CN214456850U - High-purity sodium chlorite waste-discharge-free production system - Google Patents
High-purity sodium chlorite waste-discharge-free production system Download PDFInfo
- Publication number
- CN214456850U CN214456850U CN202120469980.5U CN202120469980U CN214456850U CN 214456850 U CN214456850 U CN 214456850U CN 202120469980 U CN202120469980 U CN 202120469980U CN 214456850 U CN214456850 U CN 214456850U
- Authority
- CN
- China
- Prior art keywords
- storage tank
- pipeline
- sodium chlorite
- inlet
- tank
- 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.)
- Expired - Fee Related
Links
- UKLNMMHNWFDKNT-UHFFFAOYSA-M sodium chlorite Chemical compound [Na+].[O-]Cl=O UKLNMMHNWFDKNT-UHFFFAOYSA-M 0.000 title claims abstract description 48
- 229960002218 sodium chlorite Drugs 0.000 title claims abstract description 48
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 43
- 238000010521 absorption reaction Methods 0.000 claims abstract description 41
- 238000003860 storage Methods 0.000 claims abstract description 39
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 36
- 239000002699 waste material Substances 0.000 claims abstract description 29
- 238000001704 evaporation Methods 0.000 claims abstract description 22
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 21
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 claims abstract description 20
- 230000008020 evaporation Effects 0.000 claims abstract description 14
- 239000007787 solid Substances 0.000 claims abstract description 13
- 238000001035 drying Methods 0.000 claims abstract description 12
- 239000000428 dust Substances 0.000 claims description 11
- 238000012546 transfer Methods 0.000 claims description 8
- 238000004806 packaging method and process Methods 0.000 claims description 6
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 abstract description 60
- 239000004155 Chlorine dioxide Substances 0.000 abstract description 30
- 235000019398 chlorine dioxide Nutrition 0.000 abstract description 30
- 239000000047 product Substances 0.000 abstract description 18
- 239000002253 acid Substances 0.000 abstract description 9
- WBHQBSYUUJJSRZ-UHFFFAOYSA-M sodium bisulfate Chemical compound [Na+].OS([O-])(=O)=O WBHQBSYUUJJSRZ-UHFFFAOYSA-M 0.000 abstract description 9
- 229910000342 sodium bisulfate Inorganic materials 0.000 abstract description 9
- 238000001816 cooling Methods 0.000 abstract description 4
- 238000005119 centrifugation Methods 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 3
- 239000006227 byproduct Substances 0.000 abstract description 2
- 238000002425 crystallisation Methods 0.000 abstract description 2
- 230000008025 crystallization Effects 0.000 abstract description 2
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000000463 material Substances 0.000 abstract description 2
- 238000002360 preparation method Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 22
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 18
- 239000000243 solution Substances 0.000 description 14
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 239000000460 chlorine Substances 0.000 description 6
- 229910052801 chlorine Inorganic materials 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000002994 raw material Substances 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 5
- 239000012535 impurity Substances 0.000 description 4
- 150000002989 phenols Chemical class 0.000 description 4
- 239000011265 semifinished product Substances 0.000 description 4
- 239000011780 sodium chloride Substances 0.000 description 4
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 238000005868 electrolysis reaction Methods 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- XTEGARKTQYYJKE-UHFFFAOYSA-M Chlorate Chemical compound [O-]Cl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-M 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 239000007844 bleaching agent Substances 0.000 description 2
- 229910001919 chlorite Inorganic materials 0.000 description 2
- 229910052619 chlorite group Inorganic materials 0.000 description 2
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 239000000645 desinfectant Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000011946 reduction process Methods 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- ZKQDCIXGCQPQNV-UHFFFAOYSA-N Calcium hypochlorite Chemical compound [Ca+2].Cl[O-].Cl[O-] ZKQDCIXGCQPQNV-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- -1 chlorine ions Chemical class 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000004332 deodorization Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005684 electric field Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model provides a high-purity sodium chlorite waste-free discharge production system, which comprises a main generator and an auxiliary generator, wherein the main generator is respectively communicated with a hydrogen peroxide storage tank, a sulfuric acid storage tank and a sodium chlorate solution storage tank through pipelines, a discharge port of the main generator is connected with a feed port of the auxiliary generator, and the auxiliary generator is communicated with the hydrogen peroxide storage tank; chlorine dioxide gas generated by the main generator and the auxiliary generator is absorbed by the absorption kettle to form sodium chlorite, and a high-purity sodium chlorite finished product is obtained through evaporation concentration, cooling crystallization, centrifugation and drying; evaporating and concentrating the waste liquid generated by the secondary generator, cooling and crystallizing, and centrifugally drying to obtain a sodium bisulfate finished product; through the utility model discloses a system realizes high-purity chlorine dioxide's preparation, reduces corresponding purification equipment, and when obtaining high-purity sodium chlorite, the waste acid liquid of make full use of output produces sodium bisulfate byproduct, has realized that no waste acid and solid abandonment are arranged outward, and material saving, the energy consumption is low.
Description
Technical Field
The utility model belongs to the chemical industry field, concretely relates to high-purity sodium chlorite does not have useless emission production system.
Background
Sodium chlorite is a high-efficiency oxidant and bleaching agent, its theoretical available chlorine content is 157%, and its available chlorine content of industrial product whose purity is above 80% also can be up to 130%, and is equal to 7 times of bleaching powder. With the increasing awareness, sodium chlorite, especially as a fourth generation disinfectant, chlorine dioxide, has the effects of sterilization, algae removal, disinfection and deodorization as the most important raw material for producing chlorine dioxide, and can remove phenols and phenolic compounds from water polluted by phenols or phenolic compounds after treatment. Sodium chlorite as a carrier of high-efficiency oxidants, bleaches and disinfectants has increasingly growing market demand and high market price. But also belongs to the environmental protection industry of novel chlorine dioxide which is vigorously developed by China. At present, the waste acid liquor generated in the production of sodium chlorite is directly discharged, can pollute the environment, and the generated waste liquor is generally discharged into a collecting tank for centralized treatment, and is discharged after reaching the standard, and useful components contained in the waste liquor are not effectively recycled, so that the waste of raw materials is caused.
The production process of sodium chlorite is generally divided into an electrolytic process and a reduction process. The electrolysis method is to dissolve sodium chlorate in water and add sulfuric acid to prepare mixed solution which is added into a chlorine dioxide generator. Then the mixed gas (containing SO) of sulfur dioxide and air is mixed28% -10%) of chlorine dioxide, introducing the chlorine dioxide into a chlorine dioxide generator to react to produce chlorine dioxide gas, and sending the chlorine dioxide gas into a cathode chamber of an electrolytic cell. Brine and distilled water are continuously introduced into the anode chamber of the tank for electrolysis. The chlorine dioxide gets electrons from the cathode and turns into chlorite, and the chlorine ions are discharged at the anode and turned into chlorine gas to be discharged. Under the action of DC electric field, sodium ions are combined with chlorite at cathode to form sodium chlorite, which is evaporated, crystallized and dried to obtain solid product. The electrolysis method has the disadvantages of large power consumption, large factory building investment, complex production process and operation, generation of a large amount of chlorine, environmental pollution and gradual elimination at present when energy conservation and emission reduction are advocated.
The reduction method production process can be divided into two steps, wherein the first step is to reduce sodium chlorate or other chlorate in an acid medium to generate chlorine dioxide gas; and the second step is to absorb chlorine dioxide gas by caustic soda solution under the action of reducing agent to prepare sodium chlorite solution, and then sodium chlorite solution product with certain concentration is prepared after filtration and impurity removal. In the reduction process, the purity and efficiency of the chlorine dioxide gas generated in the first step often affect the purity of the final sodium chlorite product and the production cost of the whole process. At present, the production methods of chlorine dioxide mainly comprise a methanol method, a sulfur dioxide method, a hydrochloric acid method, a sodium chloride method and the like. They all reduce sodium chlorate under acidic conditions using a reducing agent. Although the hydrochloric acid method and the sodium chloride method have high reaction speed, 0.5mol of chlorine gas is generated every 1mol of chlorine dioxide is generated theoretically; although the chlorine generated by the methanol method and the sulfur dioxide method is less than that generated by taking chloride ions as a reducing agent, the reaction efficiency of the methanol method and the sulfur dioxide method is relatively low, and the products are impure, and moreover, formaldehyde, formic acid, methanol which is not completely reacted and sulfur dioxide which is not completely reacted in the methanol method pollute the chlorine dioxide product. In the second step of reaction for preparing sodium chlorite, chlorine in chlorine dioxide and caustic soda in the absorption liquid can easily produce sodium chloride and sodium chlorate, so that the impurity of sodium chlorite is increased, and when the sodium chlorite solution product or crystal product is prepared, the process of evaporating, filtering and removing impurity is required. On the other hand, in the methanol method, the sulfur dioxide method, the hydrochloric acid method and the sodium chloride method, the conversion rate of chlorine dioxide of key components of sodium chlorate in the reaction is relatively low in the process of producing the chlorine dioxide. In order to obtain relatively pure chlorine dioxide and, consequently, high purity sodium chlorite, a purification device is usually added after the chlorine dioxide generator, which further increases the cost.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a high-purity sodium chlorite does not have useless discharge production system realizes not having useless the emission, reduction in production cost, improvement productivity.
The utility model adopts the technical proposal that: a high-purity sodium chlorite no-waste discharge production system comprises a main generator, an auxiliary generator, a hydrogen peroxide solution storage tank, a sulfuric acid storage tank and a sodium chlorate solution storage tank; the hydrogen peroxide storage tank, the sulfuric acid storage tank and the sodium chlorate solution storage tank are respectively communicated with the main generator through pipelines, a discharge hole of the main generator is connected with a feed hole of the auxiliary generator through a pipeline, and the auxiliary generator is communicated with the hydrogen peroxide storage tank through a pipeline; the top parts of the main generator and the auxiliary generator are respectively communicated with an absorption kettle through pipelines, the absorption kettle is connected with a hydrogen peroxide storage tank and an absorption liquid storage tank through pipelines, one side of the absorption kettle is connected with an absorption liquid circulating pipeline, a circulating pump is installed on the circulating pipeline, the absorption kettle is connected with a tail gas absorption tank through a pipeline, the tail gas absorption tank is connected with an air inlet of a Roots blower through a pipeline, and an air outlet of the Roots blower is connected to the main generator through a pipeline; the outlet of the absorption kettle is connected with a sodium chlorite intermediate tank through a pipeline, and the sodium chlorite intermediate tank is respectively connected with a first evaporating tank and a sodium chlorite storage tank through pipelines; the outlet of the first evaporating pot is communicated with the inlet of the first crystallizer through a pipeline, the outlet of the first crystallizer is connected with the inlet of the first centrifugal machine, the solid outlet of the first centrifugal machine is communicated with the inlet of the first drying machine, and each connecting pipeline is internally provided with a control valve.
Further, the first centrifuge liquid outlet is in communication with the first crystallizer inlet.
Furthermore, a discharge port of the auxiliary generator is connected with an input end of a waste liquid transfer pump through a pipeline, an output end of the waste liquid transfer pump is connected to a waste liquid intermediate tank, the waste liquid intermediate tank is connected with a second evaporation tank, the second evaporation tank is communicated with an inlet of a second crystallizer through a pipeline, an outlet of the second crystallizer is connected with an inlet of a second centrifuge, and a solid outlet of the second centrifuge is communicated with an inlet of a second dryer.
Further, the liquid outlet of the second centrifuge is communicated with the inlet of the main generator.
Furthermore, the device also comprises a packaging machine, and the outlet of the first dryer is connected with the inlet of the packaging machine.
Furthermore, a dust remover is arranged on the first dryer, and a dust outlet of the dust remover is connected with an inlet of the packaging machine.
Compared with the prior art, the beneficial effects of the utility model are that:
1. the utility model discloses a system collection owner, vice generator, jet pump, evaporating pot, crystallizer, centrifuge, desiccator in an organic whole to sodium chlorate, hydrogen peroxide solution, sulphuric acid, sodium hydroxide etc. are raw materials, and the purity that generates chlorine dioxide is high, impurity content is few, need not to filter purification equipment such as edulcoration, can obtain high-purity sodium chlorite, and simultaneously, the waste acid liquid production sodium bisulfate byproduct of this system make full use of output has realized that no waste acid and solid abandonment are arranged outward, and the material saving, the energy consumption is low.
2. The utility model discloses a system utilizes the spent acid production sodium bisulfate, makes the spent acid obtain effective utilization, but mother liquor recycle again, reduces the raw materials and uses, and reduce cost makes the spent acid not arrange outward, environmental protection most importantly.
3. The utility model discloses a dispose the chlorine dioxide in the tail gas absorption tank further absorbs tail gas, reach no exhaust emission.
4. The system of the utility model has the advantages of high utilization rate of sodium chlorate raw material, simple production process of sodium chlorite, small equipment investment, strong stability, convenient operation and easy control.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
In the figure: 1. a main generator; 2. a secondary generator; 3. an injection pump; 4. a sulfuric acid storage tank; 5. a hydrogen peroxide storage tank; 6. a sodium chlorate solution storage tank; 7. an absorption kettle; 8. a tail gas absorption tank; 9. a Roots blower; 10. a first evaporator tank; 11. a first crystallizer; 12. a first centrifuge; 13. a first dryer; 14. a transfer pump; 15. a waste liquid intermediate tank; 16. a sodium chlorite intermediate tank; 17. a second evaporator tank; 18. a second crystallizer; 19. a second centrifuge; 20. a second dryer; 21. a dust remover; 22. a packaging machine; 23. a circulation pump; 24. a cooler; 25. and an absorption liquid storage tank.
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 work belong to the protection scope of the present invention.
As shown in fig. 1, a high-purity sodium chlorite waste-discharge-free production system comprises a main generator 1, an auxiliary generator 2, a hydrogen peroxide storage tank 5, a sulfuric acid storage tank 4 and a sodium chlorate solution storage tank 6; the hydrogen peroxide storage tank 5, the sulfuric acid storage tank 4 and the sodium chlorate solution storage tank 6 are respectively communicated with the main generator 1 through pipelines, a control valve is arranged in each pipeline, a discharge hole of the main generator is connected with a feed hole of the auxiliary generator 2 through a pipeline, and meanwhile, the feed hole of the auxiliary generator 2 is communicated with the hydrogen peroxide storage tank 5 through a pipeline; a jet pump 3 is connected between a main generator 1 and an absorption kettle 7, the top of an auxiliary generator 2 is communicated with the absorption kettle 7 through a pipeline, the absorption kettle 7 is connected with a hydrogen peroxide storage tank 5 through a pipeline, a control valve is installed in each connecting pipeline, one side of the absorption kettle 7 is connected with an absorption liquid circulating pipeline, the absorption liquid circulating pipeline is communicated with an absorption liquid storage tank 25, a circulating pump 23 is installed on the absorption liquid circulating pipeline, the absorption liquid circulating pipeline is cooled through a cooler 24, the absorption kettle 7 is connected with a tail gas absorption tank 8 through a pipeline, the outlet of the tail gas absorption tank 8 is connected with the air inlet of a Roots blower 9 through a pipeline, and the air outlet of the Roots blower 9 is connected to the main generator 1 through a pipeline; the absorption liquid circulating pipeline is connected with a sodium chlorite intermediate tank 16 through a pipeline, and the sodium chlorite intermediate tank is respectively connected with the first evaporating tank 10 and a sodium chlorite storage tank through a pumping pipeline; the first evaporation tank 10 is communicated with an inlet of a first crystallizer 11 through a pipeline, an outlet of the first crystallizer 11 is connected with an inlet of a first centrifugal machine 12, a solid outlet of the first centrifugal machine 12 is communicated with an inlet of a first drying machine 13, and a liquid outlet of the first centrifugal machine is communicated with an inlet of the first crystallizer 11.
The auxiliary generator 2 is connected with the input end of a waste liquid transfer pump 14 through a pipeline, the output end of the waste liquid transfer pump 14 is communicated with a waste liquid intermediate tank 15 through a pipeline, the waste liquid intermediate tank 15 is connected with a second evaporation tank 17, the second evaporation tank 17 is communicated with the inlet of a second crystallizer 18 through a pipeline, the outlet of the second crystallizer 18 is connected with the inlet of a second centrifugal machine 19, and the solid outlet of the second centrifugal machine 19 is communicated with the inlet of a second drying machine 20.
The utility model discloses a theory of operation: sodium chlorate solution, sulfuric acid solution and hydrogen peroxide are added into a main generator 1 in a fixed ratio, sodium chlorate is reduced by the hydrogen peroxide to generate chlorine dioxide gas under an acidic state, a certain temperature and a certain pressure, the chlorine dioxide gas enters an absorption kettle 7 through a jet pump 3, in this stage, in order to ensure that chemical reaction is completely carried out, the solution slowly reacting or incompletely reacting in the main generator enters an auxiliary generator 2 and is carried out in the auxiliary generator 2, the hydrogen peroxide is added into the auxiliary generator 2 to prevent the chlorine dioxide gas from being reduced into the sodium chlorate, the sodium chlorate which is not completely reacted is prevented from being discharged along with residual liquid to cause waste of raw materials, oxygen and the chlorine dioxide gas generated in the process enter the absorption kettle 7 through a pipeline, the chlorine dioxide gas entering the absorption kettle 7 is subjected to next reaction, and is circularly absorbed by absorption liquid to form a sodium chlorite product which enters a sodium chlorite intermediate tank 16, if a liquid sodium chlorite product is needed, pumping the liquid sodium chlorite product into a sodium chlorite storage tank, if a solid sodium chlorite product is needed, sending the solid sodium chlorite product into a first evaporation tank 10 for evaporation and concentration, then sending the solid sodium chlorite product into a first crystallizer 11 for cooling and crystallization, sending a solid semi-finished product from the crystallizer into a first centrifuge 12 for centrifugation, sending a sodium chlorite solid obtained after the first centrifuge into a first dryer 13, drying the first dryer 13 by using a fluidized drying bed through the first dryer 13 to obtain a finished product, and conveying the finished product to a packing machine 22 for packing; the liquid obtained by centrifugation enters a first evaporation tank 10 in the process to continuously participate in evaporation and concentration, and the liquid is recycled. During the drying process, sodium chlorite dust is generated, dust is removed by arranging a dust remover 21, and the powder collected by dust removal is conveyed to a packing machine 22 for recycling.
The waste liquid generated in the auxiliary generator 2 is output to a waste liquid intermediate tank 15 through a transfer pump 14, the waste liquid in the waste liquid intermediate tank 15 enters a second evaporation tank 17 for evaporation and concentration to form a sodium bisulfate semi-finished product, then enters a second crystallizer 18 for cooling, crystals of the cooled sodium bisulfate semi-finished product are separated out, the sodium bisulfate semi-finished product is dehydrated through a second centrifugal machine 19, sodium bisulfate is recovered and dried through a second drying machine 20, the second drying machine 20 adopts a fluidized drying bed to obtain a sodium bisulfate finished product, and the separated sodium chlorate solution alkaline solution returns to the main generator 1 to continuously participate in the reaction.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (6)
1. A high-purity sodium chlorite waste-discharge-free production system is characterized in that: comprises a main generator, an auxiliary generator, a hydrogen peroxide storage tank, a sulfuric acid storage tank and a sodium chlorate solution storage tank; the hydrogen peroxide storage tank, the sulfuric acid storage tank and the sodium chlorate solution storage tank are respectively communicated with the main generator through pipelines, a discharge hole of the main generator is connected with a feed hole of the auxiliary generator through a pipeline, and the auxiliary generator is communicated with the hydrogen peroxide storage tank through a pipeline; the top parts of the main generator and the auxiliary generator are respectively communicated with an absorption kettle through pipelines, the absorption kettle is connected with a hydrogen peroxide storage tank and an absorption liquid storage tank through pipelines, one side of the absorption kettle is connected with an absorption liquid circulating pipeline, a circulating pump is installed on the circulating pipeline, the absorption kettle is connected with a tail gas absorption tank through a pipeline, the tail gas absorption tank is connected with an air inlet of a Roots blower through a pipeline, and an air outlet of the Roots blower is connected to the main generator through a pipeline; the outlet of the absorption kettle is connected with a sodium chlorite intermediate tank through a pipeline, and the sodium chlorite intermediate tank is respectively connected with a first evaporating tank and a sodium chlorite storage tank through pipelines; the outlet of the first evaporating pot is communicated with the inlet of the first crystallizer through a pipeline, the outlet of the first crystallizer is connected with the inlet of the first centrifugal machine, the solid outlet of the first centrifugal machine is communicated with the inlet of the first drying machine, and each connecting pipeline is internally provided with a control valve.
2. The system according to claim 1, wherein the system comprises: the first centrifuge liquid outlet is communicated with the first crystallizer inlet.
3. The system for producing high-purity sodium chlorite without waste discharge according to claim 1 or 2, wherein: the discharge port of the auxiliary generator is connected with the input end of a waste liquid transfer pump through a pipeline, the output end of the waste liquid transfer pump is connected to a waste liquid intermediate tank, the waste liquid intermediate tank is connected with a second evaporation tank, the second evaporation tank is communicated with the inlet of a second crystallizer through a pipeline, the outlet of the second crystallizer is connected with the inlet of a second centrifuge, and the solid outlet of the second centrifuge is communicated with the inlet of a second dryer.
4. The system according to claim 3, wherein the system comprises: the liquid outlet of the second centrifugal machine is communicated with the inlet of the main generator.
5. The system for the waste-free production of high-purity sodium chlorite according to claim 1, 2 or 4, wherein: the outlet of the first dryer is connected with the inlet of the packaging machine.
6. The system according to claim 5, wherein the system comprises: the first drier is provided with a dust remover, and a dust outlet of the dust remover is connected with an inlet of the packaging machine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120469980.5U CN214456850U (en) | 2021-03-04 | 2021-03-04 | High-purity sodium chlorite waste-discharge-free production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120469980.5U CN214456850U (en) | 2021-03-04 | 2021-03-04 | High-purity sodium chlorite waste-discharge-free production system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214456850U true CN214456850U (en) | 2021-10-22 |
Family
ID=78152641
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120469980.5U Expired - Fee Related CN214456850U (en) | 2021-03-04 | 2021-03-04 | High-purity sodium chlorite waste-discharge-free production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214456850U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116462160A (en) * | 2023-03-29 | 2023-07-21 | 大连交通大学 | By flue gas SO 2 Method and system for preparing steady-state chlorine dioxide for raw materials |
-
2021
- 2021-03-04 CN CN202120469980.5U patent/CN214456850U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116462160A (en) * | 2023-03-29 | 2023-07-21 | 大连交通大学 | By flue gas SO 2 Method and system for preparing steady-state chlorine dioxide for raw materials |
| CN116462160B (en) * | 2023-03-29 | 2024-05-24 | 大连交通大学 | By flue gas SO2Method and system for preparing steady-state chlorine dioxide for raw materials |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN112811444B (en) | PTA incineration boiler ash solution salt separation crystallization process | |
| CN106517256A (en) | Method for producing lithium hydroxide monohydrate from lithium carbonate | |
| CN115947486B (en) | Desulfurization waste liquid recycling treatment process and system | |
| CN1235913C (en) | Production for stable chlorinedioxide solution | |
| CN214456850U (en) | High-purity sodium chlorite waste-discharge-free production system | |
| CN106995398A (en) | L proline novel technology for extracting | |
| CN217149037U (en) | Vinylene carbonate production system | |
| CN103224246B (en) | Chemical gypsum-to-ammonium sulfate reaction slurry concentration, waste heat recovery and waste ammonia recovery method | |
| CN108569812B (en) | Treatment system and treatment method for wastewater containing low-concentration sulfuric acid | |
| CN1128095C (en) | Large high-purity chlorine dioxide generator and its production process | |
| CN111807394B (en) | Method for removing organic matters from Bayer process mother liquor | |
| CN111559750A (en) | Efficient continuous electronic-grade lithium fluoride production process | |
| CN112678973B (en) | Method for dechlorinating ammonia flue gas desulfurization circulating liquid | |
| CN216073085U (en) | Household garbage incineration fly ash recycling treatment system | |
| CN113274882B (en) | Ammonium adipate waste liquid recovery method and device based on high-temperature bipolar membrane electrodialysis | |
| CN110436679A (en) | The devices and methods therefor of lithium carbonate wash water comprehensive utilization of resources | |
| CN105237402A (en) | Method and device capable of continuously preparing nitrous acid ester | |
| CN214422763U (en) | Water electrolysis hydrogen production pure oxygen recycle device | |
| CN111349015A (en) | Clean production process of monoamino anthraquinone | |
| CN109721035B (en) | Purification and concentration process of waste dilute sulfuric acid | |
| CN113800541A (en) | Processing technology for refining lithium chloride by lithium carbonate precipitation and conversion | |
| CN111196597A (en) | Method for producing chlorine dioxide and potassium sulfate | |
| CN209957374U (en) | Sodium chlorite production equipment with high capacity and no waste acid discharge | |
| CN219860931U (en) | Waste water utilization system for producing trichloroisocyanuric acid | |
| CN217795511U (en) | Production system for preparing iron phosphate from glyphosate mother liquor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20211022 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |