CN212864611U - Energy-saving and consumption-reducing ethyl acetate production line - Google Patents
Energy-saving and consumption-reducing ethyl acetate production line Download PDFInfo
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- CN212864611U CN212864611U CN202020956670.1U CN202020956670U CN212864611U CN 212864611 U CN212864611 U CN 212864611U CN 202020956670 U CN202020956670 U CN 202020956670U CN 212864611 U CN212864611 U CN 212864611U
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- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 title claims abstract description 57
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 21
- 150000002148 esters Chemical class 0.000 claims abstract description 70
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 43
- 238000009833 condensation Methods 0.000 claims abstract description 9
- 230000005494 condensation Effects 0.000 claims abstract description 9
- 238000004064 recycling Methods 0.000 claims abstract description 9
- 238000005886 esterification reaction Methods 0.000 claims description 27
- 230000032050 esterification Effects 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 26
- 239000002994 raw material Substances 0.000 claims description 26
- 238000011084 recovery Methods 0.000 claims description 22
- 238000004821 distillation Methods 0.000 claims description 6
- 239000000463 material Substances 0.000 abstract description 5
- 238000009776 industrial production Methods 0.000 abstract description 4
- 239000012071 phase Substances 0.000 abstract 5
- 239000008346 aqueous phase Substances 0.000 abstract 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 30
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 9
- 239000000047 product Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 3
- 230000001502 supplementing effect Effects 0.000 description 3
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- FMYHFHVAPZDDPJ-UHFFFAOYSA-N ethanol;ethyl acetate;hydrate Chemical class O.CCO.CCOC(C)=O FMYHFHVAPZDDPJ-UHFFFAOYSA-N 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
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Abstract
The utility model relates to an energy saving and consumption reduction ethyl acetate production line, the cauldron of esterifying is connected to a plurality of former feed tank feeds, the cauldron ejection of compact of esterifying connects the phase splitter through the condensation cooler, the ester of phase splitter connects to coarse ester dashpot mutually, the aqueous phase connects the technology water pitcher, coarse ester dashpot divides two the tunnel, the backward flow of the same kind connects back the cauldron of esterifying, another way connects the concentration tower, the concentration tower connects concentration phase splitting system, the aqueous phase of concentration phase splitting system connects the technology water pitcher, concentration phase splitting system ester connects back the concentration tower top mutually, concentration tower bottom divides two tunnel to connect the finished product metering tank respectively and connects any former feed tank or benefit ester groove through ejection of compact cooler. The device has compact structure, can effectively give consideration to material recycling while ensuring that the industrial production period can meet the requirements of production efficiency and purity.
Description
Technical Field
The utility model relates to a chemical production line, an energy saving and consumption reduction ethyl acetate production line specifically says so.
Background
The synthesis method mainly comprises four methods, namely an acetic acid esterification method, an acetaldehyde condensation method, an ethanol dehydrogenation method and an acetic acid/ethylene addition method. Among them, the acetic acid esterification method is the most common production method. The acetic acid esterification method adopts concentrated sulfuric acid as a catalyst, raw materials of acetic acid and ethanol are mixed and put into an esterification kettle for esterification, then a reaction product is evaporated out from the top of the esterification kettle in the form of an ethyl acetate-ethanol-water ternary azeotrope, and then is dehydrated and refined to obtain ethyl acetate, and materials of acetic acid with higher boiling point and the like 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 compact structure when guaranteeing that the industrial production cycle can satisfy production efficiency and purity requirement, can effectively compromise an energy saving and consumption reduction ethyl acetate production line that the material returned usefulness.
The utility model adopts the technical proposal that: an energy-saving consumption-reducing ethyl acetate production line comprises a plurality of raw material tanks, an esterification kettle, a condensation cooler, a phase splitter, a crude ester buffer tank, a concentration tower, a concentration phase splitting system, a discharge cooler, a finished product metering tank and a process water tank, wherein the raw material tanks are connected with the esterification kettle in a feeding mode, the discharge of the esterification kettle is connected with the phase splitter through the condensation cooler, the ester phase of the phase splitter is connected to the crude ester buffer tank, the water phase is connected with the process water tank, the crude ester buffer tank is divided into two paths, one path of backflow is connected back to the esterification kettle, the other path of backflow is connected with the concentration tower, the concentration tower is connected with the concentration phase splitting system, the water phase of the concentration phase splitting system is connected with the process water tank, the ester phase of the concentration phase splitting system is connected back to the top of the concentration tower, and the bottom of the concentration tower is respectively connected.
Further, the crude ester buffer tank is connected with a concentration tower through a preheater.
Furthermore, the concentration phase-splitting system comprises a head ester cooler, a head ester phase splitter, a head ester cooler connected to the top of the concentration tower, a head ester cooler connected to the head ester phase splitter, a process water tank connected to the water phase of the head ester phase splitter, and an ester phase returned to the top of the concentration tower.
Furthermore, the concentration phase-splitting system comprises a component cooler and a component phase splitter, wherein the middle part of the concentration tower is connected with the component phase splitter through the component cooler, the water phase of the component phase splitter is connected with a process water tank, and the ester phase is connected back to the top of the concentration tower.
Furthermore, the water phase of each phase separator is connected with a process water tank after passing through a recovery kettle.
Furthermore, the water phase of each phase separator is connected with a process water tank after passing through a recovery kettle.
Furthermore, the rear part of the recovery kettle is divided into two paths, one path is connected with the process water tank, and the other path is connected with the drain pipe.
Furthermore, the recovery kettle is a distillation recovery kettle, and the top of the distillation recovery kettle is connected with any raw material tank or a head ester recycling tank.
Raw materials of acetic acid, alcohol and sulfuric acid are metered in a plurality of raw material tanks and put into an esterification kettle, the raw materials are heated by steam to generate ethyl acetate and water, an azeotrope is formed in the esterification tower, the ethyl acetate and the water are evaporated from the top of the tower, the ethyl acetate, the alcohol and the water are cooled by a condensing cooler and then enter a phase separator for separation, a water phase enters a recovery kettle to recover the dissolved ester and the dissolved alcohol, an ester phase is sent into a crude ester buffer tank, a part of the ester phase reflows to the esterification tower, the other part of the ester phase is preheated by a preheater and then enters a concentration tower, the head ester of the mixture of the alcohol, the water and the ester is separated from the components at the top of the tower by rectification, the ester phase reflows to the concentration tower after sequentially passing through the head ester cooler and the head ester phase separator, the water phase is sent to the recovery kettle, the ester phase returns to the concentration tower again, a part of the components in the concentration tower is returned to the ester tank after passing through the discharging cooler for supplying to the esterification kettle, the remainder all enter the metering tank.
The wastewater containing ester and alcohol enters a recovery kettle, is subjected to distillation separation, is recovered from the tower top to obtain a certain content of head ester, is sent to a head ester tank raw material tank for supplying to an esterification kettle, part of the recovered wastewater is sent to a process water tank for standby use as process water, and the rest water is drained from the tower bottom through a drain pipe.
The utility model discloses with the tradition once cool off, the phase splitting returns the institutional advancement that utilizes and returns for concentrating first ester, component phase splitting returns many times, concentration reaches the cooling collection or the part returns the utilization after requiring in the concentrating tower, when can ensure that the industrial production cycle satisfies production efficiency and purity requirement, compromises the material and returns the usefulness, is favorable to reduction in production cost.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: alcohol raw material tank 1, acetic acid raw material tank 2, sulfuric acid raw material tank 3, ester supplementing raw material tank 4, head ester recycling tank 5, esterification kettle 6, condensation cooler 7, phase separator 8, crude ester buffer tank 9, preheater 10, concentration tower 11, head ester cooler 12, head ester phase separator 13, component cooler 14, component phase separator 15, discharge cooler 16, finished product metering tank 17, recovery kettle 18, process water tank 19 and drain pipe 20.
Detailed Description
The following further description is made in conjunction with the accompanying drawings and examples.
FIG. 1 shows: an energy-saving consumption-reducing ethyl acetate production line comprises an alcohol raw material tank 1, an acetic acid raw material tank 2, a sulfuric acid raw material tank 3, an ester supplementing raw material tank 4, a head ester recycling tank 5, an esterification kettle 6, a condensation cooler 7, a phase separator 8, a crude ester buffer tank 9, a preheater 10, a concentration tower 11, a head ester cooler 12, a head ester phase separator 13, a component cooler 14, a component phase separator 15, a discharge cooler 16, a finished product metering tank 17, a recovery kettle 18, a process water tank 19 and a drain pipe 20.
An alcohol raw material tank 1, an acetic acid raw material tank 2, a sulfuric acid raw material tank 3, the esterification reaction system comprises an ester supplementing raw material tank 4, a head ester recycling tank 5, an esterification kettle 6, a condensation cooler 7, a phase separator 8, a crude ester buffer tank 9, a water phase recovery kettle 18, a crude ester buffer tank 9, a pre-heater 10, a concentration tower 11, a component cooler 12, a head ester cooler, an ester separator 13, a water phase recovery kettle 18, an ester phase recovery tower 11, a component cooler 14, a component separator 15, a water phase recovery kettle 18, a water drainage pipe 20 and a recycling kettle 18, wherein the esterification kettle 6 is connected with the top of the recycling kettle 5; the bottom of the concentration tower 11 is respectively connected with a finished product metering tank 17 and an ester supplement raw material tank 4 in two paths through a discharge cooler 16.
In this embodiment, the recovery kettle is a distillation 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 (8)
1. An energy-saving consumption-reducing ethyl acetate production line is characterized by comprising a plurality of raw material tanks, an esterification kettle, a condensation cooler, a phase splitter, a crude ester buffer tank, a concentration tower, a concentration phase splitting system, a discharge cooler, a finished product metering tank and a process water tank, wherein the raw material tanks are connected with the esterification kettle in a feeding mode, the discharge of the esterification kettle is connected with the phase splitter through the condensation cooler, the ester phase of the phase splitter is connected to the crude ester buffer tank, the water phase of the phase splitter is connected with the process water tank, the crude ester buffer tank is divided into two paths, one path of the two paths of the crude ester buffer tank is connected back to the esterification kettle, the other path of the two paths of the crude ester buffer tank is connected to the concentration tower, the concentration tower is connected with the concentration phase splitting system.
2. The production line of ethyl acetate with energy saving and consumption reduction as claimed in claim 1, which is characterized in that: the crude ester buffer tank is connected with a concentration tower through a preheater.
3. The production line of ethyl acetate with energy saving and consumption reduction as claimed in claim 1, which is characterized in that: the concentration phase-splitting system comprises a head ester cooler, a head ester phase splitter, a head ester cooler connected to the top of the concentration tower, a head ester cooler connected to the head ester phase splitter, a process water tank connected to the water phase of the head ester phase splitter, and an ester phase returned to the top of the concentration tower.
4. The production line of ethyl acetate with energy saving and consumption reduction as claimed in claim 1 or 3, which is characterized in that: the concentration phase-splitting system comprises a component cooler and a component phase splitter, wherein the middle part of the concentration tower is connected with the component phase splitter through the component cooler, the water phase of the component phase splitter is connected with a process water tank, and the ester phase is connected back to the top of the concentration tower.
5. The production line of ethyl acetate with energy saving and consumption reduction as claimed in claim 1, which is characterized in that: the water phase of each phase separator is connected with a process water tank after passing through a recovery kettle.
6. The production line of ethyl acetate with energy saving and consumption reduction as claimed in claim 4, which is characterized in that: the water phase of each phase separator is connected with a process water tank after passing through a recovery kettle.
7. The production line of ethyl acetate with energy saving and consumption reduction as claimed in claim 5 or 6, which is characterized in that: the recycling kettle is divided into two paths, one path is connected with the process water tank, and the other path is connected with the drain pipe.
8. The production line of ethyl acetate with energy saving and consumption reduction as claimed in claim 5 or 6, which is characterized in that: the recovery kettle is a distillation recovery kettle, and the top of the distillation recovery kettle is connected with any raw material tank or a head ester recycling tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020956670.1U CN212864611U (en) | 2020-05-31 | 2020-05-31 | Energy-saving and consumption-reducing ethyl acetate production line |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020956670.1U CN212864611U (en) | 2020-05-31 | 2020-05-31 | Energy-saving and consumption-reducing ethyl acetate production line |
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| CN212864611U true CN212864611U (en) | 2021-04-02 |
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| CN202020956670.1U Expired - Fee Related CN212864611U (en) | 2020-05-31 | 2020-05-31 | Energy-saving and consumption-reducing ethyl acetate production line |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113620804A (en) * | 2021-09-13 | 2021-11-09 | 盐城市春竹香料有限公司 | Continuous esterification process and device for ethyl 2-methylbutyrate |
| CN113717051A (en) * | 2021-09-16 | 2021-11-30 | 泰兴金江化学工业有限公司 | Preparation method of butyl acetate |
| CN113880712A (en) * | 2021-09-16 | 2022-01-04 | 泰兴金江化学工业有限公司 | Preparation method of ethyl acetate |
-
2020
- 2020-05-31 CN CN202020956670.1U patent/CN212864611U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113620804A (en) * | 2021-09-13 | 2021-11-09 | 盐城市春竹香料有限公司 | Continuous esterification process and device for ethyl 2-methylbutyrate |
| CN113717051A (en) * | 2021-09-16 | 2021-11-30 | 泰兴金江化学工业有限公司 | Preparation method of butyl acetate |
| CN113880712A (en) * | 2021-09-16 | 2022-01-04 | 泰兴金江化学工业有限公司 | Preparation method of ethyl acetate |
| CN113880712B (en) * | 2021-09-16 | 2023-08-04 | 泰兴金江化学工业有限公司 | Preparation method of ethyl acetate |
| CN113717051B (en) * | 2021-09-16 | 2023-08-04 | 泰兴金江化学工业有限公司 | Preparation method of butyl acetate |
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| CF01 | Termination of patent right due to non-payment of annual fee |
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| CF01 | Termination of patent right due to non-payment of annual fee |