CN1415395A - Technique of combined concentration by evaporation with heat pump being provided - Google Patents
Technique of combined concentration by evaporation with heat pump being provided Download PDFInfo
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- CN1415395A CN1415395A CN 02145295 CN02145295A CN1415395A CN 1415395 A CN1415395 A CN 1415395A CN 02145295 CN02145295 CN 02145295 CN 02145295 A CN02145295 A CN 02145295A CN 1415395 A CN1415395 A CN 1415395A
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Abstract
A combined evaporation concentrating technology with heat pump is composed of heat pump and evaporator sets A and B. The said evaporator set A has heat pump and said evaporator set B is a multi-effect one. The external steam is mixed with the secondary steam of the first-effect evaporator in A, then boosted, and finally used as the primary steam of the first-effect evaporators in A and B. The raw liquid is preheated and then passes through A and B. Its advantage is reducing energy by 20-60%.
Description
Technical field
The present invention relates to a kind of evaporating and concentrating process, particularly a kind of evaporating and concentrating process that has heat pump.
Background technology
The multiple-effect evaporation concentration technology is present industrial the most frequently used evaporating and concentrating process, the evaporation and concentration of electrolytic lye is mainly triple effect following current evaporating and concentrating process in for example domestic chlorine industry, see document [1] (" chloralkali process ", chief editors such as Fang Du, Beijing: Chemical Industry Press, 1990, record P286-345).But there is the following shortcoming in this technology, is perplexing the development of chlorine industry always.At first be that utilizing of the energy is unreasonable, because the saturation temperature difference of the first single-effect evaporator primary steam and indirect steam differs bigger, up to 33 ℃, can't be by the available energy that means such as heat pump the make full use of external source steam ability of promptly doing work, external source steam can only enter first single-effect evaporator as primary steam behind the pressure and temperature reducing, causes the meaningless loss of energy source efficiency; It is lower that next is that material liquid enters the temperature of first single-effect evaporator, be usually less than 35～40 ℃ of its boiling points, therefore first single-effect evaporator need more primary steam and heat transfer area be that preheating electrolytic lye to boiling point is worked, thereby reduced the evaporation efficiency of first single-effect evaporator, that is to say the evaporation capacity that has reduced by first single-effect evaporator.
Above-mentioned shortcoming in view of existing technology, make that the energy consumption of domestic chlorine industry evaporating concentration process is seriously higher, hindered the development of chlorine industry, therefore, branch of industry wishes that relevant engineers and technicians improve, provide a kind of advanced person's evaporating and concentrating process, to promote the technological progress of chlorine industry.
Summary of the invention
Purpose of the present invention: for overcoming the above-mentioned shortcoming of prior art, proposed a kind of combined evaporative concentration technology that has heat pump, it fully improves the effective utilization of the energy by rational process combination, and comparable prior art cuts down the consumption of energy more than 20%.
Design of the present invention is such: keeping basically under the constant situation of evaporimeter total heat conduction area, two groups of vaporising devices of A, B are set, wherein A group evaporimeter is a vaporising device that has heat pump, and B group evaporimeter is one group of multi-effect evaporating device.Heat pump is under the driving of external source steam, and the indirect steam that A group evaporimeter is come out is able to supercharging and with after external source steam fully mixes, and is re-used as that primary steam enters A group evaporimeter and B organizes first single-effect evaporator; Regulate the evaporation capacity of evaporimeter by the operating pressure of control A group evaporator evaporation chamber, improve the mass ratio of induced-to-inducing air of heat pump, thereby the acting ability of external source steam is fully used; The material liquid that enters A group evaporimeter organizes the part indirect steam of first single-effect evaporator with B respectively and condensed water that two group of first single-effect evaporator of A, B discharged carries out preheating, improving the feeding temperature of material liquid as much as possible, thereby give full play to the evaporation effect that A group evaporimeter and B organize first single-effect evaporator.Since A group evaporimeter and B organize first single-effect evaporator finished whole technical process total evaporation half in addition over half, B group second is imitated, the evaporation task of third effect evaporator is just low weight, heat transfer area during its design just can reduce relatively, thereby the total heat transfer area of evaporimeter can be effectively controlled.
The present invention is achieved like this: a kind of combined evaporative concentration technology that has heat pump, and it mainly is made up of heat pump and two groups of evaporimeters of A, B, and wherein A group evaporimeter is a vaporising device that has heat pump, and B group evaporimeter is one group of multi-effect evaporating device.The heat pump that is adopted is a class steam power mixed type heat pump, i.e. a kind of in steam jet pump, the disjunctor heat engine-heat pump.A is organized indirect steam common primary steam after heat pump mixing supercharging of first single-effect evaporator with external source steam as A, two groups of evaporimeters of B.From the Steam Heating angle, the compound mode of A group and B group is arranged side by side, but from the evaporating concentration process of feed liquid, the compound mode of A group and B group is connected, and feed liquid is organized evaporimeter from A and organized evaporimeter to B again.Material liquid adopts combined type preheating, and the part indirect steam of organizing first single-effect evaporator with B carries out preheating earlier, and the condensed water with A group and B group evaporimeter first effect carries out preheating again, makes material liquid be preheated to temperature and is lower than boiling point and is no more than 25 ℃ and enters evaporimeter again.Material liquid at first enters A and organizes first single-effect evaporator and concentrate after preheating, enter B group evaporimeter again and further concentrate.Control A organizes the evaporation capacity of first single-effect evaporator, the concentration of easy crystallized solute is remained be lower than its saturated concentration.Control A organizes the operating pressure of the first single-effect evaporator vaporization chamber, makes the saturation temperature of its corresponding indirect steam be higher than 3～18 ℃ of the saturation temperatures that B organizes the first single-effect evaporator indirect steam.According to being evaporated the difference that concentrates system and evaporation operating mode thereof, the pressure of external source steam is 1.0～4.5Mpa, and the mass ratio of induced-to-inducing air of heat pump is 0.4～3.0.
Description of drawings
Below in conjunction with accompanying drawing technology of the present invention is described.
Fig. 1 is a process flow diagram of the present invention: it has two groups of evaporimeters of A, B, wherein:
1-external source steam and import
2-heat pump
3-material liquid and import
3a, 3b-material liquid preheater
4-A organizes first single-effect evaporator
5-B organizes first single-effect evaporator
6-B organizes second single-effect evaporator
7-B organizes third effect evaporator
8-ejector vacuum pump or vavuum pump
Dotted line is a jet chimney among Fig. 1, and fine line is the steam condensate (SC) pipeline, and heavy line is the feed liquid pipeline.A is organized indirect steam common primary steam after heat pump (2) mixes supercharging of first single-effect evaporator (4) with external source steam (1) as A, two group of first single-effect evaporator of B.Material liquid (3) is respectively by preheater 3b, 3a, after being preheated to temperature and being lower than boiling point and being no more than 25 ℃, being introduced into A organizes first single-effect evaporator and carries out evaporation and concentration, and then enter B successively and organize that first single-effect evaporator (5), B are organized second single-effect evaporator (6), B organizes third effect evaporator (7), be concentrated to discharging after the concentration of technological requirement; The indirect steam that B organizes first single-effect evaporator is used to the preheating material liquid except that part enters preheater (3b), and major part enters B and organizes second single-effect evaporator as the evaporation thermal source; The indirect steam that B organizes second single-effect evaporator all enters B group third effect evaporator as the evaporation thermal source; The indirect steam of B group third effect evaporator is then drawn by ejector vacuum pump (8).
The specific embodiment
In the present invention's technology, material liquid at first enters A and organizes first single-effect evaporator and concentrate after preheating, organize the evaporation capacity of first single-effect evaporator by control A, the concentration of easy crystallized solute is remained be lower than its saturated concentration, just can take adequate measures to reduce temperature difference loss, as adopting the forced circulation type evaporimeter that can reduce temperature difference loss, downward film evaporator, plate-type evaporator, coil evaporator, evaporation equipments such as flash type evaporator, and control A organizes the operating pressure of the first single-effect evaporator vaporization chamber, make the saturation temperature of its corresponding indirect steam be higher than 3～18 ℃ of the saturation temperatures that B organizes the first single-effect evaporator indirect steam, organize the total temperature difference of first single-effect evaporator thereby significantly reduce A.The mass ratio of induced-to-inducing air of heat pump is along with the reduction of temperature difference before and after the supercharging, its speedup is more and more higher, just can make full use of the acting ability of external source steam, effectively improve the mass ratio of induced-to-inducing air of heat pump, according to being evaporated the difference that concentrates system and evaporation operating mode thereof, the pressure limit of utilizable external source steam is 1.0～4.5Mpa, and the mass ratio of induced-to-inducing air of heat pump can reach 0.4～3.0.Material liquid adopts combined type preheating: material liquid elder generation carries out preheating with the part indirect steam that B organizes first single-effect evaporator, the condensed water of organizing first single-effect evaporator with A group and B carries out preheating again, making material liquid be preheated to temperature is lower than boiling point and is no more than 25 ℃ and enters A group evaporimeter first again and imitate, just can increase the comprehensive utilization of indirect steam and condensed water heat energy, thereby effectively reduce the heat transfer area that evaporimeter is used for the preheating feed liquid, originally the part primary steam that was used for preheating material liquid simultaneously in the B group evaporimeter saves the evaporation and concentration that can be used for this evaporimeter, thereby further increases evaporation capacity.Though increased an A and organized first single-effect evaporator this moment, but because that A organizes the temperature of the first single-effect evaporator feed liquid is higher and concentration is lower, there is not crystallization to separate out again, its heat transfer coefficient can be higher, the band automatic flushing device etc. that can also adopt evaporimeter that can augmentation of heat transfer and can reduce dirtiness resistance further improves heat transfer coefficient, simultaneously, since A group and B organize first single-effect evaporator finished whole technical process total evaporation half in addition over half, B group second, the evaporation task of third effect evaporator is just low weight, heat transfer area during its design just can reduce relatively, the heat transfer area that whole evaporation operation is total thereby can be effectively controlled is consistent substantially with existing technology or slightly reduces.Except the evaporability of the effect that improves external source steam effectively and A, two group of first single-effect evaporator of B and reduce that B group second is imitated, the evaporation capacity of B group third effect evaporator, all the other technological processes and existing resemble process, B group evaporimeter still can evaporation operation routinely carry out, so the relevant factory of convenience is to the technological transformation of existing apparatus greatly, particularly to the capacity expansion revamping of existing apparatus.The present invention's technology makes last evaporator need the indirect steam amount of condensation greatly to reduce owing to more indirect steam can be recycled, and can also reduce the consumption of cooling water greatly, thereby has very considerable energy saving, water-saving result.
Further illustrate content of the present invention below in conjunction with embodiment.
Embodiment 1
Evaporation and concentration with the chlorine industry electrolytic lye is an example, adopt the present invention's technology, the A group is a single effect evaporator, the B group is one group of triple effect following current evaporimeter, the external source steam of 1.6Mpa is used as the working steam of steam jet pump, A group evaporimeter adopts the forced circulation type evaporimeter, the temperature of primary steam is 168 ℃, the operating pressure of controlling its vaporization chamber is 0.42Mpa, then the saturation temperature of corresponding indirect steam is 145 ℃ with it, the saturation temperature of organizing the first single-effect evaporator indirect steam than B is high 9 ℃, whole indirect steams of A being organized evaporimeter with external source steam after heat pump mixing supercharging jointly as A, the primary steam of two groups of evaporimeters of B, total temperature difference is 23 ℃ before and after the heat pump supercharging, and the mass ratio of induced-to-inducing air of heat pump is about 0.4, and the boiling point of electrolytic lye (abbreviation feed liquid) is 160 ℃.Material liquid (containing about NaOH:10%, NaCl:16%) adopts B to organize the condensed water preheating (in preheater 3a) of the part indirect steam preheating (in preheater 3b) of first single-effect evaporator and A, two group of first single-effect evaporator of B successively, after being preheating to material liquid about 140 ℃, being introduced into A group evaporimeter concentrates, enter B more successively and organize that first single-effect evaporator, B are organized second single-effect evaporator, B organizes third effect evaporator, be concentrated to discharging after the concentration of technological requirement, the operation of B group evaporimeter and temperature parameter are still kept the operating conditions in the document [1] substantially.The concentration of NaOH only is about 11% in the A group evaporimeter feed liquid, and the concentration of NaCl is about 18% only also, is lower than its saturated concentration of 20.5%.Because A group evaporimeter has adopted the forced circulation type evaporimeter, feed concentration is lower and temperature is higher, therefore the heat transfer coefficient of evaporimeter can be very high, and this moment B group evaporimeter since evaporation capacity reduce and need not preheating material liquid, the also comparable original obviously minimizing of the heat transfer area of B group evaporimeter, amount to one ton of 100%NaOH by the liquid caustic soda of per hour producing 42%, the steam consumption of existing technology is 3400kg, and the total heat transfer area of evaporimeter is 174M
2, and employing the present invention's technology, mass ratio of induced-to-inducing air is 0.4, and steam consumption is 2700kg, and the total heat transfer area of evaporimeter only is 172M
2The total heat transfer area of both evaporimeters is suitable substantially, simultaneously since in the A group evaporimeter concentration of feed liquid lower, the material of evaporimeter requires also not really high, the equipment manufacturing cost of a whole set of evaporimeter thereby there is no obvious increase, and the comparable existing energy saving technology of technology that adopts the present invention is more than 20%.
Attached: the main technologic parameters contrast (amounting to one ton of 100%NaOH) of existing technology and the present invention's technology by the liquid caustic soda of per hour producing 42%:
One, triple effect following current technology
Imitate several one and imitate two effect triple effects
Each imitates steam consumption, and kg 3400,2250, and 2230
Each imitates evaporation capacity, and kg 2250,2230, and 2028
The concentration (NaOH) that each is imitated, % 13,22, and 42
Effective heat transfer temperature difference that each is imitated, ℃ 18,12,13
The overall heat-transfer coefficient that each is imitated, kJ/ (m
2H ℃) 6700,7000,6700
Each imitates the latent heat of vaporization of steam, and kJ/kg 2060,2163, and 2248
The heat transfer area that each is imitated, M
258,58,58
Two, the present invention's technology
Imitate number A1 and imitate B1 effect B2 effect B3 effect
Each imitates steam consumption, and kg 1492,2288, and 1686,1670
Each imitates evaporation capacity, and kg 1080,2157, and 1670,1601
The concentration (NaOH) that each is imitated, % 11,16, and 25,42
Effective heat transfer temperature difference that each is imitated, ℃ 8,17,12,13
The overall heat-transfer coefficient that each is imitated, kJ/ (m
2H ℃) 9000,6700,7000,6700
Each imitates the latent heat of vaporization of steam, and kJ/kg 2060,2060, and 2157,2248
The heat transfer area that each is imitated, M
243,43,43,43
Embodiment 2
Evaporation and concentration with the calcium chloride solution that contains sodium chloride is an example, and by the present invention's technology, the A group is single effect evaporator, and the B group is one group of triple effect evaporator.With pressure is the working steam of the external source steam of 1.6Mpa as heat pump; A group evaporimeter adopts automatic cleaning type falling-film evaperator, the operating temperature of primary steam is 140 ℃, the operating pressure of control vaporization chamber is 0.24Mpa, then the saturation temperature of corresponding indirect steam is 126 ℃ with it, the saturation temperature of organizing the first single-effect evaporator indirect steam than B is high 12 ℃, A is organized whole indirect steams common primary steam after heat pump mixing supercharging of evaporimeter with external source steam as A, two groups of evaporimeters of B, heat pump adopts steam jet pump or disjunctor heat engine-heat pump, and its mass ratio of induced-to-inducing air can reach 1.2.Material liquid (content: CaCl
2Be 15.4%, NaCl is 8.6%, all the other are water) be preheating to more than 115 ℃ by embodiment 1 identical mode, be introduced into A group evaporimeter, the boiling point of A group evaporimeter feed liquid is 133 ℃, is concentrated to the concentration (content: CaCl of technological requirement by technological process shown in Figure 1
2Be 41%, NaCl was 18% (containing crystallization), all the other are water) the back discharging.Adopt the present invention's technology, comparable existing energy saving technology about about 30%.
Embodiment 3
By the same feed liquid of the present invention's technology evaporation and concentration embodiment 2, with pressure is the working steam of the external source steam of 1.0Mpa as heat pump, A group evaporimeter adopts automatic cleaning type falling-film evaperator, the operating temperature of primary steam is 140 ℃, the operating pressure of control vaporization chamber is 0.264Mpa, then the saturation temperature of corresponding indirect steam is 130 ℃ with it, the saturation temperature of organizing the first single-effect evaporator indirect steam than B is high 16 ℃, whole indirect steams of A being organized evaporimeter with external source steam after heat pump mixing supercharging jointly as A, the primary steam of two groups of evaporimeters of B, heat pump adopts steam jet pump or disjunctor heat engine-heat pump, and its mass ratio of induced-to-inducing air can reach 0.4.Material liquid is preheating to more than 115 ℃, is introduced into A group evaporimeter, enters B group evaporimeter after concentrating again, is concentrated to discharging after the concentration of technological requirement.Adopt the present invention's technology, comparable existing energy saving technology about about 20%.
Embodiment 4
By the same feed liquid of the present invention's technology evaporation and concentration embodiment 2, with pressure is the working steam of the external source steam of 1.6Mpa as heat pump, A group evaporimeter adopts automatic cleaning type falling-film evaperator, the operating temperature of primary steam is 140 ℃, the operating pressure of control vaporization chamber is 0.18Mpa, then the saturation temperature of corresponding indirect steam is 117 ℃ with it, the saturation temperature of organizing the first single-effect evaporator indirect steam than B is high 3 ℃, whole indirect steams of A being organized evaporimeter with external source steam after heat pump mixing supercharging jointly as A, the primary steam of two groups of evaporimeters of B, heat pump adopts steam jet pump or disjunctor heat engine-heat pump, and its mass ratio of induced-to-inducing air can reach 0.7.Material liquid is preheating to more than 115 ℃, is introduced into A group evaporimeter, enters B group evaporimeter after concentrating again, is concentrated to discharging after the concentration of technological requirement.Adopt the present invention's technology, comparable existing energy saving technology about about 20%.
Embodiment 5
By the same feed liquid of the present invention's technology evaporation and concentration embodiment 2, with pressure is the working steam of the external source steam of 4.5Mpa as heat pump, A group evaporimeter adopts the forced circulation type evaporimeter, the operating temperature of primary steam is 140 ℃, the operating pressure of control vaporization chamber is 0.20Mpa, then the saturation temperature of corresponding indirect steam is 120 ℃ with it, the saturation temperature of organizing the first single-effect evaporator indirect steam than B is high 6 ℃, with external source steam with the indirect steam of whole A group evaporimeters after heat pump mixing supercharging jointly as A, the primary steam of two groups of evaporimeters of B, heat pump adopts the disjunctor heat engine-heat pump, and its mass ratio of induced-to-inducing air can reach 3.0.Material liquid is preheating to more than 115 ℃, is introduced into A group evaporimeter, enters B group evaporimeter after concentrating again, is concentrated to discharging after the concentration of technological requirement.Adopt the present invention's technology, comparable existing energy saving technology about about 60%.
Part technological parameter and the energy-saving effect thereof of embodiment 2～5:
The external source steam pressure, Mpa 1.6 1.0 1.6 4.5
A1 is imitated vaporization chamber pressure, and Mpa 0.24 0.264 0.18 0.20
A1 is imitated the saturation temperature of indirect steam, and ℃ 126 130 117 120
A1 and B1 are imitated the indirect steam temperature difference, and ℃ 12 16 36
The mass ratio of induced-to-inducing air 1.2 0.4 0.7 3.0 of heat pump
Energy-conservation, % 30 20 20 60
Therefore the present invention's technology by improving the mass ratio of induced-to-inducing air of heat pump, can cut down the consumption of energy greatly, improves energy-saving effect, and energy-conservation amplitude can reach 20～60%, thereby promotes the technological progress of evaporation and concentration engineering effectively.
In addition, relatively the pressure of shortage or external source steam is lower for the energy, as external source steam＜1.0MPa, even＜occasion of 0.4Mpa, can use the present invention's technology equally, but the mass ratio of induced-to-inducing air of heat pump decreases, but still have certain energy-saving effect.
Claims (5)
1, a kind of combined evaporative concentration technology that has heat pump is characterized in that: it mainly is made up of heat pump and two groups of evaporimeters of A, B, and wherein A group evaporimeter is a vaporising device that has heat pump, and B group evaporimeter is one group of multi-effect evaporating device; The heat pump that is adopted is a class steam power mixed type heat pump, i.e. a kind of in steam jet pump, the disjunctor heat engine-heat pump; A is organized indirect steam common primary steam after heat pump mixing supercharging of first single-effect evaporator with external source steam as A, two groups of evaporimeters of B; Control A organizes the operating pressure of the first single-effect evaporator vaporization chamber, makes the saturation temperature of its corresponding indirect steam be higher than 3～18 ℃ of the saturation temperatures that B organizes the first single-effect evaporator indirect steam.
2, a kind of combined evaporative concentration technology that has heat pump according to claim 1, it is characterized in that: material liquid adopts combined type preheating, elder generation carries out preheating with the part indirect steam that B organizes first single-effect evaporator, the condensed water of imitating with A group and B group evaporimeter first carries out preheating again, make feed liquid be preheated to temperature and be lower than boiling point and be no more than 25 ℃ and enter A again and organize first single-effect evaporator and concentrate, and then enter B group evaporimeter and further concentrate.
3, a kind of combined evaporative concentration technology that has heat pump according to claim 1 is characterized in that: control A organizes the evaporation capacity of first single-effect evaporator, the concentration of easy crystallized solute is remained be lower than its saturated concentration.
4, a kind of combined evaporative concentration technology that has heat pump according to claim 1, it is characterized in that: the pressure of external source steam is 1.0～4.5Mpa.
5, a kind of combined evaporative concentration technology that has heat pump according to claim 1, it is characterized in that: the mass ratio of induced-to-inducing air of heat pump is 0.4～3.0.
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| CNB021452954A CN1182900C (en) | 2002-11-14 | 2002-11-14 | Technique of combined concentration by evaporation with heat pump being provided |
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|---|---|---|---|
| CNB021452954A CN1182900C (en) | 2002-11-14 | 2002-11-14 | Technique of combined concentration by evaporation with heat pump being provided |
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| CN1182900C CN1182900C (en) | 2005-01-05 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101982213A (en) * | 2010-10-29 | 2011-03-02 | 江苏瑞普膜技术有限公司 | Technology of concentrating saline water and heat pump device thereof |
| CN102372331A (en) * | 2010-08-24 | 2012-03-14 | 刘上光 | Thermal waste water treatment apparatus and method employing heat pump |
| CN103495285A (en) * | 2013-09-25 | 2014-01-08 | 福建锦江科技有限公司 | Monomer recovery device for polyamide slice extraction water |
| CN105293527A (en) * | 2015-10-27 | 2016-02-03 | 苏州天沃科技股份有限公司 | Concentrating and flaking process of 75 caustic soda flakes |
| CN105645497A (en) * | 2016-01-12 | 2016-06-08 | 华东理工大学 | Recovery method of coal gasification system brine wastewater |
| CN106512450A (en) * | 2016-12-30 | 2017-03-22 | 无锡新弘田环保技术有限公司 | Miniaturized energy-saving evaporative regeneration device |
-
2002
- 2002-11-14 CN CNB021452954A patent/CN1182900C/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102372331A (en) * | 2010-08-24 | 2012-03-14 | 刘上光 | Thermal waste water treatment apparatus and method employing heat pump |
| CN102372331B (en) * | 2010-08-24 | 2013-06-05 | 刘上光 | Thermal waste water treatment apparatus and method employing heat pump |
| CN101982213A (en) * | 2010-10-29 | 2011-03-02 | 江苏瑞普膜技术有限公司 | Technology of concentrating saline water and heat pump device thereof |
| CN103495285A (en) * | 2013-09-25 | 2014-01-08 | 福建锦江科技有限公司 | Monomer recovery device for polyamide slice extraction water |
| CN103495285B (en) * | 2013-09-25 | 2015-07-22 | 福建锦江科技有限公司 | Monomer recovery device for polyamide slice extraction water |
| CN105293527A (en) * | 2015-10-27 | 2016-02-03 | 苏州天沃科技股份有限公司 | Concentrating and flaking process of 75 caustic soda flakes |
| CN105293527B (en) * | 2015-10-27 | 2017-06-20 | 苏州天沃科技股份有限公司 | 75 concentration sheeting techniques of alkali |
| CN105645497A (en) * | 2016-01-12 | 2016-06-08 | 华东理工大学 | Recovery method of coal gasification system brine wastewater |
| CN106512450A (en) * | 2016-12-30 | 2017-03-22 | 无锡新弘田环保技术有限公司 | Miniaturized energy-saving evaporative regeneration device |
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| CN1182900C (en) | 2005-01-05 |
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