CN202594905U - MVR (mechanical vapor recompression) efficient and energy-saving evaporating system - Google Patents
MVR (mechanical vapor recompression) efficient and energy-saving evaporating system Download PDFInfo
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- CN202594905U CN202594905U CN2012200633617U CN201220063361U CN202594905U CN 202594905 U CN202594905 U CN 202594905U CN 2012200633617 U CN2012200633617 U CN 2012200633617U CN 201220063361 U CN201220063361 U CN 201220063361U CN 202594905 U CN202594905 U CN 202594905U
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Abstract
The utility model provides an MVR (mechanical vapor recompression) efficient and energy-saving evaporating system which is used for separating sodium chloride and potassium chloride from industrial wastewater by crystallizing respectively. The MVR efficient and energy-saving evaporating system comprises a preheater, a falling film evaporator, a falling film separator, a forced circulating evaporator, a crystallizing separator, a cooling reaction kettle, a sodium salt centrifuge, a deep cooler, a potassium salt settling tank, an organic solution storing tank, a potassium salt centrifuge and a centrifugal vapor compressor. According to solubility characteristics of the sodium chloride and the potassium chloride, the MVR efficient and energy-saving evaporating system is correspondingly equipped with equipment for concentrating by evaporating, cooling, and adding an organic solvent so as to separate the sodium chloride and the potassium chloride by crystallizing respectively; the crystallizing amount is large; and the purity is high.
Description
Technical field
The utility model belongs to the technology for treating industrial waste water field, particularly a kind of energy-efficient vapo(u)rization system of MVR that is used at trade effluent difference Crystallization Separation sodium-chlor and Repone K.
Background technology
Be accompanied by industrial production, all will produce a large amount of trade effluents every day, especially produces some high salt industry waste water, and the ideal situation is from high salt industry waste water, to extract the inorganic salt that certain value is arranged, and reclaims and sells, turns waste into wealth.In the prior art; Through pre-treatment to certain high salt industry waste water; Can the impurity in this high salt industry waste water, heavy metal etc. be removed; Only being contained the trade effluent of sodium-chlor and Repone K, and potassium chloride and sodium chloride crystal that how dna purity is high from trade effluent efficiently, output is big become the technical problem that those skilled in the art need to be resolved hurrily.
The utility model content
For solving defective of the prior art; The utility model provides a kind of energy-efficient vapo(u)rization system of MVR that is used at trade effluent difference Crystallization Separation sodium-chlor and Repone K; This system utilizes the dissolubility property of sodium-chlor and Repone K; In system, correspondingly be provided with the equipment that is used for evaporation concentration, cooling and interpolation organic solvent realizing Crystallization Separation sodium-chlor and Repone K respectively, and go out that brilliant amount is big, purity is high.
Technical scheme:
The energy-efficient vapo(u)rization system of a kind of MVR; It is characterized in that; Said vaporizer includes preheater, falling-film evaporator, falling film separator, pump feed evaporator, Crystallization Separation device, cooling reaction still, sodium salt whizzer, deep cooler, sylvite slurry tank, organic solution storage tank, sylvite whizzer and centrifugal vapour compressor; Wherein stoste gets into from the feed liquid inlet end of said preheater; The material liquid outlet end of said preheater is connected through the feed liquid pipeline with the first feed liquid inlet end of falling-film evaporator; The material liquid outlet end of said falling-film evaporator is connected through the feed liquid pipeline with the feed liquid inlet end of falling film separator; The first material liquid outlet end of said falling film separator is connected through the feed liquid pipeline with the first feed liquid inlet end of Crystallization Separation device; The second material liquid outlet end of said falling film separator is connected through the feed liquid pipeline with the second feed liquid inlet end of falling-film evaporator; The first material liquid outlet end of said Crystallization Separation device is connected through the feed liquid pipeline with the feed liquid inlet end of pump feed evaporator; The material liquid outlet end of said pump feed evaporator is connected through the feed liquid pipeline with the second feed liquid inlet end of Crystallization Separation device; The second material liquid outlet end of said Crystallization Separation device is connected through the feed liquid pipeline with the feed liquid inlet end of cooling reaction still; The material liquid outlet end of said cooling reaction still and the feed liquid inlet end of sodium salt whizzer are connected through the feed liquid pipeline with the feed liquid inlet end of deep cooler through the be connected material liquid outlet end of said sodium salt whizzer of feed liquid pipeline; Said sodium salt whizzer also comprises the crystal exit end, and the material liquid outlet end of said deep cooler is connected through the feed liquid pipeline with the feed liquid inlet end of said sylvite slurry tank, and the material liquid outlet end of said sylvite slurry tank is connected with the feed liquid inlet end of sylvite whizzer; Said sylvite whizzer includes crystal exit end and material liquid outlet end; The material liquid outlet end of said organic solvent storage tank is connected through the feed liquid pipeline with the feed liquid inlet end of said sylvite slurry tank, and the vapour outlet end of said falling film separator is connected through gas pipeline with the steam-in end of centrifugal steam compressor, and the vapour outlet end of said Crystallization Separation device is connected through gas pipeline with the steam-in end of centrifugal vapour compressor; The secondary steam exit end of centrifugal vapour compressor is that said falling-film evaporator and pump feed evaporator provide secondary steam through gas pipeline, store in the said organic solvent storage tank can with the codissolved organic solvent of water.
The secondary steam exit end of said centrifugal vapour compressor is connected through gas pipeline with the secondary steam inlet end of falling-film evaporator, and the secondary steam inlet end of said pump feed evaporator is connected with the gas pipeline of the secondary steam inlet end of falling-film evaporator with the secondary steam exit end that is communicated with said centrifugal vapour compressor through gas pipeline.
Said preheater includes first plate type preheater and second plate type preheater; Said stoste gets into through the feed liquid inlet end of first plate type preheater; The material liquid outlet end of said first plate type preheater is connected through the feed liquid pipeline with the feed liquid inlet end of second plate type preheater, and the material liquid outlet end of said second plate type preheater is connected through the feed liquid pipeline with the first feed liquid inlet end of falling-film evaporator.
Said vapo(u)rization system also includes the condensation water pot; The condensation-water drain end of said falling-film evaporator and said pump feed evaporator is connected through condensing water conduit with the condensing water inlet end of condensation water pot respectively; It is the water of condensation that first plate type preheater is provided for heat exchange that the condensation-water drain end of said condensation water pot is connected with the condensing water inlet end of first plate type preheater through condensing water conduit, and the non-condensable gas that the shell of the falling-film evaporator in the said vapo(u)rization system and the shell of pump feed evaporator produce is transported to second plate type preheater and is used for and the stoste heat exchange.
The sodium chloride concentration on-line measuring device that is used to detect sodium chloride concentration is installed in the said falling film separator.
The potassium chloride concentration on-line measuring device that is used to detect potassium chloride concentration is installed in the said Crystallization Separation device.
Also include the liquid concentrator buffer tank; Said liquid concentrator buffer tank is between said sodium salt whizzer and deep cooler; The material liquid outlet end of sodium salt whizzer is connected through the feed liquid pipeline with the feed liquid inlet end of liquid concentrator buffer tank, and the material liquid outlet end of said liquid concentrator buffer tank is connected through the feed liquid pipeline with the feed liquid inlet end of deep cooler.
Said organic solution storage tank is for being used to store the alcoholic acid ethanol storage tank.
Also comprise ethanol rectification and purification device; The material liquid outlet end of sylvite whizzer is connected with the feed liquid inlet end that ethanol rectifying proposes device; The ethanol exit end of ethanol rectification and purification device is connected with the ethanol inlet end of ethanol storage tank through the feed liquid pipeline; The mother liquor exit end of ethanol rectification and purification device is connected with the feed liquid inlet end of mother liquor return tank through the feed liquid pipeline; And the material liquid outlet end of mother liquor return tank is connected with the feed liquid inlet end of pump feed evaporator through the feed liquid pipeline, and said mother liquor is a remaining feed liquid behind the separating alcohol.
Said stoste is that mass concentration is 3% sodium-chlor and Repone K trade effluent; Wherein the mass ratio of sodium-chlor and Repone K is 7: 3; Store absolute ethyl alcohol in the said ethanol storage tank, the agent water that is introduced into the absolute ethyl alcohol in the sylvite slurry tank through the feed liquid pipeline is than being 30-70%, and said dose of water is than the ratio for the quality of the water in the concentrated feed liquid in the total mass of absolute ethyl alcohol and the sylvite slurry tank; Correspondingly, the setting cooling temperature of deep cooler is 30 ℃.
The energy-efficient vapo(u)rization system of a kind of MVR is characterized in that, comprises master control system PLC, is used for each equipment of the above-mentioned energy-efficient vapo(u)rization system of MVR.
Technique effect:
The utility model provides a kind of MVR energy-efficient vapo(u)rization system; Include preheater, falling-film evaporator, falling film separator, pump feed evaporator, Crystallization Separation device, cooling reaction still, sodium salt whizzer, deep cooler, sylvite slurry tank, organic solution storage tank, sylvite whizzer and centrifugal vapour compressor; Be used for containing the trade effluent difference Crystallization Separation sodium-chlor and the Repone K of sodium-chlor and Repone K; The utility model is according to the dissolubility property of sodium-chlor and Repone K; Be that sodium-chlor belongs to thermal crystalline, Repone K belongs to cold crystallization, the energy-efficient vapo(u)rization system of the MVR that designs.Stoste (trade effluent) is through preheating in preheater; Evaporation concentration in the falling-film evaporator; Gas-liquid separation in falling film separator; Further evaporation concentration in pump feed evaporator; And then gas-liquid separation in the Crystallization Separation device; In the cooling reaction still with feed liquid cooling (because sodium salt whizzer non-refractory); In the sodium salt whizzer, isolate sodium chloride crystal; In deep cooler, carry out degree of depth cooling; In the sylvite slurry tank, add organic solvent to reduce solubleness; In the sylvite whizzer, isolate potassium chloride.In above-mentioned process, in the process of stoste (trade effluent) evaporation concentration, along with the continuous evaporation of moisture; Under vaporization temperature, because the saturation solubility of sodium-chlor is far below the saturation solubility of Repone K, it is saturated that the sodium-chlor in the trade effluent at first is tending towards; And then preferential precipitated sodium chloride crystal; When Repone K reaches capacity, stop evaporation, and isolate the sodium chloride crystal of separating out.Then, the concentrated feed liquid of isolating behind the sodium chloride crystal is carried out processing under cooling, along with the reduction of temperature, the saturation solubility of Repone K also reduces rapidly, and sodium-chlor is influenced hardly, and the crystallization that separate out this moment mainly is a potassium chloride.But the Repone K crystallization of separating out this moment only account for the Repone K in the solution total amount about 10%, and most Repone K is not also separated out in solution.Therefore, in the cooling concentration feed liquid, add can with the codissolved organic solvent of water, to reduce the saturation solubility of Repone K and sodium-chlor significantly; But the influence degree to Repone K is bigger, and have a large amount of crystal to separate out this moment, and separating this part the crystalline staple that obtains is Repone K; A spot of sodium-chlor is also arranged; So far, can be with sodium-chlor and Repone K Crystallization Separation respectively from trade effluent, and obtain the purity height, go out big sodium-chlor and the potassium chloride of brilliant amount.
In cooled concentrated feed liquid, add with the miscible organic solvent of water after, organic molecule and water molecules, a part of sodium-chlor and Repone K molecule can not exist with ionic species in water, thereby separate out with molecular form, so its solubleness reduction.Wherein can be methyl alcohol, ethanol, ether, acetone, terepthaloyl moietie, USP Kosher, formaldehyde, acetaldehyde, formic acid or acetate etc. with the codissolved organic solvent of water.
Centrifugal vapour compressor is provided for the secondary steam of heat exchange to falling-film evaporator, and simultaneously, centrifugal vapour compressor is returned the secondary steam that pump feed evaporator is provided for heat exchange.
Be used for to be two-stage plate formula preheater to the preheater of stoste preheating; I.e. first plate type preheater and second plate type preheater; Being used for the heat exchange water of condensation in first plate type preheater is the water of condensation that falling-film evaporator and pump feed evaporator produce, and the non-condensable gas that vapo(u)rization system produces is used for the heat exchange of second plate type preheater.
The sodium chloride concentration on-line measuring device that is used to detect sodium chloride concentration is installed in falling film separator.And the potassium chloride concentration on-line measuring device that is used to detect potassium chloride concentration is installed in the Crystallization Separation device.Judge next step action of system according to detected concentration.
Further, also include the liquid concentrator buffer tank, its effect is to guarantee that liquid concentrator is with constant flow rate depth of drive water cooler.
Because alcoholic acid recovery technology comparative maturity, and alcoholic acid low price, the utility model preferably adopt ethanol with the codissolved organic solvent of water.Correspondingly, the organic solution storage tank is for being used to store the alcoholic acid ethanol storage tank.Particularly; Alcoholic acid in the solution reclaims and can reclaim through distillation technology; So that add to again in the sylvite slurry tank, remove mother liquor behind the ethanol in addition and can also turn back to again and participate in evaporating concentration process in the pump feed evaporator as the organic solution additive.
The utility model also provides a kind of MVR energy-efficient vapo(u)rization system, comprises master control system PLC (programmable logic controller), is used for other equipment of system.
Description of drawings
The curve that Fig. 1 sodium-chlor and Klorvess Liquid solubility with temperature change;
A kind of embodiment of the energy-efficient vapo(u)rization system of MVR of Fig. 2 the utility model.
Each label example is following among the figure:
1-first plate type preheater, 2-second plate type preheater, 3-falling-film evaporator, 4-falling film separator, 5-pump feed evaporator; 6-Crystallization Separation device, the centrifugal vapour compressor of 7-, 8-cooling reaction still, 9-deep cooler, 10-sodium salt whizzer; 11-sylvite whizzer, 12-liquid concentrator buffer tank, 13-sylvite slurry tank, 14-rectifying preheater, 15-ethanol rectifying tower; 16-ethanol water cooler, 17-mother liquor return tank, 18-ethanol storage tank, 19-condensation water pot.
Embodiment
For the purpose, technical scheme and the advantage that make the utility model is clearer,, the utility model is further elaborated below in conjunction with accompanying drawing and embodiment.Should be appreciated that specific embodiment described herein only in order to explanation the utility model, and be not used in qualification the utility model.
The utility model provides a kind of MVR energy-efficient vapo(u)rization system, utilizes this system from trade effluent, to obtain high purity, exceeds the brilliant potassium chloride of measuring.
Shown in Figure 1 is the curve that sodium-chlor and Klorvess Liquid solubility with temperature change.As can beappreciated from fig. 1, the rate of curve that the solubility with temperature of sodium-chlor and Repone K changes is different, and temperature variation is very little to the change of the solubleness of sodium-chlor, and it belongs to thermal crystalline; And the solubleness of Repone K along with the rising of temperature increase very fast, it belongs to cold crystallization.
Shown in Figure 2 is a kind of embodiment of the energy-efficient vapo(u)rization system of MVR of the utility model.Solid line among the figure is represented the transmission of feed liquid, and the dotted line among the figure is represented the transmission of water of condensation, and the long and short dash line among the figure is represented the transmission of steam.The master control system PLC that the energy-efficient vapo(u)rization system of MVR includes first plate type preheater 1, second plate type preheater 2, falling-film evaporator 3, falling film separator 4, pump feed evaporator 5, Crystallization Separation device 6, centrifugal vapour compressor 7, cooling reaction still 8, deep cooler 9, sodium salt whizzer 10, sylvite whizzer 11, liquid concentrator buffer tank 12, sylvite slurry tank 13, rectifying preheater 14, ethanol rectifying tower 15, ethanol water cooler 16, mother liquor return tank 17, ethanol storage tank 18 and condensation water pot 19 and is used to control aforesaid device is not (when needing other equipment of master control system PLC control; Also master control system PLC can be set); Wherein first plate type preheater 1 includes feed liquid inlet end 1-1, material liquid outlet end 1-2, condensing water inlet end 1-3 and condensation-water drain end 1-4; Second plate type preheater 2 includes feed liquid inlet end 2-1, material liquid outlet end 2-2; Falling-film evaporator 3 includes the first feed liquid inlet end 3-1, material liquid outlet end 3-2, secondary steam inlet end 3-3, condensation-water drain end 3-4, the second feed liquid inlet end (not shown); Falling film separator 4 includes feed liquid inlet end 4-1, the first material liquid outlet end 4-2, vapour outlet end 4-3, the second material liquid outlet end (not shown); Pump feed evaporator 5 includes feed liquid inlet end 5-1, material liquid outlet end 5-2, condensation-water drain end 5-3, secondary steam inlet end 5-4; Crystallization Separation device 6 includes the first feed liquid inlet end 6-1, the first material liquid outlet end 6-2, the second feed liquid inlet end 6-3, the second material liquid outlet end 6-4, vapour outlet end 6-5; Centrifugal vapour compressor 7 includes steam-in end 7-1, secondary steam exit end 7-2; Cooling reaction still 8 includes feed liquid inlet end 8-1, material liquid outlet end 8-2; Deep cooler 9 includes feed liquid inlet end 9-1, material liquid outlet end 9-2; Sodium salt whizzer 10 includes feed liquid inlet end 10-1, material liquid outlet end 10-2, crystal exit end 10-3; Sylvite whizzer 11 includes feed liquid inlet end 11-1, material liquid outlet end 11-2, crystal exit end 11-3; Liquid concentrator buffer tank 12 includes feed liquid inlet end 12-1, material liquid outlet end 12-2; Sylvite slurry tank 13 includes feed liquid inlet end 13-1, material liquid outlet end 13-2; Rectifying preheater 14 includes feed liquid inlet end 14-1, material liquid outlet end 14-2, condensation-water drain end 14-3; Ethanol rectifying tower 15 includes feed liquid inlet end 15-1, mother liquor inlet end 15-2, ethanol exit end 15-3, mother liquor exit end 15-4; Ethanol water cooler 16 includes ethanol inlet end 16-1, ethanol exit end 16-2; Mother liquor return tank 17 includes mother liquor inlet end 17-1, the first mother liquor exit end 17-2, the second mother liquor exit end 17-3; Ethanol storage tank 18 includes ethanol inlet end 18-1, ethanol exit end 18-2, and condensation water pot 19 includes the first condensing water inlet end 19-1, the second condensing water inlet end 19-2, condensation-water drain end 19-3.
Wherein the material liquid outlet end 1-2 of first plate type preheater 1 is connected through the feed liquid pipeline with the feed liquid inlet end 2-1 of second plate type preheater 2; The material liquid outlet end 2-2 of second plate type preheater 2 is connected with the first feed liquid inlet end 3-1 of falling-film evaporator 3 through the feed liquid pipeline; The material liquid outlet end 3-2 of falling-film evaporator 3 is connected with the feed liquid inlet end 4-1 of falling film separator 4 through the feed liquid pipeline; The second material liquid outlet end of falling film separator 4 is connected through the feed liquid pipeline with the second feed liquid inlet end of falling-film evaporator 3; The first material liquid outlet end 4-2 of falling-film evaporator 4 is connected with the first feed liquid inlet end 6-1 of Crystallization Separation device 6 through the feed liquid pipeline; The first material liquid outlet end 6-2 of Crystallization Separation device 6 is connected through the feed liquid pipeline with the feed liquid inlet end 5-1 of pump feed evaporator 5; The material liquid outlet end 5-2 of pump feed evaporator 5 is connected through the feed liquid pipeline with the second feed liquid inlet end 6-3 of Crystallization Separation device 6; The second material liquid outlet end 6-4 of Crystallization Separation device 6 is connected with the feed liquid inlet end 8-1 of cooling reaction still 8 through the feed liquid pipeline; The material liquid outlet end 8-2 of cooling reaction still 8 is connected through the feed liquid pipeline with the feed liquid inlet end 10-1 of sodium salt whizzer 10, and the material liquid outlet end 10-2 of sodium salt whizzer 10 is connected through the feed liquid pipeline with the feed liquid inlet end 12-1 of liquid concentrator buffer tank 12, and the material liquid outlet end 12-2 of liquid concentrator buffer tank 12 is connected with the feed liquid inlet end 9-1 of deep cooler 9 through the feed liquid pipeline; The material liquid outlet end 9-2 of deep cooler 9 is connected with the feed liquid inlet end 13-1 of sylvite slurry tank 13 through the feed liquid pipeline; The ethanol exit end 18-2 of ethanol storage tank 18 is connected with the feed liquid inlet end 13-1 of sylvite slurry tank 13 through the feed liquid pipeline, and the material liquid outlet end 13-2 of sylvite slurry tank 13 is connected through the feed liquid pipeline with the feed liquid inlet end 11-1 of sylvite whizzer 11, and the material liquid outlet end 11-2 of sylvite whizzer 11 is connected with the feed liquid inlet end 14-1 of rectifying preheater 14 through the feed liquid pipeline; The material liquid outlet end 14-2 of rectifying preheater 14 is connected with the feed liquid inlet end 15-1 of ethanol rectifying tower 15 through the feed liquid pipeline; The ethanol exit end 15-3 of ethanol rectifying tower 15 is connected through the feed liquid pipeline with the ethanol inlet end 16-1 of ethanol water cooler 16, and the ethanol exit end 16-2 of ethanol water cooler 16 is connected with the ethanol inlet end 18-1 of ethanol storage tank 18 through the feed liquid pipeline, and the mother liquor exit end 15-4 of ethanol rectifying tower 15 is connected with the mother liquor inlet end 17-1 of mother liquor return tank 17 through the feed liquid pipeline; The first mother liquor exit end 17-2 of mother liquor return tank 17 is connected with the mother liquor inlet end 15-2 of ethanol rectifying tower 15 through the feed liquid pipeline; The second mother liquor exit end 17-3 of mother liquor return tank 17 is connected with the feed liquid inlet end 5-1 of pump feed evaporator 5 (or be connected with feed liquid pipeline between the first material liquid outlet end 6-2 of the feed liquid inlet end 5-1 of pump feed evaporator 5 and Crystallization Separation device 6) through the feed liquid pipeline, and the vapour outlet end 4-3 of falling film separator 4 is connected with the steam-in end 7-1 of centrifugal vapour compressor 7 through gas pipeline, and the vapour outlet end 6-5 of Crystallization Separation device 6 is through the gas passage between the steam-in end 7-1 of gas passage and vapour outlet end 4-3 that is communicated with falling film separator 4 and centrifugal vapour compressor 7 be connected (also can: the vapour outlet end 6-5 of Crystallization Separation device 6 is connected with the steam-in end 7-1 of centrifugal vapour compressor 7 through gas pipeline); The secondary steam exit end 7-2 of centrifugal vapour compressor 7 is connected with the secondary steam inlet end 3-3 of falling-film evaporator 3 through gas passage; The secondary steam inlet end of pump feed evaporator 5 is connected with the gas pipeline of the secondary steam inlet end 3-3 of falling-film evaporator 3 with the secondary steam exit end 7-2 that is communicated with centrifugal vapour compressor 7 through gas pipeline, and the condensation-water drain end 3-4 of falling-film evaporator 3 is connected with the first condensing water inlet end 19-1 of condensation water pot 19 through condensing water conduit, and the condensation-water drain end 5-3 of pump feed evaporator 5 is connected with the second condensing water inlet end 19-2 of condensation water pot 19 through condensing water conduit; The condensation-water drain end 14-3 of rectifying preheater 14 is connected with the second condensing water inlet end 19-2 of condensation water pot 19 (or the condensation-water drain end 14-3 of rectifying preheater 14 is connected through the condensing water conduit of condensing water conduit with the second condensing water inlet end 19-2 of condensation-water drain end 5-3 that is communicated with pump feed evaporator 5 and condensation water pot 19) through condensing water conduit, and the condensation-water drain end 19-3 of condensation water pot 19 is connected with the condensing water inlet end 1-3 of first plate type preheater 1 through condensing water conduit.
Preferably; The sodium chloride concentration on-line measuring device (not shown) that is used to detect sodium chloride concentration is installed in falling film separator 4; Under the control of master control system PLC; When the concentration of the sodium-chlor in the concentrating liquid in detecting falling film separator 4 reaches set(ting)value or gets in the setting range saturation concentration of sodium-chlor (promptly near); Concentrating liquid after the gas-liquid separation is introduced in Crystallization Separation device 6 and the pump feed evaporator 5; The concentration of the intravital sodium-chlor of liquid concentrator in detecting falling film separator 4 is prescribed a time limit less than set(ting)value or less than the following of setting range, concentrating liquid after the gas-liquid separation is returned said falling-film evaporator 3 proceed the evaporation concentration processing.
Preferably; Potassium chloride concentration on-line measuring device (not shown) is installed in Crystallization Separation device 6; Under the control of master control system PLC; When the concentration of Repone K reaches the saturation concentration of Repone K in the concentrating liquid in detecting Crystallization Separation device 6, the sodium-chlor crystalline concentrating liquid that contains in the Crystallization Separation device 6 is introduced sodium salt whizzer 10 through cooling reaction still 8 backs; The concentration of the Repone K in the concentrating liquid in detecting Crystallization Separation device 6 is during less than the saturation concentration of Repone K, Crystallization Separation device 6 contained sodium-chlor crystalline concentrating liquid return in the pump feed evaporator 5 and proceed forced evaporation.
In addition; Can also adopt methyl alcohol, ether, acetone, terepthaloyl moietie, USP Kosher, formaldehyde, acetaldehyde, formic acid or acetate etc. except that ethanol as organic solvent; At this moment; Ethanol storage tank 18 is substituted by corresponding organic solvent storage tank, and is used for rectification and purification alcoholic acid equipment, comprises no longer needs of 17 of rectifying well heaters 14, ethanol rectifying tower 15, ethanol water cooler 16, mother liquor return tank.The material liquid outlet end that is the organic solution storage tank is connected through the feed liquid pipeline with the feed liquid inlet end of sylvite slurry tank 13.
Under normal pressure, 101 ℃ down the pretreated trade effluents of evaporation (mass concentration is 3% sodium-chlor and Repone K mixing solutions; Wherein the mass ratio of sodium-chlor and Repone K is 7: 3); The saturation concentration that obtains sodium-chlor in this system is 25.6%, and the saturation concentration of Repone K is 31.4%.
Is example with above-mentioned trade effluent as stoste, and the working process of the energy-efficient vapo(u)rization system of MVR is following in the present embodiment:
The energy-efficient vaporizer of MVR is set to normal pressure; The vaporization temperature of falling-film evaporator is set to 100 ℃ or 101 ℃; Stoste (pretreated trade effluent; Mass concentration is 3% sodium-chlor and Repone K mixing solutions; Wherein the mass ratio of sodium-chlor and Repone K is 7: 3) at first the feed liquid inlet end 1-1 through first plate type preheater be introduced in first plate type preheater 1 and carry out preheating; Be that stoste and water of condensation carry out heat exchange in first plate type preheater 1, the water of condensation after the heat exchange is discharged the energy-efficient vaporizer of MVR from condensation-water drain end 1-4, and the feed liquid inlet end 2-1 of the material liquid outlet end 1-2 of the stoste after the heat exchange through first plate type preheater 1, feed liquid pipeline, second plate type preheater 2 gets into second plate type preheater 2.Stoste and the non-condensable gas (being produced by the shell of the shell of falling-film evaporator and pump feed evaporator) that get into second plate type preheater 2 carry out heat exchange; Stoste is reached near vaporization temperature; And with the first feed liquid inlet end 3-1 entering falling-film evaporator 3 of this part stoste through material liquid outlet end 2-2, feed liquid pipeline, falling-film evaporator 3, the non-condensable gas after the heat exchange enters the waste gas tower.
Stoste after the intensification is transported to one of falling-film evaporator 3 and imitates bottom cavity, imitates recycle pump by one again and is delivered to an effect top through liquid distributor cloth liquid, evenly gets into the tube side that one of falling-film evaporator 3 is imitated, and carries out heat exchange with compressed secondary steam, makes its evaporation.In the heat transfer process that imitates, can produce water of condensation at shell side; It is remained in the bottom cavity of an effect by spissated liquid; Flow automatically to afterwards in two effects, imitate the two effect continuation evaporation concentration that recycle pumps are delivered to falling-film evaporator 3 by two again, in like manner; In the heat transfer process that two imitate, can produce water of condensation at shell side, the gas that obtains through concentrating liquid after concentrating and evaporation separates from flowing in the falling film separator 4 through material liquid outlet end 3-2, feed liquid pipeline, feed liquid inlet end 4-1; Through two-effect evaporation, the water of condensation that obtains gets into condensation water pot 19 through condensation-water drain end 3-4, condensing water conduit, the first condensing water inlet end 19-1.
Falling film separator 4 gets into steam in the centrifugal vapour compressor 7 through vapour outlet end 4-3, gas pipeline, steam-in end 7-1; The sodium chloride concentration on-line measuring device is installed in the falling film separator 4; Be used to detect the concentration of sodium-chlor; When the concentration of the sodium-chlor in the detected concentrating liquid reaches 24-25%, during promptly near saturation concentration, concentrating liquid is introduced Crystallization Separation device 6 through the first material liquid outlet end 4-2, feed liquid pipeline, the first feed liquid inlet end 6-1; When the concentration of the sodium-chlor in the detected concentrating liquid less than 24% the time, the second feed liquid inlet end of the second material liquid outlet end of concentrating liquid through falling film separator, feed liquid pipeline, falling-film evaporator is returned falling-film evaporator 3 carries out evaporation concentration again and handle.
The potassium chloride concentration on-line measuring device is installed in the Crystallization Separation device 6; The concentrating liquid that is introduced into Crystallization Separation device 6 continues evaporation concentration between Crystallization Separation device 6 and pump feed evaporator 5; The concentration that detects the intravital Repone K of liquid concentrator when the potassium chloride concentration on-line measuring device of installing in the Crystallization Separation device 6 is less than 31.4% the time; Concentrating liquid returns pump feed evaporator 5 and proceeds forced evaporation; The water of condensation that obtains is introduced in the condensation water pot 19 through condensation-water drain end 5-3, condensing water conduit, the second condensing water inlet end 19-2; When the concentration of the intravital Repone K of liquid concentrator reaches 31.4%, will have the feed liquid inlet end 8-1 of sodium-chlor crystalline concentrating liquid through the second material liquid outlet end 6-4, feed liquid pipeline, cooling reaction still 8 and get in the cooling reaction still 8.
Because sodium-chlor belongs to thermal crystalline; Have sodium-chlor crystalline concentrating liquid and cushion (in order to lower the temperature, to cool off) through cooling reaction still 8; After its temperature is reduced to about 95 ℃; It is 4 cubical enamel reaction stills that the cooling reaction still can adopt volume, and its top is provided with whisking appliance (in order to quicken cooling), and the feed liquid inlet end 10-1 of the material liquid outlet end 8-2 of the feed liquid after cushioning through cooling reaction still 8, feed liquid pipeline, sodium salt whizzer 10 gets into sodium salt whizzer 10.
The feed liquid that gets into sodium salt whizzer 10 is dried separation; Sodium chloride crystal is wherein discharged from crystal exit end 10-3; Liquid portion wherein is a saturated potassium chloride solution, through the feed liquid inlet end 12-1 entering liquid concentrator buffer tank 12 of material liquid outlet end 10-2, feed liquid pipeline, liquid concentrator buffer tank 12.The feed liquid inlet end 9-1 of the material liquid outlet end 12-2 of saturated potassium chloride solution through liquid concentrator buffer tank 12, feed liquid pipeline, deep cooler 9 gets into deep cooler 9.Saturated potassium chloride solution carries out degree of depth cooling in deep cooler 9, be cooled to 30 ℃ after, the feed liquid inlet end 13-1 through material liquid outlet end 9-2, feed liquid pipeline, sylvite slurry tank 13 gets in the sylvite slurry tank 13.
Also from ethanol storage tank 18, introduce the absolute ethyl alcohol of certain agent water ratio in the sylvite slurry tank 13; There are a large amount of crystal to separate out in the sylvite slurry tank 13 of this moment, will have the feed liquid inlet end 11-1 introducing sylvite whizzer 11 that this part feed liquid of crystalline is passed through the material liquid outlet end 13-2 of sylvite slurry tank 13, feed liquid pipeline, sylvite whizzer 11.The feed liquid that gets into sylvite whizzer 11 is dried separation; Potassium chloride is wherein discharged from crystal exit end 11-3, and the feed liquid inlet end 14-1 of the material liquid outlet end 11-2 of liquid portion wherein through sylvite whizzer 11, feed liquid pipeline, rectifying preheater 14 gets into rectifying tower preheater 14.
The liquid that gets into rectifying tower preheater 14 is by preheating; Its temperature is reached about 75 ℃, and the second condensing water inlet end 19-2 of the condensation-water drain end 14-3 of the water of condensation that produces in the warm through rectifying preheater 14, condensing water conduit, condensation water pot 19 gets in the condensation water pot 19; The feed liquid inlet end 15-1 of the material liquid outlet end 14-2 of the liquid after the preheating through rectifying preheater 14, feed liquid pipeline, ethanol rectifying tower 15 so therefrom on the upper side position get into ethanol rectifying tower 15; Steam contacts with the liquid countercurrent of decline; Lower boiling ethanol is met steam and is constantly evaporated; The liquid that descends gets into mother liquor return tank 17 from the mother liquor inlet end 17-1 of the mother liquor exit end 15-4 of ethanol rectifying tower 15, feed liquid pipeline, mother liquor return tank 17, and the mother liquor inlet end 15-2 of the liquid in the mother liquor return tank 17 through the first mother liquor exit end 17-2, feed liquid pipeline, ethanol rectifying tower 15 returns ethanol rectifying tower 15 and carry out the round-robin distillation operation; When ethanol during near the cat head of ethanol rectifying tower 15 its concentration the highest, and get into ethanol water cooler 16-2 through the ethanol inlet end 16-1 of ethanol exit end 15-3, feed liquid pipeline, ethanol water cooler 16.Ethanol cools off in ethanol water cooler 16-2, gets into ethanol storage tank 18 with the ethanol inlet end 18-1 of the ethanol that obtains purifying and the ethanol exit end 16-2 through ethanol water cooler 16, feed liquid pipeline, ethanol storage tank 18.Sodium-chlor in the mother liquor return tank 17 and Repone K mixed solution turn back in the pump feed evaporator 5 through the second mother liquor exit end 17-3 discharge of mother liquor return tank 17, participate in evaporation concentration again.
In said process; The steam that falling film separator 4 produces gets into centrifugal vapour compressor 7 through vapour outlet end 4-3; The steam that Crystallization Separation device 6 produces gets into centrifugal vapour compressor 7 through vapour outlet end 6-5; The heat content of the secondary steam after centrifugal vapour compressor 7 compressions of process can satisfy the heat exchange balance of this vapo(u)rization system, comprises that offering falling-film evaporator 3 carries out heat exchange with pump feed evaporator 5.
In said process, the water of condensation that falling-film evaporator 3, pump feed evaporator 5 and rectifying preheater 14 produce all is introduced in the condensation water pot 19, and the water of condensation in the condensation water pot 19 is used for the heat exchange of first plate type preheater 1.
The material liquid outlet end 11-2 of sylvite whizzer can directly not link to each other with the feed liquid inlet end 14-1 of rectifying tower preheater 14; But the material liquid outlet end 11-2 of sylvite whizzer links to each other with sylvite slurry tank 13; Feed liquid is transfused to entering sylvite slurry tank 13; After ethanol adds sylvite slurry tank 13, the solution left standstill layering, supernatant liquid gets into rectifying tower preheater 14 through the feed liquid inlet end 14-1 of rectifying tower preheater 14; In this process, sylvite slurry tank 13 has played the effect of flow velocity of the feed liquid of stable entering rectifying tower preheater 14.
Ethanol in the above-mentioned ethanol storage tank 18 comprises that ethanol is reclaimed in the rectifying of a part and ethanol is added in a part of outside.
The agent water ratio of the absolute ethyl alcohol of above-mentioned interpolation is 30-70%, and 50% o'clock best results wherein the reasons are as follows:
Tested for 1 (not adding the alcoholic acid situation)
Adopt pretreated trade effluent (mass concentration is 3% sodium-chlor and Repone K mixing solutions, and wherein the mass ratio of sodium-chlor and Repone K is 7: 3) 3L, under 101 ℃, it is carried out evaporation concentration; When evaporated water was 2.914L, Repone K reached capacity, at this moment; Separate the sodium-chlor crystallization 41g that separates out; And the concentrating liquid that obtains is 86ml, wherein contains Repone K 27g, sodium chloride-containing 22g.
With the concentrating liquid that obtains is that the saturated solution cooling of Repone K is cooled to 30 ℃, leaves standstill for some time, has crystal to separate out, isolation of crystalline, and crystal is 3.187g, and wherein sodium-chlor is 0.347g, and Repone K is 2.84g.
Test 2 (agent water is than the situation that are 30%)
Adopt pretreated trade effluent (mass concentration is 3% sodium-chlor and Repone K mixing solutions, and wherein the mass ratio of sodium-chlor and Repone K is 7: 3) 3L, under 101 ℃, it is carried out evaporation concentration; When evaporated water was 2.914L, Repone K reached capacity, at this moment; Separate the sodium-chlor crystallization 41g that separates out; And the concentrating liquid that obtains is 86ml, wherein contains Repone K 27g, sodium chloride-containing 22g.
With the concentrating liquid that obtains is that the saturated solution cooling of Repone K is cooled to 30 ℃; Add absolute ethyl alcohol 14ml; (agent water is than W=30%, and agent water is than the mass ratio for the water in the quality of absolute ethyl alcohol and the concentrating liquid), preferably; The useable glass rod stirs mixing solutions, plays the blended effect that helps.Under 30 ℃, leave standstill for some time, there is crystal to separate out, isolation of crystalline, crystal is 11.01g, and wherein sodium-chlor is 1.00g, and Repone K is 10.01g.
Test 3 (agent water is than the situation that are 50%)
Adopt pretreated trade effluent (mass concentration is 3% sodium-chlor and Repone K mixing solutions, and wherein the mass ratio of sodium-chlor and Repone K is 7: 3) 3L, under 101 ℃, it is carried out evaporation concentration; When evaporated water was 2.914L, Repone K reached capacity, at this moment; Separate the sodium-chlor crystallization 41g that separates out; And the concentrating liquid that obtains is 86ml, wherein contains Repone K 27g, sodium chloride-containing 22g.
With the concentrating liquid that obtains is that the saturated solution cooling of Repone K is cooled to 30 ℃, adds absolute ethyl alcohol 23ml, (agent water is than W=50%), preferably, the useable glass rod stirs mixing solutions, plays the blended effect that helps.Under 30 ℃, leave standstill for some time, there is crystal to separate out, isolation of crystalline, crystal is 19.91g, and wherein sodium-chlor is 1.80g, and Repone K is 18.11g.
Test 4 (agent water is than the situation that are 70%)
Adopt pretreated trade effluent (mass concentration is 3% sodium-chlor and Repone K mixing solutions, and wherein the mass ratio of sodium-chlor and Repone K is 7: 3) 3L, under 101 ℃, it is carried out evaporation concentration; When evaporated water was 2.914L, Repone K reached capacity, at this moment; Separate the sodium-chlor crystallization 41g that separates out; The concentrating liquid that obtains is 86ml, wherein contains Repone K 27g, sodium chloride-containing 22g.
With the concentrating liquid that obtains is that the saturated solution cooling of Repone K is cooled to 30 ℃, adds absolute ethyl alcohol 33ml, (agent water is than W=70%), preferably, the useable glass rod stirs mixing solutions, plays the blended effect that helps.Under 30 ℃, leave standstill for some time, there is crystal to separate out, isolation of crystalline, crystal is 17.50g, and wherein sodium-chlor is 1.58g, and Repone K is 15.92g.
To test 2-4 and compare, can find with test 1:
Test 1, when not adding ethanol, the amount of separating out of Repone K is 2.84g, accounts for 10.5% of Repone K total amount 27g.Also have a large amount of Repone K still to stay in the solution.
Test 3 has improved the alcoholic acid add-on on the basis of test 2, agent water ratio brings up to 50%, and this moment, the amount of separating out of Repone K reached 18.11g, accounted for 67.1% of Repone K total amount 27g.It is thus clear that the amount of separating out of Repone K has been 6 times of the amount of separating out of the Repone K among the embodiment 1 among the embodiment 3.
Test 4 has further improved the alcoholic acid add-on on the basis of test 3, agent water ratio has brought up to 70%, and this moment, the amount of separating out of Repone K was 15.92g, accounted for 58.9% of Repone K total amount 27g.It is thus clear that though further improved agent water ratio, the amount of separating out of Repone K slightly falls after rise than the amount of separating out of the Repone K among the embodiment 3.
To sum up, be 50% o'clock at agent water ratio, the amount of separating out of Repone K reaches peak value, and further behind the rising agent water ratio, the amount of separating out of Repone K slightly falls after rise.
Claims (10)
1. energy-efficient vapo(u)rization system of MVR; It is characterized in that; Said vapo(u)rization system includes preheater, falling-film evaporator, falling film separator, pump feed evaporator, Crystallization Separation device, cooling reaction still, sodium salt whizzer, deep cooler, sylvite slurry tank, organic solution storage tank, sylvite whizzer and centrifugal vapour compressor; Wherein stoste gets into from the feed liquid inlet end of said preheater; The material liquid outlet end of said preheater is connected through the feed liquid pipeline with the first feed liquid inlet end of falling-film evaporator; The material liquid outlet end of said falling-film evaporator is connected through the feed liquid pipeline with the feed liquid inlet end of falling film separator; The first material liquid outlet end of said falling film separator is connected through the feed liquid pipeline with the first feed liquid inlet end of Crystallization Separation device; The second material liquid outlet end of said falling film separator is connected through the feed liquid pipeline with the second feed liquid inlet end of falling-film evaporator; The first material liquid outlet end of said Crystallization Separation device is connected through the feed liquid pipeline with the feed liquid inlet end of pump feed evaporator; The material liquid outlet end of said pump feed evaporator is connected through the feed liquid pipeline with the second feed liquid inlet end of Crystallization Separation device; The second material liquid outlet end of said Crystallization Separation device is connected through the feed liquid pipeline with the feed liquid inlet end of cooling reaction still; The material liquid outlet end of said cooling reaction still and the feed liquid inlet end of sodium salt whizzer are connected through the feed liquid pipeline with the feed liquid inlet end of deep cooler through the be connected material liquid outlet end of said sodium salt whizzer of feed liquid pipeline; Said sodium salt whizzer also comprises the crystal exit end, and the material liquid outlet end of said deep cooler is connected through the feed liquid pipeline with the feed liquid inlet end of said sylvite slurry tank, and the material liquid outlet end of said sylvite slurry tank is connected with the feed liquid inlet end of sylvite whizzer; Said sylvite whizzer includes crystal exit end and material liquid outlet end; The material liquid outlet end of said organic solvent storage tank is connected through the feed liquid pipeline with the feed liquid inlet end of said sylvite slurry tank, and the vapour outlet end of said falling film separator is connected through gas pipeline with the steam-in end of centrifugal steam compressor, and the vapour outlet end of said Crystallization Separation device is connected through gas pipeline with the steam-in end of centrifugal vapour compressor; The secondary steam exit end of centrifugal vapour compressor is that said falling-film evaporator and pump feed evaporator provide secondary steam through gas pipeline, store in the said organic solvent storage tank can with the codissolved organic solvent of water.
2. the energy-efficient vapo(u)rization system of MVR according to claim 1; It is characterized in that; The secondary steam exit end of said centrifugal vapour compressor is connected through gas pipeline with the secondary steam inlet end of falling-film evaporator, and the secondary steam inlet end of said pump feed evaporator is connected with the gas pipeline of the secondary steam inlet end of falling-film evaporator with the secondary steam exit end that is communicated with said centrifugal vapour compressor through gas pipeline.
3. the energy-efficient vapo(u)rization system of MVR according to claim 1; It is characterized in that; Said preheater includes first plate type preheater and second plate type preheater; Said stoste gets into through the feed liquid inlet end of first plate type preheater, and the material liquid outlet end of said first plate type preheater is connected through the feed liquid pipeline with the feed liquid inlet end of second plate type preheater, and the material liquid outlet end of said second plate type preheater is connected through the feed liquid pipeline with the first feed liquid inlet end of falling-film evaporator.
4. the energy-efficient vapo(u)rization system of MVR according to claim 3; It is characterized in that; Said vapo(u)rization system also includes the condensation water pot; The condensation-water drain end of said falling-film evaporator and said pump feed evaporator is connected through condensing water conduit with the condensing water inlet end of condensation water pot respectively; It is the water of condensation that first plate type preheater is provided for heat exchange that the condensation-water drain end of said condensation water pot is connected with the condensing water inlet end of first plate type preheater through condensing water conduit, and the non-condensable gas of the generation that the shell of the falling-film evaporator in the said vapo(u)rization system and the shell of pump feed evaporator produce is transported to second plate type preheater and is used for and the stoste heat exchange.
5. the energy-efficient vapo(u)rization system of MVR according to claim 1 is characterized in that, the sodium chloride concentration on-line measuring device that is used to detect sodium chloride concentration is installed in the said falling film separator.
6. the energy-efficient vapo(u)rization system of MVR according to claim 1 is characterized in that, the potassium chloride concentration on-line measuring device that is used to detect potassium chloride concentration is installed in the said Crystallization Separation device.
7. the energy-efficient vapo(u)rization system of MVR according to claim 1; It is characterized in that; Also include the liquid concentrator buffer tank; Said liquid concentrator buffer tank is between said sodium salt whizzer and deep cooler, and the material liquid outlet end of sodium salt whizzer is connected through the feed liquid pipeline with the feed liquid inlet end of liquid concentrator buffer tank, and the material liquid outlet end of said liquid concentrator buffer tank is connected through the feed liquid pipeline with the feed liquid inlet end of deep cooler.
8. the energy-efficient vapo(u)rization system of MVR according to claim 1 is characterized in that, said organic solution storage tank is for being used to store the alcoholic acid ethanol storage tank.
9. the energy-efficient vapo(u)rization system of MVR according to claim 8; It is characterized in that; Also comprise ethanol rectification and purification device; The material liquid outlet end of sylvite whizzer is connected with the feed liquid inlet end that ethanol rectifying proposes device, and the ethanol exit end of ethanol rectification and purification device is connected with the ethanol inlet end of ethanol storage tank through the feed liquid pipeline, and the mother liquor exit end of ethanol rectification and purification device is connected with the feed liquid inlet end of mother liquor return tank through the feed liquid pipeline; And the material liquid outlet end of mother liquor return tank is connected with the feed liquid inlet end of pump feed evaporator through the feed liquid pipeline, and said mother liquor is a remaining feed liquid behind the separating alcohol.
10. according to the energy-efficient vapo(u)rization system of the described MVR of one of claim 1-9, it is characterized in that, also comprise master control system PLC.
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