CN108883343A - A kind of gas fractionation unit - Google Patents
A kind of gas fractionation unit Download PDFInfo
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- CN108883343A CN108883343A CN201780005792.3A CN201780005792A CN108883343A CN 108883343 A CN108883343 A CN 108883343A CN 201780005792 A CN201780005792 A CN 201780005792A CN 108883343 A CN108883343 A CN 108883343A
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- tower
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- discharge port
- feed inlet
- tee tube
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
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- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
A kind of gas fractionation unit, including depropanizing tower (10), dethanizer (11), reboiler one (2), reboiler two (4) and propylene recovery tower (12), depropanizing tower (10) is equipped with feed inlet one, tower top discharge port one and tower bottom discharge port one, dethanizer (11) is equipped with feed inlet two, tower top discharge port two and tower bottom discharge port two, and propylene recovery tower (12) is equipped with feed inlet three, tower top feed inlet, tower top discharge port three and tower bottom discharge port three.
Description
Technical field
The present invention relates to a kind of gas fractionation units.
Background technique
There is a set of gas fractionation unit in Sinopec Zhongyuan Oil Field general petrochemical works of branch company, gas fractionation unit into
Expect the liquefied gas of the catalytic cracking unit production from the factory.It will be taken off under existing weaponry and equipment for the yield for further increasing propylene
The fixed gas of ethane column overhead increases a pipeline to catalytic cracking unit aerostatic press outlet liquid separation tank, makes the fixed gas of the part
Returning catalyticing cracking device recycles propylene therein.It is recorded according to pertinent literature, in two tail gas of carbon of deethanizer overhead
78.75% propylene content can be reduced to 72.28%.
Shaanxi extends 600,000 tons of annual gas fractionation units of petroleum Yan'an petrochemical plant, according to four conventional tower works
Skill, the volume fraction of propylene column overhead propylene product can reach 99.6%, and tower bottom propane volume fraction can reach 95.0%.2013
One absorption tower of engineered addition, process are as shown in Figure 1, the volume fraction of propylene column overhead propylene product can reach 99.8%
The highest device of country's propylene product yield at present.The tower top fixed gas of dethanizer is mixed into the diesel oil hydrogenation of charging by this device
Liquefied gas in, it is 3.83% that the content of propylene is increased by 0% before being transformed in the liquefied gas of diesel oil hydrogenation, every with 1,400,000 tons
330 days 1 year, 1000 tons of propylene can be recycled in the processing capacity in year, and the market price is about 5,000,000 yuan, and consumption reduction synergy is significant.Disadvantage：
The fluctuation of deethanizer overhead discharge pressure flow is especially big during operation or occurs often adjusting with the phenomenon of oil.
Summary of the invention
The present invention proposes a kind of gas fractionation unit, solves disadvantages described above existing in the prior art.
The technical proposal of the invention is realized in this way：A kind of gas fractionation unit, including depropanizing tower, dethanizer,
Reboiler one, reboiler two and propylene recovery tower, the depropanizing tower are equipped with feed inlet one, tower top discharge port one and tower bottom
Discharge port one, the dethanizer are equipped with feed inlet two, tower top discharge port two and tower bottom discharge port two, the propylene recovery tower
Equipped with feed inlet three, tower top feed inlet, tower top discharge port three and tower bottom discharge port three, the feed inlet three is set to the propylene
The tower bottom of recovery tower；The depropanizing tower is by pipeline and one connection of reboiler, and the dethanizer is by pipeline and again
Boil two connection of device；The feed inlet one of the depropanizing tower is passed through by pipeline and material inlet connection, the tower top discharge port one
Pipeline and two connection of feed inlet；The tower top discharge port two-way piping and three connection of feed inlet, the tower bottom discharge port threeway
Piping and one connection of feed inlet；The tower bottom discharge port one passes through pipeline and the first tee tube connection, first tee tube
One outlet goes out device, another outlet of first tee tube and the tower top feed inlet connection.
Preferably, the tower top discharge port one passes through pipeline successively connection condenser one, return tank one and the second threeway
The tower top connection of pipe, one of outlet of second tee tube and the depropanizing tower, second tee tube it is another
A outlet and two connection of feed inlet.
Preferably, the tower top discharge port two-way piping successively connection condenser two, return tank two and third threeway
Pipe, the one outlet of the third tee tube and the tower top connection of the dethanizer, another of the third tee tube go out
Mouth and three connection of feed inlet.
Preferably, another outlet of first tee tube is joined by heat exchanger and pump with the tower top feed inlet
It is logical.
Preferably, another outlet of first tee tube passes sequentially through heat exchanger and pump and the tower top feed inlet
Connection.
Preferably, head tank is equipped between the feed inlet one and the material inlet.
Preferably, it is equipped with the 4th tee tube between the material inlet and the head tank, the of the 4th tee tube
One end and material inlet connection, the second end and head tank connection of the 4th tee tube, the third end of the 4th tee tube
With three connection of tower top discharge port.
Beneficial effects of the present invention are：
Gas fractionation unit of the invention increases propylene recovery tower simple to operation, and the C4 that depropanizing tower tower bottom comes out makees
For absorbent, it is not necessary to buy absorbent, save the cost again again.
C4 is fed as absorbent by tower top, and C2 fixed gas is fed by tower bottom, and two materials inversely contact, and is conducive to inhale
It receives.
Propylene recovery tower tower pressure is identical as depropanizing tower overhead reflux pressure tank, is conducive to the C4 after absorbing and returns from pressure
Return depropanizing tower.
Propylene is that market at prices is higher and the biggish product of demand, status are that supply falls short of demand.The present invention passes through increase
Propylene recovery tower further recycles the component of propylene in liquefied gas, then the propylene product yield distillated by propylene recovery column overhead
99.99% is risen to, and the content of propylene is reduced to 65.9% in deethanizer overhead fixed gas, is in the market existing third
The yield and the rate of recovery that alkene recovery technology is unable to reach.Increased propylene recovery tower is not only easy to operate and investment cost is less.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
Some embodiments of invention without any creative labor, may be used also for those of ordinary skill in the art
To obtain other drawings based on these drawings.
Fig. 1 is the flow chart of the fractionating device of the prior art；
Fig. 2 is a kind of gas fractionation unit structural schematic diagram of the present invention.
In attached drawing：1- return tank one；2- reboiler one；3- return tank two；4- reboiler two；5- heat exchanger；6- pump；7- into
Batch can；8- condenser one；9- condenser two；10- depropanizing tower；11- dethanizer；12- propylene recovery tower.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, it is obtained by those of ordinary skill in the art without making creative efforts every other
Embodiment shall fall within the protection scope of the present invention.
As shown in Fig. 2, a kind of gas fractionation unit, including depropanizing tower 10, dethanizer 11, reboiler 1, reboiler
24 and propylene recovery tower 12, the depropanizing tower 10 is equipped with feed inlet one, tower top discharge port one and tower bottom discharge port one,
The dethanizer 11 is equipped with feed inlet two, tower top discharge port two and tower bottom discharge port two, and the propylene recovery tower 12 is equipped with
Feed inlet three, tower top feed inlet, tower top discharge port three and tower bottom discharge port three, the feed inlet three are set to the propylene recovery
The tower bottom of tower 12；The depropanizing tower 10 by pipeline and one 2 connection of reboiler, the dethanizer 11 by pipeline with
24 connection of reboiler；The feed inlet one of the depropanizing tower 10 passes through pipeline and material inlet connection, the tower top discharge port one
Pass through pipeline and two connection of feed inlet；The tower top discharge port two-way piping and three connection of feed inlet, the tower bottom discharge port
Threeway piping and one connection of feed inlet；The tower bottom discharge port one is by pipeline and the first tee tube connection, and the described 1st
Siphunculus one outlet goes out device, another outlet of first tee tube and the tower top feed inlet connection.
The tower top discharge port one passes through pipeline successively connection condenser 1, return tank 1 and the second tee tube, institute
One of outlet of the second tee tube and the tower top connection of the depropanizing tower 10 are stated, another of second tee tube goes out
Mouth and two connection of feed inlet.
The tower top discharge port two-way piping successively connection condenser 29, return tank 23 and third tee tube, institute
State the one outlet of third tee tube and the tower top connection of the dethanizer 11, another outlet of the third tee tube with
Three connection of feed inlet.
Another outlet of first tee tube passes through heat exchanger 5 and pump 6 and the tower top feed inlet connection.
Another outlet of first tee tube passes sequentially through heat exchanger 5 and pump 6 and the tower top feed inlet connection.
Head tank 7 is equipped between the feed inlet one and the material inlet.
Between the material inlet and the head tank 7 be equipped with the 4th tee tube, the first end of the 4th tee tube with
Material inlet connection, the second end and head tank connection, the third end of the 4th tee tube and tower top of the 4th tee tube
Three connection of discharge port.
Mainly there is carbon two (C2H6) raw material in the embodiment of the present invention, carbon three (C3H6, C3H8) carbon four (C4H10, C4H8,
C5H12, CCL2O (oxychlorination carbon, one of liquefied gas ingredient)).Ingredient in carbon four also all includes their isomerism
Body.
Head tank 7：Raw material is introduced into the mixing of this tank before entering tower, then flows into tower by the road again；
Condenser reboiler is all the heat exchanger to connect together with tower, depropanizing tower and dethanizer from functional perspective
Rectifying column is belonged to, general rectifying column is all with condenser and reboiler.Propylene recovery tower is functionally absorption tower.
The flow direction of fixed gas：When raw material in flow chart enters tower, all liquid.Tower bottom reboiler passes through different modes
Heat exchange provide heat for tower, so after raw material enters depropanizing tower, light component and heavy constituent are just separated, due to temperature liter
Height, tower top come out material in carbon two vaporize.This is that fixed gas most starts the position generated.
The gas-liquid mixture of depropanizing tower tower top enters in dethanizer, and passes through series reaction, last light component
It is come out from tower top, because tower bottom reboiler provides heat, the propylene of vaporized part.What tower top came out is exactly mainly carbon
Two fixed gas, the inside have carried our part purpose product propylene secretly.(enterprise typically now all selects fixed gas is straight
It connects to be mixed into civil liquefied gas and be sold directly as fuel, just do not reprocessed.There is seldom enterprise to mix this part fixed gas
Enter into the device in other workshops and utilized, the inside of telling somebody what one's real intentions are before is all described in detail.)
The fixed gas come out from deethanizer overhead, has carried part purpose product propylene secretly, so the present invention devises third
Alkene recovery tower is recycled.Fixed gas is entered by the tower bottom of propylene recovery tower, and gas rises from lower to upper, first tower depropanization
The heavies liquid that tower tower bottom comes out is entered by the tower top of propylene recovery tower, and liquid flows from top to bottom, is caused reverse contact and is inhaled
It receives.Heavy constituent absorbs the propylene in fixed gas, and fixed gas just almost less carries propylene, then the tower from propylene recovery tower secretly
Top row goes out fixed gas, this is the last whereabouts after fixed gas is absorbed.Absorb the heavies liquid of propylene in fixed gas again
It returns and is mixed in head tank with the raw material most started, propylene more in this way will enter the essence for carrying out a new round in depropanizing tower
Reaction is evaporated, when reaching propylene recovery tower, just has the propylene of more quality.
Depropanizing tower bottom C4 temperature after supercooling is down to 35 DEG C in the present embodiment, pump pressure increases to by pressurizeing
After 2.6MPa, device, about 10 tphs of another way entrance propylene recovery column overheads absorb deethanization as absorbent out all the way
Propylene in the fixed gas C2 of column overhead discharge.Fixed gas C2 is passed through by return tank gaseous phase outlet in deethanizer overhead return tank
Pipeline enters propylene recovery tower tower bottom, inversely contacts with C4 absorbent, and the propylene and propane in fixed gas C2 are inhaled by C4 absorbent
It receives, while a small amount of C4 enters C2 with fixed gas by propylene recovery column overhead discharger.Propylene recovery tower tower bottom can be obtained containing more
The heavy constituent mixture of high-content propylene, this material directly return at the charging of depropanizing tower, mixed with the product after catalytic cracking
Enter depropanizing tower as gas separation unit charging after conjunction.Depropanizing tower high pressure low temperature is conducive to absorb, so tower pressure is set as
2.0MPa, the discharging of propylene recovery tower tower bottom will return in depropanizing tower, so propylene recovery tower tower pressure should flow back with depropanizing tower
Tank is close, and propylene recovery tower tower pressure is set as 2.4MPa, so that it may from pressure flowing, not need again plus pump.Cryogenic high pressure not only may be used
To ensure that propylene and propane all recycle, and the emission loss of C 4 fraction can be reduced.This recycle stream was calculated through simulation softward
Cheng Hou, the content that can obtain propylene in deethanizer overhead fixed gas is 65.9%, the propylene product purity that propylene column overhead distillates
It is 99.99%.
The effect of heat exchanger 5：Because temperature is too high when pipeline comes out, propylene is volatile, if being directly entered propylene recovery
Preferable assimilation effect can be not achieved because the too high propylene caused in fixed gas of temperature is always gaseous state in tower.
Force (forcing) pump 6：Depropanizing tower come out material pressure be 18.5, propylene recovery column overhead pressure be 2.4, need by
It just can enter propylene recovery tower after pump pressurization.The pressure of pump is more and practical in 2.4 or more, 2.6 pressure pump contact
Situation may be floated, so having selected 2.6 pump.
Consider according to the actual situation, when operation, each column overhead tower bottom is provided with 0.5 pressure difference, tower top pressure
It is 0.5MPa smaller than tower bottom pressure.
The effect of overhead condenser：For depropanizing tower and dethanizer, the component in tower is all the component for being easy gasification,
It is to belong to gas-liquid mixture when tower top is conveyed outward by pipeline when temperature is higher in tower, all becomes after overhead condenser is cooling
At liquid, respectively enter in return tank of top of the tower.It is to be conducive to return stream and convey to next tower that it is latter, which to become liquid, second is that such as
Fruit may partially volatilize with the presence of gas to be caused to waste.Third is that recycling heat.So it is exactly first to go that material, which goes out tower top something,
Overhead condenser all becomes liquid.Institute's column data and phase are through tower in (one kind that condenser is heat exchanger) table
It is after cooling to push up condenser.
Propylene recovery tower is since the material of discharge is gas phase, so overhead condenser is not added.
The 1.8MPa the case where, for liquefied gas due to all liquid phases of pressurizeing, normal temperature and pressure is gas phase.Total feed is 300,000
Ton/year.
When not increasing propylene recovery tower, gas fractionation unit, which returns, directly will contain C2H6 (0.09) by pipeline B1,
The mixing fixed gas of C3H6 (0.3), C3H8 (0.01) are discharged.After propylene recovery tower is added, propylene recovery column overhead D1 pipeline row
Other components in C2H6 (0.05) C3H6 (0.00006) and raw material out.It can be seen that propylene flow is bright in the fixed gas of discharge
Aobvious decline.
It is entirely former almost without propylene C3H6 (0.00001) it can be seen from forming in 201 tower bottom line A2 of tower
Heavier component in material.It is divided into two groups by A2, one group of straight connecting device of A4, into other equipment area.One group is then that (flow is A3
100000 tons/year) enter propylene recovery tower, reactive absorption is carried out to the fixed gas mixture in B1 containing propylene, propylene is absorbed
Into the mixed liquor entered by A3 pipeline, charging is then transported to by propylene recovery tower tower bottom C3 pipeline again, is mixed with raw material.
Wherein, C3H6 (0.3) and C3H8, C4H10, C4H8, C5H12, C5H10, CCL2O (totally 10.01) are contained in pipeline C3, thus may be used
See, for propylene recovery tower, the charging in A3 pipeline absorbs the propylene in the charging of B1 pipeline, and liquid phase part is by having after absorption
The tower bottom pipeline D3 of absorbed propylene is returned and is mixed with raw material, and then, about 0.3 ten thousand tons/year of propylene is recovered.
The effect of heat exchanger 5：Because temperature is too high when pipeline A2 comes out, propylene is volatile, returns if being directly entered propylene
Preferable assimilation effect can be not achieved because the too high propylene caused in fixed gas of temperature is always gaseous state by receiving tower.
Force (forcing) pump 6：The material pressure that T-201 comes out is 18.5, and propylene recovery column overhead pressure is 2.4, is needed by pump
It just can enter propylene recovery tower after pressurization.The pressure of pump is more in 2.4 or more, 2.6 pressure pump contact, and practical feelings
Condition may be floated, so having selected 2.6 pump.
Consider according to the actual situation, when operation, each column overhead tower bottom is provided with 0.5 pressure difference, tower top pressure
It is 0.5MPa smaller than tower bottom pressure.
The effect of overhead condenser：For T-201 and T-202, the component in tower is all the component for being easy gasification, Ta Neiwen
It is to belong to gas-liquid mixture when tower top is conveyed outward by Q1 and Q2 pipeline when spending higher, it is complete after overhead condenser 8,9 is cooling
Portion becomes liquid, respectively enters return tank of top of the tower 1 and 2.It is to be conducive to return stream and convey to next tower that it is latter, which to become liquid,
Second is that causing to waste if there is gas exists partially to volatilize.Third is that recycling heat.So material goes out tower top something just
It is first to remove overhead condenser, all becomes liquid.Institute's column data and phase are equal in (one kind that condenser is heat exchanger) table
It is after cooling through overhead condenser.
Propylene recovery tower is since the material of discharge is gas phase, so overhead condenser is not added.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (7)
1. a kind of gas fractionation unit, it is characterised in that：Including depropanizing tower, dethanizer, reboiler one, reboiler two and
Propylene recovery tower, the depropanizing tower are equipped with feed inlet one, tower top discharge port one and tower bottom discharge port one, the dethanizer
Equipped with feed inlet two, tower top discharge port two and tower bottom discharge port two, the propylene recovery tower is equipped with feed inlet three, tower top is fed
Mouth, tower top discharge port three and tower bottom discharge port three, the feed inlet three are set to the tower bottom of the propylene recovery tower；Described de- third
Alkane tower passes through pipeline and two connection of reboiler by pipeline and one connection of reboiler, the dethanizer；The depropanization
The feed inlet one of tower passes through pipeline and two connection of feed inlet by pipeline and material inlet connection, the tower top discharge port one；Institute
State tower top discharge port two-way piping and three connection of feed inlet, the tower bottom discharge port threeway piping and one connection of feed inlet；
For the tower bottom discharge port one by pipeline and the first tee tube connection, the first tee tube one outlet goes out device, and described the
Another outlet of one tee tube and the tower top feed inlet connection.
2. gas fractionation unit as described in claim 1, it is characterised in that：The tower top discharge port one is successively joined by pipeline
Logical condenser one, return tank one and the second tee tube, one of outlet of second tee tube and the depropanizing tower
Tower top connection, second tee tube another outlet with two connection of feed inlet.
3. gas fractionation unit as described in claim 1, it is characterised in that：The tower top discharge port two-way piping successively joins
Logical condenser two, return tank two and third tee tube, the one outlet of the third tee tube and the tower of the dethanizer
Push up connection, another outlet of the third tee tube and three connection of feed inlet.
4. gas fractionation unit as described in claim 1, it is characterised in that：Another outlet of first tee tube passes through
Heat exchanger and pump and the tower top feed inlet connection.
5. gas fractionation unit as claimed in claim 4, it is characterised in that：Another outlet of first tee tube is successively
Pass through heat exchanger and pump and the tower top feed inlet connection.
6. gas fractionation unit as described in claim 1, it is characterised in that：Between the feed inlet one and the material inlet
Equipped with head tank.
7. gas fractionation unit as claimed in claim 6, it is characterised in that：It is set between the material inlet and the head tank
Have the 4th tee tube, the first end and material inlet connection of the 4th tee tube, the second end of the 4th tee tube with into
Batch can connection, the third end of the 4th tee tube and three connection of tower top discharge port.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/CN2017/094415 WO2019019034A1 (en) | 2017-07-26 | 2017-07-26 | Gas fractionation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108883343A true CN108883343A (en) | 2018-11-23 |
Family
ID=64325574
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780005792.3A Pending CN108883343A (en) | 2017-07-26 | 2017-07-26 | A kind of gas fractionation unit |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN108883343A (en) |
| WO (1) | WO2019019034A1 (en) |
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| CN1041935A (en) * | 1988-10-05 | 1990-05-09 | 琳德股份公司 | C 2The separation method of-materials flow and device |
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| CN101367697A (en) * | 2008-10-15 | 2009-02-18 | 上海惠生化工工程有限公司 | Separation method for light hydrocarbon products in MTO/MTP reaction products |
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| CN101844961A (en) * | 2010-07-05 | 2010-09-29 | 茂名实华东成化工有限公司 | Method and device for efficiently recovering propylene from ethane gas at the top of dethanizing tower |
| CN104193575A (en) * | 2014-09-11 | 2014-12-10 | 中建安装工程有限公司 | Device and method for extracting, distilling and separating propane and propylene |
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| US5681908A (en) * | 1995-03-03 | 1997-10-28 | Advanced Extraction Technologies, Inc. | Absorption process for rejection of reactor byproducts and recovery of monomers from waste gas streams in olefin polymerization processes |
| US5890378A (en) * | 1997-04-21 | 1999-04-06 | Elcor Corporation | Hydrocarbon gas processing |
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| US20110067443A1 (en) * | 2009-09-21 | 2011-03-24 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
| JP2016003215A (en) * | 2014-06-18 | 2016-01-12 | 住友化学株式会社 | Method for producing concentrated mixture of methylacetylene with propadiene |
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| CN104784953B (en) * | 2015-03-26 | 2016-09-21 | 神华集团有限责任公司 | A kind of product piece-rate system for preparing propylene from methanol and chilling system thereof |
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- 2017-07-26 CN CN201780005792.3A patent/CN108883343A/en active Pending
- 2017-07-26 WO PCT/CN2017/094415 patent/WO2019019034A1/en active Application Filing
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| CN1041935A (en) * | 1988-10-05 | 1990-05-09 | 琳德股份公司 | C 2The separation method of-materials flow and device |
| US5372009A (en) * | 1993-11-09 | 1994-12-13 | Mobil Oil Corporation | Cryogenic distillation |
| CN101445419A (en) * | 2007-11-27 | 2009-06-03 | 上海惠生化工工程有限公司 | Method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption |
| CN101367697A (en) * | 2008-10-15 | 2009-02-18 | 上海惠生化工工程有限公司 | Separation method for light hydrocarbon products in MTO/MTP reaction products |
| CN101844961A (en) * | 2010-07-05 | 2010-09-29 | 茂名实华东成化工有限公司 | Method and device for efficiently recovering propylene from ethane gas at the top of dethanizing tower |
| CN104193575A (en) * | 2014-09-11 | 2014-12-10 | 中建安装工程有限公司 | Device and method for extracting, distilling and separating propane and propylene |
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| Publication number | Publication date |
|---|---|
| WO2019019034A1 (en) | 2019-01-31 |
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Application publication date: 20181123 |