CN1224452C - Granulating method by using fluidized bed in rotary drum type and appt. thereof - Google Patents
Granulating method by using fluidized bed in rotary drum type and appt. thereof Download PDFInfo
- Publication number
- CN1224452C CN1224452C CN 02146785 CN02146785A CN1224452C CN 1224452 C CN1224452 C CN 1224452C CN 02146785 CN02146785 CN 02146785 CN 02146785 A CN02146785 A CN 02146785A CN 1224452 C CN1224452 C CN 1224452C
- Authority
- CN
- China
- Prior art keywords
- rotary drum
- fluid bed
- curtain
- drum
- side plate
- 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.)
- Expired - Fee Related
Links
Images
Abstract
The present invention relates to a prilling method by a revolving drum fluid bed, and a device thereof, which belongs to the technical field of prilling in chemical industries. The prilling method is characterized in that folded shovelling plates which are uniformly distributed are arranged at the inner wall of a rotary revolving drum, and a fixed fluidized bed is arranged in the revolving drum; crystal seed particles are continuously added from a material inlet end of the revolving drum, and the particles at the bottom of the revolving drum are shoveled into the fluidized bed; the particles drop from an overflow opening to form a continuous and uniform material curtain. Multiple nozzles are installed at the lateral surface of the material curtain, and the lateral surface is axially perpendicular with the revolving drum; the nozzles atomize prilling raw material liquid into liquid drops to be sprayed to the material curtain, and the liquid drops are in ccollision contact with moving particles; after the particle surfaces are coated, solidified and enlarged, the particles drop to the bottom of the revolving drum and are shoveled into the fluidized bed again to repeat the abovementioned process. In the process that the particles move from the material inlet end to a material outlet end, the grain diameter of the particle is gradually increased through multiple circulation of cooling (dryness), coating and solidification; after the particles are discharged from the material outlet end, qualified products are obtained through sieving and cooling. The prilling method has the advantages of investment saving, low energy consumption, convenient operation, good product quality and high efficiency.
Description
Technical field
Fluidized drum granulator method and device belong to chemical industry granulating technique field.
Background technology
Granulating technique is widely used in fields such as chemical industry, medicine, material, mining industry, building materials, the particularly granulation of chemical fertilizer, industrial chemicals and product, and the grain products that needs preparation certain particle size, intensity, pattern, structure and component to require is enhanced product performance.Prilling process can be divided into coating granulation, poly-granulation, sprinkling pelleting and extruder grain four classes on principle, coat granulation such as fluid bed class and expect the granulation of curtain class; Granulation of poly-group such as rotary drum class, fluid bed class and garden dish class etc.; Sprinkling pelleting such as tower granulation, steel band granulation etc.; Extruder grain such as extruding pelletization etc.The prilling process that adopt to coat the design of granulation principle can obtain good sphericity, smooth surface, mechanical strength height, grain products that the flow dispersion performance is good, is applicable to that granulating raw material is fused solution and certain density solution.
With the carbamide granulation in the chemical fertilizer is example, and its granulating raw material has two kinds, and a kind of is that concentration is about 99.8% fused solution, and a kind of is that concentration is about 96% solution, and material temperature is about 135 ℃.Existing granulating technique design principle is mainly based on sprinkling pelleting and two kinds of coating granulations.With sprinkling pelleting principle design mainly be the spray column granulating technique, be applicable to urea melting liquid.Tower height is usually above 60 meters, and diameter is from several meters to tens of meters.The pressurized granulation tower top that is pumped into of urea melting liquid, fused solution is sprayed into the drop of certain particle diameter by prilling spry, drop is unrestrained from cat head, cools off in dropping process, and drop phase transformation and cooling heat release make air themperature rising in the tower, cause air-flow to rise, cold air replenishes at the bottom of tower naturally, forms air motion from bottom to top, forms counter current contacting with top-down drop, the urea droplets cooling curing forms solid particle at the bottom of tower.There is following major defect in this granulating technique:
1. environmental pollution is serious.Because the adverse current shear action of centrifugal action, drop and the air-flow of shower nozzle rotation, the influence of spray orifice and in the sprinkling process, can produce a large amount of fine droplets, carried secretly by ascending air, cause the dust content severe overweight in the emptying gas, work the mischief for surrounding devices, environment, farmland etc.And discharge large-minded, pressure is low, is difficult to washing, purifying.
2. granule strength is low.Drop is contacting in the cooling procedure with the rising cold airflow, drop at first solidifies from external refrigeration, form duricrust, the cooling curing of drop kernel is subsequently caused restriction, because liquid-solid-phase changeable causes Volume Changes, produce internal stress, significantly reduce the shock resistance and the compression strength of solidifying the back product particle, fall, at the bottom of the bump tower from the high-altitude, be easy to crackedly, produce dust.Particle also is easy to cracked in processes such as saving fortune.When spreading fertilizer over the fields, fine particle adheres to blade easily, causes the burning seedling.
3. restraining factors are more.Tower granulation is subjected to seasonal effect bigger by natural wind convection current crystallisation by cooling, the summer temp height, and product temperature increases, high humidity in addition, particle bonds especially easily.Because depend on the granulation tower height cool time, there is certain restriction in product granularity.
Adopt the granular urea production technology that coats the design of granulation principle, can overcome the shortcoming of spray column granulating technique.Mainly contain two kinds of fluid bed class and the granulations of material curtain class; the existing granulating technique existence shortcoming in various degree that coats; as fluidized bed prilling; on the one hand; because particle air-teturning mixed phenomenon in fluid bed is remarkable; the particle size distribution of discharging particle from fluidized bed pelletizer is wide, the large granule that occupies more content after the screening must be broken into fine grained as returning charge granulation again, causes unnecessary granulation and broken invalid energy consumption.On the other hand, the bed of fluid bed class granulation is higher, needs higher fluidization air pressure, causes higher energy consumption.The remodeling of fluidized bed prilling technology-spouted bed granulation then is easy to generate dust.Another kind of coating granulation is designed to expect the granulation of curtain class, atomized drop is sprayed to moving particle, usually form the materials flow of moving by rotating rotary drum, drop contacts with motion materials flow collision, coats, solidifies at particle surface, because seed particles is mobile relatively poor, bond easily between the particle, contain poly-bigger granulation composition, cause the pattern of product particle relatively poor, shortcoming such as intensity is lower.And because materials flow is relatively poor with contacting of air, its cooling or drying efficiency are very low, cause whole granulation efficiency low.
France Ka Er rattan Bach-Di Lin company the Chinese patents document (application number: 98115143.4, publication number: 1238320), be fluidisation cylinder prilling granulator, regulate the time of staying of particle in rotary drum by the downflow weir of cylinder.In rotary drum, add fluid bed cooling particulate material, but the implementation method and the structure that lack the fluid bed cooling and particle is increased.At Jiang Dazhou patent (application number: 99122286.5, publication number: 1257053) with " urea droplets is sprayed on the interior urea granules surface of fluid bed ", and " urea granules is grown up under fluidized state ", belong to fluid bed class granulating technique, there is the upper limit in product granularity, when utilizing fluid bed formation material curtain to carry out granulation, explanation realizes even process for granulating and condition.The Jiang Dazhou patent (application number: 98249040.2, Granted publication number: adopt the sawtooth overfall CN2370006Y), form uneven material curtain easily, patent documentation does not illustrate measure and the condition that realizes even granulation.
Summary of the invention
The object of the present invention is to provide that a kind of reduced investment, energy consumption are low, processing ease, good product quality, fluidized drum granulator method and device that efficient is high.
The fluidized drum granulator method that the present invention proposes is characterised in that: hold (5～30) % that material amount volume is the rotary drum volume when one, axially and the horizontal plane inclination angle be that the rotary drum of (0～5) ° is during with the rotational speed of (2～10) rev/min, the seed particles that adds from rotary drum one end be distributed in rotary drum inboard and knuckle for the fold-type flight of (90～180) ° copy into be arranged on fixing in the rotary drum and along rotary drum axially horizontal by the fluid bed top at (0～2) ° inclination angle, make particle diameter qualification seed particles multiple spot within the specific limits even blanking on fluid bed continuously, the part seed particles drops on percent opening on the side plate of (0～3) %, under the effect of little gas flow hole on gravity and the side plate, evenly enter the percent opening that links to each other with side plate and be (90～180) ° angle with side plate on the distribuor of fluidized bed of (0.5～5) %, the apparent operating gas velocity of fluid bed is (0.1～4.0) meter per second, fluidized gas enters from the air chamber at the above-mentioned distribution grid bottom and the side plate back side to be cooled off or drying seed particles, promoting seed particles simultaneously is (0～2) ° along the angle with the axial horizontal plane of rotary drum, perpendicular to the inclination angle of the axial horizontal plane of rotary drum is the above-mentioned distribution grid of (0～30) °, through being the flash mouth of (0～200) mm highly, evenly fall to forming the major ingredient curtain; Granulating raw material liquid sprays to the material curtain through the intersection point distance of the center line of the major ingredient curtain adjustable apart from thickness and direction for after the nozzle atomization of (80～400) mm, drop is collided with the motion seed particles in the material curtain to be contacted, coat on the surface, solidify, the formed two defective material curtains of blanking that the fold-type flight of copying more seed particles was produced before arriving above the fluid bed play and prevent that the atomized drop that penetrates the major ingredient curtain on a small quantity from causing the effect that scabs in the drum inner wall accumulation, falling the particle of bottom of the drum is copied into fluid bed by the fold-type flight again, through so repeatedly circulation, grain diameter is increased continuously; Turning handle seed particles by hide processor moves the discharge end that is positioned at the axial other end of rotary drum from the axial feeding end of rotary drum.When the rotary drum level is installed, adopt the fold-type flight material to be transplanted on discharge end from feeding end along the method that drum inner wall distributes twist.The thickness of described major ingredient curtain and the adjusting of direction are to realize by the rotational angle that adjustment is arranged on the major ingredient curtain adjustable plate of overfall.The described particle diameter of copying the seed particles on fluid bed and the fluid bed side plate is to limit with being arranged on fluid bed top and the mesh diameter backstop for (10～100) mm.
The fluidized drum granulator device that the present invention proposes is characterised in that: it contains axially the rotary drum 1 horizontal by (0～5) ° inclination angle; Be evenly distributed on the inwall of rotary drum 1 and knuckle fold-type flight 2 for (90～180) °; Side and bottom surface and distribuor of fluidized bed 15 and side plate 14 constitute air chambers and along rotary drum 1 axially and horizontal plane be (0～2) ° inclination angle be arranged on the interior stationary fluidized bed 13 of rotary drum 1; In an inboard of fluid bed 13 side plates 14 that run through the axial aperture that has some of fluid bed 13 and percent openings for (0～3) %; Be with side plate 14 that (90～180) ° angle links to each other and percent opening is the distribution grid 15 of (0.5～5.0%), this distribution grid 15 is (0～2) ° with the inclination angle of horizontal plane axially along rotary drum 1, and is (0～30) ° at the inclination angle horizontal and horizontal plane perpendicular to rotary drum 1; Be provided with the overfall 16 of height of weir at end for (0～200) mm perpendicular to the axial distribution grid 15 of rotary drum 1; Be screwed on fluid bed 13 and available another screw is adjusted corner with the thickness of adjusting major ingredient curtain 21 and the major ingredient curtain adjustable plate 17 of direction; What be used to limit the seed particles particle diameter copied on fluid bed 13 and the fluid bed side plate 14 is arranged on fluid bed 13 tops and mesh diameter for (10～100) mm and by fluid bed side plate 14 and backstop supporting 19 backstops that support 18; Axially introduce material liquid pipe 8, the steam pipe 9 in the rotary drum 1 and the tracheae 10 that atomizes along rotary drum 1, steam pipe 9 provides steam insulation for material liquid pipe 8, and atomizing tracheae 10 adopts the insulation material insulation; The end that is communicated with material liquid pipe 8 and atomizing tracheae 10 and chews is the nozzle 20 of (80～400) mm apart from the intersection point distance of major ingredient curtain 21 center lines; High-end from rotary drum 1 along the rotary drum 1 axial feed pipe of introducing in the rotary drum 16; Axially introduce in the rotary drum 1 and axially run through rotary drum 1 and on tube wall, have the fluidisation tracheae 7 of venthole again along rotary drum 1; Fluidisation tracheae 7 works to support fluid bed 13 simultaneously; Be fixed on the bearing 5 in order to support roller supporting 3 of holding the rotary drum 1 that appearance wears driving cog circle 4 and static discharging opening 11 and the air-vent 12 that is located at rotary drum 1 other end relative with feeding end.
Use proof, this method and device have reached intended purposes.
Description of drawings
Fig. 1: the principle schematic of fluidized drum granulator method.
Fig. 2: the longitudinal sectional view of fluidized drum granulator device.
Fig. 3: the transverse sectional view of fluidized drum granulator device.
Fig. 4: the major ingredient curtain adjustable plate 17 of fluidized drum granulator device connects enlarged drawing.
Fig. 5: the product photo that the enforcement of fluidized drum granulator method and apparatus is obtained (granularity: (2～4) mm, intensity :～30N).
Fig. 6: the product photo that the enforcement of fluidized drum granulator method and apparatus is obtained (granularity: (6～8) mm, intensity :～80N).
Fig. 7: the product photo that the enforcement of fluidized drum granulator method and apparatus is obtained (granularity: (10～15) mm, intensity :～150N).
The specific embodiment
The present invention utilizes the good gas-solid of fluid bed contact, and reinforcing particle moves heat or dehydration when material liquid (adopt certain density).Distribuor of fluidized bed is provided with certain percent opening, fluidizing gas velocity is regulated according to the particle size of seed particles in the rotary drum, when particle diameter is big, adopt higher gas speed, particle diameter hour adopts lower gas speed, is in uniform fluidized state with particle on the assurance fluid bed, and in the material curtain that forms after seed particles is wandered, particle is in stronger motion state.With during the collision on moving particle surface contacts, realize that equiprobability coats at random, solidifies at atomized drop, the seed particles granularity is increased gradually, form the particle of fine and close homogeneous texture, improve the sphericity and the intensity of particle.Fluid bed is along axially maintenance level of rotary drum or small inclination angle is arranged, and makes fluidizing gas can axially not cause distribution of gas inhomogeneous because of the difference of bed height.At the fluid bed overfall, major ingredient curtain adjustable plate is set, be used to regulate the distance between major ingredient curtain direction, thickness and nozzle and the major ingredient curtain, realize best granulation state.Fluid bed side plate and distribution grid keep certain included angle, and side plate perforate ventilation promotes the interior material of fluid bed and moves to overfall.
The prilling granulator that the present invention relates to comprises a rotary drum, drum inner wall is equipped with the fold-type flight, rotary drum rotates with certain speed, a fixing fluid bed is installed in rotary drum, seed particles adds from the feeding end of rotary drum, flight copies particle continuously into fluid bed, because the good gas-solid contact performance of fluid bed, feeding the cooling of low temperature fluidization air moves heat or feeds hot blast with particle drying, particle in the fluid bed is ceaselessly motion under the agitaion of air-flow, wanders through overfall and forms continuously material curtain uniformly.The side that is axially perpendicular to the material curtain at rotary drum is provided with a plurality of nozzles, granulating raw material liquid forms atomized drop by nozzle, spray to the material curtain, contact with the dynamic particle collision, coat, solidify at particle surface, grain diameter is increased, the particle after the increase falls into the bottom of the drum, copied into fluid bed the circulation that cool off (or dry), coats, solidifies once more by flight.Because rotary drum and horizontal plane have certain inclination angle, or when the rotary drum level is installed with the shape distribution in the shape of a spiral in rotary drum of fold-type flight, particle moves to discharge end gradually from feeding end, moves axially in the process along rotary drum at particle, particle diameter increases gradually.Particle after the increase obtains the grain products of qualified particle diameter and temperature through screening, cooling.
The present invention will be described below in conjunction with Fig. 1～Fig. 4:
Fold-type flight 2 copies particle into fluid bed 13, and fold-type is copied and pulled the certain angle of 2 designs, and seed particles is copied in the fluid bed 13 continuously equably, can not destroy the fluidized state of fluid bed 13.Particle after coating, solidifying cool off in fluid bed 13 or is dry, because fluidized particles self mobile and from the promotion of side plate 14 air-flows, materials flow is wandered at overfall 16, formation major ingredient curtain 21.Adopt no downflow weir mode, can make fluid bed 13 when material is wandered, produce equal refining curtain, and by major ingredient curtain adjustable plate 17 adjust major ingredient curtains 21 thickness, uniformity, and nozzle 20 between distance and direction, in case of necessity, also certain overfall 16 can be set, it highly is (0～200) mm.Above fluid bed 13; the backstop 18 of mesh diameter for (10～100) mm is set; be used to limit the seed particles particle diameter of copying on fluid bed 13 and the fluid bed side plate 14; prevent that possible bonding coarse granule or caking from entering fluid bed 13 and influencing fluidized state; luming or cross coarse granule can be from backstop 18 taking-up; certain backstop angle also can be installed, make it, after screening, go fusion or fragmentation constantly discharging rotary drum 1 after the circulation through backstop 18 and whereabouts.
Distance between major ingredient curtain 21 and the nozzle 20 is regulated by major ingredient curtain adjustable plate 17, and atomizer 20 can adopt gas-liquid double-current method nozzle also can adopt the single current pressure nozzle, when adopting the single current nozzle, does not need the tracheae 10 that atomizes.Granulating raw material liquid is atomized into drop through nozzle 20, spray to major ingredient curtain 21, contact with the moving particle collision in the major ingredient curtain 21, coat, solidify at particle surface, make grain diameter obtain increasing, the particle in the major ingredient curtain 21 is fallen the bottom of rotary drum 1, copied once more and pull 2 and copy in the fluid bed 13, cool off or drying, so repeatedly circulation realizes the increase gradually of grain diameter.Need the material amount of holding that keeps certain in the rotary drum 1, copy when fold-type and pull 2 when taking up particle, material just began blanking before entering fluid bed 13, form two defective material curtains 22, helped preventing that the atomized drop that minority penetrates major ingredient curtain 21 from scabbing in the accumulation of rotary drum 1 inwall.
The basic technology parameter of the inventive method and device is as follows:
Rotary drum 1 axially and the mounted angle of horizontal plane be (0～5) °; Rotary drum 1 rotating speed is (2～10) rev/min; Fold-type is copied and is pulled 2 knuckle and be (90～180) °.
2. holding the material amount in the rotary drum 1 is (5～30) % of rotary drum 1 volume; Temperature is (80～120) ℃ in the granulating rotating drum 1; Rotary drum 1 internal pressure is (30～-200) mmH
2The O post.
3. being (0～2) ° along the angle of the axial distribuor of fluidized bed 15 of rotary drum 1 and horizontal plane, is (0～30) ° at the angle perpendicular to rotary drum 1 axial distribuor of fluidized bed 15 and horizontal plane; The percent opening of distribuor of fluidized bed 15 is (0.5～5) %, and the apparent operating gas velocity of fluidized gas is (0.1～4) m/s.
4. the angle of side plate 14 and distribution grid 15 is (90～180) °; Have the aperture of some on side plate 14, percent opening is (0～3) %.
5. the height of weir plate of overfall 16 is (0～200) mm, and nozzle 20 ends are (80～400) mm apart from the intersection point distance of material curtain center line.
The inventive method and device have carried out industrial implementation:
This granulating technique and device are used for concentration and are about 99.8% urea melting liquid granulation; average grain diameter is about under the sieve of 2mm fine grained and adds the granulation tower urea granules as crystal seed; granulation in the fluidized drum granulator machine; institute makes to such an extent that the qualified products particle grain size is (2～4) mm; as required; can produce the product particle of any particle diameter; also can produce the bigger particle of granularity as 15mm; when producing the different-grain diameter product; need to change the mesh size in the granulation flow process; and suitably adjust the superficial velocity of fluidized gas, used crystal seed is the fine grained returning charge after the comminutor screening and adds common urea particle from granulation tower.Fig. 5, Fig. 6, granular urea and the large granule urea product photo of Fig. 7 for adopting the present invention to produce, its granularity and intensity are respectively (2～4) mm ,～30N; (6～8) mm ,～80N; (10～15) mm ,～150N.Do not increase Biuret Content in the granulation process.Fig. 5 chooses the product that is obtained when being respectively 2mm and 4mm for the levels screen mesh size of screening machine in the flow process, less than the fine grained of 2mm as the returning charge crystal seed, in granulation product, seldom greater than the particle of 4mm; Fig. 6 chooses when being respectively 6mm and 8mm for the levels screen mesh size of screening machine in the flow process, and the product particle of acquisition is used for the returning charge crystal seed less than the particle of 6mm; Fig. 7 chooses for the levels screen mesh size of screening machine in the flow process and is respectively 10mm and 15mm; particle less than 10mm is used for the returning charge crystal seed; because when large granule is produced; begin to need the long granulation time from feeding intake; just begin to obtain to satisfy the product of super-size requirement; when grain diameter increases; can cause that to hold the material amount in the comminutor too big; need the more coarse grained returning charge of splitter section; in order to keep the suitable voidage of granulation material curtain, still need constantly to add the less crystal seed of granularity simultaneously.In implementation process, its basic technology parameter is as follows:
1. rotary drum mounted angle axial and horizontal plane is 1 °; Rotary drum 1 rotating speed is 6rpm; Fold-type is copied and pulled 2 knuckle is 150 °.
2. hold the material amount in the rotary drum 1 and be about 15% of rotary drum 1 volume; Temperature is 95 ℃ in the granulating rotating drum 1; Rotary drum 1 internal pressure is-50mmH
2The O post.
3. the angle along rotary drum 1 axial distribuor of fluidized bed 15 and horizontal plane is 0 °, is 0 ° at the angle perpendicular to rotary drum 1 axial distribuor of fluidized bed 15 and horizontal plane; The percent opening of distribuor of fluidized bed 15 is 3.2%, and when producing the granular urea of (2～4) mm, the apparent operating gas velocity of fluidized gas is about 1.4m/s; When producing the granular urea of (6～8) mm, the apparent operating gas velocity of fluidized gas is about 1.6m/s; When producing the large granule of (10～15) mm, the apparent operating gas velocity of fluidized gas is about 2.0m/s; All there is certain opereating specification.
4. side plate 14 is 145 ° with the angle of distribution grid 15; Have the aperture of some on side plate 14, percent opening is 0.8%.
5. the height of weir plate of overfall 16 is 0mm, and nozzle 20 ends are about 280mm apart from the intersection point distance of material curtain center line.
Claims (5)
1, the fluidized drum granulator method, contain the step that drum granulating and material curtain coat granulation, it is characterized in that: to hold material amount volume be 5～30% of rotary drum volume when one, axially and the horizontal plane inclination angle be that 0 °～5 ° rotary drum is during with 2～10 rev/mins rotational speed, the seed particles that adds from rotary drum one end be distributed in rotary drum inboard and knuckle be 90 °～180 ° fold-type flight copy be arranged in the rotary drum and along rotary drum axially horizontal by the fixed fluidized bed top at 0 °～2 ° of inclination angles, make particle diameter qualification seed particles multiple spot within the specific limits even blanking on fluid bed continuously, it is on 0～3% the side plate that the part seed particles drops on percent opening, under the effect of little gas flow hole on gravity and the side plate, evenly enter link to each other with side plate and with percent opening that side plate is 90 °～180 ° of angles be on 0.5～5% the distribuor of fluidized bed, the apparent operating gas velocity of fluid bed is 0.1～4.0 meter per second, fluidized gas enters from the air chamber at the above-mentioned distribution grid bottom and the side plate back side to be cooled off or drying seed particles, promote simultaneously seed particles along along rotary drum axially and the inclination angle of horizontal plane be 0 °～2 °, perpendicular to rotary drum axially and the inclination angle of horizontal plane be 0 °～30 ° above-mentioned distribution grid, through being the flash mouth of 0～200mm highly, evenly fall to forming the major ingredient curtain; Granulating raw material liquid is to spray to the major ingredient curtain after the nozzle atomization of 80～400mm through the intersection point distance of the center line of the major ingredient curtain adjustable apart from thickness and direction, drop is collided with the motion seed particles in the major ingredient curtain to be contacted, coat on the surface, solidify, the formed two defective material curtains of blanking that the fold-type flight of copying more seed particles was produced before arriving above the fluid bed play and prevent that the atomized drop that penetrates the major ingredient curtain on a small quantity from causing the effect that scabs in the drum inner wall accumulation, falling the particle of bottom of the drum is copied into fluid bed by the fold-type flight again, through so repeatedly circulation, grain diameter is increased continuously; Turning handle seed particles by hide processor moves into place in the discharge end of the axial other end of rotary drum from the axial feeding end of rotary drum.
2, fluidized drum granulator method according to claim 1 is characterized in that: when the rotary drum level is installed, adopt the fold-type flight along the method that drum inner wall distributes twist material to be transplanted on discharge end from feeding end.
3, fluidized drum granulator method according to claim 1 is characterized in that: the thickness of described major ingredient curtain and the adjusting of direction are to realize by the rotational angle that adjustment is arranged on the major ingredient curtain adjustable plate of overfall.
4, fluidized drum granulator method according to claim 1 is characterized in that: the described particle diameter of copying the seed particles on fluid bed and the fluid bed side plate is to be that the backstop of 10～100mm limits with being arranged on fluid bed top and mesh diameter.
5, the method according to claim 1 and device that designs is characterized in that: it contains axially the rotary drum (1) horizontal by 0 °～5 ° of inclination angles; Be evenly distributed on the inwall of rotary drum (1) and the fold-type flight (2) that knuckle is 90 °～180 °; Side and bottom surface and distribuor of fluidized bed (15) and side plate (14) constitute air chamber and along rotary drum (1) axially and horizontal plane be 0 °～2 ° of inclination angles be arranged on rotary drum (1) interior fixed fluidized bed (13); In an inboard of fluid bed (13) being one, to run through the axial aperture that has some of fluid bed (13) and percent opening be 0～3% side plate (14); Be with side plate (14) that 90 °～180 ° angles link to each other and percent opening is 0.5～5.0% distribution grid (15), this distribution grid (15) is 0 °～2 ° with the inclination angle of horizontal plane axially along rotary drum (1), and is 0 °～30 ° at the inclination angle of and horizontal plane axial perpendicular to rotary drum (1); Be provided with the overfall that height of weir is 0～200mm (16) at end perpendicular to the axial distribution grid (15) of rotary drum (1); Be screwed at fluid bed (13) and go up and available another screw is adjusted corner with the thickness of adjusting major ingredient curtain (21) and the major ingredient curtain adjustable plate (17) of direction; Be used for limiting the seed particles particle diameter copy on fluid bed (13) and the fluid bed side plate (14) to be arranged on fluid bed (13) top and mesh diameter be 10～100mm and support the backstop (18) that support (19) by fluid bed side plate (14) and backstop; Axially introduce material liquid pipe (8), the steam pipe (9) in the rotary drum (1) and the tracheae (10) that atomizes along rotary drum (1), steam pipe (9) provides steam insulation for material liquid pipe (8), and atomizing tracheae (10) adopts the insulation material insulation; The end that is communicated with material liquid pipe (8) and atomizing tracheae (10) and chews is the nozzle (20) of 80～400mm apart from the intersection point distance of major ingredient curtain (21) center line; Axially introduce feed pipe (6) in the rotary drum (1) along rotary drum (1) from rotary drum (1) is high-end; Axially introduce in the rotary drum (1) and axially run through rotary drum (1) and have the fluidisation tracheae (7) of venthole again on tube wall along rotary drum (1), fluidisation tracheae (7) works to support fluid bed (13) simultaneously; Being fixed on bearing (5) goes up in order to support roller supporting (3) of holding the rotary drum (1) that appearance wears driving cog circle (4) and static discharging opening (11) and the air-vent (12) that is located at rotary drum (1) other end relative with feeding end.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02146785 CN1224452C (en) | 2002-11-08 | 2002-11-08 | Granulating method by using fluidized bed in rotary drum type and appt. thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02146785 CN1224452C (en) | 2002-11-08 | 2002-11-08 | Granulating method by using fluidized bed in rotary drum type and appt. thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1498676A CN1498676A (en) | 2004-05-26 |
| CN1224452C true CN1224452C (en) | 2005-10-26 |
Family
ID=34232888
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02146785 Expired - Fee Related CN1224452C (en) | 2002-11-08 | 2002-11-08 | Granulating method by using fluidized bed in rotary drum type and appt. thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1224452C (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101801282B1 (en) * | 2016-04-29 | 2017-11-27 | 주식회사 홀그레인 | Rotary type dry equipment for pretreatment drying of green whole grain |
| CN108704580B (en) * | 2018-07-20 | 2020-10-27 | 河南龙昌机械制造有限公司 | Organic fertilizer rotary drum granulation process and organic fertilizer rotary drum granulation production line |
| CN115364764A (en) * | 2022-09-09 | 2022-11-22 | 北京达立科科技有限公司 | Low-energy-consumption high-capacity granulation process method |
-
2002
- 2002-11-08 CN CN 02146785 patent/CN1224452C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1498676A (en) | 2004-05-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US3991225A (en) | Method for applying coatings to solid particles | |
| RU2528670C2 (en) | Device and method for pelletising in fluidised bed | |
| JPS6034517B2 (en) | How to granulate urea in a fluidized bed | |
| CN102274703A (en) | Large-scale continuous energy-saving fluidized bed spraying, granulating and drying process | |
| US4686115A (en) | Process for granulating chemical products and apparatus therefor | |
| CN201959772U (en) | Rotary-drum granulator with fluidized bed | |
| RU2372979C2 (en) | Method of granulation in fluidised layer and granulator for its implementation (versions) | |
| US4370198A (en) | Method and apparatus for the recovery of the solid material content of solutions and/or suspensions as granules in a gas fluidized bed | |
| RU2283171C2 (en) | Method of granulation in fluidized bed and granulator for realization of this method (versions) | |
| US4749349A (en) | Granulating device and plant | |
| CN1224452C (en) | Granulating method by using fluidized bed in rotary drum type and appt. thereof | |
| US4428973A (en) | Method for the homogeneous complete encapsulation of individual grains of pourable material and apparatus for its production | |
| CN208494120U (en) | A kind of novel organic fertilizer granulating disc | |
| CN1100023C (en) | Large size particle urea composite rotary drum prilling technology and equipment | |
| CN109173926B (en) | Improved method for producing granular compound fertilizer by drum granulation | |
| EP1407814B1 (en) | Process and apparatus with a fluidised bed apparatus for producing granules | |
| RU2328338C1 (en) | Method of granulated product preparation and drum granulator | |
| CN208229853U (en) | A kind of novel atomizing condensing granulation apparatus | |
| CN100546707C (en) | Rotary drum fluid-bed heat-converter granulating method | |
| NO166761B (en) | Granulator. | |
| CN2370006Y (en) | Drum pelletizing device for urea | |
| US4425865A (en) | Method for the homogeneous complete encapsulation of individual grains of pourable material and apparatus for its production | |
| CN209484938U (en) | A kind of roller fluidized-bed granulation dryer | |
| US3475195A (en) | Process and apparatus for granulating paste | |
| CN107531583A (en) | Ammonium sulfate is granulated |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20051026 Termination date: 20181108 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |