CN103772306A - Production method of sodium dichloro isocyanurate - Google Patents
Production method of sodium dichloro isocyanurate Download PDFInfo
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- CN103772306A CN103772306A CN201410032987.5A CN201410032987A CN103772306A CN 103772306 A CN103772306 A CN 103772306A CN 201410032987 A CN201410032987 A CN 201410032987A CN 103772306 A CN103772306 A CN 103772306A
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- chlorine
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- chlorination reaction
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D251/00—Heterocyclic compounds containing 1,3,5-triazine rings
- C07D251/02—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings
- C07D251/12—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings having three double bonds between ring members or between ring members and non-ring members
- C07D251/26—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings having three double bonds between ring members or between ring members and non-ring members with only hetero atoms directly attached to ring carbon atoms
- C07D251/30—Only oxygen atoms
- C07D251/36—Only oxygen atoms having halogen atoms directly attached to ring nitrogen atoms
Abstract
The invention discloses a production method of sodium dichloro isocyanurate. A sodium dichloro isocyanurate product is obtained by the following steps: dosing; pre-chlorination; chlorination; analysis; neutralization; and drying. In the production process disclosed by the invention, not only are the product quality and production technology process normal, but also the production cost is greatly lowered due to adjustment of raw materials. As heat exchange in chlorination is skillfully utilized, heat energy of chlorination is used for gasifying liquid chlorine. Cold water generated by gasifying liquid chlorine is used for cooling chlorination, so that the conventional production process is fully changed, and the equipment investment is saved and the energy is saved and the consumption is reduced. The process guarantees that the production is safe and stable through dosing and gasifying the liquid chlorine by hot water.
Description
Technical field
The production method that the present invention relates to a kind of Surchlor GR 60, belongs to chemical field.
Background technology
The production method of Surchlor GR 60 is that soda ash, tricarbimide and process water are prepared by a certain percentage in absorption kettle, the material of preparation is added in chlorination tank, pass into slowly chlorine temperature lower than 30 ℃, and under agitation reaction, chlorine used is that liquid chlorine obtains by gasification.In this technological process, use cool ice mechanism cold to be used for controlling temperature, its power consumption is quite high; And the vaporization of the gasification of liquid chlorine use steam heating, facility investment is large, needs to consume a large amount of steam in production, and in the process of logical steam, can make the pressure of liquid chlorine tank sharply raise, and is not easy to control, and has potential safety hazard.
Summary of the invention
The object of the invention is to solve the problem existing in current techniques, the production method of the Surchlor GR 60 that a kind of equipment investment is few, energy-saving and cost-reducing, production cost is low, production safety is stable is provided.
For achieving the above object, the technology used in the present invention means are: a kind of production method of Surchlor GR 60, and step is as follows:
Step 1, batching: by cyanuric acid: calcium carbonate: water mixes by weight 1～1.2:0.7～1.0:7～16, add and in batching kettle, stir into slurries;
Step 2, prechlorination reaction: slurries are sent into and carried out prechlorination reaction in prechlorination reactor;
Step 3, chlorination reaction: step 2 is through the reacted slurries of prechlorination, enter again and in differential hydrokineter, carry out chlorination reaction, liquid chlorine is carried out to liquid chlorine vaporizing through chlorine liquid carburetor is chlorine simultaneously, pass into differential hydrokineter bottom, temperature of reaction is 10 ℃～30 ℃, and the prechlorination reactor recycling in step 2 is sent in the chlorine residue producing in chlorination reaction back to;
Step 4, parsing: the material after chlorination reaction adopts whizzer to carry out liquid-solid separation, liquid after separation carries out sedimentation dechlorination, in liquid, add hydrochloric acid, the weight that adds hydrochloric acid is liquid weight 0.1%～0.3%, after decomposing, be cyanuric acid and chlorine, chlorine sends back to the prechlorination reactor in step 2;
Step 5, neutralization: the filter cake obtaining after centrifugal washes with water, after washing, washing water are admitted to batching kettle; Filter cake after washing is carried out to solid phase neutralization with soda ash, pH value 5.8～6.5;
Step 6, dry: the filter cake after neutralization adopts air-flow to be dried, dry rear available chlorine is greater than 60%, and pH value 6.0～7.0, obtains Surchlor GR 60 product.
Further, the heat that in described step 3, liquid chlorine vaporizing utilization produces in the time of chlorination reaction by heat exchange lower the temperature produce hot water, hot water enters in chlorine liquid carburetor by water pump, for liquid chlorine vaporizing, liquid chlorine vaporization heat-absorption water temperature drop is low, after heat exchange, cold water is used further to chlorination reaction cooling, and entering chlorine liquid carburetor water temp is 30～20 ℃, and going out vaporizer water temperature is 10～20 ℃.
Beneficial effect of the present invention is: in this production technique, the adjustment of raw material not only can guarantee that the quality of product and the technological process of production are normal, greatly reduce production cost simultaneously; Owing to having utilized cleverly heat exchange in chlorination reaction, by the heat energy of chlorination reaction, for liquid chlorine vaporizing, the cold water producing after liquid chlorine vaporizing is lowered the temperature for chlorination reaction, fully changes traditional production technique, has saved equipment investment, energy-saving and cost-reducing; This technique has guaranteed that by batching and the gasification of liquid chlorine hot water production safety is stable.
Accompanying drawing explanation
Below in conjunction with drawings and Examples, the present invention is further described.
Fig. 1 is process flow sheet of the present invention.
Embodiment
embodiment 1
A production method for Surchlor GR 60, step is as follows:
Step 1, batching: by cyanuric acid: calcium carbonate: water mixes by weight 1:0.7:7, add and in batching kettle, stir into slurries,
Step 2, prechlorination reaction: slurries are sent into and carried out prechlorination reaction in prechlorination reactor;
Step 3, chlorination reaction: step 2 is through the reacted slurries of prechlorination, enter again and in differential hydrokineter, carry out chlorination reaction, liquid chlorine is carried out to liquid chlorine vaporizing through chlorine liquid carburetor is chlorine simultaneously, pass into differential hydrokineter bottom, temperature of reaction is 10 ℃～30 ℃, and the prechlorination reactor recycling in step 2 is sent in the chlorine residue producing in chlorination reaction back to; The heat that described liquid chlorine vaporizing utilization produces in the time of chlorination reaction by heat exchange lower the temperature produce hot water, hot water enters in chlorine liquid carburetor by water pump, for liquid chlorine vaporizing, liquid chlorine vaporization heat-absorption water temperature drop is low, after heat exchange, cold water is used further to chlorination reaction cooling, entering chlorine liquid carburetor water temp is 30～20 ℃, and going out vaporizer water temperature is 10～20 ℃.
Step 4, parsing: the material after chlorination reaction adopts whizzer to carry out liquid-solid separation, liquid after separation carries out sedimentation dechlorination, in liquid, add hydrochloric acid, the weight that adds hydrochloric acid is liquid weight 0.15%, after decomposing, be cyanuric acid and chlorine, chlorine sends back to the prechlorination reactor in step 2;
Step 5, neutralization: the filter cake obtaining after centrifugal washes with water, after washing, washing water are admitted to batching kettle; Filter cake after washing is carried out to solid phase neutralization with soda ash, pH value 6.0;
Step 6, dry: the filter cake after neutralization adopts air-flow to be dried, dry rear available chlorine is greater than 60%, and pH value 6.0, obtains Surchlor GR 60 product.
embodiment 2
A production method for Surchlor GR 60, step is as follows:
Step 1, batching: by cyanuric acid: calcium carbonate: water mixes by weight 1.2:1.0:10, add and in batching kettle, stir into slurries,
Step 2, prechlorination reaction: slurries are sent into and carried out prechlorination reaction in prechlorination reactor;
Step 3, chlorination reaction: step 2 is through the reacted slurries of prechlorination, enter again and in differential hydrokineter, carry out chlorination reaction, liquid chlorine is carried out to liquid chlorine vaporizing through chlorine liquid carburetor is chlorine simultaneously, pass into differential hydrokineter bottom, temperature of reaction is 10 ℃～30 ℃, and the prechlorination reactor recycling in step 2 is sent in the chlorine residue producing in chlorination reaction back to; The heat that described liquid chlorine vaporizing utilization produces in the time of chlorination reaction by heat exchange lower the temperature produce hot water, hot water enters in chlorine liquid carburetor by water pump, for liquid chlorine vaporizing, liquid chlorine vaporization heat-absorption water temperature drop is low, after heat exchange, cold water is used further to chlorination reaction cooling, entering chlorine liquid carburetor water temp is 30～20 ℃, and going out vaporizer water temperature is 10～20 ℃.
Step 4, parsing: the material after chlorination reaction adopts whizzer to carry out liquid-solid separation, liquid after separation carries out sedimentation dechlorination, in liquid, add hydrochloric acid, the weight that adds hydrochloric acid is liquid weight 0.2%, after decomposing, be cyanuric acid and chlorine, chlorine sends back to the prechlorination reactor in step 2;
Step 5, neutralization: the filter cake obtaining after centrifugal washes with water, after washing, washing water are admitted to batching kettle; Filter cake after washing is carried out to solid phase neutralization with soda ash, pH value 6.5;
Step 6, dry: the filter cake after neutralization adopts air-flow to be dried, dry rear available chlorine is greater than 60%, and pH value 7.0, obtains Surchlor GR 60 product.
The present invention adopts calcium carbonate to replace soda ash in Surchlor GR 60 production process, conforming product rate is reached respectively more than 98%, unit output also has significantly lifting, the price of calcium carbonate significantly reduces compared with soda ash simultaneously, the adjustment of raw material not only can guarantee that the quality of product and the technological process of production are normal, greatly reduce production cost simultaneously.
Liquid chlorine vaporizing is to utilize the heat that produces in the time of chlorination reaction by the lower the temperature hot water of generation of heat exchange, hot water is entered and is carried in chlorine liquid carburetor by water pump, for liquid chlorine vaporizing, liquid chlorine vaporization heat-absorption water temperature drop is low, and after heat exchange, cold water is used further to chlorination reaction cooling.Relatively existing technique, the application has utilized heat exchange in chlorination reaction cleverly, the heat energy of chlorination reaction is used for to liquid chlorine vaporizing, the cold water producing after liquid chlorine vaporizing is lowered the temperature for chlorination reaction, this technique no longer adopts ice maker that the temperature control cold of chlorination reaction is provided, do not re-use steam heating gasification, not only saved facility investment but also greatly reduce energy expenditure and and production cost.
This technique has guaranteed that by batching and the gasification of liquid chlorine hot water production safety is stable.
The present invention has the following advantages compared with the prior art:
1, technique uniqueness: utilize self production feature to carry out liquid chlorine vaporizing, utilized dexterously chlorination reaction and the two energy replacement of liquid chlorine vaporization reaction, without increase equipment, operational safety, simple, convenient.
2, save facility investment: the price of an ice maker is ten thousand yuan of 8-10, this technique is saved two ice makers, adds installation costs, can reduce approximately 200,000 yuan of investments.
3, energy-conservation: according to the gasification heat absorption of chlorine calculate utilize that this device is per hour can steam saving 104 kilograms, within one day, save 2.5 tons of steam, within 1 year, produced 750 tons of steam of steam saving altogether by 300 days, steam per ton, by 200 yuan of calculating of market price, can be economized on the use of funds approximately 150,000 yuan every year.Economize on electricity 50 per hour is spent, economize on electricity in a day 1200 degree, and 360000 degree that economize on electricity altogether for a year, kilowatt-hour, by 0.5 yuan of calculating of market price, can be economized on the use of funds approximately 180,000 yuan every year.
The embodiment of the present application is just for illustrating the disclosed technical characterictic of the application, and the change that those skilled in the art are undertaken by simple replacement, still belongs to the scope that the application protects.
Claims (2)
1. a production method for Surchlor GR 60, is characterized in that, step is as follows:
Step 1, batching: by cyanuric acid: calcium carbonate: water mixes by weight 1～1.2:0.7～1.0:7～16, add and in batching kettle, stir into slurries;
Step 2, prechlorination reaction: slurries are sent into and carried out prechlorination reaction in prechlorination reactor;
Step 3, chlorination reaction: step 2 is through the reacted slurries of prechlorination, enter again and in differential hydrokineter, carry out chlorination reaction, liquid chlorine is carried out to liquid chlorine vaporizing through chlorine liquid carburetor is chlorine simultaneously, pass into differential hydrokineter bottom, temperature of reaction is 10 ℃～30 ℃, and the prechlorination reactor recycling in step 2 is sent in the chlorine residue producing in chlorination reaction back to;
Step 4, parsing: the material after chlorination reaction adopts whizzer to carry out liquid-solid separation, liquid after separation carries out sedimentation dechlorination, in liquid, add hydrochloric acid, the weight that adds hydrochloric acid is liquid weight 0.1%～0.3%, after decomposing, be cyanuric acid and chlorine, chlorine sends back to the prechlorination reactor in step 2;
Step 5, neutralization: the filter cake obtaining after centrifugal washes with water, after washing, washing water are admitted to batching kettle; Filter cake after washing is carried out to solid phase neutralization with soda ash, pH value 5.8～6.5;
Step 6, dry: the filter cake after neutralization adopts air-flow to be dried, dry rear available chlorine is greater than 60%, and pH value 6.0～7.0, obtains Surchlor GR 60 product.
2. according to the production method of the Surchlor GR 60 described in claim 1, it is characterized in that: the heat that in described step 3, liquid chlorine vaporizing utilization produces in the time of chlorination reaction by heat exchange lower the temperature produce hot water, hot water enters in chlorine liquid carburetor by water pump, for liquid chlorine vaporizing, liquid chlorine vaporization heat-absorption water temperature drop is low, after heat exchange, cold water is used further to chlorination reaction cooling, and entering chlorine liquid carburetor water temp is 30～20 ℃, and going out vaporizer water temperature is 10～20 ℃.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103965126A (en) * | 2013-11-01 | 2014-08-06 | 山东大明消毒科技有限公司 | Preparation method for co-production of trichloroisocyanuric acid and dichloroisocyanurate |
| CN104235605A (en) * | 2014-06-22 | 2014-12-24 | 李安民 | Technique and device for continuous gasification production of overheated chlorine from liquid chlorine |
| CN109134231A (en) * | 2018-10-30 | 2019-01-04 | 杭州众立化工科技有限公司 | A kind of chloroacetic device and process of differential circulation continuous production |
| CN114436982A (en) * | 2022-01-24 | 2022-05-06 | 河北六合化工有限公司 | Method for recovering waste water from sodium dichloroisocyanurate production |
| CN114608370A (en) * | 2022-03-18 | 2022-06-10 | 聊城鲁西聚碳酸酯有限公司 | System and method for reducing consumption by using waste heat in PC production process |
| CN114736167A (en) * | 2022-04-21 | 2022-07-12 | 河北六合化工有限公司 | Continuous production method of sodium dichloroisocyanurate |
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| US3299060A (en) * | 1964-06-17 | 1967-01-17 | Fmc Corp | Method for producing stable salts of dichloroisocyanuric acid |
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| CN102229575A (en) * | 2011-05-05 | 2011-11-02 | 泾县宏发化工有限公司 | Equipment and method for producing sodium dichloroisocyanurate |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103965126A (en) * | 2013-11-01 | 2014-08-06 | 山东大明消毒科技有限公司 | Preparation method for co-production of trichloroisocyanuric acid and dichloroisocyanurate |
| CN104235605A (en) * | 2014-06-22 | 2014-12-24 | 李安民 | Technique and device for continuous gasification production of overheated chlorine from liquid chlorine |
| CN109134231A (en) * | 2018-10-30 | 2019-01-04 | 杭州众立化工科技有限公司 | A kind of chloroacetic device and process of differential circulation continuous production |
| CN109134231B (en) * | 2018-10-30 | 2024-04-02 | 杭州众立化工科技有限公司 | Device and process for continuously producing chloroacetic acid by differential circulation |
| CN114436982A (en) * | 2022-01-24 | 2022-05-06 | 河北六合化工有限公司 | Method for recovering waste water from sodium dichloroisocyanurate production |
| CN114608370A (en) * | 2022-03-18 | 2022-06-10 | 聊城鲁西聚碳酸酯有限公司 | System and method for reducing consumption by using waste heat in PC production process |
| CN114736167A (en) * | 2022-04-21 | 2022-07-12 | 河北六合化工有限公司 | Continuous production method of sodium dichloroisocyanurate |
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| CN103772306B (en) | 2015-10-14 |
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Denomination of invention: Production method of sodium dichloro isocyanurate Effective date of registration: 20200119 Granted publication date: 20151014 Pledgee: Suzhou New Area Financing Guarantee Co.,Ltd. Pledgor: ANHUI ZHONGYUAN CHEMICAL GROUP Co.,Ltd. Registration number: Y2020980000165 |
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Date of cancellation: 20230628 Granted publication date: 20151014 Pledgee: Suzhou New Area Financing Guarantee Co.,Ltd. Pledgor: ANHUI ZHONGYUAN CHEMICAL GROUP Co.,Ltd. Registration number: Y2020980000165 |
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Denomination of invention: A production method of Sodium dichloroisocyanurate Effective date of registration: 20230630 Granted publication date: 20151014 Pledgee: Suzhou New Area Financing Guarantee Co.,Ltd. Pledgor: ANHUI ZHONGYUAN CHEMICAL GROUP Co.,Ltd. Registration number: Y2023980046933 |