CN201785324U - Reactive system for producing 2-ethyl hexenoicaldehyde from butyric aldehyde - Google Patents
Reactive system for producing 2-ethyl hexenoicaldehyde from butyric aldehyde Download PDFInfo
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- CN201785324U CN201785324U CN 201020204103 CN201020204103U CN201785324U CN 201785324 U CN201785324 U CN 201785324U CN 201020204103 CN201020204103 CN 201020204103 CN 201020204103 U CN201020204103 U CN 201020204103U CN 201785324 U CN201785324 U CN 201785324U
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Abstract
The utility model provides a reactive system for producing 2-ethyl hexenoicaldehyde from butyric aldehyde, which comprises a first reactor, a second reactor, a first chromatographic device and a second chromatographic device. An outlet of the first reactor is connected with an inlet of the first chromatographic device by the aid of a pipeline; a lower outlet of the first chromatographic device is communicated with the outside; an upper outlet of the first chromatographic device is connected with an inlet of the second reactor by the aid of a pipeline; an alkali liquor inlet of the first reactor is connected with an alkali liquor tank by the aid of a pipeline; an outlet of the second reactor is connected with an inlet of the second chromatographic device by the aid of a pipeline; a lower outlet of the second chromatographic device is connected with an alkali liquor inlet of the first reactor by the aid of a pipeline; a product outlet is arranged on an upper layer of the second chromatographic device; and a raw material inlet is arranged on the first reactor. The reactive system is more moderate in condensation reaction and is not easy to generate side products, so that the content of butyric aldehyde in butaldehyde raw materials for condensation is larger than or equal to 90%, separation of the butyric aldehyde from isobutylaldehyde is omitted, and cost is substantially reduced.
Description
Technical field
The utility model relates to a kind of reactive system by butyraldehyde-n production 2-ethyl hexenal, belongs to chemical technology field.
Background technology
Accompanying drawing 1 is seen at present industrial technical process by butyraldehyde-n production 2-ethyl hexenal: butyraldehyde-n enters the aldehyde condensation reaction system, and this system is made up of three placed in-line reactors.The first step of condensation reaction is that the butyraldehyde-n raw material is sent into well heater 11, the alkaline stream of sending back to recycle pump 121 mixes, butyraldehyde-n generates the acetaldol that contracts in the presence of alkaline solution, and dehydration generates the 2-ethyl hexenal simultaneously, most being reflected in this loop produces, then material is admitted to and continues reaction in second response circuit and the 3rd response circuit, second, three loops comprise two placed in-line condensation reactors 131,132, and 2-ethyl hexenal recycle pump 121,123, finish condensation reaction and produce 2-ethyl hexenal and a small amount of poly butyraldehyde, 2-ethyl-impurity such as 4-methylpent olefine aldehydr.
The tertiary circuit expel liquid is 2-ethyl hexenal and water, through interchanger 1-4 warm-up cycle alkali lye, again through water cooler 15 coolings, send into chromatography device 16, material is divided into two-layer up and down in the chromatography device, the upper strata is 2-ethyl hexenal and poly butyraldehyde, 2-ethyl-4-methylpent olefine aldehydr and impurity such as unreacted butyraldehyde-n and isobutyric aldehyde, lower floor is for containing the buck phase, this water is extracted out with NaOH solution circulating pump 17, mend 50% fresh alkali lye, be made into the sig water of 2% concentration, after interchanger 14 preheatings, add the first condensation reaction loop, its add-on is 55%～60% of an aldehyde inlet amount.
Though this cover process system is comparatively ripe, still has certain defective.At first, in three response circuits of n butyraldehyde aldolization part, first loop feeds fresh alkaline catalyst solution, and condensation reaction intensity is bigger in first loop, and reaction is very fast, more easily generates poly butyraldehyde, 2-ethyl-by products such as 4-methylpent olefine aldehydr; Secondly the alkali concn of fresh alkaline catalyst solution is controlled to be 2% usually, if improve the then easier generation side reaction of concentration of fresh soda solution, and condensation reaction itself has the water generation, therefore, has a large amount of diluted alkaline wastewaters and produces; Once more, be applicable to butyraldehyde-n content requirement 〉=99.8% in the butyraldehyde raw material of condensation, therefore need could incite somebody to action wherein isobutyric aldehyde Impurity removal greater than the rectifying tower of 100 stage number, energy consumption is bigger, and complex process.
The utility model content
The purpose of this utility model is to provide a kind of reactive system by propyl carbinol production 2-ethyl hexenal, to overcome the deficiencies in the prior art.
The technical solution of the utility model is:
A kind of reactive system by propyl carbinol production 2-ethyl hexenal comprises first reactor, second reactor, the first layer parser and second layer parser; Wherein: the outlet of first reactor is connected through pipeline with the inlet of the first layer parser; Lower floor's outlet of the first layer parser communicates with the external world, and the upper strata outlet of the first layer parser is connected through pipeline with the inlet of second reactor; The alkali liquor inlet of second reactor and lye vat connect 1, the second reactor through pipeline outlet is connected through pipeline with the inlet of second layer parser; Lower floor's outlet of second layer parser is connected through pipeline with the alkali liquor inlet of first reactor; The product outlet is established on the upper strata of second layer parser, establishes material inlet on first reactor.
First reactor and second reactor are stirred-tank reactor.
Further, the outlet of first reactor is connected through pipeline by the inlet of first water cooler with the first layer parser; The outlet of second reactor is connected through pipeline by the inlet of second water cooler with second layer parser.
Further, the outlet of second reactor is connected through pipeline by the inlet of interchanger with second water cooler; The alkali liquor inlet of second reactor is connected through pipeline with lye vat by interchanger.
Adopt above-mentioned reactive system of the present utility model, with the butyraldehyde is raw material, condensation reaction and dehydration reaction generation 2-ethyl hexenal are taking place in first reactor and second reactor under the katalysis of basic catalyst, the butyraldehyde raw material is contacted: be about to fresh alkaline catalyst solution and in second reactor, add with the adverse current form with alkaline catalyst solution, and fresh butyraldehyde raw material added in first reactor, make the reaction milder that takes place in the reactor, be difficult for generating the poly butyraldehyde, 2-ethyl-by products such as 4-methylpent olefine aldehydr, these two kinds of by products can be controlled in below the 0.1wt%.Therefore, be used for the butyraldehyde raw material butyraldehyde-n content of condensation as long as 〉=90% (mass percent) can directly enter aldehyde condensation workshop section and carry out condensation reaction; And do not need to adopt rectifying tower to remove isobutyric aldehyde impurity in the raw material, butyraldehyde-n content is reached 〉=99.8% (mass percent).
Compare with existing technology, reactive system of the present utility model has following advantage:
1. butyraldehyde and alkaline catalyst solution counter current contact are adopted in condensation reaction, make the reaction process milder, are difficult for producing by product;
2. can improve the alkali concn of fresh basic catalyst, reduce the quantity discharged of alkaline waste water;
3. butyraldehyde-n content 〉=90% (mass percent) can be sent into condensation workshop section in the butyraldehyde raw material, has so just simplified flow process, has reduced the energy consumption of flow process.Usually propene hydroformylation reaction obtain just, butyraldehyde-n content 〉=90% (mass percent) in the mixture of isobutyric aldehyde, some hydroformylation technology just can make, butyraldehyde-n content 〉=95% (mass percent) in the mixture of isobutyric aldehyde, and 2-ethyl after such raw material condensation-4-methyl amyl alcohol impurity still less;
4. having operational path now needs earlier positive isobutyric aldehyde to be separated, and further carry out the butyraldehyde condensation reaction again, and the isomery tower that the character of positive isobutyric aldehyde has caused the butyraldehyde separation need have 110 blocks of column plates is finished, and cost is higher.And reactive system of the present utility model has saved the separation of positive isobutyric aldehyde, has only increased the chromatography device, has significantly reduced cost.
Description of drawings
Fig. 1 is the process flow diagram of prior art;
Fig. 2 is a process flow diagram of the present utility model.
Embodiment
Further set forth the utility model below in conjunction with specific embodiment, should be understood that these embodiment only be used to the utility model is described and be not used in the restriction protection domain of the present utility model.
As shown in Figure 2, a kind of reactive system by propyl carbinol production 2-ethyl hexenal that the utility model provides comprises first reactor 311, second reactor 312, the first layer parser 331 and second layer parser 332; First reactor 311 and second reactor 312 are stirred-tank reactor.Wherein: the outlet of first reactor 311 is connected through pipeline with the inlet of the first layer parser 331 by first water cooler 361; Lower floor's outlet of the first layer parser 331 communicates with the external world by NaOH solution circulating pump 321, and the upper strata outlet of the first layer parser 331 is connected through pipeline with the inlet of second reactor 312; The alkali liquor inlet of second reactor 312 is connected through pipeline by alkali lye topping-up pump 35 and lye vat 38, and the outlet of second reactor 312 is connected through pipeline with the inlet of second layer parser 332 by second water cooler 362; Lower floor's outlet of second layer parser 332 is connected through pipeline by the alkali liquor inlet of NaOH solution circulating pump 322 with first reactor 311; The product outlet is established on the upper strata of second layer parser 332, and this outlet is connected with lower procedure through pipeline by transferpump 34; Establish material inlet on first reactor 311.
Further, the outlet of second reactor 312 is connected through pipeline by the inlet of interchanger 37 with second water cooler 362; The alkali liquor inlet of second reactor 312 is connected through pipeline by interchanger 37 and lye vat 38.
Claims (4)
1. the reactive system by propyl carbinol production 2-ethyl hexenal is characterized in that, comprises first reactor (311), second reactor (312), the first layer parser (331) and second layer parser (332); Wherein: the outlet of first reactor (311) is connected through pipeline with the inlet of the first layer parser (331); Lower floor's outlet of the first layer parser (331) communicates with the external world, and the upper strata outlet of the first layer parser (331) is connected through pipeline with the inlet of second reactor (312); The alkali liquor inlet of second reactor (312) is connected through pipeline with lye vat (38), and the outlet of second reactor (312) is connected through pipeline with the inlet of second layer parser (332); Lower floor's outlet of second layer parser (332) is connected through pipeline with the alkali liquor inlet of first reactor (311); The product outlet is established on the upper strata of second layer parser (332), and first reactor is established material inlet on (311).
2. reactive system as claimed in claim 1 is characterized in that, first reactor (311) and second reactor (312) are stirred-tank reactor.
3. reactive system as claimed in claim 1 is characterized in that, the outlet of first reactor (311) is connected through pipeline by the inlet of first water cooler (361) with the first layer parser (331); The outlet of second reactor (312) is connected through pipeline by the inlet of second water cooler (362) with second layer parser (332).
4. reactive system as claimed in claim 3 is characterized in that, the outlet of second reactor (312) is connected through pipeline by the inlet of interchanger (37) with second water cooler (362); The alkali liquor inlet of second reactor (312) is connected through pipeline with lye vat (38) by interchanger (37).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201020204103 CN201785324U (en) | 2010-05-25 | 2010-05-25 | Reactive system for producing 2-ethyl hexenoicaldehyde from butyric aldehyde |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201020204103 CN201785324U (en) | 2010-05-25 | 2010-05-25 | Reactive system for producing 2-ethyl hexenoicaldehyde from butyric aldehyde |
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| CN201785324U true CN201785324U (en) | 2011-04-06 |
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| CN 201020204103 Expired - Lifetime CN201785324U (en) | 2010-05-25 | 2010-05-25 | Reactive system for producing 2-ethyl hexenoicaldehyde from butyric aldehyde |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150056105A1 (en) * | 2013-08-20 | 2015-02-26 | Institute Of Nuclear Energy Research Atomic Energy Council, Executive Yuan | Automatic system for synthesizing 123i-mibg and automatic device for synthesizing and dispensing 123i-mibg comprising the same |
| CN113813902A (en) * | 2021-09-14 | 2021-12-21 | 宁夏百川科技有限公司 | Device and process for producing octenal |
| WO2023284024A1 (en) * | 2021-07-14 | 2023-01-19 | 南京延长反应技术研究院有限公司 | Micro-interface strengthening system for preparing octenal by n-butyraldehyde condensation, and preparation method |
| CN117229133A (en) * | 2023-11-16 | 2023-12-15 | 天津渤化工程有限公司 | Octenal preparation process |
-
2010
- 2010-05-25 CN CN 201020204103 patent/CN201785324U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20150056105A1 (en) * | 2013-08-20 | 2015-02-26 | Institute Of Nuclear Energy Research Atomic Energy Council, Executive Yuan | Automatic system for synthesizing 123i-mibg and automatic device for synthesizing and dispensing 123i-mibg comprising the same |
| US9221029B2 (en) * | 2013-08-20 | 2015-12-29 | Institute Of Nuclear Energy Research Atomic Energy Council, Executive Yuan | Automatic system for synthesizing 123I-MIBG and automatic device for synthesizing and dispensing 123I-MIBG comprising the same |
| WO2023284024A1 (en) * | 2021-07-14 | 2023-01-19 | 南京延长反应技术研究院有限公司 | Micro-interface strengthening system for preparing octenal by n-butyraldehyde condensation, and preparation method |
| CN113813902A (en) * | 2021-09-14 | 2021-12-21 | 宁夏百川科技有限公司 | Device and process for producing octenal |
| CN117229133A (en) * | 2023-11-16 | 2023-12-15 | 天津渤化工程有限公司 | Octenal preparation process |
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Legal Events
| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: SHANGHAI HUAYI ENERGY + CHEMICAL INDUSTRY CO., LTD Free format text: FORMER NAME: SHANGHAI COKING CO., LTD. |
|
| CP01 | Change in the name or title of a patent holder |
Address after: 200241 Minhang District, Wu Long Road, No. 4280, Shanghai Patentee after: Shanghai Hua Yi derived energy chemical Co., Ltd Address before: 200241 Minhang District, Wu Long Road, No. 4280, Shanghai Patentee before: Shanghai Coking Co., Ltd. |
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| CX01 | Expiry of patent term |
Granted publication date: 20110406 |
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| CX01 | Expiry of patent term |