CN202657964U - Device for producing industrial monoammonium phosphate with raffinate - Google Patents
Device for producing industrial monoammonium phosphate with raffinate Download PDFInfo
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- CN202657964U CN202657964U CN 201220260910 CN201220260910U CN202657964U CN 202657964 U CN202657964 U CN 202657964U CN 201220260910 CN201220260910 CN 201220260910 CN 201220260910 U CN201220260910 U CN 201220260910U CN 202657964 U CN202657964 U CN 202657964U
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Abstract
The utility model discloses a device for producing industrial monoammonium phosphate with raffinate. The device comprises a reaction system, a filtering separation system, a first-stage concentration system, a second-stage concentration system, a crystallization system, a centrifugal dehydration system, a drying system and a packaging system. The device provided by the utility model can be used for producing the industrial grade monoammonium phosphate with the raffinate, so that full utilization of the raffinate is realized; and the device has a high application value.
Description
Technical field
The utility model relates to phosphoric acid, specifically a kind of device with raffinate manufacture monoammonium phosphate.
Technical background
Produce purifying phosphoric acid (industrial phosphoric acid or phosphoric acid for food) with Purification of Wet process Phosphoric Acid by Solvent Extraction, general phosphoric acid purification rate is about 51%, be that one ton of every production purifies acid, will produce one ton of raffinate, raffinate only is used for producing the agrochemicals such as fertilizer grade diammonium phosphate at present.
Therefore, production technique and the device of developing a kind of raffinate manufacture monoammonium phosphate can promote the Phosphorus fractionation utilization, have very real meaning to improving wet route phosphorus element value.
Summary of the invention
The purpose of this utility model is to provide a kind of device of raffinate manufacture monoammonium phosphate, realizes the taking full advantage of of raffinate produced the monoammonium phosphate of technical grade.
The technical solution of the utility model is: a kind of device of raffinate manufacture monoammonium phosphate, comprise reactive system, filtering separation system, first step concentration systems, second stage concentration systems, crystal system, centrifuge dehydration system, dehumidification system, packaging system, wherein
Reactive system comprises reactor and dashpot; Reactor comprises sour import, ammonia import and mixture export; Dashpot is provided with the mixed solution import, mother liquor import, properties-correcting agent import, phosphor ammonium slurry outlet;
The filtering separation system comprises strainer, slag stock tank, filtrate receiver; Strainer is provided with feed slurry inlet, filtrate outlet and sludge outlet; The slag stock tank is provided with slag import, raw phosphoric acid import and the outlet of slag slurry; Filtrate receiver is provided with filtrate import and filtrate outlet;
First step concentration systems comprises first step concentration systems flashing chamber, first step concentration systems recycle pump and first step concentration systems interchanger; First step concentration systems flashing chamber is provided with thin liquid import, circulation fluid import, circulation fluid outlet and primary steam outlet; First step concentration systems recycle pump is provided with first step concentration systems pump inlet and first step concentration systems circulating-pump outlet; First step concentration systems interchanger is provided with the import of first step concentration systems interchanger circulation fluid, the outlet of first step concentration systems interchanger circulation fluid, first step concentration systems interchanger steam inlet and first step concentration systems interchanger condensate outlet; Pipeline between first step concentration systems circulating-pump outlet and the import of first step concentration systems interchanger circulation fluid also is provided with pipe joint;
Second stage concentration systems comprises second stage concentration systems flashing chamber, second stage concentration systems recycle pump, second stage concentration systems interchanger and time condensation liquid recovery system; Second stage concentration systems flashing chamber is provided with circulation fluid import, circulation fluid outlet, secondary steam outlet and concentrated solution outlet; Second stage concentration systems recycle pump is provided with second stage concentration systems pump inlet and second stage concentration systems circulating-pump outlet; Second stage concentration systems interchanger is provided with second stage concentration systems interchanger circulation fluid import, the outlet of second stage concentration systems interchanger circulation fluid, second stage concentration systems interchanger steam inlet and second stage concentration systems interchanger condensate outlet; Pipeline between circulation fluid outlet and the second stage concentration systems pump inlet also is provided with pipe joint; Time condensation liquid recovery system is provided with the secondary steam import;
Crystal system comprises first step cooling crystallizer and second stage cooling crystallizer; First step cooling crystallizer is provided with the import of first step crystallizer concentrated solution, the outlet of first step crystallizer magma, first step crystallizer entrance of cooling water and first step crystallizer cooling water outlet; Second stage cooling crystallizer is provided with second stage crystallizer concentrated solution import, the outlet of second stage crystallizer magma, second stage crystallizer entrance of cooling water and second stage crystallizer cooling water outlet;
The centrifuge dehydration system comprises separating centrifuge; The separating centrifuge whizzer is provided with magma import, mother liquor outlet and crystal outlet;
Dehumidification system comprises dryer; Dryer is provided with wet feed import, drier outlet, hot blast import and tail gas outlet;
Packaging system is provided with packaging system entrance and packaging system outlet;
Above-mentioned mixture export links to each other with the mixed solution import by pipeline, the phosphor ammonium slurry outlet links to each other with feed slurry inlet by pipeline, sludge outlet links to each other with the slag import by pipeline, filtrate outlet links to each other with the filtrate import by pipeline, filtrate outlet links to each other with the thin liquid import by pipeline, the circulation fluid outlet links to each other with first step concentration systems pump inlet by pipeline, first step concentration systems circulating-pump outlet links to each other with the import of first step concentration systems interchanger circulation fluid by pipeline, the outlet of first step concentration systems interchanger circulation fluid links to each other with first step concentration systems interchanger steam inlet by pipeline, pipe joint links to each other with pipe joint by pipeline, the primary steam outlet links to each other with second stage concentration systems interchanger steam inlet by pipeline, the circulation fluid outlet links to each other with second stage concentration systems pump inlet by pipeline, second stage concentration systems circulating-pump outlet links to each other with second stage concentration systems interchanger circulation fluid import by pipeline, second stage concentration systems interchanger circulation fluid outlet links to each other with the circulation fluid import by pipeline, the secondary steam outlet links to each other with the secondary steam import by pipeline, concentrated solution outlet links to each other with the import of first step crystallizer concentrated solution by pipeline, the outlet of first step crystallizer magma links to each other with second stage crystallizer concentrated solution import by pipeline, second stage crystallizer magma outlet links to each other with the magma import by pipeline, the mother liquor outlet links to each other with the mother liquor import by pipeline, the crystal outlet links to each other with the wet feed import, and drier outlet links to each other with the packaging system entrance.
When the utility model uses, raffinate enters reactor from sour import, simultaneously, ammonia enters reactor from the ammonia import in proportion, in reactor, efficiently mix reaction, reacted slip is discharged from mixture export, enter dashpot by the mixed solution import, the mother liquor that returns from the centrifuge dehydration system enters dashpot from the mother liquor import, properties-correcting agent adds in proportion from the properties-correcting agent import, slip obtains modification and abundant slaking in dashpot after, phosphor ammonium slurry outlet from pump delivery to the filtration system, slip enters from feed slurry inlet, filtrate is discharged to filtrate receiver from filtrate outlet, filter residue enters the slag stock tank from sludge outlet by the slag import, be transported to fertilizer phosphoric acid production workshop after starching again with hot water and phosphoric acid, filtrate in the filtrate receiver enters first step concentration systems flashing chamber from filtrate outlet by the thin liquid import, filtrate is circulated in system by first step concentration systems recycle pump in first step concentration systems, steam enters interchanger from first step concentration systems interchanger steam inlet, discharge from first step concentration systems interchanger condensate outlet to becoming phlegma after the filtrate heating, filtrate is heated rear moisture and becomes primary steam, export out by second stage concentration systems interchanger steam inlet from primary steam and enter second stage concentration systems interchanger, the filtrate that is evaporated a part of water enters second stage concentration systems from pipe joint by pipe joint, in the concentration systems of the second stage, filtrate is further concentrated, the secondary steam that evaporation forms enters time condensation liquid recovery system from the secondary steam outlet by the secondary steam import, become the primary steam phlegma after primary steam heats to filtrate and enter primary steam phlegma recovery system from second stage concentration systems interchanger condensate outlet, import entered first step cooling crystallizer through concentrated solution from concentrated solution outlet after feed liquid reached hypersaturated state, water coolant enters the first step crystallizer chuck from first step crystallizer entrance of cooling water, again from first step crystallizer cooling water outlet out, feed liquid cools in first step cooling crystallizer to a certain degree and is discharged to second stage cooling crystallizer from the outlet of first step crystallizer magma by second stage crystallizer concentrated solution import afterwards, cooling crystallizer is further lowered the temperature by water coolant in the second stage, obtain magma up to specification, magma exports the magma import that enters the centrifuge dehydration system from second stage crystallizer magma, crystal is separated with mother liquor in the centrifuge dehydration system, mother liquor returns dashpot, crystal enters drying system from the crystal outlet by the wet feed import, in drying system, hot blast enters from the hot blast import, moisture in the crystal is taken away from the tail gas outlet by hot blast, the monoammonium phosphate crystal of having been dried out enters packaging system by the packaging system entrance from drier outlet, then is transported to the product storehouse from system outlet.
The device that the utility model provides can be realized can producing the monoammonium phosphate of technical grade to the taking full advantage of of raffinate, and meets the demand of development of modern industry, has very large using value.
Description of drawings
Fig. 1 is device schematic diagram of the present utility model;
Among the figure: 1, reactor, 2, the acid import, 3, the ammonia import, 4, mixture export, 5, dashpot, 6, the mixed solution import, 7 mother liquor imports, 8 properties-correcting agent imports, 9, the phosphor ammonium slurry outlet, 10, strainer, 11, feed slurry inlet, 12, sludge outlet, 13, filtrate outlet, 14, the slag stock tank, 15, the slag import, 16, the raw phosphoric acid import, 17, the outlet of slag slurry, 18, filtrate receiver, 19, the filtrate import, 20, filtrate outlet, 21, first step concentration systems flashing chamber, 22, the thin liquid import, 23, the circulation fluid outlet, 24, first step concentration systems recycle pump, 25, first step concentration systems pump inlet, 26, the dense compression system circulating-pump outlet of the first step, 27, pipe joint, 28, first step concentration systems interchanger, 29, the import of first step concentration systems interchanger circulation fluid, 30, the outlet of first step concentration systems interchanger circulation fluid, 31, first step concentration systems interchanger steam inlet, 32, first step concentration systems interchanger condensate outlet, 33, the circulation fluid import, 34, the primary steam outlet, 35, second stage concentration systems flashing chamber, 36, the circulation fluid import, 37, the circulation fluid outlet, 38, pipe joint, 39, second stage concentration systems recycle pump, 40, second stage concentration systems pump inlet, 41, second stage concentration systems circulating-pump outlet, 42, second stage concentration systems interchanger, 43, second stage concentration systems interchanger circulation fluid import, 44, second stage concentration systems interchanger circulation fluid outlet, 45, second stage concentration systems interchanger steam inlet, 46, second stage concentration systems interchanger condensate outlet, 47, the secondary steam outlet, 48, time condensation liquid recovery system, 49, the secondary steam import, 50, concentrated solution outlet, 51, the one-level cooling crystallizer, 52, the import of first step crystallizer concentrated solution, 53, the outlet of first step crystallizer magma, 54, first step crystallizer entrance of cooling water, 55, first step crystallizer cooling water outlet, 56, second stage cooling crystallizer, 57, second stage crystallizer concentrated solution import, 58, second stage crystallizer magma outlet, 59, second stage crystallizer entrance of cooling water, 60, second stage crystallizer cooling water outlet, 61, separating centrifuge, 62, the magma import, 63, the mother liquor outlet, 64, the crystal outlet, 65, dryer, 66, the wet feed import, 67, drier outlet, 68, the hot blast import, 69, the tail gas outlet, 70, packaging system, 71, the packaging system entrance, 72, the packaging system outlet.
Embodiment
Embodiment
A kind of device of raffinate manufacture monoammonium phosphate comprises reactive system, filtering separation system, first step concentration systems, second stage concentration systems, crystal system, centrifuge dehydration system, dehumidification system, packaging system, wherein
Reactive system comprises reactor 1 and dashpot 5; Reactor 1 comprises sour import 2, ammonia import 3 and mixture export 4; Dashpot 5 is provided with mixed solution import 6, mother liquor import 7, properties-correcting agent import 8, phosphor ammonium slurry outlet 9;
The filtering separation system comprises strainer 10, slag stock tank 14, filtrate receiver 18; Strainer 10 is provided with feed slurry inlet 11, filtrate outlet 13 and sludge outlet 12; Slag stock tank 14 is provided with slag import 15, raw phosphoric acid import 16 and slag slurry outlet 17; Filtrate receiver 18 is provided with filtrate import 19 and filtrate outlet 20;
First step concentration systems comprises first step concentration systems flashing chamber 21, first step concentration systems recycle pump 24 and first step concentration systems interchanger 28; First step concentration systems flashing chamber 21 is provided with thin liquid import 22, circulation fluid import 33, circulation fluid outlet 23 and primary steam outlet 34; First step concentration systems recycle pump 24 is provided with first step concentration systems pump inlet 25 and first step concentration systems circulating-pump outlet 26; First step concentration systems interchanger 28 is provided with first step concentration systems interchanger circulation fluid import 29, first step concentration systems interchanger circulation fluid outlet 30, first step concentration systems interchanger steam inlet 31 and first step concentration systems interchanger condensate outlet 32; Pipeline between first step concentration systems circulating-pump outlet 26 and the first step concentration systems interchanger circulation fluid import 29 also is provided with pipe joint 27;
Second stage concentration systems comprises second stage concentration systems flashing chamber 35, second stage concentration systems recycle pump 39, second stage concentration systems interchanger 42 and time condensation liquid recovery system 48; Second stage concentration systems flashing chamber 35 is provided with circulation fluid import 36, circulation fluid outlet 37, secondary steam outlet 47 and concentrated solution outlet 50; Second stage concentration systems recycle pump 39 is provided with second stage concentration systems pump inlet 40 and second stage concentration systems circulating-pump outlet 41; Second stage concentration systems interchanger 42 is provided with second stage concentration systems interchanger circulation fluid import 43, second stage concentration systems interchanger circulation fluid outlet 44, second stage concentration systems interchanger steam inlet 45 and second stage concentration systems interchanger condensate outlet 46; Pipeline between circulation fluid outlet 37 and the second stage concentration systems pump inlet 40 also is provided with pipe joint 38; Time condensation liquid recovery system 48 is provided with secondary steam import 49;
Crystal system comprises first step cooling crystallizer 51 and second stage cooling crystallizer 56; First step cooling crystallizer 51 is provided with first step crystallizer concentrated solution import 52, first step crystallizer magma outlet 53, first step crystallizer entrance of cooling water 54 and first step crystallizer cooling water outlet 55; Second stage cooling crystallizer 56 is provided with second stage crystallizer concentrated solution import 57, second stage crystallizer magma outlet 58, second stage crystallizer entrance of cooling water 59 and second stage crystallizer cooling water outlet 60;
The centrifuge dehydration system comprises separating centrifuge 61; Separating centrifuge whizzer 61 is provided with magma import 62, mother liquor outlet 63 and crystal outlet 64;
Dehumidification system comprises dryer 65; Dryer 65 is provided with wet feed import 66, drier outlet 67, hot blast import 68 and tail gas outlet 69;
Packaging system 70 is provided with packaging system entrance 71 and packaging system outlet 72;
Above-mentioned mixture export 4 links to each other with mixed solution import 6 by pipeline, phosphor ammonium slurry outlet 9 links to each other with feed slurry inlet 11 by pipeline, sludge outlet 12 links to each other with slag import 15 by pipeline, filtrate outlet 13 links to each other with filtrate import 19 by pipeline, filtrate outlet 20 links to each other with thin liquid import 22 by pipeline, circulation fluid outlet 23 links to each other with first step concentration systems pump inlet 25 by pipeline, first step concentration systems circulating-pump outlet 26 links to each other with first step concentration systems interchanger circulation fluid import 29 by pipeline, first step concentration systems interchanger circulation fluid outlet 30 links to each other with first step concentration systems interchanger steam inlet 31 by pipeline, pipe joint 27 links to each other with pipe joint 38 by pipeline, primary steam outlet 34 links to each other with second stage concentration systems interchanger steam inlet 45 by pipeline, circulation fluid outlet 37 links to each other with second stage concentration systems pump inlet 40 by pipeline, second stage concentration systems circulating-pump outlet 41 links to each other with second stage concentration systems interchanger circulation fluid import 43 by pipeline, second stage concentration systems interchanger circulation fluid outlet 44 links to each other with circulation fluid import 36 by pipeline, secondary steam outlet 47 links to each other with secondary steam import 49 by pipeline, concentrated solution outlet 50 links to each other with first step crystallizer concentrated solution import 52 by pipeline, first step crystallizer magma outlet 53 links to each other with second stage crystallizer concentrated solution import 57 by pipeline, second stage crystallizer magma outlet 58 links to each other with magma import 62 by pipeline, mother liquor outlet 63 links to each other with mother liquor import 7 by pipeline, crystal outlet 64 links to each other with wet feed import 66, and drier outlet 67 links to each other with packaging system entrance 71.
Claims (1)
1. the device of a raffinate manufacture monoammonium phosphate is characterized in that it comprises reactive system, filtering separation system, first step concentration systems, second stage concentration systems, crystal system, centrifuge dehydration system, dehumidification system, packaging system, wherein
Reactive system comprises reactor (1) and dashpot (5); Reactor (1) comprises sour import (2), ammonia import (3), mixture export (4); Dashpot (5) is provided with mixed solution import (6), mother liquor import (7), properties-correcting agent import (8) and phosphor ammonium slurry outlet (9);
The filtering separation system comprises strainer (10), slag stock tank (14), filtrate receiver (18); Strainer (10) is provided with feed slurry inlet (11), filtrate outlet (13) and sludge outlet (12); Slag stock tank (14) is provided with slag import (15), raw phosphoric acid import (16) and slag slurry outlet (17); Filtrate receiver (18) is provided with filtrate import (19) and filtrate outlet (20);
First step concentration systems comprises first step concentration systems flashing chamber (21), first step concentration systems recycle pump (24) and first step concentration systems interchanger (28); First step concentration systems flashing chamber (21) is provided with thin liquid import (22), circulation fluid import (33), circulation fluid outlet (23) and primary steam outlet (34); First step concentration systems recycle pump (24) is provided with first step concentration systems pump inlet (25) and first step concentration systems circulating-pump outlet (26); First step concentration systems interchanger (28) is provided with first step concentration systems interchanger circulation fluid import (29), the outlet of first step concentration systems interchanger circulation fluid (30), first step concentration systems interchanger steam inlet (31) and first step concentration systems interchanger condensate outlet (32); Pipeline between first step concentration systems circulating-pump outlet (26) and the first step concentration systems interchanger circulation fluid import (29) also is provided with pipe joint (27);
Second stage concentration systems comprises second stage concentration systems flashing chamber (35), second stage concentration systems recycle pump (39), second stage concentration systems interchanger (42) and time condensation liquid recovery system (48); Second stage concentration systems flashing chamber (35) is provided with circulation fluid import (36), circulation fluid outlet (37), secondary steam outlet (47) and concentrated solution outlet (50); Second stage concentration systems recycle pump (39) is provided with second stage concentration systems pump inlet (40) and second stage concentration systems circulating-pump outlet (41); Second stage concentration systems interchanger (42) is provided with second stage concentration systems interchanger circulation fluid import (43), the outlet of second stage concentration systems interchanger circulation fluid (44), second stage concentration systems interchanger steam inlet (45) and second stage concentration systems interchanger condensate outlet (46); Pipeline between circulation fluid outlet (37) and the second stage concentration systems pump inlet (40) also is provided with pipe joint (38); Time condensation liquid recovery system (48) is provided with secondary steam import (49);
Crystal system comprises first step cooling crystallizer (51) and second stage cooling crystallizer (56); First step cooling crystallizer (51) is provided with first step crystallizer concentrated solution import (52), the outlet of first step crystallizer magma (53), first step crystallizer entrance of cooling water (54) and first step crystallizer cooling water outlet (55); Second stage cooling crystallizer (56) is provided with second stage crystallizer concentrated solution import (57), the outlet of second stage crystallizer magma (58), second stage crystallizer entrance of cooling water (59) and second stage crystallizer cooling water outlet (60);
The centrifuge dehydration system comprises separating centrifuge (61); Separating centrifuge whizzer (61) is provided with magma import (62), mother liquor outlet (63) and crystal outlet (64);
Dehumidification system comprises dryer (65); Dryer (65) is provided with wet feed import (66), drier outlet (67), hot blast import (68) and tail gas outlet (69);
Packaging system (70) is provided with packaging system entrance (71) and packaging system outlet (72);
Mixture export (4) links to each other with mixed solution import (6) by pipeline, phosphor ammonium slurry outlet (9) links to each other with feed slurry inlet (11) by pipeline, sludge outlet (12) links to each other with slag import (15) by pipeline, filtrate outlet (13) links to each other with filtrate import (19) by pipeline, filtrate outlet (20) links to each other with thin liquid import (22) by pipeline, circulation fluid outlet (23) links to each other with first step concentration systems pump inlet (25) by pipeline, first step concentration systems circulating-pump outlet (26) links to each other with first step concentration systems interchanger circulation fluid import (29) by pipeline, first step concentration systems interchanger circulation fluid outlet (30) links to each other with first step concentration systems interchanger steam inlet (31) by pipeline, pipe joint (27) links to each other with pipe joint (38) by pipeline, primary steam outlet (34) links to each other with second stage concentration systems interchanger steam inlet (45) by pipeline, circulation fluid outlet (37) links to each other with second stage concentration systems pump inlet (40) by pipeline, second stage concentration systems circulating-pump outlet (41) links to each other with second stage concentration systems interchanger circulation fluid import (43) by pipeline, second stage concentration systems interchanger circulation fluid outlet (44) links to each other with circulation fluid import (36) by pipeline, secondary steam outlet (47) links to each other with secondary steam import (49) by pipeline, concentrated solution outlet (50) links to each other with first step crystallizer concentrated solution import (52) by pipeline, first step crystallizer magma outlet (53) links to each other with second stage crystallizer concentrated solution import (57) by pipeline, second stage crystallizer magma outlet (58) links to each other with magma import (62) by pipeline, mother liquor outlet (63) links to each other with mother liquor import (7) by pipeline, crystal outlet (64) links to each other with wet feed import (66), and drier outlet (67) links to each other with packaging system entrance (71).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220260910 CN202657964U (en) | 2012-06-05 | 2012-06-05 | Device for producing industrial monoammonium phosphate with raffinate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220260910 CN202657964U (en) | 2012-06-05 | 2012-06-05 | Device for producing industrial monoammonium phosphate with raffinate |
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| CN202657964U true CN202657964U (en) | 2013-01-09 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 201220260910 Expired - Lifetime CN202657964U (en) | 2012-06-05 | 2012-06-05 | Device for producing industrial monoammonium phosphate with raffinate |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102653395A (en) * | 2012-06-05 | 2012-09-05 | 瓮福（集团）有限责任公司 | Device for producing industrial monoammonium phosphate by extracted spent acid |
| CN106241763A (en) * | 2016-08-11 | 2016-12-21 | 贵阳开磷化肥有限公司 | A kind of phosphor ammonium slurry defecator and filter method thereof |
-
2012
- 2012-06-05 CN CN 201220260910 patent/CN202657964U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102653395A (en) * | 2012-06-05 | 2012-09-05 | 瓮福（集团）有限责任公司 | Device for producing industrial monoammonium phosphate by extracted spent acid |
| CN106241763A (en) * | 2016-08-11 | 2016-12-21 | 贵阳开磷化肥有限公司 | A kind of phosphor ammonium slurry defecator and filter method thereof |
| CN106241763B (en) * | 2016-08-11 | 2018-09-25 | 贵阳开磷化肥有限公司 | A kind of phosphor ammonium slurry filter device and its filter method |
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| C14 | Grant of patent or utility model | ||
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Granted publication date: 20130109 |