CN201873524U - Device for producing monopotassium phosphate with wet-process phosphoric acid purification technology - Google Patents
Device for producing monopotassium phosphate with wet-process phosphoric acid purification technology Download PDFInfo
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- CN201873524U CN201873524U CN2010206331240U CN201020633124U CN201873524U CN 201873524 U CN201873524 U CN 201873524U CN 2010206331240 U CN2010206331240 U CN 2010206331240U CN 201020633124 U CN201020633124 U CN 201020633124U CN 201873524 U CN201873524 U CN 201873524U
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Abstract
The utility model discloses a device for producing monopotassium phosphate with a wet-process phosphoric acid purification technology, comprising a phosphoric acid purification storage tank, a feed pump, a raw material acid preheater, a dissolving tank, a potassium chloride acid solution conveyer pump, an extraction pump, a back extraction tank, an ammonium chloride solution temporary storing tank, an ammonium chloride crystallization tank, a first centrifugal machine, a mother liquor tank, a circulating pump, a concentration evaporator, a mixing condenser, a circulating pool, a circulating water pump and a cooling tower, wherein an outlet of the feed pump is communicated with a material inlet of the raw material acid preheater; a material outlet of the raw material acid preheater is communicated with an inlet of a potassium chloride solution tank; and a material inlet of the top of the dissolving tank is communicated with a potassium chloride storage hopper. The device has simple process flow, mild reaction condition, less corrosion of equipment, high purity of a monopotassium phosphate product, and large potassium yield, produces ammonium chloride by-products, can realize cyclic regeneration of an extracting agent, and saves the production cost.
Description
Technical field
The utility model relates to a kind chemical plant installations, relates in particular to a kind of device of wet purification phosphoric acid production potassium primary phosphate.
Background technology
Potassium primary phosphate is a kind of important chemical, has a wide range of applications in industries such as agricultural, industry, food, medicine.In the processing method of existing preparation potassium primary phosphate, though the neutralisation technical process is simple, technology maturation, facility investment is few, and stable and reliable product quality is a raw material with thermal phosphoric acid and potash, costs an arm and a leg, and production cost is too high; The direct method energy expenditure is very big, and equipment corrosion is serious, also can cause quality product relatively poor because of side reaction; Double decomposition with compare cost than neutralisation and reduce, but the transformation efficiency of potassium is low, equipment corrosion is serious, non-standard equipment is many, unstable product quality; Ion exchange method can be produced high-quality potassium primary phosphate, but energy consumption is too high, and one-time investment is bigger, and actually operating has a lot of troubles; Electrolytic process technology is simple, and electrolysis is finished more thorough, but as a kind of large-scale Industrial products production method, more difficult point is arranged technically.By contrast, the extraction process technical process is simple, and scale is changeable, and low temperature is reaction down, and equipment corrosion is little, and cost is low, does not have " three wastes " and pollutes, and shortcoming is the organic solvent costliness, invests higher.Extraction process is present advanced person, has the industrial process of development prospect.
This is suitable for novel is to utilize purification of wet process phosphoric acid and industrial potassium chloride to be raw material, the production equipment of extraction preparation potassium primary phosphate technology.
Raw material phosphoric acid, Repone K and extraction agent are together added, and reaction and extraction are carried out simultaneously, and the water after will extracting again separates with organic phase, obtains the product potassium primary phosphate from aqueous phase, recycle after the organic phase regeneration.
Reaction formula is (M is an extraction agent):
H
3PO
4+KCl=KH
2PO
4+HCl
HCl+M=HCl?M
HCl?M+NH
3=M+NH
4Cl
This explained hereafter device can realize that by purification of wet process phosphoric acid and industrial potassium chloride be feedstock production high-purity phosphoric acid potassium dihydrogen technology, has rate of recovery height, cheaply advantage.
The utility model content
Technical problem to be solved in the utility model is to provide a kind of yield and purity height of potassium primary phosphate, and production consumes low, by recycle extraction agent and the coproduction of realization ammonium chloride, reduces the device of potassium primary phosphate production cost.
The technical solution of the utility model is as follows: a kind of device of wet purification phosphoric acid production potassium primary phosphate is characterized in that: described device mainly is communicated with successively by purifying phosphoric acid storage tank, feeding pump, raw material acid preheater, dissolving tank, Repone K acid solution transferpump, extraction tank, back extraction groove, the temporary storage tank of ammonium chloride solution, ammonium chloride crystals groove, first whizzer, mother liquor tank, recycle pump, concentration evaporator, mixing condenser, circulating water pool, water circulating pump, cooling tower and constitutes;
Described feeding pump outlet is connected with raw material acid preheater opening for feed, and described raw material acid preheater discharge port is connected with the import of Repone K dissolving tank, and described dissolving tank its top feed mouth is communicated with the Repone K bucket;
Described back extraction trench bottom discharge port is communicated with the temporary storage tank of ammonium chloride solution, this back extraction groove upper part discharge port is connected with rinse bath, rinse bath bottom discharge mouth is connected by the opening for feed of rinse bath recycle pump with back extraction groove top, and the rinse bath upper part discharge port is connected by the opening for feed of extraction agent recycle pump with the extraction tank top;
The temporary storage tank centre exit of described ammonium chloride solution is connected with the opening for feed of back extraction groove by back extraction groove recycle pump,
The temporary storage tank of described ammonium chloride solution top overflow port is connected with mother liquor tank its top feed mouth,
Ammonium chloride crystals groove top overflow port is connected with mother liquor tank its top feed mouth,
Mother liquor tank bottom discharge mouth is connected with concentration evaporator bottom discharge pipe by recycle pump, concentration evaporator bottom discharge pipe is connected with concentrated pump inlet, the discharge port that concentrates recycle pump is connected with the opening for feed of concentration heater, the discharge port of concentration heater is connected with the opening for feed of concentration evaporator
The water outlet of mixing condenser is connected with the circulating water pool water-in, and the water outlet of circulating water pool is connected with the water-in of cooling tower by water circulating pump, and the water outlet of cooling tower is connected with the water-in of mixing condenser.
Above-mentioned extraction tank bottom discharge mouth is in series with potassium dihydrogen phosphate storage tank, transferpump, second vaporizer, first recycle pump, second recycle pump, the 3rd well heater, vaporizer, crystallizer, stiff device, whizzer, first mother liquor tank successively through pipeline, this first mother liquor tank discharge port is communicated with circulation loop of formation again with potassium dihydrogen phosphate storage tank opening for feed, the described stiff device and first mother liquor tank two whizzers in parallel;
Through pipe connection second concentration heater is arranged between described second vaporizer and first recycle pump,
The described second base of evaporator discharge port is connected by the opening for feed of first recycle pump with second concentration heater, the discharge port of second concentration heater is connected with the opening for feed of second vaporizer, the venting port at the second vaporizer top is connected with the inlet mouth of the 3rd concentration heater, and the discharge port of first recycle pump is connected with the feed-pipe of second recycle pump;
The discharge port of base of evaporator is connected with the crystallizer opening for feed, and the crystallizer upper part discharge port is connected with second inlet of circulating pump.
Above-mentioned first whizzer and the second whizzer bottom discharge mouth all are connected with the opening for feed of moisture eliminator by transfer roller, and moisture eliminator is connected with bucket, and the discharge port of moisture eliminator is connected with the bucket opening for feed.
The hot-blast outlet of above-mentioned hotblast stove is communicated with calorifier and is connected with the hot blast import of moisture eliminator, the outlet of cooling blower is connected with the cold wind import of moisture eliminator, moisture eliminator is communicated with fly-ash separator, exhaust fan, washing tower, washing tank, cleaning circulation pump successively through pipeline, this cycles of washing pump discharge is connected with the fluid inlet of whizzer (35/36) upper inlet and washing tower respectively again, the air outlet of moisture eliminator is connected with the inlet mouth of fly-ash separator, and the discharge port of fly-ash separator bottom is connected with product bucket opening for feed.
Above-mentioned vaporizer is communicated with second mixing condenser, the air outlet, top of described vaporizer is connected with the inlet mouth of second mixing condenser, mixing condenser liquid outlet be connected with the water-in of circulating water pool, cooling tower bottom water outlet is connected with the water-in of second mixing condenser.
Beneficial effect: beneficial effect: utility model device technique flow process is simple, the reaction conditions gentleness, and equipment corrosion is little, product potassium primary phosphate purity height, the potassium yield is big, and the combined producting ammonium chloride byproduct, can realize extraction agent cyclic regeneration in addition, has saved production cost.
Description of drawings
Fig. 1 be the utility model equipment upper part;
Fig. 2 be the utility model equipment lower part.
Embodiment
The utility model is described in further detail below in conjunction with drawings and Examples:
Step 1:
As shown in Figure 1, purification of wet process phosphoric acid is pumped to phosphoric acid preheater 3 from storage tank 1 through transferpump 2, phosphoric acid after the preheating enters dissolving tank 4, directly send into extraction tank 7 and extraction agent reaction through transferpump 6 after will fully dissolving from the Repone K of bucket 5, extraction tank 7 upper organic phase flow into back extraction groove 8 through overflow port and fully react with the reverse-extraction agent gas ammonia, make extractant regeneration, extraction agent after the regeneration flows into rinse bath 9 through the overflow port on back extraction groove 8 tops, adding washings makes extraction agent obtain thorough washing, extraction agent after the washing returns extraction tank 7 through pump 11, realizes the extraction agent recycle.The inorganic phase ammonium chloride solution in bottom is through flowing into temporary storage tank 12 in the back extraction groove 8, the storage tank top stillness of night flows into mother liquor tank 16 through overflow port temporarily, the bottom dope flows into crystallizer tank 14, the ammonium chloride crystals mixed solution that comes out from crystallizer tank enters whizzer 15, and the ammonium chloride product that comes out from whizzer directly advances byproduct dress bag system; The ammonium chloride mother liquor that comes out from whizzer 15 enters mother liquor tank 16, ammonium chloride mother liquor is admitted to concentration systems through pump 17, under the effect that concentrates recycle pump 20, concentration heater 19 and concentration evaporator 18, ammonium chloride mother liquor is concentrated, ammonium chloride solution after concentrating enters crystallizer through the discharge port of vaporizer 18, realizes the ammonium chloride continuous crystallisation.The evaporated liquor that comes out from vaporizer 18 tops enters mixing condenser 21 condensations, further enters the circulating condensing water system.
Step 2:
As shown in Figure 2, the potassium dihydrogen phosphate that comes out from extraction tank 7 bottoms enters storage tank 25, squeeze into by concentration evaporator 27 through transferpump 26 potassium dihydrogen phosphates, the one-level concentration systems that second concentration heater 28 and first recycle pump 29 are formed, the potassium dihydrogen phosphate that comes out from the one-level concentration systems enters by second recycle pump 30, concentration heater 31, the secondary concentration systems that concentration evaporator (32) and crystallizer 33 are formed further concentrates, the potassium primary phosphate mixed crystal liquid that comes out from crystallizer 33 enters stiff device 34, the mixed crystal liquid that comes out from the stiff device enters whizzer 35,36, the 34 upper strata stillnesss of night of stiff device enter first mother liquor tank 37 from overflow port, from whizzer 35,36 mother liquors that come out enter first mother liquor tank 37, mother liquor first mother liquor tank 37 supernatant liquids return concentration systems, lower floor's magma returns thick back device 34 through transferpump 38, from whizzer 35,36 potassium dihydrogen phosphate product of coming out enter moisture eliminator 40 by rotary conveyor 39, enter the dress bag system through the exsiccant potassium dihydrogen phosphate product, warm air is from hotblast stove 47, under the effect of hotblast stove 48, enter moisture eliminator 40, that comes out from tail gas under the effect of induced draft fan 43 from moisture eliminator 40 venting ports enters fly-ash separator 42, after enter washing tower (44), last emptying.
Step 3:
As shown in Figure 2, the steam that comes out from one-level vaporizer 27 tops enters secondary concentration heater 31, the steam that comes out from secondary evaporimeter 32 tops enters second mixing condenser 50 and carries out condensation, further enter the circulating condensing water system, circulating condensing water is squeezed into water cooling tower 53 and is cooled off under the effect of water of condensation recycle pump 52.
Although below in conjunction with the accompanying drawings preferred embodiment of the present utility model is described; but the utility model is not limited to above-mentioned embodiment; above-mentioned embodiment only is schematic rather than determinate; those of ordinary skill in the art is under enlightenment of the present utility model; under the prerequisite of the utility model aim and claim; can make multiple similar expression, such conversion all falls within the protection domain of the present utility model.
Claims (5)
1. the device of a wet purification phosphoric acid production potassium primary phosphate, it is characterized in that: described device is mainly by purifying phosphoric acid storage tank (1), feeding pump (2), raw material acid preheater (3), dissolving tank (4), Repone K acid solution transferpump (6), extraction tank (7), back extraction groove (8), the temporary storage tank of ammonium chloride solution (12), ammonium chloride crystals groove (14), first whizzer (15), mother liquor tank (16), recycle pump (17), concentration evaporator (18), mixing condenser (21), circulating water pool (22), water circulating pump (23), cooling tower (24) is communicated with formation successively;
Described raw material acid preheater (3) discharge port is connected with Repone K dissolving tank (4) import, and described dissolving tank (4) its top feed mouth is communicated with Repone K bucket (5);
Described back extraction groove (8) bottom discharge mouth is communicated with the temporary storage tank of ammonium chloride solution (12), this back extraction groove (8) upper part discharge port is connected with rinse bath (9), rinse bath (9) bottom discharge mouth is connected by the opening for feed of rinse bath recycle pump (10) with back extraction groove (8) top, and rinse bath (9) upper part discharge port is connected by the opening for feed of extraction agent recycle pump (11) with extraction tank (7) top;
The temporary storage tank of described ammonium chloride solution (12) centre exit is connected by the opening for feed of back extraction groove recycle pump (13) with back extraction groove (8),
The temporary storage tank of described ammonium chloride solution (12) top overflow port is connected with mother liquor tank (16) its top feed mouth,
Ammonium chloride crystals groove (14) top overflow port is connected with mother liquor tank (16) its top feed mouth,
Mother liquor tank (16) bottom discharge mouth is connected with concentration evaporator (18) bottom discharge pipe by recycle pump (17), concentration evaporator (18) bottom discharge pipe is connected with concentrated recycle pump (20) import, the discharge port that concentrates recycle pump (20) is connected with the opening for feed of concentration heater (19), the discharge port of concentration heater (19) is connected with the opening for feed of concentration evaporator (18)
The water outlet of mixing condenser (21) is connected with circulating water pool (22) water-in, the water outlet of circulating water pool (22) is connected by the water-in of water circulating pump (23) with cooling tower (24), and the water outlet of cooling tower (24) is connected with the water-in of mixing condenser (21).
2. according to the device of the described wet purification phosphoric acid production of claim 1 potassium primary phosphate, it is characterized in that: described extraction tank (7) bottom discharge mouth is communicated with potassium dihydrogen phosphate storage tank (25) successively through pipeline, transferpump (26), second vaporizer (27), first recycle pump (29), second recycle pump (30), the 3rd well heater (31), vaporizer (32), crystallizer (33), stiff device (34), whizzer, first mother liquor tank (37), this first mother liquor tank (37) discharge port is communicated with circulation loop of formation, described stiff device (34) and first mother liquor tank (37) first whizzer () in parallel and second whizzer again with potassium dihydrogen phosphate storage tank (25) opening for feed;
Through pipe connection second concentration heater (28) is arranged between described second vaporizer (27) and first recycle pump (29),
Described second vaporizer (27) bottom discharge mouth is connected by the opening for feed of first recycle pump (29) with second concentration heater (28), the discharge port of second concentration heater (28) is connected with the opening for feed of second vaporizer (27), the venting port at second vaporizer (27) top is connected with the inlet mouth of the 3rd concentration heater (31), and the discharge port of first recycle pump (29) is connected with the feed-pipe of second recycle pump (30);
The discharge port of vaporizer (32) bottom is connected with crystallizer (33) opening for feed, and crystallizer (33) upper part discharge port is connected with the import of second recycle pump (30).
3. according to the device of the described wet purification phosphoric acid production of claim 1 potassium primary phosphate, it is characterized in that: described first whizzer (35) and second whizzer (36) bottom discharge mouth all are connected by the opening for feed of transfer roller (39) with moisture eliminator (40), moisture eliminator (40) is connected with bucket (41), and the discharge port of moisture eliminator is connected with bucket (41) opening for feed.
4. according to the device of the described wet purification phosphoric acid production of claim 3 potassium primary phosphate, it is characterized in that: the hot-blast outlet of described hotblast stove (47) is communicated with calorifier (48) and is connected with the hot blast import of moisture eliminator (40), the outlet of cooling blower (49) is connected with the cold wind import of moisture eliminator (40), moisture eliminator (40) is communicated with fly-ash separator (42) successively through pipeline, exhaust fan (43), washing tower (44), washing tank (45), cleaning circulation pump (46), this cleaning circulation pump (46) outlet is connected with the fluid inlet of first whizzer (35) and second whizzer (36) upper inlet and washing tower (44) respectively again, the air outlet of moisture eliminator (40) is connected with the inlet mouth of fly-ash separator (42), and the discharge port of fly-ash separator (42) bottom is connected with product bucket (41) opening for feed.
5. according to the device of the described wet purification phosphoric acid production of claim 1 potassium primary phosphate, it is characterized in that: described vaporizer (32) is communicated with second mixing condenser (50), the air outlet, top of described vaporizer (32) is connected with the inlet mouth of second mixing condenser (50), mixing condenser liquid outlet be connected with the water-in of circulating water pool (22), cooling tower (24) bottom water outlet is connected with the water-in of second mixing condenser (50).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206331240U CN201873524U (en) | 2010-11-30 | 2010-11-30 | Device for producing monopotassium phosphate with wet-process phosphoric acid purification technology |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206331240U CN201873524U (en) | 2010-11-30 | 2010-11-30 | Device for producing monopotassium phosphate with wet-process phosphoric acid purification technology |
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| Publication Number | Publication Date |
|---|---|
| CN201873524U true CN201873524U (en) | 2011-06-22 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010206331240U Expired - Lifetime CN201873524U (en) | 2010-11-30 | 2010-11-30 | Device for producing monopotassium phosphate with wet-process phosphoric acid purification technology |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113415791A (en) * | 2021-06-25 | 2021-09-21 | 云南云天化红磷化工有限公司 | Device and method for recovering extractant in production of monopotassium phosphate by wet-process phosphoric acid extraction |
-
2010
- 2010-11-30 CN CN2010206331240U patent/CN201873524U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113415791A (en) * | 2021-06-25 | 2021-09-21 | 云南云天化红磷化工有限公司 | Device and method for recovering extractant in production of monopotassium phosphate by wet-process phosphoric acid extraction |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: THE ENGINEERING RESEARCH CENTER OF SINOFERT CHONGQ Effective date: 20120405 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20120405 Address after: 408000 Chongqing Road, Fuling District No. 2 Co-patentee after: Chongqing Phosphate & Compound Fertilizer Engineering Technology Research Center of Sinofert Holdings Limited Patentee after: Zhonghua Chongqing Fulin Chemical Co., Ltd. Address before: 408000 Chongqing Road, Fuling District No. 2 Patentee before: Zhonghua Chongqing Fulin Chemical Co., Ltd. |
|
| ASS | Succession or assignment of patent right |
Owner name: ZHONGHUA CHONGQING FULIN CHEMICAL CO., LTD. Free format text: FORMER OWNER: CHONGQING PHOSPHATE COMPOUND FERTILIZER ENGINEERING TECHNOLOGY RESEARCH CENTER OF SINOFERT CO., LTD. Effective date: 20150402 Owner name: SINOFERT LIMITED Free format text: FORMER OWNER: ZHONGHUA CHONGQING FULIN CHEMICAL CO., LTD. Effective date: 20150402 |
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| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 408000 FULING, CHONGQING TO: 100031 XICHENG, BEIJING |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20150402 Address after: 100031 Beijing city Xicheng District fuxingmennei Street 28, Chemsunny World Trade Center in the 10 blocks Patentee after: Sinofert Holding Limited Patentee after: Zhonghua Chongqing Fulin Chemical Co., Ltd. Address before: 408000 Chongqing Road, Fuling District No. 2 Patentee before: Zhonghua Chongqing Fulin Chemical Co., Ltd. Patentee before: Chongqing Phosphate & Compound Fertilizer Engineering Technology Research Center of Sinofert Holdings Limited |
|
| CX01 | Expiry of patent term |
Granted publication date: 20110622 |
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| CX01 | Expiry of patent term |