CN109761733A - The method that naphtha and ethane cracking predepropanization are coupled with PDH - Google Patents
The method that naphtha and ethane cracking predepropanization are coupled with PDH Download PDFInfo
- Publication number
- CN109761733A CN109761733A CN201910051573.XA CN201910051573A CN109761733A CN 109761733 A CN109761733 A CN 109761733A CN 201910051573 A CN201910051573 A CN 201910051573A CN 109761733 A CN109761733 A CN 109761733A
- Authority
- CN
- China
- Prior art keywords
- ethylene
- unit
- pdh
- tower
- naphtha
- 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
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 naphtha and ethane cracking predepropanization are coupled with PDH, mainly solve the problems, such as that separation process is tediously long in the prior art, take up a large area, fixed investment height, unreasonable products structure, operating cost it is high.A kind of method that the present invention is coupled by using naphtha and ethane cracking predepropanization with PDH, under the premise of keeping ethylene aggregated capacity constant, for 80~1,500,000 tons/year of ethylene units, product and raw material price difference can save 3~700,000,000 yuans/year, construction investment 5~1,000,000,000 yuan can be saved simultaneously, it reduces by 1.8 hectares of occupied area of technical solution and preferably solves the above problem, can be used for naphtha and during ethane cracking predepropanization couples with PDH technique.
Description
Technical field
The present invention relates to a kind of methods that naphtha and ethane cracking predepropanization are coupled with PDH, are a kind of dehydrogenating propanes
The ethylene unit coupling technique that PDH device is separated with naphtha and ethane cracking predepropanization；Rely on ethylene unit predepropanization
The existing separation equipment of process flow, and keep ethylene aggregated capacity constant, realize that PDH device is separated with ethylene unit predepropanization
The coupling of process, reduces equipment investment, reduces construction land.The present invention replaces most of naphtha, optimization using ethane
Raw material mix, reduces operating cost, improves the adaptability to changes of ethylene process process units reply turn of the market.
Background technique
Ethylene unit includes 2 part of cracking reaction and separation and purification.Existing ethylene mainly by crack petroleum product come
It obtains, therefore the development of ethylene technology and the development of cracking technology technology are undivided.And separation process is divided into cracking
Gas cryogenic separation and cracking 2 kinds of technologies of gas and oil absorption and separation, the former at low temperature will be under hydro carbons deep cooling condensation in cracking gas
Come, then under suitable temperature and pressure, is separated each component by rectifying.According to separation sequence difference, deep cooling point
From mainly have sequence separation, 3 kinds of front-end deethanization, predepropanization separation process.The present invention uses predepropanization isolation technics, reaction
Cracking gas after compression drying, first be fractionated in depropanizing tower, tower top be C3 and C3 or less light component, tower reactor be C4 and C4 with
Upper heavy constituent.Depropanization tower top material successively carries out rectifying separation through demethanation, deethanization, ethylene distillation, propylene rectifying etc. again,
Depropanization kettle material is routed directly to debutanizing tower.
Currently, most of China's ethylene unit uses naphtha as cracking stock, but moving with international raw oil market
Variation, the raising of energy conservation and environmental requirement are swung, the lighting of ethylene unit cracking stock, diversification, high quality become inevitable hair
Exhibition trend.Therefore naphtha and ethane cracking raw material are flexibly used, replaces most of naphtha to carry out cracking production second in ethane
Alkene can be improved ethylene yield, can effectively improve the ability for resisting the market risks such as cost of material.But there are propylene yield
The deficiency and problem of decline.
In order to improve propylene yield, Patent publication No CN105152840A in the prior art is disclosed using C4 as raw material point
Method of the propane separated out as the raw material production propylene product of dehydrogenating propane PDH device.In addition, by dehydrogenating propane technique and second
Alkene technique is coupled, and also can solve the problem of propylene underproduces and declines；Patent publication No CN107602323A is related to
Dehydrogenating propane technique and the coupling of light hydrocarbon cracking predepropanization technique, CN107602324A is related to dehydrogenating propane technique and naphtha is split
The coupling of predepropanization technique is solved, CN107673947A is related to dehydrogenating propane technique and the coupling of naphtha pyrolysis front-end deethanization technique.
In recent years, the report that PDH device is coupled with ethylene unit technique is more and more, in the prior art,
Although CN105152840A and CN107602323A and CN107602324A and CN107673947A optimizes cracking stock, but
It is the report there is not yet PDH technique and naphtha and the coupling of ethane cracking predepropanization technique.Therefore, there is separation in the prior art
Long flow path, operating cost are high, fixed investment is big, the problem more than occupied area.
Summary of the invention
That the technical problem to be solved by the present invention is to separation process in the prior art is tediously long, take up a large area, fixed investment
The high problem of height, unreasonable products structure, operating cost provides a kind of new naphtha and ethane cracking predepropanization and PDH
The method of coupling, it is excellent to have that separation process is short, occupied area is small, fixed investment is low, product structure is reasonable, operating cost is low
Point.
To solve the above problems, The technical solution adopted by the invention is as follows: a kind of naphtha and ethane cracking predepropanization
The method coupled with PDH, comprising: (1) ethylene unit reaction system: naphtha and ethane cracking raw material enter cracking reaction unit
It is cracked into hydro carbons mixed air, is sent to quenching unit, drippolene and cracking fuel are isolated after chilling, washing, in cracking gas
Oil is sent out out-of-bounds as final byproduct, and the cracking gas of remaining component is sent to compression and drying unit compression, alkali cleaning, drying, depth
After cold, it is sent to downstream predepropanization separation system；(2) PDH device reaction system: fresh propane feeds and comes from propylene rectification tower
Enter propane flammable gas tank after the charging of tower bottom recycled propane and the mixing of de-oiling tower top material to gasify, the gas phase after gasification is through pre-
Enter heating furnace after heat and dehydrogenation reactor system carries out dehydrogenation reaction, the product gas of generation enters separation system progress after cooling
Separation；(3) coupling device separation system: ethylene cracking gas and PDH device product gas be sent into after mixing coupling device compression,
Dry, deep cooling and separation system, compression, dry, after deep cooling mixed air enter high pressure depropanization unit, and tower top isolates part
C3 and C3 more light component, is sent to demethanation unit；Tower reactor isolates part C3 and C3 more heavy constituent, is sent to low pressure depropanization list
Member；Low pressure depropanization unit tower top isolates C3, is sent to propylene rectification cell；Tower reactor isolates C4 and C4 more heavy constituent, is sent to
Debutanizing tower；Demethanation unit tower top is isolated methane hydrogen and is sent out out-of-bounds as by-product, and tower reactor is isolated to exist comprising all C2
Interior heavy constituent is sent to deethanization unit；Deethanization unit separates demethanation kettle material；Deethanizer overhead is C2
Component is sent to ethylene distillation unit；Tower reactor is C3 component, is sent to propylene rectification cell；Ethylene distillation unit is by dethanizer tower
Material rectifying separation is pushed up, tower top obtains ethylene, and tower bottom obtains ethane；Ethylene is sent out out-of-bounds as product, and ethane recycle return is split
Solve unit.Propylene distillation system separates low pressure depropanizer top material and deethanization unit kettle material rectifying, and tower top obtains
Propylene, tower bottom obtain propane, and propylene is sent out out-of-bounds as product, and propane cycles return to PDH reaction member；The input of debutanization system
From low pressure depropanizer substrate material and PDH device de-oiling tower materials at bottom of tower, material is separated by rectifying, and tower top obtains mixing C4
Component, tower bottom obtain drippolene, mix C4 component and send out out-of-bounds as final byproduct, drippolene with come from ethylene unit
The drippolene merging of quenching unit is also sent out out-of-bounds.
In above-mentioned technical proposal, it is preferable that ethylene unit nominal capacity is 80~1,500,000 tons/year.
In above-mentioned technical proposal, it is preferable that PDH device nominal capacity is 600,000 tons/year.
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 technique process units ethylene nominal capacity and original ethylene unit after coupling
It compares, ethylene nominal capacity is constant, and compression and separation system load are about the 101~247% of original ethylene unit.
In above-mentioned technical proposal, it is preferable that Ethylene Unit Feedstocks weight group becomes 30% naphtha, 70% ethane.
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.
The present invention is on the basis of ethylene unit existing predepropanization separation equipment, the constant premise of holding ethylene aggregated capacity
Under, using naphtha and ethane as cracking stock, using propane as dehydrogenation feed, realize PDH device and ethylene unit
Integration coupling.For 80~1,500,000 tons/year of ethylene units, wherein product and raw material price difference can save 3~700,000,000 yuans/
Year, while construction investment 5~1,000,000,000 yuan can be saved, 1.8 hectares of occupied area are reduced, preferable technical effect is achieved
And economic benefit.
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]
Ethylene unit in the prior art use predepropanization separation process, 800,000 tons/year of nominal capacity, steam thermal cracking
Raw material is naphtha, cracks selectivity P/E=0.47.80.00 ten thousand tons/year of ethylene yield, 37.60 ten thousand tons/year of propylene yield, disappear
254.96 ten thousand tons/year of naphtha of consumption.600,000 tons/year of PDH device nominal capacity, 51.90 ten thousand tons/year of propylene yield, propane consumption
62.93 ten thousand tons/year.
[embodiment 1]
The method coupled using a kind of naphtha of the present invention and ethane cracking predepropanization with PDH, process flow are as follows:
(1) ethylene unit reaction system: naphtha and ethane cracking raw material enter cracking reaction unit and are cracked into hydro carbons mixed air, are sent to
Quenching unit isolates drippolene and Pyrolysis fuel oil PFO as final byproduct after chilling, washing, in cracking gas and sends out boundary
Outside, after the cracking gas of remaining component is sent to compression and drying unit compression, alkali cleaning, drying, deep cooling, it is sent to downstream predepropanization point
From system.(2) PDH device reaction system: fresh propane feeds and feeds and take off from propylene rectification tower tower bottom recycled propane
Enter propane flammable gas tank after oily tower top material mixing to gasify, enters heating furnace after the gas phase after gasification is preheated and dehydrogenation is anti-
System is answered to carry out dehydrogenation reaction, the product gas of generation enters separation system after cooling and separated.(3) coupling device segregative line
System: it is sent into coupling device compression, dry, deep cooling and separation system after ethylene cracking gas and PDH device product gas mixing, is taken off
Oxide unit includes high pressure depropanization and low pressure depropanization unit, and compression, dry, after deep cooling mixed air enter high pressure depropanization
Unit, tower top isolate part C3 and C3 more light component, are sent to demethanation unit；Tower reactor is isolated part C3 and C3 and is more recombinated
Point, it is sent to low pressure depropanization unit.Low pressure depropanization unit tower top isolates C3, is sent to propylene rectification cell；Tower reactor is isolated
C4 and C4 more heavy constituent, is sent to debutanizing tower.Demethanation unit tower top is isolated methane hydrogen and is sent out out-of-bounds as by-product；Tower reactor
It isolates comprising the heavy constituent including all C2, is sent to deethanization unit.Deethanization unit divides demethanation kettle material
From；Deethanizer overhead is C2 component, is sent to ethylene distillation unit；Tower reactor is C3 component, is sent to propylene rectification cell.Ethylene essence
It evaporates unit to separate deethanizer overhead material rectifying, tower top obtains ethylene, and tower bottom obtains ethane；Ethylene sends out boundary as product
Outside, ethane recycle returns to cracking unit.Propylene distillation system is by low pressure depropanizer top material and deethanization unit kettle material
Rectifying separation, tower top obtain propylene, and tower bottom obtains propane, and propylene is sent out out-of-bounds as product, and it is single that propane cycles return to PDH reaction
Member.The input of debutanization system comes from low pressure depropanizer substrate material and PDH device de-oiling tower materials at bottom of tower, and material is by rectifying point
From tower top obtains mixing C4 component, tower bottom obtains drippolene, mixes C4 component as final byproduct and sends out out-of-bounds cracking
Gasoline merges with the drippolene from ethylene unit quenching unit also to be sent out out-of-bounds.
Ethylene unit in the present invention still uses predepropanization separation process, naphtha and ethane as cracking stock, second
800,000 tons/year of alkene nominal capacity；600,000 tons/year of PDH device nominal capacity.Using technical solution of the present invention, polymer grade ethylene
>=99.95wt%, 80.00 ten thousand tons/year of ethylene yield；Polymerization-grade propylene >=99.6wt%, 61.77 ten thousand tons/year of propylene yield.With
Comparative example 1 is compared, and saves 201.92 ten thousand tons/year of naphtha, more 123.76 ten thousand tons/year of ethane of consumption, product and raw material price difference can
Save about 3.83 hundred million yuans/year；About 5.32 hundred million yuans of equipment investment can be saved simultaneously, and it is public to reduce occupied area 1.8
Hectare.
Former ethylene plant increasing productivity table after 1 integration of table
[comparative example 2]
Ethylene unit in the prior art use predepropanization separation process, 1,000,000 tons/year of nominal capacity, steam hot tearing
Solution raw material is naphtha, cracks selectivity P/E=0.47.100.00 ten thousand tons/year of ethylene yield, 47.00 ten thousand tons of propylene yield/
Year, consume 318.70 ten thousand tons/year of naphtha.600,000 tons/year of PDH device nominal capacity, 51.90 ten thousand tons/year of propylene yield, propane
Consume 62.93 ten thousand tons/year.
[embodiment 2]
Ethylene unit in the present invention still uses predepropanization separation process, naphtha and ethane as cracking stock, second
1,000,000 tons/year of alkene nominal capacity；600,000 tons/year of PDH device nominal capacity.Using technical solution of the present invention, polymer grade ethylene
>=99.95wt%, 100.00 ten thousand tons/year of ethylene yield；Polymerization-grade propylene >=99.6wt%, 64.23 ten thousand tons/year of propylene yield.
Compared with comparative example 2,252.40 ten thousand tons/year of naphtha, mostly 154.70 ten thousand tons/year of ethane of consumption, product and raw material price difference are saved
About 4.75 hundred million yuans/year can be saved；About 6.71 hundred million yuans of equipment investment can be saved simultaneously, reduce occupied area 1.8
Hectare.
Former ethylene plant increasing productivity table after 2 integration of table
| Serial number | List of devices | Load lifting |
| 1 | Pyrolysis furnace | It is constant |
| 2 | Chilling tower | It is constant |
| 3 | Charge gas compressor | 53.89% |
| 4 | Caustic wash tower | 53.89% |
| 5 | Crack gas dryer | 53.89% |
| 6 | High pressure depropanizer | 53.89% |
| 7 | Low pressure depropanizer | 76.82% |
| 8 | C2 hydrogenator | 53.89% |
| 9 | Cold box system | 17.47% |
| 10 | Expanding machine | 17.47% |
| 11 | Pre- domethanizing column | 22.25% |
| 12 | Domethanizing column | 18.18% |
| 13 | Dethanizer | 45.07% |
| 14 | Ethylene rectifying column | 1.80% |
| 15 | C3 hydrogenator | 104.71% |
| 16 | Propylene rectification tower | 104.71% |
| 17 | Debutanizing tower | 103.82% |
| Invest (hundred million yuan) in ethylene separation part | 22.56 | |
| It reduces investment outlay after integration (hundred million yuan) | 6.71 |
[comparative example 3]
Ethylene unit in the prior art use predepropanization separation process, 1,200,000 tons/year of nominal capacity, steam hot tearing
Solution raw material is naphtha, cracks selectivity P/E=0.47.120.00 ten thousand tons/year of ethylene yield, 56.40 ten thousand tons of propylene yield/
Year, consume 382.45 ten thousand tons/year of naphtha.600,000 tons/year of PDH device nominal capacity, 51.90 ten thousand tons/year of propylene yield, propane
Consume 62.93 ten thousand tons/year.
[embodiment 3]
Ethylene unit in the present invention still uses predepropanization separation process, naphtha and ethane as cracking stock, second
1,200,000 tons/year of alkene nominal capacity；600,000 tons/year of PDH device nominal capacity.Using technical solution of the present invention, polymer grade ethylene
>=99.95wt%, 120.00 ten thousand tons/year of ethylene yield；Polymerization-grade propylene >=99.6wt%, 66.70 ten thousand tons/year of propylene yield.
Compared with comparative example 3,302.88 ten thousand tons/year of naphtha, mostly 185.64 ten thousand tons/year of ethane of consumption, product and raw material price difference are saved
About 5.68 hundred million yuans/year can be saved；About 8.40 hundred million yuans of equipment investment can be saved simultaneously, reduce occupied area 1.8
Hectare.
Former ethylene plant increasing productivity table after 3 integration of table
| Serial number | List of devices | Load lifting |
| 1 | Pyrolysis furnace | It is constant |
| 2 | Chilling tower | It is constant |
| 3 | Charge gas compressor | 44.30% |
| 4 | Caustic wash tower | 44.30% |
| 5 | Crack gas dryer | 44.30% |
| 6 | High pressure depropanizer | 44.30% |
| 7 | Low pressure depropanizer | 76.82% |
| 8 | C2 hydrogenator | 44.30% |
| 9 | Cold box system | 15.25% |
| 10 | Expanding machine | 15.25% |
| 11 | Pre- domethanizing column | 17.01% |
| 12 | Domethanizing column | 15.97% |
| 13 | Dethanizer | 34.59% |
| 14 | Ethylene rectifying column | 1.58% |
| 15 | C3 hydrogenator | 76.69% |
| 16 | Propylene rectification tower | 76.69% |
| 17 | Debutanizing tower | 103.82% |
| Invest (hundred million yuan) in ethylene separation part | 25.20 | |
| It reduces investment outlay after integration (hundred million yuan) | 8.40 |
[comparative example 4]
Ethylene unit in the prior art use predepropanization separation process, 1,500,000 tons/year of nominal capacity, steam hot tearing
Solution raw material is naphtha, cracks selectivity P/E=0.47.150.00 ten thousand tons/year of ethylene yield, 70.50 ten thousand tons of propylene yield/
Year, consume 478.06 ten thousand tons/year of naphtha.600,000 tons/year of PDH device nominal capacity, 51.90 ten thousand tons/year of propylene yield, propane
Consume 62.93 ten thousand tons/year.
[embodiment 4]
Ethylene unit in the present invention still uses predepropanization separation process, naphtha and ethane as cracking stock, second
1,500,000 tons/year of alkene nominal capacity；600,000 tons/year of PDH device nominal capacity.Using technical solution of the present invention, polymer grade ethylene
>=99.95wt%, 150.00 ten thousand tons/year of ethylene yield；Polymerization-grade propylene >=99.6wt%, 70.40 tons/year of propylene yield.With
Comparative example 4 is compared, and saves 378.60 ten thousand tons/year of naphtha, more 232.04 ten thousand tons/year of ethane of consumption, product and raw material price difference can
Save about 6.98 hundred million yuans/year；About 9.95 hundred million yuans of equipment investment can be saved simultaneously, and it is public to reduce occupied area 1.8
Hectare.
Former ethylene plant increasing productivity table after 4 integration of table
| Serial number | List of devices | Load lifting |
| 1 | Pyrolysis furnace | It is constant |
| 2 | Chilling tower | It is constant |
| 3 | Charge gas compressor | 34.98% |
| 4 | Caustic wash tower | 34.98% |
| 5 | Crack gas dryer | 34.98% |
| 6 | High pressure depropanizer | 34.98% |
| 7 | Low pressure depropanizer | 76.82% |
| 8 | C2 hydrogenator | 34.98% |
| 9 | Cold box system | 13.82% |
| 10 | Expanding machine | 13.82% |
| 11 | Pre- domethanizing column | 11.76% |
| 12 | Domethanizing column | 13.76% |
| 13 | Dethanizer | 24.11% |
| 14 | Ethylene rectifying column | 1.37% |
| 15 | C3 hydrogenator | 48.66% |
| 16 | Propylene rectification tower | 48.66% |
| 17 | Debutanizing tower | 103.82% |
| Invest (hundred million yuan) in ethylene separation part | 27.85 | |
| It reduces investment outlay after integration (hundred million yuan) | 9.95 |
The method coupled using naphtha of the present invention and ethane cracking predepropanization with PDH, [embodiment 1]~[embodiment
4] data summarization is shown in Table 5:
5 embodiment data summary table of table
Claims (8)
1. a kind of method that naphtha and ethane cracking predepropanization are coupled with PDH, comprising: (1) ethylene unit reaction system: stone
Cerebrol and ethane cracking raw material enter cracking reaction unit and are cracked into hydro carbons mixed air, are sent to quenching unit, through chilling, washing
Afterwards, drippolene and Pyrolysis fuel oil PFO are isolated in cracking gas to send out out-of-bounds as final byproduct, the cracking gas of remaining component
After being sent to compression and drying unit compression, alkali cleaning, drying, deep cooling, it is sent to downstream predepropanization separation system；(2) PDH device is anti-
Answer system: fresh propane charging with from propylene rectification tower tower bottom recycled propane feed and de-oiling tower top material mix after enter
Propane gasification tank gasifies, and heating furnace is entered after the gas phase after gasification is preheated and dehydrogenation reactor system carries out dehydrogenation reaction,
The product gas of generation enters separation system after cooling and is separated；(3) coupling device separation system: ethylene cracking gas with
PDH device product gas is sent into coupling device compression, dry, deep cooling and separation system after mixing, compress, is dry, is after deep cooling mixed
Gentle to enter high pressure depropanization unit, tower top isolates part C3 and C3 more light component, is sent to demethanation unit；Tower reactor is isolated
Part C3 and C3 more heavy constituent, are sent to low pressure depropanization unit；Low pressure depropanization unit tower top isolates C3, is sent to propylene rectifying
Unit；Tower reactor isolates C4 and C4 more heavy constituent, is sent to debutanizing tower；Demethanation unit tower top isolates methane hydrogen as by-product
Object is sent out out-of-bounds, and tower reactor is isolated comprising the heavy constituent including all C2, and deethanization unit is sent to；Deethanization unit is to demethanation
Kettle material is separated；Deethanizer overhead is C2 component, is sent to ethylene distillation unit；Tower reactor is C3 component, is sent to propylene
Rectification cell；Ethylene distillation unit separates deethanizer overhead material rectifying, and tower top obtains ethylene, and tower bottom obtains ethane；Second
Alkene is sent out out-of-bounds as product, and ethane recycle returns to cracking unit.Propylene distillation system is by low pressure depropanizer top material and takes off
Ethylene oxide units kettle material rectifying separation, tower top obtain propylene, and tower bottom obtains propane, and propylene is sent out out-of-bounds as product, propane
It is recycled back into PDH reaction member；The input of debutanization system comes from low pressure depropanizer substrate material and PDH device de-oiling tower bottoms
Material, material are separated by rectifying, and tower top obtains mixing C4 component, tower bottom obtains drippolene, mix C4 component as final secondary
Product is sent out out-of-bounds, and drippolene merges with the drippolene from ethylene unit quenching unit also to be sent out out-of-bounds.
2. the method that naphtha and ethane cracking predepropanization are coupled with PDH according to claim 1, it is characterised in that ethylene
Device nominal capacity is 80~1,500,000 tons/year.
3. the method that naphtha and ethane cracking predepropanization are coupled with PDH according to claim 1, it is characterised in that PDH
Device nominal capacity is 600,000 tons/year.
4. the method that naphtha and ethane cracking predepropanization are coupled with PDH 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 naphtha and ethane cracking predepropanization are coupled with PDH 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 naphtha and ethane cracking predepropanization are coupled with PDH according to claim 1, it is characterised in that coupling
For technique process units ethylene nominal capacity afterwards compared with original ethylene unit, ethylene nominal capacity is constant, compression and segregative line
Load of uniting is about the 101~247% of original ethylene unit.
7. the method that naphtha and ethane cracking predepropanization are coupled with PDH according to claim 1, it is characterised in that ethylene
Device raw material weight group becomes 30% naphtha, 70% ethane.
8. the method that naphtha and ethane cracking predepropanization are coupled with PDH 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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910051573.XA CN109761733A (en) | 2019-01-21 | 2019-01-21 | The method that naphtha and ethane cracking predepropanization are coupled with PDH |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910051573.XA CN109761733A (en) | 2019-01-21 | 2019-01-21 | The method that naphtha and ethane cracking predepropanization are coupled with PDH |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109761733A true CN109761733A (en) | 2019-05-17 |
Family
ID=66454765
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910051573.XA Pending CN109761733A (en) | 2019-01-21 | 2019-01-21 | The method that naphtha and ethane cracking predepropanization are coupled with PDH |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109761733A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 CN201910051573.XA patent/CN109761733A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Non-Patent Citations (1)
| Title |
|---|
| 王松汉等: "《乙烯工艺与技术》", 30 June 2000, 北京：中国石化出版社 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| 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 |
| 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 |
|---|---|---|
| CN107602323A (en) | The method that dehydrogenating propane technique couples with light hydrocarbon cracking predepropanization technique | |
| CN109809958A (en) | The method that light hydrocarbon cracking sequence separating technology is coupled with PDH technique | |
| CN107673947A (en) | The method that dehydrogenating propane technique couples with naphtha pyrolysis front-end deethanization technique | |
| CN109761733A (en) | The method that naphtha and ethane cracking predepropanization are coupled with PDH | |
| CN107602324A (en) | The method that dehydrogenating propane technique couples with naphtha pyrolysis predepropanization technique | |
| CN104230617B (en) | The method that MTO technique couples with Petroleum and Deposition During Propane Pyrolysis order separating technology | |
| CN109761734A (en) | The method that naphtha and ethane cracking front-end deethanization are coupled with PDH | |
| CN104151121B (en) | The method that MTO technique is coupled with naphtha cracking predepropanization technique | |
| CN102040445B (en) | Technology device and method for preparing propylene by dehydrogenating propane or propane-enriched low carbon hydrocarbon | |
| CN109809957A (en) | The method that light hydrocarbon cracking front-end deethanization technique is coupled with PDH technique | |
| CN101717658B (en) | Multi-vaporization feeding method of oil product fractionator | |
| CN104193574B (en) | The coupling process of MTO technique and naphtha steam cracking ethylene process processed | |
| CN109761735A (en) | The method that naphtha and Deposition During Propane Pyrolysis predepropanization are coupled with PDH | |
| CN101921161B (en) | Methanol To Olefins (MTO) gas separation process flow | |
| CN106609154A (en) | Method or producing gasoline from Fischer-Tropsch synthetic oil | |
| CN101092570B (en) | Method of catalytic cracking reaction for separating oil and gas rich in light hydrocarbon | |
| CN101092325A (en) | Method for preparing propylene by catalytic cracking olefin of containing carbon | |
| CN102372559B (en) | Ethylene separation method | |
| CN107144092B (en) | Device for producing high-purity ethylene by ethylene heat pump rectification and production process thereof | |
| CN109851461A (en) | The method that naphtha and Deposition During Propane Pyrolysis front-end deethanization are coupled with PDH | |
| CN109761736A (en) | Naphtha and ethane cracking sequentially separate the method coupled with PDH | |
| CN109734549A (en) | Naphtha and Deposition During Propane Pyrolysis sequentially separate the method coupled with PDH | |
| CN104193570B (en) | The method of MTO technique and the coupling of naphtha pyrolysis order separating technology | |
| CN109651038A (en) | The method that MTO technique is coupled with dehydrogenating propane technique | |
| CN107417481A (en) | The method that MTO techniques couple with light hydrocarbon cracking front-end deethanization technique |
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 | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20190517 |