CN101829521A - Fluidized bed granulator - Google Patents
Fluidized bed granulator Download PDFInfo
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- CN101829521A CN101829521A CN 201010166803 CN201010166803A CN101829521A CN 101829521 A CN101829521 A CN 101829521A CN 201010166803 CN201010166803 CN 201010166803 CN 201010166803 A CN201010166803 A CN 201010166803A CN 101829521 A CN101829521 A CN 101829521A
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Abstract
The invention discloses a fluidized bed granulator, which relates to a device for grouting, granulating and drying crystal seeds. The fluidized bed granulator is provided with a nozzle and a discharge hole; the fluidized bed granulator is provided with an air distribution chamber, an air distribution net plate, an inner heating fluidizing chamber, a spray fluidizing chamber and a separation chamber in turn from the bottom to the top; the top of a bed body is provided with a dust discharge pipe, and the exterior of the bed body is provided with cyclone; the inner heating fluidizing chamber is provided with an inner heat exchanger; the nozzle is arranged in the spray fluidizing chamber or the separation chamber; the dust discharge pipe is connected with a cyclone inlet; the cyclone is communicated with a return port through a return upper section and a return lower section at the lower part in turn; and the return port is formed on the lateral surface of the fluidizing chamber and is not higher than the closest nozzle. The fluidized bed granulator does not produce large balls during working, can keep most material in the bed body and does not need to detach the nozzle during start and stop, can work in a small gas-liquid ratio without the interference of the nozzle and the discharge hole, increases the utilization rate of heat, and reduces the running cost.
Description
Technical field
The present invention relates to a kind of crystal seed be carried out slurry-spraying pelletizing, dry a kind of device, particularly continuous fluidized bed for spraying, granulating device.
Background technology
In the prior art, crystal seed is carried out the fluidized bed prilling apparatus of slurry-spraying pelletizing, drying, often the mode that adopts is by nozzle one or more liquid materials to be sprayed in the fluid bed that contains littler than the shot-like particle that will produce basically solid particle, volatile component in one or more raw materials that evaporation is sprayed into, crystal seed is infeeded fluid bed or/and generate crystal seed in fluid bed, and discharge shot-like particle from fluid bed.
This its normal configuration of class fluidized bed prilling device is that fluid bed has some unit fluidising chamber and plurality of separate chamber, separation chamber's correspondence one by one is arranged on unit fluidising chamber top, indoor at least one the mother liquor nozzle that is equipped with of unit fluidisation, being positioned at dividing plate below in the housing keeps at a certain distance away and is provided with split-wind plate, split-wind plate is provided with some wind hole, the separation chamber that is positioned at an end on the housing is provided with charging aperture, on the opposite side housing corresponding and be positioned at the split-wind plate upside and be provided with discharging opening with charging aperture, be positioned at the split-wind plate downside on the housing and be provided with inlet air plenum one to one with unit fluidising chamber, inlet air plenum links to each other with a hot blast import respectively, the corresponding unit air outlet that is provided with in housing top with each separation chamber, it is the spouted fluidized bed nodulizer of a plurality of spouted unit that a kind of technology is wherein arranged, its patent No. is ZL02131280.X, the spouted fluidized bed nodulizer of a plurality of spouted unit that the vertical clapboard in the housing constitutes, it is characterized in that, each spouted unit is by gas distribution grid, the plate center is provided with the drive nozzle of self-clean type or the two-fluid spray nozzle of self-clean type, and the guide shell formation that center line overlaps with nozzle centerline is set above nozzle.
This class fluidized bed prilling device weak point is following one or more aspects:
1, nozzle under or during side-lower, in continuous flow procedure, because particle can be long more big more under the effect of reunion or covering, can not seethe with excitement during to certain particle diameter, rest on the branch wind web plate, more near nozzle, under the effect of nozzle, look faster, even if adopted the method for forcing discharge, also might become the super large ball, produce not go down continuously until the dead bed of fluid bed;
2, nozzle under or side-lower, when shutting down, nozzle need split out or material in the fluid bed is all discharged, not so granule can enter in the nozzle, nozzle can not be worked during the next time start.
3, nozzle under or during side-lower, nozzle is to be embedded in work in the fluosolids fully, and fluosolids bottom pressure is bigger, is the nozzle reliably working, the atomizing space tolerance that needs is bigger, gas liquid ratio is normally between 1.5: 1～3: 1.
4, nozzle under or during side-lower, normal discharging opening also below, both have interference each other, the work of granulation is stablized in influence.
5, the origin of heat of evaporating volatile composition provides indirectly by wind entirely, and heat utilization efficiency is lower.
Summary of the invention
The objective of the invention is to propose a kind of fluidized bed pelletizer that can overcome above existing fluidized bed prilling device defective.
The present invention includes nozzle and discharging opening that a body is provided with, the bed body is provided with separating chamber from bottom to top successively, divide the wind web plate, the interior fluidising chamber of heating, spray-fluidized chamber and separation chamber, bed body top is provided with dust flue, the bed external body is provided with cyclone separator, heating fluidising chamber is provided with interior heat exchanger in it is characterized in that, described nozzle is arranged in spray-fluidized chamber or the separation chamber, the air outlet of described dust flue links to each other with the import of cyclone separator, the lower end of cyclone separator is successively by connecting the refeed line epimere, the refeed line hypomere links to each other with the returning charge mouth, heat the side of fluidising chamber or spray-fluidized chamber in described returning charge mouth is arranged on, and be not higher than the horizontal line at hithermost nozzle place.
So the present invention can not produce super large ball energy serialization production in the course of the work; when startup-shutdown, can preserve most material in the bed body and do not need to split out nozzle; and can carry out work with less gas liquid ratio; reduce the atomizing air consumption; nozzle and discharging opening do not disturb the functional reliability height, reduce the size of equipment after the increase heat utilization efficiency and reduce operating cost.
The technical scheme of further improvement of the present invention is:
Nozzle is installed in the side of spray-fluidized chamber, can realize inwardly spraying into from the side liquid material.
The level height that nozzle is installed 0～800mm800mm or down in the scope of 0～400mm on the horizontal line of spray-fluidized chamber and separation chamber's boundary realizes spraying from the top down.
For further reducing the small particles material that may contain in the discharging, discharging opening connects pneumatic separator, and described pneumatic separator is provided with pneumatic separator air inlet and pneumatic separator air outlet, and the air outlet of pneumatic separator is connected the separation chamber.Air velocity in the pneumatic separator should be greater than the air velocity in the fluidising chamber, like this, can make also in pneumatic separator, can being blown afloat, separate of in fluidising chamber, can not being blown afloat less than the particle of moulding, can advance one improve shaped granule all once, reduce the burden of follow-up solids management system, improve the finished product uniformity.
In order to make the material in the refeed line enter in the fluidising chamber smoothly, do not stop up refeed line, the material that returns does not lump when entering fluosolids, between cyclone separator and refeed line epimere the returning charge Blowing stopper is set, and is provided with ajutage between refeed line epimere and refeed line hypomere.Make the wind speed in the refeed line approach the finished particle sinking speed, and it is consistent that the wind direction of air-supply and returning charge in entering fluosolids are flowed to, the granule when adopting hot blast in all right further heat cycles return movement.
Heat exchanger is coil exchanger or plate type heat exchanger in said, improves the utilization rate of its indoor heat, and above-mentioned interior heat exchanger also can be provided with automatic thermal source control valve, regulates heat.
For finished particle is moved to discharging opening easily, divide the wind web plate to be obliquely installed to discharging opening, be lower than an end of charging aperture at an end of discharging opening, or be distributed with oblique hole on the wind web plate in horizontally disposed minute, can also be to adopt step structure, to the discharging opening overflow, when scurrying split-wind plate, wind had certain horizontal force, and can make the material particles overflow to discharging opening.
In order to replenish the crystal seed adding fluid bed that crystal seed maybe will be handled, fluid bed is provided with several charging apertures, the side of heating fluidising chamber in each charging aperture is arranged on.Realization adds the solid material and sprays into the continuous production of liquid material, and in order to allow the crystal seed that enters from the fluid bed outside better mix in fluidising chamber, in the dispersed range of atomization that enters nozzle, charging aperture is arranged on the side of fluidising chamber and is in the below of nozzle.
In order to realize continous way production better, fluidising chamber is divided into several unit fluidising chamber, the indoor longitudinal baffle that is provided with of heating clamber and spray-fluidized in described is provided with spacing between described longitudinal baffle and branch wind web plate and the bed body top.
Interior heat exchanger is 10～300mm with the vertical range of dividing the wind web plate; Nozzle distance above interior heat exchanger is 50～1000mm; The interior height of fluidising chamber that heats is at 200～2000mm; The height of spray-fluidized chamber is at 500～2000mm.
Bed body of the present invention is a metal structure, and bed body ground connection can effectively be eliminated the influence of static, and operation is produced safer.
Consider from overall structure, the present invention be advantageous in that following some:
Owing to interior heat exchanger is set in the fluidising chamber bottom, played the effect of barrier and heating, heat exchanger and branch wind web plate distance are shorter in adding, when fluidising air velocity is higher in the fluid bed, make that material presents complete particulate fluidization in the granulation process, greatly reduce turbulent and generation channeling, and bubble is less, heat exchange is more abundant between air and the material particles, more be difficult for adhesion between size particles, because usefulness is heated in the direct conduction of interior heat exchanger, equipment energy consumption reduces simultaneously, and operating cost reduces.
The present invention adopts arrangement of nozzles in spray-fluidized chamber and separation chamber, when bulky grain can not seethe with excitement, just can not rest in the range of atomization of nozzle, stop to grow up, always go out after long-time, avoided the generation of super large ball, so just can produce continuously from discharging opening.
Nozzle is arranged on spray-fluidized chamber sidewall; when in side direction, spraying; produce horizontal gas-liquid flow on fluidising chamber top; adopt cyclone separator that the granule material is circulated through continuous; and return in the fluid bed by fluidising chamber's side returning charge mouth of nozzle below; enter the gas-liquid flow district again after the dispersion through fluidisation material or interior heat exchanger; make granule coating or reunion uniformly; avoided size particles to mix when uneven that granule sticks to large particle surface in a large number under nozzle act; also very little as particle diameter, can be directly up, be difficult for and the bulky grain adhesion; granulation process is more stable, and nozzle quantity also can be still less simultaneously.Nozzle is arranged on top, spray-fluidized chamber, when spraying from the top down, produces above-mentioned effect equally
When nozzle is arranged on spray-fluidized chamber and separation chamber, the material bed pressure of nozzle exit is little, and goods fluid presents particulate fluidization, and it is stifled that jet expansion is difficult for, the atomizing space tolerance that needs so can reduce naturally, and the theoretical gas liquid ratio that calculates can drop to 0.3: 1～1: 1.
Discharging opening is arranged on the horizontal below of nozzle, does not disturb between the two, and both can steady operation.
In sum: fluidized bed pelletizer of the present invention does not have the super large ball to produce; can realize the quantity-produced purpose fully; can in fluid bed, keep most material during startup-shutdown and need not tear nozzle open; the atomizing air amount can reduce; discharging opening and nozzle operation reliability height, heat energy utilization rate height simultaneously.When discontinuous production, show superiority equally.
Description of drawings
Fig. 1 is the front schematic view of fluidized bed pelletizer of the present invention;
Fig. 2 is the side schematic view of Fig. 1;
Fig. 3 bows to schematic diagram for Fig. 1's;
Fig. 4 is the selection by winnowing structural representation of fluidized bed pelletizer of the present invention;
Fig. 5 is the blower structure schematic diagram of fluidized bed pelletizer of the present invention;
Fig. 6 is the another kind of front schematic view of fluidized bed pelletizer of the present invention;
Fig. 7 is the side schematic view of Fig. 6;
Fig. 8 is the third front schematic view of fluidized bed pelletizer of the present invention;
Fig. 9 is the side schematic view of Fig. 8.
Wherein: 1 is separating chamber, and 2 for dividing a wind web plate, and 3 is interior heating fluidising chamber, 4 is the spray-fluidized chamber, and 5 is the separation chamber, and 6 is dust flue, 7 is cyclone separator, and 8 is interior heat exchanger, and 9 is nozzle, 10 is the refeed line epimere, 11 are the returning charge mouth, and 12 is discharging opening, and 13 is pneumatic separator, 14 is the pneumatic separator air outlet, 15 are the returning charge Blowing stopper, and 16 is ajutage, and 17 is charging aperture, 18 is longitudinal baffle, 19 is the refeed line hypomere, and 20 is the pneumatic separator air inlet, and 21 is the hot blast import, 22 is the bed body, and 23 is the horizontal line of spray-fluidized chamber 4 and separation chamber's 5 boundary.
The specific embodiment
Shown in Fig. 1 to 5: this fluidized bed pelletizer is provided with nozzle 9, discharging opening 12; the fluid bed main body is followed successively by separating chamber 1 from down to up, divides wind web plate 2, interior heating fluidising chamber 3, spray-fluidized chamber 4, separation chamber 5; bed body top is provided with a plurality of dust flues 6, and the fluid bed main body is provided with cyclone separator 7 outward.In interior heating fluidising chamber 3, be provided with heat exchanger 8 in the shell and tube, in the side of spray-fluidized chamber 4 nozzle 9 is installed, in fluidising chamber, be provided with vertical dividing plate 18, heat the side of fluidising chamber 3 in returning charge mouth 11 is arranged on, and be not higher than the horizontal line at hithermost nozzle 9 places.The fluid bed main frame communicates by discharging opening 12 and pneumatic separator 13, pneumatic separator air outlet 14 is connected in separation chamber 5, dust flue 6 links to each other with the import of cyclone separator 7, cyclone separator 7 communicates with returning charge mouth 11 by returning charge Blowing stopper 15, refeed line epimere 10 and the refeed line hypomere 19 of below successively, and ajutage 16 is connected between refeed line epimere 10 and the refeed line hypomere 19.
The level height that nozzle 9 is installed in the spray-fluidized chamber 4 with the horizontal line of separation chamber's 5 boundary 0～800mm or following 0～400mm more than 23.
Discharging opening 12 connects pneumatic separator 13, and pneumatic separator 13 is provided with the air inlet 20 and the pneumatic separator air outlet 14 of pneumatic separator 13, and the air outlet 14 of pneumatic separator is connected in separation chamber 5.
Divide wind web plate 2 to be lower than away from the discharging opening place, be inclined to set near the discharging opening place.
Divide wind web plate 2 also can be horizontally disposed with, on minute wind web plate 2, be distributed with oblique hole, the upper end in each oblique hole oblique sensing discharging opening direction.
The present invention can also be provided with several charging apertures 17, heating fluidising chamber 3 sides in each charging aperture 17 is separately positioned on.
Be provided with three longitudinal baffles 18 in interior heating fluidising chamber 3 and the spray-fluidized chamber 4, be provided with spacing between each longitudinal baffle 18 and branch wind web plate 2 and bed body 22 tops.
In this device, interior heat exchanger is 10～300mm with the vertical range of dividing the wind web plate; Nozzle distance above interior heat exchanger is 50～1000mm; The interior height of fluidising chamber that heats is at 200～2000mm; The height of spray-fluidized chamber is at 500～2000mm.
During work, in charging aperture 17 enters, heat in the fluidising chamber 3 as the granule materials of crystal seed; Simultaneously, supply with the thermal current of certain flow from hot blast import 21, thermal current passes branch wind web plate 2 after entering separating chamber 1, material is blown simultaneously under the barrier and heat effect of interior heat exchanger 8 by thermal current, in each unit, be the formula fluidized state that looses in heating fluidising chamber 3 and the spray-fluidized chamber 4, at this moment, from the atomizing mother liquor of nozzle 9 ejection attached to each seed surface, blow down constantly oven dry at thermal current, seed particles is constantly grown and is become the also constantly increase of big own wt simultaneously, until becoming satisfactory shaped granule, shaped granule drops on the branch wind web plate 2, thermal current blow and the guiding of the branch wind web plate 2 that tilts under, molding materials is along dividing plate 18 and divide the gap between the wind web plate 2 to move to discharging opening 12 gradually from charging aperture 17, granule materials can be to grow up while moving, the blowing of thermal current make the less material of particle in separation chamber 5 with oarse-grained feed separation, small particles material rises with thermal current and enters successively in dust flue 6 and the cyclone separator 7, after cyclone separator 7 separates, gas enters atmosphere, small particles material enters refeed line epimere 10 from cyclone separator successively under ajutage 16 air-supply effects after returning charge Blowing stopper 15 is collected, refeed line hypomere 19, enter interior the heating in the fluidising chamber 3 by returning charge mouth 11, under the effect of fluidising chamber's material and interior heat exchanger 8, disperseed by maximization, up, enter in the atomization gas liquid zone of nozzle 9, realization is reunited uniformly or clad type is grown up, go round and begin again, finished product is constantly discharged from discharging opening, crystal seed constantly enters from charging aperture, and material liquid constantly sprays into fluidising chamber from nozzle 9 atomizings.
Fluidized bed pelletizer of the present invention from the course of work as can be seen, when particle is grown up to certain particle diameter, no longer up under the gravity effect, simultaneously because nozzle on fluidising chamber top, bulky grain breaks away from outside the range of atomization of nozzle, just do not continue the possibility of growing up yet, the generation of having stopped the super large ball, fluid bed can guarantee continuous production always; Can keep most material in fluid bed during startup-shutdown and need not tear nozzle open, material particles also advances not go nozzle, and is easy to use; Because nozzle is on fluidising chamber top, the atomizing resistance reduces, and the atomizing air amount just reduces, and theoretical calculating can reduce 20%～300%; Discharging opening is arranged on the horizontal below of nozzle, does not disturb between the two, and both can steady operation; Simultaneously because interior heat exchanger belongs to direct conduction heating, when heat energy utilization rate height, same evaporation capacity, air quantity reduces, and equipment investment and operating cost reduce.
The present invention is not limited to the foregoing description, and shown in Fig. 6,7, nozzle 9 can be arranged on the top of spray-fluidized chamber 4, and spray also can be played same effect from the top down, when being applied to discontinuous production, can show above superiority equally.
Shown in Fig. 8,9, returning charge mouth 11 can be arranged on spray chamber fluidising chamber 4 and be in the below of nozzle 9, and nozzle 9 can be arranged in spray-fluidized chamber 4 or the separation chamber 5.
Claims (9)
1. fluidized bed pelletizer; comprise nozzle and discharging opening that a body is provided with; the bed body is provided with separating chamber from bottom to top successively; divide the wind web plate; the interior fluidising chamber of heating; spray-fluidized chamber and separation chamber; bed body top is provided with dust flue; the bed external body is provided with cyclone separator; heating fluidising chamber is provided with interior heat exchanger in it is characterized in that; described nozzle is arranged in spray-fluidized chamber or the separation chamber; the air outlet of described dust flue links to each other with the import of cyclone separator; the lower end of cyclone separator is successively by connecting the refeed line epimere; the refeed line hypomere links to each other with the returning charge mouth; heat the side of fluidising chamber or spray-fluidized chamber in described returning charge mouth is arranged on, and be not higher than the horizontal line at hithermost nozzle place.
2. fluidized bed pelletizer according to claim 1 is characterized in that described nozzle is arranged on the side of spray-fluidized chamber.
3. fluidized bed pelletizer according to claim 1 is characterized in that above the horizon 0～800mm or the following 0～400mm of the level height of described nozzle installation in spray-fluidized chamber and separation chamber's boundary.
4. fluidized bed pelletizer according to claim 1 is characterized in that connecting described pneumatic separator at described discharging opening, and described pneumatic separator is provided with pneumatic separator air inlet and pneumatic separator air outlet, and the air outlet of pneumatic separator is connected in the separation chamber.
5. fluidized bed pelletizer according to claim 1 is characterized in that between cyclone separator and refeed line epimere the returning charge Blowing stopper being set, and is provided with ajutage between refeed line epimere and refeed line hypomere.
6. fluidized bed pelletizer according to claim 1 is characterized in that described minute wind web plate is lower than away from the discharging opening place near the discharging opening place, is inclined to set.
7. fluidized bed pelletizer according to claim 1 is characterized in that being provided with several charging apertures, the side of heating fluidising chamber in each charging aperture is arranged on.
8. fluidized bed pelletizer according to claim 1 is characterized in that heating fluidising chamber and the indoor longitudinal baffle that is provided with of spray-fluidized in described, is provided with spacing between described longitudinal baffle and branch wind web plate and the bed body top.
9. according to each described fluidized bed pelletizer in the claim 1～8, heat exchanger is 10～300mm with the vertical range of dividing the wind web plate in it is characterized in that; Nozzle distance above interior heat exchanger is 50～1000mm; The interior height of fluidising chamber that heats is at 200～2000mm; The height of spray-fluidized chamber is at 500～2000mm.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010166803 CN101829521A (en) | 2010-04-30 | 2010-04-30 | Fluidized bed granulator |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010166803 CN101829521A (en) | 2010-04-30 | 2010-04-30 | Fluidized bed granulator |
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| CN101829521A true CN101829521A (en) | 2010-09-15 |
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| CN 201010166803 Pending CN101829521A (en) | 2010-04-30 | 2010-04-30 | Fluidized bed granulator |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659478A (en) * | 2012-05-04 | 2012-09-12 | 湖北富邦科技股份有限公司 | Continuous enveloping fluidized bed for slow/control-release fertilizers |
| CN102744010A (en) * | 2012-07-24 | 2012-10-24 | 陈林书 | Spraying granulation method |
| CN102744009A (en) * | 2012-07-24 | 2012-10-24 | 陈林书 | Fluidized bed with internal heat exchanger |
| CN103028343A (en) * | 2012-12-18 | 2013-04-10 | 天津大学 | Production method for pelletoidal calcium chloride dihydrate |
| CN104026133A (en) * | 2014-05-21 | 2014-09-10 | 沈阳化工研究院有限公司 | Water-soluble paraquat granule and preparation method and special device of granule |
| CN105941823A (en) * | 2016-05-25 | 2016-09-21 | 刘新旗 | High-soluble soybean peptide dry powder and preparation method thereof |
| CN109331740A (en) * | 2018-12-12 | 2019-02-15 | 扬州日发干燥工程有限公司 | Fluidized hot bed pelletizer in one kind |
| CN116422227A (en) * | 2022-12-09 | 2023-07-14 | 山东奥诺能源科技股份有限公司 | Fluidized bed granulator |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201120271Y (en) * | 2007-10-19 | 2008-09-24 | 王新月 | Continuous gunite granulation clothing sheet apparatus of multi-unit fluidized bed |
-
2010
- 2010-04-30 CN CN 201010166803 patent/CN101829521A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201120271Y (en) * | 2007-10-19 | 2008-09-24 | 王新月 | Continuous gunite granulation clothing sheet apparatus of multi-unit fluidized bed |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659478A (en) * | 2012-05-04 | 2012-09-12 | 湖北富邦科技股份有限公司 | Continuous enveloping fluidized bed for slow/control-release fertilizers |
| CN102744010A (en) * | 2012-07-24 | 2012-10-24 | 陈林书 | Spraying granulation method |
| CN102744009A (en) * | 2012-07-24 | 2012-10-24 | 陈林书 | Fluidized bed with internal heat exchanger |
| CN102744010B (en) * | 2012-07-24 | 2014-04-23 | 陈林书 | Spraying granulation method |
| CN102744009B (en) * | 2012-07-24 | 2014-06-18 | 陈林书 | Fluidized bed with internal heat exchanger |
| CN103028343B (en) * | 2012-12-18 | 2015-07-29 | 天津大学 | A kind of production method of pelletoidal calcium chloride dihydrate |
| CN103028343A (en) * | 2012-12-18 | 2013-04-10 | 天津大学 | Production method for pelletoidal calcium chloride dihydrate |
| CN104026133A (en) * | 2014-05-21 | 2014-09-10 | 沈阳化工研究院有限公司 | Water-soluble paraquat granule and preparation method and special device of granule |
| CN104026133B (en) * | 2014-05-21 | 2016-08-24 | 沈阳化工研究院有限公司 | A kind of N,N'-dimethyl-.gamma..gamma.'-dipyridylium water-soluble granular formulation and preparation method thereof and special purpose device |
| CN105941823A (en) * | 2016-05-25 | 2016-09-21 | 刘新旗 | High-soluble soybean peptide dry powder and preparation method thereof |
| CN109331740A (en) * | 2018-12-12 | 2019-02-15 | 扬州日发干燥工程有限公司 | Fluidized hot bed pelletizer in one kind |
| CN116422227A (en) * | 2022-12-09 | 2023-07-14 | 山东奥诺能源科技股份有限公司 | Fluidized bed granulator |
| CN116422227B (en) * | 2022-12-09 | 2024-01-30 | 山东奥诺能源科技股份有限公司 | Fluidized bed granulator |
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Application publication date: 20100915 |