CN106316760A - Separation method for reaction product of propane dehydrogenated propylene preparation - Google Patents
Separation method for reaction product of propane dehydrogenated propylene preparation Download PDFInfo
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- CN106316760A CN106316760A CN201510354671.2A CN201510354671A CN106316760A CN 106316760 A CN106316760 A CN 106316760A CN 201510354671 A CN201510354671 A CN 201510354671A CN 106316760 A CN106316760 A CN 106316760A
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- propylene
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Abstract
The invention discloses a separation method for a reaction product of propane dehydrogenated propylene preparation and belongs to the field of petrochemical industry. The method comprises the following steps: (1) the reaction product of propane dehydrogenated propylene preparation is pretreated, then, the pretreated reaction product enters a propylene and ethylene cascaded refrigeration system with an expander, and then, a liquid phase is fed to a deethanizer; (2) top oil gas of the deethanizer is condensed and then enters a reflux tank of the deethanizer, tank bottom liquid of the reflux tank of the deethanizer totally returns to the deethanizer, tank top gas of the reflux tank of the deethanizer enters a top condensation section of the deethanizer and is fractionated by the condensation section, and top gas of the condensation section is condensed by a refrigerator of the top condensation section of the deethanizer under the action of a propylene refrigerating system and then enters a deep freezing tank of the deethanizer; (3) tank top gas of the deep freezing tank of the deethanizer is delivered out of a device as fuel gas, and bottom liquid of the deethanizer enters a propylene refiner; and (4) a refined propylene product is fractionated from the top of the propylene refiner, a bottom liquid phase of the propylene refiner enters a depropanizer, and a bottom product C4+ cut of the depropanizer is delivered out of the device. By adopting the separation method, the problems, i.e., large absorbent circulating rate and high energy consumption in the prior art can be solved.
Description
Technical field
The invention belongs to petrochemical industry or gas chemical industry field, be specifically related to a kind of dehydrogenating propane
The separation method of propylene product processed.
Background technology
Propylene is basic organic chemical industry raw material important in chemical industry.The most domestic and international third
The source of alkene relies primarily on naphtha pyrolysis coproduction and FCC by-product.According to statistics, in the third of the whole world
In alkene demand, Chinese market has accounted for more than 15%, and consumption figure also with annual about 5%～
The speed increment of 6%, propylene insufficiency of supply-demand continues to increase in recent years.Tight along with petroleum resources
Lack, and Gas Prices is cheap relative to crude oil price, thus derivation and C3 and the C4 alkane that comes
Hydrocarbon is increasingly paid close attention to by people, and wherein propane catalytic dehydrogenation technology (PDH) is undoubtedly C3
Utilize the focus that field is of greatest concern.
On following domestic market, along with constantly going into operation of methanol-to-olefins (MTO) device,
Traditional FCC and cracking of ethylene will certainly be produced alkene route and produce impact.As FCC and
Propylene and the isobutene. yield of cracking of ethylene by-product can be fewer and feweri.Therefore, dehydrogenating propane system third
Alkene technology faces an extraordinary opportunity to develop, and market potential is huge.
At present, preparing propylene by dehydrogenating propane patented technology has in the world: the Oleflex of Uop Inc.
Technique, the Catofin technique of ABB Lu Musi company, the Star technique of Kang Fei (Uhde) company,
The FBD-4 technique of Snamprogetti/Yarsintz company and woods moral/BASF AG
PDH technique.The commonly used cryogenic technology of these techniques separates preparing propylene by dehydrogenating propane reaction and produces
Thing.Deep cooling process for separating is the main method that naphtha steam cracking product separates, technology maturation,
Being widely used, owing to refrigerant temperature is low, in product, carbon three virtually all condenses out,
Thus propene yield is high, but equipment material being required height, energy consumption is high.
Chinese patent CN102795956B discloses dividing of a kind of preparing propylene by dehydrogenating propane product
From method, the mode that the method uses membrance separation and cryogenic separation to combine separates dehydrogenating propane system
Propylene product.But the membrance separation hydrogen rich gas response rate is relatively low, need list as sent outside as product
Solely compression, total energy consumption does not reduce.
BASF Aktiengesellchaft disclose a series of patent CN100567230C, CN101087740B,
CN101137605A, CN101415661A, these patents include and are reacted to produce from dehydrogenating propane
The overall process that thing separates.Because product contains H2O、CO2、CO、N2Deng, CN100567230C
Disclose and use the technique of washing to remove partial impurities, CN101087740B, CN101137605A
Disclose employing inertia absorbent and separate this partial impurities.CN101415661A discloses one and adopts
By the method for pressure-variable adsorption, isolate propylene product.But the hydrogen-rich gas obtained by these methods
Middle hydrogen content is relatively low, and hydrocarbon content is high, can only burn as fuel gas.
Chinese patent CN102040445 discloses a kind of lower carbon number hydrocarbons dehydrogenation producing propylene rich in propane
Technique whole process, this patent uses gasoline to separate light group in dehydrogenating propane product as absorbent
Divide and carbon three.But in dehydrogenating propane product, hydrogen content is high, and required absorbent circulating load is very
Greatly, energy consumption is high.
Summary of the invention
It is an object of the invention to provide the separation method of a kind of preparing propylene by dehydrogenating propane product,
To overcome the absorbent circulating load that above-mentioned prior art exists big, the problem that energy consumption is high.
For solving above-mentioned technical problem, the technical solution used in the present invention is:
The separation method of a kind of preparing propylene by dehydrogenating propane product, it is characterised in that under including
State step:
1) preparing propylene by dehydrogenating propane product enters dethanizer, dethanizer tower after pretreatment
Deethanizer reflux tank, the tank bottoms liquid of deethanizer reflux tank is entered after top oil gas is condensed
All backflow returns dethanizer, and deethanizer reflux tank tank deck gas enters dethanizer
Top condensed section of fractional distillation of condensation segment, condensation segment top gas is in the effect of propylene refrigeration system
Lower entrance dethanizer deep cooling tank after deethanization tower top condensation segment refrigerator condenses；
2) dethanizer deep cooling tank tank deck gas is as fuel gas carrying device, dethanizer deep cooling tank
The backflow of tank bottoms liquid is all back to deethanization tower top condensation segment, and at the bottom of dethanizer, liquid enters
Enter fine propylene tower；
3) fractionating out fine propylene product in fine propylene column overhead, fine propylene tower tower bottom liquid enters de-third mutually
Alkane tower, fractionates out propane at depropanizing tower tower top and takes off as reaction cycle logistics return propane
Hydrogen propylene reactive moieties, depropanizing tower bottom product C4+ fraction carrying device.
The separation method of the present invention a kind of preparing propylene by dehydrogenating propane product, its further feature
It is: the pretreatment of described preparing propylene by dehydrogenating propane product is that product is through three grades of pressures
Contracting, after being compressed to 1.2～2.0MPa (gauge pressures), the most cooled and dry.By in product
Water content be down to below 1ppm.Then, the product of drying is at propylene refrigeration system
It is cooled to-35～-20 DEG C through deethanization tower top condensation segment refrigerator under effect, enters one section of deep cooling
Tank carries out gas-liquid separation, and gas phase is after heat exchange cools down, through two under the effect of ethylene refrigeration system
Section refrigerator is cooled to-95～-85 DEG C, enters two-stage nitration deep cooling tank and carries out gas-liquid separation, head space gas
After heat exchange, returning reactive moieties mostly as recycle hydrogen, residual gas is sent as propane hydrogen
Device.One section of deep cooling tank and the tank bottoms liquid phase of two-stage nitration deep cooling tank is the most boosted, heat exchange converges entrance
Dethanizer.
The separation method of the present invention a kind of preparing propylene by dehydrogenating propane product, its further feature
Be: described deethanization tower top condensation segment arranges board-like or filler tower tray, theoretical trays number be 5～
15 pieces.
The separation method of the present invention a kind of preparing propylene by dehydrogenating propane product, its further feature
It is: described deethanizer overhead operation pressure is 2.4～2.6MPa (gauge pressures), dethanizer tower
Top operation temperature 50～55 DEG C, operates temperature 65～70 DEG C, dethanizer tower at the bottom of dethanizer tower
Top oil gas condenses to 40～45 DEG C through deethanization overhead condenser, enters deethanizer reflux tank,
The tank bottoms liquid of deethanizer reflux tank through deethanizer reflux pump boost after in liquid level and flow tandem
All returning dethanizer as backflow under control, deethanizer reflux tank tank deck gas enters de-
Ethane tower top condensation segment, condensation segment top gas under propylene refrigeration system effect through dethanizer
Top condensation segment refrigerator condensation enters dethanizer deep cooling tank, tank deck gas to-25～-20 DEG C
As fuel gas carrying device under tower top pressure control, tank bottoms liquid is through deethanization overhead condensation
All it is back to take off as backflow after section reflux pump boosting under tank bottoms liquid level and flow serials control
Ethane tower top condensation segment.Liquid at the bottom of dethanizer is pressed under tower reactor liquid level and flow serials control certainly
Enter fine propylene tower.
The separation method of the present invention a kind of preparing propylene by dehydrogenating propane product, its further feature
It is: described dethanizer uses the low level heat source such as low-pressure steam or coal heating and water.Deethanization
Overhead condenser uses the low-temperature receiver such as recirculated water or air.
Described fine propylene tower and depropanizing tower, those skilled in the art, can as the case may be,
Fine propylene tower uses heat pump flowsheet or old process, and depropanizing tower is also adopted by old process.
The separation method of the present invention a kind of preparing propylene by dehydrogenating propane product, uses band deethanization
The mode of overhead condensation section deethanization technique separates preparing propylene by dehydrogenating propane product, propane
Dehydrogenation producing propylene product enters employing band deethanization tower top condensation segment deethanization after pretreatment
Tower, then through propylene rectification, depropanization, it is thus achieved that polymer grade fine propylene, propane is as reaction cycle
Logistics is back to reactive moieties and continues reaction.
The present invention compared with prior art has the advantages that
1) separation method of a kind of preparing propylene by dehydrogenating propane of present invention product, uses the de-second of band
Alkane overhead condensation section deethanization technique, dethanizer is routine operation, and dethanizer reboiler can
Use the conventional heat sources such as coal heating and water or low-pressure steam, deethanization overhead condenser can use air cooling or
Circulating water condensing tower overhead gas, operation is convenient.
2) in deethanizer reflux tank, tank deck gas phase enters deethanization tower top condensation segment, through deethanization
Overhead condensation section fractional distillation, dethanizer condensation segment top gas is through deethanization tower top condensation segment refrigerator
After condensation, entering dethanizer deep cooling tank, fixed gas delivers to fuel gas pipe network under Stress control,
Liquid phase returns dethanizer condensation through the boosting of dethanizer condensation segment reflux pump as backflow is whole
Section.The content of propylene in fixed gas can be reduced, to ensure propene yield.
3) using band deethanization tower top condensation segment deethanization technique, dethanizer need not be at low temperatures
Running, major part energy consumption is using conventional heat sources and low-temperature receiver, and operation is convenient, deethanizer reflux
In tank, the fractional distillation of tank deck gas phase provides low-temperature receiver by propylene refrigeration system, and institute's chilling requirement is few, and energy consumption is with often
Rule deethanization ratio relatively low more than 30%.
The present invention is described in further detail with detailed description of the invention below in conjunction with the accompanying drawings, but
It is not limiting as the range of the present invention.
Accompanying drawing explanation
Fig. 1 is the separation method flow process signal of the present invention a kind of preparing propylene by dehydrogenating propane product
Figure.
Reference shown in figure is: 1-preparing propylene by dehydrogenating propane product, 2-three stage compression
Machine system, 3-compression outlet cooling unit, 4-drying system, mono-section of refrigerator of 5-, 6-mono-section
Deep cooling tank, mono-section of deep cooling tank gaseous phase outlet cooling unit of 7-, 8-two-stage nitration refrigerator, 9-ethylene system
Cooling system, 10-two-stage nitration deep cooling tank, the 11-two-stage nitration tank bottoms liquid phase of deep cooling tank, mono-section of deep cooling tank liquid of 12-
Phase, 13-propane hydrogen, 14-recycle hydrogen, 15-dethanizer, 16-deethanization overhead condenser,
17-deethanizer reflux tank, 18-deethanization tower top condensation segment, 19-deethanization tower top condensation segment system
Cooler, 20-dethanizer deep cooling tank, 21-deethanization tower top condensation segment reflux pump, 22-deethanization
Tower reflux pump, 23-fine propylene tower, 24-depropanizing tower, 25-fine propylene product, 26-propane,
27-C4+ fraction, 28 propylene refrigeration system, 29-fuel gas.
Detailed description of the invention
As it is shown in figure 1, preparing propylene by dehydrogenating propane product 1 is through three stage compression system 2, compression
To 1.2～2.0MPa (gauge pressures), compressed outlet cooling unit 3 is cooled to 5～10 DEG C, enters
Drying system 4, is down to below 1ppm by the water content in product.At propylene refrigeration system
After one section of refrigerator 5 is cooled to-35～-20 DEG C, enter one section of deep cooling tank 6 under the effect of 28 enter
Row gas-liquid separation, tank deck gas phase after one section of deep cooling tank gaseous phase outlet cooling unit 7 heat exchange,
It is cooled to-95～-85 DEG C through two-stage nitration refrigerator 8 under the effect of ethylene refrigeration system 9, enters two
Section deep cooling tank 10 carries out gas-liquid separation, after head space gas heat exchange, returns mostly as recycle hydrogen 14
Returning reactive moieties, residual gas is as propane hydrogen 13 carrying device.One section of deep cooling tank liquid phase 12
, heat exchange the most boosted with the two-stage nitration tank bottoms liquid phase of deep cooling tank 11 converges entrance dethanizer 15.
Dethanizer 15 top operation pressure 2.4～2.6MPa (gauge pressure), tower top operation temperature 50～
55 DEG C, operation temperature 65 at the bottom of tower～70 DEG C, tower top oil gas condenses through deethanization overhead condenser 16
To 40～45 DEG C, entering deethanizer reflux tank 17, the tank bottoms liquid of deethanizer reflux tank is through de-
All return de-after ethane tower reflux pump 22 boosting under liquid level and flow serials control as backflow
Ethane tower 15, deethanizer reflux tank tank deck gas enters deethanization tower top condensation segment 18, condensation
Section top gas under the effect of propylene refrigeration system 28 through deethanization tower top condensation segment refrigerator
19 condensations enter dethanizer deep cooling tank 20, dethanizer deep cooling tank tank deck to-25～-20 DEG C
Gas is as fuel gas 29 carrying device under tower top pressure control, and dethanizer deep cooling tank is tank bottoms
Liquid through deethanization tower top condensation segment reflux pump 21 boost after at tank bottoms liquid level and flow serials control
Lower as backflow be all back to deethanization tower top condensation segment 18.At the bottom of dethanizer, liquid is in tower reactor
From being pressed into into fine propylene tower 23 under liquid level and flow serials control.
Under fine propylene tower 23 acts on, tower top fractionates out fine propylene product 25, and tower bottom liquid enters mutually
Depropanizing tower 24, under depropanizing tower 24 acts on, depropanizing tower tower top fractionates out propane 26 and makees
Returning reactive moieties for reaction cycle logistics and continue reaction, depropanizing tower bottom product C4+ fraction send
Go out device.
Described deethanization tower top condensation segment arranges board-like tower tray, and theoretical trays number is 5～15 pieces.
Described dethanizer uses the low level heat source such as low-pressure steam or coal heating and water.Dethanizer
Top condenser uses the low-temperature receiver such as recirculated water or air.
Described fine propylene tower and depropanizing tower, those skilled in the art, can as the case may be,
Fine propylene tower uses heat pump flowsheet or old process, and depropanizing tower is also adopted by old process.
Claims (5)
1. the separation method of a preparing propylene by dehydrogenating propane product, it is characterised in that include following step
Rapid:
1) preparing propylene by dehydrogenating propane product enters dethanizer, deethanizer overhead after pretreatment
Entering deethanizer reflux tank after oil gas is condensed, the tank bottoms liquid of deethanizer reflux tank is whole
Backflow returns dethanizer, and deethanizer reflux tank tank deck gas enters deethanization overhead condensation
Condensed section of fractional distillation of section, the de-second of condensation segment top gas warp under the effect of propylene refrigeration system
Dethanizer deep cooling tank is entered after the condensation of alkane overhead condensation section refrigerator；
2) dethanizer deep cooling tank tank deck gas is as fuel gas carrying device, dethanizer deep cooling tank tank
Liquid backflow in the end is all back to deethanization tower top condensation segment, and liquid at the bottom of dethanizer enters essence
Propylene tower；
3) fractionating out fine propylene product in fine propylene column overhead, fine propylene tower tower bottom liquid enters depropanization mutually
Tower, fractionates out propane at depropanizing tower tower top and returns dehydrogenating propane system as reaction cycle logistics
Propylene reactive moieties, depropanizing tower bottom product C4+ fraction carrying device.
The separation method of a kind of preparing propylene by dehydrogenating propane product the most according to claim 1, its
It is characterised by: described deethanization tower top condensation segment is provided with tower tray.
The separation method of a kind of preparing propylene by dehydrogenating propane product the most according to claim 2, its
Being characterised by: described tower tray is board-like or filler tower tray, theoretical trays number is 5～15 pieces.
The separation method of a kind of preparing propylene by dehydrogenating propane product the most according to claim 1, its
It is characterised by: described deethanizer overhead operation pressure is 2.4～2.6MPa (gauge pressures), de-
Ethane tower tower top operation temperature 50～55 DEG C, operates temperature 65～70 DEG C, de-second at the bottom of dethanizer tower
Alkane column overhead oil gas condenses to 40～45 DEG C through deethanization overhead condenser, enters deethanizer reflux
Tank.
The separation method of a kind of preparing propylene by dehydrogenating propane product the most according to claim 1, its
It is characterised by: the operation temperature of described dethanizer deep cooling tank is-25～-20 DEG C.
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| CN201510354671.2A CN106316760A (en) | 2015-06-24 | 2015-06-24 | Separation method for reaction product of propane dehydrogenated propylene preparation |
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| CN201510354671.2A CN106316760A (en) | 2015-06-24 | 2015-06-24 | Separation method for reaction product of propane dehydrogenated propylene preparation |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107118070A (en) * | 2017-05-11 | 2017-09-01 | 黑龙江安瑞佳石油化工有限公司 | A kind of new propylene refining method |
| CN108586185A (en) * | 2018-06-25 | 2018-09-28 | 榆林学院 | A kind of differential pressure thermocouple propylene refining piece-rate system and separation method |
| CN108645119A (en) * | 2018-06-14 | 2018-10-12 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device and method |
| CN109851461A (en) * | 2019-01-21 | 2019-06-07 | 中石化上海工程有限公司 | The method that naphtha and Deposition During Propane Pyrolysis front-end deethanization are coupled with PDH |
| CN112028731A (en) * | 2019-06-04 | 2020-12-04 | 中国石化工程建设有限公司 | Method for separating reaction product of propane dehydrogenation to propylene |
| CN112028734A (en) * | 2019-06-03 | 2020-12-04 | 中国石化工程建设有限公司 | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation |
| CN112939724A (en) * | 2019-12-11 | 2021-06-11 | 中国石油化工股份有限公司 | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation |
| CN113321564A (en) * | 2021-06-15 | 2021-08-31 | 中国石油化工股份有限公司 | Method and device for separating products from olefin production by low-carbon alkane dehydrogenation |
| CN113354504A (en) * | 2021-03-19 | 2021-09-07 | 北京欧谊德科技有限公司 | Separation device and separation method for preventing tower bottom of catalytic depropanizing tower from coking |
| CN113354503A (en) * | 2021-06-15 | 2021-09-07 | 中国石油化工股份有限公司 | Method and device for separating olefin products by dehydrogenation of low-carbon alkane |
| CN113372189A (en) * | 2021-06-15 | 2021-09-10 | 中国石油化工股份有限公司 | Separation process and device for olefin product prepared by low-carbon alkane dehydrogenation |
| WO2021237483A1 (en) * | 2020-05-25 | 2021-12-02 | 上海卓然工程技术股份有限公司 | Process method and system for co-production of propane dehydrogenation unit and ethylene unit |
| CN114573415A (en) * | 2020-11-30 | 2022-06-03 | 惠生工程（中国）有限公司 | Method and device for separating coupling type alkane catalytic dehydrogenation reaction product |
| CN115597309A (en) * | 2022-10-19 | 2023-01-13 | 中科泓能（北京）科技有限公司（Cn） | Low-energy-consumption separation method and system for propane dehydrogenation product |
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Cited By (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107118070A (en) * | 2017-05-11 | 2017-09-01 | 黑龙江安瑞佳石油化工有限公司 | A kind of new propylene refining method |
| CN108645119A (en) * | 2018-06-14 | 2018-10-12 | 北京恒泰洁能科技有限公司 | Dehydrogenating propane product gas cryogenic separation device and method |
| CN108645119B (en) * | 2018-06-14 | 2023-09-29 | 北京恒泰洁能科技有限公司 | Cryogenic separation device and method for propane dehydrogenation product gas |
| CN108586185B (en) * | 2018-06-25 | 2023-11-17 | 榆林学院 | Differential pressure thermocouple propylene refining and separating system and separating method |
| CN108586185A (en) * | 2018-06-25 | 2018-09-28 | 榆林学院 | A kind of differential pressure thermocouple propylene refining piece-rate system and separation method |
| CN109851461A (en) * | 2019-01-21 | 2019-06-07 | 中石化上海工程有限公司 | The method that naphtha and Deposition During Propane Pyrolysis front-end deethanization are coupled with PDH |
| CN112028734B (en) * | 2019-06-03 | 2023-08-29 | 中国石化工程建设有限公司 | Device and process for recycling reaction product of propylene preparation by propane dehydrogenation |
| CN112028734A (en) * | 2019-06-03 | 2020-12-04 | 中国石化工程建设有限公司 | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation |
| CN112028731B (en) * | 2019-06-04 | 2023-09-15 | 中国石化工程建设有限公司 | Method for separating propylene reaction product from propane dehydrogenation |
| CN112028731A (en) * | 2019-06-04 | 2020-12-04 | 中国石化工程建设有限公司 | Method for separating reaction product of propane dehydrogenation to propylene |
| CN112939724A (en) * | 2019-12-11 | 2021-06-11 | 中国石油化工股份有限公司 | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation |
| CN112939724B (en) * | 2019-12-11 | 2022-09-20 | 中国石油化工股份有限公司 | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation |
| WO2021237483A1 (en) * | 2020-05-25 | 2021-12-02 | 上海卓然工程技术股份有限公司 | Process method and system for co-production of propane dehydrogenation unit and ethylene unit |
| CN114573415A (en) * | 2020-11-30 | 2022-06-03 | 惠生工程（中国）有限公司 | Method and device for separating coupling type alkane catalytic dehydrogenation reaction product |
| CN114573415B (en) * | 2020-11-30 | 2024-03-19 | 惠生工程（中国）有限公司 | Separation method and device for coupled alkane catalytic dehydrogenation reaction products |
| CN113354504B (en) * | 2021-03-19 | 2023-09-08 | 北京欧谊德科技有限公司 | Separation device and separation method for preventing bottom coking of catalytic depropanizer |
| CN113354504A (en) * | 2021-03-19 | 2021-09-07 | 北京欧谊德科技有限公司 | Separation device and separation method for preventing tower bottom of catalytic depropanizing tower from coking |
| CN113372189A (en) * | 2021-06-15 | 2021-09-10 | 中国石油化工股份有限公司 | Separation process and device for olefin product prepared by low-carbon alkane dehydrogenation |
| CN113354503B (en) * | 2021-06-15 | 2022-12-02 | 中国石油化工股份有限公司 | Method and device for separating olefin products by low-carbon alkane dehydrogenation |
| CN113354503A (en) * | 2021-06-15 | 2021-09-07 | 中国石油化工股份有限公司 | Method and device for separating olefin products by dehydrogenation of low-carbon alkane |
| CN113321564A (en) * | 2021-06-15 | 2021-08-31 | 中国石油化工股份有限公司 | Method and device for separating products from olefin production by low-carbon alkane dehydrogenation |
| CN115597309A (en) * | 2022-10-19 | 2023-01-13 | 中科泓能（北京）科技有限公司（Cn） | Low-energy-consumption separation method and system for propane dehydrogenation product |
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Application publication date: 20170111 |