CN104419466A - Dry gas recovery system and dry gas recovery method for refinery plant - Google Patents
Dry gas recovery system and dry gas recovery method for refinery plant Download PDFInfo
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- CN104419466A CN104419466A CN201310409583.9A CN201310409583A CN104419466A CN 104419466 A CN104419466 A CN 104419466A CN 201310409583 A CN201310409583 A CN 201310409583A CN 104419466 A CN104419466 A CN 104419466A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
- C10G70/06—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by gas-liquid contact
Abstract
The invention discloses a dry gas recovery system and method for a refinery plant. The system comprises a compressor, an absorption tower, a re-absorption tower, a stripping tower, a cooler, a throttle valve and a flash tank, wherein the compressor is connected with a heat exchanger, and is connected with the absorption tower; the top part of the absorption tower is connected with the re-absorption tower, and the bottom part of the absorption tower is connected with the stripping tower; the cooler, the throttle valve and the flash tank are sequentially connected with the top part of the stripping tower; and the top part of the flash tank is connected with the inlet of the compressor. The method comprises the steps of compressing, cooling, absorbing, stripping and liquefying dry gas of the refinery plant to obtain carbon 2-enriched products. The method has the advantages of a little equipment, low energy consumption, simple flow and high recovery rate, and the product is easy to store and transport.
Description
Technical field
The present invention relates to oil refinery dry gas process field, furtherly, relate to a kind of dry-gas recovery system and dry-gas recovery method.
Background technology
Oil refinery dry gas is mainly derived from the secondary processing process of crude oil, as catalytic cracking, thermally splitting, delayed coking, hydrocracking etc.In general catalysis drying gas, ethylene content is higher, and in coking dry gas, ethane content is higher, about 15% ~ 25%, in addition, also containing alkene alkane such as propylene, propane, butane in oil refinery dry gas.At present, major part refinery of China will burn as fuel gas by oil refinery dry gas, and utility value is lower, and causes the great wasting of resources and environmental pollution.
Ethane is ideal cracking stock, and in steam-cracking process, sizable Partial Conversion becomes ethene.If by the ethane recovery in oil refinery dry gas, be sent to ethylene producing device, not only take full advantage of refinery exhaust resource, and reduce cracking stock cost, embody Integrated Refinery And Petrochemical advantage.But for pure Refining of Petroleum enterprise, due to without ethylene producing device, the rich ethane gas of recovery how to transport and storage is problem in urgent need to solve.
From oil refinery dry gas, the method for recovered ethylene mainly contains separation by deep refrigeration, middle cold oil absorption process, Separation by Complexation method, pressure swing adsorption process etc. at present, and various method differs from one another.Separation by deep refrigeration technical maturity, Recovery rate of ethylene is high, but investment is large, higher for rare ethylene recovery energy consumption; Separation by Complexation method, Recovery rate of ethylene is higher, but requires strict to the impurity in raw material, and pre-treatment costly, needs special complexes absorption; Pressure swing adsorption process is simple to operate, and energy consumption is lower, but product purity is low, and Recovery rate of ethylene is low, and floor space is large.
Middle cold oil absorption process mainly utilizes the different solubility of absorption agent to component each in gas to carry out separating gas mixture, the general heavy constituent first utilizing absorption agent to absorb C2 and more than C2, isolate the non-condensable gases such as methane, hydrogen, then use each component in the agent of rectification method separate absorbent.The method has the features such as small scale, strong adaptability, investment cost be low.
CN1640992 proposes a kind of refrigeration oil absorption process being absorption agent with the self-produced stable light hydrocarbon of device, is applicable to reclaim liquefied gas from associated gas or Sweet natural gas, and C3 yield requires higher recovery process.Adopt the absorption process of this refrigeration oil, with less absorption agent, can obtain higher light hydrocarbon recovery rate, and technique is simple, energy consumption is lower, better economic benefit.But the method is only applicable to reclaim liquefied gas from associated gas or Sweet natural gas, can not reclaim C2 cut, cannot be used for the recovery of plant catalytic dry gas.
US5502971 discloses a kind of low-pressure low-temperature technique reclaiming C2 and more heavy hydrocarbons, is applicable to the recovery of oil refinery dry gas.This technique eliminates traditional high pressure scheme, changes and adopts low-voltage technology, and such recovered temperature just can remain on the temperature of nitric acid resin generation, avoids dangerous Potential feasibility, can also keep higher olefin yields simultaneously.The process employs low pressure scheme, temperature is low reaches-100 DEG C, belongs to the one of deep cooling process for separating, and investment is comparatively large, and energy consumption is higher.
US6308532 proposes a kind of technique of recovered ethylene and propylene from oil refinery dry gas, this technique comprises extracts C3 out from absorption tower reactor, C4, C5, part tower bottoms phase materials is also circulated to tower top by C6 liquid, thus keep the freezing temp of overhead condenser to be not less than-95 DEG C, in absorption tower, be rich in propylene or ethylene-propylene region extraction gas phase side line simultaneously.Although part kettle material is circulated to tower top and is unlikely too low to keep tower top temperature by this technique, tower top temperature is still low reaches-95 DEG C, still belongs to the one of deep cooling process for separating, and therefore invest comparatively large, energy consumption is higher.
CN101063048A discloses the method for cold oil absorption process separating plant catalytic dry gas in a kind of employing, this technique is made up of steps such as compressing, remove sour gas, drying and purification, absorption, desorb, cold recovery and rough segmentation, there is absorption agent with low cost, lose the advantages such as low.But the method absorption agent internal circulating load is large, equipment size is large, and process CIMS is complicated, and product purity is not high.In addition, it is gas phase C-2-fraction and ethane that this technique reclaims products obtained therefrom, can only adopt Cemented filling, cause the suitability of the program to be subject to larger restriction.
In sum, existing oil refinery dry gas recycles the problems such as technique existence investment is large, energy consumption is high, suitability is limited.
Summary of the invention
Recycling the problems such as technique existence investment is large, energy consumption is high, technique suitability is limited for solving existing oil refinery dry gas in prior art, the invention provides a kind of oil refinery dry gas recovery system and dry-gas recovery method.Reclaim carbon two component in dry gas in the present invention with absorption agent, keep absorption temperature at about 15 degree, absorption tower top gas is reclaimed by resorbent mode, absorbs tower bottoms and obtains carbon two concentrated gas by desorb, then carry out cooling liquid.The inventive method equipment is few, and energy consumption is low, and flow process is simple, and the rate of recovery is high, and product is easy to store and transport.
An object of the present invention is to provide a kind of oil refinery dry gas recovery system.
Comprise: compressor, absorption tower, reabsorber, desorption tower, water cooler, throttling valve and flash tank;
Compressor connects absorption tower after connecting interchanger, and top, absorption tower connects reabsorber, and connect Analytic Tower bottom absorption tower, desorption tower top connects water cooler, throttling valve and flash tank successively, and flash drum overhead connects suction port of compressor.
Described absorption tower arranges absorption tower tower reactor reboiler; Analytic Tower arranges Analytic Tower tower reactor reboiler.
The preferred propylene water cooler of water cooler.
Two of object of the present invention is to provide a kind of dry-gas recovery method.
Comprise: oil refinery dry gas is compressed, cooling, absorption, desorb, post liquefaction obtain rich carbon two product.
Specifically comprise the following steps:
1) the compressed pressure of oil refinery dry gas brings up to 3.0 ~ 5.0MPa; Be cooled to 5 ~ 15 DEG C and enter absorption tower;
2) absorption agent sprays into from top, absorption tower, to absorb in oil refinery dry gas C2 cut and more heavy component; Desorption tower is delivered in the tower reactor logistics on absorption tower, and the logistics of tower top unabsorbed gases enters reabsorber;
3) absorption agent enters from reabsorber jacking again, absorbs by the absorption agent taken out of with not by the C2 component absorbed;
4) the C2 concentrated gas that is recycled of desorption tower tower top, the lean solvent that tower reactor obtains, after cooling, returns to top, absorption tower;
5) rich carbon two product is obtained after the further cooling liquid of C2 concentrated gas that desorption tower tower top obtains;
Described absorption agent is the C3 cut containing propane, the C-4-fraction containing normal butane, Trimethylmethane, or the C5 fraction containing Skellysolve A, iso-pentane; Be preferably the C-4-fraction containing normal butane, Trimethylmethane;
Described absorption agent is again gasoline, heavy naphtha or Aromatic raffinate, is preferably the stable gasoline component of refinery.
Concrete technical scheme is as follows:
Oil refinery dry gas of the present invention recycles technique, comprises the following steps:
1) compress: the dry gas pressure produced from the technological process such as refinery catalytic cracking, thermally splitting, delayed coking, hydrocracking is brought up to 3.0 ~ 5.0MPa;
2) cool: the dry gas after the compression obtain described step 1) is cooled to 5 ~ 15 DEG C;
3) absorb: absorption agent sprays into from top, absorption tower, to absorb in oil refinery dry gas C2 cut and more heavy component; Desorption tower process is delivered in the tower reactor logistics on main absorption tower; The logistics of tower top unabsorbed gases enters reabsorber recovery absorption agent wherein;
4) desorb: the tower reactor logistics from absorption tower enters desorption tower, the C2 concentrated gas that tower top is recycled, the lean solvent that tower reactor obtains, after cooling, returns to top, absorption tower and recycles as absorption agent.
5) liquefy: utilize the C2 concentrated gas cooling liquid that desorption tower tower top obtains by propylene refrigerant, then by its throttling expansion to normal pressure, C2 concentrated gas temperature is reduced further, and the logistics after throttling is through flash distillation, after gas-liquid separation, liquid phase is sent to tank field as product.
In compression step, oil refinery dry gas generally needs to improve pressure step by step, and preferred pressure brings up to 3.0 ~ 5.0MPa, and to the hop count compressed, there is no particular limitation, preferably adopts three sections of compressions;
In cooling step, preferably oil refinery dry gas is cooled to 5 ~ 15 DEG C, institute's chilling requirement provides corresponding cold by propylene refrigeration compressor.
In absorption step, the not special requirement of absorption agent consumption on described absorption tower, those skilled in the art can determine according to the general knowledge of prior art.
Described absorption tower Optimization Theory plate number is 25 ~ 60, and working pressure is 3.0 ~ 6.0MPa, and tower top temperature is 10 DEG C ~ 40 DEG C.
The gaseous stream of described absorption tower tower top enters reabsorber, then absorption agent enters from tower top, absorbs by the absorption agent taken out of with not by carbon two component absorbed; Top gaseous phase is directly discharged into fuel gas pipe network, and the extraction of tower reactor liquid phase is sent to outside battery limit (BL);
In desorption procedure, because the pressure and desorption tower carrying out the tower reactor logistics on autonomous absorption tower exists pressure reduction, pressure reduction is therefore relied on to enter desorption tower.
In the method for the invention, the absorption agent after the desorb that obtains of desorption tower tower reactor returns absorption tower recycle after cooling step by step.
In the present invention, absorption agent can enter reabsorber with main absorption top gaseous phase, therefore, preferably introduces one absorption agent as a supplement in desorb tower reactor, with absorptive tower absorbent consumption main in guarantee system.
The number of theoretical plate of preferred described desorption tower is 20 ~ 60, and working pressure is 1.0 ~ 4.0MPa.
In step (5), the further cooling liquid of desorb tower top carbon two concentrated gas, preferably first adopts 0 DEG C and cools with-40 DEG C of level propylene refrigerants, then by being throttled to normal pressure, C2 concentrated gas is cooled further, and the gas phase after throttling returns compressed element circulation, and liquid phase is as product extraction.
The main propylene containing the ethene of 0-40%wt, the ethane of 25-80%wt and 0-20%wt in C2 concentrated gas.
In the present invention, absorption tower tower reactor arranges reboiler, to ensure that absorbing the light constituents such as tower reactor methane, hydrogen drops to below setting requirement.Wherein absorption tower tower reactor reboiler and desorption tower tower reactor reboiler heating medium can adopt low-pressure steam, also can adopt deep fat, preferred deep fat heating, can make full use of the rich heat in refinery, also can reduce process energy consumption.
Method of the present invention can also comprise and removes sour gas step, before entering absorption tower or analytically carry out the process of acid gas removal body after overhead extraction gas phase, amine can be adopted to wash, also alkali cleaning can be adopted to remove sour gas, preferably remove sour gas after desorption, preferred alkali wash acid gas removal body.
Method of the present invention can also comprise drying step.Before drying can be arranged on and enter absorption tower, also can be arranged in step (5) liquefaction process, preferably in concentrated gas liquefaction process, carry out drying: propylene refrigeration compressor can provide the cryogen of two ranks, 0 DEG C and-40 DEG C.In concentrated gas liquefaction process, carry out drying, refer to 0 DEG C of propylene refrigerant by concentrated gas cool after carry out drying.
Oil refinery dry gas Application way of the present invention has following characteristics:
(1) product is liquid phase C2 concentrated gas, is easy to storage and transport, makes the scope of application of this technique more wide.
(2) carbon two concentrate gas liquefaction process adopts propylene refrigerant and throttling valve, and not only saves energy consumption, and decreases ethylene refrigeration compressor whole plant, and investment obviously reduces.
(3) the present invention adopts the low-grade deep fat heating in refinery, and energy consumption reduces greatly.
(4) cold that gas phase C2 concentrate gas and oil refinery dry gas all can use propylene refrigeration compressor to provide cools, a set of refrigeration system not only liquefies the finished product, can provide cold for other users of technique again, plant factor maximizes, and reduces energy consumption and investment.
(5) absorption agent selectivity is better, and each absorption agent assimilation effect is all more satisfactory, according to different manufacturers situation, can select optimum absorption agent.
Accompanying drawing explanation
Fig. 1 is oil refinery dry gas recovery system schematic diagram of the present invention
Description of reference numerals:
1 compressor; 2 interchanger; 3 absorption towers; 4 desorption towers; 5 reabsorbers; 6 water coolers; 7 throttling valve; 8 flash tanks; 9 oil refinery dry gas; 10 supplement absorption agent; 11 absorption agents again; 12 rich carbon two products; 13 fuel gas; 14 richnesses absorption agent again; 15 heavy constituents
Embodiment
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
As shown in Figure 1, a kind of oil refinery dry gas recovery system.Comprise: compressor 1, absorption tower 3, reabsorber 5, Analytic Tower 4, water cooler 6, throttling valve 7 and flash tank 8; Compressor 1 connects absorption tower 3 after connecting interchanger 2, and top, absorption tower 3 connects reabsorber 5, and connect Analytic Tower 4 bottom absorption tower 3, Analytic Tower 4 top connects water cooler 6, throttling valve 7 and flash tank 8 successively, and flash tank 8 top connects compressor 1 entrance.Described absorption tower 3 arranges absorption tower tower reactor reboiler; Analytic Tower 4 arranges Analytic Tower tower reactor reboiler.
Certain oil refinery dry gas composition is as shown in table 1,
Table 1
| Composition | mol％ | kmol／h |
| H2 | 26.18 | 371.06 |
| N2 | 9.48 | 134.37 |
| O2 | 0.00 | 0.00 |
| CO | 0.00 | 0.00 |
| CO2 | 1.37 | 19.45 |
| H2S | 0.00 | 0.00 |
| CH4 | 37.75 | 535.15 |
| C2H6 | 14.76 | 209.18 |
| C2H4 | 2.57 | 36.42 |
| C3H8 | 4.60 | 65.17 |
| C3H6 | 0.36 | 5.07 |
| Trimethylmethane | 1.97 | 27.91 |
| Normal butane | 0.05 | 0.72 |
| Iso-butylene | 0.02 | 0.32 |
| 1-butylene | 0.01 | 0.10 |
| Cis-2-butene | 0.01 | 0.08 |
| Trans-2-butene | 0.01 | 0.16 |
| 1,3-butadiene | 0.00 | 0.00 |
| Skellysolve A | 0.36 | 5.07 |
| Iso-pentane | 0.00 | 0.00 |
| Hexane | 0.15 | 2.14 |
| Water | 0.37 | 5.22 |
Oil refinery dry gas supplied materials is 26700kg/h, and after selecting ether, carbon four is as absorption agent, reclaims the ethane in oil refinery dry gas and ethene.
Oil refinery dry gas reclaims and comprises the following steps:
(1) compress: oil refinery dry gas is sent to compression system, and through two sections of compressions, pressure is increased to 3.9MPa, is cooled to 14 DEG C and enters absorption tower;
(2) absorb: the number of theoretical plate on absorption tower is 33, and working pressure is 3.8MPag, and tower top temperature 20 DEG C of j lyosorptions used are carbon four after ether, and solvent enters in tower from absorbing tower jacking, and dry gas enters from the 19th block of column plate.C2 in dry gas and heavy constituent thereof are got off by solvent absorbing, and from tower reactor extraction, tower top is the light constituent such as methane, hydrogen, and is entrained with a small amount of absorption agent.
(3) desorb: the number of theoretical plate of desorption tower is 40, and working pressure is 2.1MPag.The rich solvent absorbing the component such as C2 in dry gas enters desorption tower from the 15th block of column plate, and the C2 concentrated gas after desorb is from overhead extraction, and lean solvent is cooled to 13 DEG C and returns to absorption tower and recycle after stage-by-stage heat exchange.
(4) absorb again: absorb tower top unabsorbed gases and enter reabsorber, the number of theoretical plate of reabsorber is 20, and working pressure is 3.5MPag.Absorption agent adopts stable gasoline again, enters reabsorber from tower top, and absorb carbon two component and carbon four absorption agent, reabsorber tower reactor is rich gasoline, as the extraction of one of product, is sent to refinery's absorbing-stabilizing system.Reabsorber top gaseous phase is sent to fuel gas pipe network.
(5) liquefy: the C2 concentrated gas propylene refrigerant of desorption tower overhead extraction liquefies, and then by being throttled to normal pressure, carbon two product temperature is reduced further, and the liquid phase after throttling is as product extraction, and gas phase returns compressed element.
The C-2-fraction composition obtained is as table 2.
Table 2 carbon two product forms
| Composition | wt％ | kg／h |
| Methane | 0.17 | 16.84 |
| Ethane | 59.93 | 6034.79 |
| Ethene | 5.57 | 561.09 |
| Propane | 24.64 | 2481.17 |
| Propylene | 1.95 | 196.31 |
| Carbon four | 7.74 | 779.66 |
In the present embodiment, carbon two rate of recovery is 91%.
Claims (10)
1. an oil refinery dry gas recovery system, is characterized in that described system comprises:
Compressor, absorption tower, reabsorber, Analytic Tower, water cooler, throttling valve and flash tank;
Compressor connects absorption tower after connecting interchanger, and top, absorption tower connects reabsorber, and connect Analytic Tower bottom absorption tower, Analytic Tower top connects water cooler, throttling valve and flash tank successively, and flash drum overhead connects suction port of compressor.
2. oil refinery dry gas recovery system as claimed in claim 1, is characterized in that:
Described absorption tower arranges absorption tower tower reactor reboiler; Desorption tower arranges desorption tower tower reactor reboiler.
3. oil refinery dry gas recovery system as claimed in claim 2, is characterized in that:
Reboiler adopts refinery's deep fat heating.
4. adopt a dry-gas recovery method for the oil refinery dry gas recovery system as described in one of claims 1 to 3, it is characterized in that described method comprises:
Oil refinery dry gas is compressed, cooling, absorption, desorb, post liquefaction obtain rich carbon two product.
5. dry-gas recovery method as claimed in claim 4, is characterized in that described method comprises:
1) the compressed pressure of oil refinery dry gas brings up to 3.0 ~ 5.0MPa; Be cooled to 5 ~ 15 DEG C and enter absorption tower;
2) absorption agent sprays into from top, absorption tower, to absorb in oil refinery dry gas C2 cut and more heavy component; Desorption tower is delivered in the tower reactor logistics on absorption tower, and the logistics of tower top unabsorbed gases enters reabsorber;
3) absorption agent enters from reabsorber jacking again, absorbs by the absorption agent taken out of with not by the C2 component absorbed;
4) the C2 concentrated gas that is recycled of desorption tower tower top, the lean solvent that tower reactor obtains, after cooling, returns to top, absorption tower;
5) the C2 concentrated gas that desorption tower tower top obtains obtains rich carbon two product after cooling liquid;
Described absorption agent is the C3 cut containing propane, the C-4-fraction containing normal butane, Trimethylmethane, or the C5 fraction containing Skellysolve A, iso-pentane;
Described absorption agent is again gasoline, heavy naphtha or Aromatic raffinate.
6. dry-gas recovery method as claimed in claim 5, is characterized in that:
Described absorption agent is the C-4-fraction containing normal butane, Trimethylmethane;
Described absorption agent is again gasoline.
7. dry-gas recovery method as claimed in claim 5, is characterized in that:
The number of theoretical plate on described absorption tower is 25 ~ 60, and working pressure is 3.0 ~ 6.0MPa, and tower top temperature is 10 DEG C ~ 40 DEG C;
The number of theoretical plate of described desorption tower is 20-60, and working pressure is 1.0-4.0MPa.
The number of theoretical plate of described reabsorber is 10-50, and working pressure is 1.0-4.0MPa.
8. dry-gas recovery method as claimed in claim 5, is characterized in that:
Oil refinery dry gas before entering absorption tower or analytically carries out the process of acid gas removal body after overhead extraction gas phase;
Oil refinery dry gas carries out drying before entering absorption tower or when the cooling liquid of C2 concentrated gas.
9. dry-gas recovery method as claimed in claim 5, is characterized in that:
Cooling in step 5) first adopts 0 DEG C and-40 DEG C of level propylene refrigerant coolings respectively, and then by the throttling expansion of C2 concentrated gas to normal pressure, C2 concentrated gas temperature is reduced further.
10. the dry-gas recovery method as described in one of claim 5-9, is characterized in that:
Propylene containing the ethene of 0-40wt%, the ethane of 25-80wt% and 0-20wt% in C2 concentrated gas.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107987886A (en) * | 2016-10-26 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of apparatus and method that carbon two is recycled from catalysis drying gas |
| CN107987884A (en) * | 2016-10-26 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of apparatus and method that carbon two is recycled from catalysis drying gas |
| CN108014599A (en) * | 2016-11-02 | 2018-05-11 | 中国石油化工股份有限公司 | C in a kind of broken coal low-temperature methanol washing tail-gas2+The system and method for removing and the recycling of hydrocarbon |
| CN112410070A (en) * | 2020-10-15 | 2021-02-26 | 大连理工大学 | Energy-saving process and device for recovering carbon dioxide from refinery dry gas |
| CN113755199A (en) * | 2020-06-03 | 2021-12-07 | 中国石油化工股份有限公司 | Method for recovering carbon two and carbon three in dry gas, system and application thereof |
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| CN107987886A (en) * | 2016-10-26 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of apparatus and method that carbon two is recycled from catalysis drying gas |
| CN107987884A (en) * | 2016-10-26 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of apparatus and method that carbon two is recycled from catalysis drying gas |
| CN107987886B (en) * | 2016-10-26 | 2020-09-15 | 中国石油化工股份有限公司 | Device and method for recovering carbon dioxide from catalytic dry gas |
| CN107987884B (en) * | 2016-10-26 | 2020-09-15 | 中国石油化工股份有限公司 | Device and method for recovering carbon dioxide from catalytic dry gas |
| CN108014599A (en) * | 2016-11-02 | 2018-05-11 | 中国石油化工股份有限公司 | C in a kind of broken coal low-temperature methanol washing tail-gas2+The system and method for removing and the recycling of hydrocarbon |
| CN113755199A (en) * | 2020-06-03 | 2021-12-07 | 中国石油化工股份有限公司 | Method for recovering carbon two and carbon three in dry gas, system and application thereof |
| CN113755199B (en) * | 2020-06-03 | 2023-07-21 | 中国石油化工股份有限公司 | Method for recycling second carbon and third carbon in dry gas, system and application thereof |
| CN112410070A (en) * | 2020-10-15 | 2021-02-26 | 大连理工大学 | Energy-saving process and device for recovering carbon dioxide from refinery dry gas |
| CN115253604A (en) * | 2022-08-09 | 2022-11-01 | 大连理工大学 | Device and method for separating three dry gases rich in carbon and carbon by NMP |
| CN115253604B (en) * | 2022-08-09 | 2024-01-26 | 大连理工大学 | Device and method for separating carbon-rich two-carbon three-dry gas by NMP |
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