CN203222563U - Halogen alkylation process system for preparing chloroethane - Google Patents
Halogen alkylation process system for preparing chloroethane Download PDFInfo
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- CN203222563U CN203222563U CN 201320026094 CN201320026094U CN203222563U CN 203222563 U CN203222563 U CN 203222563U CN 201320026094 CN201320026094 CN 201320026094 CN 201320026094 U CN201320026094 U CN 201320026094U CN 203222563 U CN203222563 U CN 203222563U
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- monochloroethane
- chloroethane
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- hydrochloric acid
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Abstract
The utility model discloses a halogen alkylation process system for preparing chloroethane, wherein a special chloroethane reactor is used for replacing a plurality of reaction vessels, thereby realizing large size of equipment and automatic control, and improving raw material conversion rate. According to gas-phase partial pressure difference of ethanol aqueous solution at different temperatures and gas-phase partial pressure difference of hydrochloric acid at different temperatures, a majority of ethanol and hydrochloric acid in the mixed reaction gas are respectively distilled and separated for returning into the chloroethane reactor for repeated use. By means of different boiling points of organic matters of chloroethane and ethanol with different concentrations, rectification technique is adopted for performing rectification and separating out chloroethane of which the content satisfies quality requirement. By means of different solubility of water in chloroethane at different temperatures, the temperature of the chloroethane is reasonably controlled for realizing chloroethane dewatering. majority of hydrochloric acid and alcohol which do not react in the production process are recycled to the special reactor for reuse, thereby reducing production cost and reducing total amount of pollutant. The halogen alkylation process system for preparing chloroethane has high practical value.
Description
Technical field
The utility model belongs to chemical technology field, relates in particular to a kind of halocarbon metallization processes system for preparing monochloroethane.
Background technology
The halogen alkylation methods is produced in the monochloroethane process, and main raw material is hydrochloric acid and alcohol, and liquor zinci chloridi is catalyzer, uses sulfuric acid, caustic soda etc. to carry out the chemical purification product as absorption agent; The alcohol of 15%--20% of having an appointment in the production process will pass through sulfuric acid absorption, therefore produces to contain the dilute sulphuric acid that contains ester, the organic class material of ethers in a large number; One ton of monochloroethane of every production consumes 3.0 ton 30% hydrochloric acid approximately, produces about 0.18 ton of chemical water, will produce about 3.0 tons of dilute hydrochloric acid that contain ethanol; Salkali waste neutralization and clear water washing etc. also produce waste lye and high COD sewage.The dilute sulphuric acid that produces, dilute hydrochloric acid, waste lye etc. are because wherein containing a large amount of organic class materials, and its recycling is worth lower and usage quantity is less, only takes not hold the improvement method to handle as waste liquid, and the pollution treatment cost is bigger, brings out many environmental pollution factorses; Adopt reactor as the heating major equipment in the production process, exist separate unit to yield poorly and feed stock conversion low, many undesirable elements such as the plant area area is big limit its industrial scale.
The utility model content
The purpose of this utility model is to utilize a kind of halocarbon metallization processes system for preparing monochloroethane, is intended to solve the waste liquid that exists in the existing monochloroethane production and handles, and the pollution treatment cost is bigger, brings out many environmental pollution factorses; Adopt reactor as the heating major equipment in the production process, exist separate unit to yield poorly and feed stock conversion low, many undesirable elements such as the plant area area is big limit its production-scale problem.
The purpose of this utility model is to provide a kind of halocarbon metallization processes system for preparing monochloroethane, and the halocarbon metallization processes system of described preparation monochloroethane comprises:
The monochloroethane reactor is for the preparation of monochloroethane;
Cooler condenser is connected with described monochloroethane reactor, is used for the monochloroethane cooling liquid that produces is handled;
Monochloroethane work in-process storage tank is connected with described cooler condenser, is used for storing cooled monochloroethane;
Rectifying tower is connected the monochloroethane rectifying separation that is used for described monochloroethane work in-process storage tank;
Water trap is connected with described rectifying tower, is used for the processed of monochloroethane;
The monochloroethane pan tank is connected with described water trap, is used for the storage of product monochloroethane;
Depickling degreasing tower is connected with described monochloroethane reactor, is used for the depickling skimming treatment of monochloroethane;
The sour water neutralizer with described depickling degreasing tower, is used for the neutralization operation of sour water.
Further, the halocarbon metallization processes system of described preparation monochloroethane adopts the special-purpose monochloroethane reactor of single cover to substitute many side-by-side reactions stills.
Further, the halocarbon metallization processes system of described preparation monochloroethane adopts the method that rectifying separation, physics dehydration separate.
Further, the halocarbon metallization processes system ethanol utilization ratio of described preparation monochloroethane brings up to more than 95%, unreacted hydrochloric acid and alcohol major part are recovered and reuse in the production process.
The utlity model has following advantage:
The method and system of the halocarbon metallization processes of the preparation monochloroethane that the utility model provides are used special-purpose monochloroethane reactor, adopt that ethanol concentrate, hydrochloric acid are instead distilled, work in-process monochloroethane rectifying separation, and technology such as physics dehydration are produced the monochloroethane product.This technology can be according to the industrial scale needs, and single cover unit design ability reaches the requirement of certain scale quantity; Do not use sulfuric acid and soda ash, production process no longer produces dilute sulphuric acid and waste lye; Unreacted ethanol recycling; The reuse again of unreacted hydrochloric acid dehydration concentrate; Water brought into by raw material hydrochloric acid, alcohol and chemical water forms after the depickling dealcoholysis to contain the lower process water discharge system of acidity, carries out the sewage disposal pipe network after adjusting pH value, alleviates environmental pollution pressure.According to monochloroethane production equipment scale, the special-purpose monochloroethane reactor of single cover substitutes many side-by-side reactions stills, reduces operation labour intensity, and the raising of plant automation level realizes that the maximization device substitutes the repeated dingus of many covers; Rectifying separation, physics dehydration substitute chemical separation methods such as sulfuric acid, sodium hydroxide, no longer produce dilute sulphuric acid and waste lye; The hydrochloric amount of the water of condensation of acid vapors after the depickling dealcoholysis is lower than 1.0%, sends into sewage network after neutralizing treatment, does not produce a large amount of dilute hydrochloric acid and high COD sewage, and the environmental pollution risk reduces; The more small-sized reactors of operation index such as special-purpose monochloroethane reactor service temperature, working pressure are optimized to some extent, the ethanol utilization ratio is brought up to more than 95%, the most of recovery of unreacted hydrochloric acid and alcohol is returned in the special purpose reactor and is reused in the production process, reduce production costs, reduce the total amount of pollutant.
Description of drawings
Fig. 1 is the halocarbon metallization processes system flowchart of the preparation monochloroethane that provides of the utility model embodiment.
Embodiment
In order to make the purpose of this utility model, technical scheme and advantage clearer, below in conjunction with drawings and Examples, the utility model is further elaborated.Should be appreciated that specific embodiment described herein only in order to explaining the utility model, and be not used in restriction the utility model.
The utility model embodiment provides a kind of halocarbon metallization processes system for preparing monochloroethane, and the halocarbon metallization processes system of this preparation monochloroethane comprises:
The monochloroethane reactor is for the preparation of monochloroethane;
Cooler condenser is connected with the monochloroethane reactor, is used for the monochloroethane cooling liquid that produces is handled;
Monochloroethane work in-process storage tank is connected with cooler condenser, is used for storing cooled monochloroethane;
Rectifying tower is connected the monochloroethane rectifying separation that is used for monochloroethane work in-process storage tank;
Water trap is connected with rectifying tower, is used for the processed of monochloroethane;
The monochloroethane pan tank is connected with water trap, is used for the storage of product monochloroethane;
Depickling degreasing tower is connected with the monochloroethane reactor, is used for the depickling skimming treatment of monochloroethane;
The sour water neutralizer with depickling degreasing tower, is used for the neutralization operation of sour water.
As the prioritization scheme of the utility model embodiment, the halocarbon metallization processes system of preparation monochloroethane adopts the special-purpose monochloroethane reactor of single cover to substitute many side-by-side reactions stills.
As the prioritization scheme of the utility model embodiment, the method that the halocarbon metallization processes system of preparation monochloroethane adopts rectifying separation, physics dehydration to separate.
As the prioritization scheme of the utility model embodiment, the halocarbon metallization processes system ethanol utilization ratio of preparation monochloroethane is brought up to more than 95%, and unreacted hydrochloric acid and alcohol major part are recovered and reuse in the production process.
Following with reference to accompanying drawing, the method and system of the halocarbon metallization processes of the preparation monochloroethane of the utility model embodiment are described in further detail.
As shown in Figure 1, the system of the halocarbon metallization processes of the preparation monochloroethane of the utility model embodiment may further comprise the steps:
As shown in Figure 1, a kind of halocarbon metallization processes process for preparing monochloroethane of the present utility model: the some amount concentration that preparation meets the demands in the monochloroethane reactor 1 of special use is the zinc chloride acidic solution of 70%--80%, under the externally heat supply indirect heating condition, liquor zinci chloridi is natural circulation in special-purpose monochloroethane reactor 1; Pump into dense (rare) hydrochloric acid from special-purpose monochloroethane reactor 1 bottom, enter alcohol (overheated) gas or pump into alcohol liquid from special-purpose monochloroethane reaction middle part, ethanol in hydrogenchloride and the alcohol in the hydrochloric acid, in liquor zinci chloridi katalysis and temperature at 120 ℃--react generation monochloroethane under 160 ℃; The monochloroethane that reaction generates and unreacted ethanol externally heat and reacts that formation monochloroethane gas mixture overflows liquor zinci chloridi from coming out from special-purpose monochloroethane reactor 1 top under the effect that generates heat in special-purpose monochloroethane reactor 1; The chemical water that the water that unreacted hydrochloric acid, raw material hydrochloric acid and alcohol are brought into, reaction generate, still be dissolved in small amounts of chlorine ethane and ethanol in the liquor zinci chloridi, heating evaporation is vaporized into sour water steam and overflows liquor zinci chloridi and leave special-purpose monochloroethane reactor 1 from special-purpose monochloroethane reactor 1 top again; Liquor zinci chloridi continues self-circulation; The monochloroethane gas mixture that comes out from special-purpose monochloroethane reactor 1, in condenser 2, carry out cooling condensation liquefaction by the water coolant indirect heat exchange, chromatographic separation again, lower floor's ethanol solution hydrochloride that pump (row) goes out chromatography returns special-purpose monochloroethane reactor 1 and recycles, chromatography goes out upper strata monochloroethane after sodium hydroxide solution is adjusted its pH value and reached 6.5--8.0, drains into monochloroethane work in-process storage tank 3; The sour water steam that comes out from special-purpose monochloroethane reactor 1, enter depickling dealcoholization device 7 after the decompression and carry out cooling condensation, concentration of hydrochloric acid after the depickling is lower than 1.0% water of condensation and directly sends into and enter sewage network after neutralization tank is handled, the dilute hydrochloric acid of concentration 18.0% or more that reclaims pumps in the special-purpose monochloroethane reactor 1 use or processes concentrate reuse more outward, and the alcohol of concentration more than 50% of recovery pumps into respectively in the special-purpose monochloroethane reactor 1 and re-uses; Work in-process monochloroethane pumps into monochloroethane rectifying tower 4 and carries out rectifying separation, cat head takes out the monochloroethane of monochloroethane content 99.5%--99.9%, enter in the water trap 5, carry out decompression dehydration, moisture pumps into monochloroethane storage tank 6 less than the monochloroethane of 200ppm, uses in the special-purpose monochloroethane reactor 1 of the high boiling material pumping of discharging at the bottom of the tower.
Concrete steps of the present utility model are as follows: technical solution is: use special-purpose monochloroethane reactor, substitute many reactors, realize equipment enlarging and control automatically, improve feed stock conversion; According to aqueous ethanolic solution at gas phase partial pressure difference under the differing temps different and hydrochloric acid gaseous phase partial pressure difference under differing temps, fractionation by distillation goes out most of ethanol in the reaction mixture gas body and hydrochloric acid and returns in the monochloroethane reactor and reuse respectively; Utilize under organic class material different concns such as monochloroethane and ethanol boiling point different, adopt distillation technology, rectifying separation goes out the monochloroethane that monochloroethane content conforms to quality requirements; Utilize water under differing temps in monochloroethane different solubility, rationally control the monochloroethane temperature, realize the monochloroethane dehydration, make it water content and meet the quality product requirement.
The above only is preferred embodiment of the present utility model; not in order to limit the utility model; all any modifications of within spirit of the present utility model and principle, doing, be equal to and replace and improvement etc., all should be included within the protection domain of the present utility model.
Claims (2)
1. a halocarbon metallization processes system for preparing monochloroethane is characterized in that, the halocarbon metallization processes system of described preparation monochloroethane comprises:
The monochloroethane reactor is for the preparation of monochloroethane;
Cooler condenser is connected with described monochloroethane reactor, is used for the monochloroethane cooling liquid that produces is handled;
Monochloroethane work in-process storage tank is connected with described cooler condenser, is used for storing cooled monochloroethane;
Rectifying tower is connected the monochloroethane rectifying separation that is used for described monochloroethane work in-process storage tank;
Water trap is connected with described rectifying tower, is used for the processed of monochloroethane;
The monochloroethane pan tank is connected with described water trap, is used for the storage of product monochloroethane;
Depickling degreasing tower is connected with described monochloroethane reactor, is used for the depickling skimming treatment of monochloroethane;
The sour water neutralizer with described depickling degreasing tower, is used for the neutralization operation of sour water.
2. the halocarbon metallization processes system of preparation monochloroethane as claimed in claim 1 is characterized in that, the halocarbon metallization processes system of described preparation monochloroethane adopts the special-purpose monochloroethane reactor of single cover to substitute many side-by-side reactions stills.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320026094 CN203222563U (en) | 2013-01-17 | 2013-01-17 | Halogen alkylation process system for preparing chloroethane |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320026094 CN203222563U (en) | 2013-01-17 | 2013-01-17 | Halogen alkylation process system for preparing chloroethane |
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| CN203222563U true CN203222563U (en) | 2013-10-02 |
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| CN 201320026094 Expired - Lifetime CN203222563U (en) | 2013-01-17 | 2013-01-17 | Halogen alkylation process system for preparing chloroethane |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103044188A (en) * | 2013-01-17 | 2013-04-17 | 江苏银珠化工集团有限公司 | Halide alkylation technique and halide alkylation system for preparation of chloroethane |
| CN104892351A (en) * | 2015-05-22 | 2015-09-09 | 连云港瑞威化工有限公司 | Separation method of high-purity chloroethane |
-
2013
- 2013-01-17 CN CN 201320026094 patent/CN203222563U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103044188A (en) * | 2013-01-17 | 2013-04-17 | 江苏银珠化工集团有限公司 | Halide alkylation technique and halide alkylation system for preparation of chloroethane |
| CN104892351A (en) * | 2015-05-22 | 2015-09-09 | 连云港瑞威化工有限公司 | Separation method of high-purity chloroethane |
| CN104892351B (en) * | 2015-05-22 | 2016-07-06 | 连云港瑞威化工有限公司 | A kind of separation method of high-purity chloro ethane |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: HONGZE JINLING SPICERY CO., LTD. Free format text: FORMER OWNER: JIANGSU YINZHU CHEMICAL GROUP CO., LTD. Effective date: 20150505 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20150505 Address after: 223100 No. 20 people's North Road, Hongze County, Jiangsu, Huaian Patentee after: HONGZE JINLING PERFUME Co.,Ltd. Address before: 223100 No. 20 people's North Road, Hongze County, Jiangsu, Huaian Patentee before: JIANGSU YINZHU CHEMICAL GROUP Co.,Ltd. |
|
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 223100 No. 20 people's North Road, Hongze County, Jiangsu, Huaian Patentee after: JIANGSU YINZHU GROUP HAIBAI TECHNOLOGY Co.,Ltd. Address before: 223100 No. 20 people's North Road, Hongze County, Jiangsu, Huaian Patentee before: HONGZE JINLING PERFUME Co.,Ltd. |
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| CX01 | Expiry of patent term |
Granted publication date: 20131002 |
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| CX01 | Expiry of patent term |