CN101920122A - Backheating evaporation technology and technology system thereof - Google Patents
Backheating evaporation technology and technology system thereof Download PDFInfo
- Publication number
- CN101920122A CN101920122A CN2010102618496A CN201010261849A CN101920122A CN 101920122 A CN101920122 A CN 101920122A CN 2010102618496 A CN2010102618496 A CN 2010102618496A CN 201010261849 A CN201010261849 A CN 201010261849A CN 101920122 A CN101920122 A CN 101920122A
- Authority
- CN
- China
- Prior art keywords
- steam
- evaporimeter
- material liquid
- transfer pipeline
- heat
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Abstract
The invention relates to a backheating evaporation technology and a technology system thereof, belonging to the field of secondary steam backheating recovery and cyclic utilization. The backheating evaporation technology and the technology system thereof can be widely applied to the industrial departments of environmental protection, sea water desalination, distilled water preparation, solution concentration and solvent crystallization in chemical production, and the like. The backheating evaporation technology comprises the following sequence: raw material liquid is heated in a heat exchanger, enters an evaporator, continues to absorb heat in the evaporator and boils and vaporizes to produce secondary steam; the secondary steam is heated by exchanging heat with fresh steam, the pressure of the secondary steam is increased under the action of an air blower, and the secondary steam is converted into heating steam; the heating steam is transmitted back to the evaporator and releases heat in the evaporator to heat the raw material liquid, so that the raw material liquid boils and vaporizes to produce secondary steam, meanwhile, the heating steam is condensed into a saturated solvent; and the saturated solvent is discharged from the evaporator and transmitted back to the heat exchanger to exchange heat with the raw material liquid, so that the raw material liquid is heated, and the saturated solvent becomes a cooled solvent to be discharged after releasing heat. The invention has the advantages of wide application range, low steam-water ratio, energy saving, environmental protection, and the like.
Description
Technical field
A kind of backheat evaporation technology and process system thereof belong to indirect steam backheat recycle and reuse field.Be specifically related to a kind of latent heat of in evaporation technology, recycling indirect steam, thereby realize the technology of heat energy recycling, can be widely used in that environmental protection, desalinization, distilled water are produced, industrial department such as solution concentration and solvent crystallization in the Chemical Manufacture.
Background technology
Evaporation is to make the solvent vaporization by heating, thereby obtains the method for operating of concentrated solution or solid solute.Evaporation can be at normal pressure, reduce pressure or add to depress and carry out.Industrial evaporation type commonly used has following four kinds at present:
One, single effect evaporation is the most basic evaporation flow process, and material liquid is heated vaporization in evaporimeter, and the indirect steam of generation no longer utilizes.The energy consumption index of single effect evaporation is very high, but its equipment and factory building cost of investment are minimum.
Two, multiple-effect evaporation is the heating steam that the indirect steam that preceding effect evaporation produces is evaporated as aftereffect, heat is repeatedly utilized, so lower than the energy consumption index of single effect evaporation.But with the increase of imitating number, the energy consumption index downward trend slows down gradually, and cost of investment is the straight line rising.
Three, thermo-compression evaporation is meant the indirect steam that produces, and utilizes the adiabatic compression of compressor or utilizes the steam jet pump compression, sends heating clamber back to behind the raising pressure, once more as heating steam, provides vaporization required heat.In theory, the energy consumption index of thermo-compression evaporation is very low, but owing to the required power of drive compression machine is very big, when evaporation capacity is big, increase distribution facility, so cost of investment increases; For steam jet pump since its carry not higher than (driving quantity of steam and the ratio that sucks the indirect steam amount), so part residue indirect steam is always arranged, and, if contain drop in the driving steam that adopts, make nozzle wear easily, efficient is more descended.This evaporation pattern is representative with the MVR evaporimeter.
Four, vacuum flashing is that hot solution is sent into low-voltage space, makes its hurried vaporization under adiabatic condition.Be suitable for reclaiming the heat of hot solution or handle easy material in the heating surface fouling.
More than four kinds of evaporation type, cut both ways, but the ubiquity scope of application is wide or actual consumption than higher, shortcomings such as production cost height.
Summary of the invention
The technical problem to be solved in the present invention is: overcomes the deficiencies in the prior art, provides a kind of the indirect steam recycling use, and low backheat evaporation technology and the process system thereof of cost.
The technical solution adopted for the present invention to solve the technical problems is: this a kind of backheat evaporation technology, it is characterized in that: the backheat evaporation technology is in proper order: material liquid enters evaporimeter after heating up in heat exchanger, in evaporimeter, continue heat absorption boiling vaporization and produce indirect steam, indirect steam by with the live steam heat exchange, the rising temperature, simultaneously under fan action, increase pressure, be converted into heating steam, heating steam feeds back to evaporimeter, heat release in evaporimeter, heating raw liquid, make material liquid boiling vaporization produce indirect steam, heating steam is condensed into saturated solvent simultaneously, and saturated solvent is discharged in the evaporimeter and fed back in the heat exchanger and material liquid generation heat exchange, material liquid is heated up, form the cooling solvent after the saturated solvent heat release and discharge.
In evaporimeter, heating steam is condensed into saturated solvent and the two temperature difference of material liquid boiling vaporization is 8-20K.
Preferably, indirect steam and live steam heat exchange are undertaken by the mode of mixed heat transfer.
Indirect steam and live steam heat exchange also can be by in the secondary heat exchange devices, and live steam directly heats the mode of indirect steam transfer pipeline and carries out.
Described saturated solvent is a saturation water.
A kind of process system of backheat evaporation technology, it is characterized in that: comprise evaporimeter, heat exchanger, blower fan and transfer pipeline, material liquid links to each other with heat exchanger feed liquid inlet by transfer pipeline, the heat exchanger material liquid outlet links to each other with evaporimeter feed liquid inlet by transfer pipeline, the evaporimeter material liquid outlet links to each other with the live steam transfer pipeline, live steam mixes the back with indirect steam and links to each other with evaporimeter heating steam inlet by the threeway transfer pipeline, the threeway transfer pipeline is provided with blower fan, and the outlet of evaporimeter saturated solvent links to each other with heat exchanger saturated solvent inlet by transfer pipeline.
The process system of another kind of backheat evaporation technology, it is characterized in that: comprise evaporimeter, heat exchanger, blower fan, secondary heat exchange device and transfer pipeline, material liquid links to each other with heat exchanger feed liquid inlet by transfer pipeline, the heat exchanger material liquid outlet links to each other with evaporimeter feed liquid inlet by transfer pipeline, the evaporimeter material liquid outlet links to each other with secondary heat exchange device inlet, secondary heat exchange device heating steam inlet links to each other with the live steam transfer pipeline, indirect steam heats the back and links to each other with evaporimeter heating steam inlet by transfer pipeline in the secondary heat exchange device, the threeway transfer pipeline is provided with blower fan, and the outlet of evaporimeter saturated solvent links to each other with heat exchanger saturated solvent inlet by transfer pipeline.
The operation of backheat evaporation technology of the present invention comprises three heat transfer process:
1, the heat transfer process between liquid
Heat exchange between material liquid a original state and saturation water is carried out in heat exchanger 2, can adopt the heat exchange mode of adverse current, following current or mixed flow.
2, condense-the evaporation and heat-exchange process
In evaporimeter 1, heating steam is condensed, feed liquid boiling vaporization.
3, the heat transfer process between steam
Heat transfer process between live steam and indirect steam, purpose are to realize technology (temperature, the pressure) requirement of heating steam.
Backheat evaporation technology of the present invention is to utilize the mode of heat exchange to improve the temperature of indirect steam, increases pressure simultaneously under heating and blower fan acting in conjunction, makes indirect steam be converted into heating steam, and the required heat of vaporizing is provided.On Engineering Thermodynamics, this a part of heat that utilizes working medium to discharge comes the method for heating working medium to be called backheat.So the method for evaporation provided by the invention is referred to as the backheat evaporation.
The identical point of backheat evaporation and mechanical compression type thermo-compression evaporation:
One, all indirect steam is converted into heating steam;
Two, the two does not all have the residue indirect steam;
All need assist heating when three, starting.
The difference of backheat evaporation and mechanical compression type thermo-compression evaporation:
One, on Engineering Thermodynamics, backheat belongs to polytropic process, with the external world exchange heat is arranged; Heat pump belongs to adiabatic process, with extraneous empty calory exchange.
Two, indirect steam temperature-rise period: the backheat evaporation realizes by the heat transmission, does not occur the conversion of energy form in the process; Thermo-compression evaporation is realized by adiabatic compression, occurs the conversion of energy form in the process, i.e. electric energy → mechanical energy → heat energy.
Three, the backheat evaporation is to consume high-temperature steam; Thermo-compression evaporation is based on consumed power.
Four, blower fan is used in the backheat evaporation, and pressure is little, and power is low; The thermo-compression evaporation compressor, the pressure high power is big.
Thinking of the present invention is: the indirect steam that evaporation technology is produced passes through heat temperature raising, all is converted into available heating steam.Be specially: at first material liquid is warmed up to boiling point, enters in the evaporimeter, continue the heat absorption vaporization, produce indirect steam.Under the acting in conjunction of live steam and blower fan, the temperature and pressure of indirect steam raises jointly, can be used as heating steam, adds heat request thereby satisfy.Heating steam is heat release in evaporimeter, is condensed into saturation water.At last, heat exchange takes place in the saturation water and the material liquid of discharging from evaporimeter once more.
Because the heat transfer coefficient of superheated steam is generally all smaller, so, if no specific (special) requirements, the mode heat exchange that the present invention preferably adopts live steam and indirect steam directly to mix.
Heating steam should enter in the evaporimeter with saturation state.Because the solute concentration increase can cause the solution elevation of boiling point, so the indirect steam that evaporation obtains is superheated steam often; The live steam of introducing because pressure reduces, also becomes superheated steam.The two mixing and after blower fan pressurization, if the degree of superheat of heating steam is still very high, the heat transfer coefficient of superheated steam is generally all smaller, the method that can adopt the saturation water that will condense in the evaporimeter to spray into is eliminated the degree of superheat, makes heating steam be in saturation state.
If when requiring moisture too highly maybe can not contain moisture through the cooling solvent after the heat exchanger heat release, the mode that then can not adopt indirect steam to mix with live steam is carried out heat transmission, can adopt in heat exchanger, the mode that indirect steam heats be improved the indirect steam temperature by live steam.
Compared with prior art, backheat evaporation technology of the present invention and beneficial effect that process system had thereof are:
1, energy-conservation, widely applicable, have lower steam-water ratio.
2, cost of investment is low, and is good in economic efficiency, and live steam can directly utilize the steam that produces in the process of factory production, needn't produce separately, and the energy is recycling.
3, evaporation equipment is general, and former evaporation equipment technological transformation is convenient.
Description of drawings
Fig. 1 is process system flow implementation example 1 schematic diagram of the present invention.
Fig. 2 is process system flow implementation example 2 schematic diagrames of the present invention.
Wherein: 1, evaporimeter 2, heat exchanger 3, blower fan 4, secondary heat exchange device a, material liquid b, live steam c, cooling solvent.
Be described further below in conjunction with 1～2 pair of invention of accompanying drawing:
The specific embodiment
Fig. 1 most preferred embodiment of the present invention, with reference to accompanying drawing 1: process system is by evaporimeter 1, heat exchanger 2, blower fan 3, material liquid a, live steam b and cooling solvent c: wherein, material liquid a links to each other with heat exchanger 2 feed liquids inlet by transfer pipeline, heat exchanger 2 material liquid outlets link to each other with evaporimeter 1 feed liquid inlet by transfer pipeline, the indirect steam of output mixes the back and links to each other with evaporimeter 1 heating steam inlet by transfer pipeline, blower fan 3 in live steam b and the evaporimeter 1, and evaporimeter 1 saturated solvent exports to enter the mouth with heat exchanger 2 saturated solvents by transfer pipeline and links to each other.
After the normal operation of system, material liquid a enters in the evaporimeter 1 after heating up in heat exchanger 2, it continues heat absorption boiling vaporization in evaporimeter 1, the indirect steam that produces mixes with live steam b and carries out the heat transmission, the indirect steam temperature raises, after heating and the increase of blower fan 3 acting in conjunction pressure, indirect steam is converted into heating steam.The heating steam of gained is fed back to evaporimeter 1,1 heat release in evaporimeter, the heating feed liquid is condensed into saturated solvent.The saturated solvent of discharging from evaporimeter 1 feeds back in the heat exchanger 2 and material liquid a generation heat exchange, in order to heating raw liquid a, forms cooling solvent c after the saturated solvent heat release, thereby realizes the recycling of heat.
After testing, in evaporimeter 1, heating steam is condensed into saturated solvent and the two temperature difference of material liquid boiling vaporization is 8-20K.
With reference to accompanying drawing 2: when requiring moisture too highly maybe can not contain moisture to the cooling solvent c that forms after the saturated solvent heat release, can be in the indirect steam temperature-rise period, adopt by live steam b in heat exchanger, the mode that indirect steam is heated improves the indirect steam temperature.The process system flow process: material liquid a links to each other with heat exchanger 2 feed liquids inlet by transfer pipeline, heat exchanger 2 material liquid outlets link to each other with evaporimeter 1 feed liquid inlet by transfer pipeline, evaporimeter 1 material liquid outlet links to each other with secondary heat exchange device 4 inlets, live steam b feeds secondary heat exchange device 4 by transfer pipeline, the heating indirect steam, after indirect steam pressurizes by blower fan 3, in transfer pipeline fed evaporimeter 1 heating steam inlet, the outlet of evaporimeter 1 saturated solvent linked to each other with heat exchanger 2 saturated solvents inlet by transfer pipeline.Other processing steps are identical with embodiment 1.
The above only is preferred embodiment of the present invention, is not to be the restriction of the present invention being made other form, and any those skilled in the art may utilize the technology contents of above-mentioned announcement to be changed or be modified as the equivalent embodiment of equivalent variations.But every technical solution of the present invention content that do not break away to any simple modification, equivalent variations and remodeling that above embodiment did, still belongs to the protection domain of technical solution of the present invention according to technical spirit of the present invention.
Claims (7)
1. backheat evaporation technology, it is characterized in that: the backheat evaporation technology is in proper order: material liquid enters evaporimeter after heating up in heat exchanger, in evaporimeter, continue heat absorption boiling vaporization and produce indirect steam, indirect steam by with the live steam heat exchange, the rising temperature, simultaneously under fan action, increase pressure, be converted into heating steam, heating steam feeds back to evaporimeter, heat release in evaporimeter, heating raw liquid, make material liquid boiling vaporization produce indirect steam, heating steam is condensed into saturated solvent simultaneously, and saturated solvent is discharged in the evaporimeter and fed back in the heat exchanger and material liquid generation heat exchange, material liquid is heated up, form the cooling solvent after the saturated solvent heat release and discharge.
2. a kind of backheat evaporation technology according to claim 1 is characterized in that: in evaporimeter, heating steam is condensed into saturated solvent and the two temperature difference of material liquid boiling vaporization is 8-20K.
3. a kind of backheat evaporation technology according to claim 1 is characterized in that: indirect steam and live steam heat exchange are undertaken by the mode of mixed heat transfer.
4. a kind of backheat evaporation technology according to claim 1 is characterized in that: indirect steam and live steam heat exchange are by in the secondary heat exchange device, and live steam directly heats the mode of indirect steam transfer pipeline and carries out.
5. a kind of backheat evaporation technology according to claim 1 is characterized in that: described saturated solvent is a saturation water.
6. the process system of a kind of backheat evaporation technology according to claim 1, it is characterized in that: comprise evaporimeter, heat exchanger, blower fan and transfer pipeline, material liquid links to each other with heat exchanger feed liquid inlet by transfer pipeline, the heat exchanger material liquid outlet links to each other with evaporimeter feed liquid inlet by transfer pipeline, the evaporimeter material liquid outlet links to each other with the live steam transfer pipeline, live steam mixes the back with indirect steam and links to each other with evaporimeter heating steam inlet by the threeway transfer pipeline, the threeway transfer pipeline is provided with blower fan, and the outlet of evaporimeter saturated solvent links to each other with heat exchanger saturated solvent inlet by transfer pipeline.
7. the process system of a kind of backheat evaporation technology according to claim 1, it is characterized in that: comprise evaporimeter, heat exchanger, blower fan, secondary heat exchange device and transfer pipeline, material liquid links to each other with heat exchanger feed liquid inlet by transfer pipeline, the heat exchanger material liquid outlet links to each other with evaporimeter feed liquid inlet by transfer pipeline, the evaporimeter material liquid outlet links to each other with secondary heat exchange device inlet, secondary heat exchange device heating steam inlet links to each other with the live steam transfer pipeline, indirect steam links to each other with evaporimeter heating steam inlet by transfer pipeline after the heating of secondary heat exchange device, the threeway transfer pipeline is provided with blower fan, and the outlet of evaporimeter saturated solvent links to each other with heat exchanger saturated solvent inlet by transfer pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102618496A CN101920122A (en) | 2010-08-20 | 2010-08-20 | Backheating evaporation technology and technology system thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102618496A CN101920122A (en) | 2010-08-20 | 2010-08-20 | Backheating evaporation technology and technology system thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101920122A true CN101920122A (en) | 2010-12-22 |
Family
ID=43335491
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010102618496A Pending CN101920122A (en) | 2010-08-20 | 2010-08-20 | Backheating evaporation technology and technology system thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101920122A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659196A (en) * | 2012-05-28 | 2012-09-12 | 天津壹帆水务有限公司 | Energy-saving evaporation process and system thereof |
| CN104368163A (en) * | 2014-11-05 | 2015-02-25 | 象山医疗精密仪器有限公司 | Liquid medicine concentration and solvent recovery process |
| CN104368162A (en) * | 2014-11-05 | 2015-02-25 | 象山医疗精密仪器有限公司 | Vapor compression type concentration and solvent recovery integrated machine |
| CN104548638A (en) * | 2014-12-30 | 2015-04-29 | 徐翔 | Waste heat recovery process and device for heat pump evaporation unit |
| CN105833559A (en) * | 2016-05-11 | 2016-08-10 | 耒阳金悦科技发展有限公司 | Industrial separation equipment |
| CN105854328A (en) * | 2016-05-11 | 2016-08-17 | 耒阳金悦科技发展有限公司 | Industrial separation method |
| CN109824107A (en) * | 2019-03-26 | 2019-05-31 | 何新华 | A kind of power plant effluent evaporation process method and its waste water evaporation process system |
| CN114307208A (en) * | 2021-12-31 | 2022-04-12 | 无锡荣丰生物工程有限公司 | Liquid sugar six-effect concentration continuous-elimination system and method for carrying out liquid sugar concentration continuous-elimination by using same |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1098959A (en) * | 1994-05-21 | 1995-02-22 | 陈启松 | Energy saving evaporating apparatus |
| CN101607922A (en) * | 2009-07-24 | 2009-12-23 | 浙江杭州湾腈纶有限公司 | A kind of preparation method of acrylamide crystal |
| CN101690851A (en) * | 2009-09-30 | 2010-04-07 | 徐克俭 | Indirect vapor recompression evaporation process method |
-
2010
- 2010-08-20 CN CN2010102618496A patent/CN101920122A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1098959A (en) * | 1994-05-21 | 1995-02-22 | 陈启松 | Energy saving evaporating apparatus |
| CN101607922A (en) * | 2009-07-24 | 2009-12-23 | 浙江杭州湾腈纶有限公司 | A kind of preparation method of acrylamide crystal |
| CN101690851A (en) * | 2009-09-30 | 2010-04-07 | 徐克俭 | Indirect vapor recompression evaporation process method |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102659196A (en) * | 2012-05-28 | 2012-09-12 | 天津壹帆水务有限公司 | Energy-saving evaporation process and system thereof |
| CN104368163A (en) * | 2014-11-05 | 2015-02-25 | 象山医疗精密仪器有限公司 | Liquid medicine concentration and solvent recovery process |
| CN104368162A (en) * | 2014-11-05 | 2015-02-25 | 象山医疗精密仪器有限公司 | Vapor compression type concentration and solvent recovery integrated machine |
| CN104368162B (en) * | 2014-11-05 | 2016-01-20 | 象山医疗精密仪器有限公司 | Steam compression type is concentrated, solvent recovery all-in-one |
| CN104548638A (en) * | 2014-12-30 | 2015-04-29 | 徐翔 | Waste heat recovery process and device for heat pump evaporation unit |
| CN104548638B (en) * | 2014-12-30 | 2016-02-17 | 徐翔 | Thermo-compression evaporation unit waste heat reclaiming process and device |
| CN105833559A (en) * | 2016-05-11 | 2016-08-10 | 耒阳金悦科技发展有限公司 | Industrial separation equipment |
| CN105854328A (en) * | 2016-05-11 | 2016-08-17 | 耒阳金悦科技发展有限公司 | Industrial separation method |
| CN109824107A (en) * | 2019-03-26 | 2019-05-31 | 何新华 | A kind of power plant effluent evaporation process method and its waste water evaporation process system |
| CN109824107B (en) * | 2019-03-26 | 2022-06-24 | 何新华 | Power plant wastewater evaporation treatment method and wastewater evaporation treatment system thereof |
| CN114307208A (en) * | 2021-12-31 | 2022-04-12 | 无锡荣丰生物工程有限公司 | Liquid sugar six-effect concentration continuous-elimination system and method for carrying out liquid sugar concentration continuous-elimination by using same |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101920122A (en) | Backheating evaporation technology and technology system thereof | |
| CN102659196A (en) | Energy-saving evaporation process and system thereof | |
| CN201373623Y (en) | Combined secondary steam heat energy recovery device for conventional phase change heat exchanger of steam jet heat pump | |
| CN201762130U (en) | Dual-effect steam recompression thermal mass recovery system | |
| CN104196584A (en) | System capable of conducting power recovering and cooling by using waste heat of blast furnace slag flushing water | |
| CN102797524A (en) | Medium-and-low-temperature waste-heat utilization cooling/power combination system | |
| CN203108242U (en) | Double-effect evaporation system used for ammonium sulphate concentration | |
| CN101985368A (en) | Condenser type seawater desalting device with steam turbine generator unit | |
| CN202139185U (en) | Device for polycondensation reaction for producing rubber antioxidant RD | |
| CN201373694Y (en) | Combined secondary steam heat energy recovery device for heat pipe phase change heat exchanger of steam jet heat pump | |
| CN102494525A (en) | Process utilizing steam jet pump to recover waste heat of exhaust gas of dryer indirectly | |
| CN201882942U (en) | Power-generation turboset condenser type sea water desalinating unit | |
| CN102267733A (en) | Industrial waste heat low-temperature multi-effect seawater desalting system | |
| CN105293544A (en) | Dissolution live steam condensate water evaporation secondary utilization method | |
| CN202116342U (en) | Industrial exhaust heat low-temperature multiple-effect seawater desalinization system | |
| CN201373695Y (en) | Combined secondary steam heat energy recovery device for heat pipe phase change heat exchanger of combined heat pump | |
| CN109939454A (en) | A kind of heat pump vacuum concentration system | |
| CN201737866U (en) | Furfuraldehyde production afterheat utilization system | |
| CN214299359U (en) | MVR high-efficiency energy-saving evaporation treatment system for nano-silver industrial wastewater treatment | |
| CN105439223B (en) | A kind of pressed-steam type REFRIGERATION SYSTEM DRIVEN BY CAPILLARY FORCE desalination plant | |
| CN212901433U (en) | Xylenol rectification waste heat recovery device | |
| CN101327939A (en) | Method for solid caustic soda production by ionic membrane method | |
| CN209828291U (en) | Heat pump vacuum concentration system | |
| CN203483883U (en) | Device for evaporating and concentrating waste liquid in caprolactam device | |
| CN201353435Y (en) | Single-effect evaporation device with mechanical fan as evaporation driving force |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20101222 |