CN101293862A - Method for preparing high content monosultap and dimehypo with monosultap anticentripetal mother solution - Google Patents
Method for preparing high content monosultap and dimehypo with monosultap anticentripetal mother solution Download PDFInfo
- Publication number
- CN101293862A CN101293862A CNA2008101225153A CN200810122515A CN101293862A CN 101293862 A CN101293862 A CN 101293862A CN A2008101225153 A CNA2008101225153 A CN A2008101225153A CN 200810122515 A CN200810122515 A CN 200810122515A CN 101293862 A CN101293862 A CN 101293862A
- Authority
- CN
- China
- Prior art keywords
- mother liquor
- monosultap
- desinsection
- desinsection list
- heating
- 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.)
- Granted
Links
Abstract
The invention discloses a method for preparing high content monosultap and bisultap from centrifugal monosultap mother liquor, comprising the steps of: collecting centrifugal monosultap mother liquor during monosultap production process and adjusting the pH value thereof to weak alkality; heating and concentrating under continuous negative pressure, normal pressure or positive pressure to obtain concentrated solution; and separating the concentrated solution, desalting, adjusting pH value to week acidity, crystallizing, performing solid-liquid separation to obtain solid (monosultap) and liquid, and adjusting pH of the liquid to obtain high content bisultap solution. The inventive method reduces production conflicts and reduces the influence on environment during application process; and has the advantages of clean and environmentally friendly production process, convenient storage, transportation and utilization of bisultap, reduced cost, and reduced environmental pollution.
Description
Technical field
The invention belongs to the agricultural chemicals preparation field, be specifically related to the method that a kind of centrifuge mother liquor from desinsection list production process further prepares high-content desinsection list and disosultap.
Background technology
Clam worm poison derivative pesticide is the bionical sterilant of efficient in one, low toxicity, wide spectrum, domestic cartap, desinsection list, thiocyclam, the disosultap four big kinds of mainly containing at present, wherein disosultap is formulated for parting liquid in the production of desinsection list, nearly 100,000 tons of domestic year output, all direct marketings.But there is the deficiency of following several respects in this kind: 1. risk of carriage and cost are big.Simultaneously belong to hazardous chemical again because its effective content of aqua is low, increased risk of carriage and transportation cost.2. the high waste of packing cost is big.Aqua all adopts the polyethylene bottle packing at present, and amount does not reclaim greatly again and increases production cost greatly, and most of enterprises are in the state of breaking even.3. it is big to store pressure.Disosultap is mainly used in the control snout moth's larva of rice, and paddy rice belongs to the kind of seasonal plantation, and the aqua that produce dull season will have to be deposited in the enterprise, not only take fund but also need have big storage capacity to deposit.4. contaminate environment.Be to use pollution on the one hand, a large amount of low effective body aquas use down for a long time and will ecotope be worked the mischief; Production for the desinsection list just might directly be drained when profitless on the other hand.5. restriction development.Be not subjected to seasonal effect because of the desinsection list can synthesize the whole outlets of cartap cartap, aqua that can be a large amount of overstocks the ordinary production that will restrict the desinsection list.
Summary of the invention
The objective of the invention is to solve the problem of above-mentioned existence, provide a kind of desinsection list flour extraction rate to improve and produce the preparation method of high-content disosultap, and whole preparation process is environmental protection, can realize cleaner production, thus in contradiction of alleviate producing and the use to the influence of environment.
The desinsection list by amination → acidifying → dehydration → chlorination → sulfonation → desalination → crystallization → separation, finally obtains desinsection list finished product and centrifuge mother liquor aborning.And at present flour extraction rate of desinsection list synthesis technique is all about 60%, and wherein 40% is centrifuge mother liquor, and desinsection substance amount content is generally 20～25% in the centrifuge mother liquor in 5～40%; Weight sodium chloride content is generally 10～15% in 5～30%; Conventional treatment method is mother liquor pH to be transferred to be made into 18% dimehypo water solution after 6.5～7.5 and sell.And the present invention reaches centrifuge mother liquor can advance the spissated condition of vaporizer and carry out thermal dehydration through modulation, after obtain the desinsection list of secondary crystal except that sodium-chlor, modulation filtrate, decrease temperature crystalline, separation, its flour extraction rate is between 30～40%, and total flour extraction rate can reach about 75%; Gained secondary mother liquid weight content is up to about 35%, far above conventional content, for the disosultap of joining high density provides the foundation.
Purpose of the present invention can reach by following measure:
A kind of desinsection list centrifuge mother liquor prepares the method for high-content desinsection list and disosultap, comprises the steps:
(1) collects the centrifuge mother liquor in the desinsection list production process and its pH value is modulated to weakly alkaline;
(2) centrifuge mother liquor after will modulating concentrates by continuous negative pressure, normal pressure or malleation heating in vaporizer, obtains concentrated solution;
(3) concentrated solution is separated desalination, filtrate pH value is transferred to slightly acidic, crystallization and solid-liquid separation, wherein solid is the desinsection list, liquid is high-load desinsection biliquid.
The purpose of modulation centrifuge mother liquor pH is the solution that mother liquor is a slant acidity, the effective body of heating evaporation easily decomposes also high to the requirement of equipment simultaneously under the acidic conditions, at this situation mother liquor PH is transferred to 6.8～7.2, the general alkali of using, especially sodium hydroxide is regulated, and also available hydrogen aqueous solution of sodium oxide (be as mass concentration 25～35% aqueous sodium hydroxide solution) is regulated.
The centrifuge mother liquor that modulates concentrates the easy volatile can remove in the centrifuge mother liquor or the easy azeotropic impurity and the portion water of removing through heating, and obtains concentrated solution.Heating concentrates and can carry out at negative pressure, normal pressure or direct draught continuously, and the solution that modulates is too high as temperature in heat-processed, its effective body of overlong time also easily decomposes and coking, so the solution Heating temperature is unsuitable too high, the time should not be long.Select film-type evaporator for use, as the Thin Stainless Steel film evaporator, continuously feeding under the condition of high negative pressure simultaneously, discharging can solve decomposes coking problem.Simultaneously the charging of vaporizer is controlled, fed the process that vaporizer can be stablized whole technology with fixed flow rate by under meter.Processing condition can be: system pressure-0.098～-0.01MPa, vaporizer upper, middle and lower even heating, vapor pressure are 0.1～0.5Mpa, temperature is 50～100 ℃; Preferred technology is: system pressure-0.098～-0.08MPa, vapor pressure 0.2～0.35Mpa; Temperature 68～72C °.Centrifuge mother liquor is 40～50% through the weight content that heating is concentrated into active substance in the concentrated solution, and proportion is 1.3～1.4; Be preferably, weight content is 42～45%; Proportion is 1.36～1.37.
The water of condensation that contains impurity that evaporative condenser obtained when heating concentrated gets final product qualified discharge by the biochemical treatment of water treatment department.
Sodium chloride content also rises because the effective body burden of its solution of water evaporates rises simultaneously thereupon, and has solid sodium chloride to separate out must to separate, and considers that effective body also separates out because of separating as early as possible at a certain temperature.Preferred processing condition is: concentrated solution separates at 50～80 ℃ (preferred 55～65 ℃).The salt slag that obtains behind the desalination can be handled by the department that useless admittedly processing qualification is arranged, or as other product synthetic raw materials.
Sulfonated liquid behind the separation desalination with acid modulation pH value to 5.1～5.8, especially about 5.5 makes it become only sodium salt of desinsection again, and used acid can be selected hydrogenchloride or hydrochloride aqueous solution for use, the hydrochloride aqueous solution as 25～35% etc.
With carrying out decrease temperature crystalline after the acid modulation, temperature is-8～-5 ℃ during crystallization, and crystallization time is 18～28 hours, is preferably 22～24 hours.
With the solution solid-liquid separation after the crystallization, be desinsection list finished product behind the solid drying, its weight content is 75～96% (being preferably 90～96%), and the liquid after the separation is transferred to pH can obtain the high-load desinsection biliquid that weight content is 30～40% (being preferably 34～37%) after 6.5～7.5.
The invention provides a kind of preparation method who improves desinsection list flour extraction rate and produce the high-content disosultap, and whole preparation process is environmental protection, can realizes cleaner production, thereby alleviate in the contradiction of producing and the use influence environment.The present invention is increased to the flour extraction rate in the desinsection list synthesis technique about 75% from about 60%, and centrifuge mother liquor successfully is mixed with the desinsection biliquid of high density, big convenience the storage of disosultap, transportation and utilization, both provided cost savings, reduced environmental pollution again.
Embodiment
Embodiment 1
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 30% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.0m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.09MPa, vapor pressure 0.22Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.5 of sulfonated liquid with 30% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 23 hours, obtain the 345Kg weight content after the oven dry of isolated solid and be 95.2% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 30% that to obtain the 2070Kg weight content after 7 be 35.5% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 31.9% (i.e. the mass percent of active substance in solid quantity of goods produced of Huo Deing and the original solution), and rate of loss is 1.7%.
Embodiment 2
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 25% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.0m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.08MPa, vapor pressure 0.22Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.4 of sulfonated liquid with 25% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 24 hours, obtain the 350Kg weight content after the oven dry of isolated solid and be 95.4% desinsection list, the liquid after the separation is transferred to 7 with the aqueous sodium hydroxide solution of mass concentration 35% with pH, and to obtain the 2080Kg weight content be 35.3% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 32.3%, and rate of loss is 1.3%.
Embodiment 3
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 35% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.2m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.092MPa, vapor pressure 0.24Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.6 of sulfonated liquid with 35% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 22 hours, obtain the 385Kg weight content after the oven dry of isolated solid and be 95.2% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 35% that to obtain the 2288Kg weight content after 6.9 be 35.2% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 32.3%, and rate of loss is 1.5%.
Embodiment 4
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 29% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.2m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.091MPa, vapor pressure 0.24Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.7 of sulfonated liquid with 29% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 20 hours, obtain the 380Kg weight content after the oven dry of isolated solid and be 95.5% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 29% that to obtain the 2262Kg weight content after 7.1 be 35.7% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 31.9%, and rate of loss is 1.6%.
Embodiment 5
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 25～35% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.5m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.092MPa, vapor pressure 0.25Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.5 of sulfonated liquid with 35% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 22～24 hours, obtain the 475Kg weight content after the oven dry of isolated solid and be 95.3% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 35% that to obtain the 2429Kg weight content after 6.9 be 36.2% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 35.1%, and rate of loss is 1.5%.
Embodiment 6
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 30% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.5m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.092MPa, vapor pressure 0.25Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.5 of sulfonated liquid with 35% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 22～24 hours, obtain the 472Kg weight content after the oven dry of isolated solid and be 95.4% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 35% that to obtain the 2445Kg weight content after 7.1 be 36.1% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 34.9%, and rate of loss is 1.4%.
Embodiment 7
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 35% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.8m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.091MPa, vapor pressure 0.30Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.58 of sulfonated liquid with 35% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 22～24 hours, obtain the 485Kg weight content after the oven dry of isolated solid and be 95.3% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 35% that to obtain the 2855Kg weight content after 6.9 be 35.9% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 32.0%, and rate of loss is 1.8%.
Embodiment 8
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 35% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 2.8m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.089MPa, vapor pressure 0.30Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.6 of sulfonated liquid with 35% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 22～24 hours, obtain the 480Kg weight content after the oven dry of isolated solid and be 95.0% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 35% that to obtain the 2876Kg weight content after 7.2 be 35.8% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 31.7%, and rate of loss is 1.9%.
Embodiment 9
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 35% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 3.0m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.089MPa, vapor pressure 0.35Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.5 of sulfonated liquid with 35% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 22～24 hours, obtain the 485Kg weight content after the oven dry of isolated solid and be 94.8% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 35% that to obtain the 3128Kg weight content after 6.9 be 36.1% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 29.9%, and rate of loss is 2.1%.
Embodiment 10
Collect the centrifuge mother liquor in the desinsection list production process, wherein the mass content of desinsection list is 22.35%, and proportion is 1.21.Be positioned over 30M after with the aqueous sodium hydroxide solution of mass concentration 35% mother liquor PH being transferred to 6.8～7.2
3Jar in, through spinner-type flowmeter by fixed flow rate 3.0m
3/ hr joins 16m
2In the Thin Stainless Steel film evaporator, start simultaneously and stir and vacuum system, open steam and carry out heating evaporation 2hr, pressure-0.094MPa, vapor pressure 0.35Mpa; Temperature 68～72C °.The top evaporation condensate advances the waste water station biochemical treatment, the bottom concentrated solution carries out the filtering separation desalination under 55～65 ℃ after collecting, separate the back and regulate the pH value to 5.5 of sulfonated liquid with 35% hydrochloride aqueous solution,-8～-5 ℃ of following crystallizations 22～24 hours, obtain the 482Kg weight content after the oven dry of isolated solid and be 94.9% desinsection list, the liquid after the separation is transferred to pH with the aqueous sodium hydroxide solution of mass concentration 35% that to obtain the 3113Kg weight content after 7 be 36.3% high-load desinsection biliquid.Solid quantity of goods produced flour extraction rate is 29.7%, and rate of loss is 2.2%.
Claims (12)
1, a kind of desinsection list centrifuge mother liquor prepares the method for high-content desinsection list and disosultap, it is characterized in that comprising the steps:
(1) collects the centrifuge mother liquor in the desinsection list production process and its pH value transferred to weakly alkaline;
(2) centrifuge mother liquor after will modulating concentrates by continuous negative pressure, normal pressure or malleation heating in vaporizer, obtains concentrated solution;
(3) concentrated solution is separated desalination, filtrate pH value is transferred to slightly acidic, crystallization and solid-liquid separation, wherein solid is the desinsection list, obtains high-load desinsection biliquid behind the liquid adjust pH.
2, method according to claim 1 is characterized in that in the described centrifuge mother liquor that the mass content of desinsection list is 5～40%, and the weight content of sodium-chlor is 5～30%.
3, method according to claim 1 is characterized in that centrifuge mother liquor regulates pH value to 6.8～7.2 with sodium hydroxide.
4, method according to claim 1 is characterized in that described vaporizer is a film-type evaporator.
5, method according to claim 1 is characterized in that heating when concentrating, and system pressure is-0.098～-0.01MPa.
6, method according to claim 5 is characterized in that heating when concentrating, and system pressure is-0.098～-0.08MPa.
7, method according to claim 1 is characterized in that heating when concentrating, and vapor pressure is 0.1～0.5MPa; Temperature is 50～100 ℃.
8, method according to claim 7 is characterized in that heating when concentrating, and vapor pressure is 0.2～0.35MPa; Temperature is 68～72 ℃.
9, method according to claim 1, the temperature when it is characterized in that separating desalination are 50～80 ℃.
10, method according to claim 1 is characterized in that regulating pH value to 5.1～5.8 with hydrogenchloride after concentrated solution separates desalination.
11, method according to claim 1, the temperature when it is characterized in that crystallization are-8～-5 ℃, and crystallization time is 18～28 hours.
12, method according to claim 1, the weight content that it is characterized in that described desinsection list is 75～96%, the weight content of disosultap is 30～40% in the described desinsection biliquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008101225153A CN101293862B (en) | 2008-06-23 | 2008-06-23 | Method for preparing high content monosultap and dimehypo with monosultap anticentripetal mother solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008101225153A CN101293862B (en) | 2008-06-23 | 2008-06-23 | Method for preparing high content monosultap and dimehypo with monosultap anticentripetal mother solution |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101293862A true CN101293862A (en) | 2008-10-29 |
| CN101293862B CN101293862B (en) | 2010-12-15 |
Family
ID=40064437
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008101225153A Expired - Fee Related CN101293862B (en) | 2008-06-23 | 2008-06-23 | Method for preparing high content monosultap and dimehypo with monosultap anticentripetal mother solution |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101293862B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104447458A (en) * | 2014-12-11 | 2015-03-25 | 湖南国发精细化工科技有限公司 | Method for refining monosultap in monosultap synthetic process |
| CN105503680A (en) * | 2015-12-29 | 2016-04-20 | 江苏天容集团股份有限公司 | Method for improving flour extraction rate of monosultap centrifugal mother liquor |
| CN106518744A (en) * | 2016-08-31 | 2017-03-22 | 江苏天容集团股份有限公司 | Method for crystallizing centrifugal mother liquor of Monosultap |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1278403A (en) * | 2000-07-10 | 2001-01-03 | 溧阳市化工厂 | High-efficiency preparation of high-purity bisultap powder |
-
2008
- 2008-06-23 CN CN2008101225153A patent/CN101293862B/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104447458A (en) * | 2014-12-11 | 2015-03-25 | 湖南国发精细化工科技有限公司 | Method for refining monosultap in monosultap synthetic process |
| CN105503680A (en) * | 2015-12-29 | 2016-04-20 | 江苏天容集团股份有限公司 | Method for improving flour extraction rate of monosultap centrifugal mother liquor |
| CN105503680B (en) * | 2015-12-29 | 2017-09-19 | 江苏天容集团股份有限公司 | The method for improving Cupric sulfate centrifuge mother liquor flour extraction |
| CN106518744A (en) * | 2016-08-31 | 2017-03-22 | 江苏天容集团股份有限公司 | Method for crystallizing centrifugal mother liquor of Monosultap |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101293862B (en) | 2010-12-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101665523B (en) | The production method of L-arabinose and D-xylose pref | |
| US7781194B2 (en) | Method for using biomass in biogas process | |
| CN101966997B (en) | Process and device for producing pyrotechnite from sodium sulfate decahydrate | |
| CN104473120B (en) | A kind of production technology of monosodium glutamate | |
| CN101407350A (en) | Method for processing ion exchange waste liquor of lysine production by fermentation method | |
| CN109319998A (en) | A kind of the near-zero release processing system and technique of ternary precursor material production waste water | |
| CN101659681A (en) | Method for producing wood sugar product | |
| AU2009306177A1 (en) | Process for the production of alcohol | |
| CN102010882A (en) | Method for performing lignocelluloses raw material high-temperature diluted acid pretreatment by using extremely small amount of water | |
| CN101293862B (en) | Method for preparing high content monosultap and dimehypo with monosultap anticentripetal mother solution | |
| CN109336271B (en) | Decompression-assisted biogas slurry ammonia nitrogen membrane recovery system and method | |
| US20120009641A1 (en) | Method for producing clarified juice, packagible juice, ethanol and sugar from sugarcane and system thereof | |
| JPS6043117B2 (en) | Method for producing volatile organic compounds, especially ethanol, by continuous fermentation | |
| CN101538179B (en) | Method for preparing compound amino acid organic liquid fertilizer | |
| CN101665524B (en) | Method for producing L-arabinose | |
| CN207362101U (en) | A kind of crude naphthalene fine-processing production line | |
| JPH01502155A (en) | Method for producing ethanol by molasses fermentation | |
| CN103468753A (en) | Water saving method in process of producing sodium gluconate through aspergillus niger fermentation | |
| JP2008545403A (en) | Method and apparatus for preparing an ethanol / water mixture | |
| CN101792447A (en) | Process and device for preparing urotropine by using gas phase method | |
| CN206666494U (en) | A kind of Steam Recovery cyclic utilization system in liquor production | |
| CN207405109U (en) | A kind of water-reducing agent production system | |
| CN205420242U (en) | Furfural cleaner production assembly line | |
| CN201952420U (en) | Sugar extracting system of grain emulsion | |
| CN101691383A (en) | Method for processing PMIDA synthesis mother liquor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP02 | Change in the address of a patent holder |
Address after: The 224631 Yancheng City Xiangshui eco chemical industry zone of Jiangsu Province Port Road No. 1 Patentee after: JIANGSU TIANRONG GROUP Co.,Ltd. Patentee after: JIANGSU ZHONGYI CHEMICALS Co.,Ltd. Patentee after: Jiangsu Ruihe Chemistry Co.,Ltd. Address before: 213300 No. 147 Ling Ling Dong Road, Jiangsu, Liyang Patentee before: JIANGSU TIANRONG GROUP Co.,Ltd. Patentee before: JIANGSU ZHONGYI CHEMICALS Co.,Ltd. Patentee before: Jiangsu Ruihe Chemistry Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20190117 Address after: No.1 Shugang Road, Xiangshui Eco-chemical Zone, Yancheng City, Jiangsu Province Patentee after: JIANGSU TIANRONG GROUP Co.,Ltd. Address before: No.1 Shugang Road, Xiangshui Eco-chemical Zone, Yancheng City, Jiangsu Province Co-patentee before: JIANGSU ZHONGYI CHEMICALS Co.,Ltd. Patentee before: JIANGSU TIANRONG GROUP Co.,Ltd. Co-patentee before: Jiangsu Ruihe Chemistry Co.,Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20101215 |