CN211798889U - Refining system for by-product hydrochloric acid in methane chloride process - Google Patents
Refining system for by-product hydrochloric acid in methane chloride process Download PDFInfo
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- CN211798889U CN211798889U CN201922162353.2U CN201922162353U CN211798889U CN 211798889 U CN211798889 U CN 211798889U CN 201922162353 U CN201922162353 U CN 201922162353U CN 211798889 U CN211798889 U CN 211798889U
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Abstract
The utility model discloses a refining system of byproduct hydrochloric acid in methane chloride process, which comprises a stripping tower, a reboiler and an injection pump; a material inlet is formed in the side wall of the top of the stripping tower, a gas phase outlet is formed in a head of the top of the stripping tower, a liquid phase outlet is formed in the bottom of the stripping tower, and a circulating inlet is formed in the lower part of the side wall of the stripping tower; the liquid phase outlet of the stripping tower is connected with a discharging pipeline, the discharging pipeline is provided with a discharging branch pipe, a liquid phase outlet of the stripping tower is communicated with an inlet of a reboiler through the discharging branch pipe, an outlet of the reboiler is connected with a circulating inlet of the stripping tower, and a gas phase outlet of the stripping tower is communicated with an inlet of an injection pump. The utility model discloses not only can reduce the hydrochloric acid content in the top of the tower result, can the content of organic matter in the hydrochloric acid of extraction at the bottom of the tower of greatly reduced strip tower moreover.
Description
Technical Field
The utility model belongs to the technical field of methane chloride production, a refined of by-product hydrochloric acid in the methane chloride production technology is related to, concretely relates to refined system of methane chloride technology by-product hydrochloric acid.
Background
The statements herein merely provide background information related to the present disclosure and may not necessarily constitute prior art.
Methane chloride is also called methyl chloride, and products of methane molecules with hydrogen atoms replaced by chlorine atoms include four compounds, namely methyl chloride, dichloromethane, trichloromethane, carbon tetrachloride and the like. Wherein, the methane chloride is colorless gas with odor like ether, and the rest is colorless transparent volatile liquid. All methane chlorides are highly soluble and are therefore widely used as solvents. At present, the production process of methane chloride comprises a methane chlorination method, a methanol hydrochlorination method and the like. No matter which production process is adopted, in the process of producing methane chloride, particularly dichloromethane and trichloromethane, a byproduct hydrogen chloride is generated, and the hydrogen chloride is dissolved to form a byproduct hydrochloric acid.
Hydrochloric acid is an important chemical raw material and is widely applied to dyes, medicines, foods, printing and dyeing, leather, metallurgy and the like, so that the hydrochloric acid serving as a byproduct in methane chloride can be collected and reused. At present, the process for refining the byproduct hydrochloric acid in the methane chloride is mainly a stripping process based on a stripping tower, but the research of the inventor of the utility model finds that when the stripping process is adopted, the hydrochloric acid extracted from the bottom of the stripping tower contains a large amount of organic matters such as methane chloride, methylene dichloride and the like, thereby reducing the quality of the hydrochloric acid; meanwhile, the tower top product of the stripping tower contains a large amount of hydrochloric acid, so that the application of the byproduct hydrochloric acid in the methane chloride is influenced.
SUMMERY OF THE UTILITY MODEL
In order to solve the deficiency of the prior art, the utility model aims at providing a refining system of methane chloride technology by-product hydrochloric acid not only can reduce the hydrochloric acid content in the top of the tower product, moreover can the greatly reduced strip tower bottom extract the content of organic matter in the hydrochloric acid.
In order to realize the purpose, the technical scheme of the utility model is that:
a refining system of byproduct hydrochloric acid in a methane chloride process comprises a stripping tower, a reboiler and an injection pump;
a material inlet is formed in the side wall of the top of the stripping tower, a gas phase outlet is formed in a head of the top of the stripping tower, a liquid phase outlet is formed in the bottom of the stripping tower, and a circulating inlet is formed in the lower part of the side wall of the stripping tower;
the liquid phase outlet of the stripping tower is connected with a discharging pipeline, the discharging pipeline is provided with a discharging branch pipe, a liquid phase outlet of the stripping tower is communicated with an inlet of a reboiler through the discharging branch pipe, an outlet of the reboiler is connected with a circulating inlet of the stripping tower, and a gas phase outlet of the stripping tower is communicated with an inlet of an injection pump.
At first, the utility model discloses with the material import setting at the top of the tower, can utilize the lower feeding of temperature to bring and replace the backward flow, the lower feeding of temperature provides cold volume for the steam condensation that rises in the tower, reaches the steam condensation that makes rise through the heat transfer to reduce the content of hydrogen chloride in the top of the tower product. Secondly, the utility model discloses set up the jet pump at the top of the tower, the purpose carries out the negative pressure operation to the strip tower, and the majority is the atmospheric pressure strip or the pressurization strip in traditional strip technology, and the strip tower steam volume that rises is big in atmospheric pressure or pressurization technology, and the steam that just rises is total in the hydrogen chloride content big, organic matter content is few, just the appearance causes in the tower cauldron hydrochloric acid organic matter content can not fall to minimumly, and the extraction volume at the bottom of the tower is big. By adjusting the stripping negative pressure operation, the organic matters in the hydrochloric acid can be easier to be distilled out than hydrogen chloride, and the content of the organic matters in the hydrochloric acid in the tower bottom can be lower than 10 ppm.
And further, the tower bottom cooler is included, and an inlet of the tower bottom cooler is communicated with a liquid phase outlet of the stripping tower through a discharge pipeline.
And a material inlet of the tower top condensing device is communicated with a gas phase outlet of the stripping tower, and a liquid phase outlet of the tower top condensing device is communicated with an inlet of the jet pump.
Furthermore, the tower top condensing device comprises at least two tower top condensing devices connected in series, a material inlet of the first tower top condensing device is communicated with a gas phase outlet of the stripping tower, a gas phase outlet of the previous tower top condensing device is communicated with a material inlet of the next tower top condensing device, and a liquid phase outlet of each tower top condensing device is communicated with an inlet of the jet pump.
Furthermore, the tower top condensing device is two tower top condensing devices connected in series.
And further, the device comprises a separation tank, wherein an inlet of the separation tank is communicated with a gas phase outlet of the stripping tower, and a gas outlet of the separation tank is communicated with an inlet of the jet pump.
Further, including top of the tower condensing equipment and knockout drum, top of the tower condensing equipment's material import and the gaseous phase export intercommunication of strip tower, top of the tower condensing equipment liquid phase export and the access connection of knockout drum, the gas outlet and the import intercommunication of jet pump of knockout drum.
Furthermore, the tower top condensing device comprises at least two tower top condensing devices connected in series, a material inlet of the first tower top condensing device is communicated with a gas phase outlet of the stripping tower, a gas phase outlet of the previous tower top condensing device is communicated with a material inlet of the next tower top condensing device, and a liquid phase outlet of each tower top condensing device is communicated with an inlet of the separating tank.
Furthermore, the tower top condensing device is two tower top condensing devices connected in series.
The utility model has the advantages that:
1. the utility model arranges the material inlet on the side wall of the tower top of the stripping tower, so that the material entering the stripping tower can replace the reflux, and the content of hydrochloric acid in the tower top product is reduced; meanwhile, the process can be simplified, and the steam consumption is reduced.
2. The utility model discloses top of the tower gas phase export and the import intercommunication of jet pump can carry out the negative pressure operation to the strip tower to reduce the content of organic matter in the hydrochloric acid at the bottom of the tower, the content of organic matter can reduce to below 10ppm in its hydrochloric acid, thereby satisfies hydrochloric acid user demand.
Drawings
The accompanying drawings, which form a part of the specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention without unduly limiting the scope of the invention.
Fig. 1 is a schematic diagram of a system structure according to embodiment 1 of the present invention;
fig. 2 is a schematic structural diagram of embodiment 2 of the present invention;
the device comprises a stripping tower 1, a stripping tower 2, a reboiler 3, a jet pump 4, a tower bottom cooler 5, a primary tower top condenser 6, a secondary tower top condenser 7 and a separation tank.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
In view of prior art is difficult to refine the by-product hydrochloric acid in the methane chloride, the utility model provides a refining system of methane chloride technology by-product hydrochloric acid.
The utility model provides a typical implementation mode of a refining system of byproduct hydrochloric acid in a methane chloride process, which comprises a stripping tower, a reboiler and an injection pump;
a material inlet is formed in the side wall of the top of the stripping tower, a gas phase outlet is formed in a head of the top of the stripping tower, a liquid phase outlet is formed in the bottom of the stripping tower, and a circulating inlet is formed in the lower part of the side wall of the stripping tower;
the liquid phase outlet of the stripping tower is connected with a discharging pipeline, the discharging pipeline is provided with a discharging branch pipe, a liquid phase outlet of the stripping tower is communicated with an inlet of a reboiler through the discharging branch pipe, an outlet of the reboiler is connected with a circulating inlet of the stripping tower, and a gas phase outlet of the stripping tower is communicated with an inlet of an injection pump.
At first, the utility model discloses with the material import setting at the top of the tower, can utilize the lower feeding of temperature to bring and replace the backward flow, the lower feeding of temperature provides cold volume for the steam condensation that rises in the tower, reaches the steam condensation that makes rise through the heat transfer to reduce the content of hydrochloric acid in the top of the tower product. Secondly, the utility model discloses set up the jet pump at the top of the tower, the purpose carries out the negative pressure operation to the strip tower, and the majority is the atmospheric pressure strip or the pressurization strip in traditional strip technology, and the strip tower steam volume that rises is big in atmospheric pressure or pressurization technology, and the steam that just rises is total in the hydrogen chloride content big, organic matter content is few, just the appearance causes in the tower cauldron hydrochloric acid organic matter content can not fall to minimumly, and the extraction volume at the bottom of the tower is big. By adjusting the stripping negative pressure operation, the organic matters in the hydrochloric acid can be easier to be distilled out than hydrogen chloride, and the content of the organic matters in the hydrochloric acid in the tower bottom can be lower than 10 ppm.
One or more embodiments of this embodiment include a bottoms cooler having an inlet in communication with the liquid phase outlet of the stripper column via a discharge line. The hydrogen chloride is prevented from escaping due to overhigh temperature of the hydrochloric acid.
In one or more embodiments of this embodiment, the system includes an overhead condensing unit having a feed inlet in communication with the vapor outlet of the stripper and a liquid outlet in communication with the inlet of the ejector pump. The product at the top of the tower can be condensed and extracted.
In the series of embodiments, the tower top condensing device comprises at least two tower top condensing devices connected in series, a material inlet of the first tower top condensing device is communicated with a gas phase outlet of the stripping tower, a gas phase outlet of the previous tower top condensing device is communicated with a material inlet of the next tower top condensing device, and a liquid phase outlet of each tower top condensing device is communicated with an inlet of the jet pump. Different products at the top of the tower can be condensed and extracted.
In this series of embodiments, the overhead condensing unit is two overhead condensers connected in series.
One or more embodiments of this embodiment include a knockout drum, an inlet of the knockout drum being in communication with the gas phase outlet of the stripping column, and a gas outlet of the knockout drum being in communication with an inlet of the jet pump. The provision of a knockout drum enables the overhead product to be collected and prevents damage to the jet pump.
In one or more embodiments of the present disclosure, the stripping tower comprises a tower top condensing device and a separation tank, a material inlet of the tower top condensing device is communicated with a gas phase outlet of the stripping tower, a liquid phase outlet of the tower top condensing device is connected with an inlet of the separation tank, and a gas outlet of the separation tank is communicated with an inlet of the jet pump.
In the series of embodiments, the tower top condensing device comprises at least two tower top condensing devices connected in series, a material inlet of the first tower top condensing device is communicated with a gas phase outlet of the stripping tower, a gas phase outlet of the previous tower top condensing device is communicated with a material inlet of the next tower top condensing device, and a liquid phase outlet of each tower top condensing device is communicated with an inlet of the separating tank.
In this series of embodiments, the overhead condensing unit is two overhead condensers connected in series.
In order to make the technical solutions of the present invention more clearly understood by those skilled in the art, the technical solutions of the present invention will be described in detail below with reference to specific embodiments.
Example 1
A refining system of by-product hydrochloric acid in a methane chloride process is shown in figure 1 and comprises a stripping tower 1, a reboiler 2 and a jet pump 3.
The side wall of the top of the stripping tower 1 is provided with a material inlet, the gas phase outlet is formed in the head of the stripping tower 1, the bottom of the stripping tower 1 is provided with a liquid phase outlet, and the lower part of the side wall of the stripping tower 1 is provided with a circulating inlet.
The liquid phase exit linkage ejection of compact pipeline of strip tower 1, the ejection of compact pipeline is equipped with ejection of compact branch pipe, and the liquid phase export of strip tower is through ejection of compact branch pipe and 2 import intercommunications of reboiler, and the exit linkage of reboiler 2 strips 1's circulation import, strips 1's gaseous phase export and jet pump 3's import intercommunication.
Example 2
A refining system of a byproduct hydrochloric acid in a methane chloride process is shown in figure 2 and comprises a stripping tower 1, a reboiler 2, a jet pump 3, a tower bottom cooler 4, a primary tower top condenser 5, a secondary tower top condenser 6 and a separation tank 7.
The side wall of the top of the stripping tower 1 is provided with a material inlet, the gas phase outlet is formed in the head of the stripping tower 1, the bottom of the stripping tower 1 is provided with a liquid phase outlet, and the lower part of the side wall of the stripping tower 1 is provided with a circulating inlet.
The liquid phase exit linkage ejection of compact pipeline of strip tower 1, ejection of compact pipeline are equipped with ejection of compact branch pipe, and the liquid phase export of strip tower 1 is through ejection of compact branch pipe and 2 import intercommunications of reboiler, and the exit linkage of reboiler 2 strips tower 1's circulation import.
The inlet of the tower bottom cooler 4 is communicated with the liquid phase outlet of the stripping tower 1 through a discharge pipeline.
The material inlet of the first-stage tower top condensation container 5 is communicated with the gas phase outlet of the stripping tower 1, the gas phase outlet of the first-stage tower top condensation container 5 is communicated with the material inlet of the second-stage tower top condensation container 6, and the liquid phase outlet of each tower top condensation container is communicated with the inlet of the separation tank 7.
The gas outlet of the separation tank 7 is communicated with the inlet of the jet pump 3.
The stripping tower is kept to operate under negative pressure through the jet pump, the evaporation amount of hydrogen chloride gas in hydrochloric acid can be reduced, and the evaporation amount of organic matters is increased. The amount distilled from the tower top is greatly reduced, and the content of organic matters in hydrochloric acid in the tower bottom is obviously reduced.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A refining system of byproduct hydrochloric acid in a methane chloride process is characterized by comprising a stripping tower, a reboiler and an injection pump;
a material inlet is formed in the side wall of the top of the stripping tower, a gas phase outlet is formed in a head of the top of the stripping tower, a liquid phase outlet is formed in the bottom of the stripping tower, and a circulating inlet is formed in the lower part of the side wall of the stripping tower;
the liquid phase outlet of the stripping tower is connected with a discharging pipeline, the discharging pipeline is provided with a discharging branch pipe, a liquid phase outlet of the stripping tower is communicated with an inlet of a reboiler through the discharging branch pipe, an outlet of the reboiler is connected with a circulating inlet of the stripping tower, and a gas phase outlet of the stripping tower is communicated with an inlet of an injection pump.
2. The system for refining by-product hydrochloric acid produced in the methane chloride process according to claim 1, wherein an inlet of the tower bottom cooler is communicated with a liquid phase outlet of the stripping tower through a discharge pipeline.
3. The system for refining the byproduct hydrochloric acid in the methane chloride process according to claim 1, which comprises a tower top condensing device, wherein a material inlet of the tower top condensing device is communicated with a gas phase outlet of the stripping tower, and a liquid phase outlet of the tower top condensing device is communicated with an inlet of the jet pump.
4. The system for refining hydrochloric acid as a byproduct of a methane chloride process according to claim 3, wherein the tower top condensing unit comprises at least two tower top condensers connected in series, the material inlet of the first tower top condenser is connected to the gas phase outlet of the stripping tower, the gas phase outlet of the previous tower top condenser is connected to the material inlet of the next tower top condenser, and the liquid phase outlet of each tower top condenser is connected to the inlet of the ejector pump.
5. The system for refining by-product hydrochloric acid produced in a methane chloride process according to claim 1, which comprises a separation tank, wherein an inlet of the separation tank is communicated with a gas phase outlet of the stripping tower, and an outlet of the separation tank is communicated with an inlet of the jet pump.
6. The system for refining the byproduct hydrochloric acid in the methane chloride process according to claim 1, which comprises a tower top condensing device and a separating tank, wherein a material inlet of the tower top condensing device is communicated with a gas phase outlet of the stripping tower, a liquid phase outlet of the tower top condensing device is connected with an inlet of the separating tank, and a gas outlet of the separating tank is communicated with an inlet of the jet pump.
7. The system of claim 6, wherein the tower top condensing unit comprises at least two tower top condensers connected in series, the first tower top condenser has a material inlet connected to the gas phase outlet of the stripping tower, the previous tower top condenser has a gas phase outlet connected to the material inlet of the next tower top condenser, and the liquid phase outlet of each tower top condenser is connected to the inlet of the separation tank.
8. The system for refining hydrochloric acid as a byproduct in a methane chloride process according to claim 3 or 6, wherein the overhead condensing unit comprises two overhead condensers connected in series.
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| CN201922162353.2U CN211798889U (en) | 2019-12-04 | 2019-12-04 | Refining system for by-product hydrochloric acid in methane chloride process |
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| CN201922162353.2U CN211798889U (en) | 2019-12-04 | 2019-12-04 | Refining system for by-product hydrochloric acid in methane chloride process |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113828001A (en) * | 2021-10-29 | 2021-12-24 | 新疆晶硕新材料有限公司 | Separation system and separation method of chloromethane |
| CN114671405A (en) * | 2022-05-07 | 2022-06-28 | 鲁西化工集团股份有限公司硅化工分公司 | Process for preparing high-purity hydrogen chloride from by-product hydrochloric acid in methane chloride process |
-
2019
- 2019-12-04 CN CN201922162353.2U patent/CN211798889U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113828001A (en) * | 2021-10-29 | 2021-12-24 | 新疆晶硕新材料有限公司 | Separation system and separation method of chloromethane |
| CN113828001B (en) * | 2021-10-29 | 2022-10-11 | 新疆晶硕新材料有限公司 | Separation system and separation method of chloromethane |
| CN114671405A (en) * | 2022-05-07 | 2022-06-28 | 鲁西化工集团股份有限公司硅化工分公司 | Process for preparing high-purity hydrogen chloride from by-product hydrochloric acid in methane chloride process |
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| GR01 | Patent grant | ||
| CP03 | Change of name, title or address |
Address after: 252000 Luxi Industrial Park, high tech Industrial Development Zone, Liaocheng City, Shandong Province Patentee after: Liaocheng Luxi methyl chloride Chemical Co.,Ltd. Address before: 252211 Shandong city of Liaocheng province Dong'e County Gu Guan Tun Zhen Luxi Chemical Industrial Park Patentee before: SHANDONG LIAOCHENG LUXI SIXTH CHEMICAL FERTILIZER Co.,Ltd. |
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