EP1094997A1 - Verfahren zur herstellung von harnstoff und ammonsulfat enthaltenden düngemittel-granulaten - Google Patents
Verfahren zur herstellung von harnstoff und ammonsulfat enthaltenden düngemittel-granulatenInfo
- Publication number
- EP1094997A1 EP1094997A1 EP99931067A EP99931067A EP1094997A1 EP 1094997 A1 EP1094997 A1 EP 1094997A1 EP 99931067 A EP99931067 A EP 99931067A EP 99931067 A EP99931067 A EP 99931067A EP 1094997 A1 EP1094997 A1 EP 1094997A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- ammonium sulfate
- urea
- fluidized bed
- melt
- grain
- 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.)
- Withdrawn
Links
- 229910052921 ammonium sulfate Inorganic materials 0.000 title claims abstract description 127
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 title claims abstract description 126
- 235000011130 ammonium sulphate Nutrition 0.000 title claims abstract description 126
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 239000004202 carbamide Substances 0.000 title claims abstract description 43
- 239000008187 granular material Substances 0.000 title claims abstract description 39
- 239000003337 fertilizer Substances 0.000 title claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 15
- 239000002245 particle Substances 0.000 claims abstract description 61
- 238000000034 method Methods 0.000 claims abstract description 58
- 239000000725 suspension Substances 0.000 claims abstract description 52
- 239000000428 dust Substances 0.000 claims abstract description 35
- AOBXGGAGUYYNQH-UHFFFAOYSA-N ammonium sulfate urea Chemical compound [NH4+].[NH4+].NC(N)=O.[O-]S([O-])(=O)=O AOBXGGAGUYYNQH-UHFFFAOYSA-N 0.000 claims abstract description 24
- 238000005469 granulation Methods 0.000 claims abstract description 23
- 230000003179 granulation Effects 0.000 claims abstract description 23
- 238000002347 injection Methods 0.000 claims abstract description 5
- 239000007924 injection Substances 0.000 claims abstract description 5
- 239000000155 melt Substances 0.000 claims description 36
- 230000008569 process Effects 0.000 claims description 28
- 239000007921 spray Substances 0.000 claims description 10
- 239000000126 substance Substances 0.000 claims description 5
- 238000001238 wet grinding Methods 0.000 claims description 4
- 239000006185 dispersion Substances 0.000 claims description 3
- 230000002209 hydrophobic effect Effects 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 2
- 238000000227 grinding Methods 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 239000010419 fine particle Substances 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 3
- 239000002002 slurry Substances 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 229910052717 sulfur Inorganic materials 0.000 description 7
- 239000011593 sulfur Substances 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 6
- 230000005587 bubbling Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 238000000889 atomisation Methods 0.000 description 4
- JBKVHLHDHHXQEQ-UHFFFAOYSA-N epsilon-caprolactam Chemical compound O=C1CCCCCN1 JBKVHLHDHHXQEQ-UHFFFAOYSA-N 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000012188 paraffin wax Substances 0.000 description 3
- 239000002689 soil Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 238000005054 agglomeration Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- OHJMTUPIZMNBFR-UHFFFAOYSA-N biuret Chemical compound NC(=O)NC(N)=O OHJMTUPIZMNBFR-UHFFFAOYSA-N 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000003123 plant toxin Substances 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007493 shaping process Methods 0.000 description 1
- 238000005029 sieve analysis Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 230000007480 spreading Effects 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05C—NITROGENOUS FERTILISERS
- C05C3/00—Fertilisers containing other salts of ammonia or ammonia itself, e.g. gas liquor
Definitions
- ammonium sulfate melts at over 500 ° C, so that granulation from a mixture melt with high ammonium sulfate contents is excluded. Only up to about 20% by weight of ammonium sulfate is soluble in a urea melt at conventional melt temperatures and can therefore be granulated homogeneously.
- US Pat. No. 3,785,796 discloses a process for producing ammonium sulfate-urea granules, with which it is in principle possible to produce granules with an ammonium sulfate content of 30 to 70% by weight.
- Commercially available, unmilled ammonium sulfate is mixed with a urea melt and granulated in an "oil" or "plate” granulator, the corresponding slurry being dripped on. Both types of granulator have the advantage that they work virtually dust-free, so that dust recycling can be omitted.
- a disadvantage of this process is the fact that the granules are of poor quality due to their inhomogeneous structure due to the granulation process.
- the ammonium sulfate particles must therefore be ground very finely so that they are sufficiently wetted with liquid and non-solid ammonium sulfate particles due to the difference in density to the urea solution from the drop to solve.
- the present invention was therefore based on the object of producing a process for producing fertilizer granules containing urea and ammonium sulfate with an ammonium sulfate content of von 60% by weight, which does not have the disadvantages mentioned according to the prior art, but enables the production of homogeneous urea-ammonium sulfate granules with a relatively high proportion of ammonium sulfate, which has good application properties and at the same time can be produced with little technical effort and inexpensively.
- melt suspension comprising ammonium sulfate with an average particle size of 30 to 300 microns and urea in one
- melt suspension formed in stage a) is sprayed onto f one-piece ammonium sulfate-urea particles from below in a fluidized bed granulator with the aid of at least one nozzle, the
- Fluid bed is loosened by a gas, in particular a bubbling air stream in the area of the injection point and then c) the fertilizer granulate formed in the fluid bed is separated off and possibly worked up.
- the process according to the present invention thus comprises at least three reaction stages.
- a melt suspension comprising ammonium sulfate and urea is produced in a temperature range from 120 to 15 ° C., the ammonium sulfate having an average particle size of 30 to 300 ⁇ m.
- the mean particle size is the mean particle size determined with the aid of the sieve analysis.
- the concentration range in which ammonium sulfate can be added to the urea melt depends on the ammonium sulfate particle size and decreases with decreasing particle size due to increases in viscosity.
- ammonium sulfate and urea-containing melt suspension are unproblematic and can be done in various ways.
- preheated ammonium sulfate can be introduced into a urea melt at a preferred temperature of 100 to 150 ° C. and then dispersed.
- the ammonium sulfate has a preferred average particle size of 60 to 150 ⁇ m and the urea melt, in particular a concentration of> 98% by weight.
- ammonium sulfate and urea-containing melt suspension consists in introducing coarse-grained and preheated ammonium sulfate with a preferred temperature of 100 to 150 ° C into the corresponding urea melt, the resulting melt suspension using a wet mill to the average particle size of 30 to 300 ⁇ m, preferably 60 to 1 50 ⁇ m, milled and then dispersed.
- the coarse-grained ammonium sulfate preferably has an average particle size of 0.1 to 2.0 mm.
- the ammonium sulfate in stage a) is introduced into the urea melt by a highly turbulent dispersion. Due to this highly turbulent dispersion, Introducing kinetic energy with the aid of the usual dispersants, the viscosity of the ammonium sulfate-urea melt suspension can be reduced to ⁇ 1 50 cP and, even at high solids contents, kept sufficiently low until atomization. In general, a ratio of ammonium sulfate / urea in the melt suspension according to a) from 45/55 to 55/45 is preferred.
- the melt suspension formed in stage a) is then injected with the aid of a nozzle from below into a fluidized bed granulator onto f-piece ammonium sulfate-urea particles, which preferably have an average particle size of 1.0 to 3.0 mm exhibit.
- Such finely divided ammonium sulfate-urea particles are preferably composed of the return of undersize and comminuted oversize of the granulator product which is customary in granulation.
- the maximum moistening, at which no agglomerates are formed, depends not only on the material properties of the melt suspension, but also on the type of nozzle, its spray pattern and the design of the fluidized bed. Therefore, full cone nozzles with a spray angle of 45 to 90 °, preferably 60, are preferred up to 80 °.
- the nozzles, in particular single-substance nozzles, are preferably charged with 100 to 1,000 kg / h of the melt suspension.
- the height of the fluidized bed in the fluidized bed granulator can be varied within wide limits, but it has proven to be particularly advantageous to set fluidized bed heights of 300 to 600 mm. Fluid bed heights of ⁇ 300 mm reduce the agglomeration rate, but there is a risk of drops blowing through the fluid bed, which leads to a higher dust accumulation in the granulator. With fluidized bed heights> 600 mm there is a risk that the upper layers will no longer be sprayed on and thus only unnecessarily energy will be used to compress the fluidized air.
- the fluidized bed is loosened by a gas stream, in particular a bubbling air stream, in the region of the injection point without atomizing the melt suspension drops.
- a gas stream in particular a bubbling air stream
- This loosening effect is preferably achieved in that the melt nozzles are enveloped by the gas stream, in particular the bubbling air stream, which is preferably 0.75 to 1.5 times
- Nm 3 denotes a normal cubic meter, i.e. a cubic meter under normal conditions.
- the fertilizer granules formed in the fluidized bed are separated off and possibly worked up.
- the fertilizer granulate is separated into three grain fractions with the usual devices, namely into the fine grain with a particle size ⁇ 1.0 mm, in particular ⁇ 1.6 mm, the good grain with a particle size of 1.0 to 5.0 mm, especially 1.6 up to 5.0 mm as well as the coarse grain with a particle size> 5 mm.
- the fine grain is recycled into the fluidized bed reactor in step b), this fine grain preferably being returned to the fluidized bed reactor below the upper edge of the fluidized bed.
- the coarse grain can optionally be ground with a part of the good grain to a preferred average particle size of 1.0 to 3.0 mm and, like the fine grain, can be returned to the fluidized bed granulator.
- the good grain in particular with the preferred particle size of 1.6 to 5.0 mm, can be subjected to a final hydrophobic treatment by customary methods and can be marketed as a salable product in this form. Such hydrophobization can be carried out, for example, with oil / paraffin.
- this problem can be solved by separating the dust formed in granulation stage b) by dry separation, for example with the aid of cyclones or conventional dust filters, into a fine-grain ammonium sulfate-poor and coarse-grain ammonium sulfate-rich fraction.
- the low-ammonium sulfate fraction with an ammonium sulfate content of preferably ⁇ 60% by weight and a preferred grain size of ⁇ 50 ⁇ m is preferably separated with the aid of wet washing and discharged from the process.
- the ammonium sulfate-rich coarse-grained dust fraction with an ammonium sulfate content of preferably> 60% by weight and a particle size of> 50 ⁇ m is either returned directly to the fluidized bed of the granulator and / or after wet grinding of the coarse-grained ammonium sulfate particles to an average particle size of preferably 30 to 300 ⁇ m, in particular 60 to 1 50 / m, combined with the urea-ammonium sulfate melt suspension before the granulation stage b).
- the ammonium sulfate-rich, ground dust fraction is mixed into the urea-ammonium sulfate melt suspension in the storage container for the atomization.
- the process according to the invention proves to be particularly advantageous if part of the ammonium sulfate-rich dust fraction is returned to the fluidized bed granulator and at the same time the other part of this dust fraction is ground and dispersed together with the melt suspension. In this way, the grain size of the granulate can be optimally controlled without the need to comminute good grain. It also significantly reduces the proportion of dust that has to be returned, so that the ammonium sulfate concentration in the melt suspension does not increase by more than 3% by weight compared to the ammonium sulfate concentration in the product.
- homogeneous urea ammonium sulfate granules with a particle size of 1.0 to 5.0 mm, preferably 1.6 to 5.0 mm and an ammonium sulfate content of up to can be obtained in a technically simple and therefore inexpensive manner 60% by weight, preferably up to 55% by weight and at least 30% by weight, preferably at least 4 5% by weight. -%, s o w i e g u t e n L a g e r - and production characteristics. Since it also works in an environmentally friendly manner due to a possible dust recirculation, it is particularly suitable for implementation on a technical scale.
- homogeneous urea-ammonium sulfate granules with an ammonium sulfate content of 30 to 60% by weight can be produced without problems, the grain size of the granules being able to be adjusted in a targeted manner and the dust emissions during granulation being reduced to a minimum.
- This ammonium sulfate-urea melt suspension is fed via line 5 directly into the pump reservoir 6 and from there by means of a pump 8 via the pipeline 9 to the nozzle 10.
- a pressure of 3.5 bar is set by means of the pressure control valve 7.
- a single-component nozzle 10 sprays 875 kg / h of the melt suspension into the fluidized bed of the granulator 11.
- the full cone nozzle 1 0 produces an average drop diameter of 370 ⁇ m at a spray angle of 61 °.
- the nozzle is located at the level of the sieve base on which the fluidized bed is built and sprays from below into the bed, which has a height of 350 mm, at a speed of 29 m / s.
- the fluidized bed is generated by an empty pipe speed of 1.8 m / s.
- the nozzle 10 is located in a bubble air tube 1 3, where 900 Nm 3 / h bubble air are blown in via line 14 at a speed of 20 m / s in order to loosen up the fluidized bed at the injection point.
- the granules with an average diameter of 3.2 mm are drawn off via chute 15 and fed to the sieve 16, where the product is separated into three fractions. 350 kg / h of fine product ⁇ 2.5 mm are recycled into the granulator 11 via the conveying path 17 as below the upper edge of the fluidized bed and form the fluidized bed.
- the waste air obtained in the granulator 11 comes via channel 22 into the cyclone 23, where 60 kg / h of dust with a concentration of 82% by weight of ammonium sulfate are separated off. From the cyclone exhaust air 5 kg / h of dust with an ammonium sulfate concentration of 60% by weight and a grain size ⁇ 60 ⁇ m pass through line 24 into a wet scrubber (not shown).
- the dust separated in the cyclone is fed via the conveyor section 25 into the wet mill 26, where the ammonium sulfate particles in the ammonium sulfate-urea melt suspension circulated via line 27 are ground in a highly turbulent manner to an average diameter of 100 ⁇ m.
- the highly concentrated ammonium sulfate-urea melt suspension reaches the storage container 6 via pipeline 28.
- Example 2 proceeds as described in Example 1, except that part of the highly concentrated ammonium sulfate dust deposited in the cyclone 23 is 250 mm below the upper edge of the fluidized bed is introduced. Of the 60 kg / h of ammonium sulfate-rich dust separated in the cyclone 23, 20 kg / h are introduced directly into the granulator 11. As a result, the average particle size of the granules produced drops from 3.8 to 3.4 mm and the supply of 20 kg / h of good grain from the crusher 20 is eliminated. The amount of dust fed to the wet mill 26 is reduced to 40 kg / h, so that only 855 kg / h of melt suspension have to be atomized. The ammonium sulfate content of the melt suspension which is conveyed to the nozzles is reduced from 52.8% to 52.2% by weight.
- ammonium sulfate crystals 507 kg / h of commercially available ammonium sulfate crystals (particle size 0.1 to 1.0 mm) are fed via line 1 to pin mill 2 and ground there to an average particle size of 95 ⁇ m.
- the ammonium sulfate particles reach the heating screw 4 via line 3, where they are heated to 1,35 ° C. by means of steam from line 5.
- the ammonium sulfate particles reaching the mixer 8 via the pipeline 6 are mixed with 504 kg / h urea prills, which are fed in via the line 7.
- the solid urea melts in the presence of ammonium sulfate by supplying heat to the mixer.
- the melt suspension with a temperature of 1 30 ° C is withdrawn via pipe 9 from the pump 10 and conveyed via line 1 1 to the disperser 1 2, where the viscosity is reduced to 100 cP by introducing shear forces between stationary and rotating pins, so that the melt suspension becomes fluid.
- the melt suspension passes through the pipes 1 5a and 1 5b to two full cone nozzles 1 7 and 1 8, each with a capacity of 505.5 kg / h.
- pressure control valve 1 3 in line 14 By means of pressure control valve 1 3 in line 14, a pre-pressure of 3 bar set.
- the nozzles 1 7 and 1 8 spray the melt suspension with a spray angle of 70 ° into the fluidized bed of the granulator 1 9 at a speed of 29 m / s (measured at a distance of 1 0 cm from the nozzle outlet opening), droplets having an average diameter of 41 0 ⁇ m arise.
- the drops are injected from below into a fluidized bed, which is 450 mm above the nozzles.
- the fluidized bed is generated at an empty pipe speed of 1.9 m / s.
- the nozzles 1 7 and 1 8 are located in bubbling air pipes 21 and 22, where 550 Nm 3 / h of bubbling air are blown in via the pipe 1 6 at an empty pipe speed of 28 m / s, around the nozzles, at the points where there are nozzles to loosen the fluidized bed.
- the finished granulate is discharged via the centrally arranged discharge line 23. Air is blown into this discharge line via line 24 and discharged with an air quantity of 560 Nm 3 / h of granules with an average particle size of 3.0 mm.
- the granulate passes through the rotary valve 25 and the chute 26 to the sieve 27, where the product is separated into three fractions.
- 80 kg / h of fine product ⁇ 1 mm returns to the granulator 19 via the conveying path 28.
- 40 kg / h of coarse grain> 5 mm is fed via line 29 to the roller crusher 30 and broken there to an average diameter of 2 mm. The broken product returns to the granulator 19 via lines 31 and 28 and forms the fluidized bed here.
- the finished product (1 001 kg / h) arrives via pipe 32 from the plant with an ammonium sulfate content of 50% by weight and is stored with an oil / paraffin mixture after it has been made hydrophobic.
- the exhaust air obtained in the granulator 1 9 reaches the bag filter 34 via pipe 33, where dust particles> 50 ⁇ m are separated.
- 1,50 kg / h of dust with a concentration of 85% by weight of ammonium sulfate are piped in 35 250 mm below the upper edge of the fluidized bed returned the granulator 19.
- 10 kg / h of dust ⁇ 50 microns with a concentration of 60 wt .-% ammonium sulfate emits from the bag filter 34 via line 36 or is led to the wet wash, not shown.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Fertilizers (AREA)
- Glanulating (AREA)
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19826570 | 1998-06-15 | ||
DE19826570A DE19826570C2 (de) | 1998-06-15 | 1998-06-15 | Verfahren zur Herstellung von Harnstoff und Ammonsulfat enthaltenden Düngemittel-Granulaten |
PCT/EP1999/004094 WO1999065845A1 (de) | 1998-06-15 | 1999-06-14 | Verfahren zur herstellung von harnstoff und ammonsulfat enthaltenden düngemittel-granulaten |
Publications (1)
Publication Number | Publication Date |
---|---|
EP1094997A1 true EP1094997A1 (de) | 2001-05-02 |
Family
ID=7870912
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP99931067A Withdrawn EP1094997A1 (de) | 1998-06-15 | 1999-06-14 | Verfahren zur herstellung von harnstoff und ammonsulfat enthaltenden düngemittel-granulaten |
Country Status (10)
Country | Link |
---|---|
US (1) | US6179893B1 (bg) |
EP (1) | EP1094997A1 (bg) |
JP (1) | JP4459326B2 (bg) |
BG (1) | BG105040A (bg) |
CZ (1) | CZ20004733A3 (bg) |
DE (1) | DE19826570C2 (bg) |
EE (1) | EE200000753A (bg) |
NO (1) | NO20006283L (bg) |
PL (1) | PL344857A1 (bg) |
WO (1) | WO1999065845A1 (bg) |
Families Citing this family (34)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE10001082B4 (de) | 2000-01-13 | 2004-11-18 | Skw Stickstoffwerke Piesteritz Gmbh | Verfahren zur Herstellung eines Ammoniumsulfat und Harnstoff enthaltenden Düngemittels |
JP4535556B2 (ja) * | 2000-03-31 | 2010-09-01 | 株式会社大川原製作所 | 造粒乾燥方法並びに流動層造粒乾燥機 |
US8042740B2 (en) * | 2000-11-24 | 2011-10-25 | Metrologic Instruments, Inc. | Method of reading bar code symbols on objects at a point-of-sale station by passing said objects through a complex of stationary coplanar illumination and imaging planes projected into a 3D imaging volume |
DE10102274A1 (de) * | 2001-01-18 | 2002-08-08 | Ge Bayer Silicones Gmbh & Co | Harnstoffhaltige Zusammensetzung, Verfahren zu ihrer Herstellung und deren Verwendung |
JP2002306944A (ja) * | 2001-04-12 | 2002-10-22 | Okawara Mfg Co Ltd | 造粒乾燥方法並びに流動層造粒乾燥装置 |
DE102004005907B4 (de) * | 2004-02-05 | 2006-01-05 | Uhde Gmbh | Anlage zur Herstellung von biuretarmem harnstoffhaltigem Düngemittelgranulat |
NL1025954C2 (nl) * | 2004-04-15 | 2005-10-18 | Dsm Ip Assets Bv | Werkwijze voor het optimaliseren van een fluïdbed granulator. |
WO2009009049A2 (en) * | 2004-10-20 | 2009-01-15 | Vertiflex, Inc. | Interspinous spacer |
CA2600771C (en) * | 2005-04-18 | 2016-06-07 | Dsm Ip Assets B.V. | Process for the production of urea-comprising particles |
DE102007061408A1 (de) * | 2007-12-11 | 2009-06-18 | Sandvik Materials Technology Deutschland Gmbh | Verfahren und Tropfenformer zum Herstellen von Pastillen sowie Verfahren zum Herstellen eines schwefelhaltigen Düngers |
EP2253374A1 (en) * | 2009-05-20 | 2010-11-24 | Stamicarbon B.V. | Process for producing granules |
JP5399276B2 (ja) * | 2010-01-19 | 2014-01-29 | 日本電信電話株式会社 | コンテンツ配信システムと方法およびプログラム |
EP2431346A1 (en) * | 2010-09-15 | 2012-03-21 | Uhde Fertilizer Technology B.V. | Method for producing urea fertilizer with low moisture absorption tendencies |
WO2013019935A2 (en) | 2011-08-04 | 2013-02-07 | Mos Holdings Inc. | Compacted muriate of potash fertilizers containing nutrients and methods of making same |
CN102887777A (zh) * | 2012-10-25 | 2013-01-23 | 新疆禾稼欢肥业科技有限责任公司 | 多肽氮肥 |
RU2711444C2 (ru) * | 2013-03-14 | 2020-01-17 | Дзе Мозаик Компани | Комплексное удобрение и способ его изготовления |
US9174885B2 (en) | 2013-03-15 | 2015-11-03 | University Of Kentucky Research Foundation | Nitrogen fertilizer composition and method to improve detection and lessen the explosive potential of nitrogen-based fertilizers |
CN104072260B (zh) * | 2014-05-29 | 2016-06-22 | 苏州上研化肥科技发展有限公司 | 一种生产复合肥料的生产*** |
DE102014108703A1 (de) | 2014-06-20 | 2015-12-24 | Thyssenkrupp Ag | Harnstoffzusammensetzung und Verfahren zu ihrer Herstellung |
WO2016012925A1 (en) * | 2014-07-20 | 2016-01-28 | Sabic Global Technologies B.V. | Methods for determining low sulfate concentrations in synthetic urea samples, produced in a manufacturing process and containing high levels of impurities |
EA032243B1 (ru) * | 2015-07-06 | 2019-04-30 | Стамикарбон Б.В. | Гранулирование карбамидных продуктов |
MA42900A (fr) | 2015-07-07 | 2018-05-16 | Yara Int Asa | Procédé de fabrication de matériau particulaire à base d'urée contenant du soufre élémentaire |
CN109071370B (zh) | 2015-09-08 | 2022-11-22 | 雅苒国际集团 | 改进的基于尿素硫酸铵的组合物及其制备方法 |
JOP20190228A1 (ar) | 2017-03-31 | 2019-09-30 | Mosaic Co | أسمدة تحتوي على مصادر سريعة و بطيئة لاطلاق البورون |
EP3461803A1 (de) * | 2017-10-02 | 2019-04-03 | Evonik Degussa GmbH | Herstellverfahren für dipeptidhaltige granulate |
EP3542899A1 (en) * | 2018-03-20 | 2019-09-25 | Yara International ASA | Method and reactor for producing urea ammonium sulphate |
PL3768416T3 (pl) * | 2018-03-23 | 2023-03-06 | Thyssenkrupp Fertilizer Technology Gmbh | Układ granulatora ze złożem fluidalnym z materiałem powłokowym zapobiegającym nagromadzaniu się pyłu w układach powietrza instalacji do granulacji mocznika |
EP3567018A1 (en) | 2018-05-07 | 2019-11-13 | Yara International ASA | Improved urea ammonium sulphate-based composition and method for the manufacture thereof |
EP3567019A1 (en) | 2018-05-09 | 2019-11-13 | Yara International ASA | Improved urea-based blend composition and method for the manufacture thereof |
EP3567020A1 (en) | 2018-05-11 | 2019-11-13 | Yara International ASA | Improved urea-based composition comprising elemental sulphur and method for the manufacture thereof |
EP3593898B1 (en) * | 2018-07-13 | 2021-09-01 | thyssenkrupp Fertilizer Technology GmbH | Producing fertilizer granules with a defined size distribution |
EP3821716A1 (en) | 2019-11-15 | 2021-05-19 | Yara International ASA | Urea ammonium sulphate-based composition and method for the manufacture thereof |
EP3907208A1 (en) | 2020-05-08 | 2021-11-10 | Yara International ASA | Urea ammonium sulfate-based composition |
DE102021108187A1 (de) | 2021-03-31 | 2022-10-06 | Skw Stickstoffwerke Piesteritz Gmbh | Granuliertes pH-neutrales Harnstoff-Ammoniumsulfat-Düngemittel mit Ureaseinhibitor |
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Publication number | Priority date | Publication date | Assignee | Title |
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US3785796A (en) | 1972-01-27 | 1974-01-15 | Tennessee Valley Autority | Production of urea-ammonium sulfate |
US3928015A (en) * | 1974-10-29 | 1975-12-23 | Tennessee Valley Authority | Manufacture of urea-ammonium sulate from sulfuric acid, ammonia, and urea |
JPS5855807B2 (ja) * | 1979-10-08 | 1983-12-12 | 三井東圧化学株式会社 | 造粒方法 |
NL191557C (nl) * | 1980-05-12 | 1995-09-19 | Azote Sa Cie Neerlandaise | Werkwijze voor het vervaardigen van uit een kern en een omhulling opgebouwde korrels. |
JPS6274443A (ja) * | 1985-09-27 | 1987-04-06 | Toyo Eng Corp | 粒子の加工方法 |
NL8502838A (nl) * | 1985-10-17 | 1987-05-18 | Azote Sa Cie Neerlandaise | Werkwijze ter vervaardiging van ureum en ammoniumsulfaat bevattende meststofkorrels. |
NL8700913A (nl) | 1987-04-16 | 1988-11-16 | Nl Stikstof | Werkwijze voor het vervaardigen van kunstmestgranules. |
NL1002862C2 (nl) * | 1996-04-15 | 1997-10-17 | Dsm Nv | Werkwijze voor het bereiden van granules. |
DE19706433A1 (de) * | 1997-02-19 | 1998-08-20 | Glatt Ingtech Gmbh | Verfahren zur Herstellung von Schmelzsuspensionen, Emulsionen oder Lösungen |
DE19724142B4 (de) * | 1997-06-07 | 2007-04-19 | Glatt Ingenieurtechnik Gmbh | Verfahren zur Herstellung von granuliertem Mischdünger |
NZ331531A (en) * | 1997-09-04 | 2000-01-28 | Toyo Engineering Corp | method for granulation and granulator |
DE19744404A1 (de) * | 1997-10-08 | 1999-04-15 | Piesteritz Stickstoff | Verfahren zur Herstellung von Dicyandiamid enthaltenden Harnstoff-Düngemittel-Granulaten |
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1998
- 1998-06-15 DE DE19826570A patent/DE19826570C2/de not_active Expired - Lifetime
-
1999
- 1999-06-11 US US09/330,473 patent/US6179893B1/en not_active Expired - Lifetime
- 1999-06-14 PL PL99344857A patent/PL344857A1/xx unknown
- 1999-06-14 EE EEP200000753A patent/EE200000753A/xx unknown
- 1999-06-14 EP EP99931067A patent/EP1094997A1/de not_active Withdrawn
- 1999-06-14 WO PCT/EP1999/004094 patent/WO1999065845A1/de not_active Application Discontinuation
- 1999-06-14 CZ CZ20004733A patent/CZ20004733A3/cs unknown
- 1999-06-14 JP JP16748799A patent/JP4459326B2/ja not_active Expired - Fee Related
-
2000
- 2000-12-11 NO NO20006283A patent/NO20006283L/no not_active Application Discontinuation
- 2000-12-11 BG BG105040A patent/BG105040A/bg unknown
Non-Patent Citations (1)
Title |
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See references of WO9965845A1 * |
Also Published As
Publication number | Publication date |
---|---|
BG105040A (bg) | 2001-07-31 |
US6179893B1 (en) | 2001-01-30 |
PL344857A1 (en) | 2001-11-19 |
DE19826570A1 (de) | 1999-12-23 |
EE200000753A (et) | 2002-04-15 |
NO20006283L (no) | 2001-02-12 |
WO1999065845A1 (de) | 1999-12-23 |
NO20006283D0 (no) | 2000-12-11 |
CZ20004733A3 (cs) | 2002-01-16 |
JP2000044371A (ja) | 2000-02-15 |
DE19826570C2 (de) | 2002-10-31 |
JP4459326B2 (ja) | 2010-04-28 |
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