CN202516538U - Fluidized bed reactor for preparing butadiene through oxidative dehydrogenation of butene - Google Patents
Fluidized bed reactor for preparing butadiene through oxidative dehydrogenation of butene Download PDFInfo
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- CN202516538U CN202516538U CN2012200801788U CN201220080178U CN202516538U CN 202516538 U CN202516538 U CN 202516538U CN 2012200801788 U CN2012200801788 U CN 2012200801788U CN 201220080178 U CN201220080178 U CN 201220080178U CN 202516538 U CN202516538 U CN 202516538U
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- Prior art keywords
- cyclone separator
- group
- cyclone
- dipleg
- phase section
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- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 title claims abstract description 36
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 title abstract 2
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 title abstract 2
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 title abstract 2
- 239000003054 catalyst Substances 0.000 claims abstract description 41
- 238000003860 storage Methods 0.000 claims abstract description 11
- 238000006356 dehydrogenation reaction Methods 0.000 claims description 16
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 16
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 238000012423 maintenance Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract 2
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000009826 distribution Methods 0.000 description 6
- 238000000034 method Methods 0.000 description 4
- LVYZJEPLMYTTGH-UHFFFAOYSA-H dialuminum chloride pentahydroxide dihydrate Chemical compound [Cl-].[Al+3].[OH-].[OH-].[Al+3].[OH-].[OH-].[OH-].O.O LVYZJEPLMYTTGH-UHFFFAOYSA-H 0.000 description 3
- 238000013461 design Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 238000003911 water pollution Methods 0.000 description 2
- 230000003190 augmentative effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010298 pulverizing process Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model discloses a fluidized bed reactor for preparing butadiene through oxidative dehydrogenation of butene. The fluidized bed reactor comprises a reactor body and a waste catalyst storage tank, wherein the reactor body is divided into a concentrated phase section, a dilute phase section and an expanding section; three stages of cyclone separator sets are arranged outside the reactor body; legs of a first-stage cyclone separator set and second-stage cyclone separator sets are communicated with the concentrated phase section and the dilute phase section of the reactor body respectively; a gas outlet of the first-stage cyclone separator set is connected with inlets of the second-stage cyclone separator set; gas outlets of the second-stage cyclone separator sets are connected with inlets of third-stage cyclone separator sets through pipelines respectively; and legs of the third-stage cyclone separator sets are communicated with the waste catalyst storage tank. Since the three stages of cyclone separator sets are arranged, the separation performance is superior, about 97 percent of catalyst can be captured, the fluidizing quality can be improved; and since the cyclone separator sets are externally arranged, the cyclone separator sets can be increased according to capacity expansion and production increase requirements to perform expansion and reconstruction, the treatment capacity of the fluidized bed reactor can be improved, observation and maintenance can be facilitated, and the cost can be reduced.
Description
Technical field
The utility model relates to a kind of butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor.
Background technology
Butadiene is the most important monomer of preparation synthetic rubber, and butylene oxidation-dehydrogenation is the main technique of producing butadiene.In process of production, fluidized-bed reactor is because of its fluid mapper process temperature stabilization, and the temperature difference is very little in the whole reactor; Temperature state reaction down such as can be considered, reaction temperature is easy to control, and bed voidage distributes more even; Bed expansion does not receive the restriction of the static height of bed, and heat transfer between gas-solid, mass transfer rate are than other ways of contact height, and the gas backmixing rate is very little; Production capacity is high, and catalyst loading and unloading is easy to advantage, becomes the first-selected reactor that butylene oxidation-dehydrogenation is produced butadiene.
Existing butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor comprises reactor body, in reactor body, is provided with the cyclone separator group.Its shortcoming is: 1. receive the restriction of reactor body volume, can only arrange the two stage cyclone splitter group, be provided with a cyclone separator in every grade of cyclone separator group; Separating power is limited; Most of catalyst fines can not in time be discharged from, stay in the reactor, stop up gas distribution grid.2. built-in cyclone separator is bulky, the difficulty of in reactor, arranging, so the expansion of pre-existing reactors can be increased production and transforms and will be restricted.3,, be difficult to judge intuitively that dipleg stops up, and be difficult for mediation because the dipleg of cyclone separator group is in inside reactor.
Summary of the invention
The technical problem that the utility model will solve provides a kind of catalyst fines and can in time fully discharge, can increase production the butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor that requirement is extended transformation, is convenient to observe the dipleg stopping state according to expanding.
The utility model is achieved in that
A kind of butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor; Comprise reactor body, dead catalyst storage tank; Described reactor body is divided into concentrated phase section, dilute phase section, expanding reach; Its special character is: outside reactor body, be provided with the three-stage cyclone separator group; Wherein the dipleg of primary cyclone group communicates with the concentrated phase section of reactor body, and the dipleg of secondary cyclone group communicates with the dilute phase section of reactor body, and described primary cyclone group gas vent links to each other with secondary cyclone group inlet; Described secondary cyclone group gas vent links to each other through pipeline respectively with three-stage cyclone separator group inlet, and the dipleg of three-stage cyclone separator group communicates with the dead catalyst storage tank.
Above-mentioned butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor; Described secondary cyclone group and three-stage cyclone separator group are established the cyclone separator of a plurality of parallel connections in respectively; Prevent that catalyst from being taken out of reaction system in a large number, cause equipment to stop up and water pollution.
Above-mentioned butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor; Described primary cyclone group by cyclone separator, dipleg, be connected the terminal anti-back taper of dipleg and constitute, described secondary cyclone group and three-stage cyclone separator group are made up of cyclone separator, dipleg, the flutter valve that is connected the dipleg end respectively.
Above-mentioned butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor; Establish a cyclone separator in the described primary cyclone group; Establish two cyclone separators in the secondary cyclone group, establish four cyclone separators in the three-stage cyclone separator group, to reach optimal separating efficiency.
The beneficial effect of the utility model is:
1, adopt three-stage cyclone separator group and placing outside the reactor, not only separating property is excellent, can catch the catalyst about 97%; Reduce cyclone dip-leg and stop up, reduce the loss of catalyst, increase activity of such catalysts; Prolong catalyst life; Improve the cyclone separator separative efficiency, improve fluidization quality, and solved existing apparatus and can not remodel and expand to be difficult to satisfy and enlarge the problem of producing;
2, because cyclone separator places outside the reactor, can increase the cyclone separator number, ability augmenting response device, thus increased the catalyst filling amount, the fluidized-bed reactor disposal ability is improved greatly.External cyclone separator is convenient to check duty in process of production, is convenient to maintenance, reduces maintenance cost.
3, adopt the dead catalyst storage tank to reclaim the fine powder catalyst, avoid being lost to subsequent processing, the equipment that prevents stops up and water pollution.
Description of drawings
Fig. 1 is the structural representation (corresponding embodiment 1) of the utility model;
Fig. 2 is the structural representation (corresponding embodiment 2) of the utility model.
Among the figure: 1-reactor body, 2-primary cyclone group, 3-secondary cyclone group, 4-three-stage cyclone separator group, 5-dead catalyst storage tank; 101-concentrated phase section, 102-dilute phase section, 103-expanding reach, 201-primary cyclone; 202-primary cyclone dipleg, 203-prevents back taper, 301-secondary cyclone, 302-secondary cyclone dipleg; The 303-flutter valve, 401-three-stage cyclone separator, 402-three-stage cyclone separator dipleg, 403-flutter valve.
The specific embodiment
Embodiment 1
As shown in Figure 1, this butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor comprises reactor body 1, places primary cyclone group 2, secondary cyclone group 3, three-stage cyclone separator group 4 outside the reactor body 1, dead catalyst storage tank 5; Described reactor body 1 is provided with oval upper cover and cone-shaped low head; Be provided with gas distribution grid in reactor body 1 bottom, described reactor body 1 is divided into concentrated phase section 101, dilute phase section 102, expanding reach 103; Said concentrated phase section 101 is provided with revolves baffle plate and jacket type inner cool tube more; Described primary cyclone group 2 by primary cyclone 201, primary cyclone dipleg 202, be connected the terminal anti-back tapers 203 of primary cyclone dipleg 202 and constitute; Primary cyclone group 2 can in establish one or more primary cyclones, present embodiment is an example with one.One-level cyclonic separation dipleg 202 communicates with the concentrated phase section 101 of reactor body 1 through anti-back taper 203; Described secondary cyclone group 3 by secondary cyclone 301, secondary cyclone dipleg 302, be connected the terminal flutter valves 303 of secondary cyclone dipleg 302 and constitute; Be provided with the secondary cyclone 301 of a plurality of parallel connections in the described secondary cyclone group 3; Present embodiment is an example with two, and reality is not limited by present embodiment.Secondary cyclonic separation dipleg 302 communicates with the dilute phase section 102 of reactor body 1 through flutter valve 303; Described three-stage cyclone separator group 4 by three-stage cyclone separator 401, three-stage cyclone separator dipleg 402, be connected the terminal flutter valves 403 of three-stage cyclone separator dipleg 402 and constitute; Be provided with the secondary cyclone 401 of a plurality of parallel connections in the described three-stage cyclone separator group 4; Present embodiment is an example with four, and reality is not limited by present embodiment.Three-stage cyclone separator dipleg 402 communicates with dead catalyst storage tank 5 through flutter valve 403; Described primary cyclone group 2 gas vents link to each other through pipeline with secondary cyclone group 3 inlets, and described secondary cyclone group 3 gas vents link to each other through pipeline with three-stage cyclone separator group inlet.
During production, spheric catalyst is joined reactor body 1 concentrated phase section 101, send into unstripped gas in reactor body 1 bottom, gas cushions the back and gets into gas distribution grid in cone, alleviated the load to gas distribution grid; Not only make unstripped gas enter into bed equably, prevent the catalyst reverse flow effect, guaranteed the catalyst bed layer height but also play through gas distribution grid.Unstripped gas upwards gets into concentrated phase section 101 behind gas distribution grid; Revolve baffle plate more and break air pocket, suppress growing up of bubble, improved the contacting of gas-solid two phases of unstripped gas and catalyst; Make unstripped gas even, reduced the axial backmixing of catalyst and gas in the time that catalyst layer stops; The jacket type inner cool tube has been controlled reaction temperature effectively.Contact with spheric catalyst at concentrated phase section 101 unstripped gas, carry out the butylene oxidation-dehydrogenation reaction; Catalyst dust of being taken out of by uprising gas and the catalyst granules that splashes on a small quantity get into dilute phase section 102 and expanding reach 103; Because the diameter of expanding reach 103 is bigger than concentrated phase section 101 and dilute phase section 102 diameters; The uprising gas flow velocity slows down, so catalyst granules just can the sedimentation next part and returned concentrated phase section 101, uprising gas continues to get into primary cyclone group 2; Cyclone separator 201 is isolated the catalyst of coarsegrain through primary cyclone dipleg 202; The anti-back taper 203 upper and lower side cone angles that are positioned at the dipleg exit are respectively 90 degree and 120 degree, and the design of upper end makes catalyst go downstream along an angle of 90 degrees, send the concentrated phase section 101 of reactor body back to and proceed reaction; The design of lower end stops that catalyst gets into dipleg with from bottom to top unstripped gas; Gas continues to get into secondary cyclone group 3, and the catalyst that cyclone separator 301 is isolated than small grain size passes through secondary cyclone dipleg 302, when catalyst accumulates to certain weight in dipleg; The flutter valve 303 that is positioned at secondary cyclone dipleg 302 exits will automatically be opened, and sends the catalyst discharge back to dilute-phase zone 102 and proceeds reaction.Gas continues to get into three-stage cyclone separator group 4; Cyclone separator 401 is isolated the catalyst of the superfine granularity after the pulverizing through three-stage cyclone separator dipleg 402; When catalyst accumulates to certain weight in dipleg; The flutter valve 403 that is positioned at three-stage cyclone separator dipleg 402 exits will automatically be opened, and catalyst is sent into dead catalyst storage tank 5 reclaim, and at last the isolated gas in three-stage cyclone separator group 4 tops is collected.
As shown in Figure 2, primary cyclone group～three-stage cyclone separator group 2,3,4 is established a cyclone separator in respectively, and other structure and operation principle are with embodiment 1.
Claims (4)
1. butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor; Comprise reactor body, dead catalyst storage tank; Described reactor body is divided into concentrated phase section, dilute phase section, expanding reach; It is characterized in that: outside reactor body, be provided with the three-stage cyclone separator group; Wherein the dipleg of primary cyclone group communicates with the concentrated phase section of reactor body, and the dipleg of secondary cyclone group communicates with the dilute phase section of reactor body, and described primary cyclone group gas vent links to each other with secondary cyclone group inlet; Described secondary cyclone group gas vent links to each other through pipeline respectively with three-stage cyclone separator group inlet, and the dipleg of three-stage cyclone separator group communicates with the dead catalyst storage tank.
2. butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor according to claim 1 is characterized in that: described secondary cyclone group and three-stage cyclone separator group are established the cyclone separator of a plurality of parallel connections in respectively.
3. butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor according to claim 1; It is characterized in that: described primary cyclone group by cyclone separator, dipleg, be connected the terminal anti-back taper of dipleg and constitute, described secondary cyclone group and three-stage cyclone separator group are made up of cyclone separator, dipleg, the flutter valve that is connected the dipleg end respectively.
4. butylene oxidation-dehydrogenation system butadiene fluidized-bed reactor according to claim 1; It is characterized in that: establish a cyclone separator in the described primary cyclone group; Establish two cyclone separators in the secondary cyclone group, establish four cyclone separators in the three-stage cyclone separator group.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200801788U CN202516538U (en) | 2012-03-06 | 2012-03-06 | Fluidized bed reactor for preparing butadiene through oxidative dehydrogenation of butene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012200801788U CN202516538U (en) | 2012-03-06 | 2012-03-06 | Fluidized bed reactor for preparing butadiene through oxidative dehydrogenation of butene |
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| Publication Number | Publication Date |
|---|---|
| CN202516538U true CN202516538U (en) | 2012-11-07 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012200801788U Expired - Lifetime CN202516538U (en) | 2012-03-06 | 2012-03-06 | Fluidized bed reactor for preparing butadiene through oxidative dehydrogenation of butene |
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| CN (1) | CN202516538U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103341341A (en) * | 2013-07-16 | 2013-10-09 | 中国科学院山西煤炭化学研究所 | Fluidized bed reactor for preparing butadiene |
-
2012
- 2012-03-06 CN CN2012200801788U patent/CN202516538U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103341341A (en) * | 2013-07-16 | 2013-10-09 | 中国科学院山西煤炭化学研究所 | Fluidized bed reactor for preparing butadiene |
| CN103341341B (en) * | 2013-07-16 | 2016-01-27 | 中国科学院山西煤炭化学研究所 | One prepares butadiene fluidized-bed reactor |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 121001 No. two, Chongqing Road, Guta District, Liaoning, Jinzhou, seven Patentee after: Jinzhou Design Institute, China Petroleum Group Northeast Refining & Chemical Engineering Co., Ltd. Address before: 121001 No. two, Chongqing Road, Guta District, Liaoning, Jinzhou, seven Patentee before: Jizhou Design Institute of CNPC Northeast Petroleum Refinery Engineering Co., Ltd. |
|
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20121107 |