CN203845995U - Device for shallow condensation adsorption-absorption extraction on hydrogen and ethylene in refinery dry gas - Google Patents
Device for shallow condensation adsorption-absorption extraction on hydrogen and ethylene in refinery dry gas Download PDFInfo
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- CN203845995U CN203845995U CN201420266988.1U CN201420266988U CN203845995U CN 203845995 U CN203845995 U CN 203845995U CN 201420266988 U CN201420266988 U CN 201420266988U CN 203845995 U CN203845995 U CN 203845995U
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Abstract
The utility model discloses a device for shallow condensation adsorption-absorption extraction on hydrogen and ethylene in a refinery dry gas. The device consists of a first adsorption tower, a second adsorption tower, a shallow condensation absorption tower, a desorbing tower, an expansion machine, a compressor and a pretreatment unit. The device adopts shallow condensation absorption, low pressure adsorption is firstly performed before shallow condensation adsorption to separate concentrated C2, and uncondensed gases such as hydrogen entering a shallow condensation absorption unit are reduced, so that the operation burden and the energy consumption of absorption are reduced, and the cost is lowered.
Description
Technical field
The utility model relates to the classification of oil refinery dry gas and reclaims field, relate to the shallow enfleurage of a kind of oil refinery dry gas attached-absorption extraction extracts hydrogen, ethylene unit.
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 the techniques such as cold oil absorption extraction method, membrane separation process, adsorption method of separation.
Adsorption method of separation is to utilize the adsorption selectivity difference of sorbent material to each component in mixed gas, realize a kind of separation method of absorption and regeneration by pressure or temperature change, there is the features such as reproduction speed is fast, energy consumption is low, simple to operate, technical maturity is stable.Realize by pressure change the pressure-variable adsorption separating and reclaim hydrogen technique maturation relatively in dry gas, can obtain purity is 98%(volume ratio) above hydrogen product, but hydrogen recovery rate is generally in 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 Components, the problems such as huge are taken up an area in investment.
Membrane separation process is under certain pressure, and the difference of infiltration rate separates in film to utilize each component in feeding gas.Membrane separation process reclaims being installed on 1987 and becoming in the U.S.'s huge card urban construction of hydrogen in FCC dry gas, 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, the also relevant scheme proposition adopting with membrane sepn.
Cold oil absorption extraction technology is to utilize the difference of each component relative volatility in raw material (boiling-point difference), 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 70-80%, and purity is 70-90%.Thereafter with rectification method, wherein each class hydrocarbon is separated one by one, yield of ethene is generally more than 90%.Low temperature separation process has simultaneously recover hydrogen and ethylene-ethane, technical maturity, relatively advantages of higher of the rate of recovery, the general occasion that is applicable to processing a large amount of dry gas, be particularly suitable for area of concentration, refinery, low temperature separation process shortcoming is that product purity is not high, and energy consumption is higher.
Utility model content
The purpose of this utility model is to overcome the limitation that existing adsorption method of separation, membrane separation process and cold oil absorption extraction method are practiced separately factory's dry gas processing separately, provide the shallow enfleurage of a kind of oil refinery dry gas attached-absorption extraction extract hydrogen, ethene method and device.
The shallow enfleurage of oil refinery dry gas is attached-and absorption extraction extracts hydrogen, ethylene unit, is made up of the first adsorption tower, the second adsorption tower, shallow cold absorption tower, desorption tower, cold recovery system, compressor, pretreatment unit; Described cold recovery system is to utilize the device of input gas expansion refrigeration; The outlet at bottom of described the first adsorption tower is connected with the bottom inlet on shallow cold absorption tower, the first adsorption tower top exit is connected with the bottom inlet of the second adsorption tower, the top exit on described shallow cold absorption tower is connected with the entrance of cold recovery system, and the outlet at bottom on shallow cold absorption tower is connected with desorption tower entrance; Described desorption tower outlet at bottom is connected with the absorption agent entrance on shallow cold absorption tower, and the described cold recovery system outlet pretreatment unit entrance preposition with the first adsorption tower is connected, and described compressor is connected on the pipeline between the first adsorption tower and shallow cold absorption tower.
Preferably, it is characterized in that, described cold recovery system is made up of decompressor and ice chest.
Preferably, it is characterized in that, also comprise rectifying tower, the centre entrance of described rectifying tower is connected with desorption tower tower top outlet.
Adopt the shallow enfleurage of oil refinery dry gas described in the utility model attached-absorption extraction extracts hydrogen, ethylene unit, oil refinery dry gas is absorbed and pressure-variable adsorption by shallow cold oil, obtain respectively high-purity hydrogen and carbon two and the above component of carbon two, adopt shallow cold recovery and carry out in advance low pressure fractionation by adsorption before shallow enfleurage is received, further save cold, thereby reduce energy consumption, reduced the input of cost.
Brief description of the drawings
Fig. 1 is a kind of embodiment structural representation of the shallow cold separate absorbent hydrogen of oil refinery dry gas described in the utility model, ethene.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in further detail.
Embodiment 1
The gas per-cent that hydrogen content 56.2%, ethane content 7.2%, ethylene content 6.2%, methane content 22.2%, a nitrogen content 5.5%, the above component concentration 0.9% of carbon two, content of acid gas 1.8%(are mentioned is herein volume percent), pressure is that the oil refinery dry gas of 1 MPa carries out pre-treatment.The temperature of pretreated oil refinery dry gas is reduced to 5 to 10 degrees Celsius again, enters the first adsorption tower and adsorb for the first time, the temperature while absorption is for the first time controlled at 5 to 10 degrees Celsius; Pressure while entering is constant.
It will be clear to someone skilled in the art that low pressure is adsorbed as existing technique, for its principle, repeats no more herein.In this step, sorbent material absorption carbon two components of loading in the first adsorption tower, a small amount of hydrogen, methane, nitrogen and above component of carbon two, the hydrogen not being adsorbed, methane and nitrogen composition concentrated gas are discharged from tower top.In the time of adsorbent reactivation, carbon two components (being mainly ethene, ethane) that are adsorbed, a small amount of hydrogen, methane, nitrogen and carbon two components depart from from sorbent material, composition ethylene-rich dry gas.Ethylene-rich dry gas main component is carbon two component gas, and concentrated gas main ingredient is hydrogen; Described main ingredient is the gas of molar percentage maximum in gas; Described carbon two components herein, refer to the various alkane alkene that contain more than two carbon atom etc.
The ethylene-rich dry gas obtaining in step S1 enters shallow cold absorption step after being forced into 1-2 MPa, the absorption temperature of described shallow cold absorption step is with adsorption temp is identical for the first time, and the noncondensable gas in described shallow cold absorption step turns back to pretreatment unit after expanding and step S1 adsorbs again; Concentrated gas in step S1 is through being forced into 1-2 MPa, enters at normal temperatures the second adsorption tower and adsorbs for the second time and obtain product hydrogen.Described normal temperature is common envrionment temperature, and scope is at 0-40 degree Celsius.
The absorption liquid that described in S3, in step S2, shallow cold absorption step obtains enters desorption procedure, and desorption procedure is carried out Desorption separation to absorption liquid, be absorbed agent and carbon two components, and wherein absorption agent is recycled by step S2, and the further rectifying of carbon two component obtains ethene.
The implement device of aforesaid method is made up of the first adsorption tower, the second adsorption tower, shallow cold absorption tower, desorption tower, cold recovery system, compressor; Described cold recovery system is to utilize the device of input gas expansion refrigeration; The outlet at bottom of described the first adsorption tower is connected by compressor with the bottom inlet on shallow cold absorption tower, the first adsorption tower top exit is connected with the bottom inlet of the second adsorption tower, the top exit on described shallow cold absorption tower is connected with the entrance of cold recovery system, and the outlet at bottom on shallow cold absorption tower is connected with desorption tower entrance; Described desorption tower outlet at bottom is connected with the absorption agent entrance on shallow cold absorption tower, and described cold recovery system outlet is connected with the pretreatment unit entrance of preposition the first adsorption tower, and described compressor is connected on the pipeline between the first adsorption tower and shallow cold absorption tower.
The first adsorption tower obtains ethylene-rich dry gas by self adsorbent reactivation, and regeneration temperature is controlled at zero to ten degree Celsius, adopts and vacuumizes regeneration.Between the first adsorption tower and shallow cold absorption tower by compressor pressurizes to 1-2 MPa, absorption temperature is identical with the first adsorption tower adsorption temp.From the first adsorption tower born ethylene-rich dry gas again, at the bottom of entering shallow cold absorption tower through pressurization.And absorption liquid enters and absorbs from shallow enfleurage receipts top of tower.The absorption liquid that has absorbed carbon two components utilizes self gravitation or through pump input desorption tower top, carries out desorb.Desorption mode is according to conventional desorb.The absorption agent that is desorbed out can be from desorption tower bottom turns back to shallow enfleurage through recycle pump and connecting tube to be received top of tower and recycles, and improves the cyclic utilization rate of absorption agent.Carbon two components are flowed out at desorption tower top, further enter conventional rectifying tower and carry out rectifying, obtain highly purified ethene and other component.The hydrogen rich gas that the first absorption tower top is discharged enters the second adsorption tower bottom and carries out absorption and regeneration, discharges highly purified hydrogen from the second adsorption tower tower top.When the second adsorption tower regeneration, from tower top, resurgent gases is discharged to emptying.
The utility model adsorbs for the first time the attached superiority of the employing shallow enfleurage of low pressure and is:
The first, at the shallow cool condition of low pressure, when carbon two components of pressure-variable adsorption absorption for the first time vacuumize regeneration, than conventional pressure-variable adsorption to vacuumize regeneration more thorough, maximum thereby the ethylene-rich gas concentration obtaining reaches, enter shallow enfleurage and receive significant loss and reduce to minimum;
The second, by pressure-variable adsorption for the first time, make feed gas composition carry out the concentrated gas that is rich in hydrogen that primary separation obtains and directly enter for the second time adsorption tower and carry out essence and carry hydrogen and played and slightly mention provide protection, improve yield and the purity of hydrogen;
The 3rd, isolate the noncondensable gases such as a large amount of hydrogen by pressure-variable adsorption for the first time, greatly reduce thus the noncondensable gas load that enters shallow cold absorptive unit, and then also greatly reduce the load that shallow enfleurage is received, comprise absorption agent consumption, energy consumption, equipment size etc., corresponding investment and the running cost of having reduced
The hydrogen yield obtaining in the present embodiment is 92%, and purity is more than 99%.
Embodiment 2
The present embodiment is with on the basis of embodiment 1, and carbon two mixtures that the tower top of desorption tower is discharged are further processed, and have increased rectifying tower, and the centre entrance of described rectifying tower is connected with desorption tower tower top outlet
Desorption tower tower top ejecta is sent into rectifying tower and is carried out rectifying, rectifying tower top flows out carbon two components, can directly enter ethylene rectification tower, obtain highly purified product ethene, the heavy constituent that rectifying tower underflow goes out can directly be sent into ethane cracking furnace, obtain highly purified product ethene.
In the present embodiment, can reach 90% to the Recovery rate of ethylene in oil refinery dry gas, reclaim purity and reach 99%.
Embodiment 3
The present embodiment is identical with the apparatus and method that embodiment 2 adopts, the gaseous fraction of input oil refinery dry gas is hydrogen content 41.4%, ethane content 11.3%, ethylene content 8.4%, methane content 21.4%, a nitrogen content 11%, the above component concentration 2.9% of carbon two, content of acid gas 3.6%, and oil refinery dry gas pressure is 1 MPa; The temperature of oil refinery dry gas is reduced to 5 degrees Celsius, and the temperature while absorption is for the first time controlled at 5 degrees Celsius; Pressure while entering is 1 MPa, and the hydrogen recovery rate obtaining is 90%, and it is more than 99% reclaiming purity, and Recovery rate of ethylene can reach 92%, reclaims purity and reaches 99%.
Embodiment 4
The present embodiment is on the basis of embodiment 3, depickling gas and drying step to unstripped gas oil refinery dry gas are further increased, can utilize existing low-temp methanol washing process to remove the sour gas in oil refinery dry gas, this sour gas comprises carbonic acid gas, sulfurous gas, hydrogen sulfide etc.; Gas after can adopting activated carbon temperature-change adsorption tower to depickling gas is dried, and further to improve the separating-purifying degree of oil refinery dry gas, reduces cold consumption simultaneously.
The gaseous fraction of input oil refinery dry gas is hydrogen content 50%, ethane content 7.9%, ethylene content 7.3%, methane content 16.4%, a nitrogen content 12%, the above component concentration 3.4% of carbon two, content of acid gas 3%, and oil refinery dry gas pressure is 0.8 MPa; The temperature of oil refinery dry gas is reduced to eight degrees Celsius, and the temperature while absorption is for the first time controlled at 7 to 10 degrees Celsius; Pressure while entering is 0.8 MPa, and the hydrogen recovery rate obtaining is 91%, and it is more than 99% reclaiming purity, and Recovery rate of ethylene can reach 92%, reclaims purity and reaches more than 98%.
Previously described is each preferred embodiment of the present utility model, preferred implementation in each preferred embodiment is if not obviously contradictory or taking a certain preferred implementation as prerequisite, each preferred implementation arbitrarily stack combinations is used, design parameter in described embodiment and embodiment is only the utility model proof procedure for clear statement utility model people, not in order to limit scope of patent protection of the present utility model, scope of patent protection of the present utility model is still as the criterion with its claims, the equivalent structure that every utilization specification sheets of the present utility model and accompanying drawing content are done changes, in like manner all should be included in protection domain of the present utility model.
Claims (3)
- The shallow enfleurage of oil refinery dry gas attached-absorption extraction extracts hydrogen, ethylene unit, it is characterized in that, formed by the first adsorption tower, the second adsorption tower, shallow cold absorption tower, desorption tower, cold recovery system, compressor, pretreatment unit; Described cold recovery system is to utilize the device of input gas expansion refrigeration;The outlet at bottom of described the first adsorption tower is connected with the bottom inlet on shallow cold absorption tower, the first adsorption tower top exit is connected with the bottom inlet of the second adsorption tower, the top exit on described shallow cold absorption tower is connected with the entrance of cold recovery system, and the outlet at bottom on shallow cold absorption tower is connected with desorption tower entrance; Described desorption tower outlet at bottom is connected with the absorption agent entrance on shallow cold absorption tower, and the described cold recovery system outlet pretreatment unit entrance preposition with the first adsorption tower is connected, and described compressor is connected on the pipeline between the first adsorption tower and shallow cold absorption tower.
- As claimed in claim 1 the shallow enfleurage of oil refinery dry gas attached-absorption extraction extracts hydrogen, ethylene unit, it is characterized in that, described cold recovery system is made up of decompressor and ice chest.
- As claimed in claim 1 the shallow enfleurage of oil refinery dry gas attached-absorption extraction extracts hydrogen, ethylene unit, it is characterized in that, also comprise rectifying tower, the centre entrance of described rectifying tower is connected with desorption tower tower top outlet.
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| CN201420266988.1U CN203845995U (en) | 2014-05-23 | 2014-05-23 | Device for shallow condensation adsorption-absorption extraction on hydrogen and ethylene in refinery dry gas |
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| CN201420266988.1U CN203845995U (en) | 2014-05-23 | 2014-05-23 | Device for shallow condensation adsorption-absorption extraction on hydrogen and ethylene in refinery dry gas |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104031682A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for separating hydrogen and ethylene from refinery dry gas by shallow condensing adsorption-absorption |
| CN105258453A (en) * | 2015-11-13 | 2016-01-20 | 四川天采科技有限责任公司 | Method for recovering light hydrocarbon and hydrogen from tail gas of petrochemical plant |
| CN107057758A (en) * | 2017-06-09 | 2017-08-18 | 中石化上海工程有限公司 | The method for removing acid impurities in lighter hydrocarbons |
| CN107285985A (en) * | 2016-03-30 | 2017-10-24 | 中国石油化工股份有限公司 | A kind of joint production process and device of hydrogen and ethene |
-
2014
- 2014-05-23 CN CN201420266988.1U patent/CN203845995U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104031682A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for separating hydrogen and ethylene from refinery dry gas by shallow condensing adsorption-absorption |
| CN104031682B (en) * | 2014-05-23 | 2016-07-06 | 四川天采科技有限责任公司 | The shallow enfleurage of oil refinery dry gas is attached-absorption and separation hydrogen, ethylene method |
| CN105258453A (en) * | 2015-11-13 | 2016-01-20 | 四川天采科技有限责任公司 | Method for recovering light hydrocarbon and hydrogen from tail gas of petrochemical plant |
| CN105258453B (en) * | 2015-11-13 | 2017-11-07 | 四川天采科技有限责任公司 | A kind of method that lighter hydrocarbons and hydrogen are reclaimed in the tail gas from petrochemical plant |
| CN107285985A (en) * | 2016-03-30 | 2017-10-24 | 中国石油化工股份有限公司 | A kind of joint production process and device of hydrogen and ethene |
| CN107285985B (en) * | 2016-03-30 | 2020-10-13 | 中国石油化工股份有限公司 | Hydrogen and ethylene co-production process and device |
| CN107057758A (en) * | 2017-06-09 | 2017-08-18 | 中石化上海工程有限公司 | The method for removing acid impurities in lighter hydrocarbons |
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Granted publication date: 20140924 Termination date: 20170523 |