CN203196371U - Continuous potassium dihydrogen phosphate crystallization device - Google Patents
Continuous potassium dihydrogen phosphate crystallization device Download PDFInfo
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- CN203196371U CN203196371U CN201320178302.9U CN201320178302U CN203196371U CN 203196371 U CN203196371 U CN 203196371U CN 201320178302 U CN201320178302 U CN 201320178302U CN 203196371 U CN203196371 U CN 203196371U
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- dihydrogen phosphate
- potassium dihydrogen
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 67
- 230000008025 crystallization Effects 0.000 title claims abstract description 50
- 235000019796 monopotassium phosphate Nutrition 0.000 title claims abstract description 37
- 229910000402 monopotassium phosphate Inorganic materials 0.000 title claims abstract description 37
- PJNZPQUBCPKICU-UHFFFAOYSA-N phosphoric acid;potassium Chemical compound [K].OP(O)(O)=O PJNZPQUBCPKICU-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 238000007599 discharging Methods 0.000 claims abstract description 44
- 239000012452 mother liquor Substances 0.000 claims abstract description 37
- 239000007788 liquid Substances 0.000 claims description 48
- 238000009834 vaporization Methods 0.000 claims description 27
- 230000008016 vaporization Effects 0.000 claims description 27
- 239000000498 cooling water Substances 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 7
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 238000000034 method Methods 0.000 abstract description 15
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 238000001816 cooling Methods 0.000 abstract description 6
- 238000001704 evaporation Methods 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000002562 thickening agent Substances 0.000 abstract 4
- 230000008020 evaporation Effects 0.000 abstract 3
- 239000013078 crystal Substances 0.000 description 12
- 239000000126 substance Substances 0.000 description 12
- 238000003756 stirring Methods 0.000 description 8
- 239000012530 fluid Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 5
- 239000002826 coolant Substances 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 235000015097 nutrients Nutrition 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 235000014680 Saccharomyces cerevisiae Nutrition 0.000 description 1
- LEHOTFFKMJEONL-UHFFFAOYSA-N Uric Acid Chemical compound N1C(=O)NC(=O)C2=C1NC(=O)N2 LEHOTFFKMJEONL-UHFFFAOYSA-N 0.000 description 1
- RDXARWSSOJYNLI-UHFFFAOYSA-N [P].[K] Chemical compound [P].[K] RDXARWSSOJYNLI-UHFFFAOYSA-N 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 235000010855 food raising agent Nutrition 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 238000012858 packaging process Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- OQZCJRJRGMMSGK-UHFFFAOYSA-M potassium metaphosphate Chemical compound [K+].[O-]P(=O)=O OQZCJRJRGMMSGK-UHFFFAOYSA-M 0.000 description 1
- 229940099402 potassium metaphosphate Drugs 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010900 secondary nucleation Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model discloses a continuous potassium dihydrogen phosphate crystallization device which comprises a first-stage continuous flash evaporation crystallizer, a crystallization feeding pump, a second-stage continuous cooling crystallizer, a crystallization discharging pump, a thickener, a centrifugal machine and a mother liquor tank, wherein the first-stage continuous flash evaporation crystallizer is communicated with the second-stage continuous cooling crystallizer through the crystallization feeding pump; the second-stage continuous cooling crystallizer is communicated with the thickener through the crystallization discharging pump; the thickener is communicated with the centrifugal machine; the centrifugal machine is communicated with a subsequent potassium dihydrogen phosphate processing section; the first-stage continuous flash evaporation crystallizer, the second-stage continuous cooling crystallizer, the thickener and the centrifugal machine are respectively communicated with the mother liquor tank. The continuous potassium dihydrogen phosphate crystallization device is high in production value, small in occupying area, stable and reliable to operate and low in running energy consumption and labor intensity; the productivity and the efficiency of potassium dihydrogen phosphate are improved; the investment cost of the crystallization device is greatly saved; the stability and the reliability of the crystallization process are effectively enhanced.
Description
Technical field
The utility model relates to the process units of potassium dihydrogen phosphate, relates in particular to a kind of crystallization apparatus of potassium dihydrogen phosphate.
Background technology
Potassium dihydrogen phosphate is a kind of important chemicals, all has a wide range of applications in industries such as agricultural, industry, medicine and food.Industrial, potassium dihydrogen phosphate can be used as nutrient chemical, hardening agent, leavening agent of raw material, fermentation assistant and the brewer's yeast of buffer, nutrient chemical, potassium metaphosphate processed etc.; On agricultural, potassium dihydrogen phosphate is a kind of efficient phosphorus potassium complex fertilizer of high concentration; Pharmaceutically, potassium dihydrogen phosphate can be used for making uric acidization, makes nutritional agents etc.; On food, potassium dihydrogen phosphate can be used as the flavor enhancement of synthetic sake.
At present, the process of China's production potassium dihydrogen phosphate mainly contains neutralisation, extraction, double decomposition and ion-exchange etc.Above-mentioned preparation method's common ground is: at first make potassium dihydrogen phosphate by reaction, then gained solution is obtained final products through concentrated, crystallization, centrifugation, drying and other steps.Wherein, the technical process that concentrate, crystallization, centrifugation, drying and other steps all belongs to separation, purification potassium dihydrogen phosphate, and in this technical process, crystallisation step is its core procedure.
The crystallizer that the crystallization apparatus of existing potassium dihydrogen phosphate adopts is many based on simple stirring pot type crystallizer, there is following shortcoming in this crystallization apparatus: 1) the separate unit treating capacity is less relatively: stirring the required cold of pot type crystallizer is provided by chuck and inner coil pipe heat exchange, because heat exchange area is less relatively, make its rate of temperature fall be restricted, thereby cause the time of crystallization process longer, the treating capacity that separate unit stirred in the pot type crystallizer unit interval is less; Therefore, when large-scale production, need a large amount of stirring pot type crystallizers, area of mill site is huge; 2) stirring pot type crystallizer heat exchange area is less, therefore requires the medium of heat exchange both sides to keep reasonably temperature difference, needs in the crystallization process temperature and the flow of cooling medium are constantly adjusted to satisfy production requirement; And should requirement can be easy to cause material and heat-transfer surface contact site local overcooling in the operation, material is tied on the heat-transfer surface, and then the feasible heat-transfer effect variation that stirs the pot type crystallizer, causes that finally the amount of labour of operation subsequent treatment strengthens; 3) stir the pot type crystallizer in operating process, material takes place to reveal and splash easily, and the operation site environment is more abominable; 4) stir the pot type crystallizer and operate with intermittent mode usually, this mode of operation needs a large amount of personnel, and running cost is higher; 5) because the professional qualities between personnel and personnel there are differences, so the poor stability of whole crystallization operation and product, the product quality of different batches may there are differences.
Because there is above-mentioned shortcoming in the crystallization apparatus in the existing potassium dihydrogen phosphate production, make that the production capacity of whole potassium dihydrogen phosphate process units is less relatively, operating cost is higher, and floor space is big.
Summary of the invention
The utility model technical issues that need to address provide a kind of continous-stable operation, production capacity height, potassium dihydrogen phosphate crystallization apparatus that operating cost is low.
For solving the problems of the technologies described above, the technical scheme that the utility model adopts is:
Potassium dihydrogen phosphate continuous crystallisation device comprises the one-level successive flash vaporization crystallizer, crystallization punishment in advance pump, the continuous cooler crystallizer of secondary, crystallization discharging pump, stiff device, centrifuge and the mother liquor tank that are communicated with successively;
The charging aperture of described one-level successive flash vaporization crystallizer bottom is connected with liquor inlet to be crystallized, the discharging opening of one-level successive flash vaporization crystallizer bottom is connected by the charging aperture of crystallization punishment in advance pump with the continuous cooler crystallizer of secondary top, the discharging opening of the continuous cooler crystallizer of described secondary bottom is connected by the charging aperture of crystallization discharging pump with stiff device top, the discharging opening of described stiff device bottom and the charging aperture at centrifuge top are connected, and the discharging opening of described centrifuge bottom is connected with potassium dihydrogen phosphate solid subsequent treatment workshop section through the product outlet;
The liquid outlet of the continuous cooler crystallizer of outlet, secondary at described one-level successive flash vaporization crystallizer middle part and the overfall on stiff device top, centrifuge bottom is connected with the charging aperture at mother liquor tank top separately.
Further improvement of the present invention is: the discharging opening of described mother liquor tank bottom is connected with the recoil mouth of mother liquor outlet and stiff device bottom respectively by the mother liquor pump.
Further improvement of the present invention is: described one-level successive flash vaporization crystallizer is the DTB vacuum crystallizer, the gas outlet at described one-level successive flash vaporization crystallizer top is connected with steam and condensate system through the indirect steam outlet, and the overfall at one-level successive flash vaporization crystallizer middle part is connected with thin brilliant arrester by the thin brilliant pump of eliminating; The discharging opening of described thin brilliant arrester is communicated with closed circuit of formation with the charging aperture of one-level successive flash vaporization crystallizer; Steam enters from the air inlet at thin brilliant arrester top through the steam inlet, and the steam condensate that forms after the heat exchange is discharged through the steam condensate (SC) outlet from the gas outlet of thin brilliant arrester bottom and is communicated with the steam condensate (SC) treatment system.
Further improvement of the present invention is: the continuous cooler crystallizer of described secondary is made of outer cooler and Oslo crystallizer, the discharging opening of described one-level successive flash vaporization crystallizer bottom is connected by the central downtake of crystallization punishment in advance pump with Oslo crystallizer top, the overfall on Oslo crystallizer top is connected with the charging aperture at mother liquor tank top, and the Oslo crystallizer is connected with the charging aperture on outer cooler top by the crystallisation cycle pump that is arranged at its top; The discharging opening on described outer cooler top is communicated with closed circuit of formation with the central downtake on Oslo crystallizer top; The homonymy on outer cooler bottom and top arranges water inlet and delivery port respectively, and described water inlet and described delivery port are connected by cooling water circulating pump.
Because the technological progress of having adopted technique scheme, the utility model to obtain is:
The utility model potassium dihydrogen phosphate continuous crystallisation device, device output value height, floor space is little, stable operation is reliable, operation energy consumption is few, the required labour intensity of operation is low, overcome existing potassium dihydrogen phosphate and produced the corresponding shortcoming of crystallization apparatus, volume increase, the synergy of potassium dihydrogen phosphate have been realized, greatly save the cost of investment of crystallization apparatus, and effectively improved stability and the reliability of crystallization processes.
The utility model potassium dihydrogen phosphate continuous crystallisation device mainly comprises one-level successive flash vaporization crystallizer and the continuous cooler crystallizer of secondary, at first adopt one-level successive flash vaporization crystallizer effectively to reduce the temperature of feed liquid to be crystallized, and then utilize the continuous cooler crystallizer of secondary that feed liquid to be crystallized is carried out further effectively crystallization, greatly reduced the thermic load of crystallizer, help to reduce the heat exchange area of crystallizer, finally realized the reduction that reduces and invest of crystallization plant area area.One-level successive flash vaporization crystallizer can be controlled the temperature of feed liquid to be crystallized in 60 ℃～65 ℃ scope in the utility model, and the continuous cooler crystallizer of secondary can be controlled the temperature of feed liquid to be crystallized below 40 ℃.
The discharging opening of mother liquor tank described in the utility model bottom is connected with the recoil mouth of mother liquor outlet and stiff device bottom respectively by the mother liquor pump, can solve in the stiff device solid-liquid two phase fluid owing to the blockage problem that the solid sedimentation causes, the operation that the system that makes can continous-stable.
One-level successive flash vaporization crystallizer described in the utility model is the DTB vacuum crystallizer, and the DTB vacuum crystallizer belongs to typical magma inner circulation type crystallizer.The required pressure head of circulation is very low in this crystallizer, make screw be able to work under lower rotating speed, thereby has significantly reduced the secondary nucleation that impeller brings the collision of crystal.This makes this crystallizer can produce the crystal than coarsegrain.Feed liquid to be crystallized forms a closed circuit under the promotion of the screw of DTB vacuum crystallizer, make feed liquid evenly mix in the DTB vacuum crystallizer, and environment of crystal growth is good, can make the sedimentation from feed liquid to be crystallized of most of crystal, separate.The feed liquid that contains thin crystalline substance is discharged from the overfall of DTB vacuum crystallizer, has eliminated thin crystalline substance to the influence of crystal size growth, has realized the control to crystal size.Enough vapor-liquid separation spaces are arranged at the top of DTB crystallizer, can prevent entrainment effectively.
One-level successive flash vaporization crystallizer outer setting described in the utility model thin brilliant arrester, the feed liquid that contains thin crystalline substance is heated by steam in thin brilliant arrester and makes thin brilliant dissolving, and then enter participation circulation in the DTB vacuum crystallizer, greatly improved the crystallization rate of recovery of feed liquid to be crystallized.
The continuous cooler crystallizer of secondary described in the utility model is made up of Oslo crystallizer and outer cooler, this set-up mode is arranged zone and the crystal production zone branch that degree of supersaturation produces, gained secondary clear liquid is by the compulsory outer circulation of formation between Oslo crystallizer and outer cooler of crystallisation cycle pump, make fluidized suspension in the circulation fluid of crystal in the Oslo crystallizer, for crystal production provides good conditions, can produce granularity crystal greatly and uniformly.The Oslo crystallizer belongs to clear liquid or half clear liquid outer circulation type crystallizer, has reduced the possibility of crystal knot wall widely, has increased usage ratio of equipment, has prolonged equipment life.The flow velocity of the heat exchanger tube inner fluid of outer cooler can reach 1.5～1.8m/s, and heat transfer coefficient is bigger, and resistive connection dirt performance is good, is convenient to switch under the continued operation state clean.
The utility model floor space is less, be stir the pot type crystallizer the plant area area 1/5～1/10.Description of drawings
Fig. 1 is potassium dihydrogen phosphate continuous crystallisation schematic representation of apparatus of the present utility model.
Wherein, 1, thin brilliant arrester; 2, one-level successive flash vaporization crystallizer; 3, the continuous cooler crystallizer of secondary; 3-1, outer cooler; 3-2, Oslo crystallizer; 4, stiff device; 5, centrifuge; 6, mother liquor tank; 7, the thin brilliant pump of eliminating; 8, crystallization punishment in advance pump; 9, cooling water circulating pump; 10, crystallisation cycle pump; 11, crystallization discharging pump; 12, mother liquor pump; 13, indirect steam outlet; 14, liquor inlet to be crystallized; 15, steam inlet; 16, steam condensate (SC) outlet; 17, products export; 18, mother liquor outlet; 19, cooling water inlet; 20, coolant outlet.
The specific embodiment
Be described in further details below in conjunction with the utility model of embodiment:
Embodiment 1
As shown in Figure 1, potassium dihydrogen phosphate continuous crystallisation device comprises one-level successive flash vaporization crystallizer 2, crystallization punishment in advance pump 8, the continuous cooler crystallizer 3 of secondary, crystallization discharging pump 11, stiff device 4, centrifuge 5 and mother liquor tank 6.
The continuous cooler crystallizer 3 of described secondary is made of Oslo crystallizer 3-2 and outer cooler 3-1, and outer cooler 3-1 and crystallizer 3-2 are interconnected.
Described one-level successive flash vaporization crystallizer 2 is the DTB vacuum crystallizer, by the evaporating solvent mode to the feed liquid to be crystallized that preorder workshop section comes tentatively lower the temperature, crystallization.The charging aperture of DTB vacuum crystallizer bottom is connected with liquor inlet 14 to be crystallized by pipeline; The discharging opening of DTB vacuum crystallizer bottom is communicated with through the central downtake of crystallization punishment in advance pump 8 with Oslo crystallizer 3-2 top by pipeline; The gas outlet at DTB vacuum crystallizer top is connected with indirect steam outlet 13 by pipeline; The overfall at DTB vacuum crystallizer middle part is communicated with the charging aperture of thin brilliant arrester 1 through the thin brilliant pump 7 of eliminating by pipeline; The outlet at DTB vacuum crystallizer middle part is communicated with by the charging aperture of pipeline with mother liquor tank 6.
The discharging opening of described crystallization arrester 1 is communicated with by the charging aperture of pipeline with DTB vacuum crystallizer 2 bottoms; Steam 15 feeds the shell-side of thin brilliant arrester 1 along the air inlet of pipeline from thin brilliant arrester 1 top through the steam inlet, be used for the material of crystallization arrester 1 tube side is heated, steam changes steam condensate (SC) into after by thin brilliant arrester 1, and discharges by steam condensate (SC) outlet 16 from the steam (vapor) outlet of thin brilliant arrester 1 bottom and to enter the steam condensate (SC) treatment system.
The discharging opening of described Oslo crystallizer 3-2 bottom is communicated with through the charging aperture of crystallization discharging pump 11 with stiff device 4 tops by pipeline; The overfall on Oslo crystallizer 3-2 top is communicated with mother liquor tank 6 by pipeline; The last straight tube at Oslo crystallizer 3-2 top by crystallisation cycle pump 10 through pipeline with outside the charging aperture of cooler 3-1 be communicated with.
The discharging opening of described outer cooler 3-1 is communicated with by the central downtake of pipeline with Oslo crystallizer 3-2 top; Bottom and the top of outer cooler 3-1 homonymy arrange water inlet and delivery port respectively, cooling water through cooling water inlet 19 along pipeline from outside the water inlet of cooler 3-1 bottom enter outside the shell-side of cooler 3-1, the material that is used in the external cooler 3-1 tube side is lowered the temperature, cooling water after the heat exchange is discharged from the delivery port on outer cooler 3-1 top, and enters cooling water treatment system along pipeline through coolant outlet 20.Cooling water is by the cooling water circulating pump 9 shell-side circulation of cooler 3-1 outside.
The discharging opening of described stiff device 4 bottoms is communicated with by the charging aperture of pipeline with centrifuge 5 tops; The overfall on stiff device 4 tops is communicated with mother liquor tank 6 by pipeline.
The leakage fluid dram of described centrifuge 5 bottoms is connected by the charging aperture of pipeline with mother liquor tank 6 tops; The discharging opening of centrifuge 5 bottom opposite sides is communicated with potassium dihydrogen phosphate solid subsequent treatment workshop section through product outlet 17 by pipeline.
The discharging opening of described mother liquor tank 6 bottoms is communicated with recoil mouth and the mother liquor outlet 18 of stiff device 4 bottoms respectively through mother liquor pump 12 by pipeline.
Production procedure of the present utility model is:
Described feed liquid to be crystallized enters the DTB vacuum crystallizer through liquor inlet 14 to be crystallized along the charging aperture of pipeline from DTB vacuum crystallizer bottom, and enter the bottom of the guide shell of DTB vacuum crystallizer, the promotion lower edge guide shell that arrives the screw of feed liquid to be crystallized in the DTB vacuum crystallizer of guide shell bottom rises, after waiting to rise to the top of DTB vacuum crystallizer, the liquid level place of feed liquid to be crystallized in the DTB vacuum crystallizer carries out shwoot, cooling, and the effusion indirect steam; The indirect steam of overflowing is discharged from the gas outlet at DTB vacuum crystallizer top, and enters steam and condensate system along pipeline through indirect steam outlet 13; Through the bottom that shwoot, cooled feed liquid are back to the DTB vacuum crystallizer along guide shell and the circular passage between the baffle plate of DTB vacuum crystallizer, and be inhaled into again in the guide shell, form a closed circuit.Along with constantly carrying out of circulation, feed liquid in the DTB vacuum crystallizer begins crystallization, the concentration of feed liquid to be crystallized reduces from bottom to top gradually, the concentration of the feed liquid to be crystallized of DTB vacuum crystallizer bottom constantly increases, and at magma of the bottom of DTB vacuum crystallizer formation, form a clear liquid on the top of DTB vacuum crystallizer.
A described clear liquid enters mother liquor tank 6 from the outlet discharge at DTB vacuum crystallizer middle part and along pipeline.There is a clarifying area between a clear liquid in the DTB vacuum crystallizer and a magma, feed liquid in this zone contains thin crystalline substance, the described overfall of feed liquid from DTB vacuum crystallizer middle part that contains thin crystalline substance overflows, and enters in the tube side of thin brilliant arrester 1 from the charging aperture of thin brilliant arrester 1 through the thin brilliant pump 7 of eliminating along pipeline; Steam 15 enters the shell-side of thin brilliant arrester 1 along the air inlet of pipeline from thin brilliant arrester 1 top through the steam inlet, and carry out heat exchange with the feed liquid that contains thin crystalline substance, steam becomes steam condensate (SC) through heat exchange discharges from the gas outlet of thin brilliant arrester 1, and enters the steam condensate (SC) treatment system through steam condensate (SC) outlet 16; The feed liquid that contains thin crystalline substance after heat exchange in it contained thin crystalline substance be eliminated, the feed liquid of eliminating behind the thin crystalline substance is discharged from the discharging opening of thin brilliant arrester 1, and feed again along pipeline in the charging aperture of one-level successive flash vaporization crystallizer 2, mix the circulation that the back participates in DTB vacuum crystallizer 2 inner feed liquids in the guide shell bottom mutually with feed liquid 14 to be crystallized.A described magma is discharged from the discharging opening of DTB vacuum crystallizer bottom.
A magma of discharging from the discharging opening of DTB vacuum crystallizer bottom is pumped in the central downtake at Oslo crystallizer 3-2 top behind crystallization punishment in advance pump 8 along pipeline; A magma arrives the bottom of Oslo crystallizer 3-2 inner chamber along central downtake, and begin slow rising from the bottom of Oslo crystallizer 3-2, pass fluidised crystallization bed in the uphill process, in the crystallization bed, begin crystallization, and form secondary magma and secondary clear liquid herein gradually; The secondary clear liquid continues to move up to the upper straight section of Oslo crystallizer 3-2, and the concentration of secondary clear liquid continues to reduce in uphill process, does not contain crystal substantially in the described secondary clear liquid behind the arrival upper straight section.
The a part of secondary clear liquid that enters the upper straight section of Oslo crystallizer 3-2 is forced to be sent in the tube side of outer cooler 3-1 by crystallisation cycle pump 10, the shell-side of cooling water cooler 3-1 outside the water inlet that cools off water inlet 19 cooler 3-1 outside the pipeline warp enters, and carry out the partition heat exchange to remove the heat in the secondary clear liquid with the secondary clear liquid, and make the secondary clear liquid produce supersaturation, described cooling water is by the cooling water circulating pump 9 interior circular flow of cooler 3-1 outside, and the cooling water after the heat exchange enters cooling water treatment system from the delivery port discharge of outer cooler 3-1 and along pipeline from cooling off water out 20.Secondary clear liquid after the heat exchange is from the discharge of the discharging opening of outer cooler 3-1, and the central downtake that enters Oslo crystallizer 3-2 top again mixes with a magma, forms a closed circuit.The top of Oslo crystallizer 3-2 arranges an overfall, and a part of secondary clear liquid that overflows from overfall enters mother liquor tank 6, and gained secondary magma is discharged from the discharging opening of the bottom of Oslo crystallizer 3-2.Outer cooler 3-1 is equipped with purging system, can guarantee the normal operation of outer cooler 3-1 long-term effectively.
The secondary magma of discharging from the discharging opening of Oslo crystallizer 3-2 bottom is pumped in the stiff device 4 by crystallization discharging pump 11 along pipeline, and the secondary magma is separated into three magmas and three clear liquids further eliminate degree of supersaturation in stiff device 4 after.The overfall of three clear liquids of gained from stiff device 4 tops overflows, and enters mother liquor tank 6 along pipeline.Three magmas of gained are discharged from the discharging opening of stiff device 4 bottoms, and the charging aperture at 5 tops enters 5, three magmas of centrifuge and be separated into potassium dihydrogen phosphate solid and centrifugate in centrifuge 5 along pipeline from centrifuge then.Gained potassium dihydrogen phosphate solid is discharged from the discharging opening of centrifuge 5 bottoms, and enters potassium dihydrogen phosphate solid drying, packaging process along pipeline through product outlet 17; Centrifugate is discharged from the leakage fluid dram of centrifuge 5 bottoms, and enters mother liquor tank 6 along pipeline.
Mother liquors in the mother liquor tank 6 are discharged from the leakage fluid dram of mother liquor tank 6 bottoms, and enter the mother liquor treatment system and the recoil mouth through stiff device 4 bottoms enters stiff device 4 through mother liquor outlet 18 respectively through mother liquor pump 12.
Claims (4)
1. potassium dihydrogen phosphate continuous crystallisation device is characterized in that: comprise the one-level successive flash vaporization crystallizer (2), crystallization punishment in advance pump (8), the continuous cooler crystallizer of secondary (3), crystallization discharging pump (11), stiff device (4), centrifuge (5) and the mother liquor tank (6) that are communicated with successively;
The charging aperture of described one-level successive flash vaporization crystallizer (2) bottom is connected with liquor inlet to be crystallized (14), the discharging opening of one-level successive flash vaporization crystallizer (2) bottom is connected by the charging aperture of crystallization punishment in advance pump (8) with the continuous cooler crystallizer of secondary (3) top, the discharging opening of the continuous cooler crystallizer of described secondary (3) bottom is connected by the charging aperture of crystallization discharging pump (11) with stiff device (4) top, the charging aperture at the discharging opening of described stiff device (4) bottom and centrifuge (5) top is connected, and the discharging opening of described centrifuge (5) bottom is connected with potassium dihydrogen phosphate solid subsequent treatment workshop section through product outlet (17);
The liquid outlet of the continuous cooler crystallizer of outlet, secondary (3) at described one-level successive flash vaporization crystallizer (2) middle part and the overfall on stiff device (4) top, centrifuge (5) bottom is connected with the charging aperture at mother liquor tank (6) top separately.
2. potassium dihydrogen phosphate continuous crystallisation device according to claim 1 is characterized in that: the discharging opening of described mother liquor tank (6) bottom by mother liquor pump (12) respectively the recoil mouth bottom mother liquor outlet (18) and stiff device (4) be connected.
3. potassium dihydrogen phosphate continuous crystallisation device according to claim 1 and 2, it is characterized in that: described one-level successive flash vaporization crystallizer (2) is the DTB vacuum crystallizer, the gas outlet at described one-level successive flash vaporization crystallizer (2) top is connected with steam and condensate system through indirect steam outlet (13), and the overfall at one-level successive flash vaporization crystallizer (2) middle part is connected with thin brilliant arrester (1) by the thin brilliant pump (7) of eliminating; The discharging opening of described thin brilliant arrester (1) is communicated with closed circuit of formation with the charging aperture of one-level successive flash vaporization crystallizer (2); (15) air inlet from thin brilliant arrester (1) top enters steam through the steam inlet, and the steam condensate that forms after the heat exchange is discharged through steam condensate (SC) outlet (16) from the gas outlet of thin brilliant arrester (1) bottom and is communicated with the steam condensate (SC) treatment system.
4. potassium dihydrogen phosphate continuous crystallisation device according to claim 3, it is characterized in that: the continuous cooler crystallizer of described secondary (3) is made of outer cooler (3-1) and Oslo crystallizer (3-2), the discharging opening of described one-level successive flash vaporization crystallizer (1) bottom is connected by the central downtake of crystallization punishment in advance pump (8) with Oslo crystallizer (3-2) top, the overfall on Oslo crystallizer (3-2) top is connected with the charging aperture at mother liquor tank (6) top, and Oslo crystallizer (3-2) is connected with the charging aperture on outer cooler (3-1) top by the crystallisation cycle pump (10) that is arranged at its top; The discharging opening on described outer cooler (3-1) top is communicated with closed circuit of formation with the central downtake on Oslo crystallizer (3-2) top; The homonymy on outer cooler (3-1) bottom and top arranges water inlet and delivery port respectively, and described water inlet and described delivery port are connected by cooling water circulating pump (9).
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| CN201320178302.9U CN203196371U (en) | 2013-04-10 | 2013-04-10 | Continuous potassium dihydrogen phosphate crystallization device |
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| CN201320178302.9U CN203196371U (en) | 2013-04-10 | 2013-04-10 | Continuous potassium dihydrogen phosphate crystallization device |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104192927A (en) * | 2014-09-16 | 2014-12-10 | 青岛国标环保有限公司 | Phenol-acetone wastewater evaporation desalting pretreatment process |
| CN108905265A (en) * | 2018-07-26 | 2018-11-30 | 西安航天华威化工生物工程有限公司 | Sodium vanadate Continuous Cooling Crystallization equipment and its production method |
| CN115253364A (en) * | 2022-08-10 | 2022-11-01 | 安徽海蓝生物科技有限公司 | Centrifugation process and centrifugation equipment for tartaric acid solution |
| CN115321725A (en) * | 2022-08-29 | 2022-11-11 | 徐州天嘉食用化工有限公司 | A kind of disodium hydrogen phosphate recovery device for industrial wastewater treatment and recovery method thereof |
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2013
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104192927A (en) * | 2014-09-16 | 2014-12-10 | 青岛国标环保有限公司 | Phenol-acetone wastewater evaporation desalting pretreatment process |
| CN104192927B (en) * | 2014-09-16 | 2016-08-17 | 青岛国标环保有限公司 | Phenol-acetone waste water evaporative desalination pretreating process |
| CN108905265A (en) * | 2018-07-26 | 2018-11-30 | 西安航天华威化工生物工程有限公司 | Sodium vanadate Continuous Cooling Crystallization equipment and its production method |
| CN115253364A (en) * | 2022-08-10 | 2022-11-01 | 安徽海蓝生物科技有限公司 | Centrifugation process and centrifugation equipment for tartaric acid solution |
| CN115253364B (en) * | 2022-08-10 | 2023-10-31 | 安徽海蓝生物科技有限公司 | Centrifugal process and centrifugal equipment for tartaric acid solution |
| CN115321725A (en) * | 2022-08-29 | 2022-11-11 | 徐州天嘉食用化工有限公司 | A kind of disodium hydrogen phosphate recovery device for industrial wastewater treatment and recovery method thereof |
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