CN105276924B - A kind of lighter hydrocarbons cryogenic separation retracting device and method - Google Patents
A kind of lighter hydrocarbons cryogenic separation retracting device and method Download PDFInfo
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- CN105276924B CN105276924B CN201410455184.0A CN201410455184A CN105276924B CN 105276924 B CN105276924 B CN 105276924B CN 201410455184 A CN201410455184 A CN 201410455184A CN 105276924 B CN105276924 B CN 105276924B
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 176
- 239000001257 hydrogen Substances 0.000 claims abstract description 121
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 121
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 95
- 239000007789 gas Substances 0.000 claims abstract description 61
- 238000000926 separation method Methods 0.000 claims abstract description 49
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000007600 charging Methods 0.000 claims abstract description 25
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 22
- 238000005336 cracking Methods 0.000 claims abstract description 21
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 21
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 21
- 238000000034 method Methods 0.000 claims abstract description 17
- 238000011084 recovery Methods 0.000 claims description 52
- 229910052799 carbon Inorganic materials 0.000 claims description 47
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 45
- 239000007791 liquid phase Substances 0.000 claims description 18
- 238000002156 mixing Methods 0.000 claims description 16
- 239000012071 phase Substances 0.000 claims description 13
- 238000001816 cooling Methods 0.000 claims description 11
- 239000007792 gaseous phase Substances 0.000 claims description 6
- 150000001335 aliphatic alkanes Chemical class 0.000 claims description 4
- 238000005204 segregation Methods 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 239000000463 material Substances 0.000 claims description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 abstract description 16
- 239000005977 Ethylene Substances 0.000 abstract description 13
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 4
- 238000010791 quenching Methods 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 11
- 239000007788 liquid Substances 0.000 description 6
- 238000010992 reflux Methods 0.000 description 5
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- 239000003507 refrigerant Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000035611 feeding Effects 0.000 description 2
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 2
- 239000003949 liquefied natural gas Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000005540 biological transmission Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Separation By Low-Temperature Treatments (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of lighter hydrocarbons cryogenic separation retracting device and method.Described device is provided with methane/hydrogen piece-rate system, including：1# tail gas heat exchangers, hydrogen/methane separation tank and hydrogen flow controller；3# domethanizing columns charging knockout drum overhead line connects hydrogen/methane separation tank after 1# tail gas heat exchangers, and hydrogen/methane separation pot bottom pipeline connects domethanizing column after 1# tail gas heat exchangers；Hydrogen flow controller, the bypass line connection hydrogen methane expander system of hydrogen flow controller are set on hydrogen/methane separation tank top outlet line.The present invention can obtain high-purity H2 by carrying out Quench separation to dried light hydrocarbon cracking gas, and by CH4 and C2 ' s is nearly completely separated, and is particularly adapted to the ethylene unit using ethane as cracking stock.
Description
Technical field
The present invention relates to lighter hydrocarbons recovery field, further say, be to be related to a kind of lighter hydrocarbons cryogenic separation retracting device and side
Method.It is particularly adapted on ethylene unit, during using ethane as main cracking stock, separate section requirement has higher ethene and hydrogen
The place of the rate of recovery.
Background technology
The cracking stock of ethylene unit mainly has ethane, propane, saturation LPG, naphtha, hydrogenation tail oil and light diesel fuel etc.,
The yield of the lighter ethene of general raw material is higher, and the energy consumption of device is also lower.Develop and produce with state's inside/outside liquefied natural gas (LNG)
The continuous improvement of amount, and shale gas a large amount of exploitation, the ethylene unit using ethane as main cracking stock will certainly obtain
To further development and application.
The heavy component yield of CH4, C3s and the above is higher in heavy charge cracking gas, and in ethane cracking product H2 and
Ethane content is very high, heavy constituent yield is minimum.Domestic existing cracking of ethylene deep cooling process for separating flow, mainly for mesh
(see Fig. 1) of the liquid phase heavy charge customization of preceding China's generally existing, is not particularly suitable for the gas phases such as light component content very high ethane
The separation of raw cracked gas.For example：During using naphtha as cracking stock, yield of ethene can reach 99.6%, hydrogen purity
More than 95mol%.And when being used to separate ethane cracking gas, hydrogen purity is only 86mol%；Ethylene loss is up to 3.3%, for
The ethylene unit of a set of megaton, that is, the ethylene loss amount of about 4 ton hours, wastes serious.
External existing light hydrocarbon cracking device, there is also the ethene of high added value and hydrogen product yield for its isolation technics
It is not very high, hydrogen also needs to separately set the problem of transformation adsorption device (PSA) is purified, and causes certain loss or the device of economic benefit
The extra increase of investment.
The content of the invention
To solve produced problem in the prior art, the invention provides a kind of lighter hydrocarbons cryogenic separation retracting device and side
Method.For separating during the cracking gas using ethane as primary raw material, the rate of recovery and hydrogen purity of ethene can be significantly increased,
Make up to can be suitable with existing feed naphtha separation process degree.
An object of the present invention is to provide a kind of lighter hydrocarbons cryogenic separation retracting device.
Including:Domethanizing column, the recovery tower of carbon two, 1#~7# tail gas heat exchangers, 1#~3# domethanizing columns charging knockout drum, institute
State device and be provided with methane/hydrogen piece-rate system, including：1# tail gas heat exchangers, hydrogen/methane separation tank and hydrogen flow controller；
3# domethanizing columns charging knockout drum overhead line connects hydrogen/methane separation tank, hydrogen/methane separation tank bottom after 1# tail gas heat exchangers
Portion's pipeline connects domethanizing column after 1# tail gas heat exchangers；Hydrogen flow control is set on hydrogen/methane separation tank top outlet line
Device processed, the bypass line connection hydrogen methane expander system of hydrogen flow controller；
Demethanizer overhead connects and condenser is set in the recovery tower of carbon two, the recovery tower of carbon two, and carbon two reclaims tower bottom connection
Connection hydrogen methane expander system at the top of domethanizing column, the recovery tower of carbon two；
Hydrogen methane expander system includes：Expander inlet blending tank, expanding machine, outlet knockout drum；Hydrogen flow control
The bypass line of device processed is connected expander inlet blending tank, expander inlet blending tank after merging with the recovery tower overhead line of carbon two
Top connects connection outlet knockout drum after expanding machine, expander outlet pipeline and the merging of expander inlet blending tank outlet line,
Outlet knockout drum bottom line is divided into the condenser in two, a connection recovery tower of carbon two, and another after tail gas heat exchanger
Send out out-of-bounds.
Wherein, the recovery tower of carbon two uses segregation fractionating column pattern.
The second object of the present invention is to provide a kind of lighter hydrocarbons cryogenic separation recovery method.
Including：
1) cracking gas of drying and dehydrating is isolated after heat exchange and cooling by 1#, 2# and 3# domethanizing column charging knockout drum
Liquid phase therein, from bottom to top successively as first, second, and third burst of charging of domethanizing column；
2) into hydrogen/methane separation tank after the gas phase of 3# domethanizing columns charging knockout drum exchanges heat through 1# tail gas heat exchangers, hydrogen/
The liquid phase of methane separation tank separation is fed after being exchanged heat through 1# tail gas heat exchangers as the 4th strand of domethanizing column；Hydrogen/methane separation
The gas phase portion of tank separation is sent out out-of-bounds as high pressure hydrogen, partly branches to hydrogen methane expander system；
3) the demethanation top gaseous phase feeding recovery tower of carbon two, reclaims ethene, and the recovery tower bottom of towe of carbon two is back to domethanizing column；
4) hydrogen that the recovery of carbon two top gaseous phase is distributed with methane/hydrogen piece-rate system converges, mixed into expander inlet
Tank is closed, gas phase is as the charging of expanding machine, and liquid phase mixes with expander outlet material, enters inlet/outlet knockout drum, the gas phase separated
For second burst of hydrogen product, the liquid phase part separated provides cold for the condenser in the recovery tower of carbon two, and another part is tail
Gas heat exchanger provides deep cooling cold.
Deep cooling cold needed for methane/hydrogen piece-rate system, is not all of hydrogen and the methane throttling isolated by the system
Produce, 68~83% cold is provided by expanding machine；
In step (2), the gas phase of hydrogen/methane separation tank separation branch to the ratio of hydrogen methane expander system 63~
Between 100%.
In step (3), the recovery tower of carbon two is fed based on methane, below -108 DEG C of tower top temperature.
In step (4), the volumn concentration of hydrogen is 83~92% in expanding machine charging.
The present invention can be achieved through the following technical solutions：
The lighter hydrocarbons deep cooling process for separating flow contains a set of cracking gas chilling train.
Plate-fin tail gas heat exchanger (being placed in ice chest), multiple domethanizing columns containing some series connection in chilling train are entered
Expect knockout drum and a methane/hydrogen separator system.
The function of chilling train is mainly cooling cracking gas, provides charging for domethanizing column, and separate hydrogen.Required for it
Cold it is main provided by propylene refrigerant, ethene cryogen and hydrogen/methane expander system, while reclaiming cycle ethane, demethanation
The cold of tower bottoms, hydrogen and Methane offgas etc..
The methane/hydrogen piece-rate system contains most cold tail gas heat exchanger, a hydrogen/methane separation tank and a hydrogen
Qi leel stream controller.The hydrogen flow controller, shunt ratio between 63~100%, the hydrogen fed downstream hydrogen separated/
Methane expanding machine.The liquid phase methane that the system is isolated, is not directly to do methane product, but return tail gas heat exchange re-heat to-
After 101 DEG C, one most upper charging as domethanizing column, further to reclaim the component of carbon two therein.
The lighter hydrocarbons deep cooling process for separating flow use high pressure demethanation technology, single column, tower be pressed in 2.9~3.2MPaG it
Between, there are four bursts of chargings, by the ethene cryogen condensing reflux of most cold (- 101 DEG C) one-level.Replaced original time in demethanizer overhead
Tank is flowed, a recovery tower of carbon two is separately set, using segregation fractionating column (CFT) pattern, by a part for hydrogen/methane expander outlet
Liquid phase methane provides cold, reclaims ethene.
The lighter hydrocarbons deep cooling process for separating flow also expands/recompressed machine system containing a set of hydrogen, methane, including hydrogen/
Methane expanding machine, Methane offgas recompression machine and hydrogen each one of machine of recompression.
The hydrogen/methane expanding machine, it is mainly low temperature H2 that it, which feeds, the need for manufacturing and designing, and can also may be used for one section
It is divided into two sections, entrance sets hydrogen/methane blended tank, outlet sets knockout drum.Set expenditure and pressure valve parallel with expanding machine, be used for
Liquid phase is from entrance blending tank to the direct conveying for exporting knockout drum.
The hydrogen/methane expander system, except being that methane/hydrogen piece-rate system and the recovery tower of carbon two provide cold first
Outside, carbon two can also be reclaimed to the H2 in tower top methane and reclaim clean, and the higher hydrogen product of purity can be again separate out.
The present invention effect be：By the shunting hydrogen of vast scale, expanding machine is entered together with methane, not only can be direct
The hydrogen that one purity is 92~97mol% is isolated, tower top can also be reclaimed for chilling train, carbon two most cold one-level is provided
Cold, so as to isolate high pressure of one concentration between 95~99mol%, high-purity hydrogen, and makes whole Quench and demethanation
Ethylene loss rate is reduced to 0.039~0.084% ultra low levels in system.Hydrogen loss is can be controlled in Methane offgas
Within 0.3%.
Demethanizer reflux tank is replaced with the recovery tower of carbon two, Recovery rate of ethylene can be made to improve 0.5 percentage point, for one
1,000,000 tons/year of ethylene light hydrocarbon devices are covered, ethene about 622kg/h, annual nearly 50,000,000 yuan of yield of increase are reclaimed more equivalent to.
Brief description of the drawings
One of process flow diagram of Fig. 1 prior arts.
Fig. 1 description of symbols：
1~7-1#~7# tail gas heat exchangers；8- methane recompresses machine；9- exports water cooler；10- Methane offgas；11- low pressure
Methane；12- high pressure hydrogens；14- cycle ethanes；17- cracking gases；18- hydrocarbon liquid；The pre- domethanizing column kettle liquids of 19-；20- domethanizing columns
Kettle liquid；21- cycle ethane vaporizers；The pre- domethanizing column feed coolers of 22-；The pre- domethanizing column charging knockout drums of 23-；24~
26-1~3# domethanizing columns feed knockout drum；27- hydrogen/methane separation tank；28- domethanizing columns first feed chiller；29- piptonychias
Alkane tower second feeds chiller；The pre- domethanizing columns of 30-；The pre- demethanizer reboilers of 31-；The pre- domethanizing column condensers of 32-；33-
Domethanizing column；34- demethanizer reboilers；35- domethanizing column condensers；37- reflux pumps；38- return tanks；40- Methane offgas
Expanding machine.
The process flow diagram of Fig. 2 present invention.
Fig. 2 description of symbols：
1~7-1#~7# tail gas heat exchangers；8- methane recompresses machine；9- methane water coolers；10- Methane offgas；12- high pressures
Hydrogen；13- low pressure hydrogens；14- cycle ethanes；15- hydrogen water coolers；16- hydrogen recompresses machine；17- cracking gases；20- piptonychias
Alkane tower bottoms；21- cycle ethane vaporizers；24~26-1#~3# domethanizing columns charging knockout drum；27- hydrogen/methane separation tank；
28- domethanizing columns first feed chiller；29- domethanizing columns second feed chiller；33- domethanizing columns；34- domethanizing columns are again
Boil device；35- domethanizing column condensers；The recovery tower condenser of 36- carbon two；37- reflux pumps；The recovery tower of 39- carbon two；41- hydrogen/methane
Expanding machine；42- expander inlet blending tanks；43- choke valves；44- exports knockout drum；45- hydrogen flow controllers；46- methane/
Hydrogen separator system.
Embodiment
With reference to embodiment, the present invention is further illustrated.
Embodiment
As shown in Fig. 2 a kind of lighter hydrocarbons cryogenic separation retracting device.
Including:Domethanizing column 33, the recovery tower 39 of carbon two, 1#~7# tail gas heat exchangers, the charging separation of 1#~3# domethanizing columns
Tank, described device is provided with methane/hydrogen piece-rate system, including：1# tail gas heat exchangers 1, hydrogen/methane separation tank 27 and hydrogen flow
Controller 45；The 3# domethanizing columns charging overhead line of knockout drum 26 connects hydrogen/methane separation tank 27 after 1# tail gas heat exchangers 1,
Hydrogen/bottom line of methane separation tank 27 connects domethanizing column 33 after 1# tail gas heat exchangers 1；The top of hydrogen/methane separation tank 27 goes out
Hydrogen flow controller 45, the bypass line connection hydrogen methane expanding machine system of hydrogen flow controller 45 are set on mouth pipeline
System；
Condenser, the recovery tower bottom of carbon two are set in the top of the domethanizing column 33 connection recovery tower 39 of carbon two, the recovery tower 39 of carbon two
Portion connects domethanizing column 33, the top of two recovery tower of carbon 39 connection hydrogen methane expander system；
Hydrogen methane expander system includes：Expander inlet blending tank 42, expanding machine 41, outlet knockout drum 44；Hydrogen
The bypass line of shunt controller 45 is connected expander inlet blending tank 42 after merging with the overhead line of two recovery tower of carbon 39, expands
The top of machine entrance blending tank 42 connection expanding machine 41, the outlet line of expanding machine 41 and the outlet line of expander inlet blending tank 42 are closed
And rear connection outlet knockout drum 44, the outlet bottom line of knockout drum 44 is divided into cold in two, a connection recovery tower 39 of carbon two
Condenser, another is sent out out-of-bounds after tail gas heat exchanger.
Wherein, the recovery tower 39 of carbon two uses segregation fractionating column pattern.
The cracking gas of drying and dehydrating enters after chilling train, passes through common autoclave heat exchanger and the plate-fin tail of multiple series connection
Gas heat exchanger, through propylene refrigerants at different levels, cycle ethane, domethanizing column kettle liquid and ethene cryogen at different levels etc., is cooled to -45 step by step
~-55 DEG C, -70~-72 DEG C and -96~-98 DEG C, liquid phase therein is isolated by 1#, 2# and 3# domethanizing column charging knockout drum,
From bottom to top successively as first, second, and third burst of charging of domethanizing column 33.
Last remaining cracking gas contains the feedings such as the H2 and CO of the overwhelming majority, the CH4 more than half and a small amount of C2 ' s
Methane/hydrogen separator system, -152~-182 DEG C of even following, entrance are further cooled to through most cold end 1# tail gas heat exchangers
Hydrogen/methane separation tank.The liquid phase that tank bottom is isolated, predominantly CH4 and C2 ' s, return to 1# tail gas heat exchangers by governor valve control and answer
After extremely more than -101 DEG C of heat, as most upper one (the 4th strand) charging of domethanizing column, the component of carbon two therein is fully reclaimed.Tank
The high-purity hydrogen that the gas separated is 95~99mol% concentration is pushed up, a small part is distributed by hydrogen flow controller, through cracking
Re-heat is to normal temperature (30 DEG C) after gas chilling train recovery cold, directly as high pressure hydrogen product；After another major part is then sent to
Continuous hydrogen, methane expander system.
Demethanizer reboiler does thermal source with propylene refrigerant, it is ensured that tower reactor is free of CH4；Tower top is cooled to ethene cryogen-
98 DEG C or so.Bottom of towe kettle liquid product send downstream units through chilling train re-heat, part after vaporizing；Top gaseous phase effluent sends into carbon
Two recovery tower bottoms, reclaim ethene, improve its rate of recovery.The recovery tower of carbon two by hydrogen/methane expander outlet a part of liquid phase
Ethylene contents are in below 0.2mol% in methane condensing reflux, its controllable overhead product；Bottom of towe liquid phase returns to demethanation tower top
Flow back together.
The hydrogen that the recovery top gaseous phase product of carbon two is distributed with methane/hydrogen separator system converges, together into hydrogen/first
Alkane expander inlet blending tank, gas phase is as the charging of expanding machine, and liquid phase bypasses expansion after Liquid level is depressurized through choke valve
Machine is directly discharged material with it and mixed, and expander outlet knockout drum is discharged into jointly.The gas phase that knockout drum is separated is second strand of hydrogen
Product, purity provides the refrigeration cold of most cold level for chilling train in more than 92mol%；Liquid phase is high-purity methane, by liquid level control
System discharge a, part first provides cold for the scrubber overhead of carbon two, and chilling train is then continued as together with another part and provides deep
Cold amount.
In the latter half of chilling train, two bursts of hydrogen products, Methane offgas, cycle ethane and ethylene product are cold through propylene
Agent etc. is reclaimed after cold, by re-heat to about 30 DEG C.High Pressure Hydrogen pneumatic transmission methanation unit is directly sent outside；Low pressure hydrogen through pressing again
Contracting machine is sent outside after being increased to about 2.5MPaG, and wherein one section of hydrogen gas compressor is driven by expanding machine.Methane offgas is through recompressing machine liter
0.50MPaG or so is depressed into, send drier regenerative system to use, finally send pyrolysis furnace to make fuel.
Claims (7)
1. a kind of lighter hydrocarbons cryogenic separation retracting device, including:Domethanizing column, the recovery tower of carbon two, 1#~7# tail gas heat exchangers, 1#~
3# domethanizing columns feed knockout drum, it is characterised in that：
Described device is provided with methane/hydrogen piece-rate system, including：1# tail gas heat exchangers, hydrogen/methane separation tank and hydrogen flow control
Device processed；3# domethanizing columns charging knockout drum overhead line connects hydrogen/methane separation tank, hydrogen/methane point after 1# tail gas heat exchangers
From pot bottom pipeline domethanizing column is connected after 1# tail gas heat exchangers；Hydrogen is set on hydrogen/methane separation tank top outlet line
Shunt controller, the bypass line connection hydrogen methane expander system of hydrogen flow controller；
Demethanizer overhead connects and condenser is set in the recovery tower of carbon two, the recovery tower of carbon two, and carbon two reclaims tower bottom connection piptonychia
Connection hydrogen methane expander system at the top of alkane tower, the recovery tower of carbon two；
Hydrogen methane expander system includes：Expander inlet blending tank, expanding machine, outlet knockout drum；Hydrogen flow controller
Bypass line and the recovery tower overhead line of carbon two merge after be connected expander inlet blending tank, expander inlet blending tank top
Connect expanding machine, connection outlet knockout drum after expander outlet pipeline and expander inlet blending tank outlet line merge, outlet
Knockout drum bottom line is divided into the condenser in two, a connection recovery tower of carbon two, and another is sent out after tail gas heat exchanger
Out-of-bounds.
2. lighter hydrocarbons cryogenic separation retracting device as claimed in claim 1, it is characterised in that：
The recovery tower of carbon two uses segregation fractionating column pattern.
3. a kind of lighter hydrocarbons cryogenic separation recovery method using device as claimed in claim 1 or 2, it is characterised in that methods described
Including：
1) cracking gas of drying and dehydrating is isolated wherein after heat exchange and cooling by 1#, 2# and 3# domethanizing column charging knockout drum
Liquid phase, from bottom to top successively as first, second, and third burst of domethanizing column charging；
2) gas phase of 3# domethanizing columns charging knockout drum enters hydrogen/methane separation tank, hydrogen/methane after being exchanged heat through 1# tail gas heat exchangers
The liquid phase of knockout drum separation is fed after being exchanged heat through 1# tail gas heat exchangers as the 4th strand of domethanizing column；Hydrogen/methane separation tank point
From gas phase portion as high pressure hydrogen send out out-of-bounds, partly branch to hydrogen methane expander system；
3) the demethanation top gaseous phase feeding recovery tower of carbon two, reclaims ethene, and the recovery tower bottom of towe of carbon two is back to domethanizing column；
4) hydrogen that the recovery of carbon two top gaseous phase is distributed with methane/hydrogen piece-rate system converges, into expander inlet blending tank,
Gas phase is as the charging of expanding machine, and liquid phase mixes with expander outlet material, enters inlet/outlet knockout drum, and the gas phase separated is second
Stock hydrogen product, the liquid phase part separated provides cold for the condenser in the recovery tower of carbon two, and another part exchanges heat for tail gas
Device provides deep cooling cold.
4. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, it is characterised in that：
In step (2), the gas phase of hydrogen/methane separation tank separation branch to the ratio of hydrogen methane expander system 63~
Between 100%.
5. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, it is characterised in that：
In step (3), the recovery tower of carbon two is fed based on methane, and tower top temperature is below -108 DEG C.
6. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, it is characterised in that
In step (4), the volumn concentration of hydrogen is 83~92% in expanding machine charging.
7. lighter hydrocarbons cryogenic separation recovery method as claimed in claim 3, it is characterised in that：
68~83% of deep cooling cold needed for methane/hydrogen piece-rate system are provided by expanding machine.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107285973A (en) * | 2016-03-30 | 2017-10-24 | 中国石油化工股份有限公司 | The production and processing technology and production equipment of a kind of hydrocarbon gas containing naphthalene |
| CN106766674B (en) * | 2016-12-09 | 2019-03-08 | 杭州杭氧股份有限公司 | A kind of ice chest deep cooling separating method of preparing isobutene through dehydrogenation of iso-butane project |
| CN108276236B (en) * | 2017-01-06 | 2020-08-04 | 中国石化工程建设有限公司 | Cryogenic separation and recovery method for Fischer-Tropsch synthesis tail gas for increasing olefin yield |
| CN110006216B (en) * | 2019-03-29 | 2020-01-24 | 大连理工大学 | Separation and recovery process of non-condensable exhaust gas from ethylene cycle refrigeration system coupled with cryogenic and membrane |
| CN111895723B (en) * | 2019-05-06 | 2022-06-21 | 中国石化工程建设有限公司 | Separation device and separation method for reaction generated gas in propylene preparation through propane dehydrogenation |
| CN114034129B (en) * | 2021-11-26 | 2022-08-16 | 北京恒泰洁能科技有限公司 | Energy expansion reconstruction device and method for pyrolysis gas post-hydrogenation device |
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| US3902329A (en) * | 1970-10-28 | 1975-09-02 | Univ California | Distillation of methane and hydrogen from ethylene |
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| CN103542693A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Ethylene cryogenic separation method for large-scale ethylene plant |
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| JPS54103797A (en) * | 1978-02-03 | 1979-08-15 | Sumitomo Heavy Ind Ltd | H2 separation and purification from h2 containing gas |
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| US3902329A (en) * | 1970-10-28 | 1975-09-02 | Univ California | Distillation of methane and hydrogen from ethylene |
| CN102675024A (en) * | 2011-03-07 | 2012-09-19 | 中国石油化工股份有限公司 | Separation process for preparing low-carbon olefin gas through methanol conversion |
| CN103318859A (en) * | 2012-03-22 | 2013-09-25 | 中国石油化工集团公司 | Rectification dehydration tower and dehydration method for nitrogen dioxide |
| CN103542693A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Ethylene cryogenic separation method for large-scale ethylene plant |
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