CN216837139U - High-efficient continuous controllable sodium hypochlorite apparatus for producing - Google Patents
High-efficient continuous controllable sodium hypochlorite apparatus for producing Download PDFInfo
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Abstract
The utility model provides a continuous, high-efficiency and controllable sodium hypochlorite production device, which comprises an alkali preparation process, a tail gas treatment process and a sodium hypochlorite reaction process; the dilute alkali preparation procedure comprises a dilute water flow automatic control system, a sodium hydroxide flow automatic control system, a pipeline mixer, an alkali preparation tank and an alkali preparation pump; the tail gas treatment process comprises a dilute alkali circulation tank, a dilute alkali circulation pump, a dilute alkali flow automatic control system, an ejector, a gas-liquid separator, a dilute alkali head tank and a tail gas absorption tower; the sodium hypochlorite product generation procedure comprises a liquid inlet precooler, a chlorine buffer tank, a chlorine flow control system, a temperature control and reduction membrane reactor, an intermediate product tank and a product pump. The device has the advantages of reliable process, perfect design, simple operation and maintenance, advanced technology, capability of efficiently and controllably continuously producing sodium hypochlorite products, stable product quality, complete tail gas absorption, chlorine-free tail gas emission up to the standard without chlorine leakage, safety, environmental protection, automatic control and regulation in normal operation, and no need of personnel operation.
Description
Technical Field
The utility model relates to a controllable sodium hypochlorite apparatus for producing of high efficiency in succession, especially with sodium hypochlorite product device that sodium hydroxide and chlorine reaction generated, belong to chemical industry technical field.
Background
Sodium hypochlorite is a liquid that is completely soluble in water. As a strong sterilizing and virus killing agent with real high efficiency, broad spectrum and safety, the strong sterilizing and virus killing agent has good affinity with water, can be mutually dissolved with water in any ratio, does not have the potential safety hazards of liquid chlorine, chlorine dioxide and other medicaments, and has the disinfection effect which is known to be equivalent to that of chlorine.
At present, the domestic sodium hypochlorite production process mainly comprises an electrolysis method and a sodium hydroxide absorption method. The electrolytic product has low available chlorine content, and is mainly used for disinfection and algae removal in water treatment in occasions requiring a small amount of sodium hypochlorite. The sodium hydroxide absorption method is mainly used for pulp, textiles and chemical fibers as bleaching agents, is used as water purifying agents, bactericides and disinfectants in water treatment, is used for manufacturing chlorinated mats in the organic industry, is used for manufacturing indigo in the dye industry and is used for producing monochloramine and dicloramine in the medical industry.
The sodium hydroxide absorption process includes a packed tower multistage absorption process and a falling film absorption process. The multi-stage absorption process of the packed tower adopts the circulation tank type intermittent production, has the problems of complex operation, high labor intensity, difficult control of the content of perchloride or alkali, unstable product quality and the like. Falling film absorption technology has certain advantages in China, but most of devices at present have the problems of unstable gas and liquid feeding, unstable product quality fluctuation, incomplete chlorine-containing chlorine leakage in tail gas absorption and the like.
Disclosure of Invention
In order to solve the problems, the utility model provides a high-efficient continuous controllable sodium hypochlorite production device, which can produce sodium hypochlorite products with various concentrations efficiently, continuously and controllably. Meanwhile, the problems of unstable gas and liquid feeding, unstable product quality, incomplete tail gas absorption, chlorine leakage and the like in the falling film absorption reaction process are solved.
The invention adopts the following specific technical scheme:
the utility model provides a controllable sodium hypochlorite apparatus for producing of continuous high efficiency which characterized in that: comprises a dilute alkali preparation process, a tail gas treatment process and a sodium hypochlorite product generation process.
The dilute alkali preparation procedure comprises a dilute water flow automatic control system, a sodium hydroxide flow automatic control system, a pipeline mixer, an alkali preparation tank and an alkali preparation pump; the tail gas treatment process comprises a dilute alkali circulation tank, a dilute alkali circulation pump, a dilute alkali flow automatic control system, an ejector, a gas-liquid separator, a dilute alkali head tank, a tail gas absorption tower and a U-shaped connecting pipe; the sodium hypochlorite product generation procedure comprises a liquid inlet precooler, a chlorine buffer tank, a chlorine flow control system, a temperature control and reduction membrane reactor, an intermediate product tank, a product pump, a U-shaped connecting pipe and a cooling control valve.
Wherein the dilute water flow automatic control system is connected with the inlet I of the pipeline mixer through a pipeline, the sodium hydroxide flow automatic control system is connected with the inlet II of the pipeline mixer through a pipeline, the outlet of the pipeline mixer is connected with the inlet of the alkali distribution tank through a pipeline, the outlet of the alkali distribution tank is connected with the inlet of the alkali distribution pump through a pipeline, the outlet of the alkali distribution pump is connected with the inlet I of the dilute alkali circulation tank through a pipeline, the outlet of the dilute alkali circulation tank is connected with the inlet of the dilute alkali circulation pump through a pipeline, the outlet of the dilute alkali circulation pump is connected with the dilute alkali flow automatic control system through a pipeline, the outlet of the dilute alkali flow automatic control system is connected with the inlet I of the ejector through a pipeline, the outlet of the ejector is connected with the dilute alkali gas-liquid separator through a pipeline, the gas-liquid separator is connected with the dilute alkali elevated tank through a pipeline, the overflow port of the dilute alkali elevated tank is connected with the inlet II of the dilute alkali circulation tank through a U-shaped connecting pipe with a liquid seal effect, the gas phase outlet of the tail gas absorption tower is connected with the inlet II of the ejector through a pipeline, the liquid phase outlet of the tail gas absorption tower is connected with the inlet of the liquid inlet precooler through a U-shaped connecting pipe with a liquid sealing effect, the outlet of the liquid inlet precooler is connected with the liquid phase inlet of the temperature control falling film reactor through a U-shaped connecting pipe with a liquid sealing effect, the chlorine buffer tank is connected with the chlorine flow control system through a pipeline, the chlorine flow control system is connected with the gas phase inlet of the temperature control falling film reactor through a pipeline, the tail gas outlet of the temperature control falling film reactor is connected with the gas phase inlet of the tail gas absorption tower through a pipeline, and the liquid phase outlet of the temperature control falling film reactor is respectively connected with the inlet of the intermediate product tank and the inlet of the dilute alkali circulation tank through a U-shaped connecting pipe with a liquid sealing effect. The outlet of the intermediate product groove is connected with the inlet of the product pump through a pipeline. The cooling control valve is connected with a cooling water inlet of the liquid inlet precooler through a pipeline, and the cooling control valve is connected with a cooling water inlet of the temperature control falling film reactor through a pipeline.
The automatic dilution water flow control system, the sodium hydroxide flow control system, the dilute alkali flow control system and the chlorine flow control system respectively mainly comprise an automatic control valve, a flowmeter and a DCS system.
The flow ratio correlation is adopted by the dilution water flow automatic control system and the sodium hydroxide flow control system to carry out double-loop closed-loop regulation, so that the proportion of the dilution water and the sodium hydroxide is effectively controlled, and the stable concentration of the prepared alkali is ensured. The flow ratio can be directly set to different ratios through a control system so as to adapt to the requirements of different alkali preparation concentrations.
The dilute alkali flow control automatic control system and the chlorine flow control system adopt flow ratio correlation to carry out double-loop closed-loop regulation, effectively control the stable proportion of dilute alkali and chlorine, ensure the stable flow of dilute alkali and chlorine, effectively control the excessive alkali amount and the excessive chlorine amount of a product, and keep the stable output of the product. The flow ratio can be directly set to different ratios through the control system so as to adapt to the requirements of different product concentrations.
The alkali distribution tank, the dilute alkali circulation tank, the dilute alkali head tank and the intermediate product tank are respectively provided with a remote liquid level meter, so that the liquid level of each device can be monitored in real time, and the production regulation and control are facilitated.
The U-shaped connecting pipe is provided with a remote thermometer, so that the temperature of the pipeline material can be monitored in real time, and the remote thermometer is associated with a cooling control valve to control the liquid inlet temperature of the liquid inlet precooler; the liquid phase outlet pipeline of the temperature control falling-film reactor is provided with a U-shaped connecting pipe with a liquid sealing effect, a remote thermometer is arranged on the U-shaped connecting pipe, the temperature of the pipeline material can be monitored in real time, a cooling control valve is associated, the liquid inlet temperature of the temperature control falling-film reactor is controlled, an online PH meter is arranged on the U-shaped connecting pipe, the production and monitoring of the PH value of a product are facilitated, and an artificial sampling valve is arranged on the U-shaped connecting pipe.
The chlorine buffer tank is provided with a pressure monitoring and inlet pressure regulating valve to control the pressure of the chlorine buffer tank within a normal range.
The ejector is composed of a nozzle, a suction chamber and a diffuser pipe. Fluid with certain pressure provided by the dilute alkali circulating pump is ejected at high speed through the nozzle, vacuum is formed in the outlet area of the nozzle, a micro-negative pressure working condition is provided for the tail gas tower, tail gas of the tail gas tower is effectively led to the ejector to be sucked into the room to be fully mixed with dilute alkali, and chlorine in the tail gas is efficiently absorbed.
The inlet pipe of the gas-liquid separator is arranged as a submerged liquid seal pipe, and a gas-liquid mixture in the ejector enters the gas-liquid separator through the submerged pipe in the gas-liquid separator, so that the gas-liquid separator can separate gas from liquid, and can effectively absorb the possibly residual chlorine in the tail gas more fully, thereby ensuring that the discharged tail gas reaches the discharge standard.
The liquid inlet mode from the dilute alkali elevated tank to the tail gas absorption tower is self-flowing, the liquid inlet mode from the tail gas absorption tower to the liquid inlet precooler is self-flowing, and the liquid inlet mode from the liquid inlet precooler to the temperature-control falling-film reactor is self-flowing. Effectively ensures the stable liquid inlet of the tail gas degassing tower, the liquid inlet precooler and the temperature control falling film reactor.
The tail gas absorption tower is a corrosion-resistant packed tower or a spray tower.
The liquid inlet precooler can be a shell and tube, coil or plate heat exchanger, and the adopted heat exchange medium can be chilled water or circulating water.
The temperature control falling film reactor consists of a tube type heat exchange tube, a heat exchange barrel, a tube plate, a film making device, an upper tube box, a lower tube box, an upper seal head, a lower cone, a liquid distribution plate, a gas distribution plate, a tube opening flange and a fastener.
Further, the heat exchange tube of the temperature control falling film reactor is made of titanium.
Furthermore, a membrane making device of the temperature-control falling-film reactor is made of polytetrafluoroethylene, and the membrane making device is provided with a plurality of downward-rotating groove runners, so that a liquid film with stable flow speed and uniform thickness is formed on the inner wall of the heat exchange tube.
High-efficient controllable sodium hypochlorite apparatus for producing in succession, including three step: preparing dilute alkali, treating tail gas and generating sodium hypochlorite products.
The embodiment of each step is as follows:
1) and (3) preparing dilute alkali: the sodium hydroxide and the dilution water are mixed after controlling the respective flow according to a certain proportion to prepare the required diluted alkali concentration.
The concentration of the prepared diluted alkali is calculated and determined according to the concentration of the sodium hypochlorite product required to be produced. The calculation is as follows:
the mass concentration w2 of the sodium hypochlorite product, the mass concentration w3 of free alkali of the product, the mass concentration w1 of dilute alkali and the safety factor Y.
w1=80w2/（74.5-71w2）Y+w3
The ratio of the sodium hydroxide flow to the dilution water required for preparation was calculated as follows: the mass concentration w4 of sodium hydroxide, the density p1 of sodium hydroxide and the density p2 of dilution water require that w4 is more than or equal to w1 and the ratio B of the flow rate of sodium hydroxide to the flow rate of dilution water in actual production.
B=1:[(w4-w1)×p1/（w1×p2)]
2) And tail gas treatment: after the tail gas absorption tower is used for absorbing most of tail gas discharged from a tail gas pipe at the bottom of the temperature-control falling film reactor, absorption liquid is used as reaction liquid of the temperature-control falling film reactor to automatically flow into the temperature-control reactor stably. The residual tail gas at the top of the tail gas absorption tower is fully mixed and reacted with the dilute alkali from the dilute alkali circulating pump through the negative pressure suction of the ejector, then enters the dilute alkali gas-liquid separator in a liquid-down liquid seal liquid inlet mode, and then overflows to the dilute alkali head tank, and the dilute alkali in the dilute alkali head tank is used as the absorption liquid of the tail gas absorption tower to automatically flow and stably enter the tail gas absorption tower. The tail gas is reacted with the absorption liquid with the concentration increased relative to the concentration of the caustic soda for many times in the process from rising to emptying, so that the chlorine content in the tail gas is ensured to reach the standard and be discharged. The flow of the dilute alkali sent by the dilute alkali circulating pump can be controlled by the flow control system according to the production load condition.
3) And generation of sodium hypochlorite products: absorbing liquid from the tail gas absorbing tower is subjected to heat exchange and cooling with chilled water (or circulating water) through a liquid inlet precooler and then enters the temperature-controlled falling film reactor. The absorption liquid forms a stable and uniform liquid film on the inner wall of the tube nest through a liquid distribution plate and a film making device in the temperature control reactor. The chlorine gas sent from the chlorine gas buffer tank forms ratio adjustment through a chlorine gas flow control system and a dilute alkali flow control system according to the production load condition, and the flow ratio of the chlorine gas to the dilute alkali is stably controlled, so that the flow of the chlorine gas and the dilute alkali entering the temperature-control falling film reactor reaches the optimal reaction ratio. Chlorine enters the temperature-control falling-film reactor, is distributed by the gas distribution plate and then enters each tube, and contacts with absorption liquid of liquid films on the inner walls of the tubes to react to generate sodium hypochlorite products. And the generated sodium hypochlorite product enters an intermediate product tank and is pumped out of the production area by a product pump.
The calculated value of the dilute alkali preparation in the method is a theoretical calculation reference value, and certain adjustment can be carried out according to the reference value in the actual production operation, so that the actual production product reaches the standard and is qualified.
This controllable sodium hypochlorite apparatus for producing of high efficiency is reliable in process, and the design is perfect, and operation maintenance is simple, the technique is advanced, can high-efficient controllable continuous production sodium hypochlorite product, and product quality is stable, and tail gas absorbs completely, and tail gas does not contain chlorine and does not run chlorine discharge to reach standard, safety ring protects. The normal operation is automatic control and adjustment, and the operation of personnel is not needed.
Drawings
FIG. 1 is a schematic structural view of a sodium chlorate production apparatus of this time.
The labels in the figure are: 1-an alkali preparation tank, 2-an alkali preparation pump, 3-an ejector, 4-a gas-liquid separator, 5-a dilute alkali head tank, 6-a tail gas absorption tower, 7-a liquid inlet precooler, 8-a temperature control and drop membrane reactor, 9-a chlorine buffer tank, 10-an intermediate product tank, 11-a dilute alkali circulation tank, 12-a dilute alkali circulation pump, 13-a product pump, 14-a dilute water flow automatic control system, 15-a sodium hydroxide flow automatic control system, 16-a pipeline mixer, 17-a dilute alkali flow control system, 18-a chlorine flow control system, 19-a chlorine switch valve, 20-U-shaped connecting pipes a.b.c.d, and 21-a cooling control valve a.b.
Detailed Description
This controllable sodium hypochlorite apparatus for producing of high efficiency in succession includes that dilute alkali prepares process, tail gas treatment process and sodium hypochlorite product generate the process. As shown in fig. 1, the dilute alkali preparation process comprises a dilution water flow automatic control system 14, a sodium hydroxide flow automatic control system 15, a pipeline mixer 16, an alkali preparation tank 1 and an alkali preparation pump 2; the tail gas treatment process comprises a dilute alkali circulation tank 11, a dilute alkali circulation pump 12, a dilute alkali flow automatic control system 17, an ejector 3, a gas-liquid separator 4, a dilute alkali head tank 5, a tail gas absorption tower 6, a U-shaped connecting pipe 20a and a U-shaped connecting pipe 20 b; the sodium hypochlorite product generation procedure comprises a liquid inlet precooler 7, a chlorine buffer tank 9, a chlorine flow control system 18, a temperature control and reduction membrane reactor 8, an intermediate product tank 10, a product pump 13, a U-shaped connecting pipe 20c, a U-shaped connecting pipe 20d, a cooling control valve 21a and a cooling control valve 21 b.
Wherein the automatic control system 14 for the flow of the dilution water is connected with the inlet I of the pipeline mixer 16 through a pipeline, the automatic control system 15 for the flow of the sodium hydroxide is connected with the inlet II of the pipeline mixer 16 through a pipeline, the outlet of the pipeline mixer 16 is connected with the inlet of the alkali distribution tank 1 through a pipeline, the outlet of the alkali distribution tank 1 is connected with the inlet of the alkali distribution pump 2 through a pipeline, the outlet of the alkali distribution pump 2 is connected with the inlet I of the dilute alkali circulation tank 11 through a pipeline, the outlet of the dilute alkali circulation tank 11 is connected with the inlet of the dilute alkali circulation pump 12 through a pipeline, the outlet of the dilute alkali circulation pump 12 is connected with the automatic control system 17 for the flow of the dilute alkali through a pipeline, the automatic control system 17 for the flow of the dilute alkali is connected with the inlet I of the ejector 3 through a pipeline, the outlet of the ejector 3 is connected with the gas-liquid separator 4 through a pipeline, the gas-liquid separator 4 is connected with the dilute alkali head tank 5 through a pipeline, the overflow port of the dilute alkali circulation tank 5 is connected with the inlet II of the dilute alkali circulation tank 11 through a pipeline, the outlet of the tail gas-liquid-phase absorption tower 6 through a U-type connecting pipe with a liquid sealing function, the gas phase outlet of the tail gas absorption tower 6 is connected with the inlet II of the ejector 3 through a pipeline, the liquid phase outlet of the tail gas absorption tower 6 is connected with the inlet of the liquid inlet precooler 7 through a U-shaped connecting pipe 20b with liquid seal function, the outlet of the liquid inlet precooler 7 is connected with the liquid phase inlet of the temperature control and reduction membrane reactor 8 through a U-shaped connecting pipe 20c with liquid seal function, the chlorine buffer tank 9 is connected with the chlorine flow control system 18 through a pipeline, the chlorine flow control system 18 is connected with the gas phase inlet of the temperature control and reduction membrane reactor 8 through a pipeline, the tail gas outlet of the temperature control and reduction membrane reactor 8 is connected with the gas phase inlet of the tail gas absorption tower 6 through a pipeline, the liquid phase outlet of the temperature control and reduction membrane reactor 8 is connected with the inlet of the intermediate product tank 10 and the inlet III of the dilute alkali circulation tank 11 through a U-shaped connecting pipe 20d with liquid seal function, the outlet of the intermediate product tank 10 is connected with the inlet of the product pump 13 through a pipeline, and the cooling control valve 21a is connected with the cooling water inlet of the liquid inlet precooler 7 through a pipeline, the cooling control valve 21b is connected with a cooling water inlet of the temperature-controlled falling film reactor 8 through a pipeline.
The device is provided with a remote liquid level meter for monitoring the liquid level condition in real time in the alkali preparation tank 1, the dilute alkali head tank 5, the product intermediate tank 10 and the dilute alkali circulation tank 11. Be provided with online PH meter at U type connecting pipe 20d, the PH value of real-time supervision sodium hypochlorite product to product quality monitoring. Remote thermometers are arranged on the U-shaped connecting pipe 20c and the U-shaped connecting pipe 20d, the cooling control valve 21a and the cooling control valve 21b are correspondingly controlled in a related mode, and the temperature of the materials is automatically monitored and controlled to be a preset value. The chlorine buffer tank 9 is provided with a remote pressure gauge for monitoring the pressure condition of the chlorine buffer tank 9 in real time, and the chlorine switch valve 19 is controlled in a correlated manner, so that when the pressure of the chlorine buffer tank 9 is too high, the chlorine switch valve 19 is automatically closed.
The following is a specific example of the production of sodium hypochlorite using the present apparatus.
The flow of 30% sodium hydroxide solution (temperature 30 ℃, specific gravity 1.3217) and dilution water (specific gravity 1) is measured by a sodium hydroxide flow automatic control system 15 and a dilution water flow automatic control system 14 according to the ratio of 1:1.076, and then the measured flows enter a pipeline mixer 16 to be mixed to prepare about 16.53% sodium hydroxide solution, and then the mixed solution enters an alkali preparation tank 1.
The dilute alkali in the alkali preparation tank 1 is conveyed to a dilute alkali circulation tank 11 through an alkali preparation pump 2, the dilute alkali in the dilute alkali circulation tank 11 is metered by a dilute alkali flow control system 17 through a dilute alkali circulation pump 12 and then enters an ejector 3, the dilute alkali in the ejector 3 is fully contacted and mixed with tail gas from a tail gas tower 6, then the mixed gas enters a gas-liquid separator 4 and overflows to a dilute alkali head tank 5, and the unreacted tail gas is discharged from an exhaust port of the dilute alkali head tank 5. The dilute alkali of the dilute alkali elevated tank 5 automatically flows into a tail gas absorption tower 6, and is subjected to absorption reaction with tail gas from a temperature-controlled falling-film reactor 8 in the tail gas absorption tower 6, absorption liquid of the tail gas absorption tower 6 enters a liquid inlet precooler 7 for precooling, the absorption liquid is controlled to enter the temperature-controlled falling-film reactor 8 at 10-25 ℃, and uniform and stable liquid films are formed on the inner walls of the tubes of the temperature-controlled falling-film reactor 8.
Chlorine gas is introduced into a chlorine buffer tank 9, and after being measured by a chlorine flow control system 18 (the chlorine gas is associated with a ratio of a dilute alkali flow control system 17, and the ratio needs to be calculated and determined according to the concentration of a produced product and the concentration of dilute alkali), the chlorine gas enters a temperature-controlled falling film reactor 8 and is subjected to contact reaction with an absorption liquid film in the temperature-controlled falling film reactor 8 to form sodium hypochlorite. The generated sodium hypochlorite product is conveyed to a product middle tank through a bottom U-shaped connecting pipe 20 d. Unreacted tail gas in the temperature-controlled falling-film reactor 8 is discharged to the tail gas absorption tower 6 through a tail gas outlet.
The concentration of dilute base was set according to this example to 16.53%, the resulting sodium hypochlorite product was about 13% and contained about 0.6% free base.
The concentration w4 of the sodium hydroxide solution in the embodiment can be any concentration satisfying w4 ≥ w 1.
Claims (10)
1. The utility model provides a controllable sodium hypochlorite apparatus for producing of continuous high efficiency, characterized by: comprises a dilute alkali preparation process, a tail gas treatment process and a sodium hypochlorite product generation process; the dilute alkali preparation procedure comprises a dilute water flow automatic control system (14), a sodium hydroxide flow automatic control system (15), a pipeline mixer (16), an alkali preparation tank (1) and an alkali preparation pump (2); the tail gas treatment process comprises a dilute alkali circulation tank (11), a dilute alkali circulation pump (12), a dilute alkali flow automatic control system (17), an ejector (3), a gas-liquid separator (4), a dilute alkali head tank (5), a tail gas absorption tower (6) and a U-shaped connecting pipe (20); the sodium hypochlorite product generation procedure comprises a liquid inlet precooler (7), a chlorine buffer tank (9), a chlorine flow control system (18), a temperature control and cooling membrane reactor (8), an intermediate product tank (10), a product pump (13), a U-shaped connecting pipe (20) and a cooling control valve (21);
wherein the dilute water flow automatic control system (14) is connected with the inlet I of the pipeline mixer (16) through a pipeline, the sodium hydroxide flow automatic control system (15) is connected with the inlet II of the pipeline mixer (16) through a pipeline, the outlet of the pipeline mixer (16) is connected with the inlet of the alkali distribution tank (1) through a pipeline, the outlet of the alkali distribution tank (1) is connected with the inlet of the alkali distribution pump (2) through a pipeline, the outlet of the alkali distribution pump (2) is connected with the inlet I of the dilute alkali circulation tank (11) through a pipeline, the outlet of the dilute alkali circulation tank (11) is connected with the inlet of the dilute alkali circulation pump (12) through a pipeline, the outlet of the dilute alkali circulation pump (12) is connected with the dilute alkali flow automatic control system (17) through a pipeline, the dilute alkali flow automatic control system (17) is connected with the inlet I of the ejector (3) through a pipeline, the outlet of the ejector (3) is connected with the gas-liquid separator (4) through a pipeline, the gas-liquid separator (4) is connected with the dilute alkali high-level tank (5) through a pipeline, an overflow port of a dilute alkali elevated tank (5) is connected with a second inlet of a dilute alkali circulation tank (11) through a pipeline, an outlet of the dilute alkali elevated tank (5) is connected with a second liquid-phase inlet of a tail gas absorption tower (6) through a U-shaped connecting pipe (20 a) with a liquid sealing effect, a gas-phase outlet of the tail gas absorption tower (6) is connected with a second inlet of an ejector (3) through a pipeline, a liquid-phase outlet of the tail gas absorption tower (6) is connected with an inlet of a liquid inlet precooler (7) through a U-shaped connecting pipe (20 b) with a liquid sealing effect, an outlet of the liquid inlet precooler (7) is connected with a liquid-phase inlet of a temperature-control falling membrane reactor (8) through a U-shaped connecting pipe (20 c) with a liquid sealing effect, a chlorine buffer tank (9) is connected with a chlorine flow control system (18) through a pipeline, the chlorine flow control system (18) is connected with a gas-phase inlet of the temperature-control falling membrane reactor (8) through a pipeline, a tail gas outlet of the temperature-control falling membrane reactor (8) is connected with a gas-phase inlet of the tail gas absorption tower (6) through a pipeline, the liquid phase outlet of the temperature-control falling-film reactor (8) is respectively connected with the inlet of an intermediate product groove (10) and the inlet of a dilute alkali circulating groove (11) through a U-shaped connecting pipe (20 d), the outlet of the intermediate product groove (10) is connected with the inlet of a product pump (13) through a pipeline, a cooling control valve (21 a) is connected with the cooling water inlet of a liquid inlet precooler (7) through a pipeline, and a cooling control valve (21 b) is connected with the cooling water inlet of the temperature-control falling-film reactor (8) through a pipeline.
2. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: the automatic flow control system (14) for the dilution water, the automatic flow control system (15) for the sodium hydroxide, the automatic flow control system (17) for the dilute alkali and the chlorine flow control system (18) are respectively mainly composed of an automatic control valve, a flowmeter and a DCS system.
3. The continuous high-efficiency controllable sodium hypochlorite production device according to claim 1, which is characterized in that: a U-shaped connecting pipe (20) with a liquid sealing function is arranged on a liquid phase outlet pipeline of the temperature control falling film reactor (8), and a remote thermometer, an on-line PH meter and a manual sampling valve are arranged on the U-shaped connecting pipe (20).
4. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: the temperature control falling film reactor (8) consists of a tube type heat exchange tube, a heat exchange barrel, a tube plate, a film making device, an upper tube box, a lower tube box, an upper seal head, a lower cone, a liquid distribution plate, a gas distribution plate, a pipe orifice flange and a fastener.
5. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: the heat exchange tube of the temperature control falling film reactor (8) is made of titanium.
6. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: a membrane making device of the temperature control and drop membrane reactor (8) is made of polytetrafluoroethylene, and is provided with a plurality of downward-rotating groove runners, so that a liquid membrane with stable flow speed and uniform thickness is formed on the inner wall of a heat exchange tube.
7. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: the chlorine buffer tank (9) is provided with a pressure monitoring and inlet pressure regulating valve.
8. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: the ejector (3) is composed of a nozzle, a suction chamber and a diffuser pipe.
9. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: an inlet pipe of the gas-liquid separator (4) is a submerged liquid seal pipe.
10. The continuous, efficient and controllable sodium hypochlorite production device as claimed in claim 1, wherein: the liquid inlet mode from the dilute alkali head tank to the tail gas absorption tower is self-flowing, the liquid inlet mode from the tail gas absorption tower to the liquid inlet precooler is self-flowing, and the liquid inlet mode from the liquid inlet precooler to the temperature-control falling-film reactor is self-flowing.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115872362A (en) * | 2022-12-12 | 2023-03-31 | 江西星火航天新材料有限公司 | Method for continuously preparing high-purity sodium hypochlorite |
| CN117742278A (en) * | 2024-02-07 | 2024-03-22 | 四川飞洁科技发展有限公司 | Intelligent monitoring and management method and system for sodium hypochlorite production process |
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2022
- 2022-03-10 CN CN202220512889.1U patent/CN216837139U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115872362A (en) * | 2022-12-12 | 2023-03-31 | 江西星火航天新材料有限公司 | Method for continuously preparing high-purity sodium hypochlorite |
| CN115872362B (en) * | 2022-12-12 | 2023-11-10 | 江西星火航天新材料有限公司 | Method for continuously preparing high-purity sodium hypochlorite |
| CN117742278A (en) * | 2024-02-07 | 2024-03-22 | 四川飞洁科技发展有限公司 | Intelligent monitoring and management method and system for sodium hypochlorite production process |
| CN117742278B (en) * | 2024-02-07 | 2024-04-30 | 四川飞洁科技发展有限公司 | Intelligent monitoring and management method and system for sodium hypochlorite production process |
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