CN104069643B - A kind of gas circulating and evaporating method and apparatus - Google Patents
A kind of gas circulating and evaporating method and apparatus Download PDFInfo
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- CN104069643B CN104069643B CN201410339893.2A CN201410339893A CN104069643B CN 104069643 B CN104069643 B CN 104069643B CN 201410339893 A CN201410339893 A CN 201410339893A CN 104069643 B CN104069643 B CN 104069643B
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Abstract
A kind of gas circulation evaporator and device, with effective evaporation energy-output ratio that reduces, and improve stability and the reliability that vapo(u)rization system is run.This device includes: the first vaporizer, connects fluid foods feeding pipe, high boiling point discharging pipeline；First condenser, connects low boiling discharging pipeline；Second vaporizer and the second condenser, connect boosting warming pipeline and compression circulatory mediator pipeline between the two, and the second vaporizer connects external heat source medium intake line, external heat source medium output pipe；Recycle gas line, sequentially connects the first vaporizer, the first condenser, the second condenser to the first vaporizer formation loop；Endogenous pyrogen medium loop, connects the second vaporizer and the first condenser.
Description
Technical field
The present invention relates to method of evaporating and the device of fluid foods.
Background technology
For evaporation technique, traditional single-action, economic benefits and social benefits, triple effect, the theoretical steam consumption about 1.10 of quadruple effect,
0.57,0.40,0.30 ton of steam/ton water, corresponding ton water process steam cost about 242 yuan, 125
Unit, 88 yuan, 66 yuan (according to 220 yuan/ton of vaporimeters of commercial steam cost).If considering, circulation is cold
But the thermal efficiency that water, circulation motor consumption and fouling of evaporator cause declines problem, above-mentioned evaporation skill
Art actual consumption and operating cost far surpass above-mentioned theory level.In order to solve, evaporation technique energy consumption is higher asks
Topic, in recent years, the patent in terms of evaporation technique increases increasingly.The development of evaporation technique is main at present
From temperature waste heat sources utilize (such as CN103265091A), vapo(u)rization system self low temperature heat (as
CN102060408B, CN101784481B, CN102757105A), reduce vapo(u)rization system heat exchange
Carry out in terms of device fouling (such as CN202909470U, CN103265091A) three.
CN102060408B, CN101784481B pass through mechanical vapor recompression technology (MVR)
Vaporization chamber carry out gas-liquid (Gu) separate after, steam is carried out recompression and improves vapor (steam) temperature and pressure
Again recycle after power.By which, energy-saving effect is notable.But in such scheme implementation process
In all exist evaporation mother solution forced circulation situation, evaporation mother solution in the quality such as Organic substance, calcium ions and magnesium ions dense
Spend along with the carrying out of evaporation process steps up, and ultimately result in forced circulation heating chamber (pipe) fouling
Seriously, cause serious heat transfer efficiency to decline problem and operating cost rises violently problem, more seriously
Vapo(u)rization system maintenance may be caused frequently, the stability of vapo(u)rization system operation and stream because of fouling and clogging problem
Smooth property is poor.Simultaneously as function of mechanical steam recompression improves indirect steam temperature and pressure, uncomfortable
Reclaim for heat-sensitive substance.
CN202909470U proposes one utilization and newly increases thermal medium isolation mode of heating, passes through gas
(air, nitrogen, carbon dioxide) stripping mode carries out waste water evaporation and concentration.Because the program is not mentioned
Utilizing low-temperature heat source problem, need to individually increase and add thermal medium heating, operating cost is of a relatively high.Meanwhile,
Because the waste gas after Zheng Fa is directly outer arranges surrounding air, there is potential environmental air pollution problem, also
There is water resource waste problem.
CN103265091A propose one utilize low-temperature heat source (public work waste gas, technology waste gas,
Surrounding air, recirculated cooling water, steam condensate (SC) etc.) steam in gas heating stripping sewage mode
Send out and concentrate, to going out after the aqueous gas of this system is processed by exhaust treatment system with waste gas mode row up to standard
Put.The program provides temperature waste heat sources because taking full advantage of facility periphery, runs in implementation process
This is relatively low.But waste water is converted into waste gas and processes by the program, there is certain water resource wave
Take.This patent formula is not suitable for reclaiming high value composition in volatilization evaporation yet.
CN102757105A proposes to use air conditioner heat pump system, implements evaporative condenser alternate cycles fortune
OK, it is achieved the solid-liquid separation in high-concentration waste.Although it is relatively low that the program implements temperature, fouling
Other vapo(u)rization systems relatively are relatively low.But air conditioner heat pump system and water inlet pre-heating system are by waste water (liquid)
Forced circulation carries out heat exchange, along with the carrying out of evaporation process, Organic substance in waste water (liquid), calcium and magnesium from
The mass concentrations such as son are stepped up, and cause heat exchanger easily fouling and blocking, and system thermal efficiency is with stable
Property declines to a great extent.Owing to heat exchange uses liquid liquid mode, the gas temperature participating in circulation is relatively low, mass transfer
Inefficient, bottom vaporization chamber, solid material moisture content is higher.Meanwhile, this patent formula does not considers yet
Cryogenic heat wasting utilization problem.
In sum, affect that evaporation technique develops it is crucial that to develop and to meet high (low) temperature simultaneously
Thermal source recycles and several heat exchange modes possible without fouling.
Summary of the invention
The technical problem to be solved is to provide a kind of gas circulation evaporator, with effectively fall
Low evaporation energy-output ratio, and improve stability and the reliability that vapo(u)rization system is run.
It is as follows that the present invention solves the technical scheme that above technical problem taked:
The gas circulation evaporator of the present invention, including the first vaporizer and the first condenser, first steams
Sending out device and connect fluid foods feeding pipe, high boiling point discharging pipeline, the first condenser connects low boiling and goes out
Material pipeline, is characterized in that it also includes: the second vaporizer and the second condenser, connects boosting between the two
Warming pipeline and compression circulatory mediator pipeline, the second vaporizer connects external heat source medium intake line, outer
Heat source medium output pipe；Recycle gas line, sequentially connect the first vaporizer, the first condenser,
Second condenser forms loop to the first vaporizer；Endogenous pyrogen medium loop, connect the second vaporizer and
First condenser.
The technical problem to be solved is to provide the above gas circulation evaporator of a kind of employing
Gas circulating and evaporating method.The method comprises the steps: 1. to be not less than by boiling-point difference 5 DEG C mixed
Closing raw material and put into the first vaporizer through fluid foods feeding pipe, high boiling point composition is through high boiling point discharge nozzle
Road is sent, and the low boiling point component of separation and recyclegas contact mass transfer also enter circulating air in a gaseous form
Internal, enter the first condenser through recycle gas line；2. the mixing circulation gas containing low boiling point component
Condensing at the first condenser, low boiling point component separates with recyclegas in liquid form, goes out through low boiling
Material pipeline is sent；3. the recyclegas separating low boiling point component enters the second condensation through recycle gas line
Device, absorb from the second vaporizer external heat medium, the first endogenous thermal medium of condenser heat after,
Recyclegas temperature rises again；4. the recyclegas after heating up is again introduced into the first vaporizer to be carried out
Circulating and evaporating.
The invention has the beneficial effects as follows, evaporate energy resource consumption phase by the saving that makes full use of of interior external heat source
Than traditional method energy-conservation more than 50%；Evaporation system is improved with several gas circulating possible without fouling
Stability that system runs and reliability, compare existing mechanical vapor recompression technology (MVR), many
Effect forced-circulation evaporator, falling film evaporator parallel-adder settle-out time improve more than 3 times；Can need not
Vacuum reclaims thermal sensitivity low-boiling point material in the case of getting involved, and the input both having reduced vacuum system also drops
The low input of equipment entirety pressure (vacuum)；Significantly have dropped low boilers in high boiling substance
The amount of matter, the low boiling point component response rate can improve more than 2%, and effectively realize refuse decrement, refuse
Decrement is up to more than 40%.
Accompanying drawing explanation
This specification includes such as next width accompanying drawing:
Fig. 1 is the composition schematic diagram of gas circulation evaporator of the present invention；
Equipment and corresponding labelling in figure: the first vaporizer 10, fluid foods feeding pipe 11,
High boiling point discharging pipeline 12, recycle gas line 13；Second vaporizer 20, endogenous pyrogen medium pipeline
21, external heat source medium intake line 22, external heat source medium output pipe 23；First condenser 30,
Low boiling discharging pipeline 31, endogenous pyrogen medium pipeline 21；Second condenser 40, boosting warming pipeline
41, compressor 42, compression circulatory mediator pipeline 43, choke valve 44.
Detailed description of the invention
The present invention is further described with embodiment below in conjunction with the accompanying drawings.
With reference to Fig. 1, the gas circulation evaporator of the present invention includes: the first vaporizer 10, connects stream
Body material feeding pipe 11, high boiling point discharging pipeline 12；First condenser 30, connects low boiling and goes out
Material pipeline 31；Second vaporizer 20 and the second condenser 40, connects boosting warming pipeline between the two
41 and compression circulatory mediator pipeline 43, the second vaporizer 20 connect external heat source medium intake line 22,
External heat source medium output pipe 23；Recycle gas line 13, sequentially connect the first vaporizer 10,
One condenser the 30, second condenser 40 to the first vaporizer 10 forms loop；Endogenous pyrogen medium returns
Road 21, connects the second vaporizer 20 and the first condenser 30.
Described first vaporizer the 10, second vaporizer 20 is respectively made up of 1 evaporator unit, or
Each evaporator unit being in series by least two or being in parallel is constituted.Described first condenser 30,
Second condenser 40 is respectively made up of 1 condenser unit, or each be in series by least two or
The condenser unit being in parallel is constituted.With reference to Fig. 1, described boosting warming pipeline 41 is provided with pressure
Contracting machine 42, described compression circulatory mediator pipeline 43 is provided with choke valve 44.
With reference to Fig. 1, the gas circulating and evaporating method of the present invention, comprise the steps:
1. mixing raw material boiling-point difference being not less than 5 DEG C puts into first through fluid foods feeding pipe 11
Vaporizer 10, high boiling point composition sends through high boiling point discharging pipeline 12, the low boiling point component of separation with
Recyclegas contact mass transfer also enters in recyclegas in a gaseous form, enters through recycle gas line 13
Enter the first condenser 30.
2. the mixing circulation gas containing low boiling point component condenses at the first condenser 30, low boiling point component
Separate with recyclegas in liquid form, send through low boiling discharging pipeline 31；
3. the recyclegas separating low boiling point component enters the second condenser through recycle gas line 13
40, absorbed from the second vaporizer 20 external heat medium, the first condenser by compression circulatory mediator
After the heat of 30 endogenous thermal mediums, recyclegas temperature rises again.
4. the recyclegas after heating up is again introduced into the first vaporizer 10 and is circulated evaporation.
Mixing is after raw material enters the first vaporizer 10, recyclegas with mix raw material at the first vaporizer
10 carry out direct gas-liquid mixed heat exchange and mass transfer, and low-boiling point material enters recyclegas, circulating air
In body, low-boiling point material content increases.In the first vaporizer, high boiling point composition enters with low boiling point component
Circulation of qi promoting liquid (Gu) separate, high boiling point composition enters the first vaporizer 10 bottom discharge, containing low boiling
The mixing circulation gas of composition enters through recycle gas line 13 after entering the first vaporization chamber device 10 top
First condenser 30.
In the first condenser 30, carry out heat exchange containing low boiling point component recyclegas and endogenous pyrogen medium
After, low boiling point component progressively condenses, and in recyclegas, low boiling point component progressively declines.In recyclegas
After low boiling point component condensation, low boiling point component enters the first condenser 30 bottom discharge, separates low boiling
The recyclegas of some composition enters the second condenser 40 through recycle gas line 13.
In the second condenser 40, cold cycle gas carries out heat exchange intensification with compression circulatory mediator,
Again direct gas-liquid mixed heat exchange is carried out with charging (mixing raw material) in subsequently entering the first vaporizer
And mass transfer, enter next charging evaporative condenser circulation.
In the second vaporizer 20, from the first condenser endogenous thermal medium with from outside system
External heat medium carries out heat exchange.In second vaporizer, because evaporation absorbs, endogenous heat is situated between compression circulatory mediator
Matter, external heat medium heat.Then compression circulatory mediator is under compressor effect, carries out boosting and heats up.
Inside the second condenser, recyclegas carries out heat exchange with High Temperature High Pressure compression circulatory mediator.Part heat
Amount is transferred to the compression circulatory mediator of recyclegas and then enters the second vaporizer under choke valve effect
Evaporation endothermic.The purpose of above-mentioned compression circulatory mediator circulation is to realize external heat medium (public work
Waste gas, technology waste gas, surrounding air, recirculated cooling water, steam condensate (SC), sewage, surface water,
The one of phreatic water, underground heat etc. or several combination), endogenous thermal medium is (in the first condenser
Low-boiling point material condensation heat) heat by compression circulatory mediator transfer cycle gas, be beneficial to evaporation
Be smoothed out.
Easily (high boiling point organic compound or inorganic salt, fouling and chocking-up degree are along with quality for the material of fouling
The increase of concentration and increase) in the first vaporizer (big volume space), carry out the direct heat of mixing of gas-liquid
Exchange and mass transfer, do not have fouling of heat exchangers or blockage problem, heat transfer (matter) efficiency and evaporation system
System operational reliability is significantly increased.
It is transferred to circulating air by compression circulatory mediator by external heat medium, endogenous thermal medium heat
Body, energy consumption declines to a great extent needed for vapo(u)rization system.
Described step 2. in containing low boiling point component mixing circulation gas first condenser 30 condensation fall
Temperature is not less than 2 DEG C.
Described step 3. in separate the recyclegas of low boiling point component and absorb heat temperature rise at the second condenser 40
It is not less than 2 DEG C.External heat medium is from public work waste gas, technology waste gas, surrounding air, circulation
Cooling water, steam condensate (SC), sewage, surface water, phreatic water or the one of underground heat or some combinations,
Temperature range is 5～1200 DEG C.The temperature range of endogenous thermal medium is-150～65 DEG C.Compression circulation
Under medium mark condition, boiling point is less than 250 DEG C.
Enforcement case 1:
Certain fine chemical product mother solution content of organics 1～2%, inorganic salt content 8～12%, this gives up
Water (liquid) belongs to National Hazard refuse, have difficult degradation, poisonous, can not biochemical, high concentration is organic
The features such as thing, ammonia nitrogen in high density, high concentration salinity.
Use the technical scheme of patent CN101784481B, at 1m3During/h treatment scale, preheating is useless
Coolant-temperature gage, to 65 ± 5 DEG C (follow-up be no longer heat up), uses shell and tube forced circulation heat exchanger, at the beginning of startup
Phase runs general power about 90Kw, and after running 2 days, scale formation occurs in forced circulation heat exchanger, compression
Machine runs power and soars to 110Kw, runs power and soar to 176Kw after running 7 days, and maintenance is sent out
Reveal existing individual heater tubulation clogging.Final high boiling substance generation amount (solid-liquid mixing) is
0.63t/h, low-boiling point material generation amount are 0.27t/h (liquid).
Use the technical scheme of patent CN102757105A, at 1m3During/h treatment scale, preheating
Wastewater temperature is to 65 ± 5 DEG C (follow-up be no longer heat up), and initial operating stage runs general power about 56Kw, fortune
After row 9 days, run power along with the fouling of preheater (water inlet and air conditioner heat pump system liquid liquid heat exchange)
Rising to 82Kw, after running 21 days, preheater blocking is serious, runs general power and soars to 192Kw.
After cleaned preheater, about follow-up less than in 15 days cycle of operations, again occur that preheater blocks up
Plug phenomenon, the most thoroughly abandons the program.Final high boiling substance generation amount (solid-liquid mixing) is
0.5t/h, low-boiling point material generation amount are 0.5t/h (liquid).
Use technical scheme (the first evaporator unit 1, first condenser unit 1 of the application
Individual, the second condenser unit 4, the second evaporator unit 1, compressor unit 1), useless
Charging that the temperature remains within the normal range for water (30 ± 5 DEG C), external heat medium uses surrounding air (22～32 DEG C), interior
Source heat medium temperature is 5～12 DEG C, the gas of circulation is air, and stable operation does not occurs knot for 30 days
Dirt phenomenon, operation general power, all the time between 28～34Kw, is run after continuing stable operation 180 days
General power is still in above-mentioned fluctuation range.Recyclegas in the first condenser unit temperature from 55 ± 2 DEG C
It is cooled to 8 ± 2 DEG C.It is warming up to 79 ± 2 DEG C from 7 ± 2 DEG C at the second condenser unit.Final high boiling product
Matter (under mark condition, boiling point is higher than 105 DEG C, the molten point of mixture 789 DEG C after drying and dehydrating) generation amount is
0.23t/h (solid block), low-boiling point material (under mark condition, boiling point 100 DEG C) generation amount are 0.77t/h
(liquid).
The technical scheme using the application is the most excellent in terms of operation stability and evaporation and concentration degree
In technical scheme in contrast.
Embodiment 2:
Certain fine chemistry industry biochemical wastewater treatment mud day generation amount about 20 ton day (moisture content about 99%).
Owing to biochemical sludge belongs to National Hazard refuse, send into after needing enterprise's dehydration and burn station process.Consider
The biochemical sludge of dehydration has difficult degradation, poisonous feature (biochemical sludge absorption high activity organic compound
Thing), and further contemplate and send into the moisture percentage in sewage sludge burning station to burning cost height correlation,
Select eventually the application technical scheme (the first evaporator unit 1, the first condenser unit 2,
Second condenser unit 1, the second evaporator unit 2, compressor unit 1) dehydration after give
Enter to burn station to process.Recyclegas uses surrounding air, external heat medium to use and burns station chilled water (chw) (temperature
Spend about 60～70 DEG C, within 1s, flue gas be chilled to 200 DEG C from 1200 DEG C), endogenous thermal medium
Temperature about-15～5 DEG C, whole system stable operation 180 days, operating cost (only sludge dewatering) begins
Maintain 10Kwh/m eventually3Mud within mud (moisture percentage in sewage sludge about 99%), after dehydration contains
Water rate (sample position the first base of evaporator) about 45～48%.Recyclegas is at the first condenser
Cell temperature is cooled to 0 ± 2 DEG C from 65 ± 2 DEG C.It is warming up to from 0 ± 2 DEG C at the second condenser unit
70±2℃.(under mark condition, boiling point is higher than 105 DEG C to final high boiling substance, mixture after drying and dehydrating
Burning-point 347 DEG C) generation measures about 0.36t/d (solid block), low-boiling point material (under mark condition, boiling point
100 DEG C) generation amount is 19.64t/d (liquid).
Embodiment 3:
After certain chemical products is extracted by ethanol, need separating alcohol, product, its generation amount about 40 tons
/ sky.Common measure uses decompression distillation, about 180 yuan/ton of alcohol of processing cost.Use the application's
Technical scheme (the first evaporator unit 1, the first condenser unit 4, the second condenser unit
1, the second evaporator unit 2, compressor unit 2), recyclegas is nitrogen (purpose
Explosion-proof), external heat medium be that plant area's steam condensate (SC) (40～50 DEG C), endogenous heat medium temperature are
-15～-5 DEG C, recyclegas is cooled to-10 ± 2 DEG C in the first condenser unit temperature from 45 ± 2 DEG C.?
Second condenser unit is warming up to 68 ± 2 DEG C from-10 ± 2 DEG C, and being finally recovered cost is 53Kwh/ ton second
Alcohol, ethanol is product to continuing after within 500ppm to recycle, after separating alcohol subsequently through dehydration
Product ethanol content is less than 3 ‰.Generation amount is about for final high boiling substance (under mark condition, boiling point 181 DEG C)
13.3t/d (pressed powder), low-boiling point material (under mark condition, boiling point 78 DEG C) generation amount is 26.7t/d
(liquid).
Claims (10)
1. a gas circulation evaporator, including the first vaporizer (10) and the first condenser (30),
First vaporizer (10) connects fluid foods feeding pipe (11), high boiling point discharging pipeline (12),
First condenser (30) connects low boiling discharging pipeline (31), it is characterized in that it also includes: second
Vaporizer (20) and the second condenser (40), connect boosting warming pipeline (41) and pressure between the two
Contracting circulatory mediator pipeline (43), the second vaporizer (20) connection external heat source medium intake line (22),
External heat source medium output pipe (23)；Recycle gas line (13), sequentially connect the first vaporizer (10),
First condenser (30), the second condenser (40) form loop to the first vaporizer (10)；In
Heat source medium loop (21), connects the second vaporizer (20) and the first condenser (30).
2. gas circulation evaporator as claimed in claim 1 a kind of, is characterized in that: described the
One vaporizer (10), the second vaporizer (20) are respectively made up of 1 evaporator unit, or respectively by
The evaporator unit that at least two is in series or is in parallel is constituted.
3. gas circulation evaporator as claimed in claim 1 a kind of, is characterized in that: described the
One condenser (30), the second condenser (40) are respectively made up of 1 condenser unit, or respectively by
The condenser unit that at least two is in series or is in parallel is constituted.
4. a kind of gas circulation evaporator as claimed in claim 1, is characterized in that: described liter
It is provided with compressor (42), described compression circulatory mediator pipeline (43) in pressure warming pipeline (41)
On be provided with choke valve (44).
5. use the gas of gas circulation evaporator as described in Claims 1-4 any one to follow
Ring method of evaporating, comprises the steps:
1. boiling-point difference is not less than the mixing raw material of 5 DEG C and puts into the through fluid foods feeding pipe (11)
One vaporizer (10), high boiling point composition sends through high boiling point discharging pipeline (12), the low boiling of separation
Put composition and recyclegas contact mass transfer and enter in a gaseous form in recyclegas, through recyclegas pipe
Road (13) enters the first condenser (30)；
2. the mixing circulation gas containing low boiling point component condenses at the first condenser (30), and low boiling becomes
Divide and separate with recyclegas in liquid form, send through low boiling discharging pipeline (31)；
3. the recyclegas separating low boiling point component enters the second condenser through recycle gas line (13)
(40), by compression circulatory mediator absorb from the second vaporizer (20) external heat medium, first
After the heat of condenser (30) endogenous thermal medium, recyclegas temperature rises again；
4. the recyclegas after heating up is again introduced into the first vaporizer (10) and is circulated evaporation.
6. gas circulating and evaporating method as claimed in claim 5, is characterized in that: described step is 2.
In containing low boiling point component mixing circulation gas the first condenser (30) condensation cooling be not less than 2 DEG C.
7. gas circulating and evaporating method as claimed in claim 5, is characterized in that: described step is 3.
The recyclegas of middle separation low boiling point component is not less than 2 DEG C in the second condenser (40) heat absorption temperature rise.
8. gas circulating and evaporating method as claimed in claim 5, is characterized in that: described step is 3.
External heat medium is from public work waste gas, technology waste gas, surrounding air, recirculated cooling water, steam
The one of condensed water, sewage, surface water, phreatic water or underground heat or some combinations, temperature range be 5～
1200℃。
9. gas circulating and evaporating method as claimed in claim 5, is characterized in that: described step is 3.
In the temperature range of endogenous thermal medium be-150～65 DEG C.
10. gas circulating and evaporating method as claimed in claim 5, is characterized in that: described step is 3.
Under middle compression circulatory mediator mark condition, boiling point is less than 250 DEG C.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201410339893.2A CN104069643B (en) | 2014-07-17 | 2014-07-17 | A kind of gas circulating and evaporating method and apparatus |
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|---|---|---|---|
| CN201410339893.2A CN104069643B (en) | 2014-07-17 | 2014-07-17 | A kind of gas circulating and evaporating method and apparatus |
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| CN104069643B true CN104069643B (en) | 2016-08-24 |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107964775B (en) * | 2017-11-10 | 2019-05-03 | 珠海格力电器股份有限公司 | Heating system and method for recovering waste heat of laundry room |
| CN111057583A (en) * | 2019-12-03 | 2020-04-24 | 中国船舶重工集团公司第七一一研究所 | Gas separation device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1041110A (en) * | 1988-09-14 | 1990-04-11 | 杨极才 | Gas-carrying film concentrator |
| CN102060408A (en) * | 2010-12-07 | 2011-05-18 | 华电水处理技术工程有限公司 | Wastewater evaporating process and device system |
| CN201885590U (en) * | 2010-12-15 | 2011-06-29 | 湖南思为能源环保有限公司 | Aluminum oxide low-temperature flue gas waste heat heating and evaporation stock solution device |
| CN202909470U (en) * | 2012-03-24 | 2013-05-01 | 郭朝军 | Evaporation tower for performing evaporation treatment on salt-containing water using gas |
| CN103265091A (en) * | 2013-05-22 | 2013-08-28 | 魏华 | Mechanical ventilation forced circulation evaporation device and liquid material evaporation method |
| CN203281049U (en) * | 2013-06-19 | 2013-11-13 | 温州市森博轻工机械有限公司 | Single-effect external circulation vacuum concentrator |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4715765B2 (en) * | 2007-02-09 | 2011-07-06 | 株式会社日立プラントテクノロジー | Liquid concentrating system and liquid concentrator used therefor |
-
2014
- 2014-07-17 CN CN201410339893.2A patent/CN104069643B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1041110A (en) * | 1988-09-14 | 1990-04-11 | 杨极才 | Gas-carrying film concentrator |
| CN102060408A (en) * | 2010-12-07 | 2011-05-18 | 华电水处理技术工程有限公司 | Wastewater evaporating process and device system |
| CN201885590U (en) * | 2010-12-15 | 2011-06-29 | 湖南思为能源环保有限公司 | Aluminum oxide low-temperature flue gas waste heat heating and evaporation stock solution device |
| CN202909470U (en) * | 2012-03-24 | 2013-05-01 | 郭朝军 | Evaporation tower for performing evaporation treatment on salt-containing water using gas |
| CN103265091A (en) * | 2013-05-22 | 2013-08-28 | 魏华 | Mechanical ventilation forced circulation evaporation device and liquid material evaporation method |
| CN203281049U (en) * | 2013-06-19 | 2013-11-13 | 温州市森博轻工机械有限公司 | Single-effect external circulation vacuum concentrator |
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| CN104069643A (en) | 2014-10-01 |
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