CN205549616U - Continuous evaporation crystal system of one step of big particle diameter food level potassium chloride crystal of production - Google Patents
Continuous evaporation crystal system of one step of big particle diameter food level potassium chloride crystal of production Download PDFInfo
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- CN205549616U CN205549616U CN201620334380.7U CN201620334380U CN205549616U CN 205549616 U CN205549616 U CN 205549616U CN 201620334380 U CN201620334380 U CN 201620334380U CN 205549616 U CN205549616 U CN 205549616U
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- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 title claims abstract description 186
- 235000011164 potassium chloride Nutrition 0.000 title claims abstract description 90
- 239000001103 potassium chloride Substances 0.000 title claims abstract description 90
- 239000013078 crystal Substances 0.000 title claims abstract description 61
- 239000002245 particle Substances 0.000 title claims abstract description 28
- 238000004519 manufacturing process Methods 0.000 title abstract description 21
- 238000001704 evaporation Methods 0.000 title abstract description 17
- 230000008020 evaporation Effects 0.000 title abstract description 13
- 235000013305 food Nutrition 0.000 title abstract description 9
- 230000000694 effects Effects 0.000 claims abstract description 235
- 238000000926 separation method Methods 0.000 claims abstract description 93
- 238000002425 crystallisation Methods 0.000 claims abstract description 68
- 230000008025 crystallization Effects 0.000 claims abstract description 52
- 239000000463 material Substances 0.000 claims abstract description 32
- 239000007788 liquid Substances 0.000 claims abstract description 23
- 238000007599 discharging Methods 0.000 claims description 39
- 239000002994 raw material Substances 0.000 claims description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 230000008676 import Effects 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 24
- 239000012141 concentrate Substances 0.000 abstract description 10
- 238000009826 distribution Methods 0.000 abstract description 10
- 239000000243 solution Substances 0.000 abstract description 9
- 239000000203 mixture Substances 0.000 abstract description 5
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000012047 saturated solution Substances 0.000 abstract description 4
- 238000009834 vaporization Methods 0.000 abstract description 3
- 230000008016 vaporization Effects 0.000 abstract description 3
- 238000007701 flash-distillation Methods 0.000 abstract description 2
- 230000006872 improvement Effects 0.000 abstract description 2
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 239000008187 granular material Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 description 19
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 12
- 230000008569 process Effects 0.000 description 10
- 239000010413 mother solution Substances 0.000 description 5
- 239000007787 solid Substances 0.000 description 5
- 239000002775 capsule Substances 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 4
- 238000010792 warming Methods 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- 238000004581 coalescence Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 208000019025 Hypokalemia Diseases 0.000 description 2
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 235000002639 sodium chloride Nutrition 0.000 description 2
- OWEGMIWEEQEYGQ-UHFFFAOYSA-N 100676-05-9 Natural products OC1C(O)C(O)C(CO)OC1OCC1C(O)C(O)C(O)C(OC2C(OC(O)C(O)C2O)CO)O1 OWEGMIWEEQEYGQ-UHFFFAOYSA-N 0.000 description 1
- GUBGYTABKSRVRQ-PICCSMPSSA-N Maltose Natural products O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@@H]1O[C@@H]1[C@@H](CO)OC(O)[C@H](O)[C@H]1O GUBGYTABKSRVRQ-PICCSMPSSA-N 0.000 description 1
- 235000005135 Micromeria juliana Nutrition 0.000 description 1
- 241000246354 Satureja Species 0.000 description 1
- 235000007315 Satureja hortensis Nutrition 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- JGDITNMASUZKPW-UHFFFAOYSA-K aluminium trichloride hexahydrate Chemical compound O.O.O.O.O.O.Cl[Al](Cl)Cl JGDITNMASUZKPW-UHFFFAOYSA-K 0.000 description 1
- 229940009861 aluminum chloride hexahydrate Drugs 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- GUBGYTABKSRVRQ-QUYVBRFLSA-N beta-maltose Chemical compound OC[C@H]1O[C@H](O[C@H]2[C@H](O)[C@@H](O)[C@H](O)O[C@@H]2CO)[C@H](O)[C@@H](O)[C@@H]1O GUBGYTABKSRVRQ-QUYVBRFLSA-N 0.000 description 1
- 210000002318 cardia Anatomy 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 235000015872 dietary supplement Nutrition 0.000 description 1
- 239000002934 diuretic Substances 0.000 description 1
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- 230000037406 food intake Effects 0.000 description 1
- 235000011194 food seasoning agent Nutrition 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
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- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
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- 230000009965 odorless effect Effects 0.000 description 1
- 238000001907 polarising light microscopy Methods 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 208000007645 potassium deficiency Diseases 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 235000013324 preserved food Nutrition 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 235000011152 sodium sulphate Nutrition 0.000 description 1
- 230000000087 stabilizing effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to a continuous evaporation crystal system of one step of big particle diameter food level potassium chloride crystal of production, the system comprises vaporization system and crystal system two parts, the production of can one step continuous realization large granule food level potassium chloride, it is concentrated to pass through the vaporization system heating with potassium chloride solution, then pump sending to crystal system evaporates the crystallization in succession, obtains potassium chloride magma liquid, after the growing the grain discharges the potassium chloride magma and carries the buffer memory to buffer tank, the condition includes: feeding potassium chloride feed liquid directly gets into separation chamber's circulating line, mixes with a large amount of potassium chloride concentrates, through the high saturated solution of two effect heat transfer formation high temperature, then lets its and a large amount of potassium chloride magma liquid mix, through extrinsic cycle heat transfer improvement potassium chloride material temperature and pressure, sends into crystallizer flash distillation concentration, crystallization potassium chloride crystal. According to the utility model provides a method, the food level potassium chloride crystal average grain size that obtains is big, and particle size distribution is even, and output is high.
Description
Technical field
This utility model belongs to evaporative crystallization technique field, is specifically related to an a kind of step and produces the continuous evaporative crystallization system of big particle diameter food-grade potassium chloride crystal.
Background technology
Food-grade potassium chloride is white powder or colourless crystallization, odorless, and salty in the mouth is nontoxic, soluble in water, be dissolved in glycerol, be slightly soluble in ethanol.Food-grade potassium chloride is mainly used to produce Cardia Salt, to meet the direct kalium replenishment of human body, substitutes Sal as savory agent and nutritional supplement with part, prevents people's excess ingestion Sal；Pharmaceutically being available for taking orally, it is also possible to preparation water injection, play and supplement or the effect of balanced human's potassium deficiency, health can also manufacture diuretic, prevent kaliopenia medicine.In addition, potassium chloride can be used in the food such as agricultural production, Aquatic product, livestock products, fermentation, seasoning, canned food, instant food as Sal, can be added in proportion in various food, food tissue state, color, smell and taste and raw-food material cost control are played indispensable effect.
Food-grade potassium chloride crystal product produces and mainly includes dissolving, crystallizes, separates, be dried and pack five operations, first the saturated solution of preparation potassium chloride is dissolved by technical grade potassium chloride, then saturated solution is delivered to crystalline element and is evaporated crystallization, obtain potassium chloride magma, potassium chloride magma is delivered to centrifuge again be centrifuged separating, it is dried, packs for sale.Wherein, the evaporative crystallization of potassium chloride is most important, most crucial operation, evaporative crystallization obtains the quality of potassium chloride product, directly influence the granularity of food-grade potassium chloride product, purity and outward appearance, therefore need strictly to control potassium chloride multiple-effect evaporation crystallization processes flow process, to obtain meeting the food-grade potassium chloride crystal product of user's request.
The main mode of production of food-grade potassium chloride is " multiple-effect evaporation "+" crystallisation by cooling still " at present, this covering device is evaporation and Crystallization Procedure to be separated, first Klorvess Liquid multiple-effect evaporation is concentrated, then concentrated solution is obtained potassium chloride product by the production that cools.Along with industrially scalable constantly expands, food-grade potassium chloride crystallization processes equipment needed thereby and manual operation are the biggest, impact due to manual operation unstable factor, easily cause that edible potassium chloride crystal product crystal is tiny, particle size distribution is uneven, crystal product coalescence serious, cause subsequent handling to separate, wash, dry difficulty and increase, it is impossible to meet food potassium chloride producer to Potassium Chloride Product granularity and purity requirement.
Summary of the invention
The purpose of this utility model is to provide an a kind of step and produces the continuous evaporative crystallization system of big particle diameter food-grade potassium chloride crystal, reduce hand labor intensity, improve production efficiency and energy utilization rate so as to get food-grade potassium chloride crystal bigger, even particle size distribution, production cost reduces.
The technical scheme that this utility model is used is:
One step produces the continuous evaporative crystallization system of big particle diameter food-grade potassium chloride crystal, it is characterised in that:
Including vapo(u)rization system and crystal system two parts；
Described vapo(u)rization system includes that III effect circulating pump, III effect heat exchanger, III effect separation chamber and III effect discharging pump, I effect circulating pump, I effect heat exchanger, I imitate separation chamber；
Described crystal system includes II effect circulating pump, II effect heat exchanger, II effect crystallizer, II effect transfering material pump and crystallization discharging pump；
nullRaw material is connected to the circulating line of III effect separation chamber，It is delivered to III effect heat exchanger and III effect separation chamber charging aperture by circulating line，III effect separation chamber discharging opening connects III and imitates pump entry，III effect circulating-pump outlet is connected with III effect heat exchanger charging aperture，III effect heat exchanger discharging opening is connected with III effect separation chamber's recycle feed mouth，III effect separation chamber bottom discharge mouth connects III and imitates discharging pump entrance，III effect discharging pump outlet is connected to II and imitates crystallizer circulating line，II effect transfering material pump outlet is connected to I effect separation chamber circulating line，It is delivered to I effect heat exchanger and I effect separation chamber charging aperture by circulating line，I effect separation chamber discharging opening connects I and imitates pump entry，I effect circulating-pump outlet is connected with I effect heat exchanger charging aperture，I effect heat exchanger discharging opening is connected with I effect separation chamber's recycle feed mouth，I effect circulating line draw branch road be connected to II effect crystallizer circulating line crystallize，The overhead vapor outlet of I effect separation chamber is connected to II and imitates heat exchanger shell pass import，The overhead vapor outlet of III effect separation chamber is connected to surface condenser and cools down；
Klorvess Liquid after concentration is delivered to the circulating line of II effect crystallizer, it is delivered to II effect heat exchanger and II effect crystallizer through circulating line, II effect crystallizer circulating line discharging opening is connected to the entrance of II effect circulating pump, II effect circulation delivery side of pump connects the charging aperture of II effect heat exchanger, the discharging opening of II effect heat exchanger connects the circulating line charging aperture of II effect crystallizer, the overhead vapor outlet of II effect crystallizer separation chamber connects III and imitates heat exchanger steam inlet, and II effect crystallizer crystallisation chamber bottom discharge mouth connects crystallization discharging pump；Crystallisation cycle pipeline draws branch road imitates transfering material pump to II, is delivered to I effect separation chamber circulating line by II effect transfering material pump.
I effect heat exchanger, II effect heat exchanger, III effect heat exchanger shell pass outlet condensed water are connected to condensed water bucket caching.
Raw material is connected to the circulating line of III effect separation chamber, sequentially enters II effect crystallizer and I imitates separation chamber, then imitate crystallizer from I effect separation chamber's entrance II, be cross-flow passes with steam；
Or raw material is connected to the circulating line of III effect separation chamber, sequentially enters II effect separation chamber and I imitates crystallizer, crystallize in I effect crystallizer, be counter-current flow with steam；
Or raw material is connected to the circulating line of I effect separation chamber, sequentially enters II effect separation chamber and III imitates crystallizer, crystallize in III effect crystallizer, be co-current flow with steam.
This utility model has the advantage that
The region that the crystallizer that this utility model is used can make degree of supersaturation produce is respectively placed at the two of crystallizer with crystal growth district, crystal is fluidized suspension in circulating mother liquor, good condition is provided, it is possible to produce that granularity is bigger and uniform crystal for crystal growth.
This utility model provides an a kind of step and produces the Continuous Cooling Crystallization system of big particle diameter food-grade potassium chloride crystal, the crystallization operation of " multiple-effect evaporation "+" the crystallisation by cooling still " of the application of instead of over, stabilize input and output material and evaporative crystallization flow process, can effectively ensure that the stability of product quality, substantially increase the production efficiency of food-grade potassium chloride.
The continuous evaporative crystallization system that this utility model provides is reasonable in design, and it is less expensive to build the equipment cost that this system used, crystalline mother solution infinite reflux, it is achieved crystallization process material is without waste, process stabilizing, and interference is few, beneficially consecutive production.This system repeatedly utilizes vaporization and the condensation of indirect steam, can substantially reduce raw steam consumption, thus improve the economy of vaporising device；And the operation that evaporation can be completed in same crystallizer, concentrate and crystallize.
Accompanying drawing explanation
Fig. 1 is system composition and process flow diagram (cross-flow)；
Fig. 2 is the structural representation of crystallizer；
Fig. 3 is that the method according to this utility model embodiment 1 produces the food-grade potassium chloride Lens capsule figure obtained；
Fig. 4 is that the method according to this utility model embodiment 1 produces the potassium chloride photo obtained；
Fig. 5 is that the method according to this utility model embodiment 2 produces the food-grade potassium chloride Lens capsule figure obtained；
Fig. 6 is that the method according to this utility model embodiment 2 produces the potassium chloride photo obtained；
Fig. 7 is that the method according to this utility model embodiment 3 produces the food-grade potassium chloride Lens capsule figure obtained；
Fig. 8 is that the method according to this utility model embodiment 3 produces the potassium chloride photo obtained；
Fig. 9 is that the method according to this utility model embodiment 4 produces the food-grade potassium chloride Lens capsule figure obtained；
Figure 10 is that the method according to this utility model embodiment 4 produces the potassium chloride photomacrograph obtained；
Figure 11 is system composition and process flow diagram (countercurrently)；
Figure 12 is system composition and process flow diagram (following current).
In figure, 1-I imitates circulating pump, and 2-I imitates heat exchanger, and 3-I imitates separation chamber, and 4-II imitates circulating pump, 5-II imitates heat exchanger, and 6-II imitates crystallizer, and 7-crystallizes discharging pump, and 8-II imitates transfering material pump, 9-III imitates circulating pump, and 10-III imitates heat exchanger, and 11-III imitates separation chamber, and 12-III imitates discharging pump.
Detailed description of the invention
Below in conjunction with detailed description of the invention, this utility model is described in detail.
The method of existing production food-grade potassium chloride crystal is " multiple-effect evaporation "+" crystallisation by cooling still ", also will concentrate by Klorvess Liquid multiple-effect evaporation, then by the production that cools, concentrated solution is obtained potassium chloride product.The food-grade potassium chloride crystal product particle size distribution that this mode of production obtains is uneven, and crystal product coalescence is serious；And because increasing a crystallization kettle being specifically designed to crystallization, destructive increase, the power consumption of crystal is increased, so that production efficiency is the lowest, production cost is higher.
In order to solve the Processes and apparatus problem occurred in food-grade potassium chloride crystal production, this utility model provides a kind of continuous evaporative crystallization system producing big particle diameter food-grade potassium chloride crystal, including vapo(u)rization system and crystal system two parts:
Described vapo(u)rization system includes that III effect circulating pump 9, III effect heat exchanger 10, III effect separation chamber 11 and III effect discharging pump 12, I effect circulating pump 1, I effect heat exchanger 2, I imitate separation chamber 3；Described crystal system includes II effect circulating pump 4, II effect heat exchanger 5, II effect crystallizer 6, II effect transfering material pump 8 and crystallization discharging pump 7.
nullRaw material is connected to the circulating line of III effect separation chamber 11，It is delivered to III effect heat exchanger 10 and III effect separation chamber 11 charging aperture by circulating line，III effect separation chamber 11 discharging opening connects III and imitates circulating pump 9 entrance，III effect circulating pump 9 exports and is connected with III effect heat exchanger 10 charging aperture，III effect heat exchanger 10 discharging opening is connected with III effect separation chamber 11 recycle feed mouth，III effect separation chamber 11 bottom discharge mouth connects III and imitates discharging pump 12 entrance，III effect discharging pump 12 outlet is connected to II and imitates crystallizer 6 circulating line，II effect transfering material pump 8 outlet is connected to I effect separation chamber 3 circulating line，It is delivered to I effect heat exchanger 2 and I effect separation chamber 3 charging aperture by circulating line，I effect separation chamber 3 discharging opening connects I and imitates circulating pump 1 entrance，I effect circulating pump 1 exports and is connected with I effect heat exchanger 2 charging aperture，I effect heat exchanger 2 discharging opening is connected with I effect separation chamber 3 recycle feed mouth，I effect circulating line draw branch road be connected to II effect crystallizer 6 circulating line crystallize，The overhead vapor outlet of I effect separation chamber 3 is connected to II and imitates heat exchanger 5 shell side import，The overhead vapor outlet of III effect separation chamber 11 is connected to surface condenser and cools down.
Klorvess Liquid after concentration is delivered to the circulating line of II effect crystallizer 6, it is delivered to II effect heat exchanger 5 and II through circulating line and imitates crystallizer 6, II effect crystallizer 6 circulating line discharging opening is connected to the entrance of II effect circulating pump 4, II effect circulation delivery side of pump connects the charging aperture of II effect heat exchanger 5, the discharging opening of II effect heat exchanger 5 connects the circulating line charging aperture of II effect crystallizer 6, the overhead vapor outlet of II effect crystallizer 6 separation chamber connects III and imitates heat exchanger 10 steam inlet, and II effect crystallizer 6 crystallisation chamber bottom discharge mouth connects crystallization discharging pump 7.Crystallisation cycle pipeline draws branch road imitates transfering material pump 8 to II, is delivered to I effect separation chamber 3 circulating line by II effect transfering material pump 8.
I effect heat exchanger 2, II effect heat exchanger 5, III effect heat exchanger 10 shell-side outlet condensed water are connected to condensed water bucket caching.
Raw material is connected to the circulating line of III effect separation chamber 11, sequentially enters II effect crystallizer 6 and I and imitates separation chamber 3, then enter II effect crystallizer 6 from I effect separation chamber 3, is cross-flow passes with steam；Or raw material is connected to the circulating line of III effect separation chamber 11, sequentially enters II effect separation chamber 6 and I and imitate crystallizer 3, crystallize in I effect crystallizer, be counter-current flow with steam；Or raw material is connected to the circulating line of I effect separation chamber 3, sequentially enters II effect separation chamber 6 and III and imitate crystallizer 11, crystallize in III effect crystallizer, be co-current flow with steam.
Crystallizer crystallisation chamber part is cone structure, material after flash distillation forms supersaturated solution, crystallisation chamber is entered again by downspout, crystal contact bottom supersaturated solution and downspout, promote that crystal is constantly grown up, up flow bottom the crystallized device of feed liquid, crystal bottom agitation, up flow simultaneously, along with the interaction producing the different active forces such as the power up walked and crystal gravity, fluid resistance, realize crystal classification, separation, so that crystal grain is suspended in liquid stream and forms the fluid bed of grading.Relatively small particle crystal is predominantly located in crystallisation chamber middle and upper part, and the feed liquid rate of climb is slow, and crystal grain exists with small crystals form；Middle particle diameter crystal grain is mainly distributed on crystallisation chamber middle and lower part, and feed liquid upflow velocity is relatively big, and crystal grain quantity is many, and crystal growth is fast, and the crystal grain of this part accounts for major part；Big particle diameter crystal grain is mainly distributed on bottom crystallisation chamber, and degree of supersaturation is high, and feed liquid upflow velocity is fast, and crystal particle diameter is big, and growth rate is fast.
The step using the said equipment to carry out produces the continuous evaporative crystallization method of big particle diameter food-grade potassium chloride crystal, comprises the following steps:
By vapo(u)rization system heating, Klorvess Liquid is concentrated into potassium chloride mass percent concentration is 30% ~ 36%, then potassium chloride concentrate pump is delivered to crystal system and carry out continuous evaporative crystallization, obtaining potassium chloride magma through evaporative crystallization, the discharge of potassium chloride magma is delivered to buffer tank caching after terminating by growing the grain；
The condition of potassium chloride continuous evaporative crystallization includes: charging potassium chloride feed liquid is directly entered separation chamber's circulating line, mix with a large amount of potassium chloride concentrated solutions, high temperature height saturated solution is formed by two effect heat exchange, then it is allowed to mix with a large amount of potassium chloride magma, potassium chloride temperature of charge and pressure is improved by external circulation heat exchanging, send into crystallizer flash concentration, be allowed to crystallization potassium chloride.
Evaporation and concentration afterchlorinate potassium temperature is 55 ~ 110 DEG C.System circulating load is (50 ~ 150) with the mass ratio of inlet amount: 1.The potassium chloride time of staying in a crystallizer is 1 ~ 4h.Potassium chloride discharging magma solid content is percent by volume 15 ~ 40%.
Hereinafter, by specific embodiment, food-grade potassium chloride continuous evaporative crystallization method of the present utility model is described in further detail.Wherein, the particle size distribution of potassium chloride uses Malvern Particle Size Analyzer dry method to measure, and crystallogram is by determination of polarized light microscopy.Particle mean size refers to that sieving lower accumulating weight ratio is screen size value when 50%.
Embodiment 1:
The present embodiment is used for food-grade potassium chloride crystal and the production method thereof that this utility model provides is described.
nullKlorvess Liquid is delivered to by feed pump the circulating line of III effect separation chamber，After III effect heat exchanger and III effect separation chamber flash concentration，Material is delivered to by III effect discharging pump the further flash concentration of circulating line of II effect crystallizer，Again through being delivered to the circulating line of I effect separation chamber by II effect transfering material pump after II effect concentrates，By I effect heat exchanger heat exchange and I effect separation chamber high temperature flash concentration，Then the circulating line of II effect crystallizer it is delivered to by pipeline pressure reduction，After I effect and III effect two effect heat exchanger heating concentrate，Feed liquid is warming up to about 88 DEG C，Potassium chloride concentration is 34%(w/w)，The circulating line that then potassium chloride concentrated solution is delivered to II effect crystallizer is evaporated crystallization，Keep circulating load to be inlet amount 100 times，In maintenance crystallizer, citric acid feed temperature is 88 DEG C，In holding crystallizer, potassium chloride magma solid content is 30%，Discharge hole for discharge is passed through in a crystallizer after circulating and evaporating 2h，It is centrifuged separating，After separation, mother solution is back to the circulating line continuation evaporative crystallization of II effect crystallizer，So that potassium chloride separates out completely.The product particle mean size obtained be 1.6mm, Granularity Distribution and crystallogram as shown in Figure 3 and Figure 4.
Embodiment 2:
The present embodiment is used for food-grade potassium chloride crystal and the production method thereof that this utility model provides is described.
nullKlorvess Liquid is delivered to by feed pump the circulating line of III effect separation chamber，After III effect heat exchanger and III effect separation chamber flash concentration，Material is delivered to by III effect discharging pump the further flash concentration of circulating line of II effect crystallizer，Again through being delivered to the circulating line of I effect separation chamber by II effect transfering material pump after II effect concentrates，By I effect heat exchanger heat exchange and I effect separation chamber high temperature flash concentration，Then the circulating line of II effect crystallizer it is delivered to by pipeline pressure reduction，After I effect and III effect two effect heat exchanger heating concentrate，Feed liquid is warming up to about 88 DEG C，Potassium chloride concentration is 34%(w/w)，The circulating line that then potassium chloride concentrated solution is delivered to II effect crystallizer is evaporated crystallization，Keep circulating load to be inlet amount 150 times，In maintenance crystallizer, citric acid feed temperature is 89 DEG C，In holding crystallizer, potassium chloride magma solid content is 25%，Discharge hole for discharge is passed through in a crystallizer after circulating and evaporating 1h，It is centrifuged separating，After separation, mother solution is back to the circulating line continuation evaporative crystallization of II effect crystallizer，So that potassium chloride separates out completely.The product particle mean size obtained be 1.6mm, Granularity Distribution and crystallogram as shown in Figure 5 and Figure 6.
Embodiment 3:
The present embodiment is used for edible potassium chloride crystal and the production method thereof that this utility model provides is described.
nullKlorvess Liquid is delivered to by feed pump the circulating line of III effect separation chamber，After III effect heat exchanger and III effect separation chamber flash concentration，Material is delivered to by III effect discharging pump the further flash concentration of circulating line of II effect separation chamber，The circulating line that warp is delivered to I effect crystallizer by II effect transfering material pump after II effect concentrates again is evaporated crystallization，Behind II effect separation chamber and III effect separation chamber evaporation and concentration, feed liquid is warming up to about 110 DEG C，Potassium chloride concentration is 36%(w/w)，Material enters the circulating line of I effect crystallizer and is evaporated crystallization，Keep circulating load to be inlet amount 50 times，In maintenance crystallizer, citric acid feed temperature is about 100 DEG C，In holding crystallizer, potassium chloride magma solid content is 15%，Discharge hole for discharge is passed through in a crystallizer after circulating and evaporating 3h，It is centrifuged separating，After separation, mother solution is back to the circulating line continuation evaporative crystallization of I effect crystallizer，So that potassium chloride separates out completely.The product particle mean size obtained be 1.4mm, Granularity Distribution and crystallogram as shown in Figure 7 and Figure 8.
Embodiment 4:
The present embodiment is used for food-grade potassium chloride crystal and the production method thereof that this utility model provides is described.
nullKlorvess Liquid is delivered to by feed pump the circulating line of I effect separation chamber，After I effect heat exchanger and I effect separation chamber high temperature flash concentration，Material is delivered to by I effect circulating pump the further flash concentration of circulating line of II effect separation chamber，The circulating line that warp is delivered to III effect crystallizer by II effect transfering material pump after II effect concentrates again is evaporated crystallization，Behind I effect separation chamber and II effect separation chamber evaporation and concentration, feed liquid is warming up to about 55 DEG C，Potassium chloride concentration is 30%(w/w)，Material enters the circulating line of I effect crystallizer and is evaporated crystallization，Keep circulating load to be inlet amount 150 times，In maintenance crystallizer, citric acid feed temperature is about 55 DEG C，In holding crystallizer, potassium chloride magma solid content is 40%，Discharge hole for discharge is passed through in a crystallizer after circulating and evaporating 4h，It is centrifuged separating，After separation, mother solution is back to the circulating line continuation evaporative crystallization of III effect crystallizer，So that potassium chloride separates out completely.The product particle mean size obtained be 1.6mm, Granularity Distribution and crystallogram as shown in Figure 9 and Figure 10.
Can be drawn by embodiment 1-4 of the present utility model, the food-grade potassium chloride crystal that the food-grade potassium chloride continuous evaporative crystallization production method using this utility model to provide obtains, crystallization yield is high (in the case of material infinite reflux, crystallization yield is up to 100%), plane of crystal is glossy, coalescence is few, and even particle size distribution, product quality is higher.
This utility model described in detail above preferred embodiment, but this utility model is not limited to the detail in above-described embodiment, technical method of the present utility model is carried out simple deformation and falls within protection domain of the present utility model.
Each detail described in above-mentioned detailed description of the invention, can combine by the way of any appropriate when not contradiction, for avoiding repeating, various possible compound modes are no longer illustrated by this utility model, and these possible compound modes should be regarded as content disclosed in the utility model equally.
Above are only preferred embodiment of the present utility model; not in order to limit protection domain of the present utility model; described skilled person should be understood that; all within spirit of the present utility model and principle; the any modification, equivalent substitution and improvement etc. done, within should be included in protection domain of the present utility model.
Above-mentioned continuous evaporative crystallization system cannot be only used for the continuous evaporative crystallization of food-grade potassium chloride, can be additionally used in the inorganic or organic crystallizations such as Aluminum Chloride Hexahydrate, sodium chloride, sodium sulfate, ammonium sulfate, maltose alcohol, aforementioned system uses this continuous evaporative crystallization system also to should be regarded as content disclosed in the utility model.
Content of the present utility model is not limited to cited by embodiment, the conversion of any equivalence that technical solutions of the utility model are taked by those of ordinary skill in the art by reading this utility model description, is claim of the present utility model and is contained.
Claims (3)
1. a step produces the continuous evaporative crystallization system of big particle diameter food-grade potassium chloride crystal, it is characterised in that:
Including vapo(u)rization system and crystal system two parts；
Described vapo(u)rization system includes III effect circulating pump (9), III effect heat exchanger (10), III effect separation chamber (11) and III effect discharging pump (12), I effect circulating pump (1), I effect heat exchanger (2), I effect separation chamber (3)；
Described crystal system includes II effect circulating pump (4), II effect heat exchanger (5), II effect crystallizer (6), II effect transfering material pump (8) and crystallization discharging pump (7)；
nullRaw material is connected to the circulating line of III effect separation chamber (11)，It is delivered to III effect heat exchanger (10) and III by circulating line and imitates separation chamber (11) charging aperture，III effect separation chamber (11) discharging opening connects III and imitates circulating pump (9) entrance，III effect circulating pump (9) outlet is connected with III effect heat exchanger (10) charging aperture，III effect heat exchanger (10) discharging opening is connected with III effect separation chamber (11) recycle feed mouth，III effect separation chamber (11) bottom discharge mouth connects III and imitates discharging pump (12) entrance，III effect discharging pump (12) outlet is connected to II and imitates crystallizer (6) circulating line，II effect transfering material pump (8) outlet is connected to I and imitates separation chamber (3) circulating line，It is delivered to I effect heat exchanger (2) and I by circulating line and imitates separation chamber (3) charging aperture，I effect separation chamber (3) discharging opening connects I and imitates circulating pump (1) entrance，I effect circulating pump (1) outlet is connected with I effect heat exchanger (2) charging aperture，I effect heat exchanger (2) discharging opening is connected with I effect separation chamber (3) recycle feed mouth，I effect circulating line draw branch road be connected to II effect crystallizer (6) circulating line crystallize，I effect separation chamber (3) overhead vapor outlet is connected to II and imitates heat exchanger (5) shell side import，III effect separation chamber (11) overhead vapor outlet is connected to surface condenser and cools down；
Klorvess Liquid after concentration is delivered to the circulating line of II effect crystallizer (6), it is delivered to II effect heat exchanger (5) and II effect crystallizer (6) through circulating line, II effect crystallizer (6) circulating line discharging opening is connected to the entrance of II effect circulating pump (4), II effect circulation delivery side of pump connects the charging aperture of II effect heat exchanger (5), the discharging opening of II effect heat exchanger (5) connects the circulating line charging aperture of II effect crystallizer (6), the overhead vapor outlet of II effect crystallizer (6) separation chamber connects III and imitates heat exchanger (10) steam inlet, II effect crystallizer (6) crystallisation chamber bottom discharge mouth connects crystallization discharging pump (7)；Crystallisation cycle pipeline draws branch road imitates transfering material pump (8) to II, is delivered to I by II effect transfering material pump (8) and imitates separation chamber (3) circulating line.
A step the most according to claim 1 produces the continuous evaporative crystallization system of big particle diameter food-grade potassium chloride crystal, it is characterised in that:
I effect heat exchanger (2), II effect heat exchanger (5), III effect heat exchanger (10) shell-side outlet condensed water are connected to condensed water bucket caching.
A step the most according to claim 1 produces the continuous evaporative crystallization system of big particle diameter food-grade potassium chloride crystal, it is characterised in that:
Raw material is connected to the circulating line of III effect separation chamber (11), sequentially enters II effect crystallizer (6) and I effect separation chamber (3), then enters II effect crystallizer (6) from I effect separation chamber (3), is cross-flow passes with steam；
Or raw material is connected to the circulating line of III effect separation chamber (11), sequentially enter II effect separation chamber (6) and I effect crystallizer (3), crystallize in I effect crystallizer, be counter-current flow with steam；
Or raw material is connected to the circulating line of I effect separation chamber (3), sequentially enter II effect separation chamber (6) and III effect crystallizer (11), crystallize in III effect crystallizer, be co-current flow with steam.
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| CN201620334380.7U CN205549616U (en) | 2016-04-20 | 2016-04-20 | Continuous evaporation crystal system of one step of big particle diameter food level potassium chloride crystal of production |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105727576A (en) * | 2016-04-20 | 2016-07-06 | 西安航天华威化工生物工程有限公司 | Continuous evaporative crystallization system and method for one-step production of large-grain-size food-grade potassium chloride crystals |
| CN107626112A (en) * | 2017-10-27 | 2018-01-26 | 中国轻工业长沙工程有限公司 | A kind of continuous production vacuum cooling crystallizer |
-
2016
- 2016-04-20 CN CN201620334380.7U patent/CN205549616U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105727576A (en) * | 2016-04-20 | 2016-07-06 | 西安航天华威化工生物工程有限公司 | Continuous evaporative crystallization system and method for one-step production of large-grain-size food-grade potassium chloride crystals |
| CN107626112A (en) * | 2017-10-27 | 2018-01-26 | 中国轻工业长沙工程有限公司 | A kind of continuous production vacuum cooling crystallizer |
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