CN203447794U - Multilevel concentration flash evaporation device - Google Patents
Multilevel concentration flash evaporation device Download PDFInfo
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- CN203447794U CN203447794U CN201320462931.4U CN201320462931U CN203447794U CN 203447794 U CN203447794 U CN 203447794U CN 201320462931 U CN201320462931 U CN 201320462931U CN 203447794 U CN203447794 U CN 203447794U
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Abstract
The utility model discloses a multilevel concentration flash evaporation device which comprises eight levels of preheaters, a heater, a pre-evaporator and night levels of evaporators, wherein the eight levels of preheaters are sequentially communicated with one another through a pipeline, the night levels of evaporators are sequentially communicated with one another through a pipeline, and the multilevel concentration flash evaporation device is characterized by also comprising three levels of flash evaporation tanks, the flash evaporation tanks are sequentially communicated with one another through a pipeline, and the preheaters, the heater, the pre-evaporator, the evaporators and the flash evaporation tanks are communicated with one another. By adopting the multilevel concentration flash evaporation device, condensed water after being separated from vapor through the flash evaporation tanks and heat of the condensed water of the preheaters A1 and A2 are adequately utilized, so that the consumption of the vapor and cooling water can be reduced, and the production cost of enterprises can be reduced.
Description
Technical field
The utility model relates to multistage flash distillation device, relates in particular to for the concentrated multistage concentrated flash distillation plant of viscose rayon acid bath.
Background technology
In viscose rayon production, for reducing, consume, solidify acid bath and recycle, in fiberizing process, can generate a water, after acid bath evaporation need to being concentrated, just can recycle.What at present most producer all adopted is multi-effect flashing steam device.
Granted publication number is CN201930554U, Granted publication day is that the Chinese utility model patent on August 17th, 2011 discloses a kind of multistage body lotion flash evaporation device (as shown in Figure 1), it is characterized in that: comprise material main, steam main, graphite shell and tube body lotion preheater, graphite block hole-type body lotion heater, line with rubber preevaporator, line with rubber multi-stage evaporator, line with rubber mixing condenser, stainless steel recoler, alloy steam jet pump, plastics circulating pump and vavuum pump, described graphite shell and tube body lotion preheater comprises 5 ~ 8 grades, described line with rubber multi-stage evaporator comprises 4 ~ 9 grades of line with rubber evaporimeters, and this line with rubber multi-stage evaporator comprises heat-recovery section line with rubber evaporimeter and heat extraction section line with rubber evaporimeter, described material main, heat extraction section line with rubber evaporimeter, plastics circulating pump, graphite shell and tube body lotion pre-heater, graphite block hole-type body lotion heater, line with rubber preevaporator, heat-recovery section line with rubber evaporimeter and inspissation bath are linked in sequence by pipeline, the thermal source pipeline of described graphite shell and tube body lotion preheater is connected with the flash distillation indirect steam conveyance conduit of line with rubber preevaporator and heat-recovery section line with rubber evaporimeter, the thermal source pipeline of described graphite block hole-type body lotion heater is connected with steam main, in addition, the indirect steam conveyance conduit of described heat extraction section line with rubber evaporimeter is connected with mixing condenser, stainless steel recoler by connecting pipe successively, and steam main is connected with alloy steam jet pump, stainless steel recoler, vavuum pump by pipeline successively, and the cooling water conveyance conduit of mixing condenser and stainless steel recoler is connected with rhone.The a large amount of steam of this utility model saving and cooling water, and reduced acid cooling wastewater discharge capacity, reducing environmental pollution, energy-conserving and environment-protective, benefit popularization.
From heater H and the clean condensed water flowing out A0, import respectively that in a flash tank, to carry out carbonated drink separated, vapour enters in preheater A2, and condensed water flows in receiving slit and discharges.This method is mainly to utilize the vacuum of A2 higher than the vacuum of heat exchanger, just can make the condensing water vapor in flash tank, and flash tank and each pre-heater condensed water discharge after accumulator tank.But the condensed water after the separation of flash tank carbonated drink and the condensed water of A1 and A2 have certain temperature, fail to make full use of the heat of vaporization of this partial condensation water.Be unfavorable for the reduction of steam-water ratio, wasted more steam and cooling water, increased the production cost of enterprise.
Utility model content
In order to overcome that above-mentioned multistage body lotion flash evaporation device is underused the condensed water of condensed water after the separation of flash tank carbonated drink and preheater A1 and preheater A2 and the steam that causes and the waste of cooling water, and the defect of enterprise's production cost increase, the utility model provides a kind of multistage flash distillation device, this multistage flash distillation device, take full advantage of the heat of the condensed water of condensed water after the separation of flash tank carbonated drink and A1 and A2, thereby reduced the use amount of steam and cooling water, and then reduced the production cost of enterprise.
In order to solve the problems of the technologies described above, the technical solution adopted in the utility model is:
A kind of multistage concentrated flash distillation plant, comprise preheater, heater, preevaporator and multi-stage evaporator, described preheater, heater, preevaporator and multi-stage evaporator are interconnected by pipeline, it is characterized in that: also comprise flash tank, this flash tank is 3 grades of flash tanks, and by pipeline order, be communicated with, described preheater, heater, preevaporator, multi-stage evaporator and flash tank are interconnected.
Described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 totally 3 grades of flash tanks, and described H and A0 are connected with ES by pipeline, and described V2 and ES are connected with A2 by pipeline, described ES1 and V6 are connected with A6 by pipeline, and described ES2 and V8 are connected with A8 by pipeline.
Described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 totally 3 grades of flash tanks, described H and A0 are connected with ES by pipeline, described V2 and ES are connected with A2 by pipeline, described A1 and A2 are all connected with ES1, described ES1 is connected by pipeline and A6 with V6, and described ES2 and V8 are connected with A8 by pipeline.
Described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 be totally 3 grades of flash tanks, described H and A0 are connected with ES by pipeline, described V2 and ES are connected with A2 by pipeline, described A1 and A2 are connected with feeder by pipeline, described feeder is connected with ES1 by pipeline, and on the pipeline between feeder and ES1, heat-exchanger pump is installed, described ES1 is connected by pipeline and A6 with V6, described ES2 and V8 are connected with A8 by pipeline.
The utlity model has following advantage:
1, this utility model is by having increased by 3 grades of flash tanks, take full advantage of heater H and A0, preheater A1 and A2 steam-condensation backwater, it heats again to A2, A6 and A8, recycled steam-condensation backwater, save resource, reduced steam-water ratio to 0.26～0.28:1, reduce the use amount of steam-condensation backwater, thereby reduced the production cost of enterprise.
2, the steam-condensation backwater in heater (H and A0), by steam trap and 90 ℃ of left and right of flash tank ES water temperature, part steam condensate (SC) carries out part vaporization again, due to its pressure with result from evaporimeter V
2steam pressure in level conforms to, and is used for jointly to passing through A
2acid bath in (or pressure conform to pre-heater) is heated; 70 ℃ of left and right of steam condensate (SC) water temperature that all the other can not vaporize in flash tank ES, enter in flash tank ES1 part vaporization by pipeline, because of its pressure with result from evaporimeter V
6steam pressure conform to for jointly to passing through A
6acid bath heating in (or pressure conform to pre-heater).And do not have the part of vaporization again by pipeline, to enter in flash tank ES2, its pressure with result from evaporimeter V
8a is passed through in the steam pressure of (or pressure conform to pre-heater) the common heating that conforms to
8acid bath all the other do not have vaporization steam condensate (SC) fall into condenser accumulator tank to be used as him.By the steam-water ratio of multiple-effect being reduced to 0.26～0.28:1 after this device.
3, the steam-condensation backwater in heater (H and A0), by steam trap and 90 ℃ of left and right of flash tank ES water temperature, part steam condensate (SC) carries out part vaporization again, due to its pressure with result from evaporimeter V
2steam pressure in level conforms to, and is used for jointly to passing through A
2acid bath in (or pressure conform to pre-heater) is heated; 70 ℃ of left and right of steam condensate (SC) water temperature and pre-heater A that all the other can not vaporize in flash tank ES
1, A
2stram condenser backwater by pipeline, enter in flash tank ES1 part vaporization together, because of its pressure with result from evaporimeter V
6steam pressure conform to for jointly to passing through A
6acid bath heating in (or pressure conform to pre-heater).And do not have the part of vaporization again by pipeline, to enter in flash tank ES2, its pressure with result from evaporimeter V
8steam pressure conform to and A is passed through in common heating
8the acid bath of (or pressure conform to pre-heater), all the other do not have the steam condensate (SC) of vaporization to fall into condensed water accumulator tank to be used as him.By the steam-water ratio of multiple-effect being reduced to 0.26～0.28:1 after this device.
4, the steam-condensation backwater in heater (H and A0), by steam trap and 90 ℃ of left and right of flash tank ES condensed water temperature, part steam condensate (SC) carries out part vaporization again, due to its with result from evaporimeter V
2steam pressure in level conforms to, and is used for jointly to passing through A
2acid bath in (or pressure conform to pre-heater) is heated; 70 ℃ of left and right of steam condensate (SC) water temperature that all the other can not vaporize in flash tank ES fall into feeder.And pre-heater A
1, A
2stram condenser backwater also fall into above-mentioned feeder, by overheated water pump, squeeze in flash tank ES1, the steam condensate (SC) of 70 ℃ carries out part vaporization again, because of its pressure with result from evaporimeter V
6steam pressure conform to for jointly to passing through A
6acid bath heating in (or pressure conform to pre-heater).And do not have the part of vaporization again by pipeline, to enter in flash tank ES2, its pressure with result from evaporimeter V
8the steam pressure common heating that conforms to pass through A
8the acid bath of (or pressure conform to pre-heater), all the other do not have the steam condensate (SC) of vaporization to fall into condensed water accumulator tank to be used as him.By the steam-water ratio of multiple-effect being reduced to 0.26～0.28:1 after this device.
Accompanying drawing explanation
Fig. 1 is flash distillation plant process chart of the prior art;
Fig. 2 is the flash distillation plant process chart of embodiment 1;
Fig. 3 is the flash distillation plant process chart of embodiment 2;
Fig. 4 is the flash distillation plant process chart of embodiment 3.
Wherein: heater: H, A0; Preheater: A1～A8; Multi-stage evaporator: V3～V11; Preevaporator: V1, V2; Condenser: MK1, MK2; Recoler: HK; Circulating pump: UP; Vavuum pump: VP; Condensed water elimination groove: F2, F3, F5; Enrichment bath: F4; Flash tank: ES, ES1, ES2.
The specific embodiment
Embodiment 1
As shown in Figure 2, multistage concentrated flash distillation plant, comprise preheater, heater, preevaporator, multi-stage evaporator, condenser, recoler, circulating pump and vavuum pump, condenser is MK1 and MK2 two-stage cooler, described preheater is 8 grades of preheaters, and be communicated with by pipeline order, described multi-stage evaporator is 9 grades of evaporimeters, and be communicated with by pipeline order, multi-stage evaporator comprises heat-recovery section evaporimeter and heat extraction section evaporimeter, also comprise flash tank, this flash tank is 3 grades of flash tanks, and be communicated with by pipeline order, described preheater, heater, preevaporator, multi-stage evaporator and flash tank are interconnected.
Described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 totally 3 grades of flash tanks, and described H and A0 are connected with ES by pipeline, and described V2 and ES are connected with A2 by pipeline, described ES1 and V6 are connected with A6 by pipeline, and described ES2 and V8 are connected with A8 by pipeline.
Acid bath is after heat extraction section evaporimeter is processed, in the effect of circulating pump UP, once input preheater and heater H, after A0 heating, by pipeline, input preevaporator V1 again, V2, and heat-recovery section evaporimeter is to carry out flash distillation processing, finally input enrichment bath F4, the thermal source of described preheater is from the indirect steam of preevaporator and the flash distillation of heat-recovery section evaporimeter, the thermal source of described heater is inputted from steam main, in addition, the indirect steam that heat extraction section evaporimeter produces is by condenser MK1, MK2 processes, the incoagulable gas input recoler HK of condenser output carries out condensation process, the incoagulable gas that recoler is discharged is discharged by vavuum pump, and the cooling water that condenser and recoler produce is inputted condensed water elimination groove F2 by pipeline, F3 and F5.
The acid bath liquid that acid bath liquid is processed through tow filter device at acid station, is introduced in acid bath suction tank, under the condition of vacuum, enters the V10 section of horizontal multi-effect evaporator.The temperature reduction technology of acid bath liquid process V10, V11, U-shaped pipeline communication V11 section for V10.When acid bath liquid temp is reduced to 46 ℃ and V11 section to 40 ℃ by 50 ℃ of segmentations in V10 section, acid bath liquid again by the acid tube that falls of V11 by acid bath circulating pump, by circulating pump successively by be controlled at≤90m3/h of pre-heater A8(internal circulating load), A7, A6, A5, A4, A3, A2, A1, in pre-heater, acid bath liquid is heated to respectively 46 ℃, 52 ℃, 58 ℃, 64 ℃, 71 ℃, 77 ℃, 83 ℃, 89 ℃ through indirect steam, acid bath liquid is warming up to 89 ℃ and passes through successively heater A0 and H again, in A0 and H, is warming up to 97 ℃ and 105 ℃ ~ 107 ℃ respectively by Steam Heating.Acid bath liquid is warming up to 105 ℃ ~ 107 ℃, completes acid bath liquid temp and increases technique.Respectively by the vertical evaporator V1 of two-stage, V2, acid bath liquid temp is down to 96 ℃ again, completes prevapourising operation.
Acid bath liquid multiple-effect evaporation technique: the acid bath liquid through acid bath liquid temp adjusting process, by jet pipe, with droplet form, spray, utilize nozzle hole umbrella hood to enter each section of evaporator unit by acid bath liquid is dispersed.The V3(90 ℃ of horizontal-type evaporator, vacuum 0.098MPa), V4(83 ℃), V5(77 ℃), V6(71 ℃), V7(65 ℃), V8(58 ℃), V9(50 ℃), through obtaining temperature 50 ℃ ~ 54 ℃ concentrated acid baths after flash evaporation step by step, by the acid tube that falls of V9, entered in concentrated acid tank.
The produced indirect steams at different levels pre-heater of corresponding same sequence respectively in flash tank, V9 and the V10 supercooled water that is connected with condenser MK2 is discharged indirect steam, and V11 is connected with condenser MK1 indirect steam is discharged after by condensation.The condensed water that pre-heaters at different levels produce enters F5 for using it for anything else by downpipe.The condensed water that heater produces is because temperature is relatively high, and the flash evaporation by again forms indirect steam and is sent to A2 pre-heater.
Steam-condensation backwater in heater (H and A0), by steam trap and 90 ℃ of left and right of flash tank ES water temperature, part steam condensate (SC) carries out part vaporization again, due to its pressure with result from evaporimeter V
2steam pressure in level conforms to, and is used for jointly to passing through A
2acid bath in (or pressure conform to pre-heater) is heated; 70 ℃ of left and right of steam condensate (SC) water temperature and pre-heater A that all the other can not vaporize in flash tank ES
1, A
2stram condenser backwater by pipeline, enter in flash tank ES1 part vaporization together, because of its pressure with result from evaporimeter V
6steam pressure conform to for jointly to passing through A
6acid bath heating in (or pressure conform to pre-heater).And do not have the part of vaporization again by pipeline, to enter in flash tank ES2, its pressure with result from evaporimeter V
8steam pressure conform to and A is passed through in common heating
8the acid bath of (or pressure conform to pre-heater), all the other do not have the steam condensate (SC) of vaporization to fall into condensed water accumulator tank to be used as him.By the steam-water ratio of multiple-effect being reduced to 0.26～0.28:1 after this device.
As shown in Figure 3, multistage concentrated flash distillation plant, comprise preheater, heater, preevaporator, multi-stage evaporator, condenser, recoler, circulating pump and vavuum pump, condenser is MK1 and MK2 two-stage cooler, described preheater is 8 grades of preheaters, and be communicated with by pipeline order, described multi-stage evaporator is 9 grades of evaporimeters, and be communicated with by pipeline order, multi-stage evaporator comprises heat-recovery section evaporimeter and heat extraction section evaporimeter, also comprise flash tank, this flash tank is 3 grades of flash tanks, and be communicated with by pipeline order, described preheater, heater, preevaporator, multi-stage evaporator and flash tank are interconnected.
Described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 totally 3 grades of flash tanks, described H and A0 are connected with ES by pipeline, described V2 and ES are connected with A2 by pipeline, described A1 and A2 are all connected with ES1, described ES1 is connected by pipeline and A6 with V6, and described ES2 and V8 are connected with A8 by pipeline.
Steam-condensation backwater in heater (H and A0), by steam trap and 90 ℃ of left and right of flash tank ES water temperature, part steam condensate (SC) carries out part vaporization again, due to its pressure with result from evaporimeter V
2steam pressure in level conforms to, and is used for jointly to passing through A
2acid bath in (or pressure conform to pre-heater) is heated; 70 ℃ of left and right of steam condensate (SC) water temperature and pre-heater A that all the other can not vaporize in flash tank ES
1, A
2stram condenser backwater by pipeline, enter in flash tank ES1 part vaporization together, because of its pressure with result from evaporimeter V
6steam pressure conform to for jointly to passing through A
6acid bath heating in (or pressure conform to pre-heater).And do not have the part of vaporization again by pipeline, to enter in flash tank ES2, its pressure with result from evaporimeter V
8steam pressure conform to and A is passed through in common heating
8the acid bath of (or pressure conform to pre-heater), all the other do not have the steam condensate (SC) of vaporization to fall into condensed water accumulator tank to be used as him.By the steam-water ratio of multiple-effect being reduced to 0.26～0.28:1 after this device.
Embodiment 3
As shown in Figure 4, multistage concentrated flash distillation plant, comprise preheater, heater, preevaporator, multi-stage evaporator, condenser, recoler, circulating pump and vavuum pump, condenser is MK1 and MK2 two-stage cooler, described preheater is 8 grades of preheaters, and be communicated with by pipeline order, described multi-stage evaporator is 9 grades of evaporimeters, and be communicated with by pipeline order, multi-stage evaporator comprises heat-recovery section evaporimeter and heat extraction section evaporimeter, also comprise flash tank, this flash tank is 3 grades of flash tanks, and be communicated with by pipeline order, described preheater, heater, preevaporator, multi-stage evaporator and flash tank are interconnected.
Described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 be totally 3 grades of flash tanks, described H and A0 are connected with ES by pipeline, described V2 and ES are connected with A2 by pipeline, described A1 and A2 are connected with feeder by pipeline, described feeder is connected with ES1 by pipeline, and on the pipeline between feeder and ES1, heat-exchanger pump is installed, described ES1 is connected by pipeline and A6 with V6, described ES2 and V8 are connected with A8 by pipeline.
Steam-condensation backwater in heater (H and A0), by steam trap and 90 ℃ of left and right of flash tank ES condensed water temperature, part steam condensate (SC) carries out part vaporization again, due to its with result from evaporimeter V
2steam pressure in level conforms to, and is used for jointly to passing through A
2acid bath in (or pressure conform to pre-heater) is heated; 70 ℃ of left and right of steam condensate (SC) water temperature that all the other can not vaporize in flash tank ES fall into feeder.And pre-heater A
1, A
2stram condenser backwater also fall into above-mentioned feeder, by overheated water pump, squeeze in flash tank ES1, the steam condensate (SC) of 70 ℃ carries out part vaporization again, because of its pressure with result from evaporimeter V
6steam pressure conform to for jointly to passing through A
6acid bath heating in (or pressure conform to pre-heater).And do not have the part of vaporization again by pipeline, to enter in flash tank ES2, its pressure with result from evaporimeter V
8the steam pressure common heating that conforms to pass through A
8the acid bath of (or pressure conform to pre-heater), all the other do not have the steam condensate (SC) of vaporization to fall into condensed water accumulator tank to be used as him.By the steam-water ratio of multiple-effect being reduced to 0.26～0.28:1 after this device.
Claims (4)
1. a multistage concentrated flash distillation plant, comprise preheater, heater, preevaporator and multi-stage evaporator, described preheater, heater, preevaporator and multi-stage evaporator are interconnected by pipeline, it is characterized in that: also comprise flash tank, this flash tank is 3 grades of flash tanks, and by pipeline order, be communicated with, described preheater, heater, preevaporator, multi-stage evaporator and flash tank are interconnected.
2. a kind of multistage concentrated flash distillation plant according to claim 1, it is characterized in that: described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 totally 3 grades of flash tanks, described H and A0 are connected with ES by pipeline, described V2 and ES are connected with A2 by pipeline, described ES1 and V6 are connected with A6 by pipeline, and described ES2 and V8 are connected with A8 by pipeline.
3. a kind of multistage concentrated flash distillation plant according to claim 1, it is characterized in that: described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 be totally 3 grades of flash tanks, described H and A0 are connected with ES by pipeline, described V2 and ES are connected with A2 by pipeline, described A1 and A2 are all connected with ES1, described ES1 is connected by pipeline and A6 with V6, described ES2 and V8 are connected with A8 by pipeline.
4. a kind of multistage concentrated flash distillation plant according to claim 1, it is characterized in that: described preheater is A1～A8 totally 8 grades of preheaters, described multi-stage evaporator is V3～V11 totally 9 grades of evaporimeters, described heater is H and A0 totally 2 grades of heaters, described preevaporator is that V1 and V2 are total to two-stage preevaporator, described flash tank is ES, ES1 and ES2 be totally 3 grades of flash tanks, described H and A0 are connected with ES by pipeline, described V2 and ES are connected with A2 by pipeline, described A1 and A2 are connected with feeder by pipeline, described feeder is connected with ES1 by pipeline, and on the pipeline between feeder and ES1, heat-exchanger pump is installed, described ES1 is connected by pipeline and A6 with V6, described ES2 and V8 are connected with A8 by pipeline.
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| CN201320462931.4U CN203447794U (en) | 2013-07-31 | 2013-07-31 | Multilevel concentration flash evaporation device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108529707A (en) * | 2018-05-16 | 2018-09-14 | 南京常荣环境科技有限公司 | A kind of combination test apparatus and method using hot wind concentration-flash distillation process waste water |
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2013
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108529707A (en) * | 2018-05-16 | 2018-09-14 | 南京常荣环境科技有限公司 | A kind of combination test apparatus and method using hot wind concentration-flash distillation process waste water |
| CN108529707B (en) * | 2018-05-16 | 2023-12-12 | 南京常荣环境科技有限公司 | Combined test device and method for concentrating and flash-evaporating wastewater by using hot air |
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