CN219072545U - HCl recovery system for trimethyl orthoacetate - Google Patents
HCl recovery system for trimethyl orthoacetate Download PDFInfo
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- CN219072545U CN219072545U CN202223497476.XU CN202223497476U CN219072545U CN 219072545 U CN219072545 U CN 219072545U CN 202223497476 U CN202223497476 U CN 202223497476U CN 219072545 U CN219072545 U CN 219072545U
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- trimethyl orthoacetate
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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Abstract
The utility model relates to the field of recovery equipment, in particular to an HCl recovery system for trimethyl orthoacetate, which comprises a compressor, wherein the compressor is connected with a heat exchanger, the heat exchanger is connected with a permeation gasification unit, and the permeation gasification unit is connected with an absorption tower; the utility model discloses an HCl recovery system for trimethyl orthoacetate, which can realize the recovery and utilization of HCl for trimethyl orthoacetate, has simple process and low operation cost, and can remarkably reduce the production cost, wherein the HCl recovery rate is more than 99.5%.
Description
Technical Field
The utility model relates to the field of recovery equipment, in particular to an HCl recovery system for trimethyl orthoacetate.
Background
Trimethyl orthoacetate, also known as 1, 1-trimethoxyethane, has a structural formula of CH3C (OCH 3) 3, is insoluble in water, and can be dissolved in organic solvents such as ethanol, diethyl ether and the like. The orthoester is an important orthoester, is mainly used as an organic intermediate for synthesizing medicines and pesticides, can be used for synthesizing pyrethrin pesticides such as cypermethrin and cyhalothrin, medicaments such as sulfadiazine and the like, and can also be used as raw materials for producing dyes, fragrances, food additives and the like.
The main method for synthesizing trimethyl orthoacetate is as follows: acetonitrile, methanol and dry hydrogen chloride are used as raw materials, and in the presence of a nonpolar solvent, the raw materials are subjected to salification reaction to prepare ethylimine methyl ether hydrochloride, and then subjected to alcoholysis reaction to prepare trimethyl orthoacetate.
The HCl required for the reaction is prepared from 30% hydrochloric acid through deep resolution, condensation, defogging, dehydration and drying.
The waste gas (HCl and organic gas) is released in the preparation and salification processes of the dry HCl, and the common treatment method is that the waste gas is burnt by an alkaline washing-water washing-RTO furnace, so that the treatment capacity of alkali liquor is increased, and the waste of HCl resources is caused.
HCl is one of the important raw materials in trimethyl orthoacetate production, and recovery of the HCl-containing tail gas released is an effective means of cost reduction.
The structure of the existing recovery equipment for the tail gas of HCl is complex, for example, patent 201310539240.4-a tail gas HCl recovery system and technology has large investment and use cost in actual use, so that in order to reduce the recovery cost of the tail gas of HCl, the existing recovery equipment needs to be optimally designed.
Disclosure of Invention
The utility model aims to provide an HCl recovery system with a simple structure and low input cost.
In order to achieve the above purpose, the technical scheme adopted by the utility model is as follows:
the HCl recovery system for trimethyl orthoacetate comprises a compressor, wherein the compressor is connected with a heat exchanger, the heat exchanger is connected with an infiltration gasification unit, and the infiltration gasification unit is connected with an absorption tower; the compressor is connected with the air inlet pipeline, the compressor is connected with the heat exchanger through the first pipeline, and the heat exchanger is connected with the infiltration gasification unit through the second pipeline; the infiltration gasification unit is connected with the absorption tower through a third pipeline.
The infiltration gasification unit is connected with a heater.
The infiltration gasification unit comprises a plurality of monomer modules, and adjacent monomer modules are arranged in series or in parallel; adjacent monomer modules are connected through a communicating pipeline; the communication pipe is disposed through the heater.
The infiltration gasification unit is connected with a residual air pipeline, and the residual air pipeline passes through the heat exchanger to be arranged.
The absorption tower is connected with a hydrochloric acid storage tank; the absorption tower is communicated with the hydrochloric acid storage tank through an external pipeline.
The hydrochloric acid storage tank is connected with the absorption tower through a circulating pipeline; one end of the circulating pipeline is connected with the hydrochloric acid storage tank, and the other end of the circulating pipeline is connected with the absorption tower; the circulating pipeline and the external pipeline are distributed at two ends of the absorption tower.
And the circulating pipeline is connected with a supply pipeline.
And control valves are arranged on the circulating pipeline, the external pipeline and the supply pipeline.
The absorption tower is externally connected with a vacuum pump.
The absorption tower is a spray tower or a packed tower.
The utility model has the advantages that:
the utility model discloses an HCl recovery system for trimethyl orthoacetate, which can realize the recovery and utilization of HCl for trimethyl orthoacetate, has simple process and low operation cost, and can remarkably reduce the production cost, wherein the HCl recovery rate is more than 99.5%.
Drawings
The contents of the drawings and the marks in the drawings of the present specification are briefly described as follows:
fig. 1 is a schematic structural view of the present utility model.
The labels in the above figures are:
1. the device comprises a compressor, 2, a heat exchanger, 3, a heater, 4, an infiltration gasification unit, 5, an absorption tower, 6, a vacuum pump, 7 and a hydrochloric acid storage tank.
Detailed Description
The following detailed description of the utility model refers to the accompanying drawings, which illustrate preferred embodiments of the utility model in further detail.
The HCl recovery system for trimethyl orthoacetate comprises a compressor 1, wherein the compressor 1 is connected with a heat exchanger 2, the heat exchanger 2 is connected with an infiltration gasification unit 4, and the infiltration gasification unit 4 is connected with an absorption tower 5; the compressor 1 is connected with an air inlet pipeline, the compressor 1 is connected with the heat exchanger 2 through a first pipeline 11, and the heat exchanger 2 is connected with the infiltration gasification unit 4 through a second pipeline 12; the infiltration gasification unit 4 is connected with the absorption tower 5 through a third pipeline 13; the utility model discloses an HCl recovery system for trimethyl orthoacetate, which can realize the recovery and utilization of HCl for trimethyl orthoacetate, has simple process and low operation cost, and can remarkably reduce the production cost, wherein the HCl recovery rate is more than 99.5%.
Specifically, the HCl recovery system disclosed by the utility model mainly comprises a compressor 1, wherein the compressor 1 is externally connected with an air supply pipeline, and the air supply pipeline is arranged, so that the compressor 1 is convenient to convey tail gas containing HCl and organic gas to subsequent parts for separation and recovery; in addition, the compressor 1 is connected with the heat exchanger 2, the heat exchanger 2 is convenient for heating tail gas, energy required to be consumed by the subsequent heater 3 is reduced, HCl gas is convenient to volatilize, and the heat exchanger 2 is connected with the infiltration gasification unit 4; the pervaporation unit 4 is in fact an existing structure, the specific structure of which is not set forth here; the volatilization of HCl gas is realized, and meanwhile, the overflow of organic gas is blocked, so that the separation of the HCl gas and the organic gas is realized; the separated HCl gas enters an absorption tower 5 for countercurrent or concurrent absorption to obtain hydrochloric acid absorption liquid.
Further, in the present utility model, the infiltration gasification unit 4 is connected with a heater 3; the heater 3 can heat by tail gas, which is convenient for the overflow of HCl gas.
Furthermore, in the present utility model, the infiltration gasification unit 4 includes a plurality of monomer modules 41, and the monomer modules 41 are equivalent to a pipeline structure, so that HCl gas in the tail gas is convenient to overflow, and organic gas is avoided from overflowing; then the tail gas is separated; meanwhile, it is required in the present utility model that the adjacent monomer modules 41 are arranged in series or in parallel; by the arrangement, the movement path of the tail gas is increased, the separation of the tail gas is optimized, and then the recycling of the actual HCl gas is also facilitated, and meanwhile, the adjacent monomer modules 41 are connected through the communication pipeline 411; the communication duct 411 is disposed through the heater 3; the arrangement of the heater 3 can heat the tail gas in the communicating pipeline 411, so that the collection of HCl gas is better realized.
Further, in the present utility model, a residual gas pipe 17 is connected to the pervaporation unit 4, and the residual gas pipe 17 is disposed through the heat exchanger 2; the residual gas pipeline 17 discharges the organic gas which is not volatilized in the infiltration gasification unit 4; meanwhile, the residual air pipeline 17 passes through the heat exchanger 2 to heat the organic gas, so that the organic gas can conveniently enter an exhaust gas treatment process.
Further, in the present utility model, the absorption tower 5 is connected with a hydrochloric acid storage tank 7; the absorption tower 5 is communicated with the hydrochloric acid storage tank 7 through an external pipeline 14; the hydrochloric acid storage tank 7 is arranged, so that the hydrochloric acid absorption liquid in the absorption tower 5 can conveniently enter the hydrochloric acid storage tank 7.
In addition, in the present utility model, the hydrochloric acid tank 7 is connected to the absorption tower 5 through a circulation pipe 16; one end of the circulating pipeline 16 is connected with the hydrochloric acid storage tank 7, and the other end of the circulating pipeline is connected with the absorption tower 5; the circulating pipeline 16 and the external pipeline 14 are distributed at two ends of the absorption tower 5; the circulation pipeline 16 is arranged, so that the hydrochloric acid absorption liquid in the hydrochloric acid storage tank 7 continuously flows through the absorption tower 5, and then the concentration of hydrochloric acid in the hydrochloric acid absorption liquid is increased.
Further, in the present utility model, a supply line 18 is connected to the circulation line 16; the supply pipeline 18 is arranged, so that water or high-concentration HCl solution can be conveniently supplied from the supply pipeline 18 to the circulating pipeline 16 according to the requirement in the subsequent use; so that the hydrochloric acid absorption liquid in the absorption tower 5 can reach a set value rapidly; the hydrochloric acid storage tank 7 can realize that the hydrochloric acid absorption liquid reaching the set value enters the hydrochloric acid batching area of another process through an outer discharge pipeline.
Of course, in actual implementation, no supply line may be provided.
Further, in the present utility model, the circulation pipe 16, the external pipe 14 and the supply pipe 18 are provided with control valves 15; the control valve 15 is arranged, so that the on-off of the circulating pipeline 16, the external pipeline 14 and the supply pipeline 18 is conveniently controlled; the normal use of the whole recovery system is ensured.
Further, in the utility model, the absorption tower 5 is externally connected with a vacuum pump 6; setting a vacuum pump 6; the vacuum is formed in the absorption tower 5, and the flanging water is recycled conveniently; in addition, the absorption tower 5 is a spray tower or a packed tower in the present utility model; the gas and the liquid can be contacted in countercurrent or in parallel and are connected with a vacuum pump 6.
Specifically:
the HCl recovery system disclosed by the utility model comprises a compressor 1, wherein the compressor 1 is connected with a heat exchanger 2, the heat exchanger 2 is connected with an infiltration gasification unit 4, the infiltration gasification unit 4 is connected with an absorption tower 5, and the absorption tower 5 is connected with a hydrochloric acid storage tank 7.
Firstly, tail gas containing HCl and organic gas is conveyed to an osmotic gasification unit 4 by a compressor 1 through a heat exchanger 2, HCl separated by an osmotic gasification membrane enters an absorption tower 5, then absorption liquid in the absorption tower 5 enters a hydrochloric acid storage tank 7, and the absorption liquid returns to a hydrochloric acid batching area for use when a certain concentration is reached.
Further, the permeation gasification unit 4 may be a single membrane module, or multiple groups of membrane modules may be connected in series or parallel, the separated system is heated by the heater 3 and then sequentially enters the monomer module 41, and the blocked organic gas component enters the waste gas treatment process after passing through the heat exchanger 2.
Further, the absorption tower 5 can be a spray tower or a packed tower, and the gas and the liquid can be contacted in a countercurrent way or in a parallel way and connected with the vacuum pump 6.
Compared with the prior art, the method has the advantages that the tail gas characteristic is combined, the HCl for trimethyl orthoacetate is recovered by utilizing the osmotic gasification-absorption coupling technology, the process is simple, the operation cost is low, the HCl recovery rate is more than 99.5%, and the production cost is remarkably reduced.
Example 1
The tail gas containing 5% HCl at room temperature is conveyed to a single permeation gasification unit 4 by a compressor 1 through a heat exchanger 2, HCl separated by permeation gasification membranes enters an absorption tower 5 and is absorbed in countercurrent, and 25% hydrochloric acid absorption liquid obtained is fed into a hydrochloric acid storage tank 7 and can be returned to a hydrochloric acid batching zone for use.
Example 2
The tail gas containing 5% HCl at room temperature is conveyed to a group 2 monomer module 41 by a compressor 1 through a heat exchanger 2, HCl separated by an osmotic gasification membrane enters an absorption tower 5 and is absorbed in countercurrent, and the obtained 31% hydrochloric acid absorption liquid enters a hydrochloric acid storage tank 7 and can be returned to a hydrochloric acid batching area for use.
Example 3
The tail gas containing 5% HCl at room temperature is conveyed to a group 2 monomer module 41 by a compressor 1 through a heat exchanger 2, HCl separated by an osmotic gasification membrane enters an absorption tower 5 and is absorbed in countercurrent, and the obtained 30% hydrochloric acid absorption liquid enters a hydrochloric acid storage tank 7 and can be returned to a hydrochloric acid batching area for use.
Example 4
The tail gas containing 5% HCl at room temperature is conveyed to a group 2 monomer module 41 by a compressor 1 through a heat exchanger 2, HCl separated by an osmotic gasification membrane enters an absorption tower 5 and is absorbed in parallel flow, and the obtained 28% hydrochloric acid absorption liquid enters a hydrochloric acid storage tank 7 and can be returned to a hydrochloric acid batching area for use.
Example 5
The tail gas containing 3% HCl at room temperature is conveyed to a group 2 monomer module 41 by a compressor 1 through a heat exchanger 2, HCl separated by an osmotic gasification membrane enters an absorption tower 5 and is absorbed in countercurrent, and the obtained 30% hydrochloric acid absorption liquid enters a hydrochloric acid storage tank 7 and can be returned to a hydrochloric acid batching area for use.
It is obvious that the specific implementation of the present utility model is not limited by the above-mentioned modes, and that it is within the scope of protection of the present utility model only to adopt various insubstantial modifications made by the method conception and technical scheme of the present utility model.
Claims (10)
1. The HCl recovery system for trimethyl orthoacetate is characterized by comprising a compressor, wherein the compressor is connected with a heat exchanger, the heat exchanger is connected with an infiltration gasification unit, and the infiltration gasification unit is connected with an absorption tower; the compressor is connected with the air inlet pipeline, the compressor is connected with the heat exchanger through the first pipeline, and the heat exchanger is connected with the infiltration gasification unit through the second pipeline; the infiltration gasification unit is connected with the absorption tower through a third pipeline.
2. The HCl recovery system for trimethyl orthoacetate according to claim 1, wherein a heater is connected to the infiltration gasification unit.
3. An HCl recovery system for trimethyl orthoacetate according to any one of claims 1-2, wherein the pervaporation unit comprises a plurality of monomer modules, adjacent monomer modules being arranged in series or parallel; adjacent monomer modules are connected through a communicating pipeline; the communication pipe is disposed through the heater.
4. The HCl recovery system for trimethyl orthoacetate according to claim 1, wherein the pervaporation unit is coupled to a residual gas conduit, the residual gas conduit passing through a heat exchanger arrangement.
5. The HCl recovery system for trimethyl orthoacetate according to claim 1, wherein the absorber is connected to a hydrochloric acid tank; the absorption tower is communicated with the hydrochloric acid storage tank through an external pipeline.
6. The HCl recovery system for trimethyl orthoacetate according to claim 5, wherein the hydrochloric acid storage tank is connected to the absorber via a circulation line; one end of the circulating pipeline is connected with the hydrochloric acid storage tank, and the other end of the circulating pipeline is connected with the absorption tower; the circulating pipeline and the external pipeline are distributed at two ends of the absorption tower.
7. The HCl recovery system for trimethyl orthoacetate according to claim 6, wherein the recycle line is connected to a make-up line.
8. The HCl recovery system for trimethyl orthoacetate according to claim 7, wherein the circulation conduit, the external conduit, and the replenishment conduit are provided with control valves.
9. The HCl recovery system for trimethyl orthoacetate according to claim 1, wherein the absorber is externally connected to a vacuum pump.
10. The HCl recovery system for trimethyl orthoacetate according to claim 1, wherein the absorber is a spray tower or a packed tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223497476.XU CN219072545U (en) | 2022-12-27 | 2022-12-27 | HCl recovery system for trimethyl orthoacetate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223497476.XU CN219072545U (en) | 2022-12-27 | 2022-12-27 | HCl recovery system for trimethyl orthoacetate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219072545U true CN219072545U (en) | 2023-05-26 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223497476.XU Active CN219072545U (en) | 2022-12-27 | 2022-12-27 | HCl recovery system for trimethyl orthoacetate |
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| Country | Link |
|---|---|
| CN (1) | CN219072545U (en) |
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2022
- 2022-12-27 CN CN202223497476.XU patent/CN219072545U/en active Active
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