CN101607881B - Dry production technique and device of calcium stearate - Google Patents
Dry production technique and device of calcium stearate Download PDFInfo
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- CN101607881B CN101607881B CN200910304505A CN200910304505A CN101607881B CN 101607881 B CN101607881 B CN 101607881B CN 200910304505 A CN200910304505 A CN 200910304505A CN 200910304505 A CN200910304505 A CN 200910304505A CN 101607881 B CN101607881 B CN 101607881B
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- calcium stearate
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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 30
- 239000008116 calcium stearate Substances 0.000 title claims abstract description 30
- 235000013539 calcium stearate Nutrition 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title abstract description 15
- 238000006243 chemical reaction Methods 0.000 claims abstract description 68
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 36
- QIQXTHQIDYTFRH-UHFFFAOYSA-N octadecanoic acid Chemical compound CCCCCCCCCCCCCCCCCC(O)=O QIQXTHQIDYTFRH-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000003756 stirring Methods 0.000 claims abstract description 8
- 238000005516 engineering process Methods 0.000 claims description 19
- 239000008367 deionised water Substances 0.000 claims description 14
- 229910021641 deionized water Inorganic materials 0.000 claims description 14
- 239000011575 calcium Substances 0.000 claims description 11
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims description 10
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 claims description 8
- 229910052791 calcium Inorganic materials 0.000 claims description 8
- 239000000498 cooling water Substances 0.000 claims description 8
- 150000001875 compounds Chemical class 0.000 claims description 7
- 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
- 239000000292 calcium oxide Substances 0.000 claims description 5
- 235000012255 calcium oxide Nutrition 0.000 claims description 5
- 238000010008 shearing Methods 0.000 claims description 4
- 238000009434 installation Methods 0.000 claims description 3
- 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 9
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 230000005540 biological transmission Effects 0.000 abstract 2
- 239000003638 chemical reducing agent Substances 0.000 abstract 2
- 235000021355 Stearic acid Nutrition 0.000 abstract 1
- 229940043430 calcium compound Drugs 0.000 abstract 1
- 150000001674 calcium compounds Chemical class 0.000 abstract 1
- 230000007547 defect Effects 0.000 abstract 1
- OQCDKBAXFALNLD-UHFFFAOYSA-N octadecanoic acid Natural products CCCCCCCC(C)CCCCCCCCC(O)=O OQCDKBAXFALNLD-UHFFFAOYSA-N 0.000 abstract 1
- 239000008117 stearic acid Substances 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
- 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
- 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
- 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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Abstract
The invention discloses a dry production technique of calcium stearate, which comprises the following steps of: adding stearic acid, calcium compound and water in a reacting device according to the weight ratio of 82-88 percent to 10-15 percent to 2-5 percent, and stirring at the temperature of 80 to 150 DEG C under the pressure of 0 to 0.10 MPa for reaction for 1 to 5 hours, thus obtaining the calcium stearate. The reacting device is characterized in that a motor (1) is connected with a speed reducer (2), and the speed reducer (2) is connected with a gear transmission (3); the gear transmission (3) is connected with a stirrer (9) arranged in a reactor (4); a temperature detecting port (5) and a feeding port (6) are arranged above the reactor (4); a clamping sleeve (8) is arranged outside the reactor (4); and a discharge hole (10) is arranged below the reactor (4). The technique simplifies the operation procedures, reduces cost and energy consumption, reduces discharge of waste water, lowers pollution control cost, further reduces influence on environment and overcomes the defects of the traditional wet production technique of calcium 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, like 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 in water medium, to produce, 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 is prone to pass strainer, the situation that causes waste water COD and suspended substance to exceed standard.Therefore, this technology pollution treatment appropriate litigation fees is high.
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 Triple Pressed 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 quicklime 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 whisking appliance 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.
Whisking appliance is 2, and reverse the shearing rotated 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 step is few, and operational path is short:
The traditional wet 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 great 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 filter to do the 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.At least contain the moisture content more than 50% through in the material of filter dehydration, must be dry in moisture eliminator, also want the heat energy of labor; And deposit seeds is little, dispersity is high, surface adsorption is strong, causes the filter cake moisture content high, 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 practice thrift mass energy consumption.The by product of reaction process is a water, need not to wash, and does not almost have the spent process water 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 mikrobe that possibly in raw material, survive originally will lose activity fully, in fact play calcium stearate is played the sterilization and disinfection effect.
3, calcium hydroxide and Triple Pressed 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 whisking appliance of rotation, makes the reaction of calcium hydroxide and Triple Pressed 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, can the deionized water that add in the reaction be discharged with 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 Triple Pressed Stearic Acid and metallic compound reactions step are 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, has saved operations such as press filtration, washing, drying, has 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 great amount of wastewater, per tonly reduced by 50 tons of waste water, can practice thrift 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 reverse shearing of pair slurry rotated, 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, whisking appliance; 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 Triple Pressed Stearic Acid, 15 kilograms of deionized waters.
At first Triple Pressed Stearic Acid is dropped in the reaction vessels 4 through charging opening 6, about heated and stirred 10min, treat that temperature is raised to 50 ℃ after; With the calcium hydroxide input; Fully stir the back and pour the deionized water of 15kg into, constantly feed nitrogen, the air in the reaction vessel 4 is discharged from top feeding mouth 6 through gas inlet and outlet piping mouth 7 from opening for feed; 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 vp 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 quicklime, 285 kilograms of Triple Pressed Stearic Acid, 12 kilograms of deionized waters.
At first quicklime is dropped in the reaction vessel 4 through charging opening 6; Stir and the adding deionized water; Treat to drop into Triple Pressed Stearic Acid after quicklime and water react completely, constantly feed nitrogen, the air in the reactor drum 4 is discharged from top feeding mouth 6 through gas inlet and outlet piping mouth 7; After progressively the air displacement in the reactor drum 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 vp that deionized water in the maintenance reactor drum 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: like Fig. 1, shown in 2; This reaction unit comprises reaction vessel 4, charging opening 6 and chuck 8, and motor 1 is connected with speed reduction unit 2, and speed reduction unit 2 is connected with gear-shift mechanism 3; Gear-shift mechanism 3 is connected with the whisking appliance 9 of installation in the reaction vessel 4; Whisking appliance 9 is 2, and reverse the shearing rotated 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, and 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 through steam or water coolant.
Claims (7)
1. the technology of a dry production calcium stearate; It is characterized in that: the compound of Triple Pressed 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; Described reaction unit is the horizontal reacting device; It 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), and gear-shift mechanism (3) is connected with the whisking appliance (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); Whisking appliance (9) is 2, and reverse the shearing rotated.
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 quicklime.
6. the technology of dry production calcium stearate according to claim 1 is characterized in that: reaction vessel (4) top is provided with temperature-measuring port (5).
7. the technology of dry production calcium stearate according to claim 1 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 |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910304505A CN101607881B (en) | 2009-07-17 | 2009-07-17 | Dry production technique and device of calcium stearate |
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| CN101607881A CN101607881A (en) | 2009-12-23 |
| CN101607881B true CN101607881B (en) | 2012-10-03 |
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| CN200910304505A Active CN101607881B (en) | 2009-07-17 | 2009-07-17 | Dry production technique and device of calcium stearate |
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| CN (1) | CN101607881B (en) |
Families Citing this family (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 |
| CN103526624B (en) * | 2013-10-22 | 2015-01-07 | 湖州市菱湖新望化学有限公司 | Method for preparing microcrystalline cellulose and reaction equipment of microcrystalline cellulose |
| 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 |
| 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 |
| 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 |
| 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 |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
-
2009
- 2009-07-17 CN CN200910304505A patent/CN101607881B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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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Denomination of invention: Dry production technique and device of calcium stearate Effective date of registration: 20170810 Granted publication date: 20121003 Pledgee: Bank of Huzhou Limited by Share Ltd West Branch Pledgor: Huzhou Linghu Xinwang Chemical Co., Ltd. Registration number: 2017990000736 |
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Denomination of invention: Dry production technique and device of calcium stearate Effective date of registration: 20180731 Granted publication date: 20121003 Pledgee: Bank of Huzhou Limited by Share Ltd Pledgor: Huzhou Linghu Xinwang Chemical Co., Ltd. Registration number: 2018110000018 |
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Denomination of invention: Dry production technique and device of calcium stearate Effective date of registration: 20190730 Granted publication date: 20121003 Pledgee: Bank of Huzhou Limited by Share Ltd Pledgor: Huzhou Linghu Xinwang Chemical Co., Ltd. Registration number: 2019990000806 |
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Date of cancellation: 20200724 Granted publication date: 20121003 Pledgee: Bank of Huzhou Limited by Share Ltd. Pledgor: HUZHOU CITY LINGHU XINWANG CHEMICAL Co.,Ltd. Registration number: 2019990000806 |
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Denomination of invention: A process and device for dry production of calcium stearate Effective date of registration: 20200818 Granted publication date: 20121003 Pledgee: Bank of Huzhou Limited by Share Ltd. Pledgor: HUZHOU CITY LINGHU XINWANG CHEMICAL Co.,Ltd. Registration number: Y2020990000985 |
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Date of cancellation: 20210816 Granted publication date: 20121003 Pledgee: Bank of Huzhou Limited by Share Ltd. Pledgor: HUZHOU CITY LINGHU XINWANG CHEMICAL Co.,Ltd. Registration number: Y2020990000985 |
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Denomination of invention: A process and device for producing calcium stearate by dry method Effective date of registration: 20210816 Granted publication date: 20121003 Pledgee: Bank of Huzhou Limited by Share Ltd. Pledgor: HUZHOU CITY LINGHU XINWANG CHEMICAL Co.,Ltd. Registration number: Y2021990000725 |