CN1172800A - Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid - Google Patents
Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid Download PDFInfo
- Publication number
- CN1172800A CN1172800A CN 97106970 CN97106970A CN1172800A CN 1172800 A CN1172800 A CN 1172800A CN 97106970 CN97106970 CN 97106970 CN 97106970 A CN97106970 A CN 97106970A CN 1172800 A CN1172800 A CN 1172800A
- Authority
- CN
- China
- Prior art keywords
- smas
- chlorine
- methacrylic
- centrifugal
- reaction
- 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
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A mother liquid circulation process for preparing sodium methylacrylsulfornate (SMAS) uses methylacrylchlorine and absolute sodium sulfite as raw materials and includes such steps as reactio, early dewatering, adsorption by activated carbon, filter, evaporation, hot filter to remove salt, crystalline, centrifugal separation, washing, refining, mother liquid circulation and drying. Its advantages is high finished product output rate up to 91.6%.
Description
The present invention relates to the organic chemistry acyclic compound, be meant that especially a kind of is producing and manufacturing technique and the equipment thereof that raw material adopts Recycling Mother Solution legal system methylpropene sodium sulfonate with methacrylic chlorine and sodium sulphite anhydrous 99.3.
Methylpropene sodium sulfonate (hereinafter to be referred as SMAS) improves the dyeing behavior of acrylic fibers mainly as the 3rd monomer of making acrylic fibers, has advantages such as Heat stability is good, dyeability are good.At present, domestic still do not have other manufacturer production.Mainly adopt solvent extration and produce SMAS abroad, this processing method needs evaporating water, and needs elevated temperature heat to filter, operational difficulty, equipment requirements height, also need consume the higher organic solvent of a large amount of value, the finished product yield is lower, thereby has limited the further popularization of this technology.
Purpose of the present invention just is to overcome existing SMAS production technique defective, provides a kind of by methacrylic chlorine is dropped in the sodium sulfite solution continuously, adopts the new production technique of Recycling Mother Solution legal system SMAS.
SMAS production technique of the present invention is a raw material with methacrylic chlorine and sodium sulphite anhydrous 99.3, adopts Recycling Mother Solution legal system SMAS;＜1〉by glassed steel reaction vessels methacrylic chlorine is dropped to continuously and make thick SMAS in the sodium sulfite solution, and dealkylation reaction water in early stage, reaction solution removes the impurity iron ion through charcoal absorption then;＜2〉remove portion water in the reaction solution through dehydration by evaporation, remove most of solid sodium chloride that dehydration by evaporation is separated out through heat filtering again, by cool, crystallization separates out the SMAS major part;＜3〉this subsequently solidliquid mixture enters whizzer, Recycling Mother Solution after centrifugal is returned the absorption still and is carried out charcoal absorption, again repeating step＜2 〉,＜3, and crystallization kettle is returned in washings circulation for the first time in the centrifugal process, carry out crystallization and centrifugal again, to improve the finished product yield;＜4〉send into drying machine through the solid materials that washs after centrifugal, SMAS gets product after the drying.The main chemical reactions formula of technology of the present invention is as follows:
SMAS production technique of the present invention is divided into four processes:＜1〉reaction, dealkylation reaction early stage water, charcoal absorption and filtration procedure;＜2〉dehydration by evaporation, heat filtering desalination and crystallisation process;＜3〉centrifugation, the refining and Recycling Mother Solution process of product washing;＜4〉wet product drying process.In process of production, the centrifuge mother liquor circulation is returned the absorption still and is carried out charcoal absorption and filtration again, and then makes with extra care and the Recycling Mother Solution process through dehydration by evaporation, heat filtering desalination and crystallisation process and centrifugation, product washing; Centrifuge mother liquor after repeatedly circulating also is used for washing the salt slag that heat filtering leaches; And in the centrifugal process for the first time washings also circulate and return crystallization kettle, carry out crystallization and centrifugal again, the SMAS that is taken out of with abundant recovery centrifuge mother liquor, salt slag and centrifuge washing liquid.The main control parameters of this production process is as follows: sequence number controlled variable title index
1 raw material specification methacrylic cl content 〉=97.0% (wt%)
Sodium sulphite anhydrous 99.3 content 〉=96.0% (wt%)
2 proportioning methacrylic chlorine: sodium sulphite anhydrous 99.3 0.7-1.5: 1 (mol)
3 methacrylic chlorine drip time 0.5-5hr
4 temperature of reaction 20-100 ℃
Pressure-0.10-0.30MPa
Time 0.5-5hr
Take off 20-150 ℃ of water temp in early stage after 5 reactions
Pressure-0.10-0.30MPa
20-100 ℃ of 6 absorption still temperature
Pressure-0.10-0.30MPa
7 evaporator temperature 20-130 ℃
Pressure-0.10-0.30MPa
30-165 ℃ of 8 heat filter temperature
Pressure-0.10-0.30MPa
0-100 ℃ of 9 crystallization kettle temperature
Pressure-0.10-0.30MPa
50-150 ℃ of 10 drying machine temperature
Pressure-0.10-0.30MPa
The finished product SMAS yield that makes through technology of the present invention reaches 91.6% (to the mole yield of methacrylic chlorine), and the quality index of SMAS finished product is as follows:
Sequence number index name index
1 appearance white plate crystal
2 purity (wt%) 〉=99.00%
3 sodium chloride contents (wt%)≤0.10%
4 sodium sulphate contents (wt%)≤0.10%
5 S-WAT content (wt%)≤0.05%
6 iron level ppm≤0.4ppm
7 water-insoluble ppm≤50ppm
8 water capacities (wt%)≤0.50%
Advantage of the present invention just is to make the finished product yield reach 91.6% owing to adopted the Recycling Mother Solution method, has improved the finished product yield of product greatly.This technology is compared with solvent extration technology, does not need evaporating water and elevated temperature heat to filter, and technological operation is simple relatively, and this processing unit require low, do not consume organic solvent.Therefore this production technique has fabulous promotional value.
The invention will be further described below in conjunction with accompanying drawing; Fig. 1 is a process flow diagram of the present invention, and Fig. 2 is a technology evaporation structure synoptic diagram of the present invention.
With reference to Fig. 1, the technological process of production of the present invention is by sodium sulfite dissolution kettle [1], metering system chlorine storage tank [2], metering system chlorine head tank [3], reactor [4], dump tank [5], absorption still [6], cold filter [7], filtrate tank [8], evaporimeter [9], measuring tank [10], heat filter [11], crystallization kettle [12], centrifuge [13], wash water head tank [14a, b, c, d], the equipment such as mother liquor tank [15], drying machine [16] consist of, R represents to adsorb still [6], N represent to decrystallize still [12], K and represents wash water head tank [14a among the figure, b, c], P represents finished product SMAS.
When producing, the raw material sodium sulfite is delivered in the reactor [4] by delivery pump after sodium sulfite dissolution kettle [1] is with the pure water dissolving, raw material metering system chlorine is delivered to metering system chlorine head tank [3] by metering system chlorine storage tank [2] through delivery pump, when reaction, opening reactor [4] stirs, drip metering system chlorine 0.5-5hr by metering system chlorine head tank [3] to reactor [4], then stop to drip stirring reaction 0.5-5hr, reaction temperature is controlled at 20-100 ℃, and pressure is controlled to be-0.10-0.30MPa. React complete after, temperature be 20-150 ℃, pressure for deviate under-the 0.10-0.30MPa a certain amount of early stage water and the impurity such as unreacted metering system chlorine enter dump tank [5], send the boiler burning disposal. Reactant liquor autoreaction still [4] enters in the absorption still [6], and the unformed sawdust active carbon that adds 0.5-2% (wt%) load responsive fluid stirs, the control temperature is 20-100 ℃, pressure is-0.10-0.30MPa, then this solution with solid activated carbon is sent in the cold filter [7] and filtered, filtrate flows in the filtrate tank [8], the cake solids active carbon is done burning and is processed, filtrate is delivered in the evaporimeter [9] through delivery pump from filtrate tank [8], the control temperature is 20-130 ℃ in evaporimeter [9], pressure is-0.10-0.30MPa, through dehydration by evaporation, steaming the water yield is measured by measuring tank [10], the water yield varies with temperature the calculating gained by SMAS at the dissolved in filtrate degree, so that SMAS reaches the critical saturation state of this temperature in evaporimeter [9], to separate out most of accessory substance solid sodium chloride in the solution this moment, liquid-solid mixture behind this dehydration by evaporation is sent in the heat filter [11], the control temperature is 30-165 ℃, pressure is-0.10-0. 30MPa, carry out heat filtering, the solid salt slag that leaches is after the washing of the centrifuge mother liquor after the Recycling Mother Solution repeatedly, send boiler to process, filtrate is sent in the crystallization kettle [12], the control temperature is 0-100 ℃ in crystallization kettle [12], pressure is-0.10-0.30MPa, carry out crystallisation by cooling, separate out a large amount of solid SMAS, then this solidliquid mixture is entered in the centrifuge [13] and carry out centrifugation, centrifugal rear mother liquid obtained sending in the mother liquor tank [15], deliver to circulation production in the absorption still [6] by delivery pump again, to reclaim SMAS wherein, solid-phase product in the centrifuge [13] is removed impurity by-product solid sodium chloride in the product through wash water head tank [14] washing, the washing order is: centrifugal with carrying out spray washing in the adding centrifuge of the washing lotion in a groove [13] first, gained centrifugate through mother liquor tank [15] by being pumped in the crystallization kettle [12], with the filtrate crystallisation by cooling behind the heat filtering next time. Add with the washing lotion in the b groove that to carry out spray washing in the centrifuge [13] centrifugal, gained centrifugate is sent into a groove through mother liquor tank [15] by delivery pump, uses in order to next centrifuge washing again. Equally, it is centrifugal to carry out spray washing with the washing lotion in the c groove, and the centrifugate of gained is delivered to the b groove through mother liquor tank [15] by delivery pump, and the centrifugate after centrifugal with the washing of the pure water in the d groove is delivered to the c groove through mother liquor tank [15] by delivery pump, supplies pure water at last in the d groove. Solid purified product in the centrifuge [13] after four washings is sent in the drying machine [16] and is carried out drying, and to be 50-150 ℃, pressure be-0.10-0 .30MPa to the control temperature. Namely make finished product SMAS after the drying.
With reference to Fig. 2, evaporimeter is composite construction, and top is vaporizer, liner enamel material; The bottom is tubular heat exchanger, and wherein tubulation adopts titanium material (titanium pipe), is a center circulation pipe in section of tubulation group center, and the specification ratio of center circulation pipe and tubulation diameter is 3-6: 1. Material is heated in tubulation, reaches the vaporization purpose on evaporimeter top. Such as figure, W is that material inlet, M are that to be respectively steam import and export, T1 and T2 be that temperature-measuring port, F1 and F2 are that visor mouth, e are that pressure tap, b, c and d are that for subsequent use mouthful, a is steam outlet for material outlet, S1 and S2.
Below be embodiments of the invention, practical application of the present invention is not limited to embodiment.
Example 1 is that raw material adopts Recycling Mother Solution legal system SMAS with S-WAT and methacrylic chlorine.
300 tons/year of throughput
Raw material S-WAT content 〉=96.0% (wt)
Raw material methacrylic cl content 〉=97.0% (wt)
Main equipment specification:
1. 3000 liters of bands of S-WAT dissolution kettle K3000L volume stir glass-lined equipment
2. 5000 liters of glass-lined equipments of methacrylic chlorine storage tank TT-K5000L volume
3. 500 liters of glass-lined equipments of methacrylic chlorine header tank TT-K500L volume
4. 3000 liters of bands of reactor K3000L volume stir glass-lined equipment
5. receiver φ 600 * 1000 * 6 materials are carbon steel
6. 3000 liters of bands of absorption still K3000L volume stir pool glass equipment
7. on the cold strainer φ 1300 * 1000 not with the glass-lined equipment of end socket
8. 3000 liters of glass-lined equipments of filtrate tank TT-K3000L volume
9. scale tank φ 700 * 3000 materials are 1Cr18Ni9Ti
10. heat filter φ 1200 * 8 materials are lining titanium, (composite titanium)
11. vaporizer φ 1600 * 2400+ φ 1000 * 2000 materials (compound)
12. 5000 liters of bands of crystallization kettle K5000L volume stir glass-lined equipment
13. 4 of 500 liters of glass-lined equipments of wash water header tank TT-K500L volume
14. whizzer WG-1200
15. 3000 liters of glass-lined equipments of mother liquor tank TT-K3000L volume
16. drying machine GZQ3 * 4.5
Take by weighing the 380Kg S-WAT, join in the S-WAT dissolution kettle, add the 1503Kg pure water simultaneously, after the stirring and dissolving, deliver in the reactor with transferpump.322 liters of methacrylic chlorine of metering are delivered in the methacrylic chlorine header tank with transferpump in the methacrylic chlorine storage tank, open reactor and stir, and begin to drip methacrylic chlorine, and controlled temperature is 50-80 ℃, and pressure is 0-0.10MPa, and the dropping time is 1-3hr.After reaction finishes, be 50-80 ℃ in temperature, pressure is for beginning to take off water and impurity such as unreacted methacrylic chlorine in early stage under the-0.01-0.1MPa, and the about 156Kg of gained waste liquid enters receiver; The about 2025Kg of gained reaction solution enters the absorption still, add gac 15Kg, add pure water 33Kg simultaneously, controlled temperature is 50-80 ℃, pressure is that 0-0.10MPa stirs down, then this solidliquid mixture is put into cold strainer and filter, the 2054Kg filtrate of gained enters filtrate tank, and filtrate is sent in the vaporizer through transferpump, controlled temperature is 70-100 ℃ in vaporizer, pressure is-0.05-0.1MPa to evaporate the water yield and measured by scale tank, altogether the about 703Kg of dehydration, after arriving the dehydration terminal point, stop dehydration, last about 1351Kg liquid-solid mixture is sent in the heat filter, control heat filter temperature is 50-80 ℃, pressure is 0-0.30MPa, through heat filtering, can get about 85Kg salt slag, these salt slags must send boiler to handle after the centrifuge mother liquor washing through gained after the Recycling Mother Solution repeatedly.The about 1266Kg filtrate of gained enters crystallization kettle from heat filter, at this controlled temperature is 30-60 ℃, pressure is 0-0.10MPa, crystallisation by cooling, SMAS is separated out, then this liquid-solid mixture is entered in the whizzer, mother liquid obtained entering in the mother liquor tank after the centrifugation, send back in the absorption still with transferpump again, adsorb cold filtration, dehydration by evaporation, wherein product is reclaimed in the centrifugal circulation of heat filtering and crystallization, and two to three later centrifuge mother liquors like this remove to wash the salt slag that leaches again from heat filtering, and the washing lotion of gained loops back the absorption still again.The thick product of solid materials in whizzer washs through the wash water header tank, the washing order is: join in the whizzer with the about 40Kg spray of the washing lotion in a groove earlier, it is centrifugal to enter washing, the centrifugate of gained through mother liquor tank by the filtrate crystallization in the lump after being pumped to crystallization kettle and heat filtering next time, add in the whizzer with the about 40Kg spray of the washing lotion in the b groove again, wash centrifugal, gained centrifugate through mother liquor tank by being pumped into a groove, to make washing washing lotion next time.Equally, spray in the whizzer with the about 40Kg of washing lotion in the C groove, behind the centrifuge washing, gained centrifugate by being pumped to the b groove, is used washing lotion to do to wash next time through mother liquor tank.Spray in the whizzer with about 20Kg pure water in the d groove, gained centrifugate by being pumped to the C groove, to make washing washing lotion next time, at last, in the d of sky groove, is supplied about 20Kg pure water through mother liquor tank behind centrifuge washing, to make washing washing lotion next time.Thick product in the whizzer through four washings of washing lotion after, send into again that drying promptly makes finished product SMAS in the drying machine.
Technology of the present invention can adapt to production requirement, the SMAS steady quality of producing, and the 3rd monomer that is used as the acrylic fiber production process process conforms to quality requirements, and the user is satisfied.
Example 2, various processes method correlation data
Explained hereafter SMAS of the present invention adopts the Recycling Mother Solution method, adopts same raw material system SMAS in the laboratory, but the refining solvent extration that adopts in back, though two kinds of methods, raw material are the same, reacting phase is with, but gained difference as a result, and following table has been listed both testing datas relatively under laboratory condition.
(wherein DMF is a dimethyl formamide)
| Project | Method | |
| Solvent extration | The Recycling Mother Solution method | |
| Sodium sulphite anhydrous 99.3 mol | ????0.948 | ????0.5 |
| Methacrylic chlorine mol | ????1.2 | ????0.544 |
| The circulation mother liquor | ||
| Weight g | ????/ | ????350 |
| ??SMAS????????????????％ | ????/ | ????18.98 |
| ??NaCl????????????????％ | ????/ | ????13.1 |
| ??H2O?????????????????ml | ????260 | ????260 |
| Emulsifying agent g | ????2 | |
| Steam water yield ml | Evaporate to dryness | ????253 |
| Separate out the salt slag | ||
| Weight g | ????/ | ????26.8 |
| ??SMAS????????????????％ | ????/ | ????8.019 |
| ??NaCl????????????????％ | ????/ | ????92.04 |
| Mother liquor | ||
| Weight g | ????/ | ????321.4 |
| ??SMAS????????????????％ | ????/ | ????18.44 |
| ??NaCl????????????????％ | ????/ | ????13.91 |
| Mother liquor is condensed into amount of solid g | ????124 | ????/ |
| The DMF consumption | ||
| Ml for the first time | ????500 | ????/ |
| Ml for the second time | ????70 | ????/ |
| SMAS is separated out in crystallization | ||
| Weight g | ????52.7 | ????73.7 |
| ??SMAS????????????????％ | ????96.32 | ????97.7 |
| ??NaCl????????????????％ | ????2.66 | ????1.576 |
| Extraction gained SMAS | ||
| Weight g | ????64 | ????/ |
| ??SMAS????????????????％ | ????95.93 | ????/ |
| ??NaCl????????????????％ | ????0.5354 | ????/ |
| SMAS total yield % | ????74 | ????91.46 |
Claims (5)
1, a kind of methylpropene sodium sulfonate (SMAS) production technique is a raw material with methacrylic chlorine and sodium sulphite anhydrous 99.3, it is characterized in that it adopts Recycling Mother Solution legal system SMAS;
＜1〉by glassed steel reaction vessels methacrylic chlorine is dropped to continuously and make thick SMAS in the sodium sulfite solution, and dealkylation reaction water in early stage, reaction solution removes the impurity iron ion through charcoal absorption then;
＜2〉remove portion water in the reaction solution through dehydration by evaporation, remove most of solid sodium chloride that dehydration by evaporation is separated out through heat filtering again, by cool, crystallization separates out the SMAS major part;
＜3〉this subsequently solidliquid mixture enters whizzer, and the Recycling Mother Solution after centrifugal is returned the absorption still and carried out charcoal absorption, again repeating step＜2 〉,＜3; And crystallization kettle is returned in washings circulation for the first time in the centrifugal process, carries out crystallization and centrifugal again;
＜4〉send into drying machine through the solid materials that washs after centrifugal, SMAS gets product after the drying.
2, SMAS production technique according to claim 1, the proportioning that it is characterized in that methacrylic chlorine and S-WAT is 0.7-1.5: 1 (mol), the dropping time is 0.5-5hr to methacrylic chlorine continuously, temperature of reaction 20-100 ℃, pressure-0.10-0.30MPa, reaction times 0.5-5hr, 20-130 ℃ of vaporizer controlled temperature, pressure-0.10-0.30MPa.
3, SMAS production technique according to claim 1 is characterized in that the centrifuge mother liquor after repeatedly circulating also is used for washing the salt slag that the heat of compression leaches.
4, the employed vaporizer of a kind of production technique of SMAS according to claim 1 is characterized in that it is a composite structure, and top is vaporizing chamber, liner lass lining material, the bottom is a tubular heat exchange, and wherein tubulation adopts the titanium material, is a center circulation tube in portion of tubulation group center.
5, the employed vaporizer of SMAS production technique according to claim 4, the ratio that it is characterized in that center circulation tube and tubulation diameter is 3-6: 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106970A CN1045432C (en) | 1997-05-22 | 1997-05-22 | Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN97106970A CN1045432C (en) | 1997-05-22 | 1997-05-22 | Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1172800A true CN1172800A (en) | 1998-02-11 |
| CN1045432C CN1045432C (en) | 1999-10-06 |
Family
ID=5169168
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97106970A Expired - Fee Related CN1045432C (en) | 1997-05-22 | 1997-05-22 | Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1045432C (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101492399B (en) * | 2009-03-04 | 2012-06-27 | 太仓市新毛涤纶化工有限公司 | Method for preparing methylpropene sodium sulfonate |
| CN103204785A (en) * | 2012-01-13 | 2013-07-17 | 湖北和昌新材料科技有限公司 | Dehydration method of sodium allylsulfonate |
| US8820895B2 (en) | 2009-07-10 | 2014-09-02 | Fujifilm Dimatix, Inc. | MEMS jetting structure for dense packing |
| CN112625481A (en) * | 2020-12-16 | 2021-04-09 | 江苏德莱利建筑装饰工程有限公司 | Epoxy floor coating with formaldehyde absorption performance and preparation method thereof |
| CN112851555A (en) * | 2021-01-18 | 2021-05-28 | 浙江皇马科技股份有限公司 | Synthesis and refining method of sodium methallyl sulfonate |
| CN115403490A (en) * | 2022-08-16 | 2022-11-29 | 浙江皇马科技股份有限公司 | Refining method of sodium methallyl sulfonate |
| CN116143668A (en) * | 2023-04-17 | 2023-05-23 | 山东松川新材料有限公司 | Low-cost and high-yield sodium isobutene disulfonate production process |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100448789C (en) * | 2006-12-05 | 2009-01-07 | 攀枝花钢企瑞通制冷设备有限公司 | Technique for treating industrial wastewater of containing sodium sulfate |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE1804135C3 (en) * | 1968-10-19 | 1974-08-08 | Bayer Ag, 5090 Leverkusen | Process for the production of sodium nethallylsulfonate |
| DE2221736C2 (en) * | 1972-05-04 | 1974-03-21 | Chemische Werke Huels Ag, 4370 Marl | Process for the separation of sodium methallyl sulfonate |
-
1997
- 1997-05-22 CN CN97106970A patent/CN1045432C/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101492399B (en) * | 2009-03-04 | 2012-06-27 | 太仓市新毛涤纶化工有限公司 | Method for preparing methylpropene sodium sulfonate |
| US8820895B2 (en) | 2009-07-10 | 2014-09-02 | Fujifilm Dimatix, Inc. | MEMS jetting structure for dense packing |
| US9278368B2 (en) | 2009-07-10 | 2016-03-08 | Fujifilm Dimatix, Inc. | MEMS jetting structure for dense packing |
| US9776408B2 (en) | 2009-07-10 | 2017-10-03 | Fujifilm Dimatix, Inc. | MEMS jetting structure for dense packing |
| US10696047B2 (en) | 2009-07-10 | 2020-06-30 | Fujifilm Dimatix, Inc. | MEMS jetting structure for dense packing |
| US11413869B2 (en) | 2009-07-10 | 2022-08-16 | Fujifilm Dimatix, Inc. | MEMS jetting structure for dense packing |
| CN103204785A (en) * | 2012-01-13 | 2013-07-17 | 湖北和昌新材料科技有限公司 | Dehydration method of sodium allylsulfonate |
| CN112625481A (en) * | 2020-12-16 | 2021-04-09 | 江苏德莱利建筑装饰工程有限公司 | Epoxy floor coating with formaldehyde absorption performance and preparation method thereof |
| CN112851555A (en) * | 2021-01-18 | 2021-05-28 | 浙江皇马科技股份有限公司 | Synthesis and refining method of sodium methallyl sulfonate |
| CN115403490A (en) * | 2022-08-16 | 2022-11-29 | 浙江皇马科技股份有限公司 | Refining method of sodium methallyl sulfonate |
| CN115403490B (en) * | 2022-08-16 | 2023-11-14 | 浙江皇马科技股份有限公司 | Refining method of sodium methallyl sulfonate |
| CN116143668A (en) * | 2023-04-17 | 2023-05-23 | 山东松川新材料有限公司 | Low-cost and high-yield sodium isobutene disulfonate production process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1045432C (en) | 1999-10-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101798154B (en) | Method for processing wastewater produced in saponification cyclization step in epoxy chloropropane production method | |
| CN102145912B (en) | Process for preparing calcium chloride solution by utilizing ammonia soda filtration mother liquor | |
| CN1076174A (en) | Produce the method for sodium salt from the salt solution in sodium ore deposit | |
| CN1045432C (en) | Preparation technology and equipment for sodium salt of methyl propenyl sulfonic acid | |
| CN107033107A (en) | A kind of method for preparing epoxychloropropane | |
| CN102442917A (en) | Energy-saving and environment-friendly method for producing glycin based on chloroacetic acid method | |
| CN101353289A (en) | Method for extracting trans-dichloroethylene from low-boiling residue of ethinyltrichloride production by gas-phase catalytic process | |
| CN108250106A (en) | A kind of method for preparing Sodium Dimethyl Isophthalate-5-sulfonate, sodium sulphate by three monomer process waste water | |
| CN109806816A (en) | A kind of chlorination reaction device of continuous round-robin method production | |
| CN1204102C (en) | Method for producing 2,3-dichloro-1-propahol and epiclorohyrin | |
| CN1320647A (en) | Process for preparing macroreticular weakly acidic cationic exchange resin of acrylic series | |
| CN105254469B (en) | A kind of process for cleanly preparing of ethyl chloride and device | |
| CN102887816A (en) | Method for preparing dichloropropanol with chemical reaction-pervaporation coupling method | |
| CN104250218A (en) | Tert-butyl acrylamide sulfonic acid production method | |
| CN105480948A (en) | Method and system for recycling by-product hydrogen chloride in fatty acid or fatty acyl chloride chlorination production process | |
| CN113666805B (en) | Method and system for continuously producing 4-chloro-3, 5-dimethylphenol | |
| CN109651066A (en) | A kind of production system of 1,1,2- trichloroethanes | |
| CN104230764A (en) | Preparation method of 2-acrylamide-2-methyl propanesulfonic acid | |
| CN114130063A (en) | Extraction and impurity removal device and method for recovering methanol through chlorination in maltol production | |
| CN1462741A (en) | Method for preparing sodium methallyl sulfonic acid | |
| CN1432556A (en) | Prepn process of 2,2,2-trifluoroethyl acetate | |
| CN1215048C (en) | Method for coproducing trichloromethane and N,N-dimethyl formyl amide with chlorine oil and dimethyl amine | |
| CN1277745C (en) | Method for producing boric acid from high magnesium low grade boron ore | |
| CN116924922B (en) | Method for continuously producing benzethonium chloride | |
| CN1283632C (en) | Process for preparing N-acetyl morpholine |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee |
Owner name: LIANDA CHEMICAL CO., LTD., DANYANG CITY Free format text: FORMER NAME OR ADDRESS: DANYANG BRANCH FACTORY, NANKAI UNIV. NEW TECH. GROUP CORP. |
|
| CP03 | Change of name, title or address |
Address after: Villa town Danyang city Jiangsu Province Patentee after: Lianda Chemical Co., Ltd., Danyang City Address before: Guide town, Danyang City, Jiangsu Patentee before: Danyang Branch Factory, Nankai Univ. New Tech. Group Corp. |
|
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |