CN102875356A - Calcium stearate production method - Google Patents
Calcium stearate production method Download PDFInfo
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- CN102875356A CN102875356A CN2012104020058A CN201210402005A CN102875356A CN 102875356 A CN102875356 A CN 102875356A CN 2012104020058 A CN2012104020058 A CN 2012104020058A CN 201210402005 A CN201210402005 A CN 201210402005A CN 102875356 A CN102875356 A CN 102875356A
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- Prior art keywords
- stearate
- calcium
- reaction
- stearic acid
- calcium hydroxide
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- CJZGTCYPCWQAJB-UHFFFAOYSA-L calcium stearate Chemical compound [Ca+2].CCCCCCCCCCCCCCCCCC([O-])=O.CCCCCCCCCCCCCCCCCC([O-])=O CJZGTCYPCWQAJB-UHFFFAOYSA-L 0.000 title claims abstract description 70
- 239000008116 calcium stearate Substances 0.000 title claims abstract description 70
- 235000013539 calcium stearate Nutrition 0.000 title claims abstract description 70
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 55
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims abstract description 47
- 239000000920 calcium hydroxide Substances 0.000 claims abstract description 47
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims abstract description 47
- 229940088990 ammonium stearate Drugs 0.000 claims abstract description 43
- JPNZKPRONVOMLL-UHFFFAOYSA-N azane;octadecanoic acid Chemical compound [NH4+].CCCCCCCCCCCCCCCCCC([O-])=O JPNZKPRONVOMLL-UHFFFAOYSA-N 0.000 claims abstract description 43
- 235000021355 Stearic acid Nutrition 0.000 claims abstract description 42
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 claims abstract description 42
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 claims abstract description 42
- 239000008117 stearic acid Substances 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 33
- 239000000706 filtrate Substances 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 18
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000000725 suspension Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 13
- 239000011575 calcium Substances 0.000 claims description 10
- 125000004122 cyclic group Chemical group 0.000 claims description 9
- 239000003054 catalyst Substances 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 6
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000013505 freshwater Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 14
- 239000000047 product Substances 0.000 abstract description 11
- 239000001257 hydrogen Substances 0.000 abstract description 8
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 8
- 238000000354 decomposition reaction Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract 1
- 238000010992 reflux Methods 0.000 abstract 1
- 238000003756 stirring Methods 0.000 description 12
- 239000002002 slurry Substances 0.000 description 10
- 238000001914 filtration Methods 0.000 description 9
- 239000000292 calcium oxide Substances 0.000 description 7
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 7
- -1 hydrogen calcium oxide Chemical class 0.000 description 7
- 229910017053 inorganic salt Inorganic materials 0.000 description 6
- 230000018044 dehydration Effects 0.000 description 5
- 238000006297 dehydration reaction Methods 0.000 description 5
- 238000001035 drying Methods 0.000 description 5
- 238000005649 metathesis reaction Methods 0.000 description 5
- 238000013019 agitation Methods 0.000 description 4
- 229910001220 stainless steel Inorganic materials 0.000 description 4
- 239000010935 stainless steel Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000013543 active substance Substances 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000004800 polyvinyl chloride Substances 0.000 description 2
- 239000000344 soap Substances 0.000 description 2
- 239000003381 stabilizer Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- 241000370738 Chlorion Species 0.000 description 1
- 239000006057 Non-nutritive feed additive Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000011362 coarse particle Substances 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 229920000915 polyvinyl chloride Polymers 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Lubricants (AREA)
Abstract
The invention discloses a calcium stearate production method. The calcium stearate production method is characterized by including steps of firstly, subjecting ammonium stearate and calcium hydroxide to reaction to generate calcium stearate and ammonia water; secondly, when calcium hydroxide turbid liquid is insufficiently added, stearic acid is excessive, subjecting the stearic acid and the ammonia water to reaction to generate the ammonium stearate, and preparing the ammonium stearate required in the first step; and when calcium hydroxide turbid liquid is slightly excessively added, subjecting the ammonium stearate and the calcium hydroxide to reaction and generating calcium stearate and ammonia water, wherein the ammonia water is freed and is decomposed to generate ammonia gas on the condition of the pH (potential of hydrogen) value of 9-9.5 of the reaction system at the temperature of 65-85 DEG C, and filtrate is composed of water and precious little calcium hydroxide soluble in water. The calcium stearate production method is simple in process and is low in reaction temperature and energy consumption and low in requirements for equipment as compared with a double decomposition process, no reflux reaction is needed in the later stage of reaction, even general double decomposition process production equipment can produce products, economic benefits are evident, and accordingly, the calcium stearate production method is applicable to further popularization.
Description
Technical field
The invention belongs to the technology preparation field of thermo-stabilizer, be specifically related to water calcium stearate new synthetic process.
Background technology
Calcium stearate is a kind of Non-toxicHeat Stabilizer for Polyvinyl Chloride, is indispensable processing aid in the polyvinyl chloride (PVC) RESINS plastic working process.The domestic production calcium stearate mainly is double decomposition at present, be that stearic acid is reacted into the stearic acid soda soap aqueous solution at aqueous phase and sodium hydroxide solution, the stearic acid soda soap aqueous solution carries out replacement(metathesis)reaction with the water-soluble Ca salt of in advance preparation, generate calcium stearate and water-soluble sodium salt, the hot water that contains water-soluble inorganic salt that produces in the production process can not recycle, thereby the waste water that contains in a large number inorganic salt of generation can only discharge (if reclaim inorganic salt, energy consumption is too high, does not have economic worth).
Stearic acid and calcium hydroxide are even in the aqueous phase low-temperature mixed, slowly heat, and reaction obtains coarse grained heavy product, are easy to form parcel, and reaction not exclusively will increase in addition disintegrating apparatus and just can reach user's fineness requirement.
Another produces calcium stearate with scorification, although there is not discharge of wastewater, because calcium stearate molten mass viscosity is higher, thereby very high to equipment requirements, tooling cost is high, and the producer of domestic production calcium stearate seldom uses scorification technique.
A kind of " without the method for discharging one-step synthesis calcium stearate " publication number CN101117312A's haves no right patent in addition, although illustrate without discharging, the reaction later stage still needs to regulate with calcium chloride, it is more and more to cause chlorion to gather, still need discharging, and the reaction later stage need to be 90 ~ 100 ℃ of back flow reaction, back flow reaction needs airtight pressurized vessel, equipment requirements is high, inconvenient operation.
Summary of the invention
The present invention utilizes the device fabrication of metathesis process to go out the calcium stearate product that quality is higher than metathesis process, and water cycle is used, and does not have discharge of wastewater, and save energy is a kind of novel process of synthetic water calcium stearate.
Water calcium stearate new synthetic process process is as follows:
1. be the Catalyst Production calcium stearate with the ammonium stearate that generates in ammonium stearate or the reaction process;
2. the feed hydrogen calcium oxide is mixed with suspension liquid with 60 ~ 95 ℃ hot water, and the mass ratio of calcium hydroxide and water is 1:6, crosses 200 mesh sieves, under the agitation condition, can not form the calcium hydroxide deposition, thereby obtain the calcium hydroxide suspension liquid.(if calcium hydroxide is not processed like this, and stearic acid and calcium hydroxide react in water, and obtaining diameter is the incomplete coarse particles heavy product of reaction of 0.5 ~ 1cm);
3. stearic acid drops in the water, is heated to 58 ~ 62 ℃, and the stearic acid fusing under the agitation condition, adds catalyzer ammonium stearate or ammoniacal liquor (ammoniacal liquor and stearic acid also generate ammonium stearate).Ammonium stearate is tensio-active agent and catalyzer, stearic acid is dispersed in the water, add the calcium hydroxide suspension liquid after the sieving of the 2nd step preparation, total add-on of calcium hydroxide suspension liquid will be adjusted in right amount according to the calcium contents of feed hydrogen calcium oxide content and product (requiring in principle the feed hydrogen calcium oxide content greater than 98%), the control temperature of reaction is 65 ~ 85 ℃, after the stable reaction, final ph is 9 ~ 9.5, obtain the intermediate calcium stearate slurry of calcium stearate, the calcium stearate slurry obtains filtrate and calcium stearate tide material through dehydration, filtrate cycle is used, and calcium stearate tide material drying obtains lightweight, the calcium stearate product of high fineness.
The chemical reaction that the present invention uses:
Ammonium stearate and calcium hydroxide reaction generate calcium stearate and ammoniacal liquor.
2C
17H
35COONH
4+Ca(OH)
2=(C
17H
35COO)
2Ca+2NH
3·H
2O。
When calcium hydroxide suspension liquid add-on not during capacity, stearic acid is excessive, and stearic acid and ammoniacal liquor generate ammonium stearate.
C
17H
35COOH+?NH
3·H
2O?=?C
17H
35COONH
4+H
2O。
When the calcium hydroxide suspension liquid that adds was slightly excessive, ammonium stearate generated calcium stearate and ammoniacal liquor with calcium hydroxide reaction, and ammoniacal liquor dissociates out, and at about 65 ~ 85 ℃, reaction system ph is that ammoniacal liquor is decomposed into ammonia and overflows from reaction system under 9 ~ 9.5 the condition.Filtrate is water and the water-soluble calcium hydroxide of minute quantity.
Total reaction is 2 C
17H
35COOH+Ca (OH)
2=(C
17H
35COO)
2Ca+H
2O.
Various material proportions:
As catalyzer, do not have the cyclic water jacket time spent with ammonium stearate, raw material and catalyzer are recommended ratio:
Stearic acid: calcium hydroxide: ammonium stearate: water=456.6:76:46:4000.
As catalyzer, there is with ammonium stearate the cyclic water jacket time spent.
Stearic acid: calcium hydroxide: ammonium stearate: water=456.6:73:46:4000.
As catalyzer (ammonium stearate that ammoniacal liquor and stearic acid reaction generate plays catalyst action), do not have the cyclic water jacket time spent with ammoniacal liquor, raw material and catalyzer are recommended ratio:
Stearic acid: calcium hydroxide: ammoniacal liquor: water=500:76:10:4000.
As catalyzer (ammonium stearate that ammoniacal liquor and stearic acid reaction generate plays catalyst action), there is with ammoniacal liquor the cyclic water jacket time spent, recommends optimum proportion:
Stearic acid: calcium hydroxide: ammoniacal liquor: water=500:73:10:4000.
The invention has the advantages that:
What 1, technique of the present invention was different from CN101117312A is: do not produce inorganic salt in the reaction process, do not need to add inorganic salt yet, can not form inorganic salt gathers, therefore the filtrate after filtering all recycles, the part water of taking away when tide material calcium stearate is dry carries out subsequent reactions by replenishing fresh water, do not have discharge of wastewater fully, only discharge the ammonia (in environmental protection allows the quantity discharged scope) of minute quantity.
2, technique of the present invention, technique is simple, and the reaction later stage does not need back flow reaction, compares with metathesis process, temperature of reaction is low, and energy consumption is low, and equipment requirements is not high, general metathesis process production unit can be produced this product, and economic benefit is obvious, and this production technique is fit to further penetration and promotion.
Embodiment
Embodiment 1
With ammonium stearate as catalyzer, filtrate the applying mechanically of not circulating.
At 1 m
3Add 450 kg water in the batching kettle, and be heated to 60 ℃ ~ 95 ℃, and add again 76 kg of hydrogen calcium oxide (calcium hydroxide content is more than 98%), stirred 10 minutes, by 200 order stainless steel sifts, the calcium hydroxide suspension liquid after the filtration is sent into the calcium hydroxide header tank that band stirs.
At 5m
3Reactor in add 3550 kg water, the stearic acid that adds again 456.6 kilograms, be heated to 58 ~ 62 ℃, the stearic acid fusing, under the agitation condition, add 46 kilograms of catalyzer ammonium stearate, stir, slowly add the calcium hydroxide suspension liquid after filtering, the control temperature of reaction is no more than 85 ℃, final ph is 9 ~ 9.5, obtain the intermediate calcium stearate slurry of calcium stearate, continue to stir 15 minutes, make reaction more complete, the calcium stearate slurry obtains filtrate and calcium stearate tide material through dehydration, filtrate cycle is used, and calcium stearate tide material is dry (notices that hot blast temperature surpasses 125 ℃, because the calcium stearate of the saliferous that makes with double decomposition is compared, just fusing point is lower for salt-free calcium stearate), obtain lightweight after the drying, the calcium stearate product of high fineness.
Embodiment 2
As catalyzer, there is circulation filtrate to apply mechanically with ammonium stearate.
At 1 m
3Add 450 kilograms of circulation filtrates in the batching kettle, and be heated to 60 ℃ ~ 95 ℃, and add again 73 kg of hydrogen calcium oxide (calcium hydroxide content is more than 98%), stirred 10 minutes, by 200 order stainless steel sifts, the calcium hydroxide suspension liquid after the filtration is sent into the calcium hydroxide header tank that band stirs.
At 5m
3Reactor in add residual filtrate and 3550 kilograms of make up water totals among the embodiment 1, the stearic acid that adds again 456.6 kilograms, be heated to 58 ~ 62 ℃, the stearic acid fusing, stir lower, add 46 kilograms of catalyzer ammonium stearate, stir, slowly add the calcium hydroxide suspension liquid after filtering, the control temperature of reaction is no more than 85 ℃, final ph is 9 ~ 9.5, obtains the intermediate calcium stearate slurry of calcium stearate, continues to stir 15 minutes, make reaction more complete, the calcium stearate slurry obtains filtrate and calcium stearate tide material through dehydration, and filtrate cycle is used, and obtains lightweight after the calcium stearate tide material drying, the calcium stearate product of high fineness.
Embodiment 3
In reaction process, the ammonium stearate that ammoniacal liquor and stearic acid reaction generate plays catalyst action, filtrate the applying mechanically of not circulating.
At 1 m
3Add 450 kg water in the batching kettle, and be heated to 60 ℃ ~ 95 ℃, and add again 76 kg of hydrogen calcium oxide (calcium hydroxide content is more than 98%), stirred 10 minutes, by 200 order stainless steel sifts, the calcium hydroxide header tank that the calcium hydroxide suspension liquid after the filtration send band to stir.
At 5m
3Reactor in add 3550 kg water, the stearic acid that adds again 500 kilograms, be heated to 58 ~ 62 ℃, the stearic acid fusing, stir lower, add 10 kilograms of ammoniacal liquor, ammoniacal liquor and stearic acid generate the catalyzer ammonium stearate, ammonium stearate be catalyzer be again tensio-active agent, stearic acid is dispersed in the water, stirred 5 minutes, slowly add the calcium hydroxide suspension liquid after filtering, the control temperature of reaction is no more than 85 ℃, and final ph is 9 ~ 9.5, obtains the intermediate calcium stearate slurry of calcium stearate, continue to stir 15 minutes, make reaction more complete, the calcium stearate slurry obtains filtrate and calcium stearate tide material through dehydration, and filtrate cycle is used, calcium stearate tide material is dry (notices that hot blast temperature is not above 125 ℃, because the calcium stearate of the saliferous that makes with double decomposition is compared, just fusing point is lower for salt-free calcium stearate), obtain lightweight after the drying, the calcium stearate product of high fineness.
Embodiment 4
In reaction process, the ammonium stearate that ammoniacal liquor and stearic acid reaction generate plays catalyst action, has cyclic water jacket to use.
At 1 m
3Add the filtrate of circulating among 450 kilograms of embodiment 3 in the batching kettle, and be heated to 60 ℃ ~ 95 ℃, and add again 76 kg of hydrogen calcium oxide (calcium hydroxide content is more than 98%), stirred 10 minutes, by 200 order stainless steel sifts, the calcium hydroxide suspension liquid after the filtration is sent into the calcium hydroxide header tank that band stirs.
At 5m
3Reactor in add residual filtrate and 3550 kilograms of make up water totals among the embodiment 3, the stearic acid that adds again 500 kilograms, be heated to 58 ~ 62 ℃, the stearic acid fusing, under the agitation condition, add 10 kilograms of ammoniacal liquor, ammoniacal liquor and stearic acid generate ammonium stearate, ammonium stearate be catalyzer be again tensio-active agent, stearic acid is dispersed in the water, stirred 5 minutes, slowly add the calcium hydroxide suspension liquid after filtering, the control temperature of reaction is no more than 85 ℃, and final ph is 9 ~ 9.5, obtains the intermediate calcium stearate slurry of calcium stearate, continue to stir 15 minutes, make reaction more complete, the calcium stearate slurry obtains filtrate and calcium stearate tide material through dehydration, and filtrate cycle is used, calcium stearate tide material is dry (notices that hot blast temperature is not above 125 ℃, because the calcium stearate of the saliferous that makes with double decomposition is compared, just fusing point is lower for salt-free calcium stearate), obtain lightweight after the drying, the calcium stearate product of high fineness.
Claims (6)
1. the production method of a calcium stearate, it is characterized in that: step is as follows:
A, ammonium stearate and calcium hydroxide reaction generate calcium stearate and ammoniacal liquor,
2C
17H
35COONH
4+Ca(OH)
2=(C
17H
35COO)
2Ca+2NH
3·H
2O；
B, when calcium hydroxide suspension liquid add-on not during capacity, stearic acid is excessive, stearic acid and ammoniacal liquor generate ammonium stearate, make steps A) the required ammonium stearate of reaction,
C
17H
35COOH+?NH
3·H
2O?=?C
17H
35COONH
4+H
2O；
When the calcium hydroxide suspension liquid that adds was slightly excessive, ammonium stearate generated calcium stearate and ammoniacal liquor with calcium hydroxide reaction, and ammoniacal liquor dissociates out, and at about 65 ℃ ~ 85 ℃, reaction system ph is that ammoniacal liquor is decomposed into ammonia and overflows from reaction system under 9 ~ 9.5 the condition; Filtrate is water and the water-soluble calcium hydroxide of minute quantity;
Total reaction is 2 C
17H
35COOH+Ca (OH)
2=(C
17H
35COO)
2Ca+H
2O;
The filtrate that reaction produces can be recycled, and the water that tide material calcium stearate is taken away replenishes fresh water and carries out subsequent production when subsequent production.
2. the production method of a kind of calcium stearate according to claim 1 is characterized in that: the production method of described calcium stearate is for being the Catalyst Production calcium stearate with the ammonium stearate that generates in ammonium stearate or the reaction process.The acquisition approach of ammonium stearate is two kinds: a kind of is commercially available ammonium stearate, and another kind is in reaction process, makes ammonium stearate by ammoniacal liquor and stearic acid reaction.
3. the production method of a kind of calcium stearate according to claim 1 is characterized in that: described with ammonium stearate as catalyzer, do not have the cyclic water jacket time spent, the quality of raw material and catalyzer is than ratio:
Stearic acid: calcium hydroxide: ammonium stearate: water=456.6:76:46:4000.
4. the production method of a kind of calcium stearate according to claim 1 is characterized in that: described with ammonium stearate as catalyzer, the cyclic water jacket time spent is arranged, the quality of raw material and catalyzer is than ratio:
Stearic acid: calcium hydroxide: ammonium stearate: water=456.6:73:46:4000.
5. the production method of a kind of calcium stearate according to claim 1 is characterized in that: the described ammonium stearate that generates with ammoniacal liquor and stearic acid reaction plays catalyst action, does not have the cyclic water jacket time spent, and the quality of raw material and catalyzer is than ratio:
Stearic acid: calcium hydroxide: ammoniacal liquor: water=500:76:10:4000.
6. the production method of a kind of calcium stearate according to claim 1 is characterized in that: the described ammonium stearate that generates with ammoniacal liquor and stearic acid reaction plays catalyst action, and the cyclic water jacket time spent is arranged, and the quality of raw material and catalyzer is than ratio:
Stearic acid: calcium hydroxide: ammoniacal liquor: water=500:73:10:4000.
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|---|---|---|---|
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012104020058A CN102875356A (en) | 2012-10-22 | 2012-10-22 | Calcium stearate production method |
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| Publication Number | Publication Date |
|---|---|
| CN102875356A true CN102875356A (en) | 2013-01-16 |
Family
ID=47476918
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105086418A (en) * | 2015-07-31 | 2015-11-25 | 苏州天健竹业科技有限公司 | Weather resistance composite material for outdoor fitness facility and preparation method thereof |
| CN106565461A (en) * | 2016-11-03 | 2017-04-19 | 南阳仁创砂业科技有限公司 | Preparation of superfine calcium stearate and application of calcium stearate in precoated sand |
| CN109180465A (en) * | 2018-09-21 | 2019-01-11 | 南通诺佰恩化工科技有限公司 | A kind of preparation process of calcium stearate |
| CN109206037A (en) * | 2018-09-28 | 2019-01-15 | 镇江苏博特新材料有限公司 | The surface treatment method and cement base water-permeable brick surface layer of clay brick recycled fine aggregate |
| CN110699163A (en) * | 2019-09-04 | 2020-01-17 | 上海东升新材料有限公司 | Water-based calcium stearate dispersion liquid and preparation method thereof |
| CN112321415A (en) * | 2020-09-30 | 2021-02-05 | 南通新邦化工科技有限公司 | Calcium stearate static eliminating method and device |
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| US5356544A (en) * | 1992-09-06 | 1994-10-18 | Electrochemical Industries (Frutarom) Ltd. | Method for the preparation of metal soap aqueous dispersions |
| CN101117312A (en) * | 2006-08-04 | 2008-02-06 | 李兰生 | Method for producing calcium stearate by non-discharge one-step synthesis process |
| CN101353300A (en) * | 2008-07-30 | 2009-01-28 | 如皋市双马化工有限公司 | Method for preparing calcium stearate by geoceric acid one-step synthesis |
-
2012
- 2012-10-22 CN CN2012104020058A patent/CN102875356A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5356544A (en) * | 1992-09-06 | 1994-10-18 | Electrochemical Industries (Frutarom) Ltd. | Method for the preparation of metal soap aqueous dispersions |
| CN101117312A (en) * | 2006-08-04 | 2008-02-06 | 李兰生 | Method for producing calcium stearate by non-discharge one-step synthesis process |
| CN101353300A (en) * | 2008-07-30 | 2009-01-28 | 如皋市双马化工有限公司 | Method for preparing calcium stearate by geoceric acid one-step synthesis |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105086418A (en) * | 2015-07-31 | 2015-11-25 | 苏州天健竹业科技有限公司 | Weather resistance composite material for outdoor fitness facility and preparation method thereof |
| CN106565461A (en) * | 2016-11-03 | 2017-04-19 | 南阳仁创砂业科技有限公司 | Preparation of superfine calcium stearate and application of calcium stearate in precoated sand |
| CN109180465A (en) * | 2018-09-21 | 2019-01-11 | 南通诺佰恩化工科技有限公司 | A kind of preparation process of calcium stearate |
| CN109206037A (en) * | 2018-09-28 | 2019-01-15 | 镇江苏博特新材料有限公司 | The surface treatment method and cement base water-permeable brick surface layer of clay brick recycled fine aggregate |
| CN110699163A (en) * | 2019-09-04 | 2020-01-17 | 上海东升新材料有限公司 | Water-based calcium stearate dispersion liquid and preparation method thereof |
| CN112321415A (en) * | 2020-09-30 | 2021-02-05 | 南通新邦化工科技有限公司 | Calcium stearate static eliminating method and device |
| CN112321415B (en) * | 2020-09-30 | 2023-04-28 | 南通新邦化工科技有限公司 | Method and device for eliminating static electricity of calcium stearate |
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Application publication date: 20130116 |