CN203269817U - Improved production device for preparing isobutene from isobutane through dehydrogenation - Google Patents
Improved production device for preparing isobutene from isobutane through dehydrogenation Download PDFInfo
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- CN203269817U CN203269817U CN 201320250605 CN201320250605U CN203269817U CN 203269817 U CN203269817 U CN 203269817U CN 201320250605 CN201320250605 CN 201320250605 CN 201320250605 U CN201320250605 U CN 201320250605U CN 203269817 U CN203269817 U CN 203269817U
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- compressor
- isobutane
- rectifying tower
- dehydrogenation
- bed reactor
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Abstract
The utility model discloses an improved production device for preparing isobutene from isobutane through dehydrogenation. The improved production device comprises a fixed bed reactor; a reactant inlet of the fixed bed reactor is connected with an isobutane raw material tank through a feedstock heating furnace and a reactor material charge and discharge heat exchanger; a reaction product outlet of the fixed reactor is sequentially connected with a steam generator, a reactor material charge heat exchanger and a compressor; a liquid outlet of the compressor is connected with a rectifying tower; a gas outlet of the compressor is connected with a low-temperature recycling unit through a gas cooler and a drying separating tank; a liquid phase outlet of the drying separating tank is connected with the rectifying tower; a liquid outlet of the rectifying tower is connected with a product collecting device. The improved production device provided by the utility model recycles heat while preparing isobutene from isobutane through dehydrogenation, improves the production purity of isobutene, recycles produced tail gas, and prevents environment pollution.
Description
Technical field
The utility model relates to the improvement production equipment that a kind of dehydrogenation of isobutane prepares iso-butylene.
Background technology
Iso-butylene is as important Organic Chemicals in chemical field, can be used for producing the multiple fine chemical products such as isoprene-isobutylene rubber, polyisobutene, methylallyl chloride, trimethylacetic acid, isoprene, of paramount importancely be, the important raw materials for production of iso-butylene or main Chemicals MTBE, so the manufacture iso-butylene has become the research and development focus of chemical field.Select which kind of raw material to produce iso-butylene, and the iso-butylene that how production purity is higher, and effectively utilize and produce a large amount of tail gas and the byproduct that produces in the iso-butylene process, realize effective utilization of the energy in production process, become the technical problem that the iso-butylene production field needs to be resolved hurrily.
The utility model content
Technical problem to be solved in the utility model is to provide the improvement production equipment that a kind of dehydrogenation of isobutane prepares iso-butylene, has solved in prior art that waste gas can't utilize and the technical problem such as heat waste.
The improvement production equipment that the utility model provides a kind of dehydrogenation of isobutane to prepare iso-butylene, comprise fixed-bed reactor, the reaction-ure feeding mouth of described fixed-bed reactor is connected with the isobutane feedstock tank by charging process furnace, reactor input and output material interchanger, Trimethylmethane gasifier in turn; The regeneration air entrance of fixed-bed reactor is connected with air-heating furnace, air preheater, gas blower in turn, and the regeneration air outlet of fixed-bed reactor is connected with air preheater by the first vapour generator; The reaction product discharge port of fixed-bed reactor is connected with the second vapour generator, reactor input and output material interchanger, compressor in turn, the liquid exit of compressor connects rectifying tower, and the pneumatic outlet of compressor is connected with the low temperature recovery unit by gas cooler, dry separating tank in turn; Wherein, the liquid-phase outlet of dry separating tank is connected with rectifying tower, and the gaseous phase outlet of dry separating tank is connected with the low temperature recovery unit, and the liquid exit of rectifying tower is connected with product collection equipment.
Further, the liquid-phase outlet of the liquid exit of described compressor, dry separating tank all is connected with the charging stock tank of rectifying tower.
Further, the charging stock tank of described rectifying tower also is connected with the entrance of compressor.
The advantage that the utlity model has is:
The improvement production equipment that the utility model provides a kind of dehydrogenation of isobutane to prepare iso-butylene, when realizing the dehydrogenation of isobutane preparation, realized the recycle of heat, and improved the production purity of iso-butylene, recycled for producing tail gas, avoided environmental pollution.
Description of drawings
Fig. 1 is the structural representation that a kind of dehydrogenation of isobutane that the utility model provides prepares the improvement production equipment of iso-butylene.
In figure: 1-isobutane feedstock tank; 2-Trimethylmethane gasifier; 3-reactor input and output material interchanger; 4-charging process furnace; The 5-fixed-bed reactor; The 6-air preheater; The 7-air-heating furnace; The 8-gas blower; 9-the first vapour generator; 10-the second vapour generator; The 11-compressor; The 12-rectifying tower; 13-low temperature recovery unit; The 14-gas cooler; The dry separating tank of 15-; The 16-charging stock tank; 17-product collection equipment.
Embodiment
The utility model is described in further detail below in conjunction with the drawings and specific embodiments, so that those skilled in the art can better understand the utility model and being implemented, but illustrated embodiment is not as to restriction of the present utility model.
A kind of dehydrogenation of isobutane that the utility model provides prepares the improvement production equipment of iso-butylene, will be converted into iso-butylene under the katalysis of Trimethylmethane by the catalyzer in fixed-bed reactor.The improvement production equipment that the dehydrogenation of isobutane that the utility model provides prepares iso-butylene comprises fixed-bed reactor 5, compressor 11, low temperature recovery unit 13 and rectifying tower 12 as shown in Figure 1.At first Trimethylmethane in isobutane feedstock tank 1 gasifies by Trimethylmethane gasifier 2, and the charging after gasification realizes that by the reaction discharging of reactor input and output material interchanger 3 and fixed-bed reactor 5 heat exchange heats up, and effectively utilizes heat.After charging after intensification was further adopted charging process furnace 4 to heat up again and reached needed temperature, the reaction-ure feeding mouth by fixed-bed reactor entered fixed-bed reactor 5.
Fixed-bed reactor 5 inside carry out dehydrogenation reaction, regenerate after having reacted, steaming out at first, and then air purge heats up and catalyzer burns, and finds time and reduces.Wherein air purge heats up needed air by providing air by gas blower 8, at first carry out preheating by air preheater 6, then through entering the regeneration air entrance of fixed-bed reactor 5 after air-heating furnace 7 heat temperature raisings, after fixed-bed reactor 5, at first enter in waste heat boiler, first overheated to high pressure steam (41 kg/cm2g) in waste heat boiler, then enter the first vapour generator 9, then enter in air preheater 6, carry out the heat exchange preheating with regeneration air, finally then enter smoke stack emission.
After fixed-bed reactor 5 reactions, at first the reaction product that flows out in the reaction product discharge port of fixed-bed reactor produces high pressure steam by the second vapour generator 10 heat releases, then enter in reactor input and output material interchanger 3 and carry out heat exchange with the charging Trimethylmethane, and then pass in compressor 11, can select multi-stage compressor to boost, in every one-level compression, owing to having selected suitable compression ratio, make the efficiency optimization of compressor 11, and keep the temperature of gas lower than the minimum temperature of polymkeric substance generation.The hydrocarbons that compressed machine 11 compressions obtain is admitted in rectifying tower 12, and isolated gas is sent in low temperature recovery unit 13.
In low temperature recovery unit 13 these unit, most of rare gas element (hydrogen, nitrogen, carbon monoxide and carbonic acid gas) and some light hydrocarbon compounds are separated from reaction product.These waste gas concentrate in hydrogen-rich gas, can be used for catalyst reduction, can be used for fuel gas after hydrogen recovery is completed in the PSA unit outside the battery limit (BL).
Wherein, the rear isolated gas of compressed machine 11 is at first through gas cooler 14 propane refrigerant cooling down, then separate through super-dry separating tank 15, liquid phase after separation enters in rectifying tower 12, and gas phase enters low temperature recovery unit 13 and lowers the temperature concentratedly, and this low temperature recovery unit 13 adopts propylene refrigerations and cold process-stream to carry out progressively Multi-stage cooling in the copper aluminum heat exchanger.The gas of the purification that finally obtains send the unit of the PSA outside the battery limit (BL), after PSA unit dehydrogenation as fuel gas.
The liquid that 11 condensations obtain through compressor and dry separating tank 15 separate the liquid phase that obtains and gather in rectifying tower charging stock tank 16, the gaseous component of this charging stock tank 16 turns back to compressor 11 entrances to reduce the gas phase load of depropanizing tower, liquid phase enters in rectifying tower 12 after pump, interchanger heat exchange, and final product collection after rectifying tower 12 rectifying is in product collection equipment 17.
Described depropanizing tower is mainly for separating of propane and light constituent in Trimethylmethane, iso-butylene and other heavy constituent.The enough height of the working pressure of depropanizing tower can make tower top tail gas flow directly into battery limit (BL) outer fuel gas system without compressor.The reboiler of depropanizing tower adopts the heat supply of low-pressure steam lime set.Most of phegma of depropanizing tower comes from the condenser that the tower sidepiece is used cooling water temperature.In condenser, uncooled gas enters Pasteur's section on tower top.This a part of phegma comes from the cooling water cooler of the very useful propane refrigerant of depropanizing tower.The depropanizing tower bottom product carries out the heat exchange cooling with the interchanger that enters before tower before going out the battery limit (BL), then adopt cooling water temperature in water cooler at the bottom of tower, obtains final product iso-butylene product.
The above embodiment is the preferred embodiment that proves absolutely that the utility model is lifted, and protection domain of the present utility model is not limited to this.Being equal to that those skilled in the art do on the utility model basis substitutes or conversion, all within protection domain of the present utility model.Protection domain of the present utility model is as the criterion with claims.
Claims (3)
1. a dehydrogenation of isobutane prepares the improvement production equipment of iso-butylene, it is characterized in that: comprise fixed-bed reactor, the reaction-ure feeding mouth of described fixed-bed reactor is connected with the isobutane feedstock tank by charging process furnace, reactor input and output material interchanger, Trimethylmethane gasifier in turn; The regeneration air entrance of fixed-bed reactor is connected with air-heating furnace, air preheater, gas blower in turn, and the regeneration air outlet of fixed-bed reactor is connected with air preheater by the first vapour generator; The reaction product discharge port of fixed-bed reactor is connected with the second vapour generator, reactor input and output material interchanger, compressor in turn, the liquid exit of compressor connects rectifying tower, and the pneumatic outlet of compressor is connected with the low temperature recovery unit by gas cooler, dry separating tank in turn; Wherein, the liquid-phase outlet of dry separating tank is connected with rectifying tower, and the gaseous phase outlet of dry separating tank is connected with the low temperature recovery unit, and the liquid exit of rectifying tower is connected with product collection equipment.
2. dehydrogenation of isobutane according to claim 1 prepares the improvement production equipment of iso-butylene, it is characterized in that, the liquid exit of described compressor, the liquid-phase outlet of dry separating tank all are connected with the charging stock tank of rectifying tower.
3. dehydrogenation of isobutane according to claim 2 prepares the improvement production equipment of iso-butylene, it is characterized in that, the charging stock tank of described rectifying tower also is connected with the entrance of compressor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320250605 CN203269817U (en) | 2013-05-10 | 2013-05-10 | Improved production device for preparing isobutene from isobutane through dehydrogenation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320250605 CN203269817U (en) | 2013-05-10 | 2013-05-10 | Improved production device for preparing isobutene from isobutane through dehydrogenation |
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| Publication Number | Publication Date |
|---|---|
| CN203269817U true CN203269817U (en) | 2013-11-06 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201320250605 Expired - Fee Related CN203269817U (en) | 2013-05-10 | 2013-05-10 | Improved production device for preparing isobutene from isobutane through dehydrogenation |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104557406A (en) * | 2014-12-18 | 2015-04-29 | 安徽泰合森能源科技有限责任公司 | Isobutane dehydrogenation device |
| CN108160006A (en) * | 2018-02-13 | 2018-06-15 | 镇海石化建安工程有限公司 | Dehydrogenating propane device and dehydrogenating propane method |
-
2013
- 2013-05-10 CN CN 201320250605 patent/CN203269817U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104557406A (en) * | 2014-12-18 | 2015-04-29 | 安徽泰合森能源科技有限责任公司 | Isobutane dehydrogenation device |
| CN108160006A (en) * | 2018-02-13 | 2018-06-15 | 镇海石化建安工程有限公司 | Dehydrogenating propane device and dehydrogenating propane method |
| CN108160006B (en) * | 2018-02-13 | 2023-11-14 | 镇海石化建安工程股份有限公司 | Propane dehydrogenation device and propane dehydrogenation method |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20131106 Termination date: 20190510 |