前苏联专利SU1329606A3 Method of producing granules in fluidized bed

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专利摘要:
Preparation of granules by making nuclei grow, in a fluidized bed, by causing a liquid material to solidify thereon. The liquid material is sprayed in the bed upwards, with the aid of a spraying device provided with a central channel (1) through which the liquid material is supplied, and a channel (4) concentric therewith carrying a powerful gas stream, with the liquid material contacting the gas stream and being carried with the gas stream to a dilute zone where the growth of the nuclei takes place, which zone is created by the gas stream and is completely within the fluidized bed. The liquid material is made to come out of the central channel as a virtually closed, conical film, with a thrust exceeding the thrust of the gas stream, and this film is nebulized to very fine droplets with the aid of the gas stream. In this process a very small amount of high-energetic gas is needed, while no agglomeration occurs in the bed.
公开号:SU1329606A3
申请号:SU843786914
申请日:1984-08-24
公开日:1987-08-07
发明作者:Мартинус Петрус Мутсерс Станислаус；София Паулус Мари Краенен Герардус
申请人:Уни Ван Кунстместфабрикен Б.В. (Фирма)；
IPC主号:

专利说明:

The invention relates to a method for producing granules by spraying a liquid material in a fluidized bed of solid particles, whereby solid particles increase due to solidification of a liquid material on them, and the granules thus obtained are removed from the fluidized bed.
The aim of the invention is to reduce the energy consumption and reduce the
Figure 1 shows a spray device for carrying out the method according to the invention, longitudinal section; Fig, 2 - the outlet part of the spray device, a longitudinal section; Fig 3 is a section A-A in FIG. 2; FIG. 4 shows the outlet part of the spray device, provided with two concentric gas channels, a longitudinal section.
The spray device consists of a feed I and a spray 2 sections. The spray device is mounted in a granulating unit (not shown) with the bottom part 3 and is equipped with a bottom plate 4 having openings 5 for supplying fluidizing air. The device has an outlet port 6.
The spray device consists of a central channel 7, which at one end is connected to a liquid pipe (not shown), and the other with a rotary chamber 8. The spray device includes a channel 9 located concentrically around the central channel, while channel 9 at one end through the opening 10 - dinene with a gas pipeline (not shown), and the other with a narrowing part I1, which ends with an outlet 6,
Fig. 3 shows a modified discharge section of the spray device.
This section differs from the embodiment of FIG. 2 in that around the concentric gas duct 11 there is a second concentric gas duct 12, which ends with an outlet opening 13,
Example 1 In a 29 cm diameter circular fluid bed granulator, which includes a perforated bottom plate (hole diameter 2 mm, layer of urea particles 80 cm high), is continuously fed at a rate of 200 kg / h from bottom to top.
through this layer, a urea solution (95 wt.%), including 0.6 wt.% formaldehyde with a temperature of 1AO ° C and a pressure of 5 bar.
The solution is supplied through the central channel of the spraying device. In addition, through the gas channel located concentrically around the central channel 9, a powerful air flow is supplied with a temperature of approximately 1.50 bar feed pressure of 89 kg / h. The spraying device is provided with a perforated bottom plate in such a way that the vertical distance from the through opening of the spraying device to the bottom plate is about 4 cm.
Below are the most important dimensions of the spray device, mm:
Diameter of the central liquid channel 2 Width of the concentric gas channel 10
The width of the annular opening of the concentric channel 2.65 The diameter of the outlet channel of the central channel 3.0 The convergence angle of the concentric channel 6 The diameter of the tangential slots (2x) in the rotary chamber 1.5 The liquid flows from the central channel in the form of a wavy, closed conical film with a funnel angle of 89 ° with thickness films of about 220 microns and speeds of 29.6 m / s. The film has a rather high internal turbulence (Weber number We x i 3400). Powerful air flow comes from a concentric channel at a speed of 275 m / s and collides with the at an angle of about 10 mm from the outlet aperture 10 of the central channel. The film thickness at the time of the collision is about 60 microns, and the ratio of the grams of film and air is about 12: 1. When struck, the film is sprayed in air the flow is virtually instantaneous,
In a layer of urea particles with a temperature of about 100 ° C, which is fluidized by an upward flow
.o (1 air with tenpura around 60
Yu
and at a surface speed of 2.0 m / s, about 180 kg / h of solid urea particles with an average diameter of 1-1.5 mm and a temperature of about 39 ° C are supplied, and the particles are obtained by sieving and grinding the granulate from the bed.
Through a flowing stream, the pellets with a temperature of approximately continuously discharged from the bed into the drum cooler, where they are cooled to approximately 43 ° C with counterflow to the atmosphere with the ambient temperature. The cooled granules are then fed to a sieve section equipped with Engelman flat screens with openings of 2 and 4 mm. The resulting small fraction (approximately 165 kg / h) is returned to the bed and the large fraction (approximately 15 kg / h) is crushed to 1.1 mm using a roll crusher. Fine dust with a particle size of less than 750 microns is separated using a wind sieve, after which the residual ground material is returned to the bed.
In the form of a sifted fraction (about 2-4 mm, approximately 189 kg of pellets per hour are obtained, which have the following properties:
Crush resistance, bar 40 Water content, weight,% 0.2 Formaldehyde content, weight,% 0.6 Impact strength,% 100 Round particle content,% 80 To determine the crush strength, the granule is placed between the plates and the upper plate is subjected to increasing pressure before the destruction of the granules. The content of the round granules is determined by placing the granules on a rotating disk set at an angle of 7.5, and then the percentage of the rolling granules is determined. Impact strength is determined by firing pellets at a plate set at an angle of 45, and measuring sphericity before and after such processing,
The fluidizing air (100 ° C) that comes from the fluidized gas layer and contains urea particles is washed in a wet wash.
.one
vc i poticTHe and on, g1uchan1T rastis; Crss Hf - approx. D (neg.%, which) 5X11 is added to the paciBop urea supplied to the bed. The air entering the drum cooler (BOH), and the air contaminated during sifting passes through a bag filter. The dust of urineHhi thus obtained is melted and added to
urea solution supplied to cji ii i.
Example 2. The urea solution is fed to the fluidized bed of urea particles by the method of Example 1, but a spray device is used (Fig. 4) equipped with two concentric gas feed channels. Through the inner concentric channel (the width of the annular outlet
1.9 mm apertures) air is supplied at a rate of 67 k / h, a temperature of 140 ° C at a pressure of 1.45 bar and an exit velocity of 275 m / s. Through the outer gas concentric channel (width
annular outlet
3.5 mm, angle of convergence 6) air is supplied at a speed of 90 kg / h at a temperature of 120 ° C, a pressure of 1.1 bar and a speed of 125 m / s at the entrance. Other conditions of the method are similar to the conditions of 1,
The results obtained are actually equivalent to the results of Example 1. Example 3. By the method of example
1 99 wt.% Urea solution containing 0.4 wt.% Formaldehyde, with a temperature supplied under a pressure of 5 bar and at a speed of 200 kg / h to a ring fluidized bed granulator (diameter 44 cm) using a spraying device, as indicated in example 1. In addition, air with a temperature of 140 ° C is supplied through a spray device at a speed of 78 kg / h at a pressure of 1.45 bar through a concentric gas channel, the width of the annular outlet of which is 2.3 mm and the angle of convergence 10.
The liquid comes from the central channel in the form of a conical film (We 3000), with a yoronka angle of 87, a film thickness of 240 microns and a speed of 27 m / s, and the air flow comes out at a speed of 260 m / s. The angle of collision between film and air is 56.5.
Other conditions at the time (and after) of the granulation are in fact analogous to those of Example 1.
750
80
0.05
0.4 100
85
51
The finished granules (2-4 mm), obtained after cooling and sieving, have the following properties: Bulk density, kg / n
Crush resistance, bar Water content, weight%
Formaldehyde content, wt.% Impact strength,% Content of round particles,%
Example4. By the method of Example I, a solution of ammonium nitrate (200 kg / h) and a powerful stream of Air (87 kg / h) are continuously fed into an annular granulator with a fluidized bed (diameter 45 cm), in which there is a layer of ammonium nitrate particles of 70 a layer with a temperature of 128 ° C is maintained in a fluidized state by an upwardly directed air flow at a surface speed of 2.1 mUs and a temperature (the spray device of example 1 is used). In addition, solid ammonium nitrate particles obtained by sieving and grinding the granulate discharged from the layer are added to the layer at a rate of 195 kg / h.
Ammonium nitrate feed solution

contains 4.9 wt.% H, O and 0.34 weight
and speeds of 60 kg / h. The flow comes out of the spray device from the speed of COS (NO3) 2 (in terms of CaO) and the device supplies 35 ° at a pressure of 1.6 bar with a temperature of 147 ° C at a supply pressure of 8 bar in the form of a wavy
300 mS,
In addition, a hardness is applied to the bed at a rate of 40 about 148 kg / h.
tapered film (funnel corner 88 film thickness 190 microns, speed 32 m / s, We g 3900).
Powerful air flow is supplied with a temperature of 150 ° C at a supply pressure of 1.6 bar and exits the spray device at a speed of 300 m / s.
Discharged from the layer of granulates with a temperature of about 128 ° C is sieved in a hot state, and the screening fraction with a particle size of more than 4 mm is crushed and returned to
ammonium nitrate particles with a temperature of about 135 ° C, obtained in the screening and grinding section.
The npo-i-granulated material discharged from the bed is sown in a hot condition and the product fraction (2-4 mm) thus obtained is cooled to 35 ° C using a drum cooler. Part of this product is heated five
a layer with a sifted fraction with a size of 50 times and cooled to 15-50 C. Properties
particles less than 2 mm,
The product fraction (2-4 mm) is rapidly cooled to a fluid bed cooler. The granules obtained have the following characteristics:
Nitrogen content, wt.% 34.3 Water content, wt.% 0.06
O
five
50
955
95,100
35
0
Volume, kg / m
Content of K1) coal
particles%
Impact strength,%
Crush resistance bar
Oil absorbing
ability, weight,% 0.48
Example 5. According to the method of Example 4, the ammonium nitrate solution is granulated in a circular granulator with a fluidized bed of 45 cm in diameter at a layer temperature of 138 C.
The p-solution of ammonium nitrate contains 5.2 v "; s.% Water, 0.5 wt.% CaCOj and 2 wt.% Clay. The clay used is a sorbolite product with a particle size of less than 5 microns, consisting mainly of SiO, (73 wt.%) And ACO (14 wt .;; 0 A solution of ammonium nitrate is fed at a rate of 150 kg / h at a temperature of 145 C and a pressure of 7 bar through a spray device, as indicated in example I, but with the exception that the diameter of the liquid outlet in the sprayer 2 mm Liquid comes out in the form of a conical film with a funnel angle of 91, a speed of 30 m / s, a film thickness of 190 microns and Weber number is about 3300.
Mogtsny air stream with a temperature of 147 seconds is fed through a spray of 60 kg / h. The stream exits the spray device from the device at a pressure of 1.6 bar.
ammonium nitrate particles with a temperature of about 135 ° C, obtained in the screening and grinding section.
The npo-i-granulated material discharged from the bed is sown in a hot condition and the product fraction (2-4 mm) thus obtained is cooled to 35 ° C using a drum cooler. Part of this product is heated five
once and cooled to 15-50 C. Properties
The obtained product and the product subjected to fivefold heating-cooling cycles are presented in Table 1, Example, According to the method of Example 1, the urea solution and the solid particles of urea are continuously fed into a rectangular fluidized-bed granulator 2 m long and 1 m wide.
7ГЗ
The granulator is equipped with a perforated bottom plate, 30 spray devices are installed in a coyura, Example 1, The total amount of the urea solution to be applied is approximately 6 tons / h, and the amount of urea particles is 5.5 tons / h. The layer, the bottom plate of which is set at an angle of approximately 3 °, is provided at the lowest point with a pipe-shaped outlet with a check valve.
Other conditions of the method are actually similar to those of Example 1. The total amount of air for spraying is about 2600 kg / h and about 86 kg / h per spray device,
As a fraction (2-4 mm) of the product, when sieving the granulate discharged from the bed and cooled, approximately 5.5 tons of urea granules per hour are obtained, the properties of which actually correspond to the properties of the product of Example 1,
Table 2 presents the output of the commodity fraction and energy consumption.
Examples 1, 2, 3 and 6 relate to the preparation of urea, and examples 4 and 5 refer to the preparation of ammonium nitrate. When producing a uranium by the known method, the energy consumption is 9.1 kWh / t of product.
Example In exactly the same way as in Example 1, 96.6% by weight of a solution of urea containing 0.4% by weight of formaldehyde and having a temperature of 140 ° C is fed under a pressure of 2 bar and at a rate of 200 kg / h into a round a fluidized bed granulator (diameter 36 cm) using a spraying device as described in example 1. In addition, a powerful stream of air is supplied at a temperature under pressure of 1.2 bar. The gas flow rate is chosen such that the ratio g / 1 is 5x10 m
The mass ratio of the gas flow to the liquid material is 0.44. The liquid comes out in the form of a conical film with a vertex angle of 90, at a speed of 13 m / s with a film thickness of 400 microns. The number of Weber is about 200, with this, a reagent is added that reduces the surface tension to a value of 0.0385 I / m. At the exhaust hole, the flow converges.
s
9fifUi
under angle 23. MdinHbiii the stream falls on the film under 70.
The wounds obtained as a product (dimensions 2-A micron 1 (: bpl yutyc as a result of cooling and milking and have the following properties: (.) Lifting density,
Q Crushing strength, bar75 Water content,
weight,% 0.12
The content of formal5 dehyd ;, wt.% 0,4
Resistance to impact,% 100 Content of round granules, Z 80
0
five
0
0
45
50
55
Example 8 In exactly the same way as in example 1, a solution of ammonium nitrate (speed 200 kg / h, temperature 165 C) and a powerful air stream (speed 82 kg / h, temperature 165 C) are fed into a round granulator (diameter 29 cm) with fluidized bed. The layer of particles of ammonium nitrate 80 cm high has a temperature. Temperature provides the presence of a fluidized bed of air.
The ammonium nitrate feed solution contains 4.8 wt.%, 2 wt.% Clay, as described in Example 5, and 0.34 wt.% Ca (LOD) - (calculated on CaO).
The ammonium nitrate solution is fed under a pressure of 11 bar. The ammonium nitrate solution comes out in the form of a wavy conical film, the angle at which the angle is 83 at a film thickness of 100 µm and a speed of 37.1 m / s, while the Weber number is about 5,000. A reagent that reduces the surface tension to 0.040 is also added. P / m
A powerful air flow is introduced at a speed of 466 m / s in such an amount that the ratio of the masses of the gas to the liquid is 0.41. The ratio is 50 -10-m-.
The granules obtained after cooling and sifting as the final product (size - 2-4 mm) have the following properties:
Bulk density
kg / m-9.45
Crush strength, bar45 Water content, weight% 0.07
Resistance to impact,% Content of round granules, Z
The ability to absorb oil, VPS.% Nitrogen, wt,%
formula
100 70
0.60 34.05 invention

权利要求:
Claims (11)
[1]
1. A method of producing granules in a fluidized bed, including the flow of gas upwards through a layer of particles to create a fluidized bed, the flow of fluid into the fluidized bed of particles upwards through the central channel of the spraying device, through a powerful gas flow through the concentric channel. zones in the bed at a linear rate greater than the speed of the gas stream creating a fluidized bed; solidification of the liquid on the particles and removal of the resulting granules from the bed, characterized in that , in order to reduce energy consumption and reduce dust formation, the liquid is supplied under a pressure of 2-11 bar, and the gas flow rate is set according to the ratio
(
6, rfle frati gas density, kg / m;
Vrc (} gas flow rate,
m / s; 6, - surface tension
liquids, N / m,
the liquid is fed from the central channel in the form of a closed conical film with a thickness of 100–400 μm with an axial pressure exceeding the axial pressure of (5–50) 10 m.
A powerful gas stream, which is 45
crushed film
[2]
2. A method according to claim, characterized in that the liquid in the spray device is rotated.
[3]
3. Method according to claims I and 2, about t l and - due to the fact that the angle of the film cone is 50-110.
50
D
where r
V.
R gag - the density of
- speed fluid
m / s;
frg, - density ha VV., - speed ha
[4]
4Dl10Sob according to PP.1 and 2, about tl and - h and y y and n so that the lawn stream serves p nide cone with a funnel angle 5-25.
[5]
5, The method according to PP.1-4, about tl and h and yushi and the fact that the gas stream serves at a speed of 200-350 m / s,
[6]
6. Method according to nn.J-5, about tl and h and y - y and s, tvm, that the mass ratio of the gas stream and the liquid material is 0.25: 1-0.45: 1.
[7]
7. The method according to claims 1-6, of which is y and y with the fact that through the feed channel of a powerful gas stream serves an additional gas stream with a speed less than the speed of a powerful gas stream, but exceeding the speed falling particles. 0
[8]
8. The method according to claim 7, starting with the fact that the additional gas flow has a speed of 50-150 m / s.
[9]
9. The method according to PP, 1-8, is distinguished by 5 u and with the fact that the film has an internal turbulence corresponding to a Weber number of more than 2000, defined. l emoy by the formula (
where p is the density of the liquid material,
V, is the velocity of the liquid material,
m / s;
b — surface tension of a liquid material, N / m; C / - thickness of the film at the outlet of
central channel, micron
[10]
10. The method according to claim 9, characterized by the fact that the velocity of the liquid material is 20-50 m / s,
[11]
11. A method according to any one of claims 1-10, characterized in that the liquid material and gas are fed with rods, defined
We
V i)
five
0
D
where r
V.
8: 1-16: 1,
P gag - DENSITY of the liquid material,
- the speed of the liquid material
m / s;
frg, - gas density, VV., - gas velocity, m / s;
Nitrogen content,%
Water content
weight.%
Bulk density
Round content
particles%
Impact strength,%
Crush resistance bar
Maelon-swallowing
ability, wt.%
189
189
189
189
141.5
5600
329606
1 2 Table
33
0.08
9A6
75,100
AO 0.30
table 2
7.9 7.5 1 1 10 8.5
Fi.g.2
Fi.HZ
13
Editor G.Gerbsr
FIG.
(. (stanita whose R. Gore F; and she
Tehred M. Hsdanichcorrector M.IIIapcain
Order 3498 / 58T-tra, - 10 Subscription
Sovereign Rei.Hci O kg.mito1 i USSR
on itobrtepiy and about 1 kr: T11y 1 13035) G.ogkr, A- J5, G A-i gk, nab., d. 4/5
Production-full-scale P1E (; play, t. Uzhgorod,
ek 1: / ;;; J 4

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同族专利:

公开号 | 公开日

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IN162235B|1988-04-16|

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ZA846636B|1985-04-24|

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JPS6097037A|1985-05-30|

引用文献:

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RU2614682C2|2012-03-14|2017-03-28|Ханивелл Интернешнл Инк.|Method and device for granulation with pressure regulation|US3662960A|1966-11-21|1972-05-16|United Aircraft Corp|Injector head|

JPS4924012B1|1971-03-03|1974-06-20|

US3979069A|1974-10-11|1976-09-07|Luigi Garofalo|Air-atomizing fuel nozzle|

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

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US5236503A|1991-10-28|1993-08-17|Glatt Air Techniques, Inc.|Fluidized bed with spray nozzle shielding|

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US20060286200A1|2005-04-18|2006-12-21|Castro Armando J|Confections containing flavor delivery systems|

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法律状态:

优先权:

申请号 | 申请日 | 专利标题

NL8303000A|NL8303000A|1983-08-27|1983-08-27|METHOD FOR PREPARING GRANULES|

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