CN220573492U - Production device of ammonium phosphate - Google Patents
Production device of ammonium phosphate Download PDFInfo
- Publication number
- CN220573492U CN220573492U CN202320685836.4U CN202320685836U CN220573492U CN 220573492 U CN220573492 U CN 220573492U CN 202320685836 U CN202320685836 U CN 202320685836U CN 220573492 U CN220573492 U CN 220573492U
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- venturi scrubber
- gas
- liquid separator
- circulating
- tank
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- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 239000004254 Ammonium phosphate Substances 0.000 title claims abstract description 24
- 229910000148 ammonium phosphate Inorganic materials 0.000 title claims abstract description 24
- 235000019289 ammonium phosphates Nutrition 0.000 title claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 91
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims abstract description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000001035 drying Methods 0.000 claims abstract description 23
- 239000007921 spray Substances 0.000 claims abstract description 23
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims abstract description 22
- 239000000428 dust Substances 0.000 claims abstract description 21
- 239000006260 foam Substances 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 13
- 238000003860 storage Methods 0.000 claims abstract description 10
- 230000001502 supplementing effect Effects 0.000 claims description 9
- 238000007789 sealing Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 48
- 238000005406 washing Methods 0.000 description 43
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 28
- 229910021529 ammonia Inorganic materials 0.000 description 14
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 11
- 229910052731 fluorine Inorganic materials 0.000 description 11
- 239000011737 fluorine Substances 0.000 description 11
- 239000002002 slurry Substances 0.000 description 10
- 238000006386 neutralization reaction Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 7
- 239000005696 Diammonium phosphate Substances 0.000 description 5
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 5
- 229910000388 diammonium phosphate Inorganic materials 0.000 description 5
- 235000019838 diammonium phosphate Nutrition 0.000 description 5
- 238000005507 spraying Methods 0.000 description 5
- 239000002245 particle Substances 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 239000002253 acid Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005469 granulation Methods 0.000 description 3
- 230000003179 granulation Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- 238000004176 ammonification Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- YFYIWIZSIVZILB-UHFFFAOYSA-N N.[P] Chemical compound N.[P] YFYIWIZSIVZILB-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 206010039509 Scab Diseases 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The utility model discloses a production device of ammonium phosphate, and belongs to the technical field of ammonium phosphate. The device comprises a tubular reactor, a rotary drum granulator, a drying structure and a tail gas treatment structure, wherein the tail gas treatment structure comprises a cyclone dust collector, a fan, a first venturi scrubber, a circulating tank, a first circulating pump, a second venturi scrubber, a gas-liquid separator, a second circulating pump, a cyclone dust collector and a chimney, and the rotary drum granulator and the drying structure are connected with the cyclone dust collector; the cyclone dust collector, the fan, the first Venturi scrubber, the second Venturi scrubber, the gas-liquid separator, the cyclone foam remover and the chimney are sequentially connected, the first Venturi scrubber, the circulating tank and the first circulating pump form a circulating spray structure, and the second Venturi scrubber, the gas-liquid separator and the second circulating pump form a circulating spray structure; the cyclone foam remover is connected with a gas-liquid separator, the gas-liquid separator is connected with a process water storage tank, and overflows to a circulating tank; the circulation tank is connected with a dilute phosphoric acid storage tank, which is connected with the tubular reactor.
Description
Technical Field
The utility model belongs to the technical field of ammonium phosphate, and particularly relates to a production device of ammonium phosphate.
Background
Diammonium phosphate, also known as diammonium phosphate, ammonium hydrogen phosphate, is a white crystal of formula (NH) 4 ) 2 HPO 4 Which can be obtained by reacting phosphoric acid with ammonia.
A preparation method of diammonium phosphate is disclosed in the patent with the application number of CN 200910244335.7. The method comprises the following steps:
1) Adding 40% -60% phosphoric acid and 70% -90% ammonia into a tubular reactor to perform neutralization reaction to generate ammonium phosphate slurry;
2) Spraying the ammonium phosphate slurry prepared in the step 1) into a drum ammonification granulator, then introducing ammonia into a material bed of the drum ammonification granulator, further ammonifying the ammonium phosphate slurry to a neutralization degree of 1.7-1.9, granulating while ammonifying to generate a solid wet material and granulation tail gas, and drying the solid wet material to obtain the diammonium phosphate.
A production method of diammonium phosphate is disclosed in the patent with the application number of cn201610711886.X, and comprises the following steps: (1) preneutralization: adding concentrated phosphoric acid and a washing liquid into a neutralization tank to react with ammonia, wherein the reaction temperature is 100-120 ℃, the neutralization degree is 0.5-0.6, the slurry density is 1.45-1.5g/cm, the water content of the slurry is 16-20%, and the volume of the washing liquid is 1/4-1/3 of that of the neutralization tank; (2) neutralization: introducing the pre-neutralized slurry obtained in the step (1) into a tubular reactor containing 1/3-2/3 volume of washing liquid to react with ammonia, wherein the reaction temperature is 100-140 ℃, and the neutralization degree is 1.40-1.53; (3) granulating: feeding the neutralized slurry obtained in the step (2) into a granulator, and introducing ammonia to granulate, wherein the neutralization degree is 1.80-1.90; (4) finished product: drying, screening and cooling the particles obtained in the step (3) to obtain a finished product;
the washing liquid is from a washing system and is prepared from process water and phosphoric acid: the density is 1.40-1.55g/cm, and the neutralization degree is less than or equal to 0.6.
In the prior art, a venturi scrubber is used for treating granulation tail gas and dry tail gas, process water is used as spray liquid, and when the washing liquid reaches a certain concentration or density, the washing liquid containing phosphorus and ammonia is reused as raw materials.
A method for washing the tail gas of an ammonium phosphate device is disclosed in the patent of application CN 200910244336.1. The method comprises the following steps: the washing circulation tank is additionally provided with a water pipe, the water pipe is opened to enable water to be sent into the Venturi scrubber from the washing circulation pump to wash the granulating and drying tail gas, the index of the washing liquid is controlled, the replacement washing liquid is respectively discharged into the slurry collecting tank, the phosphoric acid underground tank or directly discharged into the sewage pool as required, and the sewage is pumped into the NPK device or the phosphoric acid workshop. The tail gas washing method of ammonium phosphate provided by the utility model adopts water as washing liquid, the washing liquid with high pH value can avoid overflow of fluoride in the granulating and drying tail gas in the form of HF, and neutral water has much stronger absorption of fluoride than dilute phosphoric acid. This solution, while reducing fluoride overflow, has the following problems:
(1) The water has relatively low ammonia and dust capturing rate in the granulating and drying tail gas;
(2) In order to improve the tail gas treatment effect, a large amount of water is needed for spraying, so that the water consumption is high;
(3) The large amount of water causes low temperature of the sprayed washing liquid, and heat in the granulating tail gas and the drying tail gas cannot be recovered.
Disclosure of Invention
In order to solve the problems, the embodiment of the utility model provides a production device of ammonium phosphate, which adopts two-stage compound washing and has the following effects: the primary is acid washing, phosphoric acid is used as a washing liquid, and the high-acid washing liquid has very high ammonia and dust capturing rate in tail gas; the temperature of the tail gas can be reduced, the temperature of the tail gas during secondary water washing is reduced, and the overflow of fluoride is reduced; the effect can be achieved by lower spraying amount, so that the temperature of the washing liquid is higher, and the heat in the granulating and drying tail gas can be recovered; can reduce the water consumption in the secondary water washing process. The second stage is water washing, so that the washing effect is further improved, the temperature and fluorine content in the tail gas after the first stage washing are low, and fluorine in the tail gas can be easily collected. The technical scheme is as follows:
the embodiment of the utility model provides a production device of ammonium phosphate, which comprises a tubular reactor, a rotary drum granulator, a drying structure and a tail gas treatment structure, wherein the tail gas treatment structure comprises a cyclone dust collector, a fan 1 and a scrubber, and a tail gas outlet of the rotary drum granulator and a tail gas outlet of the drying structure are connected with the cyclone dust collector; the scrubber comprises a first Venturi scrubber 2, a circulating tank 3, a first circulating pump 4, a second Venturi scrubber 5, a gas-liquid separator 6, a second circulating pump 7, a cyclone foam remover 8 and a chimney 9; the cyclone dust collector, the fan 1, the first venturi scrubber 2, the second venturi scrubber 5, the gas-liquid separator 6, the cyclone foam remover 8 and the chimney 9 are sequentially connected, the first venturi scrubber 2, the circulating tank 3 and the first circulating pump 4 form a primary circulating spray structure, and the second venturi scrubber 5, the gas-liquid separator 6 and the second circulating pump 7 form a secondary circulating spray structure; the liquid outlet of the cyclone foam remover 8 is connected with the gas-liquid separator 6 through a pipeline, the water supplementing port of the gas-liquid separator 6 is connected with the process water storage tank through a pipeline, and the liquid outlet overflows to the circulating tank 3; the circulating tank 3 is connected with a dilute phosphoric acid storage tank through a pipeline, and is connected with the tubular reactor through a pipeline.
The first Venturi scrubber 2 is arranged above the circulating tank 3, the bottom of the first Venturi scrubber is communicated with the circulating tank 3, and a spray head in the first Venturi scrubber is connected with the circulating tank 3 through a pipeline with a first circulating pump 4; the top of the circulating tank 3 is connected with the air inlet of the second venturi scrubber 5 as the air outlet of the first venturi scrubber 2.
Preferably, the circulation tank 3 in the embodiment of the present utility model is a sealing groove, and the first venturi scrubber 2 and the first circulation pump 4 are fixed on the top plate of the circulation tank 3.
The second venturi scrubber 5 is arranged above the gas-liquid separator 6, the bottom of the second venturi scrubber is connected with an air inlet at the top of the gas-liquid separator 6, and a spray head in the second venturi scrubber is connected with a liquid outlet at the bottom of the gas-liquid separator 6 through a pipeline with a second circulating pump 7; the exhaust port at the top of the gas-liquid separator 6 is connected with the air inlet of the cyclone foam remover 8 through a pipeline.
Preferably, the second venturi scrubber 5 in the embodiment of the present utility model is provided at the top of the gas-liquid separator 6.
Preferably, a hot air inlet of the drying structure in the embodiment of the utility model is connected with a hot air blower, the air outlet temperature of the hot air blower is 400-450 ℃, and the air outlet volume is 80000-90000m 3 /h。
The technical scheme provided by the embodiment of the utility model has the beneficial effects that: the embodiment of the utility model provides a production device of ammonium phosphate, which adopts two-stage compound washing and has the following effects: the primary step is acid washing, phosphoric acid (phosphoric acid by wet method contains a certain fluorine element, and overflows easily at a higher temperature) is used as a washing liquid, and the yield of ammonia and dust in tail gas is very high by the stronger acidic washing liquid; the temperature of the tail gas can be reduced, the temperature of the tail gas during secondary water washing is reduced, and the overflow of fluoride is reduced; the effect can be achieved by lower spraying amount, so that the temperature of the washing liquid is higher, and the heat in the granulating and drying tail gas can be recovered; can reduce the water consumption in the secondary water washing process. The second level is water washing, further improves the washing effect, and the temperature in the tail gas after the first level washing is low and the fluorine content is low (the fluorine content is tens of milligrams per cubic meter), and the fluorine in the tail gas can be easily collected (the fluorine content in the exhausted tail gas is less than 5 milligrams per cubic meter, and meets the emission standard). In addition, the first venturi scrubber is combined with the circulating tank, and the second venturi scrubber and the gas-liquid separator are combined together, so that occupied space can be reduced.
Drawings
FIG. 1 is a schematic block diagram of an apparatus for producing ammonium phosphate in an embodiment of the present utility model;
fig. 2 is a schematic structural view of an exhaust gas treatment structure in an embodiment of the present utility model.
In the figure: 1 fan, 2 first venturi scrubber, 3 circulation tank, 4 first circulating pump, 5 second venturi scrubber, 6 gas-liquid separator, 7 second circulating pump, 8 whirlwind foam remover, 9 chimney.
Detailed Description
The present utility model will be described in further detail with reference to the accompanying drawings, for the purpose of making the objects, technical solutions and advantages of the present utility model more apparent.
Example 1
Referring to fig. 1-2, example 1 provides an apparatus for producing ammonium phosphate, which comprises a tubular reactor for reacting all of concentrated phosphoric acid (concentrated wet phosphoric acid) with a part of ammonia, a rotary drum granulator, a drying structure, a tail gas treatment structure, and the like, and the reacted slurry is fed to the rotary drum granulator. The rotary drum granulator is used for realizing the reaction of slurry and the rest ammonia to obtain product particles with a certain size; which may be a rotary drum granulator in particular. The drying structure is used for drying the product particles, and hot air is used as a heat source. The tail gas treatment structure is used for treating dry tail gas and granulation tail gas, and is mainly used for absorbing ammonia and treating dust. The tail gas treatment structure comprises a cyclone dust collector, a fan 1, a scrubber and the like, and a tail gas outlet of the rotary drum granulator and a tail gas outlet of the drying structure are connected with the cyclone dust collector through pipelines. The structure is basically the same as that of the existing ammonium phosphate production device, and the difference is that: the scrubber in the embodiment comprises a first Venturi scrubber 2, a circulating tank 3, a first circulating pump 4, a second Venturi scrubber 5, a gas-liquid separator 6, a second circulating pump 7, a cyclone foam remover 8, a chimney 9 and the like; cyclone dust collector, fan 1, first venturi scrubber 2, second venturi scrubber 5, vapour and liquid separator 6, whirlwind demister 8 and chimney 9 connect gradually etc. vapour and liquid separator 6 and whirlwind demister 8 can realize carrying out vapour and liquid separation to the tail gas. The first venturi scrubber 2, the circulating tank 3 and the first circulating pump 4 form a primary circulating spray structure. The water supplementing port of the circulating tank 3 is connected with a dilute phosphoric acid storage tank through a pipeline with a pump to supplement dilute phosphoric acid, and the washing liquid outlet of the circulating tank is connected with a tubular reactor through the pipeline with the pump to recycle the wastewater with higher temperature and effective elements. In the first-stage circulating spray structure, dilute phosphoric acid (unconcentrated wet phosphoric acid) is used as spray liquid, the temperature of the circulating liquid in the circulating tank 3 is controlled to be 40-50 ℃, certain fluorine overflows (the second-stage circulating spray structure absorbs), and the washing liquid with higher temperature is sent to the tubular reactor to recover ammonia phosphorus and heat. The second venturi scrubber 5, the gas-liquid separator 6 and the second circulating pump 7 form a secondary circulating spray structure; the water supplementing port of the gas-liquid separator 6 is connected with the process water storage tank through a pipeline to supplement the process water, and the liquid draining port overflows to the circulating tank 3 to output the washing liquid with a certain concentration to the circulating tank 3. In the secondary circulation spray structure, water is used as spray liquid, and the temperature of the spray liquid is very low and is usually less than 30 ℃; the main function of the spraying structure is to remove fluorine, meanwhile, the dust and ammonia content are further reduced, and the dilute phosphoric acid can be further diluted by sending the washing liquid to the circulating tank 3, so that the possibility of fluorine overflow is further reduced, and the temperature is further lowered. The cyclone demister 8 is located above the gas-liquid separator 6, and its liquid outlet is connected with the gas-liquid separator 6 (specifically, water supplementing port) through a pipeline to recover separated liquid.
Referring to fig. 2, the first venturi scrubber 2 in the embodiment of the present utility model is disposed above the circulation tank 3, the bottom of the first venturi scrubber is communicated with the circulation tank 3, and the spray head therein is connected with the circulation tank 3 through a pipeline with a first circulation pump 4. The top of the circulation tank 3 (provided with an exhaust port) is connected as an exhaust port of the first venturi scrubber 2 with an intake port of the second venturi scrubber 5.
Preferably, referring to fig. 2, the circulation tank 3 in the embodiment of the present utility model is a sealing groove (rectangular groove or circular groove), and the first venturi scrubber 2 and the first circulation pump 4 are fixed to the top plate of the circulation tank 3. The first Venturi scrubber is combined with the circulating tank through the structure, so that occupied space can be reduced.
Referring to fig. 2, the second venturi scrubber 5 in the embodiment of the present utility model is disposed above the gas-liquid separator 6, the bottom of the second venturi scrubber is connected to the gas inlet at the top of the gas-liquid separator 6, and the spray head therein is connected to the liquid outlet at the bottom of the gas-liquid separator 6 through a pipeline with the second circulation pump 7. The exhaust port at the top of the gas-liquid separator 6 is connected with the air inlet of the cyclone foam remover 8 through a pipeline.
Preferably, referring to fig. 2, the second venturi scrubber 5 in the embodiment of the present utility model is provided at the top of the gas-liquid separator 6. The structure combines the second Venturi scrubber and the gas-liquid separator together, so that the occupied area can be reduced.
Preferably, a hot air inlet of the drying structure in the embodiment of the utility model is connected with a hot air blower, the air outlet temperature of the hot air blower is 400-450 ℃, and the air outlet volume is 80000-90000m 3 And/h. Specifically, the patent adopts a high-temperature low-air-volume mode to dry the particles, the temperature of hot air is increased to 400-450 ℃ from 250-350 ℃, and the air outlet air volume is increased from 120000-135000m 3 Reduced/h to 80000-90000m 3 Reducing the temperature of the dry tail gas from 80-100 ℃ to 70 ℃ (the dew point of the tail gas is 65-68 ℃); through practice, the problems of accumulation and scab of a tail gas pipeline and a tail gas fan do not occur when the temperature of the tail gas is reduced. The temperature of the tail gas is reduced, and the fluorine overflow rate during primary washing can be reduced.
Example 2
Referring to fig. 1-2, embodiment 2 provides a production apparatus of ammonium phosphate, which comprises a tubular reactor, a rotary drum granulator, a drying structure, a tail gas treatment structure and the like, wherein the tail gas treatment structure comprises a cyclone dust collector, a fan 1, a first venturi scrubber 2, a circulating tank 3, a first circulating pump 4, a second venturi scrubber 5, a gas-liquid separator 6, a second circulating pump 7, a cyclone foam remover 8, a chimney 9 and the like; the tail gas outlet of the rotary drum granulator and the tail gas outlet of the drying structure are connected with the air inlet of the cyclone dust collector through pipelines. The air outlet of the cyclone dust collector is connected with the air inlet of the first Venturi scrubber 2 through a pipeline with a fan 1. The first venturi scrubber 2 and the first circulating pump 4 are arranged at the top of the circulating tank 3; the bottom of the first Venturi scrubber 2 is communicated with the top of the circulating tank 3, and a spray head in the first Venturi scrubber is connected with the circulating tank 3 through a pipeline with a first circulating pump 4. The water supplementing port of the circulating tank 3 is connected with the upper part of the gas-liquid separator 6 through a pipeline, the water supplementing port is connected with the dilute phosphoric acid storage tank through a pipeline to supplement dilute phosphoric acid, the washing liquid outlet is connected with the tubular reactor through a pipeline with a pump, and the top of the washing liquid outlet is connected with the air inlet of the second Venturi scrubber 5 through a pipeline. The second Venturi scrubber 5 is arranged at the top of the gas-liquid separator 6, the bottom of the second Venturi scrubber is communicated with the top of the gas-liquid separator 6, and a spray head in the second Venturi scrubber is connected with a liquid outlet at the bottom of the gas-liquid separator 6 through a pipeline with a second circulating pump 7. The upper part of the gas-liquid separator 6 overflows to the circulating tank 3, the exhaust port at the top of the gas-liquid separator is connected with the air inlet of the cyclone foam remover 8 through a pipeline, and the water supplementing port at the upper part of the gas-liquid separator is connected with the process water storage tank through a pipeline. The cyclone foam remover 8 is higher than the gas-liquid separator 6, the liquid outlet at the bottom of the cyclone foam remover is connected with the water supplementing port at the upper part of the gas-liquid separator 6 through a pipeline, and the air outlet at the top of the cyclone foam remover is connected with the chimney 9 through a pipeline.
The "first" and "second" in this embodiment only play a role of distinction, and have no other special meaning. The pipeline in the embodiment is provided with a fan, a pump, a flowmeter or a valve and the like as required.
The foregoing description of the preferred embodiments of the utility model is not intended to limit the utility model to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the utility model are intended to be included within the scope of the utility model.
Claims (6)
1. The production device of the ammonium phosphate comprises a tubular reactor, a rotary drum granulator, a drying structure and a tail gas treatment structure, wherein the tail gas treatment structure comprises a cyclone dust collector, a fan (1) and a scrubber, and a tail gas outlet of the rotary drum granulator and a tail gas outlet of the drying structure are connected with the cyclone dust collector; the cyclone scrubber is characterized by comprising a first venturi scrubber (2), a circulating tank (3), a first circulating pump (4), a second venturi scrubber (5), a gas-liquid separator (6), a second circulating pump (7), a cyclone foam remover (8) and a chimney (9); the cyclone dust collector, the fan (1), the first venturi scrubber (2), the second venturi scrubber (5), the gas-liquid separator (6), the cyclone foam remover (8) and the chimney (9) are sequentially connected, the first venturi scrubber (2), the circulating tank (3) and the first circulating pump (4) form a primary circulating spray structure, and the second venturi scrubber (5), the gas-liquid separator (6) and the second circulating pump (7) form a secondary circulating spray structure; the liquid outlet of the cyclone foam remover (8) is connected with the gas-liquid separator (6) through a pipeline, the water supplementing port of the gas-liquid separator (6) is connected with the process water storage tank through a pipeline, and the liquid outlet overflows to the circulating tank (3); the circulating tank (3) is connected with the dilute phosphoric acid storage tank through a pipeline, and is connected with the tubular reactor through a pipeline.
2. The ammonium phosphate production device according to claim 1, wherein the first venturi scrubber (2) is arranged above the circulation tank (3), the bottom of the first venturi scrubber is communicated with the circulation tank (3), and a spray head in the first venturi scrubber is connected with the circulation tank (3) through a pipeline with a first circulation pump (4); the top of the circulating groove (3) is used as an exhaust port of the first Venturi scrubber (2) to be connected with an air inlet of the second Venturi scrubber (5).
3. The production device of ammonium phosphate according to claim 2, characterized in that the circulation tank (3) is a sealing groove, and the first venturi scrubber (2) and the first circulation pump (4) are fixed on the top plate of the circulation tank (3).
4. The ammonium phosphate production device according to claim 1, wherein the second venturi scrubber (5) is arranged above the gas-liquid separator (6), the bottom of the second venturi scrubber is connected with the gas inlet at the top of the gas-liquid separator (6), and the spray head in the second venturi scrubber is connected with the liquid outlet at the bottom of the gas-liquid separator (6) through a pipeline with a second circulating pump (7); the exhaust port at the top of the gas-liquid separator (6) is connected with the air inlet of the cyclone foam remover (8) through a pipeline.
5. The production plant of ammonium phosphate according to claim 4, characterized in that the second venturi scrubber (5) is arranged at the top of the gas-liquid separator (6).
6. The ammonium phosphate production device according to claim 1, wherein the hot air inlet of the drying structure is connected with a hot air blower, the air outlet temperature of the hot air blower is 400-450 ℃, and the air outlet volume is 80000-90000m 3 /h。
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| Application Number | Priority Date | Filing Date | Title |
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| CN202320685836.4U CN220573492U (en) | 2023-03-31 | 2023-03-31 | Production device of ammonium phosphate |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320685836.4U CN220573492U (en) | 2023-03-31 | 2023-03-31 | Production device of ammonium phosphate |
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| CN220573492U true CN220573492U (en) | 2024-03-12 |
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| CN202320685836.4U Active CN220573492U (en) | 2023-03-31 | 2023-03-31 | Production device of ammonium phosphate |
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| CN (1) | CN220573492U (en) |
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