CN205269076U - Allyl acetonitrile hydrocyanation system adiponitrile technology extractant recovery system - Google Patents
Allyl acetonitrile hydrocyanation system adiponitrile technology extractant recovery system Download PDFInfo
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- CN205269076U CN205269076U CN201520998703.8U CN201520998703U CN205269076U CN 205269076 U CN205269076 U CN 205269076U CN 201520998703 U CN201520998703 U CN 201520998703U CN 205269076 U CN205269076 U CN 205269076U
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- adiponitrile
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
This application requires protection allyl acetonitrile hydrocyanation system adiponitrile technology extractant recovery system, the utility model discloses utilize triple effect vaporization system to realize extractant recycle, in addition, through the optimization to triple effect evaporating heat exchange network, can realize effective utilization of energy, can realize the clean separation of extractant and heavy ends catalyst and auxiliary agent through the triple effect evaporation, do not contain any extractant at the bottom of the triple effect evaporation tata in heavy ends catalyst that comes out and the auxiliary agent, can get back to the preorder reactor completely and carry out recycle. The beneficial effects of the utility model reside in that, the comprehensive energy consumption of reduction in extractant recovery process to reduce the manufacturing cost of allyl acetonitrile hydrocyanation system adiponitrile technology, can separate recycle with extractant and catalyst and auxiliary agent completely and implement triple effect evaporation technology to the extractant of specific constitution.
Description
Technical field
The utility model belongs to chemical production technical field, particularly relates to a kind of pentenenitrile hydrocyanation adiponitrile technique extraction agent recovery system.
Background technology
Adiponitrile (ADN) is the oily liquids of a kind of water white transparency, is mainly used in reduction and generates hexanediamine, hexanediamine and hexanodioic acid generation neutralization reaction generation nylon salt, and this is the most important up to now industrial use of adiponitrile. Adiponitrile also can be used for the fermentation such as rocket fuel, electroplating industry, detergent additive and sterilant. Current China adiponitrile mainly relies on import, along with the fast development of China's nylon66 fiber industry in recent years, the demand of adiponitrile increases gradually, but as generating the important source material of nylon salt intermediate hexanediamine, domestic enterprise there is no throughput and relies on import completely. Therefore, the development of China's nylon66 fiber industry is had most important meaning by the production domesticization of adiponitrile production technology. Produce in the technique of adiponitrile at pentenenitrile hydrocyanation, can use with tributyl phosphate (TBP), the extraction agent that N,N-DIMETHYLACETAMIDE (DMAC) and C6��C10 alkane or aromatic hydrocarbons are mixed into certain proportion, utilizes this extraction agent to extract adiponitrile from hydrocyanation reaction liquid. The how recovery extraction agent of high-level efficiency less energy-consumption, it is achieved the recycle of extraction agent is the key factor of restriction pentenenitrile hydrocyanation Adiponitrile technique.
In pentenenitrile hydrocyanation adiponitrile production technology, a large amount of extraction agents can be used, just the adiponitrile in reaction solution can be separated by this extraction agent. How recycling extraction agent from raffinate is the key affecting adiponitrile production technology.
Summary of the invention
The purpose of this utility model is to solve in pentenenitrile hydrocyanation adiponitrile technique, and the high efficiency separation of the recycling of extraction agent, extraction agent and catalyzer reduces the energy consumption problem in extraction agent removal process. The utility model utilizes triple effect evaporation technique to achieve extraction agent and recycles, in addition, by the optimization to triple effect evaporation heat exchanger network, it is possible to realize effective utilization of energy, the comprehensive energy consumption being reduced in extraction agent removal process. The concrete technical scheme adopted is as follows:
A kind of pentenenitrile hydrocyanation adiponitrile technique extraction agent recovery process, comprises the steps:
Step 1: after the raffinate and the triple effect evaporation column overhead extraction agent steam heat-exchanging that come by extraction tower, sends into the first effect evaporator tower and evaporates, and first imitates evaporator tower tower bottom reboiler utilizes high pressure steam to heat;
Step 2: the 2nd effect evaporator tower tower bottom reboiler is first heated by the extraction agent steam sent from the first effect evaporator tower tower top, then sends into extraction agent and reclaims storage tank;
Step 3: non-vaporised liquid out at the bottom of the first effect evaporator tower tower enters the 2nd effect further reduction vaporization of evaporator tower;
Step 4: sending into triple effect evaporation tower tower bottom reboiler heat exchange from the 2nd effect evaporator tower tower top extraction agent steam out, the extraction agent steam condensate after heat exchange is sent into extraction agent and reclaimed storage tank;
Step 5: send into triple effect evaporation tower from the non-vaporised liquid sent at the bottom of the 2nd effect evaporator tower tower and do last reduction vaporization, triple effect evaporation column overhead extraction agent steam is first used for raffinate described in pre-heating step 1, then send into extraction agent and reclaim storage tank, the remaining heavy constituent of triple effect evaporation tower tower reactor is catalyzer and auxiliary agent, is delivered to anterior reactor and recycles.
The raffinate that extraction tower described in step 1 comes and triple effect evaporation column overhead steam heat-exchanging to 40��80 DEG C, extraction agent in described raffinate is by the tributyl phosphate of volume ratio 10��20%, the N,N-DIMETHYLACETAMIDE of 10��20% and C6��C10 alkane of 60��80% or aromatic hydrocarbons composition. The extraction agent of this composition can well utilize triple effect evaporation technique to be separated with auxiliary agent with catalyzer, makes not containing extraction agent in the catalyzer isolated and auxiliary agent, thus can not affect follow-up to the recycling of catalyzer and auxiliary agent.
First effect evaporator tower pressure-controlling is at 20��200kPaG, and the pressure of the 2nd effect evaporator tower and triple effect evaporation tower reduces by 40��120kPa successively.
A kind of pentenenitrile hydrocyanation adiponitrile technique extraction agent recovery system, comprise the first effect evaporator tower, 2nd effect evaporator tower, triple effect evaporation tower, first effect evaporator tower, 2nd effect evaporator tower, triple effect evaporation tower is respectively equipped with corresponding tower bottom reboiler, triple effect evaporation tower is provided with tower top interchanger, first effect evaporator tower is connected with the 2nd effect evaporator tower tower reactor by corresponding tower bottom reboiler, 2nd effect evaporator tower is connected with triple effect evaporation tower tower reactor by corresponding tower bottom reboiler, first effect evaporator tower tower top is connected with extraction agent withdrawing can by the 2nd effect evaporator tower tower bottom reboiler, 2nd effect evaporator tower tower top is connected with extraction agent withdrawing can by triple effect evaporation tower tower bottom reboiler, 3rd evaporator tower tower top is connected with extraction agent withdrawing can by tower top interchanger, raffinate entrance is connected with the first effect evaporator tower tower reactor by the 3rd evaporator tower tower top interchanger.
Above-mentioned recovery system heat exchanging network is optimized, the heat taken out of in the first effect, the 2nd effect and triple effect evaporation top of tower extraction agent steam is utilized respectively the raffinate of tower bottom reboiler and new input to be carried out preheating, ensure the optimization of heat exchanger network, effectively reduce energy consumption.
This technique and system achieve the recycling of extraction agent, being separated completely of extraction agent and heavy constituent catalyzer and auxiliary agent can be realized by triple effect evaporation system, the heavy constituent catalyzer exported at the bottom of triple effect evaporation tower tower and auxiliary agent do not contain any extraction agent, it is possible to return to preorder reactor completely and recycle. Can all return to, after first effect, the 2nd effect and triple effect evaporation column overhead portion extraction agent vapor condensation, the recycle that preorder extraction process realizes extraction agent.
The beneficial effects of the utility model are: the utility model utilizes triple effect evaporation technique to achieve extraction agent and recycles, in addition, by the optimization to triple effect evaporation heat exchanger network, effective utilization of energy can be realized, the comprehensive energy consumption being reduced in extraction agent removal process, thus reduce the production cost of pentenenitrile hydrocyanation adiponitrile technique.
Accompanying drawing explanation
Fig. 1 is pentenenitrile hydrocyanation adiponitrile technique extraction agent recovery system structure iron described in the utility model
Marginal data: 1, the first effect evaporator tower, the 2, the 2nd effect evaporator tower, 3, triple effect evaporation tower, 4, extraction agent withdrawing can, the 5, first effect evaporator tower tower bottom reboiler, the 6, the 2nd effect evaporator tower tower bottom reboiler, 7, triple effect evaporation tower tower bottom reboiler, 8, triple effect evaporation column overhead interchanger
A, raffinate, B, catalyzer and auxiliary agent, C, extraction agent
Embodiment
In order to the utility model is realized technique means, creation characteristic, reach object and effect is easy to understand; below embodiment of the present utility model is described further; but do not limit protection domain of the present utility model; it should be noted that; when not conflicting, the embodiment in the utility model creation and the feature in embodiment can combine mutually.
As shown in Figure 1, pentenenitrile hydrocyanation adiponitrile technique extraction agent recovery system described in the utility model, comprise the first effect evaporator tower 1, 2nd effect evaporator tower 2, triple effect evaporation tower 3, first effect evaporator tower 1, 2nd effect evaporator tower 2, triple effect evaporation tower 3 is respectively equipped with corresponding tower bottom reboiler 5-7, triple effect evaporation tower 3 is provided with tower top interchanger 8, first effect evaporator tower 1 is connected with the 2nd effect evaporator tower 2 tower reactor by corresponding tower bottom reboiler 5, 2nd effect evaporator tower 2 is connected with triple effect evaporation tower 3 tower reactor by corresponding tower bottom reboiler 6, first effect evaporator tower 1 tower top is connected with extraction agent withdrawing can 4 by the 2nd effect evaporator tower tower bottom reboiler 6, 2nd effect evaporator tower 2 tower top is connected with extraction agent withdrawing can 4 by triple effect evaporation tower tower bottom reboiler 7, 3rd evaporator tower 3 tower top is connected with extraction agent withdrawing can 4 by tower top interchanger 8, raffinate entrance is connected with the first effect evaporator tower 1 tower reactor by the 3rd evaporator tower tower top interchanger 8.
Embodiment 1:
The raffinate A32746kg/h of adiponitrile extraction process is preheated to 40 DEG C by triple effect evaporation column overhead interchanger 8 and enters the first effect evaporator tower 1, by percentage to the quality, containing extraction agent, the catalyzer of 20% and the auxiliary agent of 10% of 70% in raffinate A. First effect evaporator tower 1 pressure is 200kPaG, the extraction agent steam exported bottom the first effect evaporator tower 1 enters the 2nd effect evaporator tower 2, temperature 130 DEG C, pressure reduces 70kPa and carries out further reduction vaporization, then the non-vaporised liquid exported bottom the 2nd effect evaporator tower 2 enters triple effect evaporation tower 3, temperature 115 DEG C, pressure reduces 80kPa again. Finally from output catalyst and auxiliary agent B bottom triple effect evaporation tower 3, from first effect evaporator tower 1, the 2nd effect evaporator tower 2 and triple effect evaporation tower 3 top export extraction agent steam respectively through the 2nd effect evaporator tower tower bottom reboiler 6, triple effect evaporation tower tower bottom reboiler 7, triple effect evaporation column overhead interchanger 8 heat recovery and utilization after send into extraction agent withdrawing can 4, the extraction agent C reclaimed can again with the extraction for previous process, the object finally reaching separation with recycling.
The extraction agent 1,1341kg/h of 100% purity is reclaimed successively, 10683kg/h, 7213kg/h by sampling analysis measuring triple effect evaporation technique every grade of tower top; Whole catalyzer and auxiliary agent B is reclaimed bottom triple effect evaporation tower 3.
Embodiment 2:
The raffinate A37746kg/h of adiponitrile extraction process is preheated to 80 DEG C by triple effect evaporation column overhead interchanger 8 and enters the first effect evaporator tower 1, by percentage to the quality, containing extraction agent, the catalyzer of 15% and the auxiliary agent of 5% of 80% in raffinate A. First effect evaporator tower 1 pressure is 20kPaG, the extraction agent steam exported bottom the first effect evaporator tower 1 enters the 2nd effect evaporator tower 2, temperature 130 DEG C, pressure reduces 40kPa and carries out further reduction vaporization, then the non-vaporised liquid exported bottom the 2nd effect evaporator tower 2 enters triple effect evaporation tower 3, temperature 115 DEG C, pressure reduces 40kPa again. Finally from output catalyst and auxiliary agent B bottom triple effect evaporation tower 3, from first effect evaporator tower 1, the 2nd effect evaporator tower 2 and triple effect evaporation tower 3 top export extraction agent steam respectively through the 2nd effect evaporator tower tower bottom reboiler 6, triple effect evaporation tower tower bottom reboiler 7, triple effect evaporation column overhead interchanger 8 heat recovery and utilization after send into extraction agent withdrawing can 4, the extraction agent C reclaimed can again with the extraction for previous process, the object finally reaching separation with recycling.
The extraction agent 1,2427kg/h of 100% purity is reclaimed successively, 11543kg/h, 7745kg/h by sampling analysis measuring triple effect evaporation technique every grade of tower top; Whole catalyzer and auxiliary agent B is reclaimed bottom triple effect evaporation tower 3.
Embodiment 3:
The raffinate A38746kg/h of adiponitrile extraction process is preheated to 60 DEG C by triple effect evaporation column overhead interchanger 8 and enters the first effect evaporator tower 1, by percentage to the quality, containing extraction agent, the catalyzer of 18% and the auxiliary agent of 7% of 75% in raffinate A. First effect evaporator tower 1 pressure is 160kPaG, the extraction agent steam exported bottom the first effect evaporator tower 1 enters the 2nd effect evaporator tower 2, temperature 130 DEG C, pressure reduces 120kPa and carries out further reduction vaporization, then the non-vaporised liquid exported bottom the 2nd effect evaporator tower 2 enters triple effect evaporation tower 3, temperature 115 DEG C, pressure reduces 40kPa again. Finally from output catalyst and auxiliary agent B bottom triple effect evaporation tower 3, from first effect evaporator tower 1, the 2nd effect evaporator tower 2 and triple effect evaporation tower 3 top export extraction agent steam respectively through the 2nd effect evaporator tower tower bottom reboiler 6, triple effect evaporation tower tower bottom reboiler 7, triple effect evaporation column overhead interchanger 8 heat recovery and utilization after send into extraction agent withdrawing can 4, the extraction agent C reclaimed can again with the extraction for previous process, the object finally reaching separation with recycling.
The extraction agent 1,2641kg/h of 100% purity is reclaimed successively, 11879kg/h, 8143kg/h by sampling analysis measuring triple effect evaporation technique every grade of tower top; Whole catalyzer and auxiliary agent B is reclaimed bottom triple effect evaporation tower 3.
Technique described in the utility model and system are described by specific embodiment. Those skilled in the art can use for reference content of the present utility model and suitably change conversion unit; the links such as reaction parameter realize other object corresponding; its relevant change does not all depart from content of the present utility model; all the utility model create spirit and principle within; any amendment of being done, equivalent replacements, improvement etc., all should be included within the protection domain of the utility model creation.
Claims (1)
1. a pentenenitrile hydrocyanation adiponitrile technique extraction agent recovery system, comprise the first effect evaporator tower, 2nd effect evaporator tower, triple effect evaporation tower, it is characterized in that, first effect evaporator tower, 2nd effect evaporator tower, triple effect evaporation tower is respectively equipped with corresponding tower bottom reboiler, triple effect evaporation tower is provided with tower top interchanger, first effect evaporator tower is connected with the 2nd effect evaporator tower tower reactor by corresponding tower bottom reboiler, 2nd effect evaporator tower is connected with triple effect evaporation tower tower reactor by corresponding tower bottom reboiler, first effect evaporator tower tower top is connected with extraction agent withdrawing can by the 2nd effect evaporator tower tower bottom reboiler, 2nd effect evaporator tower tower top is connected with extraction agent withdrawing can by triple effect evaporation tower tower bottom reboiler, 3rd evaporator tower tower top is connected with extraction agent withdrawing can by tower top interchanger, raffinate entrance is connected with the first effect evaporator tower tower reactor by the 3rd evaporator tower tower top interchanger.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105481720A (en) * | 2015-12-04 | 2016-04-13 | 中国天辰工程有限公司 | Extractant recovery method and system of technology for preparing adiponitrile trough hydrocyanating allyl acetonitrile |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105481720A (en) * | 2015-12-04 | 2016-04-13 | 中国天辰工程有限公司 | Extractant recovery method and system of technology for preparing adiponitrile trough hydrocyanating allyl acetonitrile |
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