, be not only boost process, and be the process of the bed dead space gas reclaiming other tower, this flow process includes continuous three boost pressure processes altogether;
F. gas product boost process
After three boost pressure processes complete, can switch to reposefully to make adsorption tower and adsorb next time and ensure that product purity does not fluctuate in this course, need slowly and reposefully to use rich CH by boost adjusted valve
4gas rises to adsorptive pressure to adsorption column pressure;
After this process, adsorption tower just completes complete " adsorption-regeneration " circulation, again for absorption is next time got ready, multiple adsorption tower hockets above absorption, regenerative operation, all the time there is 1 adsorption tower to be in adsorbed state, being continuously separated and purification of secondary gas can be realized.
3. method for purifying and recovering as claimed in claim 1, is characterized in that, step 1) in the weight ratio of desulfurizer therefor consist of: FeOOH 85-90%, zinc oxide 8-12%, auxiliary agent 2-3%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310504760.1A CN103691250B (en) | 2013-10-19 | 2013-10-19 | The method for purifying and recovering of time anger in a kind of steam drive oil production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310504760.1A CN103691250B (en) | 2013-10-19 | 2013-10-19 | The method for purifying and recovering of time anger in a kind of steam drive oil production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103691250A CN103691250A (en) | 2014-04-02 |
| CN103691250B true CN103691250B (en) | 2016-04-06 |
Family
ID=50353011
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310504760.1A Active CN103691250B (en) | 2013-10-19 | 2013-10-19 | The method for purifying and recovering of time anger in a kind of steam drive oil production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103691250B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104748506B (en) * | 2015-03-13 | 2017-05-24 | 河南心连心深冷能源股份有限公司 | Device for recycling CO2 from oil field mining assisting tail gas and process thereof |
| CN111004657B (en) * | 2019-12-11 | 2021-04-27 | 中国天辰工程有限公司 | Method for comprehensively utilizing oilfield associated gas |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102580458A (en) * | 2012-02-21 | 2012-07-18 | 北京信诺海博石化科技发展有限公司 | Multi-order vacuumizing pressure swing adsorption process |
-
2013
- 2013-10-19 CN CN201310504760.1A patent/CN103691250B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102580458A (en) * | 2012-02-21 | 2012-07-18 | 北京信诺海博石化科技发展有限公司 | Multi-order vacuumizing pressure swing adsorption process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103691250A (en) | 2014-04-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2017166943A1 (en) | Full-temperature-range pressure swing adsorption gas separation, refinement and purification method | |
| CN103521033B (en) | The method for purifying and recovering of time anger in a kind of fire flood | |
| CN101274752B (en) | Separation and utilization process for sulfuric dioxide and carbon dioxide in stack gas | |
| CN105026528B (en) | Methane gas method for concentration | |
| CN101126042B (en) | Integrative purification and separation method for natural gas | |
| CN102433169A (en) | Low temperature methanol washing technology | |
| CN104058371A (en) | Pressure swing adsorption gas production system and pressure swing adsorption gas production method | |
| CN103585856A (en) | Multi-backflow pressure swing adsorption method | |
| CN112678773B (en) | Process for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas | |
| CN102190541A (en) | Method for recovering methane for industrial production of clean fuel through deep purification of landfill gas | |
| CN107433107A (en) | C2+ two sections of points of concentration PSA methods are reclaimed from oil refinery dry gas | |
| CN102391898A (en) | Method for separating and purifying carbon dioxide in marsh gas by adopting pressure swing adsorption | |
| CN203728792U (en) | High-purity methane purification device | |
| CN103540335A (en) | Technology for recycling light dydrocarbon components from flare gases | |
| CN101691320A (en) | Method for purifying and recycling methane and carbon dioxide from landfill gas and device thereof | |
| CN103861422A (en) | New technique for concentrating methane in oxygen-containing coal bed gas | |
| CN107285279A (en) | A kind of method using the purified synthesis gas of complete warm journey pressure-variable adsorption with separating | |
| CN202569906U (en) | Dry gas pressure swing adsorption (PSA) ethylene-and-hydrogen recycling device in oil refinery | |
| CN102923655A (en) | Method for extracting pure hydrogen from tail gas of semi coke | |
| CN103691250B (en) | The method for purifying and recovering of time anger in a kind of steam drive oil production | |
| CN1279006C (en) | Method for purification and recovery of methane from refuse landfill gas | |
| CN101015761A (en) | Pressure-swing-adsorption purging regeneration method without using vacuum pump | |
| CN216604669U (en) | Device for recovering high-purity hydrogen by utilizing styrene dehydrogenation tail gas | |
| CN103991845B (en) | A kind of method of hydrogen production process conversion gas carbon dioxide removal | |
| CN102600699B (en) | Pressure-variable adsorption gas separation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C53 | Correction of patent of invention or patent application | ||
| CB03 | Change of inventor or designer information |
Inventor after: Song Yinglai Inventor after: Han Xin Inventor after: Xu Shulin Inventor after: Qi Wenzhang Inventor after: Guan Dayi Inventor after: Xie Yongjia Inventor after: Yang Ling Inventor after: Wang Yu Inventor before: Send welcome Inventor before: Han Xin Inventor before: Xu Shulin Inventor before: Qi Wenzhang Inventor before: Guan Dayi Inventor before: Xie Yongjia Inventor before: Yang Ling Inventor before: Wang Yu |
|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 124010 Industrial Development Zone, Xinglongtai District, Liaoning, Panjin Patentee after: PANJIN DOBER ENVIRONMENTAL TECHNOLOGY Inc. Address before: 124010 Industrial Development Zone, Xinglongtai District, Liaoning, Panjin Patentee before: PANJIN DAOBOER PETROLEUM NEW TECHNOLOGY DEVELOPMENT Co.,Ltd. |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |
Denomination of invention: A purification and recovery method for secondary gas in steam flooding oil recovery Effective date of registration: 20240103 Granted publication date: 20160406 Pledgee: Agricultural Bank of China Limited Panjin Xinglong Branch Pledgor: PANJIN DOBER ENVIRONMENTAL TECHNOLOGY Inc. Registration number: Y2024980000355 |
|
| PE01 | Entry into force of the registration of the contract for pledge of patent right |