CN217526949U - Production device of high-concentration hydrochloric acid - Google Patents
Production device of high-concentration hydrochloric acid Download PDFInfo
- Publication number
- CN217526949U CN217526949U CN202220668793.4U CN202220668793U CN217526949U CN 217526949 U CN217526949 U CN 217526949U CN 202220668793 U CN202220668793 U CN 202220668793U CN 217526949 U CN217526949 U CN 217526949U
- Authority
- CN
- China
- Prior art keywords
- hydrochloric acid
- falling film
- film absorber
- pipeline
- gas
- 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
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a hydrochloric acid apparatus for producing technical field, concretely relates to apparatus for producing of high concentration hydrochloric acid. The production device comprises a synthesis furnace, a primary falling film absorber, a secondary falling film absorber, an absorption tower and a tail gas alkaline washing tower, wherein a jacket of the synthesis furnace is connected with a flash tank, a chlorine pipeline, a hydrogen pipeline and a nitrogen pipeline are connected below the synthesis furnace, and a gas flow monitor and a gas circuit electromagnetic control valve are respectively arranged on the chlorine pipeline and the hydrogen pipeline; the absorption tower is connected with an absorption water pipeline, and a water flow monitor and a waterway electromagnetic control valve are arranged on the absorption water pipeline; hydrogen chloride gas in the synthesis furnace sequentially passes through the primary falling film absorber, the secondary falling film absorber and the absorption tower and then enters the tail gas alkaline washing tower, and the frozen absorption water sequentially passes through the absorption tower, the secondary falling film absorber and the primary falling film absorber and then enters the high-concentration hydrochloric acid storage tank. The production device can stably produce and store 36.5 percent of high-concentration hydrochloric acid, comprehensively utilize reaction heat and increase enterprise benefits.
Description
Technical Field
The utility model relates to a hydrochloric acid apparatus for producing technical field, concretely relates to apparatus for producing of high concentration hydrochloric acid.
Background
Hydrochloric acid is an important basic chemical raw material and has wide application. The synthesis method for preparing hydrochloric acid is generally divided into three stages: synthesis, cooling and absorption of hydrogen chloride gas. The dried hydrogen and chlorine are combusted in the synthesis tower to generate hydrogen chloride gas with the purity of over 95 percent. The high-temperature hydrogen chloride gas led out from the synthesis tower is cooled by an air cooler, then is further cooled to 20-30 ℃ by an impermeable graphite cooler, then is dried by concentrated sulfuric acid by two drying towers, and then is sent into an absorption tower for absorption, the tower top is sprayed with purified water from top to bottom, the hydrogen chloride gas flows up in the countercurrent way, and the tower bottom can obtain concentrated hydrochloric acid with the concentration of about 31%.
The concentration of hydrochloric acid synthesized in chlor-alkali plants in China is generally 31-33%, and the method is mainly used for treating and balancing liquefied tail chlorine. However, the price of 31 percent of concentrated hydrochloric acid is lower, the market price is less than half of that of 36.5 percent of high-concentration hydrochloric acid, and the economic benefit is far lower than that of 36.5 percent of high-concentration hydrochloric acid. Therefore, in order to realize diversification of products and increase enterprise benefits, improvement on the existing production device and process is necessary, and high-concentration hydrochloric acid with the production concentration of more than or equal to 36.5% is produced on the premise of keeping stable production.
Patent CN206751388U discloses a high-concentration hydrochloric acid synthesis system, which comprises a graphite synthesis furnace, a graphite cooler, a first-stage falling film absorber, a second-stage falling film absorber, a tail gas absorption tower, a pure water inlet header pipe, a finished acid storage tank, a circulating water header pipe and an injection pump, wherein the system prepares high-concentration hydrochloric acid by a two-stage falling film absorption technology, the concentration of the synthesized hydrochloric acid reaches 36%, but the higher-concentration hydrochloric acid is difficult to prepare only by the two-stage falling film absorption technology, if the concentration of the hydrochloric acid reaches above 36.5% during delivery, the concentration of the hydrochloric acid is ensured to be about 38% during production, and the storage stability of the high-concentration hydrochloric acid is ensured. Adopt this patent device can't prepare the hydrochloric acid of higher concentration, and the device adopts the graphite cooler to reduce the temperature of hydrogen chloride gas, and does not carry out make full use of to the reaction heat in the production process, and whole energy consumption is higher, and manufacturing cost is high.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is: provides a production device of high-concentration hydrochloric acid, which has simple structure and convenient operation, can stably produce and store 36.5 percent of high-concentration hydrochloric acid, comprehensively utilize reaction heat and increase enterprise benefits.
The utility model relates to a production device of high-concentration hydrochloric acid, which comprises a synthesis furnace, a primary falling film absorber, a secondary falling film absorber, an absorption tower and a tail gas alkaline washing tower which are connected in sequence, wherein a jacket of the synthesis furnace is connected with a flash tank, a chlorine pipeline, a hydrogen pipeline and a nitrogen pipeline are connected below the synthesis furnace, and a gas flow monitor and a gas circuit electromagnetic control valve are respectively arranged on the chlorine pipeline and the hydrogen pipeline; the absorption tower is connected with a freezing absorption water pipeline, and a water flow monitor and a waterway electromagnetic control valve are installed on the freezing absorption water pipeline; hydrogen chloride gas of the synthesis furnace enters a tail gas alkaline washing tower after being absorbed by a primary falling film absorber, a secondary falling film absorber and an absorption tower in sequence, and frozen absorption water enters a high-concentration hydrochloric acid storage tank after being absorbed by the hydrogen chloride gas by the absorption tower, the secondary falling film absorber and the primary falling film absorber in sequence, and the high-concentration hydrochloric acid storage tank is connected with a nitrogen pipeline.
As a preferred scheme, the main body material of the synthetic furnace is composed of graphite and carbon steel, the part which is in contact with hydrogen chloride inside is composed of graphite, and the jacket is composed of carbon steel, and a jacket is reserved in the middle of the jacket and is filled with cooling water to cool the graphite and generate steam.
Preferably, the jacket outlet of the synthesis furnace is connected with the inlet of the flash tank, the outlet of the flash tank is connected with the jacket inlet of the synthesis furnace, and the gas phase outlet of the flash tank is connected with the steam line. High-temperature water or steam in a jacket of the synthesis furnace is utilized through the flash tank, the generated liquid phase is used as cooling water to cool the synthesis furnace again, and the generated high-temperature steam is conveyed to other sections for utilization. The liquid level of the flash tank is monitored at any time, and water shortage is avoided.
Preferably, the inlet of the jacket of the synthesis furnace is also connected with a cooling water pipeline, the jacket of the synthesis furnace is supplemented with cooling water.
As a preferred scheme, a tail gas outlet of the absorption tower is connected with a tail gas alkaline washing tower, an absorption liquid outlet of the tail gas alkaline washing tower is connected with a dilute alkali circulating tank, and the dilute alkali circulating tank is connected with an absorption liquid inlet of the absorption tower through a circulating pump.
As a preferred scheme, the top of the absorption tower is connected with a vent gas line.
As a preferred scheme, a gas phase outlet of the first-stage falling film absorber is connected with a gas phase inlet of the second-stage falling film absorber, and a gas phase outlet of the second-stage falling film absorber is connected with a gas phase inlet of the absorption tower; the liquid phase outlet of the absorption tower is connected with the liquid phase inlet of the secondary falling film absorber, the liquid phase outlet of the secondary falling film absorber is connected with the liquid phase inlet of the primary falling film absorber, and the liquid phase outlet of the primary falling film absorber is connected with the low-concentration hydrochloric acid storage tank and the high-concentration hydrochloric acid storage tank. The frozen absorption water sequentially passes through an absorption tower, a secondary falling film absorber and a primary falling film absorber to absorb hydrogen chloride gas, the concentration of hydrochloric acid at the initial stage of production is lower than 36.5%, the hydrochloric acid is introduced into a concentration hydrochloric acid storage tank for storage, after the production is stable, the concentration of hydrochloric acid can reach more than 38%, the hydrochloric acid is introduced into a high-concentration hydrochloric acid storage tank for storage, meanwhile, nitrogen is introduced into the high-concentration hydrochloric acid storage tank, and the flow rate is 0.5m 3 About/h, is used for inhibiting the high-concentration hydrochloric acid from volatilizing again in the storage tank and ensuring the stable concentration of the productThe content is more than 37%.
As a preferred scheme, the gas flow monitor of the chlorine pipeline is electrically connected with the gas circuit electromagnetic control valve; the gas flow monitor of the hydrogen pipeline is electrically connected with the gas circuit electromagnetic control valve; the freezing water absorption pipeline is electrically connected with the water flow monitor and the waterway electromagnetic control valve.
When 36.5% high-concentration hydrochloric acid is produced, in order to ensure the stable operation of the synthesis furnace during the production period, the flow of the freezing absorption water is controlled by a water flow monitor and a waterway electromagnetic control valve in the early stage to increase the concentration of the hydrochloric acid, when the flow of the freezing absorption water is reduced to a certain range, the pressure of the synthesis furnace is increased by reducing the flow of the freezing absorption water, the stable production can not be ensured, the hydrochloric acid concentration and the furnace pressure of the hydrochloric acid synthetic furnace are stabilized by adjusting the chlorine and hydrogen flow through the gas flow monitor and the electromagnetic control valve of the gas circuit, the hydrochloric acid concentration is ensured to reach over 38 percent, and the stable production of the whole production device is ensured.
The principle of producing hydrochloric acid is as follows: chlorine and hydrogen can be kept in balanced combustion under proper control conditions, a large amount of heat is released in the reaction, the synthesis heat of hydrogen chloride is 92kJ/mol, and the chemical equation is as follows:
H 2 +Cl 2 ＝2HCl。
the hydrogen chloride gas generated by the reaction is dissolved in high-purity water (the hydrogen chloride is absorbed by the high-purity water) to form high-purity hydrochloric acid. This absorption process is essentially the diffusion of hydrogen chloride molecules into water across a gas-liquid two-phase interface. The factors that influence the absorption process have several aspects: (1) influence of temperature: the higher the temperature is, the lower the solubility of the hydrogen chloride is, and the hydrogen chloride can emit large dissolution heat when dissolved in water, so that the solubility of the hydrogen chloride is reduced, therefore, cooling water is introduced into a jacket of the synthesis furnace to remove the dissolution heat and the synthesis heat of the hydrogen chloride, ensure the concentration of acid and improve the capacity of absorbing the hydrogen chloride; (2) influence of the purity of hydrogen chloride: at a certain temperature, the dissolving process depends on the partial pressure of hydrogen chloride gas in a gas phase, namely the purity of hydrogen chloride, and the higher the purity of hydrogen chloride is, the higher the concentration of the prepared hydrochloric acid is; (3) influence of flow rate: according to the double-membrane theory, the larger the flow velocity of the hydrogen chloride gas is, the larger the diffusion speed of hydrogen chloride molecules is, and the higher the absorption efficiency is; (4) influence of gas-liquid contact phase interface: the larger the phase interface of the gas-liquid contact, the more chance the hydrogen chloride molecules will diffuse into the water, and the higher the acid concentration.
The utility model discloses a device is theorized more than the foundation, when producing high concentration hydrochloric acid, let in the burning of synthetic furnace bottom with chlorine and hydrogen, the electrode of striking sparks who lets in small discharge nitrogen protection synthetic furnace burning torch simultaneously is not corroded by the hydrogen chloride in the synthetic furnace, and strike sparks the electrode cooling, chlorine and hydrogen burning generate HCl gas and emit a large amount of heat, the cooling water in the gas phase presss from both sides the cover in the air current rising process, increase the solubility of hydrogen chloride in aqueous, then in proper order through one-level falling liquid film absorber, get into tail gas alkali wash tower after second grade falling liquid film absorber and absorption tower absorb, the refrigeration absorption water is in proper order through the absorption tower, second grade falling liquid film absorber and one-level falling liquid film absorber absorb hydrogen chloride gas, production initial stage hydrochloric acid concentration is less than 36.5%, let in concentration hydrochloric acid storage tank and store, after production is stable, hydrochloric acid concentration can reach more than 38%, let in high concentration hydrochloric acid storage tank and store, simultaneously to letting in the nitrogen gas in the high concentration hydrochloric acid storage tank, the flow is at 0.5m 3 About/h, the method is used for inhibiting the high-concentration hydrochloric acid from volatilizing again in the storage tank and ensuring the product concentration to be stabilized above 37 percent. In the early stage of production, the flow of the freezing absorption water is controlled by a water flow monitor and a water path electromagnetic control valve in the early stage, so that the concentration of the hydrochloric acid is increased, after the freezing absorption water flow is reduced to a certain range, the furnace pressure of the synthesis furnace is increased by reducing the freezing absorption water flow, the stable production cannot be ensured, the concentration of the hydrochloric acid and the furnace pressure of the hydrochloric acid synthesis furnace are stabilized by adjusting chlorine and hydrogen flows by the gas flow monitor and the water path electromagnetic control valve, the concentration of the hydrochloric acid is ensured to reach over 38 percent, and the stable production of the whole production device is ensured. In the production process, pure water becomes high-temperature high-pressure liquid after absorbing reaction heat, the high-temperature high-pressure liquid enters a flash tank and is decompressed to generate a large amount of steam, the steam is used by other posts and is circulated to enter a synthesis furnace to be used as cooling water. The respective control device and the automatic valve in the high-purity hydrochloric acid system need to be changed into manual control when the automatic state fails.
Compared with the prior art, the utility model discloses following beneficial effect has:
the utility model discloses a production device of high concentration hydrochloric acid, simple structure, convenient operation, through absorption tower, second grade falling liquid film absorber and falling liquid film absorber's absorption to and the control of production earlier stage to freezing absorption water flow and the control of production later stage to chlorine, hydrogen flow, guarantee that the synthetic furnace operation is stable during high concentration hydrochloric acid production, the hydrochloric acid concentration of production is about 38%, increase nitrogen protection at high concentration hydrochloric acid storage tank, ensure that hydrochloric acid delivery concentration is higher than 36.5%, increased the performance of enterprises; the high-temperature high-pressure liquid in the jacket of the synthesis furnace is subjected to heat recycling by arranging the flash tank, so that more energy is saved; in addition, the HCl gas after absorbing water is subjected to alkali washing treatment, so that the method is more environment-friendly.
Drawings
FIG. 1 is a schematic structural diagram of a high-concentration hydrochloric acid production apparatus of the present invention;
in the figure: 1. a chlorine pipeline; 2. a hydrogen gas line; 3. a gas flow monitor; 4. an electromagnetic control valve of the gas circuit; 5. a synthesis furnace; 6. a steam line; 7. a flash tank; 8. a chilled absorption water line; 9. a water flow rate monitor; 10. a waterway electromagnetic control valve; 11. an absorption tower; 12. an air vent line; 13. a tail gas alkaline washing tower; 14. a cooling water line; 15. a first-order falling film absorber; 16. a secondary falling film absorber; 17. a low-concentration hydrochloric acid storage tank; 18. a high-concentration hydrochloric acid storage tank; 19. a dilute alkali circulation tank; 20. a circulation pump; 21. a nitrogen gas pipeline.
Detailed Description
Hereinafter, specific embodiments of the present invention will be described in detail. Well-known structures or functions may not be described in detail in the following embodiments in order to avoid unnecessarily obscuring the details. Unless defined otherwise, technical and scientific terms used in the following examples have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
Example 1
As shown in fig. 1, the apparatus for producing high-concentration hydrochloric acid of the present invention comprises a synthesis furnace 5, a primary falling film absorber 15, a secondary falling film absorber 16, an absorption tower 11 and a tail gas alkaline washing tower 13, which are connected in sequence, wherein a jacket of the synthesis furnace 5 is connected with a flash tank 7, a chlorine pipeline 1, a hydrogen pipeline 2 and a nitrogen pipeline 21 are connected below the synthesis furnace 5, and the chlorine pipeline 1 and the hydrogen pipeline 2 are both provided with a gas flow monitor 3 and a gas circuit electromagnetic control valve 4; the absorption tower 11 is connected with a freezing absorption water pipeline 8, and a water flow monitor 9 and a waterway electromagnetic control valve 10 are installed on the freezing absorption water pipeline 8; the hydrogen chloride gas of the synthesis furnace 5 is absorbed by the first-stage falling film absorber 15, the second-stage falling film absorber 16 and the absorption tower 11 in sequence and then enters the tail gas alkaline washing tower 13, the frozen absorption water is absorbed by the absorption tower 11, the second-stage falling film absorber 16 and the first-stage falling film absorber 15 in sequence and then enters the high-concentration hydrochloric acid storage tank 18, and the high-concentration hydrochloric acid storage tank 18 is connected with the nitrogen pipeline 21.
The main material of the synthetic furnace 5 is composed of graphite and carbon steel, the part of the inner part contacting with hydrogen chloride is composed of graphite, the jacket is composed of carbon steel, and a jacket is reserved in the middle of the jacket and filled with cooling water to cool the graphite and generate steam.
The jacket outlet of the synthesis furnace 5 is connected with the inlet of a flash tank 7, the outlet of the flash tank 7 is connected with the jacket inlet of the synthesis furnace 5, and the gas phase outlet of the flash tank 7 is connected with a steam line 6. High-temperature water or steam in a jacket of the synthesis furnace 5 is utilized through the flash tank 7, the generated liquid phase is used as cooling water to cool the synthesis furnace 5 again, and the generated high-temperature steam is conveyed to other sections for utilization. The liquid level of the flash tank 7 is monitored at any time to avoid water shortage.
The jacket inlet of the synthesis furnace 5 is also connected with a cooling water line 14 for supplementing cooling water to the jacket of the synthesis furnace 5.
A tail gas outlet of the absorption tower 11 is connected with a tail gas alkaline washing tower 13, an absorption liquid outlet of the tail gas alkaline washing tower 13 is connected with a dilute alkali circulating tank 19, and the dilute alkali circulating tank 19 is connected with an absorption liquid inlet of the absorption tower 11 through a circulating pump 20;
the top of the absorption column 11 is connected to a vent line 12.
The gas phase outlet of the first-stage falling film absorber 15 is connected with the gas phase inlet of the second-stage falling film absorber 16, and the gas phase outlet of the second-stage falling film absorber 16 is connected with the absorberA gas phase inlet of the tower 11; a liquid phase outlet of the absorption tower 11 is connected with a liquid phase inlet of a secondary falling film absorber 16, a liquid phase outlet of the secondary falling film absorber 16 is connected with a liquid phase inlet of a primary falling film absorber 15, and a liquid phase outlet of the primary falling film absorber 15 is connected with a low-concentration hydrochloric acid storage tank 17 and a high-concentration hydrochloric acid storage tank 18. The frozen absorption water sequentially passes through an absorption tower 11, a secondary falling film absorber 16 and a primary falling film absorber 15 to absorb hydrogen chloride gas, the concentration of hydrochloric acid is lower than 36.5% in the initial production stage, the hydrochloric acid is introduced into a concentrated hydrochloric acid storage tank 17 for storage, after the production is stable, the concentration of hydrochloric acid can reach more than 38%, the hydrochloric acid is introduced into a high-concentration hydrochloric acid storage tank 18 for storage, nitrogen is introduced into the high-concentration hydrochloric acid storage tank 18 at the same time, and the flow is 0.5m 3 And about/h, the method is used for inhibiting the high-concentration hydrochloric acid from volatilizing again in the storage tank and ensuring the product concentration to be stabilized above 37%.
The gas flow monitor 3 of the chlorine pipeline 1 is electrically connected with the gas circuit electromagnetic control valve 4; the gas flow monitor 3 of the hydrogen pipeline 2 is electrically connected with the gas circuit electromagnetic control valve 4; the freezing absorption water pipeline 8 is electrically connected with the water flow monitor 9 and the waterway electromagnetic control valve 10.
When 36.5% high-concentration hydrochloric acid is produced, in order to ensure that the synthesis furnace 5 operates stably during production, the flow of the freezing absorption water is controlled by the water flow monitor 9 and the waterway electromagnetic control valve 10 in the earlier stage to increase the concentration of the hydrochloric acid, when the flow of the freezing absorption water is reduced to a certain range, the furnace pressure of the synthesis furnace 5 is increased due to the reduction of the flow of the freezing absorption water, and stable production cannot be ensured, at the moment, the concentration of the hydrochloric acid and the furnace pressure of the hydrochloric acid synthesis furnace are stabilized by adjusting the chlorine and hydrogen flow through the gas flow monitor 3 and the waterway electromagnetic control valve 4, so that the concentration of the hydrochloric acid is ensured to reach over 38%, and meanwhile, the stable production of the whole production device is ensured.
The utility model discloses a device is when producing high concentration hydrochloric acid, lets in 5 bottoms burning of synthetic furnace with chlorine and hydrogen, and the electrode of striking sparks that lets in small flow nitrogen protection synthetic furnace burning torch simultaneously is not corroded by the hydrogen chloride in the synthetic furnace to the electrode of striking sparks cools down, and chlorine and hydrogen burning generate HCl gas and emit a large amount of heat, and the gas cooling in the gas flow rises the in-process gas cooling in the cover that presss from both sides, increases the cooling water that increases in the gas flowThe method comprises the steps of enabling the solubility of large hydrogen chloride in water to enter a tail gas alkaline washing tower 13 after being absorbed by a primary falling film absorber 15, a secondary falling film absorber 16 and an absorption tower 11 in sequence, enabling frozen absorption water to absorb hydrogen chloride gas through the absorption tower 11, the secondary falling film absorber 16 and the primary falling film absorber 15 in sequence, enabling the concentration of hydrochloric acid at the initial stage of production to be lower than 36.5%, introducing into a concentration hydrochloric acid storage tank 17 for storage, enabling the concentration of hydrochloric acid to reach more than 38% after production is stable, introducing into a high-concentration hydrochloric acid storage tank 18 for storage, introducing nitrogen into the high-concentration hydrochloric acid storage tank 18 at the same time, and enabling the flow to be 0.5m 3 And about/h, the method is used for inhibiting the high-concentration hydrochloric acid from volatilizing again in the storage tank and ensuring the product concentration to be stabilized above 37%. In the earlier stage of production, the flow of the freezing absorption water is controlled by the water flow monitor 9 and the waterway electromagnetic control valve 10 in the earlier stage, so that the concentration of the hydrochloric acid is increased, when the flow of the freezing absorption water is reduced to a certain range, the furnace pressure of the synthesis furnace 5 is increased due to the reduction of the flow of the freezing absorption water, and the stable production cannot be ensured, at the moment, the concentration of the hydrochloric acid and the furnace pressure of the hydrochloric acid synthesis furnace are stabilized by adjusting the chlorine and hydrogen flow through the gas flow monitor 3 and the waterway electromagnetic control valve 4, the concentration of the hydrochloric acid is ensured to reach over 38%, and the stable production of the whole production device is ensured. In the production process, pure water becomes high-temperature high-pressure liquid after absorbing reaction heat, enters a flash tank 7, is decompressed to generate a large amount of steam, is subjected to gas-liquid separation, is used for other posts, and is circulated to enter a synthesis furnace 5 to serve as cooling water. The respective control device and the automatic valve in the high-purity hydrochloric acid system need to be changed into manual control when the automatic state fails.
Preferably, the specific operation method is as follows: under the condition that the proportioning flow of chlorine and hydrogen is not changed, the water absorption amount is slowly adjusted by a water flow monitor 9 and a waterway electromagnetic control valve 10, and the adjustment amount is 0.3m each time 3 H, stabilizing for 20-30 minutes after adjustment; after the specific gravity of the acid is more than 1.18, the specific gravity is changed to 0.1m 3 H, and is stabilized for 30 minutes, ensuring the stable furnace pressure in the synthetic furnace. When the absorbed water is reduced to 4.0m 3 After the water flow is monitored, the water flow monitor 9 and the waterway electromagnetic control valve 10 control the absorbed water quantity to be unchanged, and then the absorbed water quantity is controlled to be unchanged through the waterway electromagnetic control valve 10The gas flow monitor 3 and the gas circuit electromagnetic control valve 4 slowly increase the flow of chlorine and hydrogen to increase the concentration of hydrochloric acid to over 38 percent.
The device is used for producing high-concentration hydrochloric acid (the delivery concentration is more than or equal to 36.5%) from 1 month in 2021 year, the production process of the hydrochloric acid is stable to control, the flow is smooth, the product meets the requirements of customers, and the enterprise benefit is increased.
Claims (7)
1. The utility model provides a apparatus for producing of high concentration hydrochloric acid which characterized in that: the system comprises a synthesis furnace (5), a primary falling film absorber (15), a secondary falling film absorber (16), an absorption tower (11) and a tail gas alkaline washing tower (13) which are sequentially connected, wherein a jacket of the synthesis furnace (5) is connected with a flash tank (7), a chlorine pipeline (1), a hydrogen pipeline (2) and a nitrogen pipeline (21) are connected below the synthesis furnace (5), and a gas flow monitor (3) and a gas circuit electromagnetic control valve (4) are respectively arranged on the chlorine pipeline (1) and the hydrogen pipeline (2); the absorption tower (11) is connected with a freezing and absorbing water pipeline (8), and a water flow monitor (9) and a waterway electromagnetic control valve (10) are installed on the freezing and absorbing water pipeline (8); hydrogen chloride gas of the synthesis furnace (5) enters a tail gas alkali washing tower (13) after being absorbed by a primary falling film absorber (15), a secondary falling film absorber (16) and an absorption tower (11) in sequence, frozen absorption water enters a high-concentration hydrochloric acid storage tank (18) after being absorbed by the absorption tower (11), the secondary falling film absorber (16) and the primary falling film absorber (15) in sequence, and the high-concentration hydrochloric acid storage tank (18) is connected with a nitrogen pipeline (21).
2. The apparatus for producing high-concentration hydrochloric acid according to claim 1, characterized in that: the jacket outlet of the synthesis furnace (5) is connected with the inlet of the flash tank (7), the outlet of the flash tank (7) is connected with the jacket inlet of the synthesis furnace (5), and the gas phase outlet of the flash tank (7) is connected with the steam pipeline (6).
3. The production apparatus of high-concentration hydrochloric acid according to claim 1 or 2, characterized in that: the jacket inlet of the synthesis furnace (5) is also connected with a cooling water pipeline (14).
4. The apparatus for producing high-concentration hydrochloric acid according to claim 1, characterized in that: a tail gas outlet of the absorption tower (11) is connected with a tail gas alkaline washing tower (13), an absorption liquid outlet of the tail gas alkaline washing tower (13) is connected with a dilute alkali circulating tank (19), and the dilute alkali circulating tank (19) is connected with an absorption liquid inlet of the absorption tower (11) through a circulating pump (20).
5. The production apparatus of high-concentration hydrochloric acid according to claim 1 or 4, characterized in that: the top of the absorption tower (11) is connected with an air vent pipeline (12).
6. The production apparatus of high-concentration hydrochloric acid according to claim 1, characterized in that: a gas-phase outlet of the first-stage falling film absorber (15) is connected with a gas-phase inlet of the second-stage falling film absorber (16), and a gas-phase outlet of the second-stage falling film absorber (16) is connected with a gas-phase inlet of the absorption tower (11); a liquid phase outlet of the absorption tower (11) is connected with a liquid phase inlet of the secondary falling film absorber (16), a liquid phase outlet of the secondary falling film absorber (16) is connected with a liquid phase inlet of the primary falling film absorber (15), and a liquid phase outlet of the primary falling film absorber (15) is connected with the low-concentration hydrochloric acid storage tank (17) and the high-concentration hydrochloric acid storage tank (18).
7. The production apparatus of high-concentration hydrochloric acid according to claim 1, characterized in that: the gas flow monitor (3) of the chlorine pipeline (1) is electrically connected with the gas circuit electromagnetic control valve (4); the gas flow monitor (3) of the hydrogen pipeline (2) is electrically connected with the gas circuit electromagnetic control valve (4); the water flow monitor (9) of the freezing absorption water pipeline (8) is electrically connected with the waterway electromagnetic control valve (10).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220668793.4U CN217526949U (en) | 2022-03-25 | 2022-03-25 | Production device of high-concentration hydrochloric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220668793.4U CN217526949U (en) | 2022-03-25 | 2022-03-25 | Production device of high-concentration hydrochloric acid |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN217526949U true CN217526949U (en) | 2022-10-04 |
Family
ID=83430429
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202220668793.4U Active CN217526949U (en) | 2022-03-25 | 2022-03-25 | Production device of high-concentration hydrochloric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN217526949U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115845651A (en) * | 2022-12-05 | 2023-03-28 | 金川集团股份有限公司 | Production device and method for medical high-purity hydrogen chloride organic solution |
-
2022
- 2022-03-25 CN CN202220668793.4U patent/CN217526949U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115845651A (en) * | 2022-12-05 | 2023-03-28 | 金川集团股份有限公司 | Production device and method for medical high-purity hydrogen chloride organic solution |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103223292B (en) | Ammonia process flue gas treatment method for acidic tail gas and device | |
| CN217526949U (en) | Production device of high-concentration hydrochloric acid | |
| CN113247870B (en) | Method and device for preparing high-purity nitrogen trifluoride gas | |
| CN101928016B (en) | Process for producing ammonium sulfate by adopting negative pressure double-countercurrent evaporation and crystallization mode | |
| CA2085682A1 (en) | Integrated procedure for high yield production of chlorine dioxide | |
| CN111675195A (en) | Energy-saving environment-friendly process flow for synthesizing hydrochloric acid | |
| CN208757276U (en) | A kind of device of scale reducing nitrogen oxides during preparation of silver nitrate discharge | |
| CN105478023A (en) | Ammonia water preparation system | |
| CN205288123U (en) | Aqueous ammonia preparation system | |
| CN103407971B (en) | Novel technology for production of liquid sulfur dioxide | |
| CN110388638B (en) | Steam heat energy recycling process in urea production by carbon dioxide gas stripping method | |
| CN115557468A (en) | Method for extracting bromine from brine | |
| CN210602324U (en) | Chemical reaction low-temperature thermal refrigerating system | |
| CN203373296U (en) | Carbon dioxide steam stripping urea yield increase energy-saving device | |
| CN209113500U (en) | Cold carbonization Tower System outside five one group of tower formulas | |
| CN112430176A (en) | Acetylene gas drying and dehydrating method for vinyl chloride production section | |
| CN204550489U (en) | A kind of gas employing methanation of coke oven LNG device with spraying cycle device | |
| CN215103595U (en) | Device for preparing high-purity nitrogen trifluoride gas | |
| CN221014564U (en) | Energy-saving melamine crystallization system | |
| CN216259139U (en) | Seven-effect evaporation system applied to Guinea ore low-temperature alumina production line | |
| CN218565911U (en) | Pressurized cooling liquefaction device for producing liquid sulfur dioxide | |
| CN220677283U (en) | Hydrogen recovery and purification equipment | |
| CN216919073U (en) | Device for removing sulfur and phosphorus impurities in crude acetylene gas | |
| CN212357100U (en) | Production device for co-producing dimethyl carbonate by coal glycol device | |
| CN115430262B (en) | Device and method for recycling nitrous gases |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |