CN104548634A - Solid-liquid separation process for combining multiple-effect evaporation and agitated evaporation - Google Patents
Solid-liquid separation process for combining multiple-effect evaporation and agitated evaporation Download PDFInfo
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- CN104548634A CN104548634A CN201310519642.8A CN201310519642A CN104548634A CN 104548634 A CN104548634 A CN 104548634A CN 201310519642 A CN201310519642 A CN 201310519642A CN 104548634 A CN104548634 A CN 104548634A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
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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
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Abstract
The invention relates to a solid-liquid separation process which comprises the following steps: A, concentrating an aqueous solution containing low-concentration dissolved solids or a mixed solution of water-organic solvent by virtue of multiple-effect evaporation, and producing medium-concentration mixed solution; B, discharging the medium-concentration mixed solution into an agitated evaporation tank, further evaporating and concentrating, and producing high-concentration mixed solution; and C, controlling the solid content of the high-concentration mixed solution, so that the mixed solution is discharged out of the agitated evaporation tank in a liquid form. The steam generated in the step B returns into a multiple-effect evaporation system, the liquid can be heated when the vapor phase is condensed, the heat is recovered, the solution recovery rate is guaranteed, and the high-concentration mixed solution discharged in a fluid form in the step C is cooled and cured.
Description
Technical field
The present invention is that a kind of multiple-effect evaporation that adopts combines the process stirring and evaporate and carry out Separation of Solid and Liquid, belong to Chemical Engineering and Technology solid-liquid separation technique field, be specifically related to a kind of solid-liquid separation process of the water-organic solvent mixed solution containing low concentration soluble solid.
Background technology
From solution, separate dissolved material is a common Chemical Problems.According to DDGS solubility situation in a solvent, generally adjust the object that the parameters such as temperature, pH, solution concentration can reach DDGS precipitation.Direct evaporating liquid realizes the one simply and directly method of Separation of Solid and Liquid by the concentration changing solute in solution, but directly evaporation Problems existing is that energy consumption is high, and in evaporation process, along with solute precipitation in solution, solid content is improved and easily cause equipment scaling to block.Multiple-effect evaporation is as a kind of conventional Separation of Solid and Liquid separate mode, although multiple-effect evaporation energy consumption is lower relative to direct evaporation energy consumption, also exists when last effect excessive vaporization, the problem of the easy fouling of equipment.In order to prevent equipment scaling and blocking, Chinese patent CN102641602A in the downstream of first single-effect evaporator parts, the upstream of whole single-effect evaporator parts, be provided with at least one mechanical separation equipment, its concentration for reducing the material flow in whole single-effect evaporator parts is to prevent from, in whole single-effect evaporator parts, fouling and blocking occur.Although the object controlling material concentration can be reached by external mechanical separation equipment, used device cost up.Without the need to increasing separation equipment in multiple-effect evaporation workshop section inside, the present invention can accomplish that solids level concentration controls.
In addition, along with solids level concentration improves, the equilibrium partial pressure of liquid reduces, and multiple-effect evaporation treatment effeciency also can be caused to decline.
In addition, for Separation of Solid and Liquid operation, Chinese patent CN101152969 is by adding the mode of additive, and concentrate acid adding precipitated, obtain solidliquid mixture, then carry out Separation of Solid and Liquid to mixture, processing procedure is comparatively complicated; Chinese patent CN101306260 uses centrifugal separator after multiple-effect evaporation, but for the too small material of crystalline particle, centrifugation not necessarily can be suitable for.The present invention, without the need to using extra additive, carries out Separation of Solid and Liquid operation by the mode stirring evaporation.
Summary of the invention
The invention reside in the defect for overcoming prior art and provide a kind of solid-liquid separation process, this technique combines stirring evaporation by multiple-effect evaporation and realizes Separation of Solid and Liquid.
For achieving the above object, the present invention is by the following technical solutions:
A kind of solid-liquid separation process, comprises the following steps:
A. the aqueous solution or water-organic solvent mixed solution that contain low concentration soluble solid concentrate by multiple-effect evaporation, concentration mixed solution in generation;
B. middle concentration mixed solution is entered stirring evaporating kettle, further evaporation and concentration, produce high concentration mixed solution;
C. control the solid content of high concentration mixed liquor, ensureing to discharge with fluid form to stir evaporating kettle, solidifying at least partly when the high concentration mixed liquor of discharge is through being cooled to normal temperature.
In the present invention, unless otherwise defined, involved concentration all refers to mass concentration, such as, and solute mass percent in the solution.All " in scope " includes end value, and such as 25% ~ 50% comprises 25% and 50%.
The disolvable solid mass range of described low concentration mixed solution is 0.1% ~ 5%, is preferably 0.3% ~ 2%.
In steps A Multi-effect Evaporation Processes, soluble solid concentration in concentration mixed solution in control, ensure to be less than 20% because solid concentration increase causes multiple-effect evaporation throughput to reduce, multifunctional evaporating equipment non-scaling blocks, and stirs evaporation institute consumed energy and be less than 5% of evapo tranpiration energy in step B.
In the present invention, throughput refers to the inlet amount in the unit interval of multi-effect evaporation system, such as, kg/hour.
In the present invention, the energy that evapo tranpiration energy consumes for steps A multiple-effect evaporation and step B stir the energy sum of evaporating and consuming.
In control, in concentration mixed solution, the concentration of soluble solid can reach following object: (1) is guaranteed that throughput reduces and is less than 20%, (2) prevent multifunctional evaporating equipment fouling and clogging, (3) guarantee that stirring evaporation institute consumed energy is less than 5% of evapo tranpiration energy.
In steps A, described multiple-effect evaporation is three ~ five effect evaporations.1st effective evaporator adopts malleation or tiny structure, utilizes external heat source to heat, two imitate utilize an effect to be evaporated steam as heat source, the steam that triple effect utilizes two effects to be evaporated as heat source, if be greater than triple effect, then by that analogy; One effect separator, 2nd effect evaporator and separator, triple effect evaporator and separator and be greater than the evaporimeter of triple effect and separator, condenser all adopt negative pressure; One effect vacuum is greater than two effect vacuums, and two effect vacuums are greater than triple effect vacuum, if be greater than triple effect, then by that analogy, last effect vacuum is greater than condenser vacuum.
In steps A, described soluble solid is a kind of organic matter, more than one organic mixtures, the mixture of a kind of organic matter and one or more inorganic matters, or the mixture of more than one organic matters and one or more inorganic matters.Under multiple-effect evaporation operational temperature conditions, the mass percent of soluble solid in middle concentration mixed solution is in 20% ~ 50% scope, time preferably in 25% ~ 40% scope, middle concentration mixed solution mainly exists with liquid state, at least 90% is liquid (liquid quality/middle concentration mixed solution quality), and preferably at least 95% is liquid.Solid in control in concentration mixed solution can prevent multifunctional evaporating equipment fouling and clogging effectively at lower content.
Described melting point of organic matter scope is 75 ~ 250 DEG C, is one or more mixture of organic phosphoric acid and its esters, acetamide, ammonium acetate.Described organic phosphoric acid is methyl acid phosphate and/or dimethyl phosphoric acid.
Described inorganic matter is one or more mixture etc. of phosphoric acid and its esters, Sulfates.Under multiple-effect evaporation operational temperature conditions, phosphoric acid salt, the Sulfates inorganic matter solubility in middle concentration mixed solution is greater than its concentration in middle concentration mixed solution, does not substantially generate precipitation, guarantees that multifunctional evaporating equipment non-scaling blocks.
Described organic solvent be dissolve each other with water within the scope of concentration for the treatment of, boiling point lower than a kind of organic matter of 150 DEG C or more than one organic mixtures, be preferably one or more mixture of methyl alcohol, ethanol, formic acid, acetic acid or acetone.
The external heat source of described multiple-effect evaporation technique is hot water, steam or conduction oil; Heat exchange mode adopts following current, adverse current or cross-flow.
In step C, the described type of cooling is nature cooling, water-cooled or air-cooled.
In step C, the high concentration mixed liquor of described fluid form refers under stirring evaporating kettle operational temperature conditions, due to residual a small amount of water or water and organic solvent, and/or be in molten condition due to one or more organic matters in soluble solid, SECTIONMelting points in high concentration mixed liquor is caused higher than the dissolution of solid stirring evaporating kettle operating temperature, to make high concentration mixed liquor have good mobility.Disolvable solid quality in described high concentration mixed solution in 70% ~ 95% scope, preferably in 85% ~ 95% scope, more preferably 90% ~ 95%.Solidify at least partly when the high concentration mixed liquor of discharging is through being cooled to environment temperature, preferably at least 50% solidification, more preferably at least 60% solidification, more preferably at least 70% solidification, more preferably at least 80% solidification, more preferably at least 90% solidification, most preferably at least 100% solidification.Different with geographical position according to season, environment temperature may within the scope of-40 ~ 50 DEG C.Under the condition that disolvable solid content is identical, environment temperature is different, and state of cure also can be different.
A kind of triple effect evaporation solid-liquid separation process, comprises the steps:
Enter in the effect separator in triple effect evaporation system containing the aqueous solution of low concentration soluble solid or water-organic solvent mixed solution, Matter Transfer is between each effect separator and evaporimeter, one effect separator and two imitate between separator, two imitate between separator and triple effect separator, between triple effect separator and stirring evaporating kettle respectively by circulating pump convey materials, in addition, by pressure in vavuum pump adjustment triple effect evaporation system and stirring evaporating kettle;
Low concentration mixed solution is heated by external heat source in 1st effective evaporator, in heating process, part solution flashes to vapour phase, liquid-vapor mixture enters an effect separator and realizes vapor-liquid separation, be separated the vapour phase obtained and pass into 2nd effect evaporator, as the thermal source of two effect evaporations, after heat exchange, condensate liquid is deposited in storage tank; Be separated the liquid phase part extraction obtained and deliver into two effect separators, component loops enters in 1st effective evaporator and continues evaporation.
In 2nd effect evaporator, liquid phase from an effect separator is imitated the vapour phase heating evaporation of separator from one, liquid-vapor mixture enters two effect vapour liquid separators and realizes vapor-liquid separation, be separated the vapour phase obtained and pass into triple effect evaporator, as the thermal source of triple effect evaporation, after heat exchange, condensate liquid is deposited in storage tank; Be separated the liquid phase part extraction obtained and deliver into triple effect separator, component loops enters in 2nd effect evaporator and continues evaporation.
In triple effect evaporator, liquid phase from two effect separators 3 is imitated the vapour phase heating evaporation of separators from two, liquid-vapor mixture enters triple effect separator and realizes vapor-liquid separation, is separated the vapour phase obtained and passes into condenser, the condensate liquid that condensation obtains is target product, deposits in storage tank; Be separated the liquid phase part circulation obtained and enter triple effect evaporator, part extraction delivers into stirring evaporating kettle and carries out further lock out operation.
Again evaporate in stirring evaporating kettle from concentration mixed liquor in triple effect separator, steam comes back to triple effect evaporation system, and after temperature in the kettle no longer rises, after the high concentration mixed solution discharge of formation, cooling is rear curable naturally.
Low concentration mixed liquor is original feed, middle concentration mixed liquor has low concentration mixed liquor after multiple-effect evaporation, in last effect separator of multiple-effect evaporation, (this example is triple effect evaporation in generation, therefore be created on triple effect separator 5), middle concentration mixed solution enter into stir evaporating kettle 9 again evaporate after become high concentration mixed solution.
The present invention, by controlling solution concentration in last effect of multiple-effect evaporation, solves because solid concentration increase, dividing potential drop change cause multiple-effect evaporation throughput to reduce, the problem of the easy fouling and clogging of excessive vaporization equipment.Solution after appropriateness concentrates by the present invention carries out separately stirring evaporation, does not affect the treatment effeciency of multiple-effect evaporation, and controls to stir evaporation institute consumed energy and be less than 5% of evapo tranpiration energy, averages out between energy-conservation and efficiency.And, the steam stirring evaporation generation can also be returned vapo(u)rization system, not only can solve the entrainment problem in evaporation process, the integrated of energy and comprehensive utilization can also be realized.
The present invention has following beneficial effect;
Contrast direct evaporation technology, adopt this technique to carry out evaporative crystallization Separation of Solid and Liquid energy consumption and significantly reduce, under the condition that evaporation capacity is identical, multiple-effect evaporation needs the heating steam consumed only to account for about 40% of the required heating steam of directly evaporation.This technique, by controlling solution concentration in last effect of multiple-effect evaporation, solves because solid concentration increase, dividing potential drop change cause multiple-effect evaporation throughput to reduce, the technical problems such as the easy fouling and clogging of excessive vaporization equipment.Solution after appropriateness concentrates by the present invention carries out separately stirring evaporation, does not affect the treatment effeciency of multiple-effect evaporation, and controls to stir evaporation institute consumed energy and be less than 5% of evapo tranpiration energy, averages out between energy-conservation and efficiency.And, after stirring evaporation, highly concentrated solution is discharged in liquid form, through cooling rear section or all solidifying, transport convenience can be improved, also the steam stirring evaporation generation is returned vapo(u)rization system, not only can solve the entrainment problem in evaporation process, the integrated of energy and comprehensive utilization can also be realized.
Accompanying drawing explanation
Fig. 1 is that in the embodiment of the present invention, triple effect evaporation combines the solid-liquid separation process schematic diagram stirring evaporation.
Number in the figure is:
1, an effect separator, 2,1st effective evaporator,
3, two effect separator 4,2nd effect evaporators
5, triple effect separator 6, triple effect evaporator
7, condenser 8, storage tank
9, evaporating kettle 10,11,12 circulating pump is stirred
13 vavuum pumps.
Detailed description of the invention
Further illustrate the present invention below in conjunction with accompanying drawing illustrated embodiment, but content of the present invention is not confined to cited embodiment scope.
Embodiment 1
In acetic acid-aqueous solution system, containing potassium chloride, phosphoric acid and metal thereof and ammonium salt, organic phosphoric acid and metal thereof and ammonium salt, acetamide, its gross mass content is approximately 4.5%.
Pretreated acetic acid-aqueous solution is delivered to triple-effect evaporation plant by feed pump and carries out evaporation process, be external heat source with steam in 1st effective evaporator, concurrent is adopted to heat acetic acid-aqueous solution system, (now can ensure that causing multiple-effect evaporation throughput to reduce because solid concentration increases is less than 20% when soluble solid concentration in mixed solution in triple effect separator reaches 35%, ensure the blocking of multifunctional evaporating equipment non-scaling, ensure to stir evaporation institute consumed energy and be less than 5% of evapo tranpiration energy), mixed solution is entered and stirs the further evaporation and concentration of evaporating kettle, produce high concentration mixed solution, until after in stirring evaporating kettle, temperature stabilization no longer rises, discharge and stir high concentration mixed solution residual in evaporating kettle, the high concentration mixed solution concentration of now discharging is about 95%, because its temperature is higher, still fluidised form is kept, to be discharged through water-cooled rear section or all solidify out into solid-state.
Embodiment 2
In formic acid-water solution system, containing sodium chloride, diammonium hydrogen phosphate, ammonium acetate, its gross mass content arrives 0.5%.
Pretreated formic acid-aqueous solution is delivered to four-effect evaporation device by feed pump and carries out evaporation process, be external heat source with hot water in 1st effective evaporator, reflux type is adopted to heat formic acid-water solution system, (now can ensure that causing multiple-effect evaporation throughput to reduce because solid concentration increases is less than 20% when soluble solid concentration in mixed solution in quadruple effect separator reaches 25%, ensure the blocking of multifunctional evaporating equipment non-scaling, ensure to stir evaporation institute consumed energy and be less than 5% of evapo tranpiration energy), mixed solution is entered and stirs the further evaporation and concentration of evaporating kettle, produce high concentration mixed solution, until after in stirring evaporating kettle, temperature stabilization no longer rises, discharge and stir high concentration mixed solution residual in evaporating kettle, the high concentration mixed solution concentration of now discharging is about 85%, because its temperature is higher, still fluidised form is kept, to be discharged through air-cooled rear section or all solidify out into solid-state.
Embodiment 3
In ethanol-water solution system, containing potassium sulfate, ammonium dihydrogen phosphate (ADP), ammonium acetate, its gross mass content arrives 0.1%.Pretreated ethanol-water solution is delivered to five effect evaporators by feed pump and carries out evaporation process, in 1st effective evaporator with heat with conduction oil for external heat source, cross-current flow is adopted to heat ethanol-water solution system, (now can ensure that causing multiple-effect evaporation throughput to reduce because solid concentration increases is less than 20% when soluble solid concentration in mixed solution in five effect separators reaches 30%, ensure the blocking of multifunctional evaporating equipment non-scaling, ensure to stir evaporation institute consumed energy and be less than 5% of evapo tranpiration energy), mixed solution is entered and stirs the further evaporation and concentration of evaporating kettle, produce high concentration mixed solution, until after in stirring evaporating kettle, temperature stabilization no longer rises, discharge and stir high concentration mixed solution residual in evaporating kettle, the high concentration mixed solution concentration of now discharging is about 70%, because its temperature is higher, still fluidised form is kept, to be discharged through naturally cooling rear section or all solidifying out into solid-state.
Embodiment 4
As shown in the figure, water-organic solvent mixed solution containing low concentration soluble solid enters in triple effect evaporation system, Matter Transfer is between each effect separator and evaporimeter, one effect separator 1 and two is imitated between separator 3, two imitate between separator 3 and triple effect separator 5 respectively by transport pump material, in addition, by pressure in vavuum pump adjustment triple effect evaporation system and stirring evaporating kettle.
Low concentration mixed solution is heated by external heat source in 1st effective evaporator 2, in heating process, part solution flashes to vapour phase, liquid-vapor mixture enters an effect separator 1 and realizes vapor-liquid separation, be separated the vapour phase obtained and pass into 2nd effect evaporator 4, as the thermal source of two effect evaporations, after heat exchange, condensate liquid is deposited in storage tank 8; Be separated the liquid phase part extraction obtained and deliver into two effect separators 3, component loops enters in 1st effective evaporator 2 and continues evaporation.
In 2nd effect evaporator 4, liquid phase from an effect separator 1 is imitated the vapour phase heating evaporation of separator 1 from one, liquid-vapor mixture enters two effect vapour liquid separators 3 and realizes vapor-liquid separation, be separated the vapour phase obtained and pass into triple effect evaporator 6, as the thermal source of triple effect evaporation, after heat exchange, condensate liquid is deposited in storage tank 8; Be separated the liquid phase part extraction obtained and deliver into triple effect separator 5, component loops enters in 2nd effect evaporator 4 and continues evaporation.
In triple effect evaporator 6, liquid phase from two effect separators 3 is imitated the vapour phase heating evaporation of separators 3 from two, liquid-vapor mixture enters triple effect separator 5 and realizes vapor-liquid separation, is separated the vapour phase obtained and passes into condenser 7, the condensate liquid that condensation obtains is target product, deposits in storage tank 8; Be separated the liquid phase part circulation obtained and enter triple effect evaporator, part extraction delivers into stirring evaporating kettle and carries out further lock out operation.
Again evaporate in stirring evaporating kettle 9 from concentration mixed solution in triple effect separator 5, steam comes back to triple effect evaporation system, and after temperature in the kettle no longer rises, high concentration mixed solution is discharged through cooling rear section or all solidified.
Above-mentioned is can understand for ease of those skilled in the art and use the present invention to the description of embodiment.Person skilled in the art obviously easily can make various amendment to these embodiments, and General Principle described herein is applied in other embodiments and need not through performing creative labour.Therefore, the invention is not restricted to above-described embodiment, those skilled in the art, according to announcement of the present invention, do not depart from improvement that scope makes and amendment all should within protection scope of the present invention.
Claims (15)
1. a solid-liquid separation process, is characterized in that: comprise the following steps:
A. the aqueous solution or water-organic solvent mixed solution that contain low concentration soluble solid concentrate by multiple-effect evaporation, concentration mixed solution in generation;
B. middle concentration mixed solution is entered stirring evaporating kettle, further evaporation and concentration, produce high concentration mixed solution;
C. control the solid content of high concentration mixed liquor, discharging with fluid form and stir evaporating kettle, solidifying at least partly when the high concentration mixed liquor of discharge is through being cooled to environment temperature.
2. solid-liquid separation process as claimed in claim 1, it is characterized in that: in Multi-effect Evaporation Processes controls, in concentration mixed solution, soluble solid concentration reaches following effect: (1) causes because solid concentration increases multiple-effect evaporation throughput to reduce and is less than 20%, (2) the basic non-scaling blocking of multifunctional evaporating equipment, (3) are stirred evaporation institute consumed energy and are less than 5% of evapo tranpiration energy.
3. solid-liquid separation process as claimed in claim 1 or 2, is characterized in that: described multiple-effect evaporation is three ~ five effect evaporations.
4. solid-liquid separation process as claimed in claim 1 or 2, it is characterized in that: described soluble solid is a kind of organic matter, more than one organic mixtures, a mixture for organic matter and one or more inorganic matters, or the mixture of more than one organic matters and one or more inorganic matters.
5. solid-liquid separation process as claimed in claim 4, is characterized in that: described melting point of organic matter scope is 75 ~ 250 DEG C, comprises organic phosphoric acid and its esters, acetamide, ammonium acetate.
6. solid-liquid separation process as claimed in claim 5, is characterized in that: described organic phosphoric acid is methyl acid phosphate and/or dimethyl phosphoric acid.
7. solid-liquid separation process as claimed in claim 4, is characterized in that: described inorganic matter comprises phosphoric acid and its esters, Sulfates.
8. solid-liquid separation process as claimed in claim 1 or 2, is characterized in that: described organic solvent be dissolve each other with water within the scope of concentration for the treatment of, boiling point is lower than a kind of organic matter of 150 DEG C or more than one organic mixtures.
9. solid-liquid separation process as claimed in claim 8, is characterized in that: described organic solvent is one or more mixture of methyl alcohol, ethanol, formic acid, acetic acid or acetone.
10. solid-liquid separation process as claimed in claim 1 or 2, it is characterized in that: described multiple-effect evaporation technique is three ~ five effect evaporations, 1st effective evaporator adopts malleation or tiny structure, external heat source is utilized to heat, two imitate utilize an effect to be evaporated steam as heat source, the steam that triple effect utilizes two effects to be evaporated as heat source, if be greater than triple effect, then by that analogy; One effect separator, 2nd effect evaporator and separator, triple effect evaporator and separator and be greater than the evaporimeter of triple effect and separator, condenser all adopt negative pressure; One effect vacuum is greater than two effect vacuums, and two effect vacuums are greater than triple effect vacuum, if be greater than triple effect, then by that analogy, last effect vacuum is greater than condenser vacuum.
11. solid-liquid separation process as described in claim 1 or 10, is characterized in that: the external heat source of described multiple-effect evaporation technique is hot water, steam or conduction oil; Heat exchange mode adopts following current, adverse current or cross-flow.
12. solid-liquid separation process as claimed in claim 1 or 2, is characterized in that: the disolvable solid mass range of described low concentration mixed solution is 0.1% ~ 5%.
13. solid-liquid separation process as claimed in claim 1 or 2, is characterized in that: the disolvable solid mass range of described middle concentration mixed solution is 20% ~ 50%.
14. solid-liquid separation process as claimed in claim 1 or 2, is characterized in that: the disolvable solid mass range of described high concentration mixed solution is 70% ~ 95%.
15. solid-liquid separation process as claimed in claim 1 or 2, is characterized in that: the described type of cooling is nature cooling, water-cooled or air-cooled.
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| CN201310519642.8A CN104548634B (en) | 2013-10-28 | 2013-10-28 | A kind of multiple-effect evaporation combines the solid-liquid separation process of stirring evaporation |
| PCT/CN2014/088163 WO2015062393A1 (en) | 2013-10-28 | 2014-10-09 | Solid-liquid separation process with multi-effect evaporation in combination with stirring evaporation |
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| CN106348268A (en) * | 2016-08-29 | 2017-01-25 | 四川绵竹三佳饲料有限责任公司 | Method for crystallizing ammonium dihydrogen phosphate |
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| CN111573646A (en) * | 2020-04-02 | 2020-08-25 | 江苏德邦多菱健康科技有限公司 | Preparation method of disodium hydrogen phosphate large particles by double-effect crystallization method |
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| GB411624A (en) * | 1933-03-15 | 1934-06-14 | George Scott & Son London Ltd | Improvements in or relating to the separation of dissolved solids by evaporation |
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| CN111573646A (en) * | 2020-04-02 | 2020-08-25 | 江苏德邦多菱健康科技有限公司 | Preparation method of disodium hydrogen phosphate large particles by double-effect crystallization method |
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| WO2015062393A1 (en) | 2015-05-07 |
| CN104548634B (en) | 2016-08-17 |
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