CN104031681A - Method for recovering ethylene and hydrogen from refinery dry gases by combining cold oil absorption and pressure swing adsorption (PSA) - Google Patents
Method for recovering ethylene and hydrogen from refinery dry gases by combining cold oil absorption and pressure swing adsorption (PSA) Download PDFInfo
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Abstract
The invention discloses a method for recovering ethylene and hydrogen from refinery dry gases by combining cold oil absorption and pressure swing adsorption (PSA). The method has the advantages and beneficial effects that main components such as hydrogen, ethylene and the like are obtained from the refinery dry gases through the steps of compression and pressure increase, cold oil absorption, first-segment PSA for coarse extraction of hydrogen, second-segment PSA for refining hydrogen, desorption, normal coarse distillation and the like; the main components are clearly separated; meanwhile, under the actions of PSA and membrane separation, the purity of various components can be more than 99%, the yield of hydrogen can reach 90-95%, and the yield of ethylene can reach 92-98%; the whole recovery flow is reasonable; the method has the characteristics of high yield, high purity, low operating cost and lower energy consumption.
Description
Technical field
Field is reclaimed in the classification that the present invention relates to oil refinery dry gas, the method that specifically oil refinery dry gas cold oil absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination.
Background technology
Useful component in oil refinery dry gas is mainly hydrogen, light olefin and light alkane etc.These components are all of great value in oil refinery dry gas, but they still do not realize optimum use very in a large number at present, but have directly been used as fuel, the even direct ignition torch emptying having.In oil refinery dry gas, both contain hydrogen, also contained a large amount of light olefins and light alkane.These components can be separated respectively and utilize, higher than the raw material benefit that it is directly used as to fuel or reformation hydrogen production, synthesizing methanol.
From oil refinery dry gas, the technology of recover hydrogen, light olefin and light alkane mainly contains separation by deep refrigeration, middle cold-peace shallow cold oil absorption process, membrane separation process, adsorption method of separation, and process integration etc.
Adsorption method of separation is to utilize sorbent material different to the adsorption selectivity of each component in mixed gas, by pressure or temperature change, realize a kind of separation method of absorption and regeneration, there is the features such as reproduction speed is fast, energy consumption is low, simple to operate, technical maturity is stable.By pressure change, realizing separated pressure-variable adsorption, to reclaim in dry gas hydrogen technique relatively ripe, and can obtain purity is 98%(volume ratio) above hydrogen product, but hydrogen recovery rate is generally in 80-85% left and right.Adopt the existing PSA Technology will be from containing reclaim highly purified hydrogen, ethene and ethane the oil refinery dry gas such as low-concentration hydrogen, ethene simultaneously, exist yield low, can not realize the complete sharp separation of oil refinery dry gas main ingredient, the problems such as huge are taken up an area in investment.
Membrane separation process is under certain pressure, utilizes the difference of other each components infiltration rate in film to carry out separated.Membrane separation process reclaims the 1987 Nian U.S. huge card urban construction that is installed on of hydrogen in FCC dry gas and becomes, and hydrogen recovery rate is 80-90%.Hydrogen recovery in the dry gas that membrane separation process is particularly useful for is with pressure, hydrogen content is low, that its advantage is to take up an area is little, simple to operate, energy consumption is low etc.But the purity of membrane sepn recover hydrogen is not high, is generally 95-99%.And aspect recovery ethene, ethane, also relevant employing by the scheme of membrane sepn proposes.
Cold oil absorption process is mainly to utilize absorption agent to realize separation to the difference of each components dissolved degree in dry gas.Generally to utilize C
3, C
4make absorption agent with the oil product such as aromatic hydrocarbons, first remove the noncondensable gas components such as methane and hydrogen, then by desorption method, absorption agent is reclaimed and is circulated in absorption tower, the C of enrichment
2, C
3component obtains the components such as ethylene-ethane by rectificating method separation.General operation temperature is 5 ℃ to-50 ℃, and ethene purity is more than 95%.Add decompressor technology, Recovery rate of ethylene and purity all can reach 99%.In addition, the energy consumption of cold oil absorption process will be lower than separation by deep refrigeration, and technique is relatively ripe, and ethene purity and yield are all higher, and reduced investment is simple to operate etc.But cold oil absorption process is only applicable to refining C
2and C
3component, have no idea separation and purification hydrogen, methane etc. simultaneously.
Cold separation technology just had and has developed as far back as the fifties in last century, at present this technology comparative maturity.It is the difference (boiling-point difference) of utilizing each component relative volatility in raw material, by gas turbine swell refrigeration, at low temperatures each component in dry gas is got off by processing requirement condensation, the hydrogen that is difficult for condensation obtains at first, hydrogen recovery rate is 92-95%, and purity is 95-98%.Thereafter with rectification method, wherein each class hydrocarbon is separated one by one, yield of ethene generally surpasses 85%.Low temperature separation process has simultaneously relatively advantages of higher of recover hydrogen and ethylene-ethane, technical maturity, the rate of recovery, and the general occasion that is applicable to processing a large amount of dry gas, is particularly suitable for area of concentration, refinery.The oil refinery dry gas recovery that low temperature separation process shortcoming is that product purity is not high, investment is large, energy consumption is high, be not suitable for middle and small scale etc.
Summary of the invention
The invention provides the method that oil refinery dry gas cold oil absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, while having solved in the past oil refinery dry gas recover hydrogen, ethene, have the problem that purity is not high, can not realize the complete sharp separation of oil refinery dry gas main ingredient.
Object of the present invention is achieved through the following technical solutions: the method that oil refinery dry gas cold oil absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, comprises the following steps:
(1) compression is boosted: oil refinery dry gas is after one-level compression, two-stage compression, and pressure is brought up to 2.0 ~ 3.6MPa;
(2) cold oil absorbs: the oil refinery dry gas after boosting in step (1) is carried out cooling, then send into absorption tower, the noncondensable gas that is rich in methane, hydrogen and nitrogen is discharged at top, absorption tower, and the underflow on absorption tower goes out absorbed carbon two and the above component of carbon two;
(3) two sections of pressure-variable adsorptions: the noncondensable gas that in step (2), discharge at top, absorption tower is at 2 ~ 3.6MPa pressure, under 30-40 ℃ of temperature condition, from one section of pressure-variable adsorption, slightly carrying hydrogen tower bottom enters, from bottom to top by being filled with the bed of sorbent material, the methane being adsorbed, nitrogen and hydrogen partial desorb from sorbent material by reverse step-down process, at the bottom of slightly carrying hydrogen tower, one section of pressure-variable adsorption discharges, through pressurization, send into fuel gas or unstripped gas pipe network, be not adsorbed a large amount of hydrogen and a small amount of methane of agent absorption, nitrogen and carbon two and above component are slightly carried hydrogen tower top from pressure-variable adsorption and are flowed out, at the bottom of entering the refining hydrogen tower of two sections of pressure-variable adsorptions, from bottom to top by being filled with the bed of sorbent material, the a small amount of methane being adsorbed, nitrogen and carbon two and above component desorb from sorbent material by reverse step-down process, from two sections of pressure-variable adsorptions, refine the low discharge emptying of hydrogen tower or send into fuel gas pipe network through pressurization, the hydrogen that is not adsorbed agent absorption is discharged from tower top, as product hydrogen,
(4) desorb: by absorbed carbon two and the above component that in step (2), flow out bottom, absorption tower, send into desorption tower and carry out desorb, enrichment carbon two and above component that desorption tower top is recycled directly enter topping still, and the oil of desorption tower bottom regeneration or propane class sorbent material return to absorption tower and recycle;
(5) slightly heat up in a steamer: enrichment carbon two and the above component of the desorption tower recovered overhead in step (4) enter after topping still, ethene is flowed out at topping still top, can be further to the refining high-purity ethylene that obtains of ethylene rectification tower, topping still bottom is flowed out and is rich in ethane and the above component of carbon two.
Further, as preferred version, the present invention also comprises and removes sour gas step, described in remove between the one-level compression and two-stage compression of sour gas step in step (1).The mode that removes sour gas is more, such as conventional amine is washed, alkali cleaning etc.
Further, as another preferred version, the present invention also comprises dry decontamination step, and described dry decontamination step is between two-stage compression and cold oil absorption.By the moisture removal in oil refinery dry gas, be conducive to improve the purity of hydrogen, ethene etc., also prevent that moisture from having a negative impact to absorption and sorption effect simultaneously.
Further, the present invention also comprises cold recovery step: the noncondensable gas that discharge at the top, absorption tower in step (2), enter the cold recovery system being formed by decompressor and ice chest, utilize the pressure expansion refrigeration of self, for the cooling step in step (2) provides whole colds; Meanwhile, from system, discharge methane, hydrogen and nitrogen, enter the refining hydrogen tower of pressure-variable adsorption.
Further, the refrigeration temperature that the described cold recovery system being comprised of decompressor and ice chest reaches is-100～5 ℃.
The present invention compared with prior art has the following advantages and beneficial effect:
(1) the present invention adopts cold oil absorption, pressure-variable adsorption combination process, oil refinery dry gas is absorbed by cold oil, obtain respectively noncondensable gas and carbon two and the above component of carbon two, noncondensable gas carries out essence through two sections of pressure-variable adsorptions to hydrogen to be carried, more than 99% hydrogen product of purity; And carbon two and above component be by desorb with slightly heat up in a steamer, will obtain ethene and be rich in the above component of carbon two of ethane, ethene enters ethylene rectification tower and refines that to obtain purity be 99% high-purity ethylene.
(2) the present invention is provided with the separation and Extraction hydrogen technique that one section of pressure-variable adsorption is slightly carried hydrogen and two sections of refining hydrogen of pressure-variable adsorption, be greater than under 99% prerequisite guaranteeing that hydrogen purity reaches, more than hydrogen yield can reach 90-95%, high purity, high yield recover hydrogen have been realized.
(3) the present invention is provided with a cold recovery step, the noncondensable gas that top, absorption tower is discharged carries out swell refrigeration, and the cold obtaining is used for to the cooling step of front end, has accomplished like this recycle of resource, thereby reduced energy consumption, reduced the input of cost.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of embodiments of the invention 1, embodiment 2, embodiment 3;
Fig. 2 is the process flow sheet of embodiments of the invention 4;
Fig. 3 is the process flow sheet of embodiments of the invention 5;
Fig. 4 is the process flow sheet of embodiments of the invention 6.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the present invention is described in further detail, but embodiments of the present invention are not limited only to this.
Embodiment 1:
As shown in Figure 1, the method that the oil refinery dry gas cold oil described in the present embodiment absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, comprises the following steps:
(1) compression is boosted: by the oil refinery dry gas (volume ratio) of hydrogen content 18.5%, ethane content 14.5%, ethylene content 16%, methane content 30%, a nitrogen content 14.5%, the above component concentration 3.5% of carbon two, content of acid gas 3%, after one-level compression, two-stage compression, pressure is brought up to 2.0MPa;
(2) cold oil absorbs: the oil refinery dry gas after boosting in step (1) is carried out cooling, then send into absorption tower, the noncondensable gas that is rich in methane, hydrogen and nitrogen is discharged at top, absorption tower, and the underflow on absorption tower goes out absorbed carbon two and above component;
(3) two sections of pressure-variable adsorptions: the noncondensable gas that in step (2), discharge at top, absorption tower is at 2.0MPa pressure, under 30 ℃ of temperature condition, from one section of pressure-variable adsorption, slightly carrying hydrogen tower bottom enters, from bottom to top by being filled with the bed of sorbent material, the methane being adsorbed, nitrogen and hydrogen partial desorb from sorbent material by reverse step-down process, at the bottom of slightly carrying hydrogen tower, one section of pressure-variable adsorption discharges, through pressurization, send into fuel gas or unstripped gas pipe network, be not adsorbed a large amount of hydrogen and a small amount of methane of agent absorption, nitrogen and carbon two and above component are slightly carried hydrogen tower top from pressure-variable adsorption and are flowed out, at the bottom of entering the refining hydrogen tower of two sections of pressure-variable adsorptions, from bottom to top by being filled with the bed of sorbent material, the a small amount of methane being adsorbed, nitrogen and carbon two and above component desorb from sorbent material by reverse step-down process, from two sections of pressure-variable adsorptions, refine the low discharge emptying of hydrogen tower or send into fuel gas pipe network through pressurization, the hydrogen that is not adsorbed agent absorption is discharged from tower top, as product hydrogen,
(4) desorb: by absorbed carbon two and the above component that in step (2), flow out bottom, absorption tower, send into desorption tower and carry out desorb, enrichment carbon two and above component that desorption tower top is recycled directly enter topping still, and the oil of desorption tower bottom regeneration or propane class sorbent material return to absorption tower and recycle;
(5) slightly heat up in a steamer: enrichment carbon two and the above component of the desorption tower recovered overhead in step (4) enter after topping still, ethene is flowed out at topping still top, can be further to the refining high-purity ethylene that obtains of ethylene rectification tower.Topping still bottom is flowed out and is rich in ethane and the above component of carbon two.
Oil refinery dry gas absorbs by cold oil, obtains respectively noncondensable gas and carbon two and above component, and noncondensable gas carries out essence through two sections of pressure-variable adsorptions to hydrogen to be carried, more than 99% hydrogen product of purity, and hydrogen yield can reach more than 90%.And carbon two and above component be by desorb with slightly heat up in a steamer, will obtain ethene and be rich in the above component of carbon two of ethane, ethene enters ethylene rectification tower and refines that to obtain purity be 99% high-purity ethylene, and yield of ethene reaches more than 94%.
Embodiment 2:
As shown in Figure 1, the method that described oil refinery dry gas cold oil absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, comprises the following steps:
(1) compression is boosted: by the oil refinery dry gas (volume ratio) of hydrogen content 46.5%, ethane content 12.4%, ethylene content 6.0%, methane content 20%, a nitrogen content 9.5%, the above component concentration 2.2% of carbon two, content of acid gas 3.2%, after one-level compression, two-stage compression, pressure is brought up to 2.8MPa;
(2) cold oil absorbs: the oil refinery dry gas after boosting in step (1) is carried out cooling, then send into absorption tower, the noncondensable gas that is rich in methane, hydrogen and nitrogen is discharged at top, absorption tower, and the underflow on absorption tower goes out absorbed carbon two and above component;
(3) two sections of pressure-variable adsorptions: the noncondensable gas that in step (2), discharge at top, absorption tower is under 2.8MPa pressure, 35 ℃ of temperature condition, from one section of pressure-variable adsorption, slightly carrying hydrogen tower bottom enters, from bottom to top by being filled with the bed of sorbent material, the methane being adsorbed, nitrogen and hydrogen partial desorb from sorbent material by reverse step-down process, at the bottom of one section of pressure-variable adsorption is slightly carried hydrogen tower, discharge, through pressurization, send into fuel gas or unstripped gas pipe network.The a large amount of hydrogen that is not adsorbed agent absorption is slightly proposed the outflow of hydrogen tower top with a small amount of methane, nitrogen and carbon two and above component from pressure-variable adsorption, at the bottom of entering the refining hydrogen tower of two sections of pressure-variable adsorptions, from bottom to top by being filled with the bed of sorbent material, the a small amount of methane being adsorbed, nitrogen and carbon two and above component desorb from sorbent material by reverse step-down process, from two sections of pressure-variable adsorptions, refine the low discharge emptying of hydrogen tower or send into fuel gas pipe network through pressurization; The hydrogen that is not adsorbed agent absorption is discharged from tower top, as product hydrogen.
(4) desorb: by absorbed carbon two and the above component that in step (2), flow out bottom, absorption tower, send into desorption tower and carry out desorb, enrichment carbon two and above component that desorption tower top is recycled directly enter topping still, and the oil of desorption tower bottom regeneration or propane class sorbent material return to absorption tower and recycle;
(5) slightly heat up in a steamer: enrichment carbon two and the above component of the desorption tower recovered overhead in step (4) enter after topping still, ethene is flowed out at topping still top, can be further to the refining high-purity ethylene that obtains of ethylene rectification tower, topping still bottom is flowed out and is rich in ethane and the above component of carbon two.
Oil refinery dry gas absorbs by cold oil, obtains respectively noncondensable gas and carbon two and above component, and noncondensable gas carries out essence through two sections of pressure-variable adsorptions to hydrogen to be carried, more than 99% hydrogen product of purity, and hydrogen yield can reach more than 94%.And carbon two and above component be by desorb with slightly heat up in a steamer, will obtain ethene and be rich in the above component of carbon two of ethane, ethene enters ethylene rectification tower and refines that to obtain purity be 99% high-purity ethylene, and yield of ethene can reach more than 93%.
Embodiment 3:
As shown in Figure 1, the method that described oil refinery dry gas cold oil absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, comprises the following steps:
(1) compression is boosted: by the oil refinery dry gas (volume ratio) of hydrogen content 18.5%, ethane content 14.5%, ethylene content 16%, methane content 30%, a nitrogen content 14.5%, the above component concentration 3.5% of carbon two, content of acid gas 3%, after one-level compression, two-stage compression, pressure is brought up to 3.6MPa;
(2) cold oil absorbs: the oil refinery dry gas after boosting in step (1) is carried out cooling, then send into absorption tower, the noncondensable gas that is rich in methane, hydrogen and nitrogen is discharged at top, absorption tower, and the underflow on absorption tower goes out absorbed carbon two and above component;
(3) two sections of pressure-variable adsorptions: the noncondensable gas that in step (2), discharge at top, absorption tower is under 3.6MPa pressure, 40 ℃ of temperature condition, from one section of pressure-variable adsorption, slightly carrying hydrogen tower bottom enters, from bottom to top by being filled with the bed of sorbent material, the methane being adsorbed, nitrogen and hydrogen partial desorb from sorbent material by reverse step-down process, at the bottom of one section of pressure-variable adsorption is slightly carried hydrogen tower, discharge, through pressurization, send into fuel gas or unstripped gas pipe network.The a large amount of hydrogen that is not adsorbed agent absorption is slightly proposed the outflow of hydrogen tower top with a small amount of methane, nitrogen and carbon two and above component from pressure-variable adsorption, at the bottom of entering the refining hydrogen tower of two sections of pressure-variable adsorptions, from bottom to top by being filled with the bed of sorbent material, the a small amount of methane being adsorbed, nitrogen and carbon two and above component desorb from sorbent material by reverse step-down process, from two sections of pressure-variable adsorptions, refine the low discharge emptying of hydrogen tower or send into fuel gas pipe network through pressurization; The hydrogen that is not adsorbed agent absorption is discharged from tower top, as product hydrogen.
(4) desorb: by absorbed carbon two and the above component that in step (2), flow out bottom, absorption tower, send into desorption tower and carry out desorb, enrichment carbon two and above component that desorption tower top is recycled directly enter topping still, and the oil of desorption tower bottom regeneration or propane class sorbent material return to absorption tower and recycle;
(5) slightly heat up in a steamer: enrichment carbon two and the above component of the desorption tower recovered overhead in step (4) enter after topping still, ethene is flowed out at topping still top, can be further to the refining high-purity ethylene that obtains of ethylene rectification tower, topping still bottom is flowed out and is rich in ethane and the above component of carbon two.
Oil refinery dry gas absorbs by cold oil, obtains respectively noncondensable gas and carbon two and above component, and noncondensable gas carries out essence through two sections of pressure-variable adsorptions to hydrogen to be carried, more than 99% hydrogen product of purity, and hydrogen yield can reach more than 92%.And carbon two and above component be by desorb with slightly heat up in a steamer, will obtain ethene and be rich in the above component of carbon two of ethane, ethene enters ethylene rectification tower and refines that to obtain purity be 99% high-purity ethylene, and yield of ethene can reach more than 96%.
Embodiment 4:
As shown in Figure 2, on the basis of the present embodiment three embodiment above, increased and removed sour gas step, described in remove sour gas step between one-level compression and two-stage compression.By increasing this step, partial impurities gas can be removed effectively, to guarantee the purity of main gaseous constituent, except the mode of sour gas has that conventional amine is washed, alkali cleaning etc.
Embodiment 5:
As shown in Figure 3, the present embodiment, on the basis of embodiment 2, has also increased dry decontamination step, by the moisture removal in oil refinery dry gas between two-stage compression and cold oil absorption, be conducive to improve the purity of hydrogen, ethene etc., also prevent that moisture from having a negative impact to absorption and sorption effect simultaneously.
Embodiment 6:
As shown in Figure 4, the present embodiment has increased cold recovery step on the basis of embodiment 3, the cold recovery system being formed by decompressor and ice chest, the noncondensable gas that discharge at top, absorption tower enters cold recovery system, utilize the pressure expansion refrigeration of self, for the cooling step in cold oil absorption provides whole colds, thereby save ample resources, reduced cost; In addition, from system, discharge methane, hydrogen and nitrogen, enter two sections of pressure-variable adsorptions and slightly mention refining hydrogen tower.
In addition, the refrigeration temperature that the cold recovery system being comprised of decompressor and ice chest reaches is-100～5 ℃.
The present invention is illustrated by above-described embodiment, but should be understood that, above-described embodiment is the object for giving an example and illustrating just, but not is intended to the present invention to be limited in described scope of embodiments.In addition, it will be appreciated by persons skilled in the art that the present invention is not limited to above-described embodiment, according to instruction of the present invention, can also make more kinds of variants and modifications, these variants and modifications all drop in the present invention's scope required for protection.
Claims (5)
1. the method that oil refinery dry gas cold oil absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, is characterized in that: comprise the following steps:
(1) compression is boosted: oil refinery dry gas is after one-level compression, two-stage compression, and pressure is brought up to 2.0 ~ 3.6MPa;
(2) cold oil absorbs: the oil refinery dry gas after boosting in step (1) is carried out cooling, then send into absorption tower, the noncondensable gas that is rich in methane, hydrogen and nitrogen is discharged at top, absorption tower, and the underflow on absorption tower goes out absorbed carbon two and the above component of carbon two;
(3) two sections of pressure-variable adsorptions: the noncondensable gas that in step (2), discharge at top, absorption tower is at 2 ~ 3.6MPa pressure, under 30-40 ℃ of temperature condition, from one section of pressure-variable adsorption, slightly carrying hydrogen tower bottom enters, from bottom to top by being filled with the bed of sorbent material, the methane being adsorbed, nitrogen and hydrogen partial desorb from sorbent material by reverse step-down process, at the bottom of slightly carrying hydrogen tower, one section of pressure-variable adsorption discharges, through pressurization, send into fuel gas or unstripped gas pipe network, be not adsorbed a large amount of hydrogen and a small amount of methane of agent absorption, nitrogen and carbon two and above component are slightly carried hydrogen tower top from pressure-variable adsorption and are flowed out, at the bottom of entering the refining hydrogen tower of two sections of pressure-variable adsorptions, from bottom to top by being filled with the bed of sorbent material, the a small amount of methane being adsorbed, nitrogen and carbon two and above component desorb from sorbent material by reverse step-down process, from two sections of pressure-variable adsorptions, refine the low discharge emptying of hydrogen tower or send into fuel gas pipe network through pressurization, the hydrogen that is not adsorbed agent absorption is discharged from tower top, as product hydrogen,
(4) desorb: by absorbed carbon two and the above component that in step (2), flow out bottom, absorption tower, send into desorption tower and carry out desorb, enrichment carbon two and above component that desorption tower top is recycled directly enter topping still, and the oil of desorption tower bottom regeneration or propane class sorbent material return to absorption tower and recycle;
(5) slightly heat up in a steamer: enrichment carbon two and the above component of the desorption tower recovered overhead in step (4) enter after topping still, ethene is flowed out at topping still top, can be further to the refining high-purity ethylene that obtains of ethylene rectification tower, topping still bottom is flowed out and is rich in ethane and the above component of carbon two.
2. the method that oil refinery dry gas cold oil according to claim 1 absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, it is characterized in that: also comprise and remove sour gas step, described in remove between the compression of the one-level of sour gas step in step (1) and two-stage compression.
3. the method that oil refinery dry gas cold oil according to claim 1 absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, is characterized in that: also comprise dry decontamination step, described dry decontamination step is between two-stage compression and cold oil absorption.
4. the method that oil refinery dry gas cold oil according to claim 1 absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, it is characterized in that: also comprise cold recovery step: the noncondensable gas that discharge at the top, absorption tower in step (2), enter the cold recovery system being formed by decompressor and ice chest, utilize the pressure expansion refrigeration of self, for the cooling step in step (2) provides whole colds; Meanwhile, from system, discharge methane, hydrogen and nitrogen, enter one section of pressure-variable adsorption and slightly carry hydrogen tower.
5. the method that oil refinery dry gas cold oil according to claim 4 absorbs, ethene and hydrogen are reclaimed in pressure-variable adsorption combination, is characterized in that: the refrigeration temperature that the described cold recovery system being comprised of decompressor and ice chest reaches is-100～5 ℃.
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| CN106178839A (en) * | 2015-05-25 | 2016-12-07 | 中国石油天然气股份有限公司 | Method for recovering and extracting hydrogen and light hydrocarbon in hydrogen-containing rich gas |
| CN109574786A (en) * | 2018-12-26 | 2019-04-05 | 四川天采科技有限责任公司 | Preparing propylene by dehydrogenating propane reaction mixture gas cold oil absorbs the separation method coupled with PSA |
| CN111825516A (en) * | 2019-04-19 | 2020-10-27 | 惠生工程（中国）有限公司 | Separation system and separation method of crude butadiene |
| CN111825516B (en) * | 2019-04-19 | 2023-04-28 | 惠生工程（中国）有限公司 | Separation system and separation method of crude butadiene |
| CN114570165A (en) * | 2020-11-30 | 2022-06-03 | 中国石油天然气集团有限公司 | Re-contact system for reforming hydrogen production |
| CN114570165B (en) * | 2020-11-30 | 2023-06-30 | 中国石油天然气集团有限公司 | Re-contact system for reforming hydrogen production |
| CN112777569A (en) * | 2020-12-16 | 2021-05-11 | 四川天采科技有限责任公司 | Fluorine-based SiC-CVD crystal and film growth process tail gas FTrPSA full-component recycling method |
| CN112777569B (en) * | 2020-12-16 | 2022-06-10 | 四川天采科技有限责任公司 | Method for recycling FTrPSA (fluorine-based SiC-CVD) tail gas in film growth process |
| CN114524702A (en) * | 2022-02-28 | 2022-05-24 | 东方傲立石化有限公司 | Method for removing impurities in catalytic dry gas |
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