CN114671405A - Process for preparing high-purity hydrogen chloride from by-product hydrochloric acid in methane chloride process - Google Patents
Process for preparing high-purity hydrogen chloride from by-product hydrochloric acid in methane chloride process Download PDFInfo
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- CN114671405A CN114671405A CN202210492776.4A CN202210492776A CN114671405A CN 114671405 A CN114671405 A CN 114671405A CN 202210492776 A CN202210492776 A CN 202210492776A CN 114671405 A CN114671405 A CN 114671405A
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- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/03—Preparation from chlorides
- C01B7/035—Preparation of hydrogen chloride from chlorides
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- C—CHEMISTRY; METALLURGY
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- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0712—Purification ; Separation of hydrogen chloride by distillation
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Abstract
The invention belongs to the field of preparation of hydrogen chloride, and discloses a process for preparing high-purity hydrogen chloride from a byproduct hydrochloric acid in a methane chloride process, which comprises a stripping purification process of the byproduct hydrochloric acid and a hydrochloric acid resolution process. The method comprises the following steps: stripping a byproduct hydrochloric acid in a chloromethane production process to obtain a refined byproduct hydrochloric acid; uniformly mixing the refined by-product hydrochloric acid with a calcium chloride solution, and analyzing to obtain hydrogen chloride gas; and condensing and demisting the hydrogen chloride gas to obtain the hydrogen chloride gas. The supergravity analysis tower adopted by the invention can improve the mixing effect of calcium chloride and hydrochloric acid and reduce the energy consumption and height of equipment; meanwhile, the problem that the conventional analytic tower is blocked due to calcium chloride precipitation can be effectively solved.
Description
Technical Field
The invention relates to the field of preparation of hydrogen chloride, and particularly relates to a process for preparing high-purity hydrogen chloride by using a byproduct hydrochloric acid of methane chloride.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
The production process of the 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, byproduct hydrochloric acid is generated, the concentration of the hydrochloric acid is about 20-25%, and a large amount of methyl chloride can be dissolved in the hydrochloric acid. The problem of digestion and utilization of part of byproduct hydrochloric acid becomes a common problem restricting the development of the industry.
With the continuous development of industrial technology, hydrogen chloride has been used as an important raw material for producing high value-added products such as methane chloride, epichlorohydrin, trichlorosilane, chlorine and the like. Therefore, the development of the technology for preparing high-purity hydrogen chloride from the hydrochloric acid byproduct in the methane chloride process has important practical significance.
Patent CN1922162353.2 discloses a refining system of by-product hydrochloric acid in methane chloride process, which comprises a stripping tower, a reboiler and an injection pump; and a gas phase outlet of the stripping tower is communicated with an inlet of the jet pump. But the inventor researches and discovers that: the mixing effect of calcium chloride and hydrochloric acid is still to be improved, and the problem of calcium chloride precipitation and blockage of the desorption tower is also existed.
Disclosure of Invention
In order to solve the problems, the invention aims to provide a process for preparing high-purity hydrogen chloride by using hydrochloric acid as a byproduct in a methane chloride process.
In order to achieve the purpose, the technical scheme of the invention is as follows:
in a first aspect of the present invention, there is provided a process for preparing high purity hydrogen chloride from hydrochloric acid by-produced in a methane chloride process, comprising:
stripping a byproduct hydrochloric acid in a chloromethane production process to obtain a refined byproduct hydrochloric acid;
uniformly mixing the refined by-product hydrochloric acid with a calcium chloride solution, and analyzing to obtain hydrogen chloride gas;
and condensing and demisting the hydrogen chloride gas to obtain the hydrogen chloride gas.
The invention adopts the hypergravity rectifying tower to replace the stripping tower, and simultaneously removes the mixer; hydrochloric acid is fed from a feed inlet at the side of the rectifying tower, and calcium chloride concentrated solution is fed from the top of the rectifying tower. The mixing effect of calcium chloride and hydrochloric acid can be improved, the energy consumption is reduced, the equipment height and the investment are reduced, and the problem that the conventional analytic tower is blocked due to calcium chloride precipitation can be effectively solved.
In a second aspect of the present invention, a system for preparing high purity hydrogen chloride from hydrochloric acid byproduct of a methane chloride process is provided, which comprises: a stripping tower 1, a hypergravity analysis tower 4, a condenser and a demister; the stripping tower 1, the hypergravity analysis tower 4, the condenser and the demister are connected in sequence.
In a third aspect of the present invention, there is provided a high purity hydrogen chloride production system, comprising: the system described above.
The invention has the beneficial effects that:
(1) the process for preparing high-purity hydrogen chloride by using the byproduct hydrochloric acid in the methane chloride process has the advantages that: the supergravity analysis tower adopted by the invention can improve the mixing effect of calcium chloride and hydrochloric acid and reduce the energy consumption and height of equipment; meanwhile, the problem that the conventional analytic tower is blocked due to calcium chloride precipitation can be effectively solved.
(2) The operation method is simple, low in cost, universal and easy for large-scale production.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention.
Fig. 1 is a schematic structural diagram of a process device for preparing high-purity hydrogen chloride from a byproduct hydrochloric acid in a methane chloride process, which is provided by the invention, and comprises a stripping tower 1, a stripping tower 2, a reboiler 3, an injection pump 4, a supergravity desorption tower 5, a hydrogen chloride primary condenser 6, a hydrogen chloride secondary condenser 7, a demister 8 and a multi-effect evaporation reboiler.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. 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.
Firstly, stripping a byproduct hydrochloric acid in a chloromethane production process by a stripping tower to obtain a refined byproduct hydrochloric acid with the concentration of 20-31% and the organic matter content of less than 10ppm at a tower bottom.
The top of the stripping tower is provided with an injection pump, negative pressure operation is carried out on the stripping tower, the evaporation amount of hydrogen chloride gas in hydrochloric acid can be reduced, the evaporation amount of organic matters is increased, and the content of the organic matters in the hydrochloric acid in the tower kettle is lower than 10 ppm.
In some embodiments, the stripper temperature is from 40 to 60 ℃.
In some embodiments, the stripper pressure is between-0.01 and-0.1 MPa.
In some embodiments, the stripped refined byproduct hydrochloric acid enters from a side feed inlet of the hypergravity resolution tower, and the calcium chloride solution enters from a top feed inlet of the hypergravity resolution tower and is mixed under the action of hypergravity. The hydrogen chloride gas generated by the analysis enters a condenser and a demister in sequence through the top of the analysis tower to obtain pure hydrogen chloride gas.
The refined by-product hydrochloric acid is extracted from the kettle of the stripping tower without being cooled by a heat exchanger, the temperature of the kettle of the stripping tower can be fully utilized, and the preheating process after mixing with calcium chloride is reduced.
The hydrogen chloride gas is subjected to a two-stage condenser and a demister to remove impurities such as water and the like; the concentration of the calcium chloride solution at the bottom of the tower is reduced to about 40 percent after being analyzed, the concentration of the calcium chloride is improved to more than 40 percent through multi-effect evaporation, and the concentrated calcium chloride returns to the jet type fluid static mixer for recycling. On the other hand, parameters such as the temperature and the pressure of the analysis tower are adjusted by adjusting the temperature and the pressure of the multi-effect evaporator.
In some embodiments, the concentration of the calcium chloride solution is 40-60%.
In some embodiments, the pressure of the desorption column is 0.1 to 0.4 MPa.
In some embodiments, the temperature at the top of the stripper column is 100 to 120 ℃.
The following examples are presented to enable one of ordinary skill in the art to more fully understand the present invention and are not intended to limit the scope of the embodiments described herein.
Example 1
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the stripping tower heats the tower body by using a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 50 ℃, and the pressure at the top of the tower is-0.01 MPa.
(2) After steam stripping, the concentration of the refined hydrochloric acid at the tower bottom is 25.4 percent, and the content of the chloromethane is 5 ppm.
(3) Refined hydrochloric acid enters the desorption tower from a side feed inlet of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution and the hypergravity solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 110 ℃, and the pressure is controlled at 0.1 MPa.
(4) The desorbed hydrogen chloride gas is condensed by a condenser, demisted and dried, and has the purity of 99.95 percent and the water content of 10 ppm.
Example 2
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the stripping tower heats the tower body by using a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 45 ℃, and the pressure at the top of the tower is-0.1 MPa.
(2) After steam stripping, the concentration of the refined hydrochloric acid at the tower bottom is 25.5 percent, and the content of the chloromethane is 2 ppm.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 110 ℃, and the pressure is controlled at 0.25 MPa.
(4) The desorbed hydrogen chloride gas is condensed by a condenser, demisted and dried, and the purity is 99.8 percent, and the water content is 32 ppm.
Example 3
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the stripping tower heats the tower body by using a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 60 ℃, and the pressure at the top of the tower is-0.05 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 110 ℃, and the pressure is controlled at 0.1 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Example 4
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the stripping tower heats the tower body by using a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 40 ℃, and the pressure at the top of the tower is-0.08 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 110 ℃, and the pressure is controlled at 0.1 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Example 5
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the tower body of the stripping tower is heated by a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 40 ℃, and the pressure at the top of the tower is-0.08 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 100 ℃, and the pressure is controlled at 0.4 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Example 6
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the tower body of the stripping tower is heated by a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 40 ℃, and the pressure at the top of the tower is-0.08 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 120 ℃, and the pressure is controlled at 0.2 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Example 7
(1) A by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% is introduced from a liquid feed inlet of the stripping tower by using a feed pump at the flow rate of 2 tons/hour; the tower body of the stripping tower is heated by a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 40 ℃, and the pressure at the top of the tower is-0.08 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 115 ℃, and the pressure is controlled at 0.3 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Example 8
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the stripping tower heats the tower body by using a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 50 ℃, and the pressure at the top of the tower is-0.06 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 60% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 105 ℃, and the pressure is controlled at 0.3 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Example 9
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the stripping tower heats the tower body by using a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 50 ℃, and the pressure at the top of the tower is-0.06 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the desorption tower from a feed inlet at the side of the hypergravity desorption tower, 40% calcium chloride solution enters the desorption tower from the top of the hypergravity desorption tower, and the calcium chloride solution are fully mixed by utilizing the hypergravity effect in the desorption tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 105 ℃, and the pressure is controlled at 0.3 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Example 10
(1) Introducing by-product hydrochloric acid (the content of methyl chloride is 1.6%) with the concentration of 22% from a liquid feed inlet of a stripping tower by using a feed pump at the flow rate of 2 tons/hour; the stripping tower heats the tower body by using a reboiler at the bottom of the tower, so that the temperature of the tower body is controlled at 50 ℃, and the pressure at the top of the tower is-0.06 MPa.
(2) After steam stripping, hydrochloric acid is refined in the tower bottom.
(3) Refined hydrochloric acid enters the resolution tower from a feed inlet at the side of the hypergravity resolution tower, 50% calcium chloride solution enters the resolution tower from the top of the hypergravity resolution tower, and the calcium chloride solution and the hypergravity solution are fully mixed by utilizing the hypergravity effect in the resolution tower. The tower kettle supplies heat through a multi-effect evaporation reboiler, the temperature of the top of the desorption tower is controlled at 105 ℃, and the pressure is controlled at 0.3 MPa.
(4) And condensing, demisting and drying the desorbed hydrogen chloride gas by a condenser to obtain the high-purity hydrogen chloride gas.
Finally, it should be noted that, although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof. 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 (10)
1. A process for preparing high-purity hydrogen chloride from hydrochloric acid as a byproduct of a methane chloride process is characterized by comprising the following steps of:
stripping a byproduct hydrochloric acid in a chloromethane production process to obtain a refined byproduct hydrochloric acid;
uniformly mixing the refined by-product hydrochloric acid with a calcium chloride solution, and analyzing to obtain hydrogen chloride gas;
and condensing and demisting the hydrogen chloride gas to obtain the hydrogen chloride gas.
2. The process for preparing high-purity hydrogen chloride from hydrochloric acid as a byproduct of a methane chloride process according to claim 1, wherein the stripping temperature is 40-60 ℃ and the pressure is-0.01-0.1 MPa.
3. The process for producing high-purity hydrogen chloride according to claim 1, wherein the calcium chloride solution obtained by the desorption is concentrated and then mixed with the purified by-product hydrochloric acid.
4. The process for preparing high-purity hydrogen chloride from hydrochloric acid as a byproduct of a methane chloride process according to claim 1, wherein the concentration of the calcium chloride solution is 40-60%.
5. The process for preparing high-purity hydrogen chloride from hydrochloric acid as a byproduct of a methane chloride process according to claim 1, wherein the desorption pressure is 0.1-0.4 MPa, and the temperature is 100-120 ℃.
6. The process for preparing high-purity hydrogen chloride from the byproduct hydrochloric acid in the methane chloride process according to claim 1, wherein the concentration of the refined byproduct hydrochloric acid is 20-31%, and the content of organic matters is less than 10 ppm.
7. A system for preparing high-purity hydrogen chloride from by-product hydrochloric acid in a methane chloride process is characterized by comprising the following steps: a stripping tower 1, a hypergravity analysis tower 4, a condenser and a demister; the stripping tower 1, the hypergravity analysis tower 4, the condenser and the demister are connected in sequence.
8. The system for preparing high-purity hydrogen chloride from hydrochloric acid byproduct of a methane chloride process according to claim 1, wherein the condenser comprises: a hydrogen chloride primary condenser 6 and a hydrogen chloride secondary condenser 7.
9. The system for preparing high-purity hydrogen chloride from by-product hydrochloric acid in the methane chloride process according to claim 1, wherein a jet pump is arranged at the top of the stripping tower.
10. A high-purity hydrogen chloride production system, comprising: the system of any one of claims 7-9.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115417381A (en) * | 2022-09-06 | 2022-12-02 | 江苏瑞祥化工有限公司 | Method for recycling byproduct hydrochloric acid containing machine components |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2836139A1 (en) * | 2002-02-18 | 2003-08-22 | Atofina | Drying hydrogen chloride derived from aqueous hydrochloric acid solutions comprises contacting the hydrogen chloride with anhydrous calcium chloride |
| CN211255245U (en) * | 2019-07-04 | 2020-08-14 | 南通星球石墨股份有限公司 | Production device for resolving hydrogen chloride from hydrochloric acid |
| CN211798889U (en) * | 2019-12-04 | 2020-10-30 | 山东聊城鲁西化工第六化肥有限公司 | Refining system for by-product hydrochloric acid in methane chloride process |
| CN214399818U (en) * | 2021-01-20 | 2021-10-15 | 杭州东日节能技术有限公司 | Device for purifying hydrogen chloride by calcium chloride method containing impurity dilute hydrochloric acid |
-
2022
- 2022-05-07 CN CN202210492776.4A patent/CN114671405A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2836139A1 (en) * | 2002-02-18 | 2003-08-22 | Atofina | Drying hydrogen chloride derived from aqueous hydrochloric acid solutions comprises contacting the hydrogen chloride with anhydrous calcium chloride |
| CN211255245U (en) * | 2019-07-04 | 2020-08-14 | 南通星球石墨股份有限公司 | Production device for resolving hydrogen chloride from hydrochloric acid |
| CN211798889U (en) * | 2019-12-04 | 2020-10-30 | 山东聊城鲁西化工第六化肥有限公司 | Refining system for by-product hydrochloric acid in methane chloride process |
| CN214399818U (en) * | 2021-01-20 | 2021-10-15 | 杭州东日节能技术有限公司 | Device for purifying hydrogen chloride by calcium chloride method containing impurity dilute hydrochloric acid |
Non-Patent Citations (1)
| Title |
|---|
| 王杏等: "《纳米二氧化钛的生产与应用》", 31 July 2014, 贵州科技出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115417381A (en) * | 2022-09-06 | 2022-12-02 | 江苏瑞祥化工有限公司 | Method for recycling byproduct hydrochloric acid containing machine components |
| CN115417381B (en) * | 2022-09-06 | 2023-11-24 | 江苏瑞祥化工有限公司 | Method for recycling byproduct hydrochloric acid containing organic components |
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