CN109809958A - The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique - Google Patents
The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique Download PDFInfo
- Publication number
- CN109809958A CN109809958A CN201910051602.2A CN201910051602A CN109809958A CN 109809958 A CN109809958 A CN 109809958A CN 201910051602 A CN201910051602 A CN 201910051602A CN 109809958 A CN109809958 A CN 109809958A
- Authority
- CN
- China
- Prior art keywords
- ethylene
- pdh
- propylene
- light hydrocarbon
- tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique, mainly solves the problems, such as that yield of light olefins is low in the prior art, separation process is tediously long, propylene yield is few, construction investment is high, takes up a large area.The present invention is by using a kind of method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique, the ethylene unit that nominal capacity is 80~1,200,000 tons/year is coupled with 600,000 tons/year of PDH device, propylene product volume increase 195.5~293.3%, equipment investment expense reduces by 3.31~4.88 hundred million yuans, the technical solution that 1.8 hectares of land seizure area savings preferably solves the above problem, can be used for during light hydrocarbon cracking sequence separating technology couples with PDH technique.
Description
Technical field
The present invention relates to a kind of methods that light hydrocarbon cracking sequence separating technology is coupled with PDH technique, are dehydrogenating propane PDH dresses
The method of the technology set coupling integrated with the light hydrocarbon cracking ethylene unit technology of sequence separating technology.In this method
PDH device only retains dehydrogenation reaction part and product gas preprocessing part, other separation equipments rely on the separation of ethylene unit
Equipment not only reduces equipment investment and occupied area, but also effective propylene enhancing, solves light hydrocarbon cracking ethylene unit product structure
Single problem can be applied to prepare in the industrial production of ethylene.
Background technique
Ethylene is the most important basic material of petrochemical industry, the hair of production level mark one national oil chemical engineering industry
Up to degree.The cracking stock of production ethylene can be naphtha, light paraffins, hydrogenated diesel oil etc., generally using ethane, propane etc.
Light paraffins are that the yield of cracking stock production ethylene is higher.Ethylene production technique includes cracking and separating two processes, separation
Process includes: ABB Lummus company using sequence separation process；Linde AG company then uses point of front-end deethanization front-end hydrogenation
From process；Stone&Webster company and KBR company use the separation process of predepropanization front-end hydrogenation.Wherein: sequence separation stream
Journey cracking gas initially enters domethanizing column, and tower top obtains methane and hydrogen, and tower reactor obtains C2 and C2 or more group and is distributed into deethanization
Tower, the C2 group dispensing ethylene rectifying column that deethanizer overhead obtains obtain ethylene product, the C3 and C3 that dethanizer tower reactor obtains
Above group is distributed into depropanizing tower, and the C3 group dispensing propylene rectification tower that depropanizing tower tower top obtains obtains propylene product, depropanization
Tower tower reactor C4 and C4 or more group is distributed into debutanizing tower and further separates.
Propylene is also one of the important alkene for producing petrochemicals.It, which is produced, is mainly derived from steam cracking device life
Produce the byproduct of ethylene and the byproduct of refinery catalytic cracking unit's production petrol and diesel oil, but both the above Conventional processing methods third
Alkene yield is low, energy consumption is high.Dehydrogenating propane PDH technology propene yield is high, low energy consumption, byproduct is few due to having many advantages, such as and
It attracts attention, in the industrial production, is increasingly used widely, associated patented invention is also more and more.Existing skill
103687666 A of Patent publication No CN in art discloses a kind of catalyst method for being re-activated dehydrogenating propane, is used to increased portion
Divide the dehydrogenating propane activity of the dehydrogenation of inactivation.107970950 A of Patent publication No CN relates to a kind of dehydrogenating propane system
Propylene catalyst regeneration method.Patent publication No CN 107602323A, 107673947 A of 107602324 CN A, CN are related to
And the coupling of dehydrogenating propane device separating technology and ethylene unit separating technology, it discloses and leverages fully on ethylene unit separation equipment
Carry out the technical method of material rectifying separation.
There are the separation of PDH device to flow by 103687666 A of Patent publication No CN and 107970950 A of CN in the prior art
The problem of journey is tediously long, separation equipment investment is high, process units takes up a large area.Patent publication No CN in the prior art
107602323A, CN 107602324 A, CN 107673947 A although relate to integrated coupling of the PDH technique with ethylene process
Manufacturing technique method is closed, but is not yet applied in the technique production procedure of light hydrocarbon cracking raw material and sequence separation ethylene unit,
Also there is not yet the report of PDH technique and light hydrocarbon cracking sequence separation ethylene process coupling.Therefore, prior art ethylene unit and
That there are yield of light olefins is low for the conventionally produced route of PDH device, separation process is tediously long, propylene yield is few, construction investment is high,
The problem of taking up a large area.
Summary of the invention
That the technical problem to be solved by the present invention is to yield of light olefins in the prior art is low, separation process is tediously long, propylene
Yield is few, construction investment is high, the problem of taking up a large area, and provides a kind of new light hydrocarbon cracking sequence separating technology and PDH technique
The method of coupling, with that yield of light olefins is high, separation process is short, propylene yield is more, construction investment is low, occupied area is small is excellent
Point.
To solve the above problems, The technical solution adopted by the invention is as follows: a kind of light hydrocarbon cracking sequence separating technology and PDH
The method of technique coupling, comprising: (1) PDH device: fresh propane charging and the recycled propane from de-oiling tower and propylene rectification tower
The charging for being incorporated as PDH device initially enters propane gasification tank, and the gas phase after gasification goes to heating furnace and catalytic reactor,
In catalytic reactor, dehydrogenating propane reaction occurs, generates propylene product, is sent to the compressor and alkali of ethylene unit after pretreatment
Unit, propane gasification tank tank bottom recombination dispensing to de-oiling tower are washed, and is sent to heating furnace as supplement liquid fuel；(2) ethylene fills
Set: lighter hydrocarbons enter pyrolysis furnace as cracking stock, and the Pintsch process gas being cracked to form condenses and separates after chilling, washing cooling
Drippolene and Pyrolysis fuel oil PFO are sent out out-of-bounds out, and cracking pneumatic transmission to compression, dry, alkali cleaning are further processed；(3) coupling
Attach together and set: ethylene cracking gas merges with PDH device product gas is sent to ethylene cracking gas suction port of compressor, compressed,
Domethanizing column is sent to after drying, alkali cleaning, deep cooling, domethanizing column tower base stream is successively through dethanizer, depropanizing tower, debutanizing tower
It is separated, wherein deethanizer overhead is chosen plus hydrogen makes acetylene be changed into ethylene and ethane and be removed, and obtains
C2 group dispensing ethylene rectifying column obtains ethylene product, and depropanizing tower overhead product is chosen plus hydrogen is changed into propine/allene
Propylene and propane and be removed, obtained C3 group dispensing propylene rectification tower obtains propylene product.
In above-mentioned technical proposal, it is preferable that ethylene unit nominal capacity 80~1,200,000 ton/year, light hydrocarbon cracking raw material by
40% ethane and 40% propane and 20% butane composition, product propylene/ethylene ratio are 0.22.
In above-mentioned technical proposal, it is preferable that 600,000 tons/year of PDH device nominal capacity, 51.90 ten thousand tons/year of propylene yield.
In above-mentioned technical proposal, it is preferable that the operating condition of Furnace of Ethylene Cracking Plant are as follows: reaction pressure 0.10~
0.25MPaA, 810~870 DEG C of reaction temperature.
In above-mentioned technical proposal, it is preferable that the operating condition of PDH device reaction device are as follows: reaction pressure 0.10~
0.35MPaA, 500~700 DEG C of reaction temperature.
In above-mentioned technical proposal, it is preferable that after coupling, product propylene/ethylene ratio is 0.65~0.87.
In above-mentioned technical proposal, it is preferable that it leverages fully on ethylene unit existing equipment and is separated, ethylene unit portion
Subset produce load is opposite to be improved, but the equipment that PDH device uses is reduced, and it is dry to eliminate product air compressor, product gas
Device, dethanizer feed drier, dethanizer, cold box system, propylene rectification tower, propylene rectification tower feed desulfurization bed, ethylene
Refrigeration compressor, propylene refrigeration compressor.
In above-mentioned technical proposal, it is preferable that the coupling device that ethylene cracking gas and PDH device product gas are combined into
Using sequence separation process.
The present invention relates to a kind of methods that light hydrocarbon cracking sequence separating technology is coupled with PDH technique, using lighter hydrocarbons as cracking
The ethylene unit of raw material yield of ethene with higher, dehydrogenating propane PDH technique using single propane feed it is available compared with
High propene yield.PDH technique, which is separated ethylene process coupling with sequence, can effectively improve the low-carbon alkene of ethylene, propylene etc.
Yield.For ethylene unit using lighter hydrocarbons as cracking stock, PDH device, as dehydrogenation feed, optimizes raw material using propane as a result,
Structure, and the yield of can make rational planning for ethylene product and propylene product.Meanwhile it leveraging fully on the existing separation of ethylene unit and setting
It is standby, simplify PDH device separation process, separation equipment investment is effectively reduced, reduces occupied area.The present invention cracks ethylene unit
Gas relies on ethylene unit separation equipment to carry out component rectifying and separates after mixing with PDH device reaction product gas, eliminate PDH device
Separation equipment, simplify separating technology process.It is 80~1,200,000 tons/year of ethylene unit and 600,000 tons/year by nominal capacity
PDH device coupling, propylene enhancing product 195.5~293.3%, reduce about 3.31~4.88 hundred million yuan of people of equipment investment expense
Coin, achieves preferable technical effect and economic benefit by about 1.8 hectares of Economization on land area occupied.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[comparative example 1]
Sequence separation ethylene unit nominal capacity is 800,000 tons/year, is formed with 40% ethane, 40% propane, 20% butane
Lighter hydrocarbons as cracking stock.80.00 ten thousand tons/year of ethylene product yield, 17.60 ten thousand tons/year of propylene product yield, product third
Alkene/ethylene ratio is 0.22, consumes 171.38 ten thousand tons/year of cracking stock lighter hydrocarbons.
[embodiment 1]
The method coupled using light hydrocarbon cracking sequence separating technology of the present invention with PDH technique, process flow are as follows: (1) PDH
Device reaction unit: the reaction member mainly includes the equipment such as propane gasification tank, heating furnace and reactor, de-oiling tower.Fresh third
Alkane and propane is recycled back into as raw material gasifies in propane gasification tank first, enter after heating furnace is preheating to reaction temperature
Dehydrogenation reactor.In dehydrogenation reactor, propane generates the product gas of the components such as propylene by dehydrogenation reaction.Propane gasification tank tank
The recombination at bottom is distributed to de-oiling tower, and tower top isolates propane as recycle stock and returns to propane gasification tank, and tower bottom group, which is distributed to, to be added
Hot stove is as supplement liquid fuel.(2) ethylene unit cracks unit: cracking reaction occurs in pyrolysis furnace for light hydrocarbon cracking raw material,
The different cracking gas of ethylene, propylene equimolecular quantity is generated, cracking gas enters chilling system and carries out fast cooling, isolates cracking vapour
Oil and Pyrolysis fuel oil PFO, cracking pneumatic transmission to compression unit are further processed.(3) coupling device separative unit: separation is single
Member is sequence separating technology process.Ethylene cracking gas mixed with the product gas of PDH device after after compressor boost, dry
Into cryogenic system, mixed material is successively separated through domethanizing column, dethanizer, depropanizing tower, debutanizing tower.It is mixed
It closes gas and isolates methane hydrogen through ice chest and domethanizing column, deethanizer overhead isolates C2 component, ethylene rectifying column is sent to be divided
From.Ethylene distillation column overhead obtains polymer grade ethylene product, and tower bottom obtains ethane and returns to pyrolysis furnace.Depropanizing tower tower top is isolated
C3 component, send propylene rectification tower to be separated.Propylene rectification tower tower top obtains polymerization-grade propylene product, and tower reactor obtains propane conduct
Recycle stock returns to PDH device propane gasification tank.Debutanizing tower tower top isolates C4 component, and tower reactor isolates drippolene.
The PDH device that sequence separates 800,000 tons/year of ethylene units with nominal capacity is 600,000 tons/year is coupled, second is kept
Alkene yield is 80.00 ten thousand tons/year constant, and propylene total output is 69.22 ten thousand tons/year, and product propylene/ethylene ratio is 0.87.With than
It is compared compared with example 1, integral coupling device propylene enhancing product 293.3%, consumes 168.62 ten thousand tons/year of light hydrocarbon cracking raw material, separately
Outside, 62.93 ten thousand tons/year of fresh propane raw material are consumed, saves 3.31 hundred million yuans of engineering construction investment, reduces occupied area
1.8 hectare.
1 ethylene unit machine utilization of table is promoted
[comparative example 2]
Sequence separation ethylene unit nominal capacity is 1,000,000 tons/year, is formed with 40% ethane, 40% propane, 20% butane
Lighter hydrocarbons as cracking stock.100.00 ten thousand tons/year of ethylene product yield, 22.00 ten thousand tons/year of propylene product yield, product third
Alkene/ethylene ratio is 0.22, consumes 214.22 ten thousand tons/year of cracking stock lighter hydrocarbons.
[embodiment 2]
The PDH device that sequence separates 1,000,000 tons/year of ethylene units with nominal capacity is 600,000 tons/year is coupled, second is kept
Alkene yield is 100.00 ten thousand tons/year constant, and propylene total output is 73.62 ten thousand tons/year, and product propylene/ethylene ratio is 0.74.With than
It is compared compared with example 2, integral coupling device propylene enhancing product 234.6%, consumes 211.46 ten thousand tons/year of light hydrocarbon cracking raw material, separately
Outside, 62.93 ten thousand tons/year of fresh propane raw material are consumed, saves 3.97 hundred million yuans of engineering construction investment, reduces occupied area
1.8 hectare.
2 ethylene unit machine utilization of table is promoted
[comparative example 3]
Sequence separation ethylene unit nominal capacity is 1,100,000 tons/year, is formed with 40% ethane, 40% propane, 20% butane
Lighter hydrocarbons as cracking stock.110.00 ten thousand tons/year of ethylene product yield, 24.20 ten thousand tons/year of propylene product yield, product third
Alkene/ethylene ratio is 0.22, consumes 235.65 ten thousand tons/year of cracking stock lighter hydrocarbons.
[embodiment 3]
The PDH device that sequence separates 1,100,000 tons/year of ethylene units with nominal capacity is 600,000 tons/year is coupled, second is kept
Alkene yield is 110.00 ten thousand tons/year constant, and propylene total output is 75.82 ten thousand tons/year, and product propylene/ethylene ratio is 0.69.With than
It is compared compared with example 3, integral coupling device propylene enhancing product 210.7%, consumes 232.88 ten thousand tons/year of light hydrocarbon cracking raw material, separately
Outside, 62.93 ten thousand tons/year of fresh propane raw material are consumed, saves 4.26 hundred million yuans of engineering construction investment, reduces occupied area
1.8 hectare.
3 ethylene unit machine utilization of table is promoted
[comparative example 4]
Sequence separation ethylene unit nominal capacity is 1,200,000 tons/year, is formed with 40% ethane, 40% propane, 20% butane
Lighter hydrocarbons as cracking stock.120.00 ten thousand tons/year of ethylene product yield, 26.40 ten thousand tons/year of propylene product yield, product third
Alkene/ethylene ratio is 0.22, consumes 257.07 ten thousand tons/year of cracking stock lighter hydrocarbons.
[embodiment 4]
The PDH device that sequence separates 1,200,000 tons/year of ethylene units with nominal capacity is 600,000 tons/year is coupled, second is kept
Alkene yield is 120.00 ten thousand tons/year constant, and propylene total output is 78.02 ten thousand tons/year, and product propylene/ethylene ratio is 0.65.With than
It is compared compared with example 4, integral coupling device propylene enhancing product 195.5%, consumes 254.31 ten thousand tons/year of light hydrocarbon cracking raw material, separately
Outside, 62.93 ten thousand tons/year of fresh propane raw material are consumed, saves 4.88 hundred million yuans of engineering construction investment, reduces occupied area
1.8 hectare.
4 ethylene unit machine utilization of table is promoted
| Serial number | Ethylene unit | Load lifting |
| 1 | Pyrolysis furnace | It is constant |
| 2 | Chilling tower | It is constant |
| 3 | Charge gas compressor | 49.14% |
| 4 | Caustic wash tower | 49.14% |
| 5 | Crack gas dryer | 49.14% |
| 6 | Depropanizing tower | 186.78% |
| 7 | C2 hydrogenator | 3.41% |
| 8 | Cold box system | 49.14% |
| 9 | Expanding machine | 49.14% |
| 10 | Domethanizing column | 49.14% |
| 11 | Dethanizer | 57.18% |
| 12 | Ethylene rectifying column | 3.41% |
| 13 | C3 hydrogenator | 364.34% |
| 14 | Propylene rectification tower | 364.34% |
| 15 | Debutanizing tower | 8.46% |
The method coupled using light hydrocarbon cracking sequence separating technology of the present invention with PDH technique, [embodiment 1]~[embodiment
4] summarize with [comparative example 1]~[comparative example 4], be shown in Table 5.
5 embodiment of table and comparative example summary sheet
Claims (8)
1. a kind of method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique, comprising: (1) PDH device: fresh propane into
The charging that material is incorporated as PDH device with the recycled propane from de-oiling tower and propylene rectification tower initially enters propane gasification tank,
Gas phase after gasification goes to heating furnace and catalytic reactor, and in catalytic reactor, dehydrogenating propane reaction occurs, generates propylene and produces
Object is sent to the compressor and caustic wash unit of ethylene unit after pretreatment, and the recombination of propane gasification tank tank bottom is sent to de-oiling tower, and
Heating furnace is sent to as supplement liquid fuel；(2) ethylene unit: lighter hydrocarbons enter pyrolysis furnace as cracking stock, are cracked to form
Pintsch process gas is sent out out-of-bounds after chilling, washing cooling condensation and separation of drippolene and Pyrolysis fuel oil PFO, and cracking pneumatic transmission is extremely
Compression, dry, alkali cleaning are further processed；(3) coupling device: ethylene cracking gas merges with PDH device product gas
It is sent to ethylene cracking gas suction port of compressor, domethanizing column, domethanizing column tower bottom are sent to after compression, drying, alkali cleaning, deep cooling
Logistics is successively separated through dethanizer, depropanizing tower, debutanizing tower, and wherein deethanizer overhead is chosen plus hydrogen makes
Acetylene is changed into ethylene and ethane and is removed, and obtained C2 group dispensing ethylene rectifying column obtains ethylene product, depropanizing tower tower
Top product is chosen plus hydrogen makes propine/allene be changed into propylene and propane and be removed, obtained C3 group dispensing propylene rectifying
Tower obtains propylene product.
2. the method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique according to claim 1, it is characterised in that ethylene
Device nominal capacity 80~1,200,000 ton/year, light hydrocarbon cracking raw material are made of 40% ethane and 40% propane and 20% butane,
Product propylene/ethylene ratio is 0.22.
3. the method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique according to claim 1, it is characterised in that PDH
600,000 tons/year of device nominal capacity, 51.90 ten thousand tons/year of propylene yield.
4. the method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique according to claim 1, it is characterised in that ethylene
The operating condition of device pyrolysis furnace are as follows: 0.10~0.25MPaA of reaction pressure, 810~870 DEG C of reaction temperature.
5. the method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique according to claim 1, it is characterised in that PDH
The operating condition of device reaction device are as follows: 0.10~0.35MPaA of reaction pressure, 500~700 DEG C of reaction temperature.
6. the method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique according to claim 1, it is characterised in that coupling
Afterwards, product propylene/ethylene ratio is 0.65~0.87.
7. the method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique according to claim 1, it is characterised in that sufficiently
Ethylene unit existing equipment is relied on to be separated, ethylene unit equipment component produce load is opposite to be improved, but PDH device makes
Equipment is reduced, and eliminates product air compressor, product gas dryer, dethanizer feed drier, dethanizer, ice chest
System, propylene rectification tower, propylene rectification tower feed desulfurization bed, ethylene refrigeration compressor, propylene refrigeration compressor.
8. the method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique according to claim 1, it is characterised in that ethylene
The coupling device that device cracking gas and PDH device product gas are combined into is using sequence separation process.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910051602.2A CN109809958A (en) | 2019-01-21 | 2019-01-21 | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910051602.2A CN109809958A (en) | 2019-01-21 | 2019-01-21 | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109809958A true CN109809958A (en) | 2019-05-28 |
Family
ID=66604672
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910051602.2A Pending CN109809958A (en) | 2019-01-21 | 2019-01-21 | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109809958A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111201210A (en) * | 2017-10-10 | 2020-05-26 | 陶氏环球技术有限责任公司 | Method for increasing hydrocarbon production efficiency |
| CN111747813A (en) * | 2020-07-08 | 2020-10-09 | 中国石油化工股份有限公司 | Method for coupling hydrocarbon steam cracking sequential separation process and propane dehydrogenation process |
| CN111807921A (en) * | 2020-07-08 | 2020-10-23 | 中国石油化工股份有限公司 | Coupling method of deethanization process before hydrocarbon steam cracking and propane dehydrogenation process |
| CN111848327A (en) * | 2020-07-08 | 2020-10-30 | 中国石油化工股份有限公司 | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111875466A (en) * | 2020-07-08 | 2020-11-03 | 中国石油化工股份有限公司 | Coupling method of depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111875467A (en) * | 2020-07-08 | 2020-11-03 | 中国石油化工股份有限公司 | Coupling method of hydrocarbon steam cracking sequential separation process and propane dehydrogenation process |
| CN111892475A (en) * | 2020-06-30 | 2020-11-06 | 中石化宁波工程有限公司 | Method for increasing propylene and ethylene yield of propane dehydrogenation device |
| CN111943800A (en) * | 2020-06-30 | 2020-11-17 | 中石化宁波工程有限公司 | Method for producing propylene and ethylene by thermal cracking of light hydrocarbon |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107602323A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique |
| CN107602324A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique |
| CN107673947A (en) * | 2017-10-11 | 2018-02-09 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with naphtha pyrolysis front-end deethanization technique |
-
2019
- 2019-01-21 CN CN201910051602.2A patent/CN109809958A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107602323A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique |
| CN107602324A (en) * | 2017-10-11 | 2018-01-19 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique |
| CN107673947A (en) * | 2017-10-11 | 2018-02-09 | 中石化上海工程有限公司 | The method that dehydrogenating propane technique couples with naphtha pyrolysis front-end deethanization technique |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111201210B (en) * | 2017-10-10 | 2023-06-27 | 陶氏环球技术有限责任公司 | Method for improving hydrocarbon production efficiency |
| CN111201210A (en) * | 2017-10-10 | 2020-05-26 | 陶氏环球技术有限责任公司 | Method for increasing hydrocarbon production efficiency |
| CN111892475A (en) * | 2020-06-30 | 2020-11-06 | 中石化宁波工程有限公司 | Method for increasing propylene and ethylene yield of propane dehydrogenation device |
| CN111892475B (en) * | 2020-06-30 | 2023-04-07 | 中石化宁波工程有限公司 | Method for increasing propylene and ethylene yield of propane dehydrogenation device |
| CN111943800B (en) * | 2020-06-30 | 2023-04-07 | 中石化宁波工程有限公司 | Method for producing propylene and ethylene by thermal cracking of light hydrocarbon |
| CN111943800A (en) * | 2020-06-30 | 2020-11-17 | 中石化宁波工程有限公司 | Method for producing propylene and ethylene by thermal cracking of light hydrocarbon |
| CN111848327A (en) * | 2020-07-08 | 2020-10-30 | 中国石油化工股份有限公司 | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111875467A (en) * | 2020-07-08 | 2020-11-03 | 中国石油化工股份有限公司 | Coupling method of hydrocarbon steam cracking sequential separation process and propane dehydrogenation process |
| CN111807921B (en) * | 2020-07-08 | 2022-10-14 | 中国石油化工股份有限公司 | Coupling method of deethanization process before hydrocarbon steam cracking and propane dehydrogenation process |
| CN111747813B (en) * | 2020-07-08 | 2022-10-14 | 中国石油化工股份有限公司 | Method for coupling hydrocarbon steam cracking sequential separation process and propane dehydrogenation process |
| CN111875466B (en) * | 2020-07-08 | 2022-10-14 | 中国石油化工股份有限公司 | Coupling method of depropanization process before hydrocarbon steam cracking and propane dehydrogenation process |
| CN111875466A (en) * | 2020-07-08 | 2020-11-03 | 中国石油化工股份有限公司 | Coupling method of depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
| CN111807921A (en) * | 2020-07-08 | 2020-10-23 | 中国石油化工股份有限公司 | Coupling method of deethanization process before hydrocarbon steam cracking and propane dehydrogenation process |
| CN111747813A (en) * | 2020-07-08 | 2020-10-09 | 中国石油化工股份有限公司 | Method for coupling hydrocarbon steam cracking sequential separation process and propane dehydrogenation process |
| CN111848327B (en) * | 2020-07-08 | 2023-07-11 | 中国石油化工股份有限公司 | Method for coupling depropanization process and propane dehydrogenation process before hydrocarbon steam cracking |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109809958A (en) | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique | |
| CN100551885C (en) | From the product gas of preparation alkene, reclaim the method for low-carbon alkene | |
| CN107673947A (en) | The method that dehydrogenating propane technique couples with naphtha pyrolysis front-end deethanization technique | |
| CN107602323A (en) | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique | |
| CN102795956B (en) | Method for separating reaction products produced during preparation of propylene by dehydrogenating propane | |
| CN100398498C (en) | Separating method for converting methanol to prepare low carbon olefin gas | |
| CN104230617B (en) | The method that MTO technique couples with Petroleum and Deposition During Propane Pyrolysis order separating technology | |
| CN107602324A (en) | The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique | |
| CN108976099A (en) | A kind of deep cooling separating method of low carbon olefin gas | |
| CN103087772A (en) | Device and method for separating refinery dry gas through oil absorption | |
| CN108017499B (en) | Comprehensive utilization system and comprehensive utilization method for methanol-to-olefin reaction product | |
| CN109761734A (en) | The method that naphtha and ethane cracking front-end deethanization are coupled with PDH | |
| CN104557387A (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN109809957A (en) | The method that light hydrocarbon cracking front-end deethanization technique is coupled with PDH technique | |
| CN104557384A (en) | Refinery mixed dry gas recovery system and recovery method | |
| CN109761736A (en) | Naphtha and ethane cracking sequentially separate the method coupled with PDH | |
| CN101921161B (en) | Methanol To Olefins (MTO) gas separation process flow | |
| CN106316761A (en) | Method for separation of products of reaction for preparation of propylene from propane by dehydrogenation | |
| CN109761735A (en) | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH | |
| CN107056568A (en) | The method that MTO techniques are coupled with naphtha and Deposition During Propane Pyrolysis predepropanization technique | |
| CN109761733A (en) | The method that naphtha and ethane cracking predepropanization are coupled with PDH | |
| CN101092570B (en) | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon | |
| CN109851461A (en) | The method that naphtha and Deposition During Propane Pyrolysis front-end deethanization are coupled with PDH | |
| CN101092325A (en) | Method for preparing propylene by catalytic cracking olefin of containing carbon | |
| CN110407658B (en) | Low-energy-consumption cryogenic separation process method for ethane pyrolysis gas |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190528 |
|
| RJ01 | Rejection of invention patent application after publication |