CN101811994A - Method for continuously drying sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry - Google Patents
Method for continuously drying sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry Download PDFInfo
- Publication number
- CN101811994A CN101811994A CN201010170791A CN201010170791A CN101811994A CN 101811994 A CN101811994 A CN 101811994A CN 201010170791 A CN201010170791 A CN 201010170791A CN 201010170791 A CN201010170791 A CN 201010170791A CN 101811994 A CN101811994 A CN 101811994A
- Authority
- CN
- China
- Prior art keywords
- sodium
- slurry
- olefin sulfonate
- fluidized
- aliphatic alcohol
- 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.)
- Pending
Links
Images
Abstract
The invention provides a method for continuously drying sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry with easy continuous processing and low cost. The method comprises the following steps of: inputting airflow at the temperature of between 70 and 180 DEG C into a fluidized bed dryer (5) to ensure that inert particles in the dryer are fluidized; preheating the measured sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry to the temperature of between 50 and 150 DEG C, and inputting the measured sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry into the fluidized bed dryer (5) in a pulsating flow mode; allowing the slurry to pass through a mesh distribution screen (6); rupturing the slurry into short columns; ,making the slurry fall into a fluidized bed layer of the dryer; fluidizing the slurry and the inertia particles, and drying the fluidized slurry and the inertia particles to obtain the material; separating the dried material from surfaces of the inert particles to form fine powder; discharging the fine powder from the top of the fluidized bed dryer along with air flow, and allowing the fine powder to enter a bag separator (7); and exhausting tail gas from the top of the bag separator, and outputting the product of fine powder from the lower part of the bag separator. The method is suitable for drying a surface active agent.
Description
Technical field
The present invention relates to the dry materials method, the method for particularly a kind of successive drying high density sodium alkyl sulfate, sodium olefin sulfonate.
Background technology
Sodium alkyl sulfate, sodium olefin sulfonate are anion surfactants, have good decontamination, foaming, emulsifying capacity, are widely used in daily-use chemical industry, industrial cleaning agent, in the products such as building materials whipping agent.Sodium alkyl sulfate is to be raw material with the Fatty Alcohol(C12-C14 and C12-C18), through SO
3Among sulfonation, the NaOH and etc. chemical reaction make liquiform product; And sodium olefin sulfonate is to be raw material with alkene, through SO
3Chemical reactions such as sulfonation, NaOH neutralization and hydrolysis make liquiform product.Aqueous sodium alkyl sulfate, sodium olefin sulfonate can make solid phase prod by suitable drying mode.Because aqueous sodium alkyl sulfate, sodium olefin sulfonate can progressively improve with its active matter content, apparent viscosity can sharply rise, the high viscosity of tens thousand of centipoises makes the conveying of high density liquiform product and use become very difficult, generally can not use active matter content to surpass 35% product for this reason.When producing the product of the sodium alkyl sulfate of solid form, sodium olefin sulfonate, usually also be to be about 35% lower concentration liquiform product with active matter content, the form by high tower spray drying makes.Such as, Japanese kokai publication sho 55-69698, spy open clear 53-39037, the disclosed manufacture method of Chinese ZL00131365.7.The problem of the maximum that these methods exist is, dry lower concentration material need evaporate a large amount of moisture, power consumption is big, efficient is low, simultaneously owing to can not solve the problem that powder is stained with sticking tower wall well, cause cannot be sustained power lifetime, and it is very difficult to be stained with the cleaning of sticking powder on the tower wall, washes away the material of clearing up with a large amount of hot water and also is difficult to recycling, serious and the contaminate environment of loss of material obviously is uneconomical and irrational.
In addition, also there are many reports to be to use the high concentration slurry of solid content 60～80% (weight), produce the product of solid form in spray-dired mode.Such as, Japanese kokai publication sho 54-106428, Chinese CN1680303A, No. 6140301 disclosed manufacture method of patent in Europe.Because high density sodium alkyl sulfate, sodium olefin sulfonate slurry have high apparent viscosity; the feasible stable very difficulty of carrying out to its atomizing; the instability of atomizing causes frequent deadlock to stop production, and it is very difficult that large-scale production becomes, the example that for this reason rarely has stable large-scale industrial to produce.
Also having report is the high concentration slurry that adopts moisture 20%～35% (weight), through the technology of film under vacuum successive drying.Report as Japanese kokai publication hei 2-222498, Chinese CN101456829A.Reported method, not only need baroque film under vacuum moisture eliminator, these machine rotatable parts are many and accuracy requirement is high, so equipment failure rate is higher, cost is also higher, and, because prepared is irregular laminar product, use for convenience, need solve by secondary processing, more loaded down with trivial details.
U.S. US5723433 discloses the mode with anion surfactants such as turbulent flow tubular drier (TTD) drying fatty acid methyl esters sodium sulfonates.This method is the preheating of at first material being pressurizeed, and after carrying out a vacuum flashing and remove part moisture by nozzle decompression again, carries out the two alternate turbulent heat transfers of material and steam again and further evaporate moisture in the material in straight tube, reaches final exsiccant purpose.Because the online detection of micro-moisture is the hang-up of fine solution not as yet in the international coverage in the tensio-active agent, this technology is difficult to realize effectively control automatically for this reason, so in actual applications, the turbulent pipe of turbulent flow tubular drier (TTD), flash tank etc. are located often to be stopped up by undried material and are forced to breaks in production.
Summary of the invention
The present invention will solve sodium alkyl sulfate, energy consumption for drying was big when solid phase prod was produced in the sodium olefin sulfonate slurry dehydration, continue processing difficulties, facility investment is big, problems such as production cost height, a kind of successive drying high density sodium alkyl sulfate of the present invention is provided for this reason, the method of sodium olefin sulfonate slurry, this method technical process is simple, rationally, the Energy Efficiency Ratio height, equipment manufacturing cost is low, the reliability height, but steady and continuous large-scale industrial production, this method adopt low temperature hot blast successive drying high density sodium alkyl sulfate, sodium olefin sulfonate slurry is produced corresponding finely powdered product.
For addressing the above problem, its special character of the technical solution used in the present invention is: employing comprises fresh feed pump, material preheater, the fluidized bed dryer of inert particle and the dehumidification system of cloth bag separator is housed, by gas blower and airheater 70～180 ℃ airflow is imported fluidized bed dryer, make the described inert particle fluidisation in the moisture eliminator; With the sodium alkyl sulfate after the metering, sodium olefin sulfonate slurry, carry in the pulsating flow mode with fresh feed pump and to pass through material preheater, be preheated to 50～150 ℃, in the input fluidized bed dryer, the material of input divides sheet by mesh, fragment into short cylinder, fall into the fluidized-bed layer of described moisture eliminator, the material of input is disperseed once more and be attached to the inert particle surface, be fluidized together with inert particle, be able to drying after material and the hot gas flow heat exchange, dry material is with the collision of inert particle, friction, coming off from the inert particle surface becomes fine powder, powder material is discharged from the fluidized bed dryer top with air-flow, enters cloth bag separator, under the induced draft fan effect, tail gas in the cloth bag separator is discharged from the top, and the fine powder of aggregation is by the bleeder valve output of bottom in the cloth bag separator.
The activity concentration of sodium alkyl sulfate or sodium olefin sulfonate is 60～85% in the described slurry.
The moisture content of dry back sodium alkyl sulfate, sodium olefin sulfonate is≤4%.
The carbonatoms of the alkyl or alkenyl of sodium alkyl sulfate of the present invention, sodium olefin sulfonate is 8～24; The alkyl or alkenyl of sodium alkyl sulfate, sodium olefin sulfonate be straight chain or side chain.
Described fluidized-bed is the inverted cone tubular preferably.
Described fresh feed pump is constituted by feed worm pump, snubber and reciprocation pump successively, makes described slurry enter fluidized bed dryer with pulsation shape flow pattern.
The present invention adopts inert particle fluidized-bed dryer to carry out drying, this moisture eliminator is to add inert particle in common fluidized bed dryer, during work, the hot gas flow of input is gone into the fluidisation bed by gas distribution grid is laggard, and the inert particle in the bed enters fluidized state under the effect of air-flow; Slurry input to be dried divides sheet to become short strip shape to extrude by mesh, falls into fluidized-bed layer, disperseed once more and be attached to inert particle surface and inert particle fluidisation together, and transmitted with hot gas flow generation heat, moisture in the material is transferred in the air-flow, and material is able to drying.The exsiccant material collides mutually with inert particle and rubs, from the particle surface powder of detached, after the material that comes off is fluidized particle continuation dispersion and fining, discharge from the fluidized bed dryer top with air-flow, enter cloth bag separator, under the induced draft fan effect, the tail gas in the cloth bag separator is discharged from the top, and the fine powder of aggregation is by the bleeder valve output of bottom in the cloth bag separator.
The present invention can work continuously.Slurry after the metering of the present invention is meant the slurry by under meter.
Fresh feed pump of the present invention makes slurry import in the pulsating flow mode by spiral pump and reciprocation pump combination, divides the sheet disposed slurry to fall into fluidized-bed layer with short cylinder by mesh.
It is 60～85% high density sodium alkyl sulfate or sodium olefin sulfonate slurry that the present invention should adopt activity concentration.The present invention is with slurry to be dried dispersive mode in two steps, and the first step is that slurry is imported with pulse mode, divide sheet by mesh after, fragment into short cylinder and be dispersed, second step was that the short cylinder material is dispersed in fluidized-bed layer.So, both avoided the difficult point that high density sodium alkyl sulfate, sodium olefin sulfonate slurry are difficult to continual and steady atomizing, can prevent again the high viscosity slurry enter fluidized-bed layer after inter-adhesive uniting cause the dead bed of fluidized-bed.Slurry is carried with pulse mode, and by rupturing behind the net distribution cover, this disperses very important for the first time, and it is to disperse smooth prerequisite and assurance for the second time.The pulsation frequency of delivery of material is 1～20 time/second, preferred 5～10 times/second.The realization that pulsation is carried can have various ways, remove the implementation that the present invention adopts with spiral pump-reciprocation pump combination, also can substitute above-mentioned corresponding pump type and make up by identical toothed gear pump, the surge pump of use principle, can also use spiral pump, toothed gear pump separately, and the form that drives with pulsafeeder realizes.
The sodium alkyl sulfate of the dried finely powdered of the present invention, sodium olefin sulfonate, its moisture content is≤4%, be preferably≤2.5%.
The carbonatoms of the alkyl or alkenyl of sodium alkyl sulfate of the present invention, sodium olefin sulfonate is 8～24, is preferably 12～18, more preferably 12～14.
Inert particle of the present invention can be to make with the mixtures a kind of or more than two kinds in the materials such as glass, quartz, crystal, pottery, aluminum oxide, zirconium white, agate, tetrafluoroethylene, also can adopt the mixing of various material particle, particle is preferably sphere or almost spherical, diameter is 1～5mm, preferred 2～3mm.During operation, inert particle is fluidized state under the hot blast airflow effect of input, its effect is, breaks up the short cylinder material of input, makes material be attached to fluidized bed surface, be able to drying with the hot gas flow heat exchange, and efflorescence, come off, besides, to the collision of fluidized-bed barrel with wash away, played the effect of cleaning barrel, avoided material to adhere to barrel and be heated for a long time and decompose.
The hot blast grid distributor of fluidized bed dryer of the present invention bottom has adopted stamping forming jet tray, both can improve fluid effect, reduce and leak material, can conveniently empty bed again when stopping.
The present invention is because to discharge in the tail gas of fluidized bed dryer moisture content few and temperature is low, so adopted this unpack format efficiently of cloth bag separator to handle tail gas, thereby thoroughly to have solved be in the high tower spray drying mode of raw material with the lower concentration slurry, because the temperature of tail gas is high and wherein contain a large amount of moisture, can only use cyclonic separator and can not use cloth bag separator, cause the tail gas separating effect not good enough, product yield is on the low side, problems such as the dust polluting environment of carrying secretly in the tail gas.
The present invention also is:
1. utilize the sodium alkyl sulfate of high density, the characteristic of sodium olefin sulfonate material and the effect of inert particle, adopt the mode of dispersed material in two steps, both avoided the difficult point that high density sodium alkyl sulfate, sodium olefin sulfonate material are difficult to continual and steady atomizing, can guarantee the viscous material fracture again, prevent that inter-adhesive uniting from causing the dead bed of fluidized-bed, thereby realized high density sodium alkyl sulfate, sodium olefin sulfonate are carried out highly effective drying.
2. for high tower spray drying, inert particles fluidized bed of the present invention has used cryogenic hot blast, has avoided the risk of material pyrolytic decomposition.
3. because the inert particle that is fluidized to the continuous collision of fluidized-bed barrel with wash away, has played the effect of cleaning barrel, avoided material to stick on the barrel and decomposed because of being heated for a long time, thus continuous and stable production for a long time.
4. adopt water content to compare up to 60～65% raw material with high tower spray drying, the raw material water content that the present invention adopts is much lower, and dry power consumption significantly reduces, and energy-saving effect is remarkable.
5. inert particle fluidized-bed dryer average volume heat transfer coefficient height is about 20 times of high tower spray drying, the volume of the equipment of same steam capability, and the former has only the latter's 1/20.Equipment manufacturing cost is low for this reason, and floor space is little, has reduced investment and production cost significantly.
Since in the fluidized-bed discharge tail gas moisture content few and temperature is low, so adopted this unpack format efficiently of cloth bag separator to handle tail gas, with tail gas in the high tower spray drying mode because temperature is high and its washiness, can only use cyclonic separator to compare, solve problems such as tail gas inferior separating effect, product yield are low, dust polluting environment.
7. dry solid fatty alcohol sodium sulfate, the sodium olefin sulfonate of producing of the present invention is the finely powdered product, compare with the dust product of the hollow bead shape produced of high tower since pellet density the former increase to some extent than the latter, so the former solvability also is better than the latter.
The present invention need not material to be dried is atomized, and can stablize, reliably and efficiently successive drying high density sodium alkyl sulfate, sodium olefin sulfonate slurry, produces corresponding finely powdered product.Avoid the material pyrolytic decomposition simultaneously, improve dry heat efficient, guarantee quality product.
Description of drawings
Fig. 1 is an equipment used synoptic diagram of the present invention.
Be labeled as among the figure: 1 spiral pump, 2 snubbers, reciprocation pump, 4 material preheaters, 5 fluidized bed dryers, 6 mesh covers, 7 cloth bag separators, 8 bleeder valves, 9 induced draft fans, 10 gas blowers, 11 airheaters.
Embodiment
Embodiment 1: be 75% C with active matter content
12-14Be preheated to 75 ℃ after the sodium alkyl sulfate metering, send into inert particle fluidized-bed dryer 5 with 3 combinations of spiral pump 1-reciprocation pump continuously with pulse mode, after dividing sheet 6, the mesh that material distributes by multiple spot in the moisture eliminator is broken into the short cylindrical shape, the inert particle that the short cylindrical shape material that enters fluidized-bed layer is in fluidized immediately again further disperses, wet stock after the dispersion and inert particle coexistence are under fluidized state, the temperature that wet stock is entered by the bottom by 100 ℃ hot blast drying, dried material becomes finely powdered under the collision of inert particle and rubbing effect, dried fine powder is taken out of by tail gas immediately and is entered cloth bag separator, tail gas is discharged from cloth bag separator top under induced draft fan 9 effects, the fine powder that cloth bag separator is collected is discharged by bleeder valve 8, obtains water content and is about 2% C
12-14Sodium alkyl sulfate finely powdered product.
Embodiment 2: be 60% C with active matter content
16-18Be preheated to 70 ℃ after the sodium alkyl sulfate metering, with spiral pump 1---reciprocation pump 3 combinations are sent into inert particle fluidized-bed dryer 5 continuously with pulse mode, after dividing sheet 6, the mesh that material distributes by multiple spot in the moisture eliminator is broken into the short cylindrical shape, the inert particle that the short cylindrical shape material that enters fluidized-bed layer is in fluidized immediately again further disperses, wet stock after the dispersion and inert particle coexistence are under fluidized state, the temperature that wet stock is entered by the bottom by 90 ℃ hot blast drying, dried material becomes finely powdered under the collision of inert particle and rubbing effect, dried fine powder is taken out of by tail gas immediately and is entered cloth bag separator, tail gas is discharged from cloth bag separator top under induced draft fan 9 effects, the fine powder that cloth bag separator is collected is discharged by bleeder valve 8, obtains water content and is about 2.5% C
16-18Sodium alkyl sulfate finely powdered product.
Embodiment 3: be 70% C with active matter content
14-18Be preheated to 150 ℃ after the sodium olefin sulfonate metering, send into inert particle fluidized-bed dryer with spiral pump-reciprocation pump combination continuously with pulse mode, after dividing sheet, the mesh that material distributes by multiple spot in the moisture eliminator is broken into the short cylindrical shape, the inert particle that the short cylindrical shape material that enters fluidized-bed layer is in fluidized immediately again further disperses, wet stock after the dispersion and inert particle coexistence are under fluidized state, the temperature that wet stock is entered by the bottom by 180 ℃ hot blast drying, dried material becomes finely powdered under the collision of inert particle and rubbing effect, dried fine powder is taken out of by tail gas immediately and is entered cloth bag separator, tail gas is discharged from cloth bag separator top under the induced draft fan effect, the fine powder that cloth bag separator is collected is discharged by bleeder valve, obtains water content and is about 3% C
14-18Sodium olefin sulfonate finely powdered product.
Embodiment 4: be 85% C with active matter content
8-14Be preheated to 50 ℃ after the sodium alkyl sulfate metering, send into inert particle fluidized-bed dryer with spiral pump-reciprocation pump combination continuously with pulse mode, after dividing sheet, the mesh that material distributes by multiple spot in the moisture eliminator is broken into the short cylindrical shape, the inert particle that the short cylindrical shape material that enters fluidized-bed layer is in fluidized immediately again further disperses, wet stock after the dispersion and inert particle coexistence are under fluidized state, the temperature that wet stock is entered by the bottom by 70 ℃ hot blast drying, dried material becomes finely powdered under the collision of inert particle and rubbing effect, dried fine powder is taken out of by tail gas immediately and is entered cloth bag separator, tail gas is discharged from cloth bag separator top under induced draft fan 9 effects, the fine powder that cloth bag separator is collected is discharged by bleeder valve, obtains water content and is about 1.5% C
8-14Sodium alkyl sulfate finely powdered product.
Claims (7)
1. the method for a continuously drying sodium aliphatic alcohol sulfate, sodium olefin sulfonate slurry, it is characterized in that: employing comprises fresh feed pump, material preheater (4), the fluidized bed dryer (5) of inert particle and the dehumidification system of cloth bag separator (7) is housed, by gas blower and airheater 70～180 ℃ airflow is imported fluidized bed dryer, make the described inert particle fluidisation in the moisture eliminator; With the sodium alkyl sulfate after the metering, sodium olefin sulfonate slurry, carry by material preheater (4) in the pulsating flow mode with fresh feed pump, be preheated to 50～150 ℃, in the input fluidized bed dryer (5), the material of input divides sheet (6) by mesh, fragment into short cylinder, fall into the fluidized-bed layer of described moisture eliminator, the material of input is disperseed once more and be attached to the inert particle surface, be fluidized together with inert particle, be able to drying after material and the hot gas flow heat exchange, dry material is with the collision of inert particle, friction, coming off from the inert particle surface becomes fine powder, powder material is discharged from the fluidized bed dryer top with air-flow, enters cloth bag separator (7), under induced draft fan (9) effect, tail gas in the cloth bag separator is discharged from the top, and the fine powder of aggregation is by bleeder valve (8) output of bottom in the cloth bag separator.
2. the method for a continuously drying sodium aliphatic alcohol sulfate according to claim 1, sodium olefin sulfonate slurry is characterized in that the activity concentration of sodium alkyl sulfate in the described slurry or sodium olefin sulfonate is 60～85%.
3. the method for a kind of continuously drying sodium aliphatic alcohol sulfate according to claim 1, sodium olefin sulfonate slurry is characterized in that the moisture content of dry back sodium alkyl sulfate, sodium olefin sulfonate is≤4%.
4. the method for a kind of continuously drying sodium aliphatic alcohol sulfate according to claim 1, sodium olefin sulfonate slurry, the carbonatoms that it is characterized in that the alkyl or alkenyl of sodium alkyl sulfate, sodium olefin sulfonate is 8～24.
5. the method for a kind of continuously drying sodium aliphatic alcohol sulfate according to claim 1, sodium olefin sulfonate slurry, the alkyl or alkenyl that it is characterized in that sodium alkyl sulfate, sodium olefin sulfonate be straight chain or side chain.
6. the method for a kind of continuously drying sodium aliphatic alcohol sulfate according to claim 1, sodium olefin sulfonate slurry is characterized in that described fluidized-bed is the inverted cone tubular.
7. the method for a kind of continuously drying sodium aliphatic alcohol sulfate according to claim 1, sodium olefin sulfonate slurry, it is characterized in that described fresh feed pump is constituted by spiral pump (1), snubber (2) and reciprocation pump (3) successively, make described slurry enter fluidized bed dryer with pulsation shape flow pattern.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010170791A CN101811994A (en) | 2010-05-12 | 2010-05-12 | Method for continuously drying sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010170791A CN101811994A (en) | 2010-05-12 | 2010-05-12 | Method for continuously drying sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101811994A true CN101811994A (en) | 2010-08-25 |
Family
ID=42619380
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010170791A Pending CN101811994A (en) | 2010-05-12 | 2010-05-12 | Method for continuously drying sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101811994A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104807346A (en) * | 2015-04-30 | 2015-07-29 | 云南创森环保科技有限公司 | Powdery material cooling system |
| CN105254540A (en) * | 2015-10-30 | 2016-01-20 | 嘉兴赞宇科技有限公司 | Preparation method and device for powdery fatty acid methyl ester sodium sulfonate |
| CN105413210A (en) * | 2015-12-30 | 2016-03-23 | 江苏丰益化工科技有限公司 | Drying device used for powdery surfactant and drying method |
| CN107033036A (en) * | 2017-04-21 | 2017-08-11 | 江苏丰益化工科技有限公司 | A kind of drying system and method for lauryl sodium sulfate |
| CN107308882A (en) * | 2017-06-09 | 2017-11-03 | 常州大学 | A kind of preparation method of K12 pulvis surfactant |
| CN109210870A (en) * | 2018-09-06 | 2019-01-15 | 浙江工业大学 | A kind of back-shaped inert particles fluidized bed drying equipment and its drying means |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1680303A (en) * | 2005-01-14 | 2005-10-12 | 中轻物产浙江化工有限公司 | Production of granular dodecyl-sodium sulfate |
| CN101456829A (en) * | 2008-12-28 | 2009-06-17 | 浙江赞宇科技股份有限公司 | Dry process of dodecyl sodium sulfate |
-
2010
- 2010-05-12 CN CN201010170791A patent/CN101811994A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1680303A (en) * | 2005-01-14 | 2005-10-12 | 中轻物产浙江化工有限公司 | Production of granular dodecyl-sodium sulfate |
| CN101456829A (en) * | 2008-12-28 | 2009-06-17 | 浙江赞宇科技股份有限公司 | Dry process of dodecyl sodium sulfate |
Non-Patent Citations (1)
| Title |
|---|
| 刘巍等: "洗衣粉悬浮液在惰性粒子流化床中干燥的研究", 《日用化学工业》 * |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104807346A (en) * | 2015-04-30 | 2015-07-29 | 云南创森环保科技有限公司 | Powdery material cooling system |
| CN105254540A (en) * | 2015-10-30 | 2016-01-20 | 嘉兴赞宇科技有限公司 | Preparation method and device for powdery fatty acid methyl ester sodium sulfonate |
| CN105254540B (en) * | 2015-10-30 | 2017-03-22 | 嘉兴赞宇科技有限公司 | Preparation method and device for powdery fatty acid methyl ester sodium sulfonate |
| CN105413210A (en) * | 2015-12-30 | 2016-03-23 | 江苏丰益化工科技有限公司 | Drying device used for powdery surfactant and drying method |
| CN105413210B (en) * | 2015-12-30 | 2017-05-17 | 江苏丰益化工科技有限公司 | Drying device used for powdery surfactant and drying method |
| CN107033036A (en) * | 2017-04-21 | 2017-08-11 | 江苏丰益化工科技有限公司 | A kind of drying system and method for lauryl sodium sulfate |
| CN107033036B (en) * | 2017-04-21 | 2019-08-16 | 江苏丰益化工科技有限公司 | A kind of drying system and method for lauryl sodium sulfate |
| CN107308882A (en) * | 2017-06-09 | 2017-11-03 | 常州大学 | A kind of preparation method of K12 pulvis surfactant |
| CN109210870A (en) * | 2018-09-06 | 2019-01-15 | 浙江工业大学 | A kind of back-shaped inert particles fluidized bed drying equipment and its drying means |
| CN109210870B (en) * | 2018-09-06 | 2023-11-28 | 浙江工业大学 | Drying equipment and drying method for annular inert particle fluidized bed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101811994A (en) | Method for continuously drying sodium aliphatic alcohol sulfate and sodium olefin sulfonate slurry | |
| CN102274703A (en) | Large-scale continuous energy-saving fluidized bed spraying, granulating and drying process | |
| CN111928578A (en) | Drying process for salt and saltpeter materials | |
| CN203061148U (en) | Powder extruding granulating system capable of continuous automatic production | |
| CN105413210A (en) | Drying device used for powdery surfactant and drying method | |
| CN100368282C (en) | Sodium percarbonate dry method granulation processes and apparatus thereof | |
| JP2007285619A (en) | Spray drying device and spray drying method | |
| CN102051287A (en) | Method and equipment for preparing washing powder | |
| CN201565289U (en) | Large-sized spraying and granulating fluidized bed dryer | |
| CN103773618B (en) | Process and device for continuously preparing powdery washing powder particles | |
| CN106563390A (en) | Dry-process ceramic wall and ground tile green body powder granulation technology | |
| CN206184393U (en) | Powder material non -slurry pelletizing equipment | |
| CN101302123A (en) | Large size particle urea composite rotary drum prilling process and equipment | |
| CN106422966A (en) | Powdery material dry granulation equipment | |
| CN109718597B (en) | Preparation method of filter material for roller kiln dust removal | |
| CN104492348A (en) | Fluidized bed used for preparing granular pills | |
| CN104014277A (en) | Fluid bed granulating drying process | |
| CN111001353A (en) | Vacuum spray fluidization granulator | |
| CN216024528U (en) | Powder mixing device utilizing airflow | |
| CN112742185A (en) | Flue gas desulfurization reactor, flue gas treatment system and process method | |
| CN105254540B (en) | Preparation method and device for powdery fatty acid methyl ester sodium sulfonate | |
| CN204281866U (en) | The device of commercial auxiliaries is prepared in a kind of electrostatic acid | |
| CN100487066C (en) | Drying coating technology for sodium percarbonate | |
| CN104451714B (en) | Production process and production device for preparing industrial additives from electrostatic acid and application thereof | |
| CN217409755U (en) | Produce yeast concentrate drying tower rich in powder |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20100825 |