CN101773765A - Method for reclaiming hydrogen in refinery dry gas - Google Patents
Method for reclaiming hydrogen in refinery dry gas Download PDFInfo
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- CN101773765A CN101773765A CN201010000591A CN201010000591A CN101773765A CN 101773765 A CN101773765 A CN 101773765A CN 201010000591 A CN201010000591 A CN 201010000591A CN 201010000591 A CN201010000591 A CN 201010000591A CN 101773765 A CN101773765 A CN 101773765A
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- 239000007789 gas Substances 0.000 title claims abstract description 105
- 239000001257 hydrogen Substances 0.000 title claims abstract description 96
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 96
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 89
- 238000000034 method Methods 0.000 title claims abstract description 28
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 7
- 239000012466 permeate Substances 0.000 claims description 5
- 230000008569 process Effects 0.000 claims description 5
- 239000000047 product Substances 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 239000012528 membrane Substances 0.000 abstract description 16
- 238000001179 sorption measurement Methods 0.000 abstract description 11
- 239000003921 oil Substances 0.000 description 20
- 238000006555 catalytic reaction Methods 0.000 description 16
- 238000005516 engineering process Methods 0.000 description 13
- 238000001035 drying Methods 0.000 description 10
- 238000011084 recovery Methods 0.000 description 9
- 238000005265 energy consumption Methods 0.000 description 7
- 150000002431 hydrogen Chemical class 0.000 description 7
- 230000009466 transformation Effects 0.000 description 7
- 230000008901 benefit Effects 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000003463 adsorbent Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 2
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000001808 coupling effect Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000007781 pre-processing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
Abstract
The invention discloses a method for reclaiming hydrogen in refinery dry gas, which comprises the following steps: (1) firstly, pre-separating the refinery dry gas in which the molar content of the hydrogen is 20 to 35 percent and the pressure is not lower than 0.8MPa by using a membrane separation unit so as to enrich H2 in the refinery dry gas on the permeation side of a membrane; (2) secondly, pressurizing the gas rich in hydrogen after enriching on the permeation side of the membrane in the membrane separation unit to 1.0 to 1.2MPa, and feeding the gas into a pressure swing adsorption unit; and (3) finally, further adsorbing the hydrocarbons contained in the gas by using the pressure swing adsorption unit to ensure that the purity of the H2 reaches 95 to 99.5 percent based on mole percent and the pressure is kept between 0.9 and 1.1MPa, and delivering the hydrocarbons serving as hydrogen products. The method mainly comprises the membrane separation unit and the pressure swing adsorption unit. The method can purify the hydrogen in the refinery dry gas in which the molar content of the hydrogen is 20 to 35 percent to over 95 percent so as to fully reclaim the hydrogen resources.
Description
Technical field
The present invention relates to recover hydrogen (H from oil refinery dry gas
2: the method for 20mol%～35mol%) is a kind of method by film separation/transformation absorption integrated technique recover hydrogen from oil refinery dry gas.
Background technology
Refinery gas is mainly derived from the crude oil secondary operations, as the gas that produces in the processes such as catalytic cracking, thermal cracking, time-delay coking, hydrocracking.5% of its output average out to crude runs mainly contains components such as hydrogen, methane, ethene, ethane, propylene, propane, is a kind of valuable source of petrochemical industry.Catalytic cracked dry gas amount maximum in China's refinery gas was recycled because of no appropriate method in the past, can only act as a fuel and burn in vain, caused huge waste.Contain a large amount of hydrogen in China's refinery gas, as refining at gasoline and diesel hydrogenation, in the processing procedures such as lube oil hydrogenation, the hydrogen content that has in the discharge tail gas is up to 80% (mol%); Hydrogen content in the catalytic cracked dry gas is generally at 20%～50% (mol%).The recycling of hydrogen in these tail gas not only can significantly reduce the consumption of hydrogen feedstock, reduces the hydrogen manufacturing cost, and the recycling of realizing refinery gas is all had very significant meaning.
Transformation adsorbed gas isolation technics (PSA) is to rely on the variation of pressure to realize the absorption of gas and regeneration, has characteristics such as reproduction speed is fast, energy consumption is low, simple to operate, stable.China introduces external PSA since early 1980s and puies forward the hydrogen technology, as the Shanghai petrochemical industry, raise sub-petrochemical industry, Maoming petrochemical industry, Liaoyang chemical fibre etc.Since early 1990s the PSA technology developed voluntarily of China be used for the recovery of refinery gas hydrogen.At present, the PSA technology of China is ripe, and for the hydroforming gas of PETROLEUM PROCESSING enterprise of the tens of family of China and catalytic cracked dry gas etc. provide hydrogen to reclaim service, production scale can substitute import fully in continuous expansion.The PSA method has two advantages: the one, and the removal efficiency height to impurity can satisfy the requirement of any technology, and the 2nd, can produce high-purity hydrogen.This method is applicable to from hydrogen concentration greater than extracting the higher hydrogen-rich gas of concentration the unstripped gas of 40% (mol%).Can be more than the hydrogen upgrading to 99.9% (mol%); Hydrogen recovery rate is about about 85%～90%.And because hydrogen is non-stripping gas, when the content lower (being lower than 40%) of hydrogen, make that the amount of the adsorbent that PSA needs is very big, thereby investment, occupation of land, the energy consumption of device are all corresponding bigger.
Membrane separation technique has been widely used in ethene, propylene, lighter hydrocarbons, oil gas and hydrogen and has reclaimed, China reclaims nearly 30 covers of device of hydrogen in the refinery gas, adopts membrane technology at refinery's low pressure (existing application example of recover hydrogen in the dry gas of 0.8MPa～1.2MPa) especially over the past two years.Membrane separation process is applicable to from hydrogen concentration greater than extracting the higher hydrogen-rich gas of concentration the refinery gas of 35% (mol%).Can be according to the composition of unstripped gas, hydrogen upgrading to 90%～99% (mol%); Hydrogen recovery rate is about 80%～90% (mol%).The gas film separating technology have take up an area of little, energy consumption is low, simple operation and other advantages.
Adopt membrane separation technique separately, be not suitable for and density of hydrogen in the oil refinery dry gas be lower than hydrogen reclaims in the gas of 35% (mol%), be difficult to carry dense to more than 90% (mol%), if but utilize transformation adsorbed gas isolation technics to reclaim the hydrogen of this concentration separately, invest hugely, lost the economic implications of recover hydrogen.Therefore the hydrogen that is lower than in the oil refinery dry gas of 35% (mol%) for hydrogen concentration does not at present also have cost-effective recovering means.
Summary of the invention
The object of the present invention is to provide the recovery technology of hydrogen in a kind of oil refinery dry gas, utilizing this technology can be more than the hydrogen upgrading to 95% (mol%) in the oil refinery dry gas of 20%～35% (mol%) with hydrogen concentration.
The technical solution used in the present invention is the reclaiming hydrogen in refinery dry gas of integrated film separation and adsorption gas separating technology, and its process is:
(1) at first, utilizing film separation unit is that 20%～35% oil refinery dry gas carries out pre-separation with the hydrogen molar content, makes H2 in the oil refinery dry gas be enriched in the per-meate side (membrane permeate gas) of film;
(2) then, the gas pressurized that is rich in hydrogen after the per-meate side enrichment of film in the film separation unit behind 1.0MPa～1.2MPa, is entered psa unit;
(3) last, utilize the hydro carbons that contains in the further adsorbed gas of psa unit, make H
2Purity reach 95%～99.5% by mole percentage, pressure remains on 0.9MPa～1.1MPa, sends as hydrogen product.
Oil refinery dry gas also carried out demist before advancing film separation unit handles to remove condensable liquid.Also need to carry out filtration treatment to remove particle, avoid the film in the polluted membrane unit greater than 0.01 μ m.Oil refinery dry gas also needs to be preheated to earlier more than the dew-point temperature before entering film separation unit, avoids the infringement of liquid hydrocarbon to film.
Film in film separation unit oozes stripping gas in residual air and the psa unit can be sent into the gas pipe network as tail gas and focus on.
Film separates and pressure swing adsorption all has its best applications scope, optimum technique for applying, though it is unsatisfactory or economical inadequately no matter to be that membrane separation technique or pressure swing adsorption are lower than the refining effect of hydrogen in 35% the oil refinery dry gas for density of hydrogen, but the present invention utilizes film separation/pressure swing adsorption organic integration technology can give full play to the advantage of each monotechnics, original density of hydrogen can be lower than hydrogen in 35% the oil refinery dry gas reclaims and is purified to 95% (mol%), be the effective technology means that solve the oil refinery dry gas resource, can enlarge the range of application of from oil refinery dry gas, extracting hydrogen, resource is utilized effectively.
Description of drawings
Fig. 1 is that certain factory's film separation/transformation adsorbing integration technology hydrogen reclaims technological process and material balance schematic diagram.
The specific embodiment
Calculated examples below by the comprehensive reutilization of certain plant catalytic dry gas describes in further detail the present invention.
Hydrogen content is molar percentage in the following calculated examples:
At present, certain refinery's three catalysis drying gas amount is 141.4t/d (7000Nm
3/ h), all entering the gas pipe network, four catalysis drying gas amounts are 482.4t/d (25000Nm
3/ h), wherein there is 295t/d to advance triphen, 187.4t/d enters the gas pipe network; According to the too high problem of the present hydrogen manufacturing cost of the said firm, the hydrogen in three catalysis, four catalysis drying gas is recycled, with minimizing hydrogen feedstock consumption and reduction hydrogen cost, and assurance reaches the purity (hydrogen purity 〉=95%) of customer requirements hydrogen.
Specifically technological process is as shown in Figure 1:
Three catalysis, four catalysis drying gas at first carry out demist and filter: promptly earlier enter demister respectively and carry out demist, remove most of condensable liquid; The gas that demister comes out enters two-stage filter respectively, further to remove mist of oil and greater than the particle of 0.01 μ m.Through preheater unstripped gas is heated to 75 ℃ respectively again through the dry gas after the demist filtration, makes unstripped gas away from dew point.The gas that heated enters membrane separator through tubular filter to be separated, and at low-pressure side generation hydrogen, it is 84.5% through film separation back hydrogen content that three catalysis drying gas reach 77.2%, four catalysis drying gas through film separation back hydrogen content.The gas that is rich in hydrogen that separates the back low-pressure side through film of three catalysis and four catalysis is pressurized to 1.2MPa again through compressor and advances VPSA Vacuum Pressure Swing Adsorption recovery hydrogen production device.Tail gas after three catalysis drying gas separate through film advances the gas pipeline, and the tail gas after four catalysis drying gas separate through film advances gas pipeline and triphen respectively.
Refinery gas amounts to the about 8379.1Nm of recyclable hydrogen after film separation/transformation absorption integrated technique is handled
3/ h, recover hydrogen purity 〉=95%, pressure 1.15MPa.The VPSA stripping gas advances the gas pipeline.
The result of each burst parameter of materials comprises that film separates and transformation absorption two parts, lists table 1 and table 2 respectively in.
Table 1 film separating part result
Three catalysis:
Four catalysis:
Table 2 Vacuum Pressure Swing Adsorption result
Illustrate: 1. because hydrogen sulfide adopts dry method to deviate from, this mass balance calculates.
2. to the material in the diesel oil hydrogenation tail gas, divide carbon four and carbon five saturated and unsaturated adding together to calculate.
As seen from the above table, three, four catalysis drying gas separate/transformation absorption integrated technique recyclable hydrogen 8379Nm with diesel oil hydrogenation tail gas through film
3/ h (hydrogen purity 〉=95%), gross investment about 2,700 ten thousand (not containing booster pump and civil engineering expense), device builds up the back operation and can recoup capital outlay less than 1 year.
Utilize film to separate to anticipate catalysis drying gas, not only raw hydrogen concentration and has guaranteed that hydro carbons tail gas does not need supercharging can directly advance the triphen device in the optimum operation scope of PSA, and integrated coupling effect is remarkable.
Technological merit
(1) is applicable to hydrogen content at 20%～35% oil refinery dry gas, hydrogen recovery rate and to reclaim concentration all higher
Hydrogen content after reclaiming with membrane separation process separately, in the situation that guarantees certain rate of recovery, can only bring up to 60%～80% with density of hydrogen at 20%～35% oil refinery dry gas, can not directly be used as hydrogen product. And separately with the method recovery of PSA, because hydrogen is non-stripping gas, the content of hydrogen is low, so that the amount of the adsorbent that PSA needs is very big, thereby investment, occupation of land, the energy consumption of device are all corresponding bigger. And utilize film separation/pressure-variable adsorption integrated technique, and hydrogen recovery rate is reached more than 80%, recover hydrogen concentration reaches more than 95%, can meet the needs of production fully, and small investment, energy consumption is low.
(2) small investment, the total system energy consumption is lower
Integrated technique can take full advantage of the pressure of oil refinery dry gas self and realize membrane separating. At film separation unit, only have preprocessing part, purging and instrument partly to need seldom power consumption. Secondly, through film separation unit, the density of hydrogen of gas brings up to 70%～85% from 20%～35%, and tolerance is about 1/3rd of unstripped gas, enters psa unit again. The raising of density of hydrogen, the minimizing of tolerance are so that all greatly reductions such as the scale of the consumption of adsorbent, psa unit, investment, occupation of land, energy consumptions; At psa unit, because the hydrogen that reclaims is non-desorption gas, the pressure loss is very little, does not need compressor boost or increase pressure seldom just can directly enter the hydrogen pipe network; And ooze residual air (tolerance be about unstripped gas 2/3rds) through what film separation unit separated, almost not loss of pressure can directly enter the gas pipe network or as the raw material of styrene device.
(3) simple to operate, operating cost is low
Equipment is simple and safe, easy to operate, occupation of land is little, and operating cost is low, does not have new pollutant to produce. According to the purity requirement of density of hydrogen, product hydrogen in material gas quantity, unstripped gas square one not, can realize by regulating the methods such as membrane operations parameter.
(4) remarkable in economical benefits
Utilize film separation/pressure-variable adsorption integrated technique that the hydrogen of hydrogen content in 20%～35% oil refinery dry gas is reclaimed, and as the hydrogen product utilization, a large amount of wastes of hydrogen have been avoided, greatly reduced the consumption of hydrogen feedstock in the refinery, reduced the hydrogen cost, it 1 year was recoverable fully invested that remarkable in economical benefits, device are built up rear operation.
Claims (4)
1. reclaiming hydrogen in refinery dry gas, its process is:
(1) at first, utilizing film separation unit is that 20%～35% oil refinery dry gas carries out pre-separation with the hydrogen molar content, makes the H in the oil refinery dry gas
2Be enriched in the per-meate side of film;
(2) then, the gas pressurized that is rich in hydrogen after the per-meate side enrichment of film in the film separation unit behind 1.0MPa～1.2MPa, is entered psa unit;
(3) last, utilize in the psa unit hydro carbons that contains in the further adsorbed gas, make H
2Purity reach 95%～99.5% by mole percentage, pressure remains on 0.9MPa～1.1MPa, sends as hydrogen product.
2. the method for claim 1 is characterized in that: described oil refinery dry gas also carried out demist before advancing film separation unit handles to remove condensable liquid.
3. method as claimed in claim 1 or 2 is characterized in that: described oil refinery dry gas also carried out filtration treatment to remove the particle greater than 0.01 μ m before advancing film separation unit.
4. as claim 1 or 3 described methods, it is characterized in that: described oil refinery dry gas also was preheated to more than the dew-point temperature earlier before entering film separation unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN2010100005914A CN101773765B (en) | 2010-01-14 | 2010-01-14 | Method for reclaiming hydrogen in refinery dry gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010100005914A CN101773765B (en) | 2010-01-14 | 2010-01-14 | Method for reclaiming hydrogen in refinery dry gas |
Publications (2)
| Publication Number | Publication Date |
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| CN101773765A true CN101773765A (en) | 2010-07-14 |
| CN101773765B CN101773765B (en) | 2012-07-25 |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101905112A (en) * | 2010-09-03 | 2010-12-08 | 魏伯卿 | Method and device for separating hydrogen and hydrocarbon in petroleum drying gas by using multi-stage cascade temperature-changing membrane |
| CN103552984A (en) * | 2013-10-30 | 2014-02-05 | 四川天采科技有限责任公司 | Method for producing hydrogen with high yield and high purity by reforming and transforming dry refinery gas |
| CN104030245A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Hydrogen purifying method and device for refinery dry gas after recovery of light olefins with high yield and high purity |
| CN104607000A (en) * | 2015-02-11 | 2015-05-13 | 中凯化学(大连)有限公司 | Method for recovering C2 component, C3 component, light dydrocarbon component and hydrogen gas in refinery dry gas |
| CN106831304A (en) * | 2017-04-01 | 2017-06-13 | 天邦膜技术国家工程研究中心有限责任公司 | A kind of method and device for improving catalysis drying gas ethylbenzene efficiency |
| CN108011119A (en) * | 2017-12-18 | 2018-05-08 | 陕西省石油化工研究设计院 | The method and system of hydrogeneous exhaust gas coupling fuel cells clean electric power generation recycling |
| CN109022033A (en) * | 2017-06-09 | 2018-12-18 | 中石化广州工程有限公司 | A kind of group technology that oil refinery dry gas recycling is isolated |
| CN111467913A (en) * | 2020-03-27 | 2020-07-31 | 大连海奥膜技术有限公司 | Comprehensive recycling process and equipment for refinery tail gas |
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| ES2061189T3 (en) * | 1990-11-16 | 1994-12-01 | Texaco Development Corp | PROCEDURE TO PRODUCE HIGH PURITY HYDROGEN. |
| CN1048417C (en) * | 1992-10-19 | 2000-01-19 | 中国科学院大连化学物理研究所 | Method for separating hydrocarbon from catalytic cracked dry gas |
| US6179900B1 (en) * | 1997-10-09 | 2001-01-30 | Gkss Forschungszentrum Geesthacht Gmbh | Process for the separation/recovery of gases |
| US6589303B1 (en) * | 1999-12-23 | 2003-07-08 | Membrane Technology And Research, Inc. | Hydrogen production by process including membrane gas separation |
| CN1465523A (en) * | 2002-07-02 | 2004-01-07 | 鹰 杨 | Method for refining mixed gas at least containing carbon monoxide, carbon dioxide, nitrogen and hydrogen |
| CN101528591B (en) * | 2006-10-19 | 2012-03-14 | 国际壳牌研究有限公司 | Process for the extraction of hydrogen from a gas mixture |
| CN101525120A (en) * | 2009-04-16 | 2009-09-09 | 罗东晓 | Method for utilizing refinery tail gas and coke oven gas efficiently and rationally |
-
2010
- 2010-01-14 CN CN2010100005914A patent/CN101773765B/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101905112A (en) * | 2010-09-03 | 2010-12-08 | 魏伯卿 | Method and device for separating hydrogen and hydrocarbon in petroleum drying gas by using multi-stage cascade temperature-changing membrane |
| CN103552984A (en) * | 2013-10-30 | 2014-02-05 | 四川天采科技有限责任公司 | Method for producing hydrogen with high yield and high purity by reforming and transforming dry refinery gas |
| CN104030245A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Hydrogen purifying method and device for refinery dry gas after recovery of light olefins with high yield and high purity |
| CN104030245B (en) * | 2014-05-23 | 2016-06-01 | 四川天采科技有限责任公司 | After reclaiming light olefin, in oil refinery dry gas, high receipts rate high purity carries hydrogen methods and device |
| CN104607000A (en) * | 2015-02-11 | 2015-05-13 | 中凯化学(大连)有限公司 | Method for recovering C2 component, C3 component, light dydrocarbon component and hydrogen gas in refinery dry gas |
| CN106831304A (en) * | 2017-04-01 | 2017-06-13 | 天邦膜技术国家工程研究中心有限责任公司 | A kind of method and device for improving catalysis drying gas ethylbenzene efficiency |
| CN109022033A (en) * | 2017-06-09 | 2018-12-18 | 中石化广州工程有限公司 | A kind of group technology that oil refinery dry gas recycling is isolated |
| CN108011119A (en) * | 2017-12-18 | 2018-05-08 | 陕西省石油化工研究设计院 | The method and system of hydrogeneous exhaust gas coupling fuel cells clean electric power generation recycling |
| CN108011119B (en) * | 2017-12-18 | 2020-12-01 | 陕西省石油化工研究设计院 | Method and system for clean power generation and resource utilization of hydrogen-containing waste gas coupled fuel cell |
| CN111467913A (en) * | 2020-03-27 | 2020-07-31 | 大连海奥膜技术有限公司 | Comprehensive recycling process and equipment for refinery tail gas |
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|---|---|
| CN101773765B (en) | 2012-07-25 |
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