CN206927855U - A kind of sulfuric acid process is alkylated process units - Google Patents
A kind of sulfuric acid process is alkylated process units Download PDFInfo
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- CN206927855U CN206927855U CN201720622932.9U CN201720622932U CN206927855U CN 206927855 U CN206927855 U CN 206927855U CN 201720622932 U CN201720622932 U CN 201720622932U CN 206927855 U CN206927855 U CN 206927855U
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Abstract
The utility model belongs to alkylated reaction engineering device technique field, and in particular to a kind of sulphation is alkylated process units.Reactor is connected by pipeline with flash tank,Entered through the gas phase that flash tank is isolated by pipeline in knockout drum,Gas phase in knockout drum enters in water condenser and compound air cooling after refrigeration compressor compresses,Converge and connect cryogen surge tank in the outlet of water condenser and compound air cooling,Cryogen surge tank liquid outlet connects flash tank by the Liquid level adjusting valve on pipeline and pipeline,Also include deisobutanizer,Gas phase iso-butane in deisobutanizer enters condenser,Gas phase iso-butane enters return tank after condenser condenses,Return tank is connected by pipeline with coalescence dehydrator,Coalescence dehydrator is connected with cryogen surge tank,Reactor connects sour hydrocarbon knockout drum,Circulation fluid after the separation of sour hydrocarbon knockout drum delivers into reactor cycles by valve and used,The liquid outlet of flash tank is connected by pipeline with reactor,Cryogenic fluid pump is set in connecting pipeline.
Description
Technical field
The utility model belongs to alkylated reaction engineering device technique field, and in particular to a kind of sulphation alkylation production dress
Put.
Background technology
Because alkyl plant is that iso-butane-butene feed enters reactor together with device recycle isobutane and cryogen,
Under the catalytic action of sulfuric acid, alkylated reaction occurs for iso-butane and butylene, generates alkylate oil.Alkylated reaction is that heat release is anti-
Should be, it is necessary to carry out controlling reaction temperature by substantial amounts of circulation cryogen, reaction temperature more low reaction effect is better for theory, oil quality
Better, side reaction is fewer.
After former alkyl plant technology needs substantial amounts of recycle isobutane to be mixed with raw material, then with after reaction effluent heat exchange
It is mixed with cryogen into alkylation reactor；If recycle isobutane is proceeded directly to after treatment refrigeration compressor to go out
In the surge tank of mouth,（Using cryogen buffer tank pressure 0.57MPA, flash tank pressure 30KPA, liquid phase iso-butane is due to pressure
Change, liquid phase is changed into gas phase, vaporization heat absorption, obtains the relatively low cryogen of temperature）；Can so produce more circulate it is cold
Agent, furthermore it is exactly to remove the temperature after the raw material after recycle isobutane exchanges heat with reactant can greatly reduce, reaction temperature
It can be controlled better；Due to some devices, designed capacity is limited at the beginning of design, how the processing load of aggrandizement apparatus,
It is increasing enterprise's problems faced to reduce production cost, and the often control of reaction temperature is emphasis.In existing alkyl
To change in reaction unit, the temperature after recycle isobutane 30T exchanges heat after being mixed with raw material 25T with reaction effluent is 14.5 degree, then
With circulation cryogen heat exchange, the temperature of charge into reactor is 8 degree, and the flow of such cryogen is certain, is reacted if proposing production
Temperature in device cannot control well.
The content of the invention
The purpose of this utility model is to provide a kind of sulfuric acid process alkylation production for problems of the prior art
Device, the device improve the flow of cryogen and reduce the reaction temperature of alkylation reactor, improve the effect of alkylated reaction.
The technical solution of the utility model is：
A kind of sulfuric acid process is alkylated process units, including reactor and flash tank, and reactor is connected by pipeline and flash tank
Connect, entered through the gas phase that flash tank is isolated by pipeline in knockout drum, the gas phase in knockout drum is through refrigerant compression
Enter after machine compression in water condenser and compound air cooling, the outlet of water condenser and compound air cooling converges and connects cryogen buffering
Tank, cryogen surge tank liquid outlet connect flash tank by the Liquid level adjusting valve on pipeline and pipeline, also include deisobutanizer,
Gas phase iso-butane in deisobutanizer enters condenser by pipeline, and gas phase iso-butane enters backflow after condenser condenses
Tank, return tank are connected by pipeline with coalescence dehydrator, and coalescence dehydrator is connected with cryogen surge tank, and described reactor passes through
Pipeline connects sour hydrocarbon knockout drum, and the circulation fluid after the separation of sour hydrocarbon knockout drum delivers into reactor cycles by valve and used,
The liquid outlet of described flash tank is connected by pipeline with reactor, and cryogenic fluid pump is set in connecting pipeline.
Specifically, raw material heat exchanger is connected on the pipeline that the flash tank liquid outlet is connected with reactor.
Specifically, described return tank is connected by pipeline through circulating pump with coalescence dehydrator.
Specifically, described circulating pump connects deisobutanizer simultaneously.
The beneficial effects of the utility model are：The present apparatus will exchange heat in raw material heat exchanger with reaction effluent, reactant
The amount of heat exchange material is reduced, and the temperature after raw material heat exchange is reduced to 6 degree, then enters together with the circulation cryogen from cryogenic fluid pump
Enter and alkylated reaction is completed in alkylation reactor.Due to the injection of iso-butane, the amount for circulating cryogen is improved, due to cryogen
Buffer tank pressure 0.57MPA, flash tank pressure 30KPA, for liquid phase iso-butane due to the change of pressure, liquid phase is changed into gas phase, vapour
Change heat absorption, obtain the relatively low cryogen of temperature.Using the pressure differential of the gateway of refrigeration compressor, cryogen yield is added, is improved
Reaction effect, oil quality are improved, and are realized and are proposed production synergy.The utility model device less investment, expense are low, reaction temperature
Degree is well controlled.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
1 raw material heat exchanger, 2 reactors, 3 sour hydrocarbon knockout drums, 4 flash tanks, 5 knockout drums,
6 refrigeration compressors, 7 water condensers, 8 compound air coolings, 9 cryogen surge tanks, 10 Liquid level adjusting valves,
11 deisobutanizers, 12 gas condensers, 13 return tanks, 14 circulating pumps, 15 coalescence dehydrators,
16 cryogenic fluid pumps.
Embodiment
The structural representation of process units, including reactor 2 and flash tank 4 are alkylated for a kind of sulfuric acid process as shown in Figure 1,
Reactor 2 is connected by pipeline with flash tank 4, is entered through the gas phase that flash tank 4 is isolated by pipeline in knockout drum 5,
Gas phase in knockout drum 5 enters in water condenser 7 and compound air cooling 8 after the compression of refrigeration compressor 6, the He of water condenser 7
Converge and connect cryogen surge tank in the outlet of compound air cooling 8（9）, cryogen surge tank（9）Liquid outlet passes through on pipeline and pipeline
Liquid level adjusting valve 10 connects flash tank（4）, also include deisobutanizer 11, the gas phase iso-butane in deisobutanizer 11 passes through
Pipeline enters condenser 12, and gas phase iso-butane enters return tank 13 after the condensation of condenser 12, return tank 13 by pipeline and
Coalescence dehydrator 15 is connected, and coalescence dehydrator 15 is connected with cryogen surge tank 9, and described reactor 2 connects sour hydrocarbon by pipeline
Knockout drum 3, the circulation fluid after the separation of sour hydrocarbon knockout drum 3 deliver into reactor 2 by valve and recycled, described flash distillation
The liquid outlet of tank 4 is connected by pipeline with reactor 2, and cryogenic fluid pump 16 is set in connecting pipeline.The liquid outlet of flash tank 4 with it is anti-
Answer and raw material heat exchanger 1 is connected on the pipeline of the connection of device 2.Described return tank 13 is by pipeline through circulating pump 14 and coalescence dehydrator
15 connections.Described circulating pump connects deisobutanizer 11 simultaneously.
When being reacted using device provided by the utility model, the recycle isobutane for carrying out self-circulating pump 14 is passed through
After coalescing the further dehydration of dehydrator 15, into cryogen surge tank 9, control to flash tank 4 and carry out by Liquid level adjusting valve 10
Flash distillation,（Due to cryogen buffer tank pressure 0.57MPA, flash tank pressure 30KPA, liquid phase iso-butane is due to the change of pressure, liquid
Mutually it is changed into gas phase, vaporization heat absorption, obtains the relatively low cryogen of temperature）, due to the injection of iso-butane, circulate measuring for cryogen and carry
It is high.
Finally it should be noted that:Above example is only illustrating the technical solution of the utility model rather than it is limited
System；Although the utility model is described in detail with reference to preferred embodiment, those of ordinary skill in the art should
Understand：Specific embodiment of the present utility model can still be modified or some technical characteristics are equally replaced
Change；Without departing from the spirit of technical solutions of the utility model, it all should cover in the claimed technical scheme of the utility model
Among scope.
Claims (4)
1. a kind of sulfuric acid process is alkylated process units, including reactor（2）And flash tank（4）, reactor（2）By pipeline with dodging
Steaming pot（4）Connection, through flash tank（4）The gas phase isolated enters knockout drum by pipeline（5）In, knockout drum（5）
In gas phase through refrigeration compressor（6）Enter water condenser after compression（7）With compound air cooling（8）In, water condenser（7）With it is compound
Air cooling（8）Outlet converge and connect cryogen surge tank（9）, cryogen surge tank（9）Liquid outlet passes through the liquid on pipeline and pipeline
Position regulating valve（10）Connect flash tank（4）, it is characterised in that also include deisobutanizer（11）, deisobutanizer（11）It is interior
Gas phase iso-butane condenser is entered by pipeline（12）, gas phase iso-butane passes through condenser（12）Enter return tank after condensation
（13）, return tank（13）Pass through pipeline and coalescence dehydrator（15）Connection, coalesce dehydrator（15）With cryogen surge tank（9）Even
Connect, described reactor（2）Sour hydrocarbon knockout drum is connected by pipeline（3）, through sour hydrocarbon knockout drum（3）Circulation fluid after separation passes through
Valve delivers into reactor（2）Recycle, described flash tank（4）Liquid outlet pass through pipeline and reactor（2）Connection,
Cryogenic fluid pump is set in connecting pipeline（16）.
2. sulfuric acid process alkylation process units according to claim 1, it is characterised in that the flash tank（4）Liquid outlet with
Reactor（2）Raw material heat exchanger is connected on the pipeline of connection（1）.
3. sulfuric acid process alkylation process units according to claim 1, it is characterised in that described return tank（13）Pass through pipe
Line is through circulating pump（14）With coalescing dehydrator（15）Connection.
4. sulfuric acid process alkylation process units according to claim 3, it is characterised in that described circulating pump（14）Connect simultaneously
Connect deisobutanizer（11）.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720622932.9U CN206927855U (en) | 2017-06-01 | 2017-06-01 | A kind of sulfuric acid process is alkylated process units |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201720622932.9U CN206927855U (en) | 2017-06-01 | 2017-06-01 | A kind of sulfuric acid process is alkylated process units |
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| CN206927855U true CN206927855U (en) | 2018-01-26 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020048519A1 (en) * | 2018-09-06 | 2020-03-12 | 中国石油化工股份有限公司 | Alkylation product separation method, alkylation reaction and separation method, and related apparatus |
-
2017
- 2017-06-01 CN CN201720622932.9U patent/CN206927855U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2020048519A1 (en) * | 2018-09-06 | 2020-03-12 | 中国石油化工股份有限公司 | Alkylation product separation method, alkylation reaction and separation method, and related apparatus |
| US11759726B2 (en) | 2018-09-06 | 2023-09-19 | China Petroleum & Chemical Corporation | Process for separating alkylation product, alkylation reaction and separation process, and related apparatus |
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| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20230117 Address after: 457000 new industrial park, Fanxian industrial cluster zone, Puyang City, Henan Province Patentee after: PUYANG SHENGYUAN ENERGY TECHNOLOGY CO.,LTD. Address before: 457000 New Industrial Park, Industrial Cluster Zone, Fan County, Puyang City, Henan Province Patentee before: PUYANG SHENGYUAN PETROCHEMICAL (Group) Co.,Ltd. |