CN203269816U - Production device for increasing conversion rate of isobutene - Google Patents
Production device for increasing conversion rate of isobutene Download PDFInfo
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- CN203269816U CN203269816U CN 201320250575 CN201320250575U CN203269816U CN 203269816 U CN203269816 U CN 203269816U CN 201320250575 CN201320250575 CN 201320250575 CN 201320250575 U CN201320250575 U CN 201320250575U CN 203269816 U CN203269816 U CN 203269816U
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- rectifying tower
- bed reactor
- compressor
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- isobutene
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Abstract
The utility model provides a production device for increasing the conversion rate of isobutene. The production device comprises a fixed bed reactor, wherein a reactant feed port of the fixed bed reactor is connected with an isobutane raw material tank through a feeding heating furnace and a reactor feeding and discharging heat exchanger; a reactant product discharge port in the fixed bed reactor is sequentially connected with a first steam generator, a reactor feeding 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 separation tank, a liquid-phase outlet of the drying separation tank is connected with an inlet of the rectifying tower sequentially through a flash tank, a feed pump, a rectifying tower heat exchanger and an inlet of the rectifying tower, and an outlet of the rectifying tower is connected with a product collection device sequentially through the rectifying tower heat exchanger and a cooling device. The production device provided by the utility model realizes the cyclic utilization of heat while realizing the dehydrogenation preparation of the isobutene and can be used for increasing the conversion rate of the isobutene and improving the production purity of the isobutene.
Description
Technical field
The utility model relates to a kind of production equipment that improves isobutene conversion.
Background technology
Iso-butylene is as important Organic Chemicals in chemical field, mainly for the production of 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 production to come the manufacture iso-butylene, and can greatly improve in process of production the transformation efficiency of iso-butylene, the maximized raw materials for production that utilize, reducing production costs becomes 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 a kind of production equipment that improves isobutene conversion, has solved in prior art that waste gas can't utilize and the technical problem such as heat waste.
The utility model provides a kind of production equipment that improves isobutene conversion, 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 reaction product discharge port of fixed-bed reactor is connected with the first vapour generator, reactor input and output material interchanger, compressor in turn, the liquid exit of compressor is connected with the entrance of rectifying tower by flash tank, fresh feed pump, rectifying tower interchanger in turn, 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 also is connected with the entrance of rectifying tower by described flash tank, fresh feed pump, rectifying tower interchanger in turn, the gaseous phase outlet of dry separating tank is connected with the low temperature recovery unit, and the outlet of rectifying tower is connected with product collection equipment by rectifying tower interchanger, refrigerating unit in turn.
Further, described flash tank also is connected with the entrance of compressor.
Further, the regeneration air entrance of described 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 second vapour generator.
The advantage that the utlity model has is:
The utility model provides a kind of production equipment that improves isobutene conversion, when realizing the dehydrogenation of isobutane preparation, realized the recycle of heat, and improved transformation efficiency and the production purity of iso-butylene, recycled for producing tail gas, avoided environmental pollution.
Description of drawings
Fig. 1 is a kind of structural representation that improves the production equipment of isobutene conversion that the utility model provides.
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 second vapour generator; 10-the first vapour generator; The 11-compressor; The 12-rectifying tower; 13-low temperature recovery unit; 14 gas coolers; The dry separating tank of 15-; The 16-flash tank; 17-product collection equipment; The 18-fresh feed pump, 19-rectifying tower interchanger; The 20-refrigerating unit.
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 production equipment that improves isobutene conversion that the utility model provides is converted into iso-butylene by fixed-bed reactor 5 with Trimethylmethane under the katalysis of catalyzer.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 5 entered fixed-bed reactor 5.
Dehydrogenation reaction, reaction that the hydrocarbon compound charging is carried out in fixed-bed reactor 5 inside finish the rear steaming out of using, and burn with air purge intensification and catalyzer, vacuumize and reduce.Wherein the needed air of air purge intensification is provided by gas blower 8.At first air carries out preheating by air preheater 6, then through entering fixed-bed reactor 5 after air-heating furnace 7 heating, at first discharge fixed-bed reactor 5 enter in waste heat boiler when rear, first high pressure steam (41 kg/cm2g) overheated in waste heat boiler, then enter the second vapour generator 9, enter at last in air preheater 6, carry out preheating with the regeneration air of coming in, finally enter smoke stack emission.
After fixed-bed reactor 5 reactions, the reaction product that flows out in the reaction product discharge port of fixed-bed reactor is at first by the first vapour generator 10 coolings, then enter in reactor feed interchanger 3 and carry out heat exchange with charging, 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, and part is used for catalyst reduction, and remaining PSA unit outside the battery limit (BL) can be used for fuel gas after hydrogen recovery.
The rear isolated gas of compressed machine 11 is at first through gas cooler 14 use propylene refrigeration agent cooling downs, then separate through super-dry separating tank 15, liquid phase after separation enters in rectifying tower 12, and dry gas phase enter low temperature recovery unit 13 lower the temperature concentrated, this low temperature recovery unit 13 adopt the cooling and cold process-stream of propane refrigerant to carry out progressively in the copper aluminum heat exchanger Multi-stage cooling concentrates.The gas that finally obtains removes PSA outside the battery limit (BL).
The liquid that in process compressor 11, disengaging obtains and dry separating tank 15 separate the liquid phase that obtains and gather in flash tank 16, gaseous component in flash tank 16 turns back to compressor 11 to reduce the gas phase load of depropanizing tower, and the liquid phase of process flash tank 16 enters in rectifying tower 12 after fresh feed pump 18,19 heat exchange of rectifying tower interchanger.And the product after the rectifying that finally obtains also needed first to pass through rectifying tower interchanger 19 before collecting, and carried out heat exchange with it, realized that heat effectively utilizes, then after apparatus for supercooling 20 cools, was collected in product collection equipment 17.
Described depropanizing tower is 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 water of condensation of the water slurry tank of the side line of the knockout drum of compressor 11, dry separating tank 15 and distillation tower and the return tank at top and depropanizing tower before sewage treatment equipment, need to be sloughed the hydrocarbon compound component in water vaporization tower 22 outside being sent to the battery limit (BL).
At first water of condensation is assembled in water vaporization tower 22 holding tanks, is then controlled by liquid level-flow cascade controller and injects water vaporization tower 22.The hydrocarbon compound of the weight that gathers for a long time can regularly be seen processing off with truck.All light hydrocarbon compounds are separated and deliver to the hydrocarbon compound blowdown system.
The low-pressure steam that enters water vaporization tower 22 bottoms is controlled by flow director.The waste water of stripping tower is first used water quench in water cooler bottom stripping tower, then extract out with pump under the control of fluid level controller.The stripping tower top gas enters charging process furnace 4 after its knockout drum, to burn stripping hydrocarbon compound out.Condensed fluid in knockout drum with nitrogen pressure to sewage lagoon.
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. production equipment that improves isobutene conversion, 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 reaction product discharge port of fixed-bed reactor is connected with the first vapour generator, reactor input and output material interchanger, compressor in turn, the liquid exit of compressor is connected with the entrance of rectifying tower by flash tank, fresh feed pump, rectifying tower interchanger in turn, 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 also is connected with the entrance of rectifying tower by described flash tank, fresh feed pump, rectifying tower interchanger in turn, the gaseous phase outlet of dry separating tank is connected with the low temperature recovery unit, and the outlet of rectifying tower is connected with product collection equipment by rectifying tower interchanger, refrigerating unit in turn.
2. the production equipment of raising isobutene conversion according to claim 1, is characterized in that, described flash tank also is connected with the entrance of compressor.
3. the production equipment of raising isobutene conversion according to claim 2, it is characterized in that, the regeneration air entrance of described 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 second vapour generator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320250575 CN203269816U (en) | 2013-05-10 | 2013-05-10 | Production device for increasing conversion rate of isobutene |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320250575 CN203269816U (en) | 2013-05-10 | 2013-05-10 | Production device for increasing conversion rate of isobutene |
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| Publication Number | Publication Date |
|---|---|
| CN203269816U true CN203269816U (en) | 2013-11-06 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201320250575 Expired - Fee Related CN203269816U (en) | 2013-05-10 | 2013-05-10 | Production device for increasing conversion rate of isobutene |
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| Country | Link |
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| CN (1) | CN203269816U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106278844A (en) * | 2016-09-13 | 2017-01-04 | 天津渤化永利化工股份有限公司 | A kind of reduce the device and method of consumption of raw materials during propenecarbonyl |
-
2013
- 2013-05-10 CN CN 201320250575 patent/CN203269816U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106278844A (en) * | 2016-09-13 | 2017-01-04 | 天津渤化永利化工股份有限公司 | A kind of reduce the device and method of consumption of raw materials during propenecarbonyl |
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Legal Events
| 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 |
Granted publication date: 20131106 Termination date: 20190510 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |