CN107185460A - A kind of dehydrogenation of isobutane reactor and dehydrogenation of isobutane reaction process - Google Patents
A kind of dehydrogenation of isobutane reactor and dehydrogenation of isobutane reaction process Download PDFInfo
- Publication number
- CN107185460A CN107185460A CN201710554634.5A CN201710554634A CN107185460A CN 107185460 A CN107185460 A CN 107185460A CN 201710554634 A CN201710554634 A CN 201710554634A CN 107185460 A CN107185460 A CN 107185460A
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- China
- Prior art keywords
- catalyst
- dehydrogenation
- layer
- isobutane
- cylinder
- Prior art date
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- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 title claims abstract description 54
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 32
- 239000001282 iso-butane Substances 0.000 title claims abstract description 27
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 19
- 239000003054 catalyst Substances 0.000 claims abstract description 69
- 239000013049 sediment Substances 0.000 claims abstract description 13
- 239000000463 material Substances 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 5
- 238000006555 catalytic reaction Methods 0.000 claims description 4
- 230000035484 reaction time Effects 0.000 abstract description 5
- 238000004939 coking Methods 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 5
- 239000012535 impurity Substances 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0278—Feeding reactive fluids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a kind of dehydrogenation of isobutane reactor and dehydrogenation of isobutane reaction process.Catalyst is disposed with a kind of dehydrogenation of isobutane reactor, including cylinder (1), the cylinder (1), it is characterized in that：Cylinder (1) internal upper part is provided with multiple sediment incrustation baskets (2), the cylinder (1) if in catalyst be divided into dried layer arrangement, if if including dried layer catalyst layer A and dried layer catalyst layer B, every layer of catalyst layer A includes the catalyst that four groups of horizontal intervals are evenly arranged, every layer of catalyst layer B includes one group of catalyst, catalyst layer A and catalyst layer B arranged for interval, the inherent catalyst bottom of the cylinder (1) are provided with grid (6).Arrangement, change reacting environment form of the invention by changing catalyst, and change corresponding technological parameter so that dehydrogenation reaction is selectively increased substantially, coking phenomenon is reduced, reaction time lengthens.
Description
Technical field
The present invention relates to a kind of dehydrogenation of isobutane reactor, belong to technical field of chemical.The invention further relates to use
The technique that the dehydrogenation of isobutane reactor carries out dehydrogenation of isobutane reaction.
Background technology
At present, the charging of dehydrogenation of isobutane reactor is used radially fed (as shown in Figure 1), its feeder be with
The space that the coaxial cylinder of cylinder is surrounded with cylinder, the catalyst of cylinder is from top to bottom evenly arranged, and its reaction temperature is 610
DEG C, pressure be 0.3Mpa, exist in this structure of reactor and its technique raw material with catalyst reaction unbalanced, reaction time
Short, pressure drop is big, catalyst easy incrustation the problems such as, cause catalyst activity reduction, stability deficiency etc., influence product quality.
The content of the invention
For drawbacks described above present in prior art, dehydrogenation reaction selectivity can be caused significantly the invention provides a kind of
The dehydrogenation of isobutane reactor that degree is improved, coking phenomenon is reduced, reaction time lengthens.
The present invention is achieved by the following technical solution：A kind of dehydrogenation of isobutane reactor, including cylinder, the cylinder
Catalyst is disposed with vivo, it is characterized in that：The cylinder internal upper part is provided with the catalyst point in multiple sediment incrustation baskets, the cylinder
If being arranged for dried layer, if if including dried layer catalyst layer A and dried layer catalyst layer B, every layer of catalyst layer A includes four groups of levels
The catalyst being evenly arranged is spaced, every layer of catalyst layer B includes one group of catalyst, catalyst layer A and catalyst layer B intervals cloth
Put, catalyst bottom is provided with grid in the cylinder.
In the present invention, raw material first passes around sediment incrustation basket after reactor is entered, and catalyst layer is then flowed through vertically.Raw material
When by sediment incrustation basket, sediment incrustation basket can be intercepted impurity in raw material etc., prevent impurity from forming product into catalyst layer
Dirt, influences catalyst activity.Grid is used to support catalyst.
Further, the catalyst layer B corresponds to catalyst layer A middle part setting.
Further, material outlet of the grid away from the cylinder lower end has certain distance.Grid and cylinder lower end
Material outlet there is certain distance so that grid and outlet between have certain space, can make reaction product increase it is stagnant
The time is stayed, reaction is complete.
Present invention also offers a kind of dehydrogenation of isobutane reaction process, its technical scheme used is：Using above-mentioned different
Butane dehydrogenation reactor carries out dehydrogenation of isobutane reaction, and its feeding manner is the axial admission along dehydrogenation of isobutane reactor, thing
Material from top to bottom passes axially through the catalyst in the cylinder, and reaction temperature is 530-560 DEG C, and pressure is 0.1-0.2Mpa.
Preferably, reaction temperature is 550 DEG C, and pressure is 0.15Mpa.
The beneficial effects of the invention are as follows：The present invention can effectively reduce catalyst fouling problem, carry by setting sediment incrustation basket
High catalyst activity；By carrying out special arrangement to the arrangement of catalyst, and by by feeding manner by original footpath
It is changed into axial admission to charging, and by adjusting corresponding technological parameter so that dehydrogenation reaction is selectively increased substantially, coking
Phenomenon is reduced, reaction time lengthens.
Brief description of the drawings
Fig. 1 is the schematic diagram of dehydrogenation of isobutane reactor of the prior art；
Fig. 2 is structural representation of the invention in embodiment；
In figure, 1, cylinder, 2, sediment incrustation basket, 3, catalyst layer A, 4, catalyst layer B, 5, catalyst, 6, grid.
Embodiment
Below by non-limiting embodiment and the present invention is further illustrated with reference to accompanying drawing：
As shown in drawings, it is a kind of dehydrogenation of isobutane reactor, it includes being disposed with catalysis in cylinder 1, the cylinder 1
Agent, the internal upper part of cylinder 1 is provided with multiple sediment incrustation baskets 2, if the catalyst in the cylinder 1 is divided into dried layer arrangement, includes
If if dried layer catalyst layer A and dried layer catalyst layer B, every layer of catalyst layer A include the catalysis that four groups of horizontal intervals are evenly arranged
Agent, every layer of catalyst layer B is included in one group of catalyst, catalyst layer A and catalyst layer B arranged for interval, the cylinder 1 in catalysis
Agent bottom is provided with grid 6, and material outlet of the grid 6 away from the lower end of cylinder 1 has certain distance.
It is preferred that, the middle part that the catalyst layer B corresponds to catalyst layer A is set.
The feeding manner for the dehydrogenation of isobutane reactor that the present invention is used is axial admission, and material is from top to bottom along reactor
Axially past the catalyst in cylinder 1.Raw material enter reactor after first pass around sediment incrustation basket 2, then along reactor axis to
Flow through catalyst layer.Raw material is when by sediment incrustation basket 2, and sediment incrustation basket 2 can be intercepted impurity in raw material etc., prevent impurity
Into catalyst layer formation incrustation, catalyst activity is influenceed.The one side of grid 6 can support catalyst, on the other hand, grid with
There is certain space between material outlet, reaction product can be made to increase the holdup time so that reaction is complete.In course of reaction
The technological parameter used for：Reaction temperature is 530-560 DEG C, and pressure is 0.1-0.2Mpa.
The present invention can select dehydrogenation reaction by changing charging, reacting environment's form, and relevant art parameter adjustment
Property is increased substantially, coking phenomenon is reduced, reaction time lengthens；By setting sediment incrustation basket, catalyst incrustation can be effectively reduced
Problem, improves catalyst activity.
Other parts in the present embodiment use known technology, will not be repeated here.
Claims (5)
1. catalyst is disposed with a kind of dehydrogenation of isobutane reactor, including cylinder (1), the cylinder (1), it is characterized in that：Institute
State cylinder (1) internal upper part be provided with multiple sediment incrustation baskets (2), the cylinder (1) if in catalyst be divided into dried layer arrangement, include
If if dried layer catalyst layer A and dried layer catalyst layer B, every layer of catalyst layer A include the catalysis that four groups of horizontal intervals are evenly arranged
Agent, every layer of catalyst layer B includes one group of catalyst, catalyst layer A and catalyst layer B arranged for interval, and cylinder (1) inherence is urged
Agent bottom is provided with grid (6).
2. dehydrogenation of isobutane reactor according to claim 1, it is characterized in that：The catalyst layer B corresponds to catalyst
Layer A middle part is set.
3. dehydrogenation of isobutane reactor according to claim 1 or 2, it is characterized in that：The grid (6) is away from the cylinder
(1) material outlet of lower end has certain distance.
4. a kind of dehydrogenation of isobutane reaction process, it is characterized in that：It uses any described dehydrogenation of isobutane in claim 1-3
Reactor carries out dehydrogenation of isobutane reaction, and its feeding manner is the axial admission along dehydrogenation of isobutane reactor, and material is by up to
Under pass axially through catalyst in the cylinder (1), reaction temperature is 530-560 DEG C, and pressure is 0.1-0.2Mpa.
5. dehydrogenation of isobutane reaction process according to claim 4, it is characterized in that：Reaction temperature is 550 DEG C, and pressure is
0.15Mpa。
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710554634.5A CN107185460A (en) | 2017-07-10 | 2017-07-10 | A kind of dehydrogenation of isobutane reactor and dehydrogenation of isobutane reaction process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710554634.5A CN107185460A (en) | 2017-07-10 | 2017-07-10 | A kind of dehydrogenation of isobutane reactor and dehydrogenation of isobutane reaction process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107185460A true CN107185460A (en) | 2017-09-22 |
Family
ID=59882349
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710554634.5A Pending CN107185460A (en) | 2017-07-10 | 2017-07-10 | A kind of dehydrogenation of isobutane reactor and dehydrogenation of isobutane reaction process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107185460A (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201776133U (en) * | 2010-06-25 | 2011-03-30 | 山东齐旺达集团海仲化工科技有限公司 | Improved low-carbon hydrocarbon aromatization reactor |
| CN103420767A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Isobutene preparation method |
| CN105536654A (en) * | 2015-12-15 | 2016-05-04 | 惠生工程（中国）有限公司 | Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene |
| CN206924733U (en) * | 2017-07-10 | 2018-01-26 | 山东海丰能源科技有限公司 | A kind of dehydrogenation of isobutane reactor |
-
2017
- 2017-07-10 CN CN201710554634.5A patent/CN107185460A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201776133U (en) * | 2010-06-25 | 2011-03-30 | 山东齐旺达集团海仲化工科技有限公司 | Improved low-carbon hydrocarbon aromatization reactor |
| CN103420767A (en) * | 2012-05-16 | 2013-12-04 | 中国石油化工股份有限公司 | Isobutene preparation method |
| CN105536654A (en) * | 2015-12-15 | 2016-05-04 | 惠生工程（中国）有限公司 | Large-scale axial multistage-mixing heat exchange type oxydehydrogenation reactor for butylene |
| CN206924733U (en) * | 2017-07-10 | 2018-01-26 | 山东海丰能源科技有限公司 | A kind of dehydrogenation of isobutane reactor |
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