CN104419465B - A kind of oil refinery dry gas recovery system and dry-gas recovery method - Google Patents
A kind of oil refinery dry gas recovery system and dry-gas recovery method Download PDFInfo
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- CN104419465B CN104419465B CN201310409493.XA CN201310409493A CN104419465B CN 104419465 B CN104419465 B CN 104419465B CN 201310409493 A CN201310409493 A CN 201310409493A CN 104419465 B CN104419465 B CN 104419465B
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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
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of oil refinery dry gas recovery system and method.Described system includes: compressor, absorption tower, reabsorber, Analytic Tower, liquefaction cooler and flash tank；Compressor connects absorption tower after connecting heat exchanger, and top, absorption tower connects reabsorber, connects Analytic Tower bottom absorption tower, and Analytic Tower top is sequentially connected with liquefaction cooler and flash tank, and flash drum overhead connects suction port of compressor.Method includes: oil refinery dry gas is compressed, cool down, absorb, resolve, liquefy after obtain rich carbon two product.The inventive method equipment is few, and energy consumption is low, and flow process is simple, and the response rate is high, and product is easily stored and transports.
Description
Technical field
The present invention relates to oil refinery dry gas process field, furtherly, relate to a kind of oil refinery 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, such as catalytic cracking, thermal cracking, delay coke
Change, be hydrocracked.In general catalysis drying gas, ethylene contents is higher, and in coking dry gas, ethane content is higher,
15%～about 25%, additionally, possibly together with 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 value is relatively low, and causes greatly
The wasting of resources and environmental pollution.
Ethane is ideal cracking stock, and in steam-cracking process, sizable Partial Conversion becomes
Ethylene.If by the ethane recovery in oil refinery dry gas, being sent to ethylene producing device, not only take full advantage of refinery
Tail gas resource, and reduce cracking stock cost, embody Integrated Refinery And Petrochemical advantage.But, for pure
From the point of view of Refining of Petroleum enterprise, owing to without ethylene producing device, how the rich ethane gas of recovery transports and storage is anxious
The problem needing to solve.
The method reclaiming ethylene at present from oil refinery dry gas mainly has separation by deep refrigeration, middle cold oil absorption process, network
Closing partition method, pressure swing adsorption method etc., various methods differ from one another.Separation by deep refrigeration technical maturity, ethylene returns
Yield is high, but investment is big, higher for dilute ethylene recovery energy consumption；Separation by Complexation method, Recovery rate of ethylene is higher,
But requiring the impurity in raw material strict, pretreatment costly, needs special complexes absorption；Transformation
Absorption method is simple to operate, and energy consumption is relatively low, but product purity is low, and Recovery rate of ethylene is low, and floor space is big.
Middle cold oil absorption process separates gas mainly by absorbent to the different solubility of component each in gas
Mixture, typically absorbs the heavy constituent of C2 and more than C2, isolates methane, hydrogen etc. first with absorbent
Incoagulable gas, then by each component in rectification method separate absorbent agent.The method has small scale, adaptability
The feature such as by force, investment cost is low.
CN1640992 proposes a kind of refrigeration oil absorption process with the self-produced stable light hydrocarbon of device as absorbent,
Be applicable to recovered liquid activating QI from associated gas or natural gas, and C3 yield requires higher recovery process.
Use the absorption process of this refrigeration oil, less absorbent can be used, it is thus achieved that higher light hydrocarbon recovery rate, and
Technique is simple, and energy consumption is relatively low, better economic benefit.But the method is only applicable to from associated gas or natural
Recovered liquid activating QI in gas, can not reclaim C2 fraction, it is impossible to for the recovery of plant catalytic dry gas.
US5502971 discloses a kind of low-pressure low-temperature technique reclaiming C2 and more heavy hydrocarbons, it is adaptable to refinery
The recovery of dry gas.This technique eliminates traditional high pressure scheme, changes and uses low-voltage technology, so reclaims temperature
Degree is maintained on the temperature that nitric acid resin generates, it is to avoid dangerous Potential feasibility, also simultaneously
Higher olefin yields can be kept.The process employs low pressure scheme, temperature is low reaches-100 DEG C, belongs to deep cooling
The one of separating technology, investment is relatively big, and energy consumption is higher.
US6308532 proposes a kind of recovery ethylene and technique of propylene from oil refinery dry gas, and this technique includes
Extracting C3 out from absorbing tower reactor, part tower bottoms phase materials is also recycled to tower top, thus protects by C4, C5, C6 liquid
The cryogenic temperature holding overhead condenser is not less than-95 DEG C, simultaneously rich in propylene or ethylene-propylene district in absorption tower
Gas phase side line is extracted in territory out.Will not with holding tower top temperature although part kettle material is recycled to tower top by this technique
In too low, but tower top temperature is the lowest reaches-95 DEG C, still falls within the one of deep cooling process for separating, therefore invests relatively big,
Energy consumption is higher.
CN101063048A discloses a kind of method of cold oil absorption process separating plant catalytic dry gas in using,
This technique is by compressing, remove sour gas, being dried and purification, absorption, desorbing, cold recovery and rough segmentation etc.
Step forms, and has absorbent with low cost, loses the advantages such as low.But, the method absorbent circulating load
Greatly, equipment size is big, and process CIMS is complicated, and product purity is the highest.Additionally, this technique reclaims products obtained therefrom
For gas phase C-2-fraction and ethane, pipeline can only be used to carry, cause the suitability of the program by the relatively day of one's doom
System.
In sum, the existence investment of existing oil refinery dry gas recycling technique is big, energy consumption is high, the suitability is subject to
The problems such as limit.
Summary of the invention
In order to solve in prior art, the existence investment of existing oil refinery dry gas recycling technique is big, energy consumption is high, technique
The problems such as the suitability is limited, the invention provides a kind of oil refinery dry gas recovery system and dry-gas recovery method.This
Invention reclaims with absorbent carbon two component in dry gas, keeps absorbing temperature at about 15 degree, absorption tower
Top gas is reclaimed by resorbent mode, absorbs tower bottoms and obtains carbon two concentrated gas by desorbing, then carries out cold
But liquefy.The inventive method equipment is few, and energy consumption is low, and flow process is simple, and the response rate is high, product easily stored and
Transport.
An object of the present invention is to provide a kind of oil refinery dry gas recovery system.
Including: compressor, absorption tower, reabsorber, Analytic Tower, liquefaction cooler and flash tank；
Compressor connects absorption tower after connecting heat exchanger, and top, absorption tower connects reabsorber, connects bottom absorption tower
Connecing Analytic Tower, Analytic Tower top is sequentially connected with liquefaction cooler and flash tank, and flash drum overhead connects compressor
Entrance.
Described absorption tower arranges absorption tower tower reactor reboiler；Reboiler uses refinery's deep fat heating.
Liquefaction cooler preferably employs: propylene cooler and ethylene chiller.
The two of the purpose of the present invention are to provide a kind of dry-gas recovery method.
Including: oil refinery dry gas is compressed, cool down, absorb, resolve, liquefy after obtain rich carbon two product.
Specifically include following steps:
1) the compressed pressure of oil refinery dry gas brings up to 3.0～5.0MPa；It is cooled to 5～15 DEG C and enters absorption tower；
2) absorbent sprays into from top, absorption tower, absorbs C2 fraction and more heavy component in oil refinery dry gas；Absorb
Desorber is delivered in the tower reactor logistics of tower, and tower top unabsorbed gases logistics enters reabsorber；
3) re-absorption agent enters from reabsorber jacking, absorbs the absorbent that is carried over and is not got off by absorption
C2 component；
4) the C2 concentrated gas that desorber tower top is recycled, the lean solvent that tower reactor obtains after cooling,
Return to top, absorption tower；
5) rich carbon two product is obtained after the cooled liquefaction of C2 concentrated gas that desorber tower top obtains.
Described absorbent is the C3 fraction containing propane, containing normal butane, the C-4-fraction of iso-butane, or
Containing pentane, the C5 fraction of isopentane；It is preferably containing normal butane, the C-4-fraction of iso-butane；
Described re-absorption agent is gasoline, heavy naphtha or Aromatic raffinate, preferably gasoline, more preferably refinery
Stable gasoline component.
Concrete technical scheme is as follows:
(1) compression: will from refinery catalytic cracking, thermal cracking, delayed coking, the technique mistake such as be hydrocracked
The dry gas that journey produces, pressure brings up to 3.0～5.0MPa；
(2) cooling: the dry gas after the compression obtain described step 1) is cooled to 5～15 DEG C；
(3) absorb: absorbent sprays into from top, absorption tower, absorb in oil refinery dry gas C2 fraction and more recombinate
Part；The tower reactor logistics on absorption tower is delivered to desorber and is processed；Tower top unabsorbed gases logistics enters re-absorption
Tower reclaims absorbent therein；
(4) desorbing: the tower reactor logistics from absorption tower enters desorber, and the C2 that tower top is recycled concentrates
Gas, the lean solvent that tower reactor obtains, after cooling, returns to top, absorption tower and recycles as absorbent.
(5) liquefaction: be utilized respectively propylene refrigerant and ethylene cryogen, the C2 obtained by desorber tower top concentrates
It is sent to tank field as product after the cooled liquefaction of gas.
In compression step, oil refinery dry gas is it is generally required to improve pressure, preferably pressure step by step and bring up to
3.0～5.0MPa, to the hop count compressed, there is no particular limitation, it is preferred to use three sections of compressions；
In cooling step, preferably oil refinery dry gas being cooled to 5～15 DEG C, institute's chilling requirement is by propylene refrigeration compressor
Machine provides corresponding cold.
In absorption step, described absorbent can be the C3 fraction containing propane, containing normal butane, isobutyl
The C-4-fraction of alkane, or containing pentane, the C5 fraction of isopentane.Preferably comprise normal butane, isobutyl
The C-4-fraction of alkane.
In the method for the invention, to the not particularly requirement of absorbent consumption, those skilled in the art are permissible
General knowledge according to prior art determines.
Described absorption tower Optimization Theory plate number is 25～60, and operation 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, and re-absorption agent enters from tower top, absorbs quilt
The absorbent taken out of and carbon two component do not got off by absorption, reabsorber top gaseous phase is directly discharged into fuel gas
Pipe network, tower reactor liquid phase extraction is sent to outside battery limit (BL)；Described re-absorption agent is gasoline, or heavy naphtha, aromatic hydrocarbons
Raffinate oil, preferably the stable gasoline component of refinery.
The number of theoretical plate of the most described reabsorber is 10-50, and operation pressure is 1.0-4.0MPa.
In desorption procedure, owing to there is pressure reduction from the pressure of the tower reactor logistics on absorption tower and desorber, because of
This relies on pressure reduction can enter desorber.Absorbent after the desorbing that desorber tower reactor obtains is after cooling step by step
Return absorption tower recycles.Absorbent can enter reabsorber with absorbing top gaseous phase, it is therefore preferable that
Desorbing tower reactor introduce one absorbent as supplement, with absorptive tower absorbent consumption in guarantee system.
The number of theoretical plate of the most described desorber is 20-60, and operation pressure is 1.0-4.0MPa.
In liquefaction step, the desorbing tower top carbon two further cooling liquid of concentrated gas, the most first use 0 DEG C and-40 DEG C
Level propylene refrigerant cools down step by step, the most again with-100 DEG C of ethylene cryogen coolings, is cooled down further by C2 concentrated gas,
The gas phase wherein not cooled down returns compression unit circulation, and liquid phase is as product extraction.0 DEG C and-40 DEG C of level propylene
Cryogen ,-100 DEG C of ethylene cryogens are by propylene refrigeration compressor, ethylene refrigeration compressor, or binary refrigeration compression
Machine provides.
C2 concentrated gas mainly contains the ethylene of 0-40wt%, the ethane of 25-80wt% and the propylene of 0-20wt%.
In the present invention, absorption tower tower reactor arranges reboiler, to ensure to absorb the light component such as tower reactor methane, hydrogen
Drop to set below requirement.Wherein to add thermal medium permissible for absorption tower tower reactor reboiler and desorber tower reactor reboiler
Use low-pressure steam, it would however also be possible to employ deep fat, preferably deep fat heating, refinery's affluence heat can be made full use of,
Also process energy consumption can be reduced.
If it is required, the method for the present invention also includes removing sour gas step, before fingering enters absorption tower
Or after desorber, carry out de-Sour gas disposal, amine can be used to wash, it would however also be possible to employ alkali cleaning removes
Sour gas, removes sour gas, preferably alkali wash the most after desorption and takes off sour gas.
The method of the present invention also includes drying steps.It is dried before can being arranged on entrance absorption tower, it is also possible to
It is arranged in liquefaction process, is preferably dried in C2 concentrated gas liquefaction process: propylene refrigeration compressor can
To provide the cryogen of two ranks, 0 DEG C and-40 DEG C.C2 concentrated gas liquefaction process is dried, refers to
It is dried after concentration air cooling with 0 DEG C of propylene refrigerant.
The oil refinery dry gas Application way of the present invention has the following characteristics that
1) product is liquid phase C2 concentrated gas, it is easy to stores and transports so that the scope of application of this technique is wider
Wealthy.
2) present invention uses refinery's low-grade deep fat heating, and energy consumption is substantially reduced.
3) cold that gas phase C2 concentrated gas and oil refinery dry gas can all use propylene refrigeration compressor to provide is carried out
Cooling, a set of refrigeration system not only liquefies final products, can be again that other users of technique provide cold, if
Standby utilization rate maximizes, and reduces energy consumption and investment.
4) absorbent selectivity is relatively big, and each absorbent assimilation effect is the most more satisfactory, can be according to difference
Producer's situation, selects optimum absorbent.
Accompanying drawing explanation
Fig. 1 is the oil refinery dry gas recovery system schematic diagram of the present invention.
Description of reference numerals:
1 compressor；2 heat exchangers；3 absorption towers；4 desorbers；5 reabsorbers；6 propylene refrigerant coolers；
7 ethylene cryogen coolers；8 flash tanks；9 oil refinery dry gas；10 supplement absorbent；11 re-absorption agent；12
Rich carbon two product；13 fuel gas；14 rich re-absorption agent；15 heavy constituents
Detailed description of the invention
Below in conjunction with embodiment, further illustrate the present invention.
Embodiment:
As it is shown in figure 1, a kind of oil refinery dry gas recovery system.Including: compressor 1, absorption tower 3, re-absorption
Tower 5, Analytic Tower 4, propylene refrigerant cooler 6, ethylene cryogen cooler 7 and flash tank 8；
Compressor 1 connects absorption tower 3 after connecting heat exchanger 2, and top, absorption tower 3 connects reabsorber 5, inhales
Receiving and connect Analytic Tower 4 bottom tower 3, Analytic Tower 4 top is sequentially connected with propylene refrigerant cooler 6, ethylene cryogen
Cooler 7 and flash tank 8, flash tank 8 top connects compressor 1 entrance；Described absorption tower 2 arranges absorption
Tower tower reactor reboiler；Analytic Tower 4 arranges Analytic Tower tower reactor reboiler.
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 |
| Iso-butane | 1.97 | 27.91 |
| Normal butane | 0.05 | 0.72 |
| Isobutene. | 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 |
| Pentane | 0.36 | 5.07 |
| Isopentane | 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 absorbent, reclaims in oil refinery dry gas
Ethane and ethylene.
Comprise the following steps:
(1) compression: oil refinery dry gas is sent to compressibility, compresses through two-stage nitration, and pressure is increased to 3.9MPa,
It is cooled to 14 DEG C and enters absorption tower；
(2) absorb: the number of theoretical plate on absorption tower is 33, and operation pressure is 3.8MPag, tower top temperature 20 DEG C；
Lyosoption used is carbon four after ether, and solvent enters in tower from absorbing tower jacking, and dry gas enters from the 18th block of column plate
Enter.C2 and heavy constituent thereof in dry gas are got off by solvent absorption, and from tower reactor extraction, tower top is methane, hydrogen
Etc. light component, and it is entrained with a small amount of absorbent.
(3) desorbing: the number of theoretical plate of desorber is 40, operation pressure is 2.1MPag, the C2 after desorbing
Concentrated gas is from overhead extraction, and lean solvent is cooled to 13 DEG C after stage-by-stage heat exchange and returns absorption tower recycling.
(4) re-absorption: absorb tower top unabsorbed gases and enter reabsorber, the theoretical plate of reabsorber
Number is 20, and operation pressure is 3.5MPag.Re-absorption agent uses stable gasoline, enters reabsorber from tower top,
Absorbing carbon two component and carbon four absorbent, reabsorber tower reactor is rich gasoline, as the extraction of one of product, send
Toward refinery's absorbing-stabilizing system.Reabsorber top gaseous phase is sent to Hydrogen Unit, therefrom separates hydrogen product,
Remaining fuel pneumatic transmission is toward fuel gas pipe network.
(5) liquefaction: the C2 concentrated gas of desorber overhead extraction is first carried out with 0 DEG C and-40 DEG C of level propylene refrigerants
Cooling, then continues cooling with-100 DEG C of level ethylene cryogens, and gas phase therein returns compression unit, liquid phase conduct
Rich carbon two product extraction.
Obtained rich carbon two product composition is shown in Table 2.
Table 2
| Composition | wt% | kg/h |
| Methane | 1.15 | 116.39 |
| Ethane | 61.29 | 6187.92 |
| Ethylene | 7.38 | 745.06 |
| Propane | 24.74 | 2498.19 |
| Propylene | 1.96 | 197.44 |
| Carbon four | 3.48 | 351.33 |
In the present embodiment, carbon two response rate is 95%.
Claims (10)
1. an oil refinery dry gas recovery system, it is characterised in that described system includes:
Compressor, absorption tower, reabsorber, Analytic Tower, liquefaction cooler and flash tank；
Compressor connects absorption tower after connecting heat exchanger, and top, absorption tower connects reabsorber, connects bottom absorption tower
Connecing Analytic Tower, Analytic Tower top is sequentially connected with liquefaction cooler and flash tank, and flash drum overhead connects compressor
Entrance；
Described liquefaction cooler uses propylene cooler and ethylene chiller.
2. oil refinery dry gas recovery system as claimed in claim 1, it is characterised in that:
Described absorption tower arranges absorption tower tower reactor reboiler.
3. oil refinery dry gas recovery system as claimed in claim 2, it is characterised in that:
Reboiler uses refinery's deep fat heating.
4. a dry-gas recovery method for employing oil refinery dry gas recovery system as described in one of claims 1 to 3,
It is characterized in that described method includes:
Oil refinery dry gas is compressed, cool down, absorb, resolve, liquefy after obtain rich carbon two product.
5. dry-gas recovery method as claimed in claim 4, it is characterised in that described method includes:
1) the compressed pressure of oil refinery dry gas brings up to 3.0～5.0MPa；It is cooled to 5～15 DEG C and enters absorption tower；
2) absorbent sprays into from top, absorption tower, absorbs C2 fraction and more heavy component in oil refinery dry gas；Absorb
Desorber is delivered in the tower reactor logistics of tower, and tower top unabsorbed gases logistics enters reabsorber；
3) re-absorption agent enters from reabsorber jacking, absorbs the absorbent that is carried over and is not got off by absorption
C2 component；
4) the C2 concentrated gas that desorber tower top is recycled, the lean solvent that tower reactor obtains after cooling,
Return to top, absorption tower；
5) rich carbon two product is obtained after the cooled liquefaction of C2 concentrated gas that desorber tower top obtains；
Described absorbent is the C3 fraction containing propane, containing normal butane, the C-4-fraction of iso-butane, or
Containing pentane, the C5 fraction of isopentane；
Described re-absorption agent is gasoline, heavy naphtha or Aromatic raffinate.
6. dry-gas recovery method as claimed in claim 5, it is characterised in that:
Described absorbent is containing normal butane, the C-4-fraction of iso-butane；
Described re-absorption agent is gasoline.
7. dry-gas recovery method as claimed in claim 5, it is characterised in that:
The number of theoretical plate on described absorption tower is 25～60, and operation pressure is 3.0～6.0MPa, and tower top temperature is
10 DEG C～40 DEG C；
The number of theoretical plate of described desorber is 20-60, and operation pressure is 1.0-4.0MPa；
The number of theoretical plate of described reabsorber is 10-50, and operation pressure is 1.0-4.0MPa.
8. dry-gas recovery method as claimed in claim 5, it is characterised in that:
Oil refinery dry gas carries out de-Sour gas disposal before entering absorption tower or after Analytic Tower；
It is dried when oil refinery dry gas is before entering absorption tower or in C2 concentrated gas cooling liquid.
9. dry-gas recovery method as claimed in claim 5, it is characterised in that:
Step 5) in cooling be first to be respectively adopted 0 DEG C and-40 DEG C of level propylene refrigerants cool down step by step, use the most again
-100 DEG C of ethylene cryogen coolings.
10. the dry-gas recovery method as described in one of claim 5-9, it is characterised in that:
Containing the ethylene of 0-40wt%, the ethane of 25-80wt% and the propylene of 0-20wt% in C2 concentrated gas.
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| CN105505440B (en) * | 2015-12-16 | 2017-09-26 | 华南理工大学 | Lean gas reabsorbs unit and flow in a kind of absorbing-stabilizing system |
| CN107986932B (en) * | 2016-10-26 | 2020-07-24 | 中国石油化工股份有限公司 | Device and method for recycling carbon dioxide from byproduct dry gas generated in preparation of aromatic hydrocarbon from methanol |
| CN107827698B (en) * | 2017-12-01 | 2020-08-04 | 北京石油化工工程有限公司 | Non-cryogenic separation method and system for ethylene-containing pyrolysis gas |
| CN112920830B (en) * | 2019-12-05 | 2023-06-30 | 中国石油天然气股份有限公司 | Method for recovering C2 fraction in refinery dry gas |
| CN113387769A (en) * | 2021-03-19 | 2021-09-14 | 北京欧谊德科技有限公司 | Separation method for recovering C1, C2 and C3 in refinery saturated dry gas by combined absorption method |
| CN113354506B (en) * | 2021-03-19 | 2023-02-28 | 北京欧谊德科技有限公司 | Method for recovering and separating low-carbon hydrocarbons from refinery saturated dry gas by combined absorption |
| CN113121301B (en) * | 2021-05-18 | 2022-10-28 | 北京欧谊德科技有限公司 | Recovery method of light hydrocarbon in refinery dry gas |
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