CN101607881A - A kind of technology of dry production calcium stearate and device - Google Patents
A kind of technology of dry production calcium stearate and device Download PDFInfo
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- CN101607881A CN101607881A CNA2009103045056A CN200910304505A CN101607881A CN 101607881 A CN101607881 A CN 101607881A CN A2009103045056 A CNA2009103045056 A CN A2009103045056A CN 200910304505 A CN200910304505 A CN 200910304505A CN 101607881 A CN101607881 A CN 101607881A
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- Prior art keywords
- reaction
- calcium stearate
- reaction vessel
- water
- calcium
- 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.)
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Links
- CJZGTCYPCWQAJB-UHFFFAOYSA-L calcium stearate Chemical compound [Ca+2].CCCCCCCCCCCCCCCCCC([O-])=O.CCCCCCCCCCCCCCCCCC([O-])=O CJZGTCYPCWQAJB-UHFFFAOYSA-L 0.000 title claims abstract description 31
- 239000008116 calcium stearate Substances 0.000 title claims abstract description 31
- 235000013539 calcium stearate Nutrition 0.000 title claims abstract description 31
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- 238000005516 engineering process Methods 0.000 title claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 77
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000011575 calcium Substances 0.000 claims abstract description 12
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 claims abstract description 12
- 235000021355 Stearic acid Nutrition 0.000 claims abstract description 10
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000008117 stearic acid Substances 0.000 claims abstract description 10
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910052791 calcium Inorganic materials 0.000 claims abstract description 9
- 150000001875 compounds Chemical class 0.000 claims abstract description 8
- 238000003756 stirring Methods 0.000 claims abstract description 8
- 238000009434 installation Methods 0.000 claims abstract description 4
- 239000008367 deionised water Substances 0.000 claims description 14
- 229910021641 deionized water Inorganic materials 0.000 claims description 14
- 238000000034 method Methods 0.000 claims description 14
- 239000000498 cooling water Substances 0.000 claims description 8
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical group [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 6
- 239000000920 calcium hydroxide Substances 0.000 claims description 6
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 6
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims description 5
- 239000000292 calcium oxide Substances 0.000 claims description 5
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 5
- 150000002500 ions Chemical group 0.000 claims description 3
- 239000012154 double-distilled water Substances 0.000 claims description 2
- 239000002351 wastewater Substances 0.000 abstract description 10
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000003723 Smelting Methods 0.000 abstract 1
- 239000000047 product Substances 0.000 description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 11
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 238000001035 drying Methods 0.000 description 5
- DPDMMXDBJGCCQC-UHFFFAOYSA-N [Na].[Cl] Chemical compound [Na].[Cl] DPDMMXDBJGCCQC-UHFFFAOYSA-N 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 239000003643 water by type Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000006073 displacement reaction Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012065 filter cake Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910000765 intermetallic Inorganic materials 0.000 description 1
- 238000005649 metathesis reaction Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 238000007127 saponification reaction Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of technology of dry production calcium stearate, the compound of stearic acid, calcium and water are 82～88%: 10～15% with weight ratio: 2～5% ratio is added in the reaction unit, under the condition of 80 ℃～150 ℃ of temperature, pressure 0～0.10MPa, stirring reaction 1～5 hour promptly obtains calcium stearate.This reaction unit is that motor (1) is connected with speed reduction unit (2), and speed reduction unit (2) is connected with gear-shift mechanism (3), and gear-shift mechanism (3) is connected with the agitator (9) of installation in the reaction vessel (4); Reaction vessel (4) top is provided with temperature-measuring port (5), charging opening (6), the outer chuck (8) that is provided with of reaction vessel (4), and reaction vessel (4) below is provided with discharge port (10).The present invention's step that simplifies the operation reduces cost and energy consumption, has reduced discharged waste water, reduces the dirty expense of smelting, more reduced the influence to environment, has overcome the shortcoming that conventional wet is produced the technology of stearate.
Description
Technical field
The present invention relates to a kind of production technique and device of calcium stearate, is a kind of technology and device of dry production calcium stearate specifically.
Background technology
Calcium stearate (claiming calcium soap again) is of wide application, as medicine industry, and foodstuffs industry, coating, papermaking, stationery, makeup, plastics, rubber, synthon etc. are widespread use all.
The production of calcium stearate product, traditional technology makes with the double decomposition method.The disadvantage of double decomposition production is that efficient is low, wastewater flow rate is big.Calcium stearate good market prospects at present, this product does not have toxicity, is of wide application, and the annual demand in domestic and international market reaches 100,000 tons according to incompletely statistics.But the traditional technology calcium stearate all is to produce in water medium, and reaction finishes to contain a large amount of by product sodium-chlor in the calcium stearate of back gained, must be through press filtration, and will float with a large amount of water to wash just and can obtain standard compliant product.Produce one ton of calcium stearate and often will produce nearly 50 tons waste water, contain a large amount of sodium-chlor in the waste water.In the rinse cycle, a spot of superfine powder easily passes strainer, the situation that causes waste water COD and suspended substance to exceed standard.Therefore, this technology pollution treatment appropriate litigation fees height.
Summary of the invention
Technical problem to be solved by this invention provides a kind of technology and device of dry production calcium stearate, and the step that simplifies the operation reduces cost and energy consumption, reduce discharged waste water, reduce the pollution treatment expense, avoid environmental pollution, overcome the shortcoming that conventional wet is produced the technology of calcium stearate.
In order to address the above problem, the invention provides following technical scheme:
A kind of technology of dry production calcium stearate, the compound of stearic acid, calcium and water are 82～88%: 10～15% with mass ratio: 2～5% ratio is added in the reaction unit, 50～150 ℃ of temperature,, under the condition of pressure 0～0.10MPa, stirring reaction 1～5 hour promptly obtains calcium stearate.
The compound of calcium and stearic temperature of reaction are 80～120 ℃.
The water that adds is deionized water; Deionized water comprises ion exchanged water, electrodialytic water or double distilled water etc.
The compound of calcium is calcium hydroxide or calcium oxide etc.
The reaction unit that uses in the calcium stearate production technique, it comprises reaction vessel, charging opening and chuck, and motor is connected with speed reduction unit, and speed reduction unit is connected with gear-shift mechanism, and gear-shift mechanism is connected with the agitator of installation in the reaction vessel; The reaction vessel top is provided with charging opening, gas inlet and outlet piping mouth, and reaction vessel is provided with chuck outward, and the reaction vessel below is provided with discharge port, and the chuck side is provided with steam and entrance of cooling water and steam and cooling water outlet.
Agitator is 2, and oppositely shears rotation, the variable ratio frequency changer speed governing;
The reaction vessel top is provided with temperature-measuring port; Reaction vessel is a pressure vessel.
Compared with prior art, the present invention has following advantage:
1, reactions steps is few, and operational path is short:
Traditional Wet Method Reaction principle:
NaOH+CH
3(CH
2)
16COOH Zhao CH
3(CH
2)
16COONa+H
2O
CaCl
2+ 2CH
3(CH
2)
16COONa Zhao (CH
3(CH
2)
16COO)
2Ca+2NaCl
Operational path: saponification reaction Zhao replacement(metathesis)reaction Zhao press filtration Zhao rinsing Zhao dries the dry Zhao of Zhao and pulverizes the Zhao packing.
Dry process reaction principle of the present invention:
Ca (OH)
2+ 2CH
3(CH
2)
16COOH Zhao (CH
3(CH
2)
16COO)
2Ca+2H
2O
Operational path: the reaction Zhao is pulverized the Zhao packing.
2,1 ton of calcium stearate of the every production of conventional wet technology needs 20 tons of process waters to participate in reaction as reaction medium, and temperature of reaction needs to consume a large amount of heat energy and heats between 90 ~ 110 ℃.1 ton of calcium stearate of every production will produce the sodium-chlor by product about 207kg, needs to filter dried back water after reaction finishes and carries out rinsing, will consume a large amount of water to these sodium-chlor wash cleans, is easy to totally not cause impurity content exceeding index because of washing.Through containing the moisture content more than 50% in the material of filter dehydration at least, must be dry in moisture eliminator, also to expend a large amount of heat energy; And deposit seeds is little, dispersity is high, surface adsorption is strong, causes filter cake moisture content height, and energy consumption for drying is big, and production efficiency is low and the product apparent density is little, and dust from flying is serious, packing, accumulating expense height.It is less relatively that dry technology for production of the present invention heats total inventory, can save a large amount of energy consumptions.The by product of reaction process is a water, need not to wash, and does not almost have the processing wastewater discharging.And do not need the product baking operation, and greatly reduce energy consumption, react also very complete.In addition, material is in high temperature more than 100 ℃, the sealing equipment in the process of stoichiometric number hour, and the microorganism that may survive in raw material will lose activity fully originally, has in fact played calcium stearate is played the sterilization and disinfection effect.
3, calcium hydroxide and stearic acid are weak acid and middle alkaline neutralization reaction, and extent of reaction is slower, and granularity is arranged, and is difficult for reacting completely. also be difficult for making high quality, highly purified calcium stearate; And the deionized water that has added mass ratio 2～5% among the present invention plays the effect of catalyzer, and in conjunction with homemade reaction unit among the present invention, it has 2 two oars and oppositely shears the agitator of rotation, makes the reaction of calcium hydroxide and stearic acid thorough mixing.
4, temperature of reaction 80-120 of the present invention ℃, high temperature helps the compound and the stearic reaction of calcium, the deionized water that adds in the reaction can be discharged in the mode of water vapor simultaneously, like this when reacting completely, product has been carried out drying, handled just having obtained finished product after the discharge a little.The finished product that dry process makes the finished product quality produce than other direct methods is more loose, and better quality, aftertreatment are simpler.
5, quality product of the present invention is more stable, more superior, because directly employing stearic acid and metallic compound reactions steps is few, process does not have waste water, does not exist sodium salt to exceed standard or washs the mass discrepancy that difference causes.
6, reduced cost, material cost specific humidity Pharaoh technology has reduced by 1600 yuan/ton, operations such as press filtration, washing, drying have been saved, shortened the production cycle, production efficiency, energy consumption and labor cost have been improved, reduce by 1000 yuan/ton, add that the pollution treatment cost descends, total cost has reduced more than 2600 yuan/ton.
7, protected environment; the dry method novel process only adds the deionized water that is equivalent to product 5% in reaction process; need not filter, wash; reduce the generation of a large amount of waste water, per tonly reduced by 50 tons of waste water, can save 300,000 yuan wastewater treatment expense the whole year; for good basis has been laid in enterprise development; strengthened the market competitiveness of enterprise product, more efforts at environmental protection have been done and should have been done duty, and its social benefit can't be estimated.
8, the present invention adopts deionized water to participate in reaction, effectively reduces or eliminate the interference of foreign ion in the reaction process.
9, the present invention adopts double stirrer, and is that pair slurry is oppositely sheared rotation, and is simple in structure, makes reaction raw materials stir, fully react.
Description of drawings
Fig. 1 is the synoptic diagram of reaction unit of the present invention, wherein 1, motor, and 2, step-down gear, 3, gear-shift mechanism, 4, reaction vessel, 5, temperature-measuring port, 6, charging opening, 7, gas inlet and outlet piping mouth, 8, chuck, 9, agitator, 10, discharge port, 11, steam and cooling water inlet, 12, steam and cooling water outlet.
Fig. 2 is the partial top view of Fig. 1.
Embodiment
Embodiment 1: reaction raw materials: 48 kilograms in calcium hydroxide, 352 kilograms of stearic acid, 15 kilograms of deionized waters.
At first stearic acid is dropped in the reaction vessel 4 by charging opening 6, about heated and stirred 10min, after treating that temperature is raised to 50 ℃, with the calcium hydroxide input, pour the deionized water of 15kg after fully stirring from opening for feed into, constantly feed nitrogen, the air in the reaction vessel 4 is discharged from top feeding mouth 6 by gas inlet and outlet piping mouth 7, after progressively the air displacement in the reaction vessel 4 being become nitrogen, fasten charging opening 6 and gas inlet and outlet piping mouth 7 valves.When stirring, gradually reaction mass is heated between 80 ℃～120 ℃.The vapour pressure that deionized water in the maintenance reaction vessel 4 and water generation reaction form is between 0～0.1MPa.React after about two hours, open gas inlet and outlet piping mouth 7 valves, the water vapour of wherein nitrogen, deionized water steam and reaction generation is discharged reaction vessel 4.Survey product moisture and whether meet the industry specified requirement, if moisture is higher, then from gas pipeline 7 be evacuated to meet moisture requirement till, then product is emitted from discharge port 10.
Embodiment 2: reaction raw materials: 30 kilograms in calcium oxide, 285 kilograms of stearic acid, 12 kilograms of deionized waters.
At first calcium oxide is dropped in the reaction vessel 4 by charging opening 6, stir and the adding deionized water, treat to drop into stearic acid after calcium oxide and water react completely, constantly feed nitrogen by gas inlet and outlet piping mouth 7, air in the reactor 4 is discharged from top feeding mouth 6, after progressively the air displacement in the reactor 4 being become nitrogen, fasten charging opening 6 and gas inlet and outlet piping mouth 7 valves.When stirring, gradually reaction mass is heated between 80 ℃～120 ℃.The vapour pressure that deionized water in the maintenance reactor 4 and water generation reaction form is between 0～0.1MPa.React after about two hours, open gas inlet and outlet piping mouth 7 valves, the water vapour of wherein nitrogen, deionized water steam and reaction generation is discharged reaction vessel 4.Survey product moisture and whether meet the industry specified requirement, if moisture is higher, then from gas pipeline 7 be evacuated to meet moisture requirement till, then product is emitted from discharge port 10.
Embodiment 3: as shown in Figure 1, 2, this reaction unit comprises reaction vessel 4, charging opening 6 and chuck 8, motor 1 is connected with speed reduction unit 2, speed reduction unit 2 is connected with gear-shift mechanism 3, gear-shift mechanism 3 is connected with the agitator 9 of installation in the reaction vessel 4, agitator 9 is 2, and oppositely shears rotation, the variable ratio frequency changer speed governing; Reaction vessel 4 is a pressure vessel, reaction vessel 4 tops are provided with charging opening 6, gas inlet and outlet piping mouth 7 and temperature-measuring port 5, the reaction vessel 4 outer chucks 8 that are provided with, reaction vessel 4 belows are provided with discharge port 10, chuck 8 sides are provided with steam and entrance of cooling water 11 and steam and cooling water outlet 12, can heat or cool off by steam or water coolant.
Claims (9)
1. the technology of a dry production calcium stearate, it is characterized in that: the compound of stearic acid, calcium and water are 82～88%: 10～15% with mass ratio: 2～5% ratio is added in the reaction unit, under the condition of 50～150 ℃ of temperature, pressure 0～0.10MPa, stirring reaction 1～5 hour promptly obtains calcium stearate.
2. the technology of dry production calcium stearate according to claim 1 is characterized in that: the compound of calcium and stearic temperature of reaction are 80～120 ℃.
3. the technology of dry production calcium stearate according to claim 1 is characterized in that: the water of adding is deionized water.
4. the technology of dry production calcium stearate according to claim 3 is characterized in that: deionized water comprises ion exchanged water, electrodialytic water or double distilled water.
5. the technology of dry production calcium stearate according to claim 1 is characterized in that: the compound of calcium is calcium hydroxide or calcium oxide.
6. the reaction unit that uses in the calcium stearate production technique as claimed in claim 1, it comprises reaction vessel (4), charging opening (6) and chuck (8), it is characterized in that: motor (1) is connected with speed reduction unit (2), speed reduction unit (2) is connected with gear-shift mechanism (3), and gear-shift mechanism (3) is connected with the agitator (9) of installation in the reaction vessel (4); Reaction vessel (4) top is provided with charging opening (6), gas inlet and outlet piping mouth (7), the outer chuck (8) that is provided with of reaction vessel (4), reaction vessel (4) below is provided with discharge port (10), and chuck (8) side is provided with steam and entrance of cooling water (11) and steam and cooling water outlet (12).
7. the reaction unit that uses in the calcium stearate production technique according to claim 6 is characterized in that: agitator (9) is 2, and oppositely shears rotation.
8. the reaction unit that uses in the calcium stearate production technique according to claim 6 is characterized in that: reaction vessel (4) top is provided with temperature-measuring port (5).
9. the reaction unit that uses in the calcium stearate production technique according to claim 6 is characterized in that: reaction vessel (4) is a pressure vessel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910304505A CN101607881B (en) | 2009-07-17 | 2009-07-17 | Dry production technique and device of calcium stearate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910304505A CN101607881B (en) | 2009-07-17 | 2009-07-17 | Dry production technique and device of calcium stearate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101607881A true CN101607881A (en) | 2009-12-23 |
| CN101607881B CN101607881B (en) | 2012-10-03 |
Family
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Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101607881B (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102344354A (en) * | 2010-08-06 | 2012-02-08 | 南通新邦化工科技有限公司 | Calcium stearate fusion production process and calcium stearate reaction kettle thereof |
| CN102690187A (en) * | 2012-03-27 | 2012-09-26 | 江苏汉光实业股份有限公司 | Stabilizer production system |
| CN103526624A (en) * | 2013-10-22 | 2014-01-22 | 湖州市菱湖新望化学有限公司 | Method for preparing microcrystalline cellulose and reaction equipment of microcrystalline cellulose |
| CN103694100A (en) * | 2013-11-25 | 2014-04-02 | 广州科技职业技术学院 | Production method for barium stearate |
| CN107056598A (en) * | 2017-05-27 | 2017-08-18 | 湖州市菱湖新望化学有限公司 | The technique and device of a kind of solid phase method production calcium acetylacetonate |
| CN108558643A (en) * | 2018-05-28 | 2018-09-21 | 郴州浩伦生化助剂有限公司 | A kind of preparation process and its Preparation equipment of calcium stearate |
| CN108752196A (en) * | 2018-05-28 | 2018-11-06 | 郴州浩伦生化助剂有限公司 | A kind of preparation process of calcium stearate |
| CN110183324A (en) * | 2019-06-11 | 2019-08-30 | 东莞市汉维科技股份有限公司 | A kind of preparation process of stearate |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN2530718Y (en) * | 2002-01-15 | 2003-01-15 | 上海建筑材料集团新材料有限公司 | Carbonizing claded reactor |
| CN101265173A (en) * | 2008-04-23 | 2008-09-17 | 顾泽元 | Method for preparing calcium stearate particles |
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2009
- 2009-07-17 CN CN200910304505A patent/CN101607881B/en active Active
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102344354A (en) * | 2010-08-06 | 2012-02-08 | 南通新邦化工科技有限公司 | Calcium stearate fusion production process and calcium stearate reaction kettle thereof |
| CN102690187A (en) * | 2012-03-27 | 2012-09-26 | 江苏汉光实业股份有限公司 | Stabilizer production system |
| CN103526624A (en) * | 2013-10-22 | 2014-01-22 | 湖州市菱湖新望化学有限公司 | Method for preparing microcrystalline cellulose and reaction equipment of microcrystalline cellulose |
| CN103694100A (en) * | 2013-11-25 | 2014-04-02 | 广州科技职业技术学院 | Production method for barium stearate |
| CN103694100B (en) * | 2013-11-25 | 2015-07-15 | 广州科技职业技术学院 | Production method for barium stearate |
| CN107056598A (en) * | 2017-05-27 | 2017-08-18 | 湖州市菱湖新望化学有限公司 | The technique and device of a kind of solid phase method production calcium acetylacetonate |
| CN108558643A (en) * | 2018-05-28 | 2018-09-21 | 郴州浩伦生化助剂有限公司 | A kind of preparation process and its Preparation equipment of calcium stearate |
| CN108752196A (en) * | 2018-05-28 | 2018-11-06 | 郴州浩伦生化助剂有限公司 | A kind of preparation process of calcium stearate |
| CN110183324A (en) * | 2019-06-11 | 2019-08-30 | 东莞市汉维科技股份有限公司 | A kind of preparation process of stearate |
| CN110183324B (en) * | 2019-06-11 | 2021-09-21 | 东莞市汉维科技股份有限公司 | Preparation process of stearate |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101607881B (en) | 2012-10-03 |
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