CN1094383C - Spraying-fluidized bed prilling method for precipitation of hydrated silicon dioxide - Google Patents
Spraying-fluidized bed prilling method for precipitation of hydrated silicon dioxide Download PDFInfo
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- CN1094383C CN1094383C CN98112245A CN98112245A CN1094383C CN 1094383 C CN1094383 C CN 1094383C CN 98112245 A CN98112245 A CN 98112245A CN 98112245 A CN98112245 A CN 98112245A CN 1094383 C CN1094383 C CN 1094383C
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- silicon dioxide
- precipitated hydrated
- bed
- hydrated silicon
- fluidized bed
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Abstract
The present invention discloses a method for granulating precipitated hydrated silicon dioxide. The present invention is characterized in that a filtered and washed precipitated hydrated silicon dioxide filter cake is beaten into slurry; the slurry is sprayed onto a gas-solid fluidized bed, is dried and granulated simultaneously. The mean grain size of the product is from 0.4mm to 0.6mm.
Description
The invention belongs to the prilling process of precipitated hydrated silica.
Precipitated hydrated silica is commonly called as white carbon, is widely used in aspects such as rubber, papermaking, agricultural chemicals, coating, paint, printing ink, adhesive.Since its good reinforcing rubber performance, rubber industry consumption maximum.Precipitated hydrated silica mixes rubber to carry out when mixing, and its profile is very big to mixing operating influence.It is slow to eat powder when powder product is mixing, and mixing time is long; Dust from flying is big, causes damage, and operating environment is worsened.And that granulation product is eaten powder is fast, and mixing time is short, dust from flying is few, has improved operating environment.
The production procedure of precipitated hydrated silica such as Fig. 1:
Through reaction, filter, the filter cake after the washing, moisturely be generally 80～85%, need drying to use as product.Main drying mode has at present: centrifugal spray-drying, press spray drying and rotary flashing drying.Obtained product with these drying modes and be fine powder, particle diameter is less than 50 μ m.
The U.S. is special that the prilling process introduced of 4.336.219 is, in mixing screw, and with powdery precipitated hydrated silica and 33% ammonium stearate suspension mixing granulating, and then drying.The prilling process that Japan Patent 8256.314 is introduced is: with homogenizer filter cake (moisture 86%) pulp again after, in the high-pressure filteration machine with 30kg/cm
2Pressure dewaters, and the gained filter cake is moisture 72%, uses heated-air drying after will this filter cake pulverizing.The former is through twice drying, and the latter needs high-tension apparatus.
Prilling process of the present invention, be that moisture about 85% filter cake is broken into slurry, spray into gas then---solid fluid bed in, thermal current passes bed, the drop that sprays into is applied to the particle surface of fluidized-bed layer, the heat that receives bed heat and fluidizing agent makes water evaporates, and the solid of separating out grows up particle attached to particle surface.After perhaps drop-coated is distributed in particle surface, have little time drying and mutual bonding, particle is grown up.Do not reach after the drop that also has sprays into combine with solids promptly dry, this small-particle or raised to roll over and take out of, or be deposited in and become " seed " that new particle is grown up in the bed.
In bed, also exist opposite process simultaneously.Promptly because the passing through of fluidizing agent causes an interior particle to clash into mutually, and cold liquid sprays into the hott bed layer and makes particle inside generation thermal stress, makes particle fragmentation, and size reduces.
When growth rate in the bed equated with broken speed, the average-size of particle no longer changed and reaches a stationary value, and operation at this moment tends towards stability and can be continuous.Be that feed liquid constantly sprays into, the bed particle draws off in a certain stable dimensions scope continuously.
Characteristics of the present invention are dry and granulation is carried out simultaneously, and a step finishes.In granulation process, do not add any binding agent.Evaporated water only is a filter cake institute water content, and no extra moisture adds.
Fig. 1 is the flow sheet of precipitated hydrated silica.
Embodiment
The granulation white carbon of usefulness of getting up of packing in sieve plate plate body diameter is the fluid bed of 2.40m is sent into hot blast and is made it be in normal fluidized state.Spray into slip toward bed, keep 50～150 ℃ of bed temperature, be generally 60～120 ℃, treat discharging continuously behind the stable operation, per hour can protect product 50～100kg.
The product average grain diameter is 0.4～0.6mm, is lower than 15% less than the fine powder percentage by weight of 125 μ m particle diameters.
The powder time of normally eating of standard code precipitated hydrated silica is 18min, and I am 17min the powder time of eating of institute's powder product, and the powder time of eating of granulation product is 10min, shortens 7min than powder product, shortens 8min than standard.
Claims (5)
1, a kind of prilling process of precipitated hydrated silica; It is characterized in that this method is with the reaction of the weak solution of diluted acid and alkali silicate, be settled out hydration silica, after filtration, after the washing, filter cake breaks into slurry, sprays into gas---solid fluid bed in, thermal current passes through bed.
2, method according to claim 1 is characterized in that diluted acid can be the weak solution of sulfuric acid, hydrochloric acid, nitric acid, and carbon dioxide.
3, method according to claim 1 is characterized in that alkali silicate can be sodium metasilicate or potassium silicate.
4, method according to claim 1 is characterized in that the granulation of precipitated hydrated silica and drying carry out simultaneously.
5, method according to claim 1, the average grain diameter that it is characterized in that products obtained therefrom is 0.4～0.6mm, is lower than 15% less than the fine powder percentage by weight of 125 μ m particle diameters.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98112245A CN1094383C (en) | 1998-09-11 | 1998-09-11 | Spraying-fluidized bed prilling method for precipitation of hydrated silicon dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN98112245A CN1094383C (en) | 1998-09-11 | 1998-09-11 | Spraying-fluidized bed prilling method for precipitation of hydrated silicon dioxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1214957A CN1214957A (en) | 1999-04-28 |
| CN1094383C true CN1094383C (en) | 2002-11-20 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98112245A Expired - Fee Related CN1094383C (en) | 1998-09-11 | 1998-09-11 | Spraying-fluidized bed prilling method for precipitation of hydrated silicon dioxide |
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Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE102008035867A1 (en) * | 2008-08-01 | 2010-02-04 | Evonik Degussa Gmbh | Novel precipitated silicas for carrier applications |
| US10016734B2 (en) * | 2016-07-30 | 2018-07-10 | Ningbo Wanglong Tech Co.,Ltd | Method of producing potassium sorbate particles |
| CN111909619A (en) * | 2020-08-19 | 2020-11-10 | 马惠琪 | Production method of high-hardness silica sol for grinding and polishing |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056503A (en) * | 1990-04-27 | 1991-11-27 | 日本触媒化学工业株式会社 | The continuous prilling process and the device thereof of super absorbent resin powder |
| CN1155297A (en) * | 1994-08-05 | 1997-07-23 | 尤尼利弗公司 | Granulation in a fluidised bed |
| CN2258975Y (en) * | 1995-06-14 | 1997-08-06 | 蒋大洲 | Fluidized bed granulating drying apparatus |
| CN1182377A (en) * | 1995-04-21 | 1998-05-20 | 底古萨股份公司 | Process and device for producing granulates by fluidised-bed spray granulation |
-
1998
- 1998-09-11 CN CN98112245A patent/CN1094383C/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1056503A (en) * | 1990-04-27 | 1991-11-27 | 日本触媒化学工业株式会社 | The continuous prilling process and the device thereof of super absorbent resin powder |
| CN1155297A (en) * | 1994-08-05 | 1997-07-23 | 尤尼利弗公司 | Granulation in a fluidised bed |
| CN1182377A (en) * | 1995-04-21 | 1998-05-20 | 底古萨股份公司 | Process and device for producing granulates by fluidised-bed spray granulation |
| CN2258975Y (en) * | 1995-06-14 | 1997-08-06 | 蒋大洲 | Fluidized bed granulating drying apparatus |
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| Publication number | Publication date |
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| CN1214957A (en) | 1999-04-28 |
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