WO2006111331A1 - Process for the production of urea-comprising particles - Google Patents

Process for the production of urea-comprising particles Download PDF

Info

Publication number
WO2006111331A1
WO2006111331A1 PCT/EP2006/003450 EP2006003450W WO2006111331A1 WO 2006111331 A1 WO2006111331 A1 WO 2006111331A1 EP 2006003450 W EP2006003450 W EP 2006003450W WO 2006111331 A1 WO2006111331 A1 WO 2006111331A1
Authority
WO
WIPO (PCT)
Prior art keywords
urea
belt
particles
liquid
particle
Prior art date
Application number
PCT/EP2006/003450
Other languages
French (fr)
Inventor
Jan Wiebe Werf Van Der
Marc Jozeph Brouwer
Original Assignee
Dsm Ip Assets B.V.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Dsm Ip Assets B.V. filed Critical Dsm Ip Assets B.V.
Priority to AU2006237137A priority Critical patent/AU2006237137B8/en
Priority to EP06724336.0A priority patent/EP1868963B1/en
Priority to CN2006800128719A priority patent/CN101160271B/en
Priority to EA200702262A priority patent/EA011329B1/en
Priority to CA2600771A priority patent/CA2600771C/en
Priority to US11/918,233 priority patent/US7700012B2/en
Priority to JP2008506981A priority patent/JP5649781B2/en
Publication of WO2006111331A1 publication Critical patent/WO2006111331A1/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
    • B01J2/26—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic on endless conveyor belts
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05C—NITROGENOUS FERTILISERS
    • C05C9/00—Fertilisers containing urea or urea compounds
    • C05C9/005—Post-treatment
    • C—CHEMISTRY; METALLURGY
    • C05—FERTILISERS; MANUFACTURE THEREOF
    • C05G—MIXTURES OF FERTILISERS COVERED INDIVIDUALLY BY DIFFERENT SUBCLASSES OF CLASS C05; MIXTURES OF ONE OR MORE FERTILISERS WITH MATERIALS NOT HAVING A SPECIFIC FERTILISING ACTIVITY, e.g. PESTICIDES, SOIL-CONDITIONERS, WETTING AGENTS; FERTILISERS CHARACTERISED BY THEIR FORM
    • C05G5/00—Fertilisers characterised by their form
    • C05G5/10—Solid or semi-solid fertilisers, e.g. powders
    • C05G5/12—Granules or flakes

Definitions

  • the invention is directed to a process for the production of urea- comprising particles.
  • Known and frequently used processes for the production of urea- comprising particles are prilling and granulation.
  • Prilling is performed in a prilling tower wherein a urea-comprising liquid is sprayed in the form of fine droplets. On their way down these droplets are cooled and solidified by rising air. At the bottom of the prilling tower the solid particles are collected.
  • Granulation of a urea-comprising liquid can take place in different types of granulation equipment. Seed particles are added to the granulation equipment and are kept moving within the granulation equipment. The urea-comprising liquid is sprayed over the seed particles and cooled. In this way the seed particles grow to obtain urea granules.
  • a drawback of the above-described processes is that by spraying of the urea-comprising solution fine dust is formed that is collected into the cooling air.
  • the large amount of cooling air used during prilling and granulation must be cleaned of most of the dust before it can be discharged into the environment.
  • prilling and granulation For prilling and granulation the use of a lot of cooling air is required. This results in a high energy consumption. Moreover, prilling and granulation are environmentally unfriendly processes, because of the dust formation during these processes. The aim of the present invention is to eliminate these drawbacks.
  • the urea-comprising particles are produced in a pelletizer, comprising a feeding device, a belt and a device to remove the formed pellets from the belt, by feeding a urea-comprising liquid to the feeding device from which droplets of the urea- comprising liquid are dosed to the belt, whereon the urea-comprising droplets solidify and cool to a temperature of ⁇ 55 °C, whereafter the formed urea-comprising particles are removed from the belt.
  • urea-comprising particles are formed without the need to spray fine droplets and without the use of cooling air that is in direct contact with the particles. In this way an air stream comprising urea dust is not formed.
  • a further advantage of the use of a pelletizer is that particles are obtained with a uniform, predetermined shape and composition.
  • a pelletizer comprises a feeding device, a belt and a device to remove the formed pellets from the belt.
  • a pelletizer is, for instance, described as an endless-belt system in the Encyclopedia of Chemical Technology, Fourth Edition, vol. 22, p. 244 and 245.
  • the urea-comprising liquid is fed to the feeding device.
  • the feeding device can, for instance, comprise a screen with holes through which the urea- comprising liquid is pressed.
  • the feeding device is located above the belt and the urea- comprising liquid is dosed through the holes in the screen at the bottom of the feeding device. In this way droplets of urea-comprising liquid are formed on the belt.
  • the feeding device can, for instance, be a perforated cylindrical drum, which rotates and which doses droplets to the belt at the bottom of the cylindrical drum.
  • the belt can be a continuous belt that moves away from the feeding device with the urea-comprising droplets on it. The part of the belt after the feeding device is cooled indirectly by, for instance, cooling water.
  • urea-comprising particles solidify on the belt and are removed as urea-comprising particles from the belt after solidifcation.
  • the urea-comprising particles are normally removed from the belt by scraping, but other ways known to the man skilled in the art to remove the particles can also be used.
  • the urea-comprising liquid leaves the feeding device, normally, with a temperature above the melting point of urea.
  • the melting point of urea is a temperature of 135 ° C.
  • the urea-comprising liquid leaves the feeding device at a temperature of 135-140 ° C.
  • On the belt the droplets are cooled and solidified to a temperature of ⁇ 55 ° C.
  • the urea-comprising particles are removed from the belt.
  • the urea-comprising particles are not solid enough to handle. The particles break easily and dust will be present in the final product. The presence of dust promotes caking of the particles during shipment and storage.
  • the temperature of the particles can be influenced by the speed of the belt, the length of the belt and by the temperature and amount of the cooling medium.
  • a release agent can be applied to the belt after removal of the solidified particles from the belt and before the droplets are dosed to the belt. It can also be necessary to clean the belt from remains of the urea-comprising particles. This can, for instance, be done by scraping off the remains of the particles after wetting.
  • the urea-comprising particles that are obtained are not spherical, such as the particles resulting from prilling and granulation, but are flat at the side of the particle that contacts the belt.
  • the particles have a height/diameter ratio (h/d ratio) of 0.99 to 0.1.
  • the 'diameter of the particle' is the diameter of the flat side of the particle.
  • particles with a h/d ratio between 0.7 and 0.3 are formed. This because of a higher bulk density and a lower chance of caking of the particles during transport.
  • the urea-comprising liquid can be defined as any liquid comprising urea in a dissolved, dispersed or liquid form.
  • the liquid can thus be a urea-comprising solution, a urea-comprising slurry or a urea-comprising melt.
  • the urea-comprising liquid is a urea melt. More preferably the urea melt comprises > 99 wt. % urea and most preferably > 99.7 wt. % urea.
  • a urea-comprising solution can also comprise other substances or be a mixture of urea with one or more other substances.
  • the amount of urea in the urea- comprising liquid is preferably between 20 and 100 wt. %.
  • the urea-comprising liquid can contain an additive. Because the particles obtained in the pelletizer have a uniform composition each particle contains the same amount of additive.
  • the additives can be mixed with the urea-comprising liquid before the pelletizer, whereafter the additives are evenly distributed in the particle.
  • additives are, for instance, formaldehyde and urea- formaldehyde reaction products, micronutrients and nitrification and urease inhibitors.
  • Formaldehyde solutions can be added as such or formaldehyde can be reacted with urea to form a reaction product of urea and formaldehyde.
  • micronutrients are boron, manganese, iron, zinc, copper and molybdenum.
  • the micronutrients can be present in the urea-comprising liquid as salts, (sulphates, chloride, nitrates), as oxides or as very small metal particles (flour).
  • nitrification inhibitors are, for instance, pyridines, dicyandiamide and pyrazoles.
  • urease inhibitors are, for instance, phosphoric triamides and ammonium thiosulphate.
  • the urea-comprising liquid can also comprise another fertilizer. -A-
  • fertilizers are, for instance, ammonium sulphate and various phosphates, like monoammonium phosphate, diammonium phospate and nitrophosphate.
  • An advantage of the use of a pelletizer is that slurries with a high amount of solid can still be pelletized. Such slurries can not easily be sprayed in a prilling tower or a granulator.
  • Ammonium sulphate is, up to an amount of 30 wt.% soluble in urea and liquids containing such an amount of ammonium sulphate can be prilled or granulated. A higher amount of ammonium sulphate will be present as a solid in the mixture. The mixture will then be a slurry.
  • a urea/ ammonium sulphate mixture with > 30 wt.% of ammonium sulphate can be pelletized with the process according to the invention, but can not easily be sprayed in a prilling tower or a granulator.
  • the urea-comprising particles that are obtained can be coated after leaving the pelletizer.
  • Coating means applying to the particle a thin layer to reduce the caking tendency.
  • coatings are fine, inert powders, wax, oil and polymers.
  • fine, inert powders are kieselguhr, talcum, lime kaolin and sulfur.
  • wax are polyethylene waxes, parafins, fatty amines and sulfonates.
  • polymer coatings are poly(vinylidene chloride) (PVDC) coatings, polyolefins (polyethylene, polypropylene and ethylene copolymers), polyurethane, urea-formaldehyde resins, polyesters and alkyd resins.
  • PVDC poly(vinylidene chloride)
  • the obtained urea-comprising particles can be used as a fertilizer.
  • the urea-comprising particles according to the invention can be used as such or be mixed with other fertilizer particles with about the same shape and size to be spread together over the field in one fertilizer spreading apparatus.
  • the crushing strength was determined with the apparatus LRX+ Material Testing Systems of Lloyd Instruments.
  • a particle of the sample was placed in the centre of the pressing table of the crushing tester.
  • the particle was placed in such a way that the flat side of the particle is the side on which the pressure was enforced.
  • the particle was subjected to a force, which is increased at a constant rate.
  • the force applied at the moment at which the particle was crushed is determined and is the crushing strength of the particle.
  • the crushing strength was determined in Newton (N).
  • Example I In a Rotoform apparatus of Sandvik Process Systems a urea melt was pelletized.
  • the Rotoform apparatus had a belt width of 600 mm and a cooling length of 11 m.
  • the urea melt with a urea content of 99.8 wt.% was fed to the feeding device of the pelletizer.
  • the urea melt was dosed to the belt with a temperature of 137 ° C.
  • the belt was rotating with a speed of about 50 m/min.
  • the belt was cooled with cooling water with a temperature of about 22 ° C and with a flow of 6,5-9 m 3 /h.
  • the urea pellets that were formed were scraped off at the turning point of the belt.
  • the urea pellets had a temperature of 32-38 ° C, a diameter of 3.15-4.00 mm and a height of 2.0 mm.
  • the crushing strength of the pellets was 15 N.
  • Example II With the urea pellets obtained according to Example I a spreading test was performed. The urea pellets were fed to a fertilizer speading apparatus, type ZA-M Maxi S 1500 of Amazone. A working width of 24 m could be realized.
  • a urea melt was pelletized.
  • the Rotoform apparatus had a belt width of 600 mm and a cooling length of 11 m.
  • the urea melt with a urea content of 99.8 wt.% was fed to the feeding device of the pelletizer.
  • the urea melt was dosed to the belt with a temperature of 150 ° C.
  • the belt was rotating with a speed of about 90 m/min.
  • the belt was cooled with cooling water with a temperature of about 22 ° C and with a flow of 8,5-10 m 3 /h.
  • the urea pellets that were formed were scraped off at the turning point of the belt.
  • the urea pellets had a temperature of 56-59 ° C, a diameter of 3.5-5.4 mm and a height of
  • the urea pellets could be removed from the belt, but there was a lot of dust formed during removal of the pellets from the belt. The pellets showed caking after storage.

Abstract

Process for the production of urea-comprising particles, wherein the urea-comprising particles are produced in a pelletizer, comprising a feeding device, a belt and a device to remove the formed pellets from the belt, by feeding a urea- comprising liquid to the feeding device from which droplets of the urea-comprising liquid are dosed to the belt, whereon the urea-comprising droplets solidify and cool to a temperature of ≤ 55°C, whereafter the formed urea-comprising particles are removed from the belt.

Description

PROCESS FOR THE PRODUCTION OF UREA-COMPRISING PARTICLES
The invention is directed to a process for the production of urea- comprising particles. Known and frequently used processes for the production of urea- comprising particles are prilling and granulation. Prilling is performed in a prilling tower wherein a urea-comprising liquid is sprayed in the form of fine droplets. On their way down these droplets are cooled and solidified by rising air. At the bottom of the prilling tower the solid particles are collected. Granulation of a urea-comprising liquid can take place in different types of granulation equipment. Seed particles are added to the granulation equipment and are kept moving within the granulation equipment. The urea-comprising liquid is sprayed over the seed particles and cooled. In this way the seed particles grow to obtain urea granules.
These processes are, for instance, described in Ullmann's Encyclopedia of Industrial Chemistry, 2002 in the chapters relating to Urea and Fertilizer Granulation.
A drawback of the above-described processes is that by spraying of the urea-comprising solution fine dust is formed that is collected into the cooling air. The large amount of cooling air used during prilling and granulation must be cleaned of most of the dust before it can be discharged into the environment.
For prilling and granulation the use of a lot of cooling air is required. This results in a high energy consumption. Moreover, prilling and granulation are environmentally unfriendly processes, because of the dust formation during these processes. The aim of the present invention is to eliminate these drawbacks.
This aim is achieved with the process according to the present invention wherein the urea-comprising particles are produced in a pelletizer, comprising a feeding device, a belt and a device to remove the formed pellets from the belt, by feeding a urea-comprising liquid to the feeding device from which droplets of the urea- comprising liquid are dosed to the belt, whereon the urea-comprising droplets solidify and cool to a temperature of ≤ 55 °C, whereafter the formed urea-comprising particles are removed from the belt.
In a pelletizer urea-comprising particles are formed without the need to spray fine droplets and without the use of cooling air that is in direct contact with the particles. In this way an air stream comprising urea dust is not formed.
A further advantage of the use of a pelletizer is that particles are obtained with a uniform, predetermined shape and composition. A pelletizer comprises a feeding device, a belt and a device to remove the formed pellets from the belt. A pelletizer is, for instance, described as an endless-belt system in the Encyclopedia of Chemical Technology, Fourth Edition, vol. 22, p. 244 and 245.
The urea-comprising liquid is fed to the feeding device. The feeding device can, for instance, comprise a screen with holes through which the urea- comprising liquid is pressed. The feeding device is located above the belt and the urea- comprising liquid is dosed through the holes in the screen at the bottom of the feeding device. In this way droplets of urea-comprising liquid are formed on the belt. The feeding device can, for instance, be a perforated cylindrical drum, which rotates and which doses droplets to the belt at the bottom of the cylindrical drum. The belt can be a continuous belt that moves away from the feeding device with the urea-comprising droplets on it. The part of the belt after the feeding device is cooled indirectly by, for instance, cooling water. Other media to cool the belt indirectly are, for instance, air and other liquids. The droplets solidify on the belt and are removed as urea-comprising particles from the belt after solidifcation. The urea-comprising particles are normally removed from the belt by scraping, but other ways known to the man skilled in the art to remove the particles can also be used.
The urea-comprising liquid leaves the feeding device, normally, with a temperature above the melting point of urea. The melting point of urea is a temperature of 135 °C. Normally, the urea-comprising liquid leaves the feeding device at a temperature of 135-140 °C. On the belt the droplets are cooled and solidified to a temperature of < 55 °C. Thereafter the urea-comprising particles are removed from the belt. At a temperature of more than 55 °C the urea-comprising particles are not solid enough to handle. The particles break easily and dust will be present in the final product. The presence of dust promotes caking of the particles during shipment and storage.
The temperature of the particles can be influenced by the speed of the belt, the length of the belt and by the temperature and amount of the cooling medium. For easy removal of the urea-comprising particles from the belt a release agent can be applied to the belt after removal of the solidified particles from the belt and before the droplets are dosed to the belt. It can also be necessary to clean the belt from remains of the urea-comprising particles. This can, for instance, be done by scraping off the remains of the particles after wetting. The urea-comprising particles that are obtained are not spherical, such as the particles resulting from prilling and granulation, but are flat at the side of the particle that contacts the belt. The particles have a height/diameter ratio (h/d ratio) of 0.99 to 0.1. The 'diameter of the particle' is the diameter of the flat side of the particle. Preferably, particles with a h/d ratio between 0.7 and 0.3 are formed. This because of a higher bulk density and a lower chance of caking of the particles during transport.
The urea-comprising liquid can be defined as any liquid comprising urea in a dissolved, dispersed or liquid form. The liquid can thus be a urea-comprising solution, a urea-comprising slurry or a urea-comprising melt. Preferably, the urea-comprising liquid is a urea melt. More preferably the urea melt comprises > 99 wt. % urea and most preferably > 99.7 wt. % urea.
A urea-comprising solution can also comprise other substances or be a mixture of urea with one or more other substances. The amount of urea in the urea- comprising liquid is preferably between 20 and 100 wt. %. The urea-comprising liquid can contain an additive. Because the particles obtained in the pelletizer have a uniform composition each particle contains the same amount of additive.
It is an advantage of the process according to the invention that the additives can be mixed with the urea-comprising liquid before the pelletizer, whereafter the additives are evenly distributed in the particle.
Examples of additives are, for instance, formaldehyde and urea- formaldehyde reaction products, micronutrients and nitrification and urease inhibitors. Formaldehyde solutions can be added as such or formaldehyde can be reacted with urea to form a reaction product of urea and formaldehyde. Examples of micronutrients are boron, manganese, iron, zinc, copper and molybdenum. The micronutrients can be present in the urea-comprising liquid as salts, (sulphates, chloride, nitrates), as oxides or as very small metal particles (flour). Examples of nitrification inhibitors are, for instance, pyridines, dicyandiamide and pyrazoles. Examples of urease inhibitors are, for instance, phosphoric triamides and ammonium thiosulphate. The urea-comprising liquid can also comprise another fertilizer. -A-
Examples of other fertilizers are, for instance, ammonium sulphate and various phosphates, like monoammonium phosphate, diammonium phospate and nitrophosphate.
An advantage of the use of a pelletizer is that slurries with a high amount of solid can still be pelletized. Such slurries can not easily be sprayed in a prilling tower or a granulator.
Ammonium sulphate is, up to an amount of 30 wt.% soluble in urea and liquids containing such an amount of ammonium sulphate can be prilled or granulated. A higher amount of ammonium sulphate will be present as a solid in the mixture. The mixture will then be a slurry.
A urea/ ammonium sulphate mixture with > 30 wt.% of ammonium sulphate, can be pelletized with the process according to the invention, but can not easily be sprayed in a prilling tower or a granulator.
The urea-comprising particles that are obtained can be coated after leaving the pelletizer. Coating means applying to the particle a thin layer to reduce the caking tendency. Examples of coatings are fine, inert powders, wax, oil and polymers. Examples of fine, inert powders are kieselguhr, talcum, lime kaolin and sulfur. Examples of wax are polyethylene waxes, parafins, fatty amines and sulfonates. Examples of polymer coatings are poly(vinylidene chloride) (PVDC) coatings, polyolefins (polyethylene, polypropylene and ethylene copolymers), polyurethane, urea-formaldehyde resins, polyesters and alkyd resins.
The obtained urea-comprising particles can be used as a fertilizer. To this end the urea-comprising particles according to the invention can be used as such or be mixed with other fertilizer particles with about the same shape and size to be spread together over the field in one fertilizer spreading apparatus.
Examples
Determination of the crushing strength.
The crushing strength was determined with the apparatus LRX+ Material Testing Systems of Lloyd Instruments.
With a pair of tweezers a particle of the sample was placed in the centre of the pressing table of the crushing tester. The particle was placed in such a way that the flat side of the particle is the side on which the pressure was enforced. The particle was subjected to a force, which is increased at a constant rate. The force applied at the moment at which the particle was crushed is determined and is the crushing strength of the particle. The crushing strength was determined in Newton (N).
Example I In a Rotoform apparatus of Sandvik Process Systems a urea melt was pelletized. The Rotoform apparatus had a belt width of 600 mm and a cooling length of 11 m. The urea melt with a urea content of 99.8 wt.% was fed to the feeding device of the pelletizer. The urea melt was dosed to the belt with a temperature of 137 °C. The belt was rotating with a speed of about 50 m/min. The belt was cooled with cooling water with a temperature of about 22 °C and with a flow of 6,5-9 m3/h.
The urea pellets that were formed were scraped off at the turning point of the belt. The urea pellets had a temperature of 32-38 °C, a diameter of 3.15-4.00 mm and a height of 2.0 mm. The crushing strength of the pellets was 15 N.
Example Il
With the urea pellets obtained according to Example I a spreading test was performed. The urea pellets were fed to a fertilizer speading apparatus, type ZA-M Maxi S 1500 of Amazone. A working width of 24 m could be realized.
Comparative experiment A
In a Rotoform apparatus of Sandvik Process Systems a urea melt was pelletized. The Rotoform apparatus had a belt width of 600 mm and a cooling length of 11 m. The urea melt with a urea content of 99.8 wt.% was fed to the feeding device of the pelletizer. The urea melt was dosed to the belt with a temperature of 150 °C. The belt was rotating with a speed of about 90 m/min. The belt was cooled with cooling water with a temperature of about 22 °C and with a flow of 8,5-10 m3/h.
The urea pellets that were formed were scraped off at the turning point of the belt. The urea pellets had a temperature of 56-59 °C, a diameter of 3.5-5.4 mm and a height of
1.9 mm. The urea pellets could be removed from the belt, but there was a lot of dust formed during removal of the pellets from the belt. The pellets showed caking after storage.

Claims

I . Process for the production of urea-comprising particles, characterized in that the urea-comprising particles are produced in a pelletizer, comprising a feeding device, a belt and a device to remove the formed pellets from the belt, by feeding a urea-comprising liquid to the feeding device from which droplets of the urea-comprising liquid are dosed to the belt, whereon the urea- comprising droplets solidify and cool to a temperature of < 55 °C, whereafter the formed urea-comprising particles are removed from the belt.
2. Process according to claim 1 , characterized in that the urea-comprising liquid is a urea melt.
3. Process according to claim 2, characterized in that the urea melt comprises > 99 wt. % urea.
4. Process according to any one of claims 1-3, characterized in that the belt is cleaned after removing the urea-comprising particles from the belt.
5. Process according to any one of claims 1-4, characterized in that the urea- comprising liquid contains an additive.
6. Process according to claim 5, characterized in that the additive is a formaldehyde solution or a reaction product of urea and formaldehyde.
7. Process according to any one of claims 1-6, characterized in that the urea- comprising liquid is a mixture of urea with another fertilizer.
8. Process according to claim 7, characterized in that the urea-comprising liquid is a mixture of urea with ammoniumsulphate.
9. Process according to claim 8, characterized in that the urea-comprising liquid is a mixture of urea with > 30 gew. % ammoniumsulphate.
10. Urea-comprising particle, characterized in that the h/d ratio of the particle is 0.99 to 0.1.
I 1. Urea-comprising particle according to claim 10, characterized in that the particle comprises an additive.
12. Urea-comprising particle according to claim 11 , characterized in that the additive is a formaldehyde solution or a reaction product of urea and formaldehyde.
13. Urea-comprising particle according to claim 10, characterized in that the particle comprises urea and an other fertilizer.
14. Urea-comprising particle according to claim 13, characterized in that the particle comprises urea and ammoniumsulphate.
15. Urea-comprising particle according to claim 14, characterized in that the particle comprises urea and > 30 gew.% ammoniumsulphate.
PCT/EP2006/003450 2005-04-18 2006-04-03 Process for the production of urea-comprising particles WO2006111331A1 (en)

Priority Applications (7)

Application Number Priority Date Filing Date Title
AU2006237137A AU2006237137B8 (en) 2005-04-18 2006-04-03 Process for the production of urea-comprising particles
EP06724336.0A EP1868963B1 (en) 2005-04-18 2006-04-03 Process for the production of urea-comprising particles
CN2006800128719A CN101160271B (en) 2005-04-18 2006-04-03 Process for the production of urea-comprising particles
EA200702262A EA011329B1 (en) 2005-04-18 2006-04-03 Process for the production of urea-comprising particles
CA2600771A CA2600771C (en) 2005-04-18 2006-04-03 Process for the production of urea-comprising particles
US11/918,233 US7700012B2 (en) 2005-04-18 2006-04-03 Process for the production of urea-comprising particles
JP2008506981A JP5649781B2 (en) 2005-04-18 2006-04-03 Method for producing urea-containing particles

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP05075927.3 2005-04-18
EP05075927 2005-04-18

Publications (1)

Publication Number Publication Date
WO2006111331A1 true WO2006111331A1 (en) 2006-10-26

Family

ID=35677560

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2006/003450 WO2006111331A1 (en) 2005-04-18 2006-04-03 Process for the production of urea-comprising particles

Country Status (10)

Country Link
US (1) US7700012B2 (en)
EP (1) EP1868963B1 (en)
JP (2) JP5649781B2 (en)
CN (1) CN101160271B (en)
AR (1) AR056658A1 (en)
AU (1) AU2006237137B8 (en)
CA (1) CA2600771C (en)
EA (1) EA011329B1 (en)
MY (1) MY144732A (en)
WO (1) WO2006111331A1 (en)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102007061408A1 (en) 2007-12-11 2009-06-18 Sandvik Materials Technology Deutschland Gmbh Method and drop former for producing pastilles and method for producing a sulfur-containing fertilizer
WO2011032786A1 (en) 2009-09-16 2011-03-24 Dsm Ip Assets B.V. Removal of urea and ammonia from exhaust gases
WO2012007331A1 (en) * 2010-07-16 2012-01-19 Sandvik Materials Technology Deutschland Gmbh Method for producing tablets containing ammonium nitrate
ITMI20121648A1 (en) * 2012-10-02 2014-04-03 Sbs Steel Belt Systems S R L PROCESS AND EQUIPMENT FOR THE PRODUCTION OF FERTILIZER IN TABLETS
US8835005B2 (en) 2009-09-10 2014-09-16 Stamicarbon B.V. Process for producing granules
WO2017111588A1 (en) 2015-12-21 2017-06-29 Stamicarbon B.V. Urea ammonium nitrate production comprising condensation
WO2017111585A1 (en) 2015-12-21 2017-06-29 Stamicarbon B.V. Urea ammonium nitrate production
EP2237867B1 (en) 2008-01-04 2018-03-14 Casale Sa Fluid bed granulation process and apparatus
WO2018122377A1 (en) 2016-12-30 2018-07-05 Yara International Asa Processing of exhaust gases from a urea plant
DE102017108842A1 (en) * 2017-04-25 2018-10-25 Thyssenkrupp Ag Process and apparatus for the production of urea
EP3036206B1 (en) 2013-08-23 2021-07-07 Koch Agronomic Services, LLC Urea and nitrogen stabilizer compositions

Families Citing this family (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7771505B2 (en) * 2008-07-16 2010-08-10 Agrium Inc. Controlled release fertilizer composition
US7985393B2 (en) * 2009-03-31 2011-07-26 Uop Llc Pastillation of ammonium sulfate nitrate
EP2477705A1 (en) * 2009-09-15 2012-07-25 Shock Doctor Inc. Chest protector
EP2431346A1 (en) * 2010-09-15 2012-03-21 Uhde Fertilizer Technology B.V. Method for producing urea fertilizer with low moisture absorption tendencies
USD663484S1 (en) 2011-07-01 2012-07-10 Shock Doctor, Inc. Soft chest protector
WO2013062410A1 (en) 2011-10-24 2013-05-02 Stamicarbon B.V. Method of making controlled release fertilizer particles
WO2015127219A1 (en) * 2014-02-21 2015-08-27 Alcoa Inc. Fertilizer compositions and methods of making the same
EP3000524A1 (en) * 2014-09-29 2016-03-30 Casale SA Apparatus and method for prilling a liquid, preferably urea melt
US10626058B2 (en) * 2015-09-08 2020-04-21 Yara International Asa Urea ammonium sulphate-based composition and method for the manufacture thereof
EP3372576A1 (en) * 2017-03-07 2018-09-12 Yara International ASA Urea-based composition and method for the manufacture thereof
EP3581550A1 (en) * 2018-06-13 2019-12-18 Pursell Agri-Tech, LLC Fertilizer coating method
WO2021137699A1 (en) 2019-12-30 2021-07-08 Stamicarbon B.V. Urea plant with chilled condensation section
WO2021137700A1 (en) 2019-12-30 2021-07-08 Stamicarbon B.V. Ammonia removal from urea finishing
CA3166412C (en) 2019-12-30 2023-08-15 Stamicarbon B.V. Urea production with multiple evaporators
CN111330405B (en) * 2020-04-10 2022-03-11 福建永宏环保科技有限公司 Formaldehyde purification particle and preparation system and method thereof
EP4001246A1 (en) 2020-11-20 2022-05-25 Clariant Produkte (Deutschland) GmbH Vinasse containing fertilizer
CN114057522B (en) * 2021-11-17 2023-02-24 中化农业（临沂）研发中心有限公司 Biological stimulin type liquid fertilizer containing double-effect slow-release nitrogen and preparation method thereof

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3388989A (en) * 1963-04-25 1968-06-18 Exxon Research Engineering Co Fertilizer composition consisting of urea, a urease inhibitor, and a hydrocarbon binder
DE4422403C1 (en) * 1994-06-27 1995-06-01 Santrade Ltd Granulating machine with one toothed roll inside another
US6254655B1 (en) * 1999-03-18 2001-07-03 Oms Investments, Inc. Processes for preparing granular composite fertilizer compositions and products produced thereby
US20020045727A1 (en) * 2000-09-21 2002-04-18 Hartmut Weyer Method for producing methylene urea polymers
WO2003011446A1 (en) * 2001-07-27 2003-02-13 Santrade Ltd. Device for pressing out flowable substances

Family Cites Families (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2118439A (en) * 1937-07-20 1938-05-24 Solvay Process Co Process for the preparation of fertilizers
US2830036A (en) * 1955-06-06 1958-04-08 Nitro Form Agricultural Chemic Production of fertilizer compositions
US3100698A (en) * 1960-09-23 1963-08-13 Shell Oil Co Urea-sulfur fertilizer composition and method for its production
US3265779A (en) * 1963-12-06 1966-08-09 United States Steel Corp Method and apparatus for pelletizing pitch
JPS5022534B1 (en) * 1970-09-08 1975-07-31
GR76402B (en) * 1981-07-03 1984-08-10 Azote Sa Cie Neerlandaise
CA1237292A (en) * 1983-07-28 1988-05-31 G. Graham Allan Sustained release compositions for biologically active materials
US4587358A (en) * 1985-08-26 1986-05-06 Tennessee Valley Authority Production of high-strength, storage-stable particulate urea
JPH0332506Y2 (en) * 1986-10-23 1991-07-10
NL8700913A (en) * 1987-04-16 1988-11-16 Nl Stikstof METHOD FOR MANUFACTURING FERTILIZER GRANULES
DE19507316A1 (en) * 1994-12-22 1996-09-05 Santrade Ltd Process for the crystallization of chemical substances
US5676729A (en) * 1995-06-29 1997-10-14 Western Industrial Clay Products, Ltd. Particulate urea with mineral filler incorporated for hardness
DE19826570C2 (en) * 1998-06-15 2002-10-31 Piesteritz Stickstoff Process for the production of fertilizer granules containing urea and ammonium sulfate
US6217630B1 (en) * 1999-05-03 2001-04-17 Cargill, Incorporated Conditioned fertilizer product, method for conditioning fertilizer, and method for using conditioned fertilizer product
US6749660B2 (en) * 2001-06-04 2004-06-15 Geovation Technologies, Inc. Solid-chemical composition and method of preparation for the anaerobic bioremediation of environmental contaminants coupled to denitrification
JP5063843B2 (en) * 2001-07-23 2012-10-31 東ソー株式会社 Method for dripping granulation of slurry melt and method for producing urea-based composite fertilizer granule using the same
EA009533B1 (en) * 2003-11-10 2008-02-28 ДСМ АйПи ЭССЕТС Б.В. Process for the preparation of urea granules

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3388989A (en) * 1963-04-25 1968-06-18 Exxon Research Engineering Co Fertilizer composition consisting of urea, a urease inhibitor, and a hydrocarbon binder
DE4422403C1 (en) * 1994-06-27 1995-06-01 Santrade Ltd Granulating machine with one toothed roll inside another
US6254655B1 (en) * 1999-03-18 2001-07-03 Oms Investments, Inc. Processes for preparing granular composite fertilizer compositions and products produced thereby
US20020045727A1 (en) * 2000-09-21 2002-04-18 Hartmut Weyer Method for producing methylene urea polymers
WO2003011446A1 (en) * 2001-07-27 2003-02-13 Santrade Ltd. Device for pressing out flowable substances

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EA018093B1 (en) * 2007-12-11 2013-05-30 Сэндвик Материалз Текнолоджи Дойчланд Гмбх Method and drop former for producing tablets made of mixtures of a plurality of materials
WO2009074250A2 (en) 2007-12-11 2009-06-18 Sandvik Materials Technology Deutschland Gmbh Method and drop former for producing tablets and method for producing a sulfurous fertilizer
WO2009074250A3 (en) * 2007-12-11 2009-11-05 Sandvik Materials Technology Deutschland Gmbh Method and drop former for producing tablets and method for producing a sulfurous fertilizer
DE102007061408A1 (en) 2007-12-11 2009-06-18 Sandvik Materials Technology Deutschland Gmbh Method and drop former for producing pastilles and method for producing a sulfur-containing fertilizer
US8349229B2 (en) 2007-12-11 2013-01-08 Sandvik Materials Technology Deutschland Gmbh Method and drop former for producing tablets and method for producing a sulfurous fertilizer
EP2237867B1 (en) 2008-01-04 2018-03-14 Casale Sa Fluid bed granulation process and apparatus
EP2475455B1 (en) 2009-09-10 2019-09-11 Stamicarbon B.V. Process for producing granules
US8835005B2 (en) 2009-09-10 2014-09-16 Stamicarbon B.V. Process for producing granules
EP2477961B1 (en) 2009-09-16 2016-04-20 Stamicarbon B.V. Removal of urea and ammonia from exhaust gases
WO2011032786A1 (en) 2009-09-16 2011-03-24 Dsm Ip Assets B.V. Removal of urea and ammonia from exhaust gases
CN102596901A (en) * 2009-09-16 2012-07-18 斯塔米卡邦有限公司 Removal of urea and ammonia from exhaust gases
EA021089B1 (en) * 2009-09-16 2015-04-30 Стамикарбон Б.В. Removal of urea and ammonia from exhaust gases
US9464009B2 (en) 2009-09-16 2016-10-11 Stamicarbon B.V. Removal of urea and ammonia from exhaust gases
US9556077B2 (en) 2009-09-16 2017-01-31 Stamicarbon B.V. Removal of urea and ammonia from exhaust gases
EP2301917A1 (en) 2009-09-16 2011-03-30 Stamicarbon B.V. Removal of urea and ammonia from exhaust gases
US10640428B2 (en) 2009-09-16 2020-05-05 Stamicarbon B.V. Removal of urea and ammonia from exhaust gases
WO2012007331A1 (en) * 2010-07-16 2012-01-19 Sandvik Materials Technology Deutschland Gmbh Method for producing tablets containing ammonium nitrate
US9366485B2 (en) 2010-07-16 2016-06-14 Sandvik Materials Technology Deutschland Gmbh Method for producing tablets containing ammonium nitrate
EA024242B1 (en) * 2010-07-16 2016-08-31 Сэндвик Материалз Текнолоджи Дойчланд Гмбх Method for producing tablets containing ammonium nitrate
ITMI20121648A1 (en) * 2012-10-02 2014-04-03 Sbs Steel Belt Systems S R L PROCESS AND EQUIPMENT FOR THE PRODUCTION OF FERTILIZER IN TABLETS
EP3036206B1 (en) 2013-08-23 2021-07-07 Koch Agronomic Services, LLC Urea and nitrogen stabilizer compositions
WO2017111588A1 (en) 2015-12-21 2017-06-29 Stamicarbon B.V. Urea ammonium nitrate production comprising condensation
WO2017111585A1 (en) 2015-12-21 2017-06-29 Stamicarbon B.V. Urea ammonium nitrate production
WO2018122377A1 (en) 2016-12-30 2018-07-05 Yara International Asa Processing of exhaust gases from a urea plant
DE102017108842A1 (en) * 2017-04-25 2018-10-25 Thyssenkrupp Ag Process and apparatus for the production of urea

Also Published As

Publication number Publication date
AU2006237137B2 (en) 2011-08-11
EP1868963B1 (en) 2017-05-10
EP1868963A1 (en) 2007-12-26
EA011329B1 (en) 2009-02-27
CA2600771C (en) 2016-06-07
AU2006237137A1 (en) 2006-10-26
JP5649781B2 (en) 2015-01-07
JP2008536790A (en) 2008-09-11
CN101160271B (en) 2013-02-06
AU2006237137B8 (en) 2011-12-22
MY144732A (en) 2011-10-31
US7700012B2 (en) 2010-04-20
AR056658A1 (en) 2007-10-17
EA200702262A1 (en) 2008-02-28
JP5823582B2 (en) 2015-11-25
CN101160271A (en) 2008-04-09
CA2600771A1 (en) 2006-10-26
US20090084149A1 (en) 2009-04-02
JP2014237585A (en) 2014-12-18

Similar Documents

Publication Publication Date Title
CA2600771C (en) Process for the production of urea-comprising particles
US5917110A (en) Moisture-resistant calcium containing particles
EP2414307B1 (en) Pastillation of ammonium sulfate nitrate
WO2013035106A1 (en) A process for manufacturing a composite fertilizer
EP2616412A1 (en) Method for producing urea fertilizer with low moisture absorption tendencies
Rutland Fertilizer caking: mechanisms, influential factors, and methods of prevention
CN102603387A (en) Method for producing compound fertilizer by high tower tubular reactor
EP3548452A1 (en) Fertilizer particle
JP5068926B2 (en) Method for producing stabilized sulfur-coated fertilizer
US20100263420A1 (en) Process for the continuous granulation of fertilizers
RU2789161C2 (en) Method for granulation of melt of composition based on aqueous nitrate mineral salt, system, and their use
JP4044765B2 (en) Coated fertilizer
CA2229483C (en) Anti-caking solids
JPH075421B2 (en) Coated granular urea nitrate fertilizer
JPH05212262A (en) Coating method of granular substance
OA16343A (en) Method for producing urea fertilizer with low moisture absorption tendencies

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application
REEP Request for entry into the european phase

Ref document number: 2006724336

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2006724336

Country of ref document: EP

Ref document number: 2006237137

Country of ref document: AU

Ref document number: 2600771

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 7433/DELNP/2007

Country of ref document: IN

ENP Entry into the national phase

Ref document number: 2006237137

Country of ref document: AU

Date of ref document: 20060403

Kind code of ref document: A

WWP Wipo information: published in national office

Ref document number: 2006237137

Country of ref document: AU

WWE Wipo information: entry into national phase

Ref document number: 11918233

Country of ref document: US

WWE Wipo information: entry into national phase

Ref document number: 200680012871.9

Country of ref document: CN

Ref document number: 2008506981

Country of ref document: JP

NENP Non-entry into the national phase

Ref country code: DE

WWW Wipo information: withdrawn in national office

Ref document number: DE

NENP Non-entry into the national phase

Ref country code: RU

WWW Wipo information: withdrawn in national office

Ref document number: RU

WWE Wipo information: entry into national phase

Ref document number: 200702262

Country of ref document: EA

WWP Wipo information: published in national office

Ref document number: 2006724336

Country of ref document: EP