CN113003539A - Method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid - Google Patents
Method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid Download PDFInfo
- Publication number
- CN113003539A CN113003539A CN202110370173.2A CN202110370173A CN113003539A CN 113003539 A CN113003539 A CN 113003539A CN 202110370173 A CN202110370173 A CN 202110370173A CN 113003539 A CN113003539 A CN 113003539A
- Authority
- CN
- China
- Prior art keywords
- hydrochloric acid
- raw material
- dechlorination
- free chlorine
- valve
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid, which comprises the following steps: reduction dechlorination, distillation impurity removal and other steps; the preparation method utilizes redox reaction, stannous chloride is added into hydrochloric acid containing free chlorine, and the free chlorine generates stannic chloride through the redox reaction to achieve the aim of removing chlorine. Excessive stannous chloride and reaction product stannic chloride are left in heavy components in the distillation process, so that free chlorine is completely removed, and no metal ion impurity is introduced.
Description
Technical Field
The invention relates to a method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid, belonging to the technical field of fine chemical engineering.
Background
Hydrogen chloride is an important part of the chlorine industry. Hydrogen chloride is mostly produced as by-product hydrogen chloride and cannot be recycled in the process. With the rapid development of chlorine industry, especially the rapid expansion of the scale of organic chlorine products in recent years, the total amount of byproduct hydrogen chloride is gradually increased year by year, when a process system cannot be completely recycled, the byproduct hydrogen chloride is often introduced into water to produce byproduct hydrochloric acid, and most of the byproduct hydrochloric acid contains organic matters and metal impurities due to substandard indexes, so that the byproduct hydrogen chloride is not sold on the market. When the byproduct hydrochloric acid is sold as a burden, individual enterprises can sacrifice the environment for the benefits of the enterprises, but under the severe environment condition, the method is not suitable. Some enterprises can adopt a neutralization mode to treat and then discharge the hydrochloric acid, so that the treatment cost is high, resources are wasted, secondary pollution is caused, the environmental protection and the sustainable development of resource and energy are not facilitated, and the byproduct hydrochloric acid is a problem in industrial production. The high-purity hydrochloric acid belongs to fine chemicals and has the characteristics of strong acting force, high speed and obvious effect. The high-purity hydrochloric acid has wide application in various fields of our lives, such as the industries of medicine, chemical industry, semiconductors, photovoltaics, large-scale integrated circuits and the like. At present, with the development of large-scale integrated circuits, the requirement on the purity of hydrochloric acid required by manufacturing is higher and higher, and besides the requirement on the purity, the requirement on the content of impurities in the hydrochloric acid is higher and higher, and particularly, the heavy metal impurities are strictly limited. Since the by-product hydrochloric acid is an inexpensive means, it is necessary to utilize the by-product hydrochloric acid produced in the production process, remove free chlorine in the by-product hydrochloric acid, and further remove impurities by distillation to obtain high-quality hydrochloric acid. Related electronic grade hydrochloric acid products have been successfully developed by domestic units, but most of the products are glass instruments, and the capacity of the products is far from meeting the market demand of the electronic industry.
Disclosure of Invention
The present invention has been made in view of the above-mentioned problems of the prior art, and an object of the present invention is to provide a method for removing free chlorine from hydrochloric acid to obtain highly pure hydrochloric acid.
The technical scheme provided by the invention is as follows: a method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid is characterized by comprising the following steps:
the method comprises the following steps: adding stannous chloride into a hydrochloric acid raw material storage tank filled with hydrochloric acid raw material, and circularly stirring for reaction for 1-2 hours to obtain dechlorination raw material; the adding amount of the stannous chloride is added according to the concentration of free chlorine in the hydrochloric acid raw material, when the free chlorine in the synthetic hydrochloric acid for the chlor-alkali industry is more than 1ppm and less than 10ppm, 0.02-0.08 kg of the stannous chloride is added in each ton of the hydrochloric acid raw material, and when the free chlorine in the hydrochloric acid raw material is more than 10ppm, the adding amount of the stannous chloride in each ton of the hydrochloric acid raw material is 0.0001-0.001% of the amount of the hydrochloric acid raw material;
step two: after the reaction is finished, opening a discharging valve of a hydrochloric acid raw material storage tank and a feeding valve of a metering tank, enabling a dechlorination raw material to enter the metering tank, closing the discharging valve of the hydrochloric acid raw material storage tank and the feeding valve of the metering tank after the liquid level of the dechlorination raw material reaches 1200-1500 mm, opening a feeding pump, pumping the dechlorination raw material into a head tank, enabling the volume of the dechlorination raw material entering the head tank to be no more than three quarters of the total volume of the head tank, setting the height of the liquid level to be 1000-1300 mm, interlocking the head tank with the feeding pump, automatically closing the feeding pump when the height of the liquid level of the dechlorination raw material entering the head tank is higher than 80% of the set height of the liquid level, and automatically opening the feeding pump when the height of the liquid level of the dechlorination raw material entering the head tank is lower;
step three: opening a discharge valve of the head tank to enable the dechlorination raw material to flow into the upper half part of a finished product condenser for preheating, then flowing into a hydrochloric acid distiller for heating and distilling, opening a circulating water valve of the finished product condenser to enable circulating water to enter the finished product condenser, simultaneously opening a steam self-control regulating valve, interlocking with the pressure of the circulating water, setting the interlocking to be that when the pressure of the circulating water is less than 0.1MPa, the steam self-control regulating valve is closed, when the pressure of the circulating water is more than 0.1MPa, the steam self-control regulating valve is opened, and the pressure value displayed by a steam pressure gauge is controlled between 0.10MPa and 0.25MPa, so that the hydrochloric acid distiller is heated to 84-88 ℃, the dechlorination raw material is heated to be boiled, and the distilled gas-; the condensed hydrochloric acid is collected and flows into a finished product receiving groove, and the dilute acid is cooled by a dilute acid cooler and then flows into a dilute acid receiving groove 5.
Furthermore, the hydrochloric acid raw material is the synthetic hydrochloric acid for chlor-alkali industry, and the total acidity is more than or equal to 31 percent in mass percentage counted by HCl.
The invention has the beneficial effects that: the invention utilizes oxidation-reduction reaction, stannous chloride is added into the synthetic hydrochloric acid for chlor-alkali industry containing free chlorine, and the free chlorine generates stannic chloride through oxidation-reduction reaction to achieve the aim of removing chlorine. Chlorine is a strong oxidant, so SnCl2+Cl2=SnCl4And carrying out thin-wall ethanol chromatography at 20 ℃ under the condition that the boiling point of tin tetrachloride is 114.1 ℃ and the density is 2.226 g/cm. Carrying out thin film chromatography on the obtained stannous chloride by using the method of carrying out heavy plantation at the boiling point of 623 ℃ and the density of 2.710 g/cm, carrying out thin film chromatography on the obtained 32% hydrochloric acid by using the method of carrying out thin film chromatography on the obtained liquid film chromatography on the obtained thin film chromatography on the obtained. In the distillation process, stannic chloride and excessive stannous chloride are left in the heavy components, so that free chlorine is completely removed, and no metal ion impurities are introduced after distillation. The invention solves the problem that the free chlorine in the byproduct hydrochloric acid exceeds the standard, does not introduce new impurities, reduces the content of metal impurities through further distillation, ensures that all indexes reach the high-purity standard, and achieves the purposes of economy and environmental protection in the preparation process. In addition, the hydrochloric acid distiller, the finished product condenser and the dilute acid cooler are made of graphite immersion equipment, so that the production yield is high, the energy consumption is low, and the production quality is continuous and stable.
Drawings
FIG. 1 is a flow chart of the present invention.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings in which:
as shown in figure 1 of the drawings, in which,
example 1: as shown in fig. 1, a method for removing free chlorine from hydrochloric acid to obtain high-purity hydrochloric acid, comprises the following steps:
the method comprises the following steps: adding stannous chloride into a hydrochloric acid raw material storage tank 1 filled with hydrochloric acid raw material, wherein the hydrochloric acid raw material is synthetic hydrochloric acid for chlor-alkali industry (the total acidity is more than or equal to 31% by mass of HCl), and circularly stirring for reaction for 1.5h to obtain the dechlorination raw material. The adding amount of stannous chloride is added according to the concentration of free chlorine in the hydrochloric acid raw material. When the free chlorine in the synthetic hydrochloric acid for chlor-alkali industry is more than 1ppm and less than 10ppm, 0.05kg of stannous chloride is added to each ton of the synthetic hydrochloric acid for industry, and when the free chlorine in the synthetic hydrochloric acid for industry is more than 10ppm, the amount of the stannous chloride added to each ton of the synthetic hydrochloric acid for industry is 0.0005 percent of the amount of the synthetic hydrochloric acid for industry.
Step two: after the reaction is finished, opening a hydrochloric acid raw material storage tank discharge valve 11 and a metering tank feeding valve 12, enabling the dechlorination raw material to enter a metering tank 2, closing the hydrochloric acid raw material storage tank discharge valve 11 and the metering tank feeding valve 12 after the dechlorination raw material liquid level reaches 1400mm, starting a feeding pump 7, pumping the dechlorination raw material into a head tank 3, enabling the volume of the dechlorination raw material entering the head tank 3 to be not more than three quarters of the total volume of the head tank, setting the liquid level height to be 1200mm, interlocking the head tank 3 with the feeding pump 7, automatically closing the feeding pump when the dechlorination raw material liquid level height entering the head tank 3 is higher than 80% of the set liquid level height, automatically starting the feeding pump 7 when the dechlorination raw material liquid level height entering the head tank 3 is lower than 50% of the set liquid level height, ensuring automatic interlocking feeding, and realizing automatic continuous production.
Step three: the discharge valve 13 of the elevated tank is opened to enable the dechlorination raw material to flow into the upper half part of the finished product condenser 8 for preheating (the preheating aims are to fully utilize the heat of the gas-phase hydrochloric acid distilled by the hydrochloric acid distiller 9 to heat the dechlorination raw material and then flow into the hydrochloric acid distiller 9 for heating and distilling, and steam is saved). Then the hydrochloric acid flows into a hydrochloric acid distiller 9 to be heated and distilled, a circulating water valve 14 of a finished product condenser 8 is opened, circulating water enters the finished product condenser 8, a steam self-control regulating valve 15 is opened and interlocked with the pressure of the circulating water, the interlocking is set to be that when the pressure of the circulating water is less than 0.1MPa, the steam self-control regulating valve 15 is closed, when the pressure of the circulating water is more than 0.1MPa, the steam self-control regulating valve 15 is opened, the pressure value displayed by a steam pressure gauge 16 is strictly controlled at 0.2MPa, the hydrochloric acid distiller 9 is heated to 86 ℃, a dechlorination raw material is heated to be boiled, and gas-phase hydrochloric acid distilled by the hydrochloric acid distiller 9 returns to the finished. The condensed hydrochloric acid is collected and flows into a finished product receiving groove 4, and the dilute acid flows into a dilute acid receiving groove 5 after being cooled by a dilute acid cooler 10.
Example 2: as shown in fig. 1, a method for removing free chlorine from hydrochloric acid to obtain high-purity hydrochloric acid, comprises the following steps:
the method comprises the following steps: adding stannous chloride into a hydrochloric acid raw material storage tank 1 filled with hydrochloric acid raw material, wherein the hydrochloric acid raw material is synthetic hydrochloric acid for chlor-alkali industry (the total acidity is more than or equal to 31 percent by mass of HCl), and circularly stirring for reaction for 1 hour to obtain the dechlorination raw material. The adding amount of stannous chloride is added according to the concentration of free chlorine in the hydrochloric acid raw material. When the free chlorine in the synthetic hydrochloric acid for chlor-alkali industry is more than 1ppm and less than 10ppm, 0.02kg of stannous chloride is added into each ton of the synthetic hydrochloric acid for industry, and when the free chlorine in the synthetic hydrochloric acid for industry is more than 10ppm, the amount of the stannous chloride added into each ton of the synthetic hydrochloric acid for industry is 0.0001 percent of the amount of the synthetic hydrochloric acid for industry.
Step two: after the reaction is finished, opening a hydrochloric acid raw material storage tank discharging valve 11 and a metering tank feeding valve 12, enabling the dechlorination raw material to enter a metering tank 2, closing the hydrochloric acid raw material storage tank discharging valve 11 and the metering tank feeding valve 12 after the dechlorination raw material liquid level reaches 1200mm, starting a feeding pump 7, pumping the dechlorination raw material into a head tank 3, enabling the volume of the dechlorination raw material entering the head tank 3 to be not more than three quarters of the total volume of the head tank, setting the liquid level height to be 1000mm, interlocking the head tank 3 with the feeding pump 7, automatically closing the feeding pump when the dechlorination raw material liquid level height entering the head tank 3 is higher than 80% of the set liquid level height, automatically starting the feeding pump 7 when the dechlorination raw material liquid level height entering the head tank 3 is lower than 50% of the set liquid level height, ensuring automatic interlocking feeding, and realizing automatic continuous production.
Step three: the discharge valve 13 of the elevated tank is opened to enable the dechlorination raw material to flow into the upper half part of the finished product condenser 8 for preheating (the preheating aims are to fully utilize the heat of the gas-phase hydrochloric acid distilled by the hydrochloric acid distiller 9 to heat the dechlorination raw material and then flow into the hydrochloric acid distiller 9 for heating and distilling, and steam is saved). Then the hydrochloric acid flows into a hydrochloric acid distiller 9 to be heated and distilled, a circulating water valve 14 of a finished product condenser 8 is opened, circulating water enters the finished product condenser 8, a steam self-control regulating valve 15 is opened and interlocked with the pressure of the circulating water, the interlocking is set to be that when the pressure of the circulating water is less than 0.1MPa, the steam self-control regulating valve 15 is closed, when the pressure of the circulating water is more than 0.1MPa, the steam self-control regulating valve 15 is opened, the pressure value displayed by a steam pressure gauge 16 is strictly controlled at 0.10MPa, the hydrochloric acid distiller 9 is heated to 84 ℃, a dechlorination raw material is heated to be boiled, and distilled gas-phase hydrochloric acid returns to the finished product condenser. The condensed hydrochloric acid is collected and flows into a finished product receiving groove 4, and the dilute acid flows into a dilute acid receiving groove 5 after being cooled by a dilute acid cooler 10.
Example 3: as shown in fig. 1, a method for removing free chlorine from hydrochloric acid to obtain high-purity hydrochloric acid, comprises the following steps:
the method comprises the following steps: adding stannous chloride into a hydrochloric acid raw material storage tank 1 filled with hydrochloric acid raw material, wherein the hydrochloric acid raw material is synthetic hydrochloric acid for chlor-alkali industry (the total acidity is more than or equal to 31 percent by mass of HCl), and circularly stirring for reaction for 2 hours to obtain the dechlorination raw material. The adding amount of stannous chloride is added according to the concentration of free chlorine in the hydrochloric acid raw material. When the free chlorine in the synthetic hydrochloric acid for chlor-alkali industry is more than 1ppm and less than 10ppm, 0.08kg of stannous chloride is added in each ton of the synthetic hydrochloric acid for industry, and when the free chlorine in the synthetic hydrochloric acid for industry is more than 10ppm, the amount of the stannous chloride added in each ton of the synthetic hydrochloric acid for industry is 0.001 percent of the amount of the synthetic hydrochloric acid for industry.
Step two: after the reaction is finished, the discharging valve 11 of the hydrochloric acid raw material storage tank and the feeding valve 12 of the metering tank are opened, the dechlorination raw material enters the metering tank 2, the discharging valve 11 of the hydrochloric acid raw material storage tank and the feeding valve 12 of the metering tank are closed after the liquid level of the dechlorination raw material reaches 1500mm, the feeding pump 7 is started, the dechlorination raw material is pumped into the elevated tank 3, the volume of the dechlorination raw material entering the elevated tank 3 is not more than three quarters of the total volume of the elevated tank, the set liquid level height is 1300mm, the elevated tank 3 is linked with the feeding pump 7, the feeding pump is automatically closed when the liquid level of the dechlorination raw material entering the elevated tank 3 is higher than 80% of the set liquid level height, the feeding pump 7 is automatically started when the liquid level of the dechlorination raw material entering the elevated tank 3 is lower than 50% of the set liquid level height, automatic linkage feeding is ensured.
Step three: the discharge valve 13 of the elevated tank is opened to enable the dechlorination raw material to flow into the upper half part of the finished product condenser 8 for preheating (the preheating aims are to fully utilize the heat of the gas-phase hydrochloric acid distilled by the hydrochloric acid distiller 9 to heat the dechlorination raw material and then flow into the hydrochloric acid distiller 9 for heating and distilling, and steam is saved). Then the hydrochloric acid flows into a hydrochloric acid distiller 9 to be heated and distilled, a circulating water valve 14 of a finished product condenser 8 is opened, circulating water enters the finished product condenser 8, a steam self-control regulating valve 15 is opened and interlocked with the pressure of the circulating water, the interlocking is set to be that when the pressure of the circulating water is less than 0.1MPa, the steam self-control regulating valve 15 is closed, when the pressure of the circulating water is more than 0.1MPa, the steam self-control regulating valve 15 is opened, the pressure value displayed by a steam pressure gauge 16 is strictly controlled at 0.25MPa, the hydrochloric acid distiller 9 is heated to 88 ℃, a dechlorination raw material is heated to be boiled, and distilled gas-phase hydrochloric acid returns to the finished product condenser. The condensed hydrochloric acid is collected and flows into a finished product receiving groove 4, and the dilute acid flows into a dilute acid receiving groove 5 after being cooled by a dilute acid cooler 10.
The index of the finished product of the continuous production of the high-purity hydrochloric acid is controlled to be 36 percent~38 percent, free chlorine less than or equal to 0.000005 percent, iron (Fe) less than or equal to 0.000001 percent, tin (Sn) less than or equal to 0.00002 percent, copper (Cu) less than or equal to 0.000001 percent, arsenic (As) less than or equal to 0.000001 percent, lead (Pb) less than or equal to 0.000001 percent, Sulfate (SO)4) Less than or equal to 0.00005 percent and Sulfite (SO)3) Less than or equal to 0.00005 percent, less than or equal to 0.0002 percent of ignition residues and less than or equal to 5 percent of chroma/Wuzhen unit.
The following is a comparative table of the test results:
it should be understood that parts of the specification not set forth in detail are well within the prior art. The above examples are only for describing the preferred embodiments of the present invention, and are not intended to limit the scope of the present invention, and various modifications and improvements made to the technical solution of the present invention by those skilled in the art without departing from the spirit of the present invention should fall within the protection scope defined by the claims of the present invention.
Claims (2)
1. A method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid is characterized by comprising the following steps:
the method comprises the following steps: adding stannous chloride into a hydrochloric acid raw material storage tank filled with hydrochloric acid raw material, and circularly stirring for reaction for 1-2 hours to obtain dechlorination raw material; the adding amount of the stannous chloride is added according to the concentration of free chlorine in the hydrochloric acid raw material, when the free chlorine in the synthetic hydrochloric acid for the chlor-alkali industry is more than 1ppm and less than 10ppm, 0.02-0.08 kg of the stannous chloride is added in each ton of the hydrochloric acid raw material, and when the free chlorine in the hydrochloric acid raw material is more than 10ppm, the adding amount of the stannous chloride in each ton of the hydrochloric acid raw material is 0.0001-0.001% of the amount of the hydrochloric acid raw material;
step two: after the reaction is finished, opening a discharging valve of a hydrochloric acid raw material storage tank and a feeding valve of a metering tank, enabling a dechlorination raw material to enter the metering tank, closing the discharging valve of the hydrochloric acid raw material storage tank and the feeding valve of the metering tank after the liquid level of the dechlorination raw material reaches 1200-1500 mm, opening a feeding pump, pumping the dechlorination raw material into a head tank, enabling the volume of the dechlorination raw material entering the head tank to be no more than three quarters of the total volume of the head tank, setting the height of the liquid level to be 1000-1300 mm, interlocking the head tank with the feeding pump, automatically closing the feeding pump when the height of the liquid level of the dechlorination raw material entering the head tank is higher than 80% of the set height of the liquid level, and automatically opening the feeding pump when the height of the liquid level of the dechlorination raw material entering the head tank is lower;
step three: opening a discharge valve of the head tank to enable the dechlorination raw material to flow into the upper half part of a finished product condenser for preheating, then flowing into a hydrochloric acid distiller for heating and distilling, opening a circulating water valve of the finished product condenser to enable circulating water to enter the finished product condenser, simultaneously opening a steam self-control regulating valve, interlocking with the pressure of the circulating water, setting the interlocking to be that when the pressure of the circulating water is less than 0.1MPa, the steam self-control regulating valve is closed, when the pressure of the circulating water is more than 0.1MPa, the steam self-control regulating valve is opened, and the pressure value displayed by a steam pressure gauge is controlled between 0.10MPa and 0.25MPa, so that the hydrochloric acid distiller is heated to 84-88 ℃, the dechlorination raw material is heated to be boiled, and the distilled gas-; the condensed hydrochloric acid is collected and flows into a finished product receiving groove, and the dilute acid is cooled by a dilute acid cooler and then flows into a dilute acid receiving groove 5.
2. The method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid as claimed in claim 1, wherein the hydrochloric acid is industrial synthetic hydrochloric acid of chlor-alkali, and the total acidity is equal to or greater than 31% by mass of HCl.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110370173.2A CN113003539A (en) | 2021-04-07 | 2021-04-07 | Method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110370173.2A CN113003539A (en) | 2021-04-07 | 2021-04-07 | Method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113003539A true CN113003539A (en) | 2021-06-22 |
Family
ID=76388381
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110370173.2A Pending CN113003539A (en) | 2021-04-07 | 2021-04-07 | Method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113003539A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115006975A (en) * | 2022-05-07 | 2022-09-06 | 南通星球石墨股份有限公司 | Method for recycling hydrogen chloride in dichlorobenzene byproducts |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1165110A (en) * | 1997-06-19 | 1997-11-19 | 刘建昆 | Method and equipment for preparing reagent grade hydrochloric acid |
| WO2010064552A1 (en) * | 2008-12-03 | 2010-06-10 | 住友化学株式会社 | Hydrochloric acid purifying method |
| CN103879964A (en) * | 2014-04-03 | 2014-06-25 | 苏州晶瑞化学有限公司 | Continuous production method of high-purity hydrochloric acid |
| CN110436416A (en) * | 2019-08-19 | 2019-11-12 | 四川金山制药有限公司 | A kind of technique preparing electronic grade hydrochloric acid except free chlorine |
| CN111960384A (en) * | 2020-08-26 | 2020-11-20 | 浙江凯圣氟化学有限公司 | Method for removing free chlorine in hydrochloric acid |
-
2021
- 2021-04-07 CN CN202110370173.2A patent/CN113003539A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1165110A (en) * | 1997-06-19 | 1997-11-19 | 刘建昆 | Method and equipment for preparing reagent grade hydrochloric acid |
| WO2010064552A1 (en) * | 2008-12-03 | 2010-06-10 | 住友化学株式会社 | Hydrochloric acid purifying method |
| CN103879964A (en) * | 2014-04-03 | 2014-06-25 | 苏州晶瑞化学有限公司 | Continuous production method of high-purity hydrochloric acid |
| CN110436416A (en) * | 2019-08-19 | 2019-11-12 | 四川金山制药有限公司 | A kind of technique preparing electronic grade hydrochloric acid except free chlorine |
| CN111960384A (en) * | 2020-08-26 | 2020-11-20 | 浙江凯圣氟化学有限公司 | Method for removing free chlorine in hydrochloric acid |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115006975A (en) * | 2022-05-07 | 2022-09-06 | 南通星球石墨股份有限公司 | Method for recycling hydrogen chloride in dichlorobenzene byproducts |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101899665B (en) | Method for recycling copper from acid copper chloride etching liquid | |
| CN101270490B (en) | Dissipated metal indium chloride/chloridization 1-methyl-3-butyl imidazole system plating solution | |
| CN101984097A (en) | Method for comprehensive recovery of heavy metal from spent solder stripper | |
| WO2008139021A1 (en) | Metthod of regeneration method of acid cupper(ii)chloride etching waste | |
| CN106185810B (en) | A kind of joint disposal technique of acidic copper chloride waste etching solution | |
| CN102140578B (en) | Molybdenum-tungsten separating process for molybdenum-tungsten mixed ammonium salt solution in tungsten hydrometallurgy | |
| CN101701292A (en) | Method for recovering indium and tin from ITO waste targets by utilizing oxidation method | |
| CN113003539A (en) | Method for removing free chlorine in hydrochloric acid to obtain high-purity hydrochloric acid | |
| CN101367542A (en) | Preparation method for high purity silver nitrate | |
| CN108658096B (en) | Ammonium sulfate production method using coke oven gas as raw material | |
| CN102943284A (en) | Preparation method of indium electrolyte solution | |
| CN105862068B (en) | A kind of synthetic method of stannous chloride | |
| CN110029354B (en) | Method for preparing battery-grade lithium hydroxide by direct electrolysis of lithium chloride | |
| CN111204725A (en) | Wet-process phosphoric acid extraction spent acid purification process based on ion exchange membrane | |
| CN103086329A (en) | Method for producing electronic-grade sulfuric acid through falling film crystallization | |
| CN106565455A (en) | Electronic grade malonic acid | |
| CN109536992A (en) | A kind of method of two de- two products purifying copper electrolytes | |
| CN101332977A (en) | Method for separating free chlorine in dilute hydrochloric acid | |
| CN114381612A (en) | Industrialization method for purifying lead by vacuum method | |
| CN104610407B (en) | The process for purification of hydrocortisone acetate | |
| CN1249135C (en) | Method for recovering perfluoro caprylic acid from waste liquid of producing teflon resin | |
| CN103112872B (en) | Preparation method of ultrapure fluorine-ammonium etching solution for micro-electronics | |
| CN217612990U (en) | Reflux water replenishing system of azeotropic distillation tower in acetic acid recovery process | |
| CN110330423A (en) | The method that pressurization prepares stannous octoate | |
| CN115872839B (en) | Preparation method of high-purity glycerol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20210622 |