CN212864610U - Integrative waste water waste residue comprehensive utilization production system of butyl acrylate - Google Patents
Integrative waste water waste residue comprehensive utilization production system of butyl acrylate Download PDFInfo
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- CN212864610U CN212864610U CN202020956701.3U CN202020956701U CN212864610U CN 212864610 U CN212864610 U CN 212864610U CN 202020956701 U CN202020956701 U CN 202020956701U CN 212864610 U CN212864610 U CN 212864610U
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- tower
- tank
- condenser
- light component
- dehydration
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- CQEYYJKEWSMYFG-UHFFFAOYSA-N butyl acrylate Chemical compound CCCCOC(=O)C=C CQEYYJKEWSMYFG-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 239000002351 wastewater Substances 0.000 title claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- 239000002699 waste material Substances 0.000 title claims abstract description 13
- 238000011084 recovery Methods 0.000 claims abstract description 52
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 43
- 230000018044 dehydration Effects 0.000 claims abstract description 40
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 40
- 239000002994 raw material Substances 0.000 claims abstract description 40
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 31
- 238000005886 esterification reaction Methods 0.000 claims abstract description 25
- 238000007670 refining Methods 0.000 claims abstract description 22
- 230000032050 esterification Effects 0.000 claims abstract description 21
- 150000002148 esters Chemical class 0.000 claims abstract description 20
- 238000000605 extraction Methods 0.000 claims abstract description 19
- 238000005406 washing Methods 0.000 claims abstract description 18
- 239000003054 catalyst Substances 0.000 claims abstract description 15
- 238000000034 method Methods 0.000 claims abstract description 15
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000004065 wastewater treatment Methods 0.000 claims description 5
- 239000000463 material Substances 0.000 abstract description 6
- 238000009776 industrial production Methods 0.000 abstract description 5
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 14
- 239000000047 product Substances 0.000 description 13
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 7
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 7
- 238000001704 evaporation Methods 0.000 description 7
- 230000008020 evaporation Effects 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- -1 acrylic ester Chemical class 0.000 description 3
- AFVFQIVMOAPDHO-UHFFFAOYSA-N Methanesulfonic acid Chemical compound CS(O)(=O)=O AFVFQIVMOAPDHO-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- JOXIMZWYDAKGHI-UHFFFAOYSA-N toluene-4-sulfonic acid Chemical compound CC1=CC=C(S(O)(=O)=O)C=C1 JOXIMZWYDAKGHI-UHFFFAOYSA-N 0.000 description 2
- 239000003377 acid catalyst Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 229940098779 methanesulfonic acid Drugs 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a butyl acrylate integrative waste water waste residue comprehensive utilization production system, the upper part of an esterification reactor is connected with the lower part of a dehydration tower, the upper part of the dehydration tower is connected with a dehydration tower condenser, the dehydration tower condenser is connected with a dehydration tower liquid receiving groove, the dehydration tower liquid receiving groove is connected with the upper part of the dehydration tower in an ester phase return mode, and the dehydration tower is connected with a process water tank by liquid tank water; the lower part of the esterification reactor is connected with an extraction tower, the water phase of the extraction tower is connected with a catalyst raw material tank, the ester phase of the extraction tower is connected with a washing tower, the water phase of the washing tower is connected with an alcohol recovery tower, the ester phase is connected with a light component removal tower, the top of the light component removal tower is connected with a light component removal condenser, the light component removal condenser is divided into two paths, one path returns to the raw material tank, the other path returns to the upper part of the light component removal tower, the lower part of the light component removal tower is connected with the lower part of a refining tower, the top of the refining tower is connected with a finished product tank, the bottom of the refining tower is connected with an evaporator. The material is reused, the cost is reduced, the wastewater discharge is reduced, and the requirements of industrial production efficiency and purity can be met.
Description
Technical Field
The utility model relates to a chemical production system, an integrative waste water waste residue comprehensive utilization production system of butyl acrylate specifically says so.
Background
Butyl acrylate is an important organic solvent and chemical basic raw material, the current industrial production synthesis method mainly adopts acrylic acid and n-butyl alcohol to mix and put into an esterification kettle for esterification, then a reaction product is evaporated out from the top of the esterification kettle in an azeotrope form, and then dehydration and refining are carried out to obtain the butyl acrylate, and materials with higher boiling point and intermediate products brought out from the esterification kettle are refluxed into the esterification kettle from the bottom of the esterification kettle for continuous reaction. But the simple material returns for continuous reaction, wherein the content of the raw material substance is relatively low, and the raw material substance is directly returned for use, so that the industrial production period is increased, and the improvement of the production efficiency and the improvement of the purity are not facilitated.
Disclosure of Invention
The utility model provides a simple structure, compactness, the material returns usefulness, and reduction in production cost reduces wastewater discharge, can compromise the integrative waste water waste residue comprehensive utilization production system of butyl acrylate of industrial production efficiency and purity requirement.
The utility model adopts the technical proposal that: the utility model provides an integrative waste water waste residue of butyl acrylate comprehensive utilization production system, includes raw material tank, the former groove of catalyst, esterification reaction ware, and raw material tank, the former groove of catalyst connect esterification reaction ware upper portion, its characterized in that: the upper part of the esterification reactor is connected with the lower part of the dehydration tower, the upper part of the dehydration tower is connected with a condenser of the dehydration tower, the condenser of the dehydration tower is connected with a liquid receiving tank of the dehydration tower, the ester phase of the liquid receiving tank of the dehydration tower is returned to the upper part of the dehydration tower, and the water of the liquid receiving tank of the dehydration tower is connected with a process water tank; the lower part of the esterification reactor is connected with an extraction tower, the water phase of the extraction tower is connected with a catalyst raw material tank, the ester phase of the extraction tower is connected with a washing tower, the water phase of the washing tower is connected with an alcohol recovery tower, the ester phase of the washing tower is connected with a light component removal tower, the top of the light component removal tower is connected with a light component removal condenser, the light component removal condenser is divided into two paths and returns to the raw material tank, the other path returns to the upper part of the light component removal tower, the lower part of the light component removal tower is connected with the lower part of a refining tower, the top of the refining tower is connected with a finished product tank, the bottom of the refining tower is connected with an evaporator, the top.
Furthermore, the process water tank is connected with the middle part of the alcohol recovery tower through a pump, the top part of the alcohol recovery tower is connected with an alcohol recovery condenser, the alcohol recovery condenser is connected with an alcohol recovery liquid receiving tank, the alcohol recovery liquid receiving tank is connected with the process water tank in a water connection mode, and the ester phase of the extraction tower are connected with the washing tower together.
Further, the residue tank is connected with a heavy component recovery kettle, the heavy component recovery kettle is a steam heating kettle, the top of the heavy component recovery kettle is connected with a raw material tank in a gas-phase mode, and the bottom of the heavy component recovery kettle is connected with an incinerator.
Further, the evaporator is a flash evaporator.
Furthermore, the top of the refining tower is connected with a finished product condenser, and the finished product condenser is connected with a finished product tank.
Further, the bottom of the alcohol recovery tower is connected with a wastewater treatment unit.
Raw materials in an acrylic acid raw material tank, an n-butyl alcohol raw material tank, p-toluenesulfonic acid and a methanesulfonic acid catalyst raw material tank are fed into an esterification reactor according to a proportion, and are reacted under a steam heating condition. Part of water, n-butyl acrylate and raw material alcohol enter the bottom of a dehydration tower in an azeotrope gas phase form, are evaporated from the top of the tower, enter a dehydrating tower liquid receiving tank after being condensed by a dehydrating tower condenser, enter a process water tank from the dehydrating tower liquid receiving tank, and return an upper layer ester phase material to the top of the dehydrating tower to be added for countercurrent contact. The reaction liquid at the bottom of the esterification reactor is sent to an extraction tower, unreacted catalyst is extracted into a water phase and returned to a catalyst raw material tank, an upper ester phase enters a washing tower, the unextracted acid catalyst, unreacted acrylic acid and the like are completely neutralized, the neutralized ester is sent to a light component removal tower, and the water phase enters an alcohol recovery tower. Crude acrylic ester enters a light component removal tower, after rectification separation, butanol, water and part of acrylic ester are evaporated from the top of the light component removal tower, after condensation of a light component removal condenser, part of the butyl acrylate and part of the acrylic ester are returned to an esterification reactor or a raw material tank in an esterification working section for continuous use, the tower bottom liquid of the light component removal tower is n-butyl acrylate and some high-boiling-point substances and is sent to the bottom of a refining tower, n-butyl acrylate is distilled from the top of the refining tower and is collected by a finished product condenser through a finished product tank to obtain a finished n-butyl acrylate product, the tower bottom liquid of the refining tower is sent to an evaporator for flash evaporation, the n-butyl acrylate evaporated from the top of the evaporator is condensed by an evaporation condenser and then returns to the refining tower, and the. Sending residual liquid at the bottom of the evaporator, acrylic acid and a catalyst collected in the residue tank into a heavy component recovery kettle, reacting under the steam heating condition, returning generated gas-phase substances to a raw material tank for recycling, enriching the residual liquid which cannot react in the heavy component recovery kettle to certain viscosity and concentration, discharging, and sending to an incineration unit for treatment.
The waste water from the process water tank is added from the middle part of the alcohol recovery tower, the azeotrope containing alcohol, n-butyl acrylate and water is distilled from the top of the alcohol recovery tower, condensed by an alcohol recovery condenser and then enters an alcohol recovery liquid receiving tank for layering, the upper ester phase is sent to a washing tower, and the water phase enters the process water tank. And discharging the tower bottom liquid of the alcohol recovery tower to a wastewater treatment unit, and sending the wastewater to a sewage treatment station for treatment after the wastewater reaches the standard through biochemical treatment.
The utility model discloses with the tradition once cool off, the phase splitting returns the institutional advancement that utilizes and returns for the component is hierarchical, the phase splitting is a lot of, loops through extraction, play the butterfly, take off after the light component refined concentration reach the requirement after the cooling collect or the part returns the utilization, when can ensure that the industrial production cycle satisfies production efficiency and purity requirement, compromise the material and return the usefulness, be favorable to reduction in production cost.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: acrylic acid raw material tank 1, n-butanol raw material tank 2, alcohol return raw material tank 3, catalyst raw material tank 4, esterification reactor 5, dehydration tower 6, dehydration tower condenser 7, dehydration tower liquid receiving tank 8, process water tank 9, extraction tower 10, washing tower 11, alcohol recovery tower 12, alcohol recovery condenser 13, alcohol recovery liquid receiving tank 14, light component removal tower 15, light component removal condenser 16, refining tower 17, finished product condenser 18, finished product tank 19, flash evaporator 20, evaporation condenser 21, residue tank 22, heavy component recovery tank 23, incinerator 24, liquid return raw material tank 25 and wastewater treatment unit 26.
Detailed Description
The present invention will be further explained with reference to the drawings and examples.
FIG. 1 shows: the production system for comprehensively utilizing butyl acrylate integrated wastewater and waste residues comprises an acrylic acid raw material tank 1, an n-butanol raw material tank 2, an alcohol return raw material tank 3, a catalyst raw material tank 4, an esterification reactor 5, a dehydration tower 6, a dehydration tower condenser 7, a dehydration tower liquid-receiving tank 8, a process water tank 9, an extraction tower 10, a washing tower 11, an alcohol recovery tower 12, an alcohol recovery condenser 13, an alcohol recovery liquid-receiving tank 14, a light component removal tower 15, a light component removal condenser 16, a refining tower 17, a finished product condenser 18, a finished product tank 19, a flash evaporation evaporator 20, an evaporation condenser 21, a residue tank 22, a heavy component recovery tank 23, an incinerator 24, a liquid return raw material tank 25 and a wastewater treatment unit 26.
The acrylic acid raw material tank 1, the n-butanol raw material tank 2, the alcohol return raw material tank 3, the catalyst raw material tank 4 and the liquid return raw material tank 25 are all connected to an esterification reactor 5, the upper part of the esterification reactor 5 is connected to the lower part of a dehydration tower 6, the upper part of the dehydration tower 6 is connected to a dehydration tower condenser 7, the dehydration tower condenser is connected to a dehydration tower liquid receiving tank 8, the dehydration tower liquid receiving tank is connected to the upper part of the dehydration tower in an ester phase return mode, and the dehydration tower liquid receiving tank is connected to a process water tank 9; the lower part of an esterification reactor 5 is connected with an extraction tower 10, the water of the extraction tower 10 is connected with a catalyst raw material tank 4, the ester of the extraction tower 10 is connected with a washing tower 11, the water of the washing tower 11 is connected with an alcohol recovery tower 12, a process water tank 9 is connected with the middle part of the alcohol recovery tower 12 through a pump, the top of the alcohol recovery tower 12 is connected with an alcohol recovery condenser 13, the alcohol recovery condenser 13 is connected with an alcohol recovery liquid receiving tank 14, the alcohol recovery liquid receiving tank 14 is connected with the process water tank 9, the ester and the ester of the extraction tower are connected with the washing tower 11 together, and the bottom of the alcohol recovery; the ester phase of a washing tower 11 is connected with a light component removal tower 15, the top of the light component removal tower 15 is connected with a light component removal condenser 16, the light component removal condenser 16 is divided into two paths, one path returns to an alcohol raw material tank 3, the other path returns to the upper part of the light component removal tower, the lower part of the light component removal tower 16 is connected with the lower part of a refining tower 17, the top of the refining tower 17 is connected with a finished product tank 19 through a finished product tank 18, the bottom of the refining tower 17 is connected with a flash evaporator 20, the top of the flash evaporator is connected with an evaporation condenser 21, the evaporation condenser is connected with the upper part of the refining tower, the bottom of the evaporator is connected with a residue tank 22, the residue tank is connected with a heavy component recovery kettle 23, the heavy component recovery kettle is a steam heating kettle, the top of the heavy component recovery kettle.
In the above embodiments, the chemical vessels such as the kettles, the tanks, the phase separators, and the towers are connected with a uniform channel pipeline, and the pipeline is provided with flow, valve control, and the like.
Claims (6)
1. The utility model provides an integrative waste water waste residue of butyl acrylate comprehensive utilization production system, includes raw material tank, the former groove of catalyst, esterification reaction ware, and raw material tank, the former groove of catalyst connect esterification reaction ware upper portion, its characterized in that: the upper part of the esterification reactor is connected with the lower part of the dehydration tower, the upper part of the dehydration tower is connected with a condenser of the dehydration tower, the condenser of the dehydration tower is connected with a liquid receiving tank of the dehydration tower, the ester phase of the liquid receiving tank of the dehydration tower is returned to the upper part of the dehydration tower, and the water of the liquid receiving tank of the dehydration tower is connected with a process water tank; the lower part of the esterification reactor is connected with an extraction tower, the water phase of the extraction tower is connected with a catalyst raw material tank, the ester phase of the extraction tower is connected with a washing tower, the water phase of the washing tower is connected with an alcohol recovery tower, the ester phase of the washing tower is connected with a light component removal tower, the top of the light component removal tower is connected with a light component removal condenser, the light component removal condenser is divided into two paths and returns to the raw material tank, the other path returns to the upper part of the light component removal tower, the lower part of the light component removal tower is connected with the lower part of a refining tower, the top of the refining tower is connected with a finished product tank, the bottom of the refining tower is connected with an evaporator, the top.
2. The butyl acrylate integrated wastewater and waste residue comprehensive utilization production system as claimed in claim 1, which is characterized in that: the process water tank is connected with the middle part of the alcohol recovery tower through a pump, the top part of the alcohol recovery tower is connected with an alcohol recovery condenser, the alcohol recovery condenser is connected with an alcohol recovery liquid receiving tank, the alcohol recovery liquid receiving tank is connected with the process water tank through water, and the ester phase of the extraction tower are connected with the washing tower together.
3. The butyl acrylate integrated wastewater and waste residue comprehensive utilization production system as claimed in claim 1, which is characterized in that: the residue tank is connected with a heavy component recovery kettle, the heavy component recovery kettle is a steam heating kettle, the top gas of the heavy component recovery kettle is connected with a raw material tank, and the bottom of the heavy component recovery kettle is connected with an incinerator.
4. The butyl acrylate integrated wastewater and waste residue comprehensive utilization production system as claimed in claim 1, which is characterized in that: the evaporator is a flash evaporator.
5. The butyl acrylate integrated wastewater and waste residue comprehensive utilization production system as claimed in claim 1, which is characterized in that: the top of the refining tower is connected with a finished product condenser, and the finished product condenser is connected with a finished product tank.
6. The butyl acrylate integrated wastewater and waste residue comprehensive utilization production system as claimed in claim 1, which is characterized in that: the bottom of the alcohol recovery tower is connected with a wastewater treatment unit.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020956701.3U CN212864610U (en) | 2020-05-31 | 2020-05-31 | Integrative waste water waste residue comprehensive utilization production system of butyl acrylate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020956701.3U CN212864610U (en) | 2020-05-31 | 2020-05-31 | Integrative waste water waste residue comprehensive utilization production system of butyl acrylate |
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| CN212864610U true CN212864610U (en) | 2021-04-02 |
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| CN202020956701.3U Expired - Fee Related CN212864610U (en) | 2020-05-31 | 2020-05-31 | Integrative waste water waste residue comprehensive utilization production system of butyl acrylate |
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| Country | Link |
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| CN (1) | CN212864610U (en) |
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- 2020-05-31 CN CN202020956701.3U patent/CN212864610U/en not_active Expired - Fee Related
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| GR01 | Patent grant | ||
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20210402 |