CN212101988U - Improved generation sodium hypochlorite production on-line control system - Google Patents
Improved generation sodium hypochlorite production on-line control system Download PDFInfo
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- CN212101988U CN212101988U CN202020651592.4U CN202020651592U CN212101988U CN 212101988 U CN212101988 U CN 212101988U CN 202020651592 U CN202020651592 U CN 202020651592U CN 212101988 U CN212101988 U CN 212101988U
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Abstract
The utility model discloses an improved sodium hypochlorite production on-line control system, which comprises an alkali distribution tank, a first alkali absorption tank, an absorption tower, a second alkali absorption tank, a pest eliminating tower and a sodium hypochlorite finished product tank; the alkali liquor pipeline is provided with an alkali liquor flowmeter and an alkali liquor automatic control valve, the deionized water pipeline is provided with a deionized water flowmeter and a deionized water automatic control valve, the chlorine pipeline is provided with a chlorine flowmeter and a chlorine automatic control valve, and the first circulating pipeline is provided with a sodium hypochlorite flowmeter, an absorption tower inlet ORP monitor, an absorption tower outlet ORP monitor, an absorption tower inlet temperature monitor and an absorption tower outlet temperature monitor; the second circulation pipeline is provided with an ORP monitor of the harmful-in removing tower, an ORP monitor of the harmful-out removing tower, a temperature monitor of the harmful-in removing tower and a temperature monitor of the harmful-out removing tower. This improved generation sodium hypochlorite production on-line control system can promote the efficiency of sodium hypochlorite production and the quality of product.
Description
Technical Field
The utility model relates to a chemical industry technical field, in particular to improved generation sodium hypochlorite production on-line control system.
Background
Sodium hypochlorite (NaClO) is a high-efficiency oxidant and a chlorine-containing disinfectant, has the functions of bleaching, sterilization and disinfection, is used as a bleaching agent, an oxidant and a water purifying agent, is mainly used in the fields of bleaching, papermaking, spinning, pharmacy, fine chemical industry, sanitary disinfection, industrial wastewater treatment and the like, has an ever-expanding application range, and has been researched and shown nowadays.
In the prior art, the preparation method of sodium hypochlorite mainly comprises brine electrolysis and contact reaction of chlorine and sodium hydroxide, and the latter is mostly adopted for preparing the sodium hypochlorite. Because sodium hypochlorite can be decomposed under the conditions of acidity, illumination, heating or heavy metal even in the environment without a reducing agent, in order to ensure that the effective chlorine content of the product reaches the standard, the input of raw materials can be increased, thereby increasing the production cost and the cost of tail gas treatment, and the sodium hypochlorite serving as a drinking water product meets the national product standard requirements, and also meets the drinking water sanitary standard GB5749-2006 after the water is sterilized and disinfected by the sodium hypochlorite, and the chlorite and chlorate remained in the water are required to be below the limit value of 0.7 mg/L. The method has the advantages that higher requirements are provided for the production of sodium hypochlorite, the effective chlorine content must reach the standard, the control stability in the production process of the sodium hypochlorite is improved, and side reactions and decomposition are prevented; reduce the impurity content in the product. The drinking water industry requires that the chlorate content in the sodium hypochlorite product is below 0.3% (2500mg/L), and the existing patent technology preparation method for contact reaction of chlorine and sodium hydroxide has an unsatisfactory effect on controlling chlorate, so that the quality of the sodium hypochlorite related to the drinking water product is difficult to ensure.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing an online control system of improved generation sodium hypochlorite production aims at promoting the efficiency of sodium hypochlorite production and the quality of product.
In order to realize the aim, the utility model provides an improved sodium hypochlorite production online control system, which comprises an alkali distribution tank, a first alkali absorption tank, an absorption tower, a second alkali absorption tank, a harm removal tower and a sodium hypochlorite finished product tank; the first feed port and the second feed port of the alkali distribution groove are respectively communicated with an alkali liquor pipeline and an deionized water pipeline, the alkali liquor pipeline is provided with an alkali liquor flow meter and an alkali liquor automatic control valve, the deionized water pipeline is provided with an deionized water flow meter and an deionized water automatic control valve, and the outlet of the alkali distribution groove is communicated with the feed port of the first alkali absorption groove and the feed port of the second alkali absorption groove; the feed inlet of the absorption tower is communicated with a chlorine pipeline, a chlorine flow meter and a chlorine self-control valve are arranged on the chlorine pipeline, a circulating inlet and a circulating outlet of the absorption tower are respectively communicated with a circulating outlet and a circulating inlet of the first alkali absorption tank through a first circulating pipeline, and a first sodium chlorate circulating pump, a sodium hypochlorite cooler, a sodium hypochlorite flow meter, an absorption tower inlet ORP monitor, an absorption tower outlet ORP monitor, an absorption tower inlet temperature monitor and an absorption tower outlet temperature monitor are arranged on the first circulating pipeline; the feed inlet of the harm removal tower is communicated with the tail gas port of the absorption tower, the circulating inlet and the circulating outlet of the harm removal tower are respectively communicated with the circulating outlet and the circulating inlet of the second absorption alkali tank through a second circulating pipeline, and a second sodium chlorate circulating pump, a circulating alkali cooler, an ORP monitor of the harm removal tower, a temperature monitor of the harm removal tower and a temperature monitor of the harm removal tower are arranged on the second circulating pipeline; and a feed inlet of the sodium hypochlorite finished product tank is respectively communicated with the first circulating pipeline and the second circulating pipeline through a first feed pipeline and a second feed pipeline.
Optionally, the alkali distribution tank is a ceramic alkali distribution tank and is provided with a jacket temperature control device.
Optionally, the circulation inlet and the circulation outlet of the alkali-blending tank are communicated through an alkali-blending circulation pipeline, and an alkali-blending circulation pump is arranged on the alkali-blending circulation pipeline.
Optionally, the first feed inlet, the second feed inlet and the circulation inlet of the alkali distribution groove are located at the upper part of the alkali distribution groove, and the circulation outlet of the alkali distribution groove is located at the lower part of the alkali distribution groove.
Optionally, the first alkali absorption tank is a ceramic alkali absorption tank, and is provided with a jacket temperature control device.
Optionally, the circulation inlet and the feed inlet of the absorption column are located at the upper part and the lower part of the absorption column, respectively.
Optionally, the recycling inlet and the feed inlet of the pest eliminating tower are respectively positioned at the upper part and the lower part of the pest eliminating tower.
Optionally, from the circulation outlet of the first alkali absorption tank to the circulation inlet of the absorption tower, the first circulation pipeline is provided with the first sodium chlorate circulation pump, the absorption tower ORP monitor, a first switch valve, the sodium hypochlorite flow meter, the sodium hypochlorite cooler and the absorption tower temperature monitor in sequence; and the first circulating pipeline is communicated with the first feeding pipeline at a position between the ORP monitor of the absorption tower and the first switch valve, and the first feeding pipeline is provided with a second switch valve.
Optionally, from the circulation outlet of the second absorption alkali tank to the circulation inlet of the hazard eliminating tower, the second circulation pipeline is provided with the second sodium chlorate circulation pump, the hazard eliminating tower ORP monitor, a third switch valve, the circulation alkali cooler and the hazard eliminating tower temperature monitor in sequence; and the second circulating pipeline is communicated with the second feeding pipeline at a position between the harmful-feeding tower ORP monitor and the third switch valve, and the second feeding pipeline is provided with a fourth switch valve.
In the technical scheme provided by the utility model, the total amount of chlorine introduced by automatic control can be determined by the amount of the alkali liquor to prevent the over-chlorination reaction at the end point of the reaction from producing sodium chlorate; the opening of the regulating valve is controlled by a system (such as a DCS system), and the chlorine introducing speed is controlled in a linear decreasing mode (namely the chlorine introducing speed is gradually changed into 0 within a certain time after the chlorine introducing speed is stably introduced with a large chlorine introducing amount for a certain time), so that the local over-chlorination reaction can be effectively prevented from occurring in the reaction process, and sodium chlorate is generated; by utilizing the ORP on-line analysis technology, the process value and the reaction end point of the effective chlorine content of the circulating liquid are provided by the ORP monitor, the reaction end point can be quickly and accurately controlled, the content of the effective chlorine in the product is effectively ensured to reach the standard, the chemical detection frequency is reduced (the chemical detection consumes a long time), and the production efficiency is improved.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the structures shown in the drawings without creative efforts.
Fig. 1 is a schematic structural diagram of an embodiment of the improved online control system for sodium hypochlorite production provided by the present invention.
The reference numbers illustrate: an improved sodium hypochlorite production online control system 100, an alkali preparation tank 1, a first alkali absorption tank 2, an absorption tower 3, a second alkali absorption tank 4, a harmful elimination tower 5, an alkali preparation circulating pump 6, a first sodium chlorate circulating pump 7, a second sodium chlorate circulating pump 8, a sodium hypochlorite cooler 9, a circulating alkali cooler 10, an alkali liquid flowmeter 11, a deionized water flowmeter 12, a chlorine gas flowmeter 13, a sodium hypochlorite flowmeter 14, an alkali liquid automatic control valve 15, a deionized water automatic control valve 16, a chlorine gas automatic control valve 17, an absorption tower inlet ORP monitor 18, an absorption tower outlet ORP monitor 19, an absorption tower outlet temperature monitor 20, an absorption tower inlet temperature monitor 21, a harmful elimination tower inlet ORP monitor 22, a harmful elimination tower outlet ORP monitor 23, a harmful elimination tower inlet temperature monitor 24, a harmful elimination tower outlet temperature monitor 25, a sodium hypochlorite finished product tank 26, a first switch valve 27, a second switch valve 28, a third switch valve 29, a chlorine absorption tower inlet temperature monitor 13, a chlorine gas temperature, And a fourth switching valve 30.
The objects, features and advantages of the present invention will be further described with reference to the accompanying drawings.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
It should be noted that, if directional indications (such as upper, lower, left, right, front and rear … …) are involved in the embodiment of the present invention, the directional indications are only used to explain the relative position relationship between the components, the motion situation, etc. in a specific posture (as shown in the drawings), and if the specific posture is changed, the directional indications are changed accordingly.
In addition, if there is a description relating to "first", "second", etc. in the embodiments of the present invention, the description of "first", "second", etc. is for descriptive purposes only and is not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In addition, the meaning of "and/or" appearing throughout includes three juxtapositions, exemplified by "A and/or B" including either A or B or both A and B. In addition, the technical solutions in the embodiments may be combined with each other, but it must be based on the realization of those skilled in the art, and when the technical solutions are contradictory or cannot be realized, the combination of the technical solutions should not be considered to exist, and is not within the protection scope of the present invention.
Sodium hypochlorite (NaClO) is a high-efficiency oxidant and a chlorine-containing disinfectant, has the functions of bleaching, sterilization and disinfection, is used as a bleaching agent, an oxidant and a water purifying agent, is mainly used in the fields of bleaching, papermaking, spinning, pharmacy, fine chemical industry, sanitary disinfection, industrial wastewater treatment and the like, has an ever-expanding application range, and has been researched and shown nowadays.
In the prior art, the preparation method of sodium hypochlorite mainly comprises brine electrolysis and contact reaction of chlorine and sodium hydroxide, and the latter is mostly adopted for preparing the sodium hypochlorite. Because sodium hypochlorite can be decomposed under the conditions of acidity, illumination, heating or heavy metal even in the environment without a reducing agent, in order to ensure that the effective chlorine content of the product reaches the standard, the input of raw materials can be increased, thereby increasing the production cost and the cost of tail gas treatment, and the sodium hypochlorite serving as a drinking water product meets the national product standard requirements, and also meets the drinking water sanitary standard GB5749-2006 after the water is sterilized and disinfected by the sodium hypochlorite, and the chlorite and chlorate remained in the water are required to be below the limit value of 0.7 mg/L. The method has the advantages that higher requirements are provided for the production of sodium hypochlorite, the effective chlorine content must reach the standard, the control stability in the production process of the sodium hypochlorite is improved, and side reactions and decomposition are prevented; reduce the impurity content in the product. The drinking water industry requires that the chlorate content in the sodium hypochlorite product is below 0.3% (2500mg/L), and the existing patent technology preparation method for contact reaction of chlorine and sodium hydroxide has an unsatisfactory effect on controlling chlorate, so that the quality of the sodium hypochlorite related to the drinking water product is difficult to ensure.
In view of this, the utility model provides an improved generation sodium hypochlorite production on-line control system, fig. 1 is the utility model discloses an embodiment of improved generation sodium hypochlorite production on-line control system.
Specifically, referring to fig. 1, in this embodiment, the improved online control system 100 for sodium hypochlorite production includes an alkali preparation tank 1, a first alkali absorption tank 2, an absorption tower 3, a second alkali absorption tank 4, a pest eliminating tower 5, and a sodium hypochlorite finished product tank 26; the first feed inlet and the second feed inlet of the alkali distribution groove 1 are respectively communicated with an alkali liquor pipeline and an deionized water pipeline, the alkali liquor pipeline is provided with an alkali liquor flow meter 11 and an alkali liquor automatic control valve 15, the deionized water pipeline is provided with an deionized water flow meter 12 and an deionized water automatic control valve 16, and the outlet of the alkali distribution groove 1 is communicated with the feed inlet of the first alkali absorption groove 2 and the feed inlet of the second alkali absorption groove 4; the feed inlet of the absorption tower 3 is communicated with a chlorine pipeline, a chlorine flow meter 13 and a chlorine self-control valve 17 are arranged on the chlorine pipeline, a circulating inlet and a circulating outlet of the absorption tower 3 are respectively communicated with a circulating outlet and a circulating inlet of the first alkali absorption tank 2 through a first circulating pipeline, and the first circulating pipeline is provided with a first sodium chlorate circulating pump 7, a sodium hypochlorite cooler 9, a sodium hypochlorite flow meter 14, an absorption tower inlet ORP monitor 18, an absorption tower outlet ORP monitor 19, an absorption tower inlet temperature monitor 21 and an absorption tower outlet temperature monitor 20; the feed inlet of the harm removal tower 5 is communicated with the tail gas port of the absorption tower 3, the circulating inlet and the circulating outlet of the harm removal tower 5 are respectively communicated with the circulating outlet and the circulating inlet of the second absorption alkali tank 4 through a second circulating pipeline, and the second circulating pipeline is provided with a second sodium chlorate circulating pump 8, a circulating alkali cooler 10, an ORP monitor 22 of an in harm removal tower, an ORP monitor 23 of an out harm removal tower, a temperature monitor 24 of the in harm removal tower and a temperature monitor 25 of the out harm removal tower; the feed inlet of the sodium hypochlorite finished product tank 26 is respectively communicated with the first circulating pipeline and the second circulating pipeline through a first feed pipeline and a second feed pipeline.
In the technical scheme provided by the utility model, the total amount of chlorine introduced by automatic control can be determined by the amount of the alkali liquor to prevent the over-chlorination reaction at the end point of the reaction from producing sodium chlorate; the opening of the regulating valve is controlled by a system (such as a DCS system), and the chlorine introducing speed is controlled in a linear decreasing mode (namely the chlorine introducing speed is gradually changed into 0 within a certain time after the chlorine introducing speed is stably introduced with a large chlorine introducing amount for a certain time), so that the local over-chlorination reaction can be effectively prevented from occurring in the reaction process, and sodium chlorate is generated; by utilizing an ORP (Oxidation-Reduction Potential) online analysis technology, the process value and the reaction end point of the effective chlorine content of the circulating liquid are provided by an ORP monitor, the reaction end point can be quickly and accurately controlled, the content of the effective chlorine in the product can be effectively ensured to reach the standard, the chemical detection frequency is reduced (the chemical detection consumes a long time), and the production efficiency is improved.
Referring to fig. 1, in the present embodiment, the alkali distribution tank 1 is a ceramic alkali distribution tank and is provided with a jacket temperature control device. Thus, the temperature of the alkali distribution tank 1 can be controlled by the jacket temperature control device on the alkali distribution tank 1.
Referring to fig. 1, in the present embodiment, the circulation inlet and the circulation outlet of the alkali-blending tank 1 are communicated through an alkali-blending circulation pipeline, and an alkali-blending circulation pump 6 is disposed on the alkali-blending circulation pipeline. Through the arrangement of the alkali-blending circulation pipeline, the alkali solution and the deionized water entering the alkali-blending tank 1 can be uniformly mixed in the alkali-blending tank 1, and the qualified NaOH solution is obtained.
Further, in this embodiment, the first feed inlet, the second feed inlet and the circulation inlet of the alkali distribution tank 1 are all located at the upper part of the alkali distribution tank 1, and the circulation outlet of the alkali distribution tank 1 is located at the lower part of the alkali distribution tank 1. And the outlet of the alkali blending tank 1 is positioned at the lower part of the alkali blending tank 1.
Referring to fig. 1, in the present embodiment, the first alkali absorption tank 2 is a ceramic alkali absorption tank and is provided with a jacket temperature control device. Thus, the temperature of the first alkali absorption tank 2 can be controlled by the jacket temperature control device on the first alkali absorption tank 2.
Referring to fig. 1, in this embodiment, the feed inlet and the circulation inlet of the first alkali absorption tank 2 are located at the upper part of the first alkali absorption tank 2, and the circulation outlet of the first alkali absorption tank 2 is located at the lower part of the first alkali absorption tank 2.
Referring to fig. 1, in the present embodiment, the circulation inlet and the feed inlet of the absorption tower 3 are respectively located at the upper part and the lower part of the absorption tower 3. The off-gas port of the absorber 3 is located at the upper part of the absorber 3.
Referring to fig. 1, in the present embodiment, the circulation inlet and the feed inlet of the destruction tower 5 are respectively located at the upper and lower portions of the destruction tower 5. And the tail gas port and the circulating outlet of the harm removing tower 5 are respectively positioned at the upper part and the lower part of the harm removing tower 5.
Referring to fig. 1, in this embodiment, from the circulation outlet of the first alkali absorption tank 2 to the circulation inlet of the absorption tower 3, the first circulation pipeline is sequentially provided with the first sodium chlorate circulation pump 7, the absorption tower ORP monitor 18, a first on-off valve 27, the sodium hypochlorite flow meter 14, the sodium hypochlorite cooler 9, and the absorption tower temperature monitor 21; the first circulation line communicates with the first feed line at a position between the feed absorption tower ORP monitor 18 and the first on-off valve 27, and the first feed line is provided with a second on-off valve 28.
Referring to fig. 1, in the present embodiment, from the circulation outlet of the second absorption alkali tank 4 to the circulation inlet of the harmful substance removal tower 5, the second circulation pipeline is sequentially provided with the second sodium chlorate circulation pump 8, the harmful substance removal tower ORP monitor 22, the third on-off valve 29, the circulation alkali cooler 10, and the harmful substance removal tower temperature monitor 24; and the second circulation pipeline is communicated with the second feeding pipeline at a position between the harmful-feeding tower ORP monitor 22 and the third on-off valve 29, and a fourth on-off valve 30 is arranged on the second feeding pipeline.
The following is an operation mode of the improved sodium hypochlorite production online control system 100:
the amount of alkali liquor conveyed from the outer pipe is controlled by an alkali liquor flow meter 11, and the amount of deionized water conveyed from the outer pipe is controlled by a deionized water flow meter 12; the NaOH solution with the concentration of 170-180 g/l is prepared by refluxing and circulating mixing of an alkali preparation circulating pump 6, and the generated heat is taken away by jacket circulating water of an alkali preparation tank 1, so that the temperature is guaranteed to be below 40 ℃; and the NaOH solution flows into the first alkali absorption tank 2 after the preparation is qualified, and is sprayed by the upper part of the absorption tower 3 through the second first sodium chlorate circulating pump 7, the sodium hypochlorite flow meter 14 and the sodium hypochlorite cooler 9 and flows back to the first alkali absorption tank 2. The chlorine flowmeter 13 and the chlorine self-control valve 17 enter from the lower part of the absorption tower 3, the concentration of the alkali liquor is continuously reduced along with the continuous absorption of the chlorine by the sodium hydroxide solution, the DCS system controls the opening degree of the chlorine self-control valve 17, and the chlorine introducing speed is controlled in a linear decreasing mode. Chlorine gas enters the absorption tower 3 and then reversely contacts with circulating cooling alkali liquor sprayed on the upper part of the absorption tower to absorb sodium hypochlorite, and heat generated by reaction is taken away by a sodium hypochlorite cooler 9 on the first circulating pipeline and jacket circulating water of the first alkali absorption tank 2. The residual tail gas is discharged from the top of the absorption tower 3, enters the harm removal tower 5, flows into the second absorption alkali tank 4 by the alkali preparation tank 1, is conveyed by the second sodium chlorate circulating pump 8, is continuously absorbed by the sprayed alkali liquor after the circulating alkali cooler 10, and ensures that the temperature of the circulating liquid is not more than 40 ℃. And (3) carrying out product inspection when the ORP of the products in the first alkali absorption tank 2 and the second alkali absorption tank 4 is 500-600mv, and sending the products into a sodium hypochlorite finished product tank 26 after the products are qualified through inspection. An absorption tower temperature monitor 20 is installed on a blanking pipe of the absorption tower 3, an absorption tower temperature monitor 21 is installed behind a sodium hypochlorite cooler 9, an inlet harmful-removing tower temperature monitor 24 is installed behind a circulating alkali cooler 10, a harmful-removing tower temperature monitor 25 is installed on a blanking pipe of the harmful-removing tower 5, and the temperature of circulating liquid is guaranteed not to exceed 40 ℃. An absorption tower ORP monitor 18 is arranged behind the first sodium chlorate circulating pump 7, an absorption tower ORP monitor 19 is arranged on the blanking pipe of the absorption tower 3, a harm-removing tower ORP monitor 22 is arranged behind the second sodium chlorate circulating pump 8, a harm-removing tower ORP monitor 23 is arranged on the blanking pipe of the harm-removing tower 5, the ORP in the process is monitored, and product inspection is carried out when 500 mv plus 600mv is used.
The above only is the preferred embodiment of the present invention, not so limiting the patent scope of the present invention, all under the concept of the present invention, the equivalent structure transformation made by the contents of the specification and the drawings is utilized, or the direct/indirect application is included in other related technical fields in the patent protection scope of the present invention.
Claims (9)
1. An improved sodium hypochlorite production online control system is characterized by comprising an alkali preparation tank, a first alkali absorption tank, an absorption tower, a second alkali absorption tank, a pest eliminating tower and a sodium hypochlorite finished product tank;
the first feed port and the second feed port of the alkali distribution groove are respectively communicated with an alkali liquor pipeline and an deionized water pipeline, the alkali liquor pipeline is provided with an alkali liquor flow meter and an alkali liquor automatic control valve, the deionized water pipeline is provided with an deionized water flow meter and an deionized water automatic control valve, and the outlet of the alkali distribution groove is communicated with the feed port of the first alkali absorption groove and the feed port of the second alkali absorption groove;
the feed inlet of the absorption tower is communicated with a chlorine pipeline, a chlorine flow meter and a chlorine self-control valve are arranged on the chlorine pipeline, a circulating inlet and a circulating outlet of the absorption tower are respectively communicated with a circulating outlet and a circulating inlet of the first alkali absorption tank through a first circulating pipeline, and a first sodium chlorate circulating pump, a sodium hypochlorite cooler, a sodium hypochlorite flow meter, an absorption tower inlet ORP monitor, an absorption tower outlet ORP monitor, an absorption tower inlet temperature monitor and an absorption tower outlet temperature monitor are arranged on the first circulating pipeline;
the feed inlet of the harm removal tower is communicated with the tail gas port of the absorption tower, the circulating inlet and the circulating outlet of the harm removal tower are respectively communicated with the circulating outlet and the circulating inlet of the second absorption alkali tank through a second circulating pipeline, and a second sodium chlorate circulating pump, a circulating alkali cooler, an ORP monitor of the harm removal tower, a temperature monitor of the harm removal tower and a temperature monitor of the harm removal tower are arranged on the second circulating pipeline;
and a feed inlet of the sodium hypochlorite finished product tank is respectively communicated with the first circulating pipeline and the second circulating pipeline through a first feed pipeline and a second feed pipeline.
2. The improved online control system for sodium hypochlorite production as claimed in claim 1, wherein the alkali distribution tank is a ceramic alkali distribution tank and is provided with a jacket temperature control device.
3. The improved online control system for sodium hypochlorite production as claimed in claim 1, wherein the circulation inlet and the circulation outlet of the alkali-blending tank are communicated through an alkali-blending circulation pipeline, and an alkali-blending circulation pump is arranged on the alkali-blending circulation pipeline.
4. The improved online control system for sodium hypochlorite production as claimed in claim 3, wherein the first feeding port, the second feeding port and the recycling inlet of the alkali distribution tank are all located at the upper part of the alkali distribution tank, and the recycling outlet of the alkali distribution tank is located at the lower part of the alkali distribution tank.
5. The improved online control system for sodium hypochlorite production as claimed in claim 1, wherein the first alkali absorption tank is a ceramic alkali absorption tank and is provided with a jacket temperature control device.
6. The improved online control system for sodium hypochlorite production as claimed in claim 1, wherein the circulation inlet and the feed inlet of the absorption tower are respectively located at the upper part and the lower part of the absorption tower.
7. The improved online control system for sodium hypochlorite production as claimed in claim 1, wherein the recycling inlet and the feed inlet of the pest eliminating tower are respectively located at the upper part and the lower part of the pest eliminating tower.
8. The improved online control system for sodium hypochlorite production as claimed in claim 1, wherein the first circulating pipeline is sequentially provided with the first sodium chlorate circulating pump, the absorption tower ORP monitor, a first switch valve, the sodium hypochlorite flow meter, the sodium hypochlorite cooler and the absorption tower temperature monitor from the circulating outlet of the first alkali absorption tank to the circulating inlet of the absorption tower; and the first circulating pipeline is communicated with the first feeding pipeline at a position between the ORP monitor of the absorption tower and the first switch valve, and the first feeding pipeline is provided with a second switch valve.
9. The improved online control system for sodium hypochlorite production as claimed in claim 1, wherein the second circulating pipeline is provided with the second sodium chlorate circulating pump, the harm-eliminating-tower ORP monitor, a third switch valve, the circulating alkali cooler and the harm-eliminating-tower temperature monitor in sequence from the circulating outlet of the second absorption alkali tank to the circulating inlet of the harm-eliminating tower; and the second circulating pipeline is communicated with the second feeding pipeline at a position between the harmful-feeding tower ORP monitor and the third switch valve, and the second feeding pipeline is provided with a fourth switch valve.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115196600A (en) * | 2021-04-10 | 2022-10-18 | 惠州科创美环保技术有限公司 | Novel sodium hypochlorite production process |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115196600A (en) * | 2021-04-10 | 2022-10-18 | 惠州科创美环保技术有限公司 | Novel sodium hypochlorite production process |
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