Granular ammonium phosphate sulfate and urea-ammonium phosphate sulfate using a common pipe-cross reactor

• US 4,134,750 A
• Filed: 12/19/1977
• Issued: 01/16/1979
• Est. Priority Date: 07/25/1977
• Status: Expired due to Term

• Current Assignee: Tennessee Valley Authority (Government of the United States of America)
• Original Assignee: Tennessee Valley Authority (Government of the United States of America)
• Inventors: Parker, Byron R., Norton, Melvin M.
• Primary Examiner(s): Schor, Kenneth M.
• Application Number:
  US05/861,585
• Time in Patent Office: 393 Days
• Field of Search: 71/29, 71/34, 71/37, 71/43, 71/64 DA, 71/36, 71/28, 23/259.2, 23/259.3, 423/313, 423/305, 423/ 315
• US Class Current: 71/29
• CPC Class Codes: C05B 7/00 Fertilisers based essentially on alkali or ammonium orthophosphates C05B11/00 takes precedence
• CPC Class Codes: C05C 9/00 Fertilisers containing urea or urea compounds
• CPC Class Codes: C05G 1/00 Mixtures of fertilisers belonging individually to different subclasses of C05

Abstract

A process for the production of fertilizers from phosphoric and sulfuric acids, anhydrous ammonia, and urea, and more specifically, the production of high-analysis granular ammonium phosphates, ammonium phosphate sulfates, and urea-ammonium phosphate sulfates--some with polyphosphate contents of up to 68 percent of the total P₂ O₅. A specially designed pipe-cross reactor is used to produce a homogeneous melt or slurry of low moisture content from the reactants and thus eliminates the need for a preneutralizer as used in many prior-art granular fertilizer processes. In addition, because of the low melt or slurry moisture content, the dryer (also used in most of the previous processes) is eliminated. The elimination of these two items greatly simplifies pollution abatement, since both items are sources of fumes and dust. The equipment used to produce granular monoammonium phosphate, diammonium phosphate, urea-ammonium phosphate sulfate, and ammonium phosphate sulfate fertilizers is uncomplicated, relatively inexpensive, and simple to operate. The products produced are dust-free and of such particle size that they are well suited for bulk blends. Ammonium phosphate sulfate grades of 12-48-0, 6-24-24, 13-13-13, 10-40-10, a monoammonium phosphate grade of 11-55-0, a diammonium phosphate and diammonium phosphate sulfate grade of 18-46-0, and urea-ammonium phosphate sulfate grades of 33-11-0, 17-17-17, and 20-10-10 have been produced with this process.

Claims

1. An improved process for preparing granular substantially dust-free ammonium phosphate sulfates of a particle size distribution eminently suitable for subsequent bulk blending with other fertilizer values, which process consists essentially of simultaneously supplying a stream of anhydrous ammonia to the common pipe section of a pipe-cross reactor;

simultaneously supplying a stream of phosphoric acid to the cross section of said pipe-cross reactor, said phosphoric acid having a P₂ O₅ content in the range from about 30 to about 52 percent by weight and a free water content ranging from about 15 to 55 percent by weight;

simultaneously supplying a stream of sulfuric acid to said cross section of said pipe-cross reactor, said sulfuric acid containing from about 78 to about 98 percent H₂ SO₄, said streams of phosphoric acid and sulfuric acid contacting said anhydrous ammonia introduced into said common pipe section of said pipe-cross reactor at said cross section of said pipe-cross reactor, at a temperature sufficiently high so that additional water is not necessary for continuous operation;

subsequently introducing the reaction product resulting from contacting said anhydrous ammonia, phosphoric acid, and sulfuric acid into the vapor tube extension of said pipe-cross reactor to ensure continued intimate contact therebetween;

subsequently discharging from the downstream end of said vaporization tubular extension an essentially anhydrous molten ammonium phosphate sulfate into the upper end of an inclined rotating drum;

therein maintaining a bed of rolling discrete particles of ammonium phosphate sulfate;

withdrawing ammonium phosphate sulfate material from the lower end of said inclined rotating drum;

introducing said withdrawn material into cooling means;

withdrawing the resulting cooled material from said cooling means;

introducing said material withdrawn from said cooling means into sizing means;

returning particles of predetermined size from said sizing means into the upper end of said drum and withdrawing from said sizing means granular particles of ammonium phosphate sulfate as product;

said process characterized by the fact that there is a reduction in moisture content ranging from about 0.1 to about 1.2 percent by weight of said ammonium phosphate sulfate by said step of removing same from the lower end of said inclined rotating drum to the step of recovery of same as product, said percent reduction in moisture content based on the moisture content of said ammonium phosphate sulfate as it leaves the lower end of said inclined rotating drum and caused by evaporation while said material is being cooled.

2. The process of claim 1 wherein the NH₃ :

H₃ PO₄ mole ratio of the reaction product from the pipe-cross reactor is maintained at about 1, thereby producing a monoammonium phosphate sulfate containing up to about 30 percent of its P₂ O₅ as polyphosphate.

3. The process of claim 1 for producing monoammonium phosphate sulfate wherein the NH₃ :

H₃ PO₄ mole ratio of the reaction product from the pipe-cross reactor is maintained at about 0.6, and the NH₃ ;

H₃ PO₄ mole ratio of the material withdrawn from the lower end of said drum is adjusted to about 1 by continuously introducing anhydrous ammonia, in addition to that supplied to said pipe-cross reactor, beneath the surface of said bed in a broad stream substantially countercurrent to the upward movement of said rolling discrete particles therein, the breadth of said stream extending substantially the entire length of said bed.

4. The process of claim 1 wherein the NH₃ :

H₃ PO₄ mole ratio of the ammonium phosphate sulfate material withdrawn from the lower end of said drum is maintained at about 1.9 by the additional step of continuously introducing anhydrous ammonia, in addition to that added to the cross section of said pipe-cross reactor, beneath the surface of said bed of rolling discrete particles in a broad stream substantially countercurrent to the upper movement of said particles, the breadth of said stream extending substantially the entire length of said bed.

5. The process of claim 1 wherein a urea-ammonium phosphate sulfate material is produced by means of the additional step of adding particulate solid urea together with the returned particles of predetermined size from said sizing means into the upper end of said drum.

6. The process of claim 1 wherein a urea ammonium phosphate sulfate material is produced by means of the additional step of adding either a concentrated urea solution or a substantially anhydrous urea melt, or both, onto the top surface of said bed of rolling discrete particles.

7. The process of claim 1 wherein a urea ammonium phosphate sulfate material is produced by means of the additional step of simultaneously supplying a stream of highly concentrated urea solution or a stream of substantially anhydrous urea melt, or both, to the stream of anhydrous ammonia fed to the cross section of said pipe-cross reactor.

8. The process of claim 1 wherein the phosphoric acids contain from about 42 to about 52 percent P₂ O₅ by weight and from about 15 to about 30 percent free H₂ O by weight, and said sulfuric acid contains up to about 93 percent H₂ SO₄ by weight.