SU1125213A1 - Method for producing complex fertilizer - Google Patents

Abstract

A METHOD FOR PREPARING COMPLEX FERTILIZER, including the stepwise decomposition of phosphate raw material with nitric acid in the presence of ammonium sulfate, followed by the introduction of the remaining nitric acid, the addition of sulfuric acid, the separation of the resulting calcium sulfate by filtration, its npOKe iBKy and the return of the simple solutions of the chromphene during the manor, during the procession, during the procession, during the procession, during the procession, during the procession, during the procession, it should have left the part of the hidleto manne prostatum during the progression; to increase the yield of the finished product and to intensify the process by reducing the duration of the decomposition of the raw material and increasing the filtration performance of the sulfate Alzen, decomposition of nitric acid are beginning to pH O - (- 0.8), and the washings rastvoryvozvraschayut to step decomposition voltage phosphate raw material with nitric acid.

Description

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Invention from: number to method (.; M a 3 o n o k and s l o t ii o i g: e r o r a f o t k i f o o f Fto of raw materials into complex processors .and and;:,

Known spos; o6 of the production of complex (Ogo fertilizer, slug1; oii oDpaCjoTJiy phosphate ciijpijH nitric; and seunoic acids and solution-ol s-u-sulphate sulphate in the presence of fipcjMbiBHHix water for 4 hours , a seduction of calcium, and the return of the washings of the CFCs and the process, | 1rOrganic-: the first plant is processed 3 s, the fertilizer is neutralized - ;; az aerated a.4. miac, cleanly, .eiHieM with kalkyyga

salt n CyilKOlT ji:

To disadvantage | am, cric: co5a OTEiOCHTCfl thread), i: P ,; f i; and the finished product (96), zu eghranirovani or phos-aat grains: -e; l -kmi crystals of sul); rata ka.gyyi, not arriving with ripOMtJHiii.iMM.-ashes, v; edstl is sufficient; p711 filtering phospho1: and soss; th suspension (1000 kg / mch),: 1., s. ;;::) n.pe; 1a on the crystallization of sul / tUata.-gts G not- () L (1HOPRIYATNK y with l GCH) them.

The most: near-L- - g; pm of the akhnichs essence and lkggi-asmoy ul;, tatu. ; g: t is a method of obtaining a complex ulo ;; ronine by decomposing phosphate; h-1 of the raw material of Pn and sulfur Kiu ;; jciTa-.u} Kisougst-tiny sulfate of JPY. Pfm;: (i.;:; Azlo rot:. I ;; i h-ps: -G / - -th azotns5G1; pslotm and. O-L; that is ammon; up to pI 4,0 at t .- -: i; i- /;.p 11 one-; c; on zero-one p-time-h ;. ;; arinarat, where r-os yiaiC-T nitric acid Z1O pM.: -; :( :. and}: : :-(. and then enter; a: ;; Mii: ipv: Tijcip and 92% ssr ;; -.; .- ||. nni 7 (V (:, this process; .- Y-; -: site1.,

} 1eDOST; -: 3 ::; /: -. C, JV ..:. P. but

is ma'h; ; D.: and h. ; T ;; : Ki-: c; if; ij isfo;: I eat ;; th p: j ::: and f | asfatnyh raw material /; a gf; with i A.on: -.),

what DRIVE T;: i; : ii; i C AND H 10 BYSHL G

READY g: pc,) ;; y; Cjc,:, number ;, DIMA M; iic; c with clothes RJ and HP with; from - :: i - /: ;;:. ф; г-; с.ПЭВ on this С1чг; и and З1.: dpt to ooze the kristgop process ;; - ::; arias su. ;;; fata of calcium and um-11g; s; NU about; L.-ma sediment. The purpose of the Isob-RSG: lower -:; with: ;; g; n: us and exit 1 "O; n: :) jo: nJH tipo.py; -: and and ggsnsification r; p.Mif; C-Ci; c ;; | h.) ai: they ddit flaxplash 1 and I with; |.; pb and increase npOH330ZP; TCJibHOi J and FiltrS,) vani sulyyats ka.zts: - ;; „

Delivered to the purpose of the acquisition by the fact that, according to the method of complex fertilization, the hustadium decomposition of the fuxfatnoto raw material is nitrogen 11 (; 1Ki (;:: | otoi; 1gps; sulphate aMivKHiJ-ui from 1; os: l1; yi; yy; and emos: i-a ln about g-;) to with l and h: g; t and nitric acid., lot, before ... 4.f weed acid, about the case, s y; i; -; s-g.) with

sul: f, u1 ;; calcium by filtration, its .p-; | {y and returning the flushing; J-U; THOI: O J to zugl, decomposition of nitrogen; k; and,: first, lead to pH 0-- (-., o),. and return wash solutions: -dg1 phosphate decomposition stage -: -; th; zlr acid;

Pu 3-IOM pr - washing solutions of mixture, -1Hg-a) it with nitric acid, which is rg1SD: H 1.) the small

U crystalline calcium sulfate, that

cnocf j6) C tv u pt ul n filtra non sulphate sulphate precipitate 1Iau

CC1; i-) stable; —th analysis known-ioic: the proposed methods of pref 5 dep; tab. .one ,

1p; D.: the agaim method allows for a G) chs-p score), from; the supply of reagents ps; .; i, -MTb 11roxo, 1; 1 nst filter | -, calcium sulfate calcium in times, th; (; d5 zano-znuchen; by large, x - ar: h; about the filtering crystals of the salt; 14 | a7a calcium, - to this aid--,; blah:; - met; tla conditions for the cris; ; ga.ai ggpi kala ..; and at the stage of processing of g / pIro / dno-phosphate a-otnu-kslo; oh and with a solution judge :: / a and zl1 account of / excess restraint oy :: b ;: .at-iaaop, and the lack of

. IU; p-.o-o sediment; e; -1romyvy; waters

when they are applied to the precipitation stage.: p k ;: g: sssy acid (; TG1y per sag ,,,; ac 1 nap; pi: pistadi sudfa a, ka1ts1 I in azodio ;; gsisdgd-e,

K, .isnd T1 ;; -:;.) Yes R., O in the preposition- as-m ;;; -; scyobobo-nosed; ichipae1-s up to 97V 3 V, 3i.:j;o:;c-rchi i.) beam (h-1i at decomposition -; i (ci ;; - H (.t .; raw materials ;; large Kristadlgm; g: st1) Ra and -zddddi, not ekayrifuyudmh sch ;;

0 f.-М1 .-; ogg: increased; then g-БО - /: 000 kg / g, Гч.

acids (copy 7b of total laccbi), pH 0 “At this:; ha,;. 1c)) 1 iod. () 8;, L kg 40 - 10To a solution (NH,) ,, S (,

Choroz LO min serves rast-7-op, liojiychenmy, -cMemeHpo.fi 100 washings: -: o ;;,: -16.4 kg of nitrogenous kgg:,; off at, P,; brook; p-u a pu / ; npu (522.9 kg) at the stage of sedimentation of s., hertz, kalsh fata; /;, s; bottom, ch; ;-simply gsd 200 kt

4ir) -; a narrowing solution and 44.0 kg of H? 8D (93%), 7–6.9 kt-suspension are fed and separated after 100 kg of water, 216.9 KI and 1 sulphate of sulfate; Wash water is fed to the mixture with nitric acid. The chidratrat (L50) is divided into two, nOTci1 a: 2C; 0 kg is used as a quality product: -1p of the diluting solution, and .50 to g (38, 4 kg PjO .;) obra: atzaett, 2 kg

1azoabraz nodo a-.g-.shaka. ; (- - hr y / ;. a.iiri in the process of evaporation 163.2 kg, the suspension in an amount of 1.96 kg is mixed with 64 kg of KC1 {60% K20) and dried. In this case, 34 kg of water is removed and 226 kg of l: l: i nitroammofosci is obtained. Output ,; in the finished product 97.5%, eat from-the-ear from this sediment is .1850,

PRI me R 2, JUS kg of apatite is treated with 139 kg of 50% nitric acid (in the amount of 90% of the total mass), pH -0.8. This stage was introduced in 168.5 kg of a 40% solution.

(. After 30 minutes, the solution obtained is mixed with J 00 kg of urine water with 15.4 kg of nitric acid at. The resulting slurry

(522.9 kg) is fed to the calcium sulphate precipitation stage, 200 kg of the circulating solution and 44.0 kg are simultaneously injected into the pool, | (93%). 766.9 kg of the suspension is filtered with separation after washing with JOO of water of 216.9 kg of wet calcium sulfate. BSDY served to mix with aero acid acid. Filtrate

(550 kg) is divided into two streams ;: 200 kg are used as a circulating solution and 350 kg (38.4 kg of P. 05). 9.2 kg of ammonia gas is processed. After removing 163.2 kg of water in the process of parrying, the suspension in the amount of 196 kg of mixed material from 64 kg of KC1 (60% C20) and dry; t ”This removes 35 kg of zodia and produces 225 kg of nitroad mofoska (1: 1; 1 ), The yield in the finished product is 97%, and the removal of the dry washed sludge is 1800 kg / m

Froze 100 kg of apatite are treated with 123 ,, 5 kg of 50% nitric acid (in the amount of 80% of the total mass) “Enter 168, 5 kg of a 40% (NH) SC solution at this stage. After 40 minutes, the solution is supplied; obtained by mixing 100 kg of prolyl water from 30.9 kg of nitric acid with ,, The resulting pulp (522.9 kg) is fed to the stage of precipitation of calcium sulfate where 200 kg of circulating solution and 44.0 kg of NgZO are simultaneously introduced (93%) , 766.9 kg of suspension. Filtered after separation, after washing 100 kg of water 216, 9 kg of wet calcium sulphate. Wash water is fed to the mixture with nitric acid. The filtrate (550 kg) is divided into two streams: 200 kg are used as a circulating solution, and 350 kg (38.6 kg of P are treated with 9.3 kg of ammonia gas. After removing 161.3 kg of water in the process of evaporation, 198 kg are mixed with 65 KIX1 (60%) and dried. This removes 35 kg of water and yields

227 kg of nitroammofoski (1: 1: 1). Output P Ot; - to the finished product 98%, removal of dry, shallow precipitate is 2000.

In tab. Table 2 presents examples of how the process is conducted within the suggested limits of the parameters (1-3), as well as for values outside these limits.

From tab. 2 that when the parameters go beyond the proposed limits (examples 4-9), such characteristics as the removal of the dry washed sludge and the release of P "Oy to the product are worsened.

A decrease in the fraction of nitric acid used to decompose apatite in the first stage (Example 4) results in a decrease in the P 0 yield of the product due to a decrease in the degree of raw material opening, which is associated with a decrease in the rate of nitric acid at the decomposition stage and the optimum content of excess sulfate. iono at this stage. The latter leads to a deterioration in the crystallization of calcium sulfate and a decrease in the removal of sediment.

An increase in the proportion of nitric acid to 92% (Example 5) at the decomposition stage also reduces the yield to the finished product and the removal of the precipitate due to the deterioration of its washing conditions, since the bulk of the solid phase consists of small sulfate crystals, which is caused by their crystallization with a shortage of sugations and a return to the stage of decomposition of fine calcium sulfate crystals due to the lack of nitric acid in their dissolution.

When the time of decomposition of apatite with nitric acid is less than 30 minutes (Example 6), its phosphate component is incompletely opened,

Thus, using the invention allows to increase the yield ratio of the product to 97-98% (in the known method, 94.9-95.4%) and to increase the filtration performance of calcium sulfate to 1800 2000 by dry sediment (instead of 1200-1300 in the known method) . It should also be noted that when washing solutions are supplied to the displacement with nitric acid, the filtration time at the sulfuric acid stage of crystallization of calcium sulfate due to the creation of favorable conditions for its precipitation is reduced by 3 times, which accelerates the processing of phosphate raw materials to 1.8- 2.0 instead of 2.7-2.8 hours

Table 1,

Technological parameters

The amount of nitric acid from stoichiometric: norms,%, supplied in stages:

1 2 3 Introduction of ammonium sulfate

Excess sulfate ion concentration,%

Crystallization of fine calcium sulfate crystals

pH according to stages: 1 2. 3

The return of the washing solution in the cycle

 Process indicators The output of Pj Og in the product,%

Calcium sulphate filtration capacity,

The duration of the process before filtering calcium sulfate, h

60 30 40 40

70 90 80 68

70-90 10-30 None

Introduced at first

first stage

Not

Not

0 - {- 0.8) -0.8

Served on a blend. Served to mix with sulfuric acid and a nitrogen cystic acid.

94.9-95.4

97-98.0

1600-2000

1200-1300

2.7-2.8

1.8-2.0

table 2

97.5

1850 97.0 1800 98.0 2000 96.0 1600

40 25 65 40 40

92

80 80 80 80 100

Continued table. 2

95.5

1500 95.0 1700 97.0. 1850 98.0 1200 96.0 1200 95.0 1200

Claims (1)

A METHOD FOR PRODUCING A COMPLEX FERTILIZER, including the stepwise decomposition of phosphate feedstock with nitric acid in the presence of ammonium sulfate, followed by the introduction of the remaining amount of nitric acid, the addition of sulfuric acid, separation of the resulting calcium sulfate by filtration, washing and returning the washing solutions to the cycle, characterized in that, - in order to increase output ₽ ₂ ^O 5 in the finished product and of process intensification by reducing the duration of the decomposition of raw materials and increase in filtration performance sulfa and calcium, decomposition of nitric acid are beginning to pH 0 - (- 0.8), and the washings rastvory'vozvraschayut to step decomposition phosphate rock with nitric acid. ..... >