CN110127615B - On-line purification method of hydrochloric acid in process of producing potassium sulfate by Mannheim method - Google Patents
On-line purification method of hydrochloric acid in process of producing potassium sulfate by Mannheim method Download PDFInfo
- Publication number
- CN110127615B CN110127615B CN201910380684.5A CN201910380684A CN110127615B CN 110127615 B CN110127615 B CN 110127615B CN 201910380684 A CN201910380684 A CN 201910380684A CN 110127615 B CN110127615 B CN 110127615B
- Authority
- CN
- China
- Prior art keywords
- tower
- hydrochloric acid
- stage
- distillation
- enters
- 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.)
- Active
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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/02—Preparation of sulfates from alkali metal salts and sulfuric acid or bisulfates; Preparation of bisulfates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/06—Preparation of sulfates by double decomposition
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses an online purification method of hydrochloric acid in the process of producing potassium sulfate by a Mannheim method, wherein gas discharged from a Mannheim furnace is cooled by a cooler, and then enters a first-stage washing tower, a second-stage washing tower, a third-stage falling film absorption tower and a fourth-stage washing tower in sequence and is emptied; washing liquid obtained by washing and absorbing the environment-friendly tail gas by deionized water sequentially enters a second-stage washing tower and a first-stage washing tower to be washed, and finally hydrochloric acid B is obtained, the hydrochloric acid B enters a distillation tower to be distilled, distilled fractions are cooled to obtain food-grade hydrochloric acid, the deionized water washes hydrogen chloride gas in a fourth-stage washing tower, the hydrogen chloride gas enters a third-stage falling film absorption tower to be absorbed, and gas distilled by the distillation tower enters a third-stage falling film absorption tower to be absorbed to obtain hydrochloric acid A; the heat required by the distillation tower is provided by tail gas generated by a combustion chamber which provides heat for the Mannheim furnace. The invention utilizes the waste heat of the tail gas of the combustion chamber to carry out on-line distillation and purification on the hydrochloric acid, and can obtain the food-grade hydrochloric acid.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to an online purification method of hydrochloric acid in a process of producing potassium sulfate by a Mannheim method.
Background
The process for producing potassium sulfate by Mannheim method is characterized by that the sulfuric acid and potassium chloride are reacted in Mannheim furnace under the condition of high temp. to produce potassium sulfate and produce hydrogen chloride, the hydrogen chloride is absorbed by water to produce hydrochloric acid, and the potassium sulfate is cooled to obtain the invented product. The Mannheim method is the most mature and reliable method for producing potassium sulfate with the most stable quality.
However, the hydrogen chloride gas generated by the mannheim process contains a small amount of impurities such as water vapor, sulfuric acid gas, potassium sulfate dust, potassium chloride dust and the like, and the impurities and the hydrogen chloride gas exist in a mist form, so that the hydrochloric acid impurities obtained by absorption according to the existing mature technical method (as shown in fig. 1) are high in content, low in quality and limited in application, and enterprises need to pay additional fees to entrust other people to consume the impurities, so that certain economic losses are brought to the enterprises.
Disclosure of Invention
The invention provides an online purification method of hydrochloric acid in a process of producing potassium sulfate by a Mannheim method, which can utilize the waste heat of tail gas of a combustion chamber in the process of producing the potassium sulfate by the Mannheim method to carry out online distillation and purification on the hydrochloric acid to obtain food-grade hydrochloric acid.
The technical scheme adopted by the invention is that the online purification method of hydrochloric acid in the process of producing potassium sulfate by using the Mannheim method is characterized by comprising the following steps:
cooling the gas from the Mannheim furnace by a cooler, and then sequentially entering a first-stage washing tower, a second-stage washing tower, a third-stage falling film absorption tower and a fourth-stage washing tower for emptying; washing liquid obtained by washing and absorbing the environment-friendly tail gas by deionized water sequentially enters a secondary washing tower and a primary washing tower for washing to finally obtain hydrochloric acid B, the hydrochloric acid B enters a distillation tower for distillation, the distilled fraction is cooled to obtain food-grade hydrochloric acid, the deionized water washes hydrogen chloride gas in a quaternary washing tower, the hydrogen chloride gas enters a tertiary falling film absorption tower for absorbing hydrogen chloride gas, and the gas distilled by the distillation tower enters a tertiary falling film absorption tower for absorbing to obtain hydrochloric acid A; the heat required by the distillation tower is provided by tail gas generated by a combustion chamber which provides heat for the Mannheim furnace. The temperature of tail gas generated by the combustion chamber is 245-295 ℃ after the tail gas is cooled by a cooler, and the flow of the tail gas is 10-14 m3/s。
Further, the environment-friendly tail gas is the tail gas collected in the production environment in the process of producing potassium sulfate by the Mannheim method.
Further, the residual liquid part of the distillation tower enters a first-stage washing tower to be used as washing liquid for circular washing.
Further, the flow ratio of the hydrochloric acid B entering the distillation tower to the flow ratio of the distillation raffinate entering the first-stage washing tower is 2: 1-4: 1.
Further, when the sulfate concentration in the distillation raffinate exceeds 30wt%, the raffinate is evaporated to dryness, and the residue is directly fed into a Mannheim furnace to produce potassium sulfate.
Further, gas generated in the Mannheim furnace is introduced into a cooler by adopting a draught fan behind a four-stage washing tower for cooling, and then enters a first-stage washing tower, a second-stage washing tower, a three-stage falling film absorption tower and a four-stage washing tower in sequence.
The invention has the following beneficial effects:
1. the hydrochloric acid B coming out of the first-stage washing tower directly enters a distillation tower for distillation without being cooled, and a distillate enters an acid storage tank through condensation to obtain the food-grade hydrochloric acid, so that the added value of the product is greatly improved, and the problem that the hydrochloric acid is high in impurity content and difficult to utilize is solved. And the hydrogen chloride tail gas generated in the distillation process almost does not contain impurities, and directly enters a three-stage falling film absorption tower to be absorbed, so that the hydrochloric acid A is obtained. The hydrochloric acid B does not undergo temperature reduction, so that the energy required by distillation can be reduced, and the distillation time can be shortened.
2. The heat required in the distillation process of the hydrochloric acid B is provided by tail gas generated by a combustion chamber for providing heat for a Mannheim furnace, the temperature of the tail gas is about 500 ℃, and the flow of the tail gas is 10-14 m3And s. In the prior art, the temperature is generally reduced to below 300 ℃ and then the waste gas is directly discharged into the air. The invention adopts the heat of the tail gas of the combustion chamber to completely meet the distillation and purification requirements of the hydrochloric acid B, the tail gas of the combustion chamber is introduced into the distillation tower through the induced draft fan to heat the hydrochloric acid B by adopting immersion, the tail gas after heat exchange is discharged into the air through the exhaust pipe, and the waste heat in the production process of the Mannheim method is fully utilized.
3. In the distillation process of the hydrochloric acid B, the hydrogen chloride gas distilled out has high purity and enters a three-stage falling film absorption tower to be absorbed, so that the quality of the hydrochloric acid A is improved.
4. In the distillation process of the hydrochloric acid B, certain residual liquid is kept in the distillation tower, the content of hydrogen chloride in the residual liquid is low, the residual liquid can directly enter a first-stage washing tower to continuously wash and absorb hydrogen chloride gas,the dosage of the deionized water in the four-stage washing tower can be reduced by the same amount. But when sulfate (in SO) is present in the raffinate4 2-Calculated), the residual liquid needs to be evaporated to dryness, the residue directly enters a Mannheim furnace to produce potassium sulfate, and the main components in the residue are potassium chloride and potassium sulfate. The part of the impurities can be recycled through treatment.
5. The method provided by the invention provides heat for tail gas generated by a combustion chamber for providing heat for a Mannheim furnace, and the absorbed hydrochloric acid is distilled and purified, so that online purification can be realized, no additional energy consumption is caused, the purification cost of the hydrochloric acid is low, the quality of the purified hydrochloric acid is good, and no three wastes are discharged in the whole process.
Drawings
FIG. 1 is a flow chart of the process for gas absorption from the foreman furnace using the process of the present invention.
FIG. 2 is a flow chart of the on-line purification process of hydrochloric acid in the process of producing potassium sulfate by the Mannheim method of the present invention.
Detailed Description
The invention will be further illustrated by reference to the following examples (taking a 30 ton daily potassium sulfate production line as an example).
Comparative example:
as shown in figure 1, gas from a Mannheim furnace (flow rate is 13500L/min, flow rate is 3.7m/s, and HCl content is about 50%) is cooled by a cooler, and then sequentially passes through a first-stage washing tower (tower height is 10m, tower diameter is 1.45m, and internal circulation amount is 40L/min), a second-stage washing tower (tower height is 10m, tower diameter is 1.45m, and internal circulation amount is 40L/min), a third-stage falling film absorption tower (tower height is 10m, tower diameter is 1.45m, and internal circulation amount is 40L/min), and a fourth-stage washing tower (tower height is 10m, tower diameter is 1.45m, and internal circulation amount is 40L/min), and then is emptied, deionized water (flow rate is 9.44L/min) is washed from the fourth-stage washing tower to absorb hydrogen chloride gas, and then enters the third-stage falling film absorption tower to absorb hydrogen chloride gas to obtain 32% hydrochloric acid A, wherein the yield of hydrochloric acid A is 20 tons/day. Tail gas in a production environment collected in the process of producing potassium sulfate by using a Mannheim method is washed by deionized water (the flow is 7.08L/min), and washing liquid collected after washing is discharged from a primary washing tower after being washed and absorbed by a secondary washing tower and the primary washing tower in sequence to obtain 32% hydrochloric acid B, wherein the yield of the hydrochloric acid B is 15 tons/day.
The flow rate of the washing liquid entering the second-stage washing tower and the first-stage washing tower is 7.08L/min.
The quality of the obtained hydrochloric acid is detected as the following table 1:
| item | Sulfate (SO)4 2-,％) | Fe3+(％) | HCl(％) | Colour(s) |
| Hydrochloric acid A | 0.02 | 0.0008 | 32.2 | Light yellow |
| Hydrochloric acid B | 1.25 | 0.003 | 32.3 | Yellow colour |
TABLE 1
The content of hydrogen chloride in the tail gas is as follows: 5.11mg/m3And meets the environmental emission standard.
The waste heat temperature of the tail gas of a combustion chamber for heating the Mannheim furnace is about 500 ℃, and the waste heat temperature is reducedDirectly discharging the waste gas into the air after the temperature reaches 245-295 ℃, wherein the flow of the tail gas is 10-14 m3/s。
The invention provides an online purification method of hydrochloric acid in the process of producing potassium sulfate by a Mannheim method, the technological process is shown in figure 2, gas (flow is 13500L/min, flow rate is 3.7m/s, HCl content is about 50%) from a Mannheim furnace is cooled by a cooler, and then enters a first-stage washing tower (tower height is 10m, tower diameter is 1.45m, internal circulation amount is 40L/min), a second-stage washing tower (tower height is 10m, tower diameter is 1.45m, internal circulation amount is 40L/min), a third-stage falling film absorption tower (tower height is 10m, tower diameter is 1.45m, internal circulation amount is 40L/min) and a fourth-stage washing tower (tower height is 10m, tower diameter is 1.45m, internal circulation amount is 40L/min) in sequence and then is emptied; washing and absorbing environment-friendly tail gas (gas collected in the environment of producing potassium sulfate by the Mannheim method) by deionized water (flow is 7.08L/min) to obtain washing liquid, sequentially feeding the washing liquid into a second-stage washing tower and a first-stage washing tower for washing to obtain hydrochloric acid B, feeding the hydrochloric acid B (flow is 7.08-14.16L/min) into a distillation tower for distillation, cooling distilled fractions to obtain food-grade hydrochloric acid (yield is 10-15 tons/day), and feeding the distilled gas into a third-stage falling film absorption tower for absorption to obtain hydrochloric acid A; washing the hydrogen chloride gas in the four-stage washing tower by deionized water (the flow is 9.44-11.8L/min), and absorbing the hydrogen chloride gas in a three-stage falling film absorption tower to obtain hydrochloric acid A (the yield is 20-25 tons/day); the heat required by the distillation tower is tail gas (the tail gas temperature is 245-295 ℃, and the tail gas flow is 10-14 m) generated by a combustion chamber for providing heat for the Mannheim furnace3And/s) is provided. The hydrochloric acid can be distilled and purified on line by utilizing the waste heat of the tail gas of a combustion chamber in the process of producing the potassium sulfate by using the Mannheim method, so that the food-grade hydrochloric acid is obtained.
Furthermore, the temperature of tail gas generated by the combustion chamber is 245-295 ℃, and the flow of the tail gas is 10-14 m3/s。
Further, cooling the gas phase of the distillation tower to obtain food-grade hydrochloric acid (yield is 10-15 tons/day), and introducing the residual gas into a three-stage falling film absorption tower to be absorbed to obtain hydrochloric acid A (yield is 20-25 tons/day); and (4) allowing part of residual liquid in the distillation tower to enter a first-stage washing tower to be used as washing liquid for circular washing.
Further, tail gas in the production environment collected in the process of producing potassium sulfate by the Mannheim method is washed by deionized water, and washing liquid collected after washing sequentially enters a secondary washing tower and a primary washing tower for washing, so that hydrochloric acid B is finally obtained.
Further, the ratio of the flow rate of the hydrochloric acid B entering the distillation tower to the flow rate of the distillation waste liquid entering the primary washing tower is 2: 1-4: 1.
Further, when the concentration of sulfate in the residual liquid exceeds 30%, evaporating the residual liquid to dryness to obtain 297-301 kg of distillation residue, and directly feeding the residue into a Mannheim furnace to produce potassium sulfate.
The quality standards of the food grade hydrochloric acid are shown in table 2 below.
TABLE 2
The concrete cases are as follows:
example 1:
pumping the hydrochloric acid B in the first-stage washing tower into a hydrochloric acid distillation tower (with the flow rate of 14.16L/min), introducing the hydrochloric acid B into the hydrochloric acid distillation tower at 245 ℃ and with the flow rate of 10m3The combustion chamber tail gas/s is distilled. The flow rate of the residual liquid entering the first-stage washing tower is 7.08L/min, and the distillate enters an acid storage tank through condensation to obtain the food-grade hydrochloric acid. The food-grade hydrochloric acid is clear in color, the sulfate content is 0.002%, the iron salt content is 0.0005%, the acid concentration is 32.7%, and the yield is 15 tons/day.
Deionized water (the flow is 9.44L/min) is used for washing the hydrogen chloride gas in the four-stage washing tower, the hydrogen chloride gas enters the three-stage falling film absorption tower to be absorbed, the hydrogen chloride tail gas generated in the distillation tower also directly enters the three-stage falling film absorption tower to be absorbed, and finally the hydrochloric acid A is obtained. The hydrochloric acid A is clear in color, 0.003 percent of sulfate, 0.0005 percent of iron salt and 32.5 percent of acid concentration, and the yield is 20 tons/day.
When the concentration of sulfate in the raffinate exceeds 30%, the raffinate is evaporated to dryness to obtain 298kg of distillation residue.
Example 2:
pumping hydrochloric acid B into a first-stage washing tower (with the flow rate of 14.16L/min) to distill hydrochloric acidIntroducing into a distillation tower at 295 deg.C and with a flow rate of 14m3The combustion chamber tail gas/s is distilled. The flow rate of the residual liquid entering the first-stage washing tower is 3.54L/min, and the distillate enters an acid storage tank through condensation to obtain the food-grade hydrochloric acid. The food-grade hydrochloric acid is clear in color, the sulfate content is 0.001%, the iron salt content has no definite value, the acid concentration is 33.6%, and the yield is 10 tons/day.
Deionized water (the flow is 11.80L/min) washes hydrogen chloride gas in the four-stage washing tower, the hydrogen chloride gas enters the three-stage falling film absorption tower to be absorbed, hydrogen chloride tail gas generated in the distillation tower also directly enters the three-stage falling film absorption tower to be absorbed, and finally hydrochloric acid A is obtained. The hydrochloric acid A is clear in color, 0.003 percent of sulfate, 0.0005 percent of iron salt and 32.6 percent of acid concentration, and the yield is 25 tons/day.
When the concentration of sulfate in the raffinate exceeded 30%, the raffinate was evaporated to dryness to obtain 301kg of distillation residue.
Example 3:
pumping hydrochloric acid B in the first stage washing tower into a hydrochloric acid distillation tower (flow rate is 9.44L/min), introducing into the hydrochloric acid distillation tower at 260 deg.C and flow rate of 13.7m3The combustion chamber tail gas/s is distilled. The flow rate of the residual liquid entering the first-stage washing tower is 3.14L/min, and the distillate enters an acid storage tank through condensation to obtain the food-grade hydrochloric acid. The food-grade hydrochloric acid is clear in color, the sulfate content is 0.001%, the iron salt content is 0.0005%, the acid concentration is 32.1%, and the yield is 13.3 tons/day.
Deionized water (the flow is 10.24L/min) is used for washing the hydrogen chloride gas in the four-stage washing tower, the hydrogen chloride gas enters the three-stage falling film absorption tower to be absorbed, the hydrogen chloride tail gas generated in the distillation tower also directly enters the three-stage falling film absorption tower to be absorbed, and finally, hydrochloric acid A is obtained. Hydrochloric acid A was clear, with a sulfate content of 0.003%, an iron salt content of 0.0005%, an acid concentration of 32.4%, and a yield of 21.7 tons/day.
When the concentration of sulfate in the raffinate exceeded 30%, the raffinate was evaporated to dryness to obtain 297kg of distillation residue.
Example 4:
pumping hydrochloric acid B in the first stage washing tower into a hydrochloric acid distillation tower (with the flow rate of 7.08L/min), introducing 285 ℃ and the flow rate of 14m3The combustion chamber tail gas/s is distilled.The flow rate of the residual liquid entering the first-stage washing tower is 3.54L/min, and the distillate enters an acid storage tank through condensation to obtain the food-grade hydrochloric acid. The food-grade hydrochloric acid is clear in color, the sulfate content is 0.001%, the iron salt content is 0.0005%, the acid concentration is 32.8%, and the yield is 10 tons/day.
Deionized water (the flow is 11.80L/min) washes hydrogen chloride gas in the four-stage washing tower, the hydrogen chloride gas enters the three-stage falling film absorption tower to be absorbed, hydrogen chloride tail gas generated in the distillation tower also directly enters the three-stage falling film absorption tower to be absorbed, and finally hydrochloric acid A is obtained. The hydrochloric acid A is clear in color, 0.003 percent of sulfate, 0.0005 percent of iron salt and 32.5 percent of acid concentration, and the yield is 25 tons/day.
When the concentration of sulfate in the raffinate exceeds 30%, the raffinate is evaporated to dryness to obtain 300kg of distillation residue.
Example 5:
pumping hydrochloric acid B in the first stage washing tower into a hydrochloric acid distillation tower (with the flow rate of 12.03L/min), introducing into the hydrochloric acid distillation tower at 258 ℃, and introducing the hydrochloric acid distillation tower at the flow rate of 12.2m3The combustion chamber tail gas/s is distilled. The flow rate of the residual liquid entering the first-stage washing tower is 6.00L/min, and the distillate enters an acid storage tank through condensation to obtain the food-grade hydrochloric acid. The food-grade hydrochloric acid is clear in color, the sulfate content is 0.001%, the iron salt content is 0.0005%, the acid concentration is 32.3%, and the yield is 12.8 tons/day.
Deionized water (the flow is 10.48L/min) is used for washing the hydrogen chloride gas in the four-stage washing tower, the hydrogen chloride gas enters the three-stage falling film absorption tower to be absorbed, the hydrogen chloride tail gas generated in the distillation tower also directly enters the three-stage falling film absorption tower to be absorbed, and finally, hydrochloric acid A is obtained. Hydrochloric acid A was clear, with a sulfate content of 0.003%, an iron salt content of 0.0005%, an acid concentration of 32.7%, and a yield of 22.3 tons/day.
When the concentration of sulfate in the raffinate exceeds 30%, the raffinate is evaporated to dryness to obtain 299kg of distillation residue.
Claims (5)
1. The online purification method of hydrochloric acid in the process of producing potassium sulfate by the Mannheim method is characterized by comprising the following steps:
cooling the gas from the Mannheim furnace by a cooler, and then sequentially entering a first-stage washing tower, a second-stage washing tower, a third-stage falling film absorption tower and a fourth-stage washing tower and then emptying; washing liquid obtained by washing and absorbing the environment-friendly tail gas by deionized water sequentially enters a second-stage washing tower and a first-stage washing tower to be washed, and finally hydrochloric acid B is obtained, the hydrochloric acid B enters a distillation tower to be distilled, distilled fractions are cooled to obtain food-grade hydrochloric acid, the deionized water washes hydrogen chloride gas in a fourth-stage washing tower, the hydrogen chloride gas enters a third-stage falling film absorption tower to be absorbed, and gas distilled by the distillation tower enters a third-stage falling film absorption tower to be absorbed to obtain hydrochloric acid A; the heat required by the distillation tower is provided by tail gas generated by a combustion chamber for providing heat for the Mannheim furnace; the residual liquid part of the distillation tower enters a first-stage washing tower to be used as washing liquid for circular washing; the flow ratio of the hydrochloric acid B entering the distillation tower to the flow ratio of the distillation residual liquid entering the primary washing tower is 2: 1-4: 1.
2. The method of claim 1, wherein: the environment-friendly tail gas is the tail gas collected in the production environment in the process of producing potassium sulfate by the Mannheim method.
3. The method of claim 1, wherein: when the sulfate concentration in the distillation raffinate exceeds 30wt%, the raffinate is evaporated to dryness, and the residue is directly fed into a Mannheim furnace to produce potassium sulfate.
4. The method of claim 1, wherein: and the gas generated in the Mannheim furnace is introduced into a cooler by adopting a draught fan behind a four-stage washing tower, and then enters a first-stage washing tower, a second-stage washing tower, a three-stage falling film absorption tower and a four-stage washing tower in sequence.
5. The method of claim 1, wherein: and the temperature of tail gas generated by the combustion chamber is 245-295 ℃ after the tail gas is cooled by a cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910380684.5A CN110127615B (en) | 2019-05-08 | 2019-05-08 | On-line purification method of hydrochloric acid in process of producing potassium sulfate by Mannheim method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910380684.5A CN110127615B (en) | 2019-05-08 | 2019-05-08 | On-line purification method of hydrochloric acid in process of producing potassium sulfate by Mannheim method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110127615A CN110127615A (en) | 2019-08-16 |
| CN110127615B true CN110127615B (en) | 2022-07-22 |
Family
ID=67576855
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910380684.5A Active CN110127615B (en) | 2019-05-08 | 2019-05-08 | On-line purification method of hydrochloric acid in process of producing potassium sulfate by Mannheim method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110127615B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112158862B (en) * | 2020-05-15 | 2021-06-29 | 青岛碱业钾肥科技有限公司 | Production method of low-chlorine potassium sulfate |
| CN112794345B (en) * | 2021-01-20 | 2022-12-27 | 宁夏中泰富瑞科技有限公司 | Equipment for preparing potassium sulfate from potassium chloride and manufacturing process thereof |
| CN114288841A (en) * | 2021-12-31 | 2022-04-08 | 山东三方化工集团有限公司 | Mannheim method potassium sulfate tail gas processing system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106554019A (en) * | 2015-09-29 | 2017-04-05 | 新特能源股份有限公司 | A kind of technique of trichlorosilane synthetic tail gas cleaning system |
| CN206424751U (en) * | 2016-12-23 | 2017-08-22 | 青上化工（惠州）有限公司 | A kind of 7th grade of recovery tower of hydrochloric acid tail gas |
-
2019
- 2019-05-08 CN CN201910380684.5A patent/CN110127615B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106554019A (en) * | 2015-09-29 | 2017-04-05 | 新特能源股份有限公司 | A kind of technique of trichlorosilane synthetic tail gas cleaning system |
| CN206424751U (en) * | 2016-12-23 | 2017-08-22 | 青上化工（惠州）有限公司 | A kind of 7th grade of recovery tower of hydrochloric acid tail gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110127615A (en) | 2019-08-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN110127615B (en) | On-line purification method of hydrochloric acid in process of producing potassium sulfate by Mannheim method | |
| CN102247708B (en) | Process for treating tail gas of rare earth mineral powder and concentrated sulphuric acid roasting process | |
| WO2016119720A1 (en) | System and method for highly effective chlorination and vanadium extraction from vanadium slag | |
| RU2662515C1 (en) | System and method of purification vanadium pentoxide | |
| CN104828995A (en) | Treatment method of ferrous waste hydrochloric acid | |
| RU2663777C1 (en) | System and method for producing high-purity vanadium pentoxide powder | |
| US10099939B2 (en) | System and method for producing high-purity vanadium pentoxide powder | |
| AU2016212453B2 (en) | System and method for producing high-purity vanadium tetraoxide powder | |
| CN107892280A (en) | A kind of high concentration SO2The method of metallurgical off-gas acid-making | |
| CN104495953A (en) | Process for treating industrial waste hydrochloric acid in recycling way through salt fractionation method | |
| CN102424368A (en) | Process for removing F, Cl and As from waste acid by hot air concentration method | |
| CN203741248U (en) | Improved oxidation reaction and tail gas adsorption device for synthesizing glyoxylic acid | |
| CN104087691A (en) | Process for recycling waste heat of slag flushing water vapor and dispersing fog and equipment adopted in same | |
| CN105819607A (en) | Equipment and method for treating acid-containing waste water | |
| CN102530893B (en) | Nitric acid extraction and concentration method | |
| CN103613127B (en) | The recoverying and utilizing method of low boilers in titanium tetrachloride production | |
| CN206940519U (en) | A kind of recycling vulcanizing treatment system of acid waste water containing heavy metal | |
| CN108298507B (en) | Method and device for treating sulfur-containing flue gas generated by calcining petroleum coke by using pyrite acid making device | |
| CN105731394A (en) | Refined sulfuric acid preparation device and preparation method thereof | |
| CN212769875U (en) | Purification system of gas distribution acid making process | |
| CN113213433B (en) | Method for directly preparing sulfuric acid for storage battery by using secondary lead smelting flue gas | |
| CN211595042U (en) | Smelting flue gas acid making device | |
| CN102745652B (en) | Technology for producing sulphuric acid purification feed gas by using medium or low concentration waste acid | |
| CN106167326A (en) | A kind of useless acid treatment process | |
| CN106139823B (en) | A kind of comprehensive reutilization method of coal chemical industry transformation condensate liquid stripping tail gas |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |