CN207862226U - The device of preparing propylene by dehydrogenating propane - Google Patents
The device of preparing propylene by dehydrogenating propane Download PDFInfo
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- CN207862226U CN207862226U CN201820092008.9U CN201820092008U CN207862226U CN 207862226 U CN207862226 U CN 207862226U CN 201820092008 U CN201820092008 U CN 201820092008U CN 207862226 U CN207862226 U CN 207862226U
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- Prior art keywords
- heating furnace
- export pipeline
- connects
- reactor
- dehydrogenation
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- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 52
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 33
- 239000001294 propane Substances 0.000 title claims abstract description 26
- 238000006356 dehydrogenation reaction Methods 0.000 claims abstract description 47
- 238000010438 heat treatment Methods 0.000 claims abstract description 40
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000001257 hydrogen Substances 0.000 claims abstract description 25
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 25
- 239000007789 gas Substances 0.000 claims abstract description 21
- 239000000463 material Substances 0.000 claims abstract description 11
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 10
- 238000012545 processing Methods 0.000 claims abstract description 10
- 239000001273 butane Substances 0.000 claims abstract description 5
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 5
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000011069 regeneration method Methods 0.000 claims description 24
- 230000008929 regeneration Effects 0.000 claims description 23
- 239000003054 catalyst Substances 0.000 claims description 17
- 239000002737 fuel gas Substances 0.000 claims description 11
- 238000001035 drying Methods 0.000 claims description 4
- 238000005262 decarbonization Methods 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000005516 engineering process Methods 0.000 abstract description 7
- 238000006477 desulfuration reaction Methods 0.000 abstract description 2
- 230000023556 desulfurization Effects 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 15
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000002994 raw material Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 150000001335 aliphatic alkanes Chemical class 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003546 flue gas Substances 0.000 description 3
- 239000012495 reaction gas Substances 0.000 description 3
- 206010011416 Croup infectious Diseases 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000004073 vulcanization Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000002401 inhibitory effect Effects 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000012797 qualification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
- 238000004227 thermal cracking Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model is related to propylene manufacturing technology fields, the device of specifically a kind of preparing propylene by dehydrogenating propane, including material processing device, dehydrogenation reaction device, dry gas and product separator, material processing device includes debutanizing tower, debutanizing tower side connects propane inlet wire, debutanizing tower bottom connects butane outlet, the tower top export pipeline of debutanizing tower connects the first heating furnace, first heating furnace is connected with hydrogen inlet wire, first heating furnace export pipeline connects hydrogenation reactor, at the top of the export pipeline connection digester of hydrogenation reactor bottom, desulfurization pot bottom export pipeline sequentially passes through First Heat Exchanger, dehydrogenation reaction device is connected after adding hydrogen heating furnace, dehydrogenation reaction device connects dry gas and product separator.The utility model reactor pass cycle of operation is long, and one way is run more than 15 days.
Description
Technical field
The utility model is related to propylene manufacturing technology field, the device of specifically a kind of preparing propylene by dehydrogenating propane.
Background technology
Industrialized dehydrogenating propane（PDH）Propylene technique processed mainly has the Oleflex works of UOP
Skill, the Catofin techniques of American AB B lomars company, the fluid bed of Italian Snamprogetti (Si Namu companies)
(STAR) work is reformed in the steam activation of dehydrogenation (FBD) technique, German Krupp Uhdewcng (Krupp Wood company)
The PDH of skill and Linde (Lin De), BASF (BASF) and Statoil (Den Norske Stats Oljeselskap a.s. (Statoil Group)) joint development
Technique.
Oleflex techniques are developed in the 80's of 20th century, realize industrialization in Thailand first within 1990.
Oleflex techniques are mainly characterized by using moving-burden bed reactor, and reaction is uniform, stablizes, and catalyst activity is kept not for a long time
Become, reactor need not close or circulate operation when catalyst regeneration, while can continuous supplementation catalyst.It is dilution with hydrogen
Agent for inhibiting coking and thermal cracking, and makees thermophore and maintains dehydrogenation reaction temperature.The technology olefin yields are stablized, catalyst
Regeneration method is ideal, and catalyst service life is long, loadings are few, but moving bed technique is more complicated, investment and power consumption compared with
Greatly.
Catofin techniques are C3~C5 dehydrating alkanes production monoolefine technologies of American AB B lomars company exploitation.Mesh
Before, whole world You10Yu Jia factories use Catofin technique productions alkene.Catofin techniques include 4 processes: PDH
Propylene processed, the compression of reactor discharge material, the recycling of product and refined.Due to using hydro carbons/hot-air endless form operation, production
Product are single propylene.
FBD techniques are grown up on the basis of the vulcanization bed dehydrogenation preparing isobutene of Russia's exploitation, technological core
It is reactor-regenerative system, reaction and regeneration are completed in vulcanization bed.
The PDH techniques of Lin De, BASF and Den Norske Stats Oljeselskap a.s.'s cooperative development, dehydrogenating propane（PDH）It has become and works as
Preceding mainstream production technology, the system of the prior art short, high energy consumption the shortcoming there are the one way cycle of operation.
Utility model content
The technical problems to be solved in the utility model is to overcome the deficiencies of existing technologies, and provides a kind of preparing propylene by dehydrogenating propane
Device.
In order to solve the above-mentioned technical problem, the utility model provides the following technical solution：
A kind of device of preparing propylene by dehydrogenating propane, including material processing device, dehydrogenation reaction device, dry gas and product separation
Device.
Material processing device includes debutanizing tower, and debutanizing tower side connects propane inlet wire, and debutanizing tower bottom connects fourth
The tower top export pipeline of alkane outlet, debutanizing tower connects the first heating furnace, and the first heating furnace is connected with hydrogen inlet wire, the first heating
Stove export pipeline connects hydrogenation reactor, and hydrogenation reactor bottom export pipeline connects at the top of digester, the output of desulfurization pot bottom
Pipeline connects dehydrogenation reaction device after sequentially passing through First Heat Exchanger plus hydrogen heating furnace.
Dehydrogenation reaction device includes the first dehydrogenation reactor, the second dehydrogenation reactor, the first dehydrogenation reactor, the second dehydrogenation
Reactor is the fixed bed reactors for being loaded with catalyst, and the export pipeline of the first dehydrogenation reactor connects after adding hydrogen heating furnace
The export pipeline of second dehydrogenation reactor, the second dehydrogenation reactor passes through connection dry gas and product separation dress after First Heat Exchanger
It sets.
The dry gas and product separator include ice chest seperation system, and ice chest seperation system output end is separately connected de- second
Alkane tower and PSA system, PSA system are pressure swing adsorption system, for detaching hydrogen.Deethanizer bottom export pipeline connects propylene
Rectifying column, propylene rectification tower tower top connect propylene outlet, and propylene rectification tower bottom export pipeline connects propane inlet wire.
The device of preparing propylene by dehydrogenating propane further includes catalyst regeneration device, and catalyst regeneration device includes regeneration gas compression
Machine, regeneration air compressor connection regeneration heating furnace, regeneration heating furnace export pipeline are passed through in dehydrogenation reactor.
The ice chest seperation system includes sequentially connected stage compressor, decarbonization device, split-compressor, drying device
And ice chest.
The PSA system output end connection hydrogen outlet and fuel gas outlet, the top export pipeline connection of dethanizer
Fuel gas outlet.
First heating furnace plus hydrogen heating furnace are to be passed through fuel gas heating.
The utility model operation technological process be：
Feedstock processing：Raw material propane first passes around debutanizing tower and sloughs butane, by the first heating furnace after being mixed with hydrogen
It is heated to required temperature, and raw material is made all to vaporize, the raw material after vaporization, which enters into hydrogenation reactor, takes off alkene therein
Hydrocarbon, then deviate from sulfide therein through digester, it then exchanges heat with dehydrogenation reaction gas to 350 DEG C.
Reactive moieties：After the hydrogenated heating furnace of raw material from digester is heated to required reaction temperature, into dehydrogenation
Reactor, dehydrogenation reactor are two-stage, and raw material propane carries out dehydrogenation reaction, dehydrogenation reaction gas and raw material under the effect of the catalyst
40 DEG C are cooled further into dry gas and product separative element with air-cooled fully after heat exchange.
Dry gas and product separate section：C3 products and hydrogen rich gas are obtained by liquefaction separation mode using ice chest seperation system
Product, ice chest seperation system include reaction gas compression, decarburization, drying, four part of liquefaction separation；C3 products pass through deethanization successively
Tower, propylene rectification tower isolate qualified propylene and are sent into tank field, and propane cycles return to material processing unit；Hydrogen rich gas product enters
After PSA system extracts H2, fuel gas of the resolution gas as heating furnace.
In addition, catalyst regeneration and burning process are：Before burning beginning, first starts regeneration air compressor, enter from compressor
Nitrogen is introduced at mouthful, the nitrogen of supercharging is by flue gas heat-exchange unit heat exchange and production line to be regenerated, by regeneration heating furnace according to temperature
Degree is heated, and hot nitrogen purge operations are carried out into dehydrogenation reactor, burns gas through flue gas heat-exchange unit heat exchange and cigarette after heat exchange
After the cooling of air water cooler, into flue gas surge tank, gradually to take the oil gas in reactor out of.When the oil gas in reactor reaches peace
It is complete to require, and when reactor inlet temperature reaches the temperature for burning needs, air is introduced from suction port of compressor, according to reaction
The device situation of burning steps up oxygen content and reactor inlet temperature in circular regeneration gas, when there is no Wen Shenghou in reactor,
End is burnt, the activated centre further to catalyst is needed to redistribute after burning.System is purged with nitrogen finally and is replaced,
After oxygen content qualification in system, device can carry out the production operating in next period.
The advantageous effect that the utility model is reached is：
The utility model reactor pass cycle of operation is long, and one way is run more than 15 days；
The utility model uses fixed bed reactors, mature and reliable, small investment；
The utility model thoroughly recycles residual heat of reaction, and low energy consumption, highly selective, low material consumption.
Description of the drawings
Attached drawing is used to provide a further understanding of the present invention, and a part for constitution instruction, with this practicality
Novel embodiment for explaining the utility model, does not constitute limitations of the present invention together.In the accompanying drawings：
Fig. 1 is the utility model structure diagram；
In figure：1, hydrogen inlet wire；2, propane inlet wire；3, debutanizing tower；4, the first heating furnace；5, hydrogenation reactor；6, it takes off
Sulphur tank；7, First Heat Exchanger；8, air compressor is regenerated；9, heating furnace is regenerated；10, ice chest；11, stage compressor；12, decarburization fills
It sets；13, PSA system；14, add hydrogen heating furnace；15, the first dehydrogenation reactor；16, the second dehydrogenation reactor；17, drying device；
18, split-compressor；19, dethanizer；20, propylene rectification tower；21, hydrogen outlet；22, fuel gas outlet；23, propylene goes out
Line；24, butane outlet.
Specific implementation mode
The preferred embodiment of the utility model is illustrated below in conjunction with attached drawing, it should be understood that described herein excellent
It selects embodiment to be only used for describing and explaining the present invention, is not used to limit the utility model.
Embodiment：
As shown in Figure 1, a kind of device of preparing propylene by dehydrogenating propane, including material processing device, dehydrogenation reaction device, dry gas
And product separator, catalyst regeneration device.
Material processing device includes debutanizing tower 3, and 3 side of debutanizing tower connects propane inlet wire 2, and 3 bottom of debutanizing tower connects
Butane outlet 24 is connect, the tower top export pipeline of debutanizing tower 3 connects the first heating furnace 4, and the first heating furnace 4 is connected with hydrogen inlet wire
1,4 export pipeline of the first heating furnace connects hydrogenation reactor 5, and 5 bottom export pipeline of hydrogenation reactor connects 6 top of digester,
6 bottom export pipeline of digester connects dehydrogenation reaction device after sequentially passing through First Heat Exchanger 7 plus hydrogen heating furnace 14.
Dehydrogenation reaction device includes the first dehydrogenation reactor 15, the second dehydrogenation reactor 16, the first dehydrogenation reactor 15, the
Two dehydrogenation reactors 16 are the fixed bed reactors for being loaded with catalyst, and the export pipeline of the first dehydrogenation reactor 15 passes through plus hydrogen adds
The second dehydrogenation reactor 16 is connected after hot stove 14, the export pipeline of the second dehydrogenation reactor 16 connects after First Heat Exchanger 7
Dry gas and product separator.
The dry gas and product separator include ice chest seperation system, and ice chest seperation system output end is separately connected de- second
Alkane tower 19 and PSA system 13, PSA system 13 are pressure swing adsorption system.19 bottom export pipeline of dethanizer connects propylene rectifying
Tower 20,20 tower top of propylene rectification tower connect propylene outlet 23,20 bottom export pipeline connection propane inlet wire 2 of propylene rectification tower.
Catalyst regeneration device includes regeneration air compressor 8, the regeneration connection regeneration heating furnace 9 of air compressor 8, regeneration heating
9 export pipeline of stove is passed through in dehydrogenation reactor.
The ice chest seperation system includes sequentially connected stage compressor 11, decarbonization device 12, split-compressor 18, does
Dry device 17 and ice chest 10.
The PSA system output end connection hydrogen outlet 21 and fuel gas outlet 22, the top efferent duct of dethanizer 19
Line connects fuel gas outlet 22.
First heating furnace 4 plus hydrogen heating furnace 14 are to be passed through fuel gas heating.
Finally it should be noted that：The above descriptions are merely preferred embodiments of the present invention, is not limited to this
Utility model, although the utility model is described in detail with reference to the foregoing embodiments, for those skilled in the art
For, it still can be with technical scheme described in the above embodiments is modified, or to which part technical characteristic
Carry out equivalent replacement.Within the spirit and principle of the utility model, any modification, equivalent replacement, improvement and so on,
It should be included within the scope of protection of this utility model.
Claims (5)
1. a kind of device of preparing propylene by dehydrogenating propane, which is characterized in that including material processing device, dehydrogenation reaction device, dry gas
And product separator, material processing device include debutanizing tower, debutanizing tower side connects propane inlet wire, debutanizing tower bottom
Butane outlet is connected, the tower top export pipeline of debutanizing tower connects the first heating furnace, and the first heating furnace is connected with hydrogen inlet wire, the
One heating furnace export pipeline connects hydrogenation reactor, and hydrogenation reactor bottom export pipeline connects at the top of digester, digester bottom
Portion's export pipeline connects dehydrogenation reaction device after sequentially passing through First Heat Exchanger plus hydrogen heating furnace, and dehydrogenation reaction device includes the
One dehydrogenation reactor, the second dehydrogenation reactor, the first dehydrogenation reactor, the second dehydrogenation reactor are the fixed bed for being loaded with catalyst
The export pipeline of reactor, the first dehydrogenation reactor connects the second dehydrogenation reactor after adding hydrogen heating furnace, and the second dehydrogenation is anti-
The export pipeline of device is answered to pass through connection dry gas and product separator, the dry gas and product separator packet after First Heat Exchanger
Ice chest seperation system is included, ice chest seperation system output end is separately connected dethanizer and PSA system, Deethanizer bottom efferent duct
Line connect propylene rectification tower, propylene rectification tower tower top connect propylene outlet, propylene rectification tower bottom export pipeline connect propane into
Line.
2. the device of preparing propylene by dehydrogenating propane according to claim 1, which is characterized in that further include catalyst regeneration dress
It sets, catalyst regeneration device includes regeneration air compressor, and regeneration air compressor connection regeneration heating furnace regenerates heating furnace efferent duct
Line is passed through in dehydrogenation reactor.
3. the device of preparing propylene by dehydrogenating propane according to claim 1 or 2, which is characterized in that the ice chest seperation system
Including sequentially connected stage compressor, decarbonization device, split-compressor, drying device and ice chest.
4. the device of preparing propylene by dehydrogenating propane according to claim 1 or 2, which is characterized in that the PSA system output end
Hydrogen outlet and fuel gas outlet are connected, the top export pipeline of dethanizer connects fuel gas outlet.
5. the device of preparing propylene by dehydrogenating propane according to claim 4, which is characterized in that first heating furnace plus hydrogen
Heating furnace is to be passed through fuel gas heating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820092008.9U CN207862226U (en) | 2018-01-19 | 2018-01-19 | The device of preparing propylene by dehydrogenating propane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820092008.9U CN207862226U (en) | 2018-01-19 | 2018-01-19 | The device of preparing propylene by dehydrogenating propane |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN207862226U true CN207862226U (en) | 2018-09-14 |
Family
ID=63462390
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820092008.9U Expired - Fee Related CN207862226U (en) | 2018-01-19 | 2018-01-19 | The device of preparing propylene by dehydrogenating propane |
Country Status (1)
| Country | Link |
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| CN (1) | CN207862226U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110937975A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| CN110937971A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| CN110937970A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| 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 |
| CN112902022A (en) * | 2021-02-23 | 2021-06-04 | 浙江华泓新材料有限公司 | Product gas compressor system |
-
2018
- 2018-01-19 CN CN201820092008.9U patent/CN207862226U/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110937975A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| CN110937971A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| CN110937970A (en) * | 2018-09-21 | 2020-03-31 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| CN110937970B (en) * | 2018-09-21 | 2022-08-19 | 中国石化工程建设有限公司 | Method and system for preparing propylene |
| 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 |
| 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 |
| CN112902022A (en) * | 2021-02-23 | 2021-06-04 | 浙江华泓新材料有限公司 | Product gas compressor system |
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