Method of producing granules in fluidized bed

专利摘要:
The invention relates to a method for producing granules in a fluidized bed and reduces energy consumption and reduces dust formation. The method of obtaining granules in the fluidized bed involves feeding the gas stream upward through a layer of particles to create a fluidized bed, supplying the fluid to the fluidized bed of particles from the bottom upwards through the central channel of the feeding device, feeding a powerful gas stream through the concentric channel with it to create a rarefied zone in the layer with a linear at a rate greater than that of the gas stream creating a fluidized bed; solidifying the liquid on the particles and removing the resulting granules from the layer. Liquid is supplied under pressure from 1.5 to 6 bar with a linear speed of 10 to 25 m / s in the form of a closed conical film with a thickness after the impact of 25-500 μm, and the particles from the layer are moved through the film due to a powerful gas stream that is fed under pressure from 1.1 to 1.5 bar at a speed of 50-250 m / s. 7 hp f-ly, 4 ill. i o) oa sd ate
公开号:SU1351511A3
申请号:SU843784997
申请日:1984-08-24
公开日:1987-11-07
发明作者:Мартинус Петрус Мутсерс Станислаус
申请人:Уни Ван Кунстместфабрикен Б.В.(Фирма)；
IPC主号:

专利说明:

eleven
The invention relates to a method for producing granules by feeding a liquid material in a fluidized bed of solid particles, whereby the particles are increased by solidifying a liquid material on them and by removing the granules thus obtained from the fluidized bed.
The purpose of the invention is to reduce energy consumption and reduce dust generation.
Figure 1 shows a spray device for carrying out the method according to the invention, longitudinal pais-cut; figure 2 - node I in figure 1; on fig.Z - section aa in figure 2; 4 shows the outlet part of the spray device, in which the gas and liquid outlet openings are installed at approximately the same vertical height, with a longitudinal section.
The spray device consists of a feed 1 and raspishitelnoy 2 sections. The spray device is installed in a granulating unit (not shown) with a bottom part 3 and an integrated bottom plate 4 that has openings 5 for the passage of fluidizing air, while unloading is done through hole 6. The spray device consists of a central pile 7, which - .nen with a liquid pipeline (not shown), and the other with a rotary chamber 8. In addition, the spreading device is equipped with a channel 9, which is located concentrically around the central channel, while 9 at one end through the holes. 10 is connected to a gas pipeline (not shown), and at the other end there is a narrowing gas channel 11, which ends at an outlet 12.
I
The discharge part of the spray
The device consists of a liquid outlet nozzle 13, around which there is a narrowing gas channel 11, equipped with an outlet 12. The liquid outlet nozzle 13 consists of a liquid supply channel 7, which is connected to the rotary chamber 8 through the holes 14 and liquid channels 15,
one . 2
equipped with a central outlet channel 16 with an outlet 17 Example 1. In a circular granulator with a fluid bed of 27 cm in diameter, which is provided with a perforated bottom plate with a hole diameter of 2 mm and contains a layer of ammonium nitrate particles
ammonium nitrate melt and a powerful gas stream through the spray device (Figures 1 and 2) are continuously fed. The melt of ammonium nitrate containing, in wt.%: Water 0,65; dolomite
2.0; clay 2.0, temperature 182 C pbat through the central channel 7 of the spray device at a speed of 195 kg / h at a pressure of 2.7 bar. Sorbitol with a particle size of less than 5 microns, which consists mainly of SiO (73 wt.%), (14 wt.%), Is used as clay.
A powerful stream of air is fed through the gas channel 9, which is mounted concentrically with respect to the central channel, at a speed of 50 kg / h, with a temperature of 180 s at a pressure of 1.4 bar.
In the rotary chamber 8, the melt is served using four tangentially located small liquid channels 15.
The spreading device has the following dimensions: the diameter of the central channel is 10 mm, the diameter of the concentric channel is 12 mm, the diameter of the outlet opening 17 of the central channel is 3 mm, the width of the clearance of the outlet opening 12 is concentric. 1.2 mm, the vertical distance from the outlet 17 of the gas channel to the bottom plate is 4 cm, the vertical distance from the outlet 17 of the gas channel to the outlet 12 of the liquid channel 1.8 cm, the angle of convergence of the outer side of the wall of the liquid channel 22, 5 °, the outer diameter of the gas channel 23.4 mm.
Liquid is supplied from the central channel in the form of a closed conical film with an outlet thickness of 275 microns, a funnel angle of 87 ° and a speed of 15.5 m / s. The film has a slightly wavy surface due to low internal turbulence (Weber number We is 1400).
Air flow is supplied from a concentric gas channel at a speed of 200 m / s. Although the gas channel is not sho
3 The convergence of the gas stream is several degrees. In the collision of a gas stream loaded with particles and a film, there is almost no mixing of gas and liquid
Kg / h of solid particles of ammonium nitrate with an average diameter of 1–1.5 mm and temperature C, which are obtained by sieving and grinding the granulate discharged from the layer, are fed into the layer.
The particle layer has a temperature of / 135 ° C and is fluidized by means of an upwardly directed air jet with a temperature of 70 ° C and a speed of 2.1 m /
In the form of a flowing stream, the granules (temperature 135 ° C) are continuously discharged from the bed and cooled to 90 ° C in a drum cooler in a countercurrent of air. The cooled beads are then sifted through Engelmann flat screens of 2-4 mm in size. 166 kg / h of the screened fraction with a diameter of less than 2 mm are obtained, which is returned to the bed, and 14 kg / h of the screened fraction with a diameter of more than 4 mm, which is crushed to 1.1 mm using a roller crusher. A shallow pish (less than 750 microns) is separated using a wind sieve, after which the residual crushed material is returned to the bed.
193 kg / h of pellets were obtained as a sieved fraction of the product (2-4 mm), which were cooled to 40 ° C in a drum.
The granules thus obtained have the following properties:
Nitrogen content
wt.% 33.7
Water content
wt.% 0.15
The content of round granules,% 80
Volume weight,
kg / m 935
Shock strength,%. 100
Crush resistance, bar 60
Oil absorbing
ability,
wt.% 0.60
Penetration
mercury, cm / g
0.085
Some of this product is heated and cooled five times in the range of 15-50 ° C. Thus obtained
51511
granules have a crush resistance of 50 bar and an oil absorption capacity of 2.2% by weight.
The crush resistance is determined by placing the granule between two plates, on the top of which gradually increasing pressure is applied until fracture occurs.
10 granules. The content of the round granules is determined by placing the granules on a rotating disk set at a slope of 7.5, and determining the percentage of rolling granules. Shock
15, the strength is determined by bursting the pellets into a plate set at an angle of 45, and determining the percentage of round pellets before and after the test.
20 Dust-containing fluidizing air of temperature C coming from the bed is fed to a wet washer, in which a dilute solution of nitrate is obtained.
25 ammonium (about 35 wt.%).
This solution is evaporated and ammonium nitrate fed to the bed is added to the melt.
The dust-laden air currents from the refrigerators and the grinding section are directed to a bag filter to clean the duster. The ammonium nitrate so produced is dissolved in a hot melt.
25 ammonium nitrate supplied to the layer. Example 2. 195 kg / h of molten ammonium nitrate, containing 0.39 wt.% Water and 0.3 wt.% Mg (NOj) ,. (in terms of MgO), temperature
40 1VO ° C is fed at a pressure of 1.9 bar to a fluidized bed granulator, which is similar to the granulator of example 1, but is equipped with a spray (figure 4). In addition, 55 kg / h of air at a temperature of 180 ° C at a pressure of 1.5 bar are fed through a spray device.
The conical liquid film, CQ coming from the center channel, with the outlet opening diameter A mm, has a thickness of 300 µm, a speed of 11.9 m / s, and a funnel angle of 90 (Weg). The outgoing air flow is 195 m / s. 175 kg / h of solid particles are also fed into the bed with a temperature that is fluidized with air at a temperature of 40 ° C and a surface speed of 2.1 m / s.
5,11315
scientists in the sieving and grinding sections.
The granulate discharged from the layer in the form of a flowing stream is cooled, as in Example 1, to 90 ° C in a drum and sieved, and a kg / h product fraction with a size of 2-4 mm is obtained, which is cooled to a drum.
The granules thus obtained have the following properties:
Nitrogen content
wt.% 33.8
Water content Ig
wt.% 0.15
Bulk density
kg / m®965
Round content
granules,% 95
Impact strength,% 100
Resistance
crush
bar45 25
Oil absorbing
ability, wt.% 0.90
Penetration
mercury, cm / g 0.04
A portion of this product is heated 30 times and cooled in the range of 15-50 ° C. Five times. The granules treated in this way have a crush resistance of 45 bar and an oil absorption capacity of 1.9% by weight.
Example Z.V ring zero torus A fluid bed with a diameter of 4b cm, containing a layer with a temperature of 100 C of urea particles 60 cm in height, which is fluidized by air with a spirit of 35 ° C and a surface speed of 2.0 m / s, 180 kg / h of urea solids are fed, which are obtained by sieving and grinding the granulate.
In addition, using a splitter-. which device is similar to the example
1 in a layer in the upper direction of the flow
Ustav; Shave urea and powerful air flow. Urea melt tem-.,
at 140 ° C, the water content is O, 5. wt.%, the formaldehyde content, wt.%, served in the amount of 195 kg / h at a pressure of 3.3 bar. Powerful air flow has a temperature C and serves in the amount of 50 kg / h at a pressure of 1.4 bar.
Urea melt is fed from a spray device in the form of a slightly
35
45
0
15
g
g
five
0
. „
.

35
45
11, b of a wavy conical film with a funnel angle of 88 (We about 1950), 300 microns thick and an exit velocity of 20 m / s. At the outlet of the spray device, the air flow has a speed of m / s.
In the form of a flowing stream, the granules are unloaded from the bed, cooled to -v40 ° C in a fluidized bed refrigerator, and then classified by sifting into a product fraction of 2-4 mm in size (190 kg / h), fraction less than 2 mm (165 kg / h) h) and a fraction larger than 4 mm (15 kg / h). The last fraction is crushed and returned to the layer together with a fraction of less than 2 mm.
The obtained granules have the following properties:
Water content, wt.% 0.04
The formaldehyde content, wt.% 0.3 Volume weight,
The content of round granules,% 90
Crush resistance bar60
Shock
strength,% 100 Example 4. In an annular granulator with a fluidized bed with a diameter of 46 cm, a temperature of 60 cm in height of urea particles, which is fluidized by air at a temperature of 110 C and a surface speed of 2.0 m / s, solid particles of urea are fed into amount of 180 kg / h, which is served when sifting and grinding the granulate from the layer.
In addition, in example 1 using the spray device serves to melt the urea and powerful air flow in the upper direction. The urea melt has a temperature of 140 ° C, a water content of 1.20 wt.% And does not contain formaldehyde. The melt is fed in the amount of 195 kg / h at a pressure of 3.3 bar. Powerful air flow has a temperature of 140 ° C and is served in the amount of 88 kg / h at a pressure of 0.40 bar.
Urea melt is fed from a spray device in the form of a slightly wavy conical film with a funnel angle of 88 and (Weg 1950) 300 microns thick and at a speed of
course of 20 m / s. At the exit from the raspytelny device, the air flow has a speed of 190 m / s.
In the form of a flowing stream, the granules are unloaded from the bed, cooled C in the refrigerator, with a fluidized bed, and then classified into a fraction of 2-4 mm (190 kg / h), a fraction less than 2 mm (165 kg / h) and a fraction larger than 4 mm ( 15 kg / h). The last fraction is crushed and returned to the layer together with a fraction of less than 2 mm.
The obtained granules have the following properties:
Water content
wt.% 0.04
Volume weight,
Formaldehyde content,
May.% About
Content
round granules,%
90
Impact strength,% 100 Content
dust% O ,, 6
Example 5. A ring granulator with a fluid bed of 44 cm in diameter, containing a layer (43 C) of sulfur particles (average diameter 2.90 mm) with a height of 55 cm, is continuously fed kg / h of sulfur particles with an average diameter of 1.0-1 , 5 mm and a temperature of 36 ° C, which is obtained by sieving and grinding the granulate from a layer. The layer is fluidized using an upwardly directed air flow of 20 ° C and a surface speed of 2.0 m / s.
In addition, in Example 1, a layer of 150 kg / h of sulfur melting at a temperature of 135 ° C at a pressure of 3.1 bar and 55 kg / h of air at a temperature of 35 ° C at a pressure of 1.7 bar is fed using a spraying device. The sulfur melt is fed from a disintegrating device in the form of an actually smooth film (the Wag number is -1000) at a speed of 12.5 m / s, a thickness of 280 mm and a funnel angle of 87. At the exit, the powerful air flow has a speed of 175 m / with.
From the layer, the granules are discharged as a flowing stream and classified into a fraction less than 2.5 mm (112 kg / h), a fraction larger than 4.5 mm.
51511S
(38 kg / h), which is crushed to an average size of 1.0-1.5 mm and returned to the layer together with small facings, and the product fraction with a diameter of 2.5-4.5 mm (145 kg / h ), which has the following properties: Volume weight,
kg / m 1130
10 Contents
round granules,% 20 Shock
strength,% 20
15 Crush resistance, bar35
The degree of dust 20 20 602,90 mm
Example 6. In Example 1, 180 kg / h of lime-ammonium nitrate (temperature 100 ° C, average particle diameter 1.5 mm) are fed into a 25 layer of particles of calcium ammonium nitrate (temperature 105 ° C), which is maintained in a fluidized state using air (temperature 20 C, surface 30 at a speed of 2 m / s), In addition, in example 1, using a spray device serves to melt lime-ammonium nitrate in an amount of 200 kg / h, containing 35 wt.%: nitrogen 26 | CaCOj 24; water 0.75, temperature at a pressure of 2.7 bar; as well as 50 kg / h of powerful airflow with a temperature at a pressure of 1.4 bar. 40 The conical film (funnel angle 88 °), coming from the spray device, has a speed of 14.5 m / s, a thickness of 270 microns and a Weber number 1200. At the exit, the speed 45 of the air flow is 200 m / s, the granulate discharging out of sieved in hot condition. The fraction larger than 4 mm is ground and voz-. rotate in a layer with a fraction of 50 less than 2 mm.
five
The fraction of 2-4 mm is cooled in the drum before and discharged as a product. The product has the following properties:
Water content
wt.% 0.09
Volume weight.
kg / m
1005
Impact strength,% 100 Resistance to crushing, bar45 Composition of round granules,% 95 Example 7. A round granule with a fluidized bed having a diameter of 45 cm, containing a layer of urea particles (temperature 105 s) and a height of 65 mm subjected to fluidization by means of air, which has a temperature and surface speed of 2 m / s, serves solid urea particles at a speed of 160 kg / h, moreover, these particles were obtained by sieving and grinding the granulate. of the word
In addition, using a spraying device, similarly to example 1, a urea melt and a powerful air flow going up are introduced into the layer. The urea melt has a temperature, contains water 0.3 wt.% And formaldehyde 0.18 mas,% serves in the amount of 200 kg / h under a pressure of 1.5 bar. The powerful air flow has a temperature of 140 ° C and is served in an amount of 50 kg / h under a pressure of 1.5 bar.
The povaine melt coming out of the spraying device has the shape of a conical film (We 1480). With an angle at the apex of the cone equal to 68,. moreover, the film thickness is 980 µm, and the exit velocity is 10 m / s. Film thickness at impact of 480 microns.
The airflow from the spray device is 350 m / s.
By transfusing, the granules are discharged from the bed, cooled to 35 ° C and sieved for separation into fractions with sizes less than 2 µm (152 kg / h), more than 4 µm (12 kg / h) and the fraction that is the final product (198.8 kg / h), and the granules obtained as a finished product (2-4 microns) have the following properties:
Water content, wt.% 0.2
The formaldehyde content, wt.% 0,18
Bulk density, kg / m 780 Capacity
- rolling,% 85
Durability. When grinding, bar 60 Resistance to impact,% 100 Isolation of a drink, wt.% From the supplied amount of 0.6 Sintering tendencies. About Example 8. 200 kg / h of molten ammonium nitrate, containing, wt.%: Water 0, 56; sorbolite 2; dolomite. 2 and having a temperature of 170 ° C., are introduced into a fluid-bed granulator with a diameter of 27 cm, similar to a granulator. In Example 2, under a pressure of 6 bar. In addition, 84 kg / h of air at a temperature of 170 C is fed through a spraying device under a pressure of 1, 1 bar.
The conical liquid film emerging from the central channel has a thickness of 171 microns, a speed of 22 m / s, and a corner angle of a cone of 92 (We 1790). The film thickness when exposed is about 30 microns. In a layer whose temperature is 135 ° C and which is fluidized with air having a temperature of –70 ° C and a surface speed of 2.09 m / s, solid particles obtained from screening and grinding sites are fed at a speed of 170 kg / h. .
The final product granules (sizes 2-4 µm) are obtained after cooling and sieving for separation into fractions with sizes less than 2 µm (163 kg / h), more than 4 µm (11 kg / h) and a fraction containing the final product with dimensions 2-4 microns (199 kg / h), while they have the following properties:
The nitrogen content, wt.% 33,15
Water content, wt.% 0.05 Bulk density, kg / m 955 Rollability,% 85 Isolation of the lierich, wt.% 0.5
eleven
Resistance to
exposure,% 100
Strength at
grinding, bar 60
Absorbency
oil, wt.% 0.10
Penetration rate
new mercury
CMVr0,042
The quality of the final product (urea), obtained in accordance with the known methods, is determined by the following data:
Water content
wt.% 0.25
Formaldehyde content, May.% 0.4
Bulk density
700
70-90
45-55
100
ness, kg / m Rollability,% Durability during grinding, bar
Resistance to the effects of% Dust generation, wt.%, Of the supplied amount 4 Sintering tendencies. O After sifting the granules obtained by the blasting method, the number of particles of large and small sizes is actually equal to the yield achieved in accordance with the invention.

权利要求:
Claims (8)
[1]
1. A method of producing pellets in the PSA fluidized bed, including gas upwards through a bed of particles, creating a fluidized bed, transferring a fluid to the fluidized bed of particles upward through the central channel of the feed device, feeding a powerful gas stream through a concentric channel with it to create a rarefied gas. zone in a layer with a linear velocity exceeding the velocity of the gas flow creating a fluidized bed, the solidification of the liquid on
5151112
particles and removing the formed granules from the layer, characterized in that, in order to reduce energy costs and reduce dust generation, the liquid is supplied under pressure from 1.5 to 6 bar and at a speed from 10 to 25 m / s in the form of a closed conical films with a thickness of 25-500 μm, at 10 than particles from the layer are moved through the film due to the powerful gas flow, which is fed under pressure from 1.1 to 1.5 bar and at a speed of 50-250 m / s.
15
[2]
2. Method POP.1, ply shf rf and so that the liquid material is rotated in the delivery device.
[3]
3. The method according to claims 1 or 2, that is, that the film has internal turbulence, which meets the conditions
25 5
where Wej- is the Weber number;
p is the density of the liquid material
V is the potential velocity of the liquid material, m / s; G is the surface tension of the liquid material, N / m; o is the thickness of the film at the exit from the central channel, m.
[4]
4. The method according to claims 1 to 3, of which the liquid material is supplied to the layer that is higher in level than the input of a powerful gas stream.
[5]
5. The method according to claim 4, about tl and aaaaa and so that the vertical distance between the levels of supply of the liquid material and the gas stream to the bed is 0.5-3.0 cm.
[6]
6. The method according to claims 1-5, about tl and h and-yi and the fact that the mass ratio of the gas stream and the liquid material is 0.1: 1-0.5: 1.
[7]
7. The method according to claim 6, characterized by the fact that the mass ratio of the gas flow and the liquid material is 0.2: 1-0.4: 1.
[8]
 8. The method according to claims 1 to 7, characterized in. - in that the gas flow is output at an angle of not more than 25.
Figure 1 L / b 8 i5
/ J
Favor
A a
/four
13
FIG.

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引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

RU2491262C1|2012-04-10|2013-08-27|Открытое Акционерное Общество "Научно-Исследовательский И Проектный Институт Карбамида И Продуктов Органического Синтеза" |Method and apparatus for producing granular fertiliser|JPS4924012B1|1971-03-03|1974-06-20|

---

US4171091A|1976-03-26|1979-10-16|Stamicarbon, B.V.|Process and device for spraying liquid|

---

GB1581761A|1977-06-09|1980-12-17|Azote Sa Cie Neerlandaise|Urea granulation|

---

JPS6034517B2|1978-03-03|1985-08-09|Ube Industries|

---

NL191557C|1980-05-12|1995-09-19|Azote Sa Cie Neerlandaise|A method for manufacturing granules built up from a core and an envelope.|US5227017A|1988-01-29|1993-07-13|Ohkawara Kakohki Co., Ltd.|Spray drying apparatus equipped with a spray nozzle unit|

---

US5499768A|1989-05-31|1996-03-19|Ohkawara Kakohki Co., Ltd.|Spray nozzle unit|

---

DE3909455A1|1989-03-22|1990-09-27|Hoechst Ag|METHOD FOR PRODUCING WATER DISPERSIBLE GRANULES|

---

US5364832A|1990-08-10|1994-11-15|Hoechst Aktiengesellschaft|Water-dispersible granules comprising fenoxaprop-ethyl and/or fenchlorazole|

---

KR0159947B1|1991-03-12|1998-11-16|마사아키 오카와라|Two-fluid pressure nozzle of upward injection type spray dryer using the nozzle and method for control of droplet diameter in the nozzle|

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US5264078A|1991-07-05|1993-11-23|Aptus Inc.|Apparatus and method for spray drying solids-laden high temperature gases|

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PL307334A1|1992-08-07|1995-05-15|Hydro Agri Sluiskil Bv|Method of obtaining carbamide pellets|

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---

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---

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---

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---

NL1017130C2|2001-01-17|2002-07-18|Dsm Nv|Process for preparing granules.|

---

US7498055B2|2003-11-10|2009-03-03|Dsm Ip Assets B.V.|Process for the preparation of urea granules|

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法律状态:

优先权:

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申请号 | 申请日 | 专利标题

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NL8302999A|NL8302999A|1983-08-27|1983-08-27|METHOD FOR PREPARING GRANULES|

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