CN203428945U - Mechanical ventilation forced-circulation evaporation device - Google Patents
Mechanical ventilation forced-circulation evaporation device Download PDFInfo
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- CN203428945U CN203428945U CN201320282969.3U CN201320282969U CN203428945U CN 203428945 U CN203428945 U CN 203428945U CN 201320282969 U CN201320282969 U CN 201320282969U CN 203428945 U CN203428945 U CN 203428945U
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- evaporation
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- delivery system
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Abstract
The utility model provides a mechanical ventilation forced-circulation evaporation device and a liquid material evaporation method thereof, and aims to effectively improve the operation reliability of an evaporation system, and reduce energy consumption and operation cost. The device comprises an evaporation container (10), a liquid material circulation system, a hot air delivery system and a tail gas collection and exhaust system, wherein the evaporation container (10) is sealed, and a discharge pipe (11) is arranged at the bottom of the evaporation container (10); initial and terminated ends of the liquid material circulation system are respectively positioned below and above the liquid level (A) in the evaporation container (10); the terminated end of the hot air delivery system is communicated with a cavity of the evaporation container (10); the tail gas collection and exhaust system is communicated with the cavity above the liquid level (A) in the evaporation container (10).
Description
Technical field
The utility model relates to liquid material evaporation unit, can be used for the processing of liquid material evaporation concentration or trade effluent.
Background technology
For used water difficult to degradate (B/C value is lower than 0.3), high-salt wastewater (salinity in sodium-chlor higher than 0.5%wt), at present main treatment technology has that evaporation, film are processed, advanced oxidation, enters generate subsequent chemical industry section process through above-mentioned processed waste water (less salt, can be biochemical).
For evaporation technique, the theoretical steam of current single-action, economic benefits and social benefits, triple effect, quadruple effect consumes approximately 1.10,0.57,0.40,0.30 tons of steam/ton water, approximately 242 yuan, 125 yuan, 88 yuan, 66 yuan of corresponding ton wastewater treatment steam costs, if add, the actual motion costs such as recirculated cooling water, electrical consumption further go up.In addition, common tubular type heating chamber+separate chamber evaporation technique stops up causes such as (salt crystallization, greasy dirt, calcium foulings etc.), the more difficult steady running of evaporation equipment due to heating tube burn into.As for function of mechanical steam recompression technology (MVR), function of mechanical steam recompression type evaporating, concentrating and crystallizing (MVC) evaporation technique, because vaporization temperature is generally higher than 60 ℃, steam consumption is equivalent to 7～12 effects, and direct operating cost is all not less than 45 yuan/ton of waste water, and running cost declines to some extent.But MVR, MVC evaporation technique still face the problems such as flow passage components burn into heating tube (interchanger) obstruction, general liquid, its operation steady in a long-term still has and necessarily faces certain challenge.In addition, the vapour compressor of MVR, MVC device is mainly derived from abroad, causes one-time investment to rise violently higher with after service cost.For adopting evaporation to carry out material, concentrate similar to above-mentioned trade effluent evaporation process situation.
For membrane technology, domestic main production microfiltration membrane (MF), ultra-filtration membrane (UF), be that colloid or suspension class material are more effective and economical to waste water composition at present, inapplicable for hardly degraded organic substance and the salt of solubilised state.For sodium filter membrane (NF), reverse osmosis membrane (RO), main manufacturer is offshore company, and the application of the product heavy industrialization of domestic production producer need to be checked by putting into practice.NF, RO film are directly processed high-concentration waste water (or in advance suspended substance, wet goods being carried out to pre-treatment) and are still faced irreversible blockage problem, and the flux decline of film is very fast.Meanwhile, the dense water of NF, RO (organic content 0.5%wt is above, salinity in sodium-chlor higher than 1.0%wt) still needs further processing, cannot solve all waste water completely.
For high-level oxidation technology, domestic many employing hydrogen peroxide catalytic oxidations (as Fenton), electrolytic oxidation, ozone oxidation, photochemical catalytic oxidation etc. at present.Due to oxidation technology selective oxidation difficulty, can not realize preferential oxidation hardly degraded organic substance, oxidant consumption amount is larger, and running cost is still higher.Even according to the hydrogen peroxide of 1.0%wt (30%wt) or 50～100ppm ozone (ozone 10%wt, oxygen 90%wt) dosage, only the cost of oxygenant is all at 20 yuan/ton more than waste water (the power set running cost that oxygen-free agent adds).
In addition, high-level oxidation technology can not solve the problem of salt, even if the waste water after oxidation improves wastewater biodegradability, in generate subsequent gasifying device, the high problem of salinity is still unresolved, its steady running more difficult (salinity fluctuation of trade effluent causes the interior solvency concentration of the cytolemma of bacterium to change, and bacterial activity is subject to suppressing more by force).At present common solution be high-salt wastewater after advanced oxidation, follow-up thin up is reduced to biochemistry by salinity and accepts scope, causes thus water resource waste and total amount of pollutants discharge to increase along with the increase of extension rate, pollution emission reduction difficulty.Domestic tap water price is approximately at 2.0～10.0 yuan/ton, the cost of wastewater dilution and extension rate linear dependence.In addition, install whole operation stability and be limited to into water fluctuation, the operation stability fluctuation of oxidation unit water outlet and biochemical device water outlet is all larger.
How solving the problems such as domestic industry waste water (or material is concentrated) running cost is high, device operation stability is poor, the whole production domesticization of device is key issues that this patent quasi-solution is determined.
Utility model content
Technical problem to be solved in the utility model is to provide a kind of power ventilation forced circulation evaporation device, effectively to increase the serviceability of vapo(u)rization system, reduces energy consumption and running cost.
It is as follows that the utility model solves the technical scheme that above technical problem adopts:
Power ventilation forced circulation evaporation device of the present utility model, is characterized in that it comprises: container for evaporation, the liquid material recycle system, hot gas delivery system and exhaust collection blowdown system; Container for evaporation is airtight, and its bottom arranges drainage conduit; The initiating terminal of the liquid material recycle system, terminal lay respectively in container for evaporation under liquid level, on; The terminal of hot gas delivery system and the intracavity inter-connection of container for evaporation; The initiating terminal of exhaust collection blowdown system is connected with the cavity on liquid level in container for evaporation.
The beneficial effects of the utility model are, because vaporization temperature is lower and approach normal pressure operation, liquid material in container for evaporation (the especially viscous material after crystallization) does not participate in heat exchange, and container for evaporation fouling probability, general liquid probability are very low, and system stable operation improves a lot; Each device all can be realized production domesticization, is conducive to reduce device capital cost; Owing to evaporating the source of thermal source, be ambient air, technology waste gas, general facilities waste gas, recirculated cooling water, steam condensate etc., effectively solved the higher problem of existing evaporation unit energy consumption, and running cost is significantly reduced.
Accompanying drawing explanation
This specification sheets comprises as next width accompanying drawing:
Fig. 1 is the structural representation of a kind of power ventilation forced circulation evaporation of the utility model device embodiment 1;
Fig. 2 is the structural representation of a kind of power ventilation forced circulation evaporation of the utility model device embodiment 2;
Member and corresponding mark in figure: container for evaporation 10, drainage conduit 11, packing layer 12; Liquid material circulation line 21, pump 22, liquid-inlet pipe 23; Admission passage 31, thermal source transfer lime 32, blower fan 33, interchanger 34; Exhaust emissions pipeline 41, vent gas treatment container 42.
Embodiment
Below in conjunction with drawings and Examples, the utility model is further illustrated.
With reference to Fig. 1, power ventilation forced circulation evaporation device of the present utility model, it comprises: container for evaporation 10, the liquid material recycle system, hot gas delivery system and exhaust collection blowdown system; Container for evaporation 10 is airtight, and its bottom arranges drainage conduit 11; The initiating terminal of the liquid material recycle system, terminal lay respectively under the interior liquid level A of container for evaporation 10, on; The intracavity inter-connection of the terminal of hot gas delivery system and container for evaporation 10; The initiating terminal of exhaust collection blowdown system is connected with the cavity on the interior liquid level A of container for evaporation 10.
Power ventilation forced circulation evaporation device of the present utility model is mainly used in the processing of liquid material evaporation concentration or trade effluent, and its step comprises:
1. pending liquid material is conveyed in container for evaporation 10, and carries out pump circulation by the liquid material recycle system.
2. through hot gas delivery system to passing into hot gas in container for evaporation 10 or suction hot gas evaporates.The temperature of hot gas is 5～300 ℃ (fixed with calorific value that can supplying heat source), and the volume ratio of institute's hot gas that passes into and container for evaporation 10 liquid material internal circulating loads is 10～15000:1(with calorific value that can supplying heat source calmly, m
3.h
-1/ m
3.h
-1).Thermal source is from least one in general facilities waste gas, technology waste gas, ambient air, recirculated cooling water, steam condensate, steam, electrically heated.
3. by exhaust collection blowdown system by the collection and confinement of gases in container for evaporation 10 upper spaces to container for evaporation 10.Tail gas condensing qualifiedly can directly discharge by detecting, or phlegma is transported to subsequent wastewater treatment system processes, or tail gas (or the non-condensable gas after aforementioned condensation) is as the treated qualified rear discharge of waste gas.
4. by drainage conduit 11, the enriched material that is deposited on container for evaporation 10 bottoms is delivered to outside container for evaporation 10.The enriched material of Industrial Wastewater Treatment need be tested according to GB5085.1-3, presses Hazardous wastes, general refuse processing, or carry out resource reutilization according to its value according to qualification result.
With reference to Fig. 1, the described liquid material recycle system comprises liquid material circulation line 21 and pump 22 and liquid-inlet pipe 23 is thereon set, the initiating terminal of liquid material circulation line 21 is fixedly connected on the bottom of container for evaporation 10, and its terminal extends into cavitys more than container for evaporation 10 liquid level A.Described hot gas delivery system comprises admission passage 31, blower fan 33 and thermal source transfer lime 32, and admission passage 31 is connected with thermal source transfer lime 32.
In container for evaporation 10, also can pack filler into, filler can adopt a kind of or combination in the wrong filler of oblique, honeycomb filler, S ripple filler, trapezoidal filler etc., and filling ratio (filler volume and container for evaporation 10 volume ratios) is 10～80%.With reference to Fig. 2, in described container for evaporation 10, on liquid level A, liquid material recycle system terminal part is provided with packing layer 12.Described hot gas delivery system comprises admission passage 31 and is attached thereto the thermal source transfer lime 32 connecing, blower fan 33 is set in the space at packing layer more than 12.
See figures.1.and.2, described hot gas delivery system also comprises interchanger 34, and thermal source transfer lime 32 is connected with admission passage 31 by interchanger 34.Interchanger 34 can be arranged in container for evaporation 10, also interchanger 34 can be set, and directly hot blast is passed in container for evaporation 10.Thermal source is from least one in general facilities waste gas, technology waste gas, ambient air, recirculated cooling water, steam condensate, steam, electrically heated, and gas derives from least one in ambient air, industrial gaseous waste, general facilities waste gas.
See figures.1.and.2, described exhaust collection blowdown system generally comprises tail gas discharging pipe 41 and is attached thereto the vent gas treatment container 42 connecing.
Embodiment 1:
Certain project daily output 40 tons/hour of used water difficult to degradate of saliferous (chemical oxygen demand (COD) 0.5～30%wt, inorganic salt 1.0～30.0%wt, oil-contg 0.01～1.2%wt), belongs to Hazardous wastes according to < < country this waste water of Hazardous wastes catalogue > >.If process according to Hazardous wastes, its processing cost is 1800～3000 yuan/ton up to the 172～288 Wan/Tian， unit direct processing costs of waste water.For addressing this problem, this project waste water 1 cover three-effect evaporation and condensation device that started, a day processing cost is 13.4～20.2 ten thousand yuan/day (containing waste treatment costs), the direct processing cost of unit waste water is 140～210 yuan/ton.But device start soon, and the situations such as fouling, heating tube obstruction, general liquid appear in this device successively, effluent quality fluctuation greatly, causes heavy burden to follow-up biochemical system.Simultaneously, due to reasons such as brine corrosion, high temperature evaporation, foulings, heating chamber (shell and tube) turnover rate is 1 time/week of 1 time/March, heating chamber detergent line, irregular general liquid 1 time, water outlet chemical oxygen demand (COD) between 0.2～3.0%wt, go out salinity water between 0.2～1.5%wt.Meanwhile, for ease of the operation discharge of dope, evaporation dope shifts while reaching 7～15% solid content from vaporizer, and execute-in-place condition is more severe.
With reference to Fig. 1, for solving said apparatus unsteady phenomena and the high problem of working cost, this project has adopted power ventilation forced circulation evaporation device of the present utility model, and concrete technical measures are as follows:
Wastewater treatment scale is 40 tons/hour, and water quality characteristic is chemical oxygen demand (COD) 0.5～30%wt, inorganic salt 1.0～30.0%wt, oil-contg 0.01～1.2%wt, ammonia-nitrogen content 0.02～1.5%wt.The low-temperature heat source that enterprise provides or waste heat source are that the circulating cooling water yield is 2500-3000m
3/ h(temperature is 42～45 ℃), Incineration of waste tail gas 2800～3100m
3/ h(temperature is 150～220 ℃), coal firing boiler waste gas 120000～152000m
3/ h(temperature is 150～220 ℃).Evaporation unit waste water internal recycling amount is 1800～2200m
3/ h, gas-water ratio 700-800:1(gas insufficient section is mended with ambient air, the long-term medial temperature of local environment air is 28 ℃), design evaporator room temperature is 32 ± 2 ℃.Device exhaust is introduced waste water station by Liqiud-gas mixing device and is discharged after biochemical treatment as aerobic aeration oxygen source.Refuse after concentrated is solid-state (water ratio is 40～50%), regularly migrates out vapo(u)rization system.The dope problem that no longer has three-effect evaporation and condensation, execute-in-place environment significantly takes a turn for the better.Because vaporization temperature is normal temperature substantially, evaporation unit changes to glass steel material by the titanium material of triple effect evaporation, and the relative triple effect evaporation of cost of investment is saved more than 70%.Device moves the maintenance of the day-to-day operation except blower fan and pump in 3 months continuously, does not run into fouling, obstruction, the general liquid problem of triple-effect evaporation plant again.The running cost of this engineering is mainly from blower fan and waste water circulation pump electric power consumption, and day operation cost is 384～960 yuan (not containing refuse processing cost, through steady running, within 3 months, investigating result), and the direct processing cost of unit waste water is 0.4～1.2 yuan/ton.The result of waste gas being carried out to condensation test shows, its phlegma chemistry oxygen requirement is that 0.1～0.2%wt, salinity (take sodium-chlor) are 0.02～0.1%wt, is better than the water quality of triple effect evaporation phlegma.
Embodiment 2:
With reference to Fig. 2, wastewater treatment scale is 4 tons/hour, and water quality characteristic is chemical oxygen demand (COD) 0.2～1.0%wt, inorganic salt 1.0～8.0%wt, oil-contg 0～0.01%wt, ammonia-nitrogen content 0.02～1.5%wt.The low-temperature heat source that enterprise provides is ambient air (the long-term medial temperature of current ambient air is 28 ℃), and evaporation unit waste water internal recycling amount is 160～250m
3/ h, gas-water ratio 800-1200:1, inside establishes the wrong filler (filling ratio is 60%) of oblique, and design evaporator room temperature is 28 ± 3 ℃.Device exhaust stimulates the menstrual flow and enters waste water station after condensation and further process, and non-condensable gas further enters follow-up exhaust treatment system.Refuse after concentrated is solid-state (water ratio is 40～50%), regularly migrates out vapo(u)rization system.Continuous and steady operation does not run into general liquid, fouling, the blockage problem of three-effect evaporation and condensation for 1 year.The running cost of this engineering is mainly from blower fan, waste water circulation pump electric power, not solidifying vent gas treatment and phlegma biochemical treatment.Wherein the running cost of this device is 0.8～1.5 yuan/ton, and total system running cost (containing evaporation, vent gas treatment, phlegma biochemical treatment) is 2.0～5.0 yuan/ton (not containing refuse processing costs).Phlegma chemistry oxygen requirement is that 0.06～0.15%wt, salinity (take sodium-chlor) are 0.02～0.1%wt.
Claims (6)
1. a power ventilation forced circulation evaporation device, is characterized in that it comprises: container for evaporation (10), the liquid material recycle system, hot gas delivery system and exhaust collection blowdown system; Container for evaporation (10) is airtight, and its bottom arranges drainage conduit (11); The initiating terminal of the liquid material recycle system, terminal lay respectively under the interior liquid level of container for evaporation (10) (A), on; The intracavity inter-connection of the terminal of hot gas delivery system and container for evaporation (10); The initiating terminal of exhaust collection blowdown system is connected with the cavity on the interior liquid level of container for evaporation (10) (A).
2. a kind of power ventilation forced circulation evaporation device as claimed in claim 1, it is characterized in that: the described liquid material recycle system comprises liquid material circulation line (21) and pump (22) and liquid-inlet pipe (23) is thereon set, the initiating terminal of liquid material circulation line (21) is fixedly connected on the bottom of container for evaporation (10), and its terminal extends in the above cavity of container for evaporation (10) liquid level (A).
3. a kind of power ventilation forced circulation evaporation device as claimed in claim 1, it is characterized in that: described hot gas delivery system comprises admission passage (31), blower fan (33) and thermal source transfer lime (32), admission passage (31) is connected with thermal source transfer lime (32).
4. a kind of power ventilation forced circulation evaporation device as claimed in claim 3, is characterized in that: described hot gas delivery system also comprises interchanger (34), and thermal source transfer lime (32) is connected with admission passage (31) by interchanger (34).
5. a kind of power ventilation forced circulation evaporation device as claimed in claim 1, is characterized in that: described exhaust collection blowdown system comprises tail gas discharging pipe (41) and is attached thereto the vent gas treatment container (42) connecing.
6. a kind of power ventilation forced circulation evaporation device as claimed in claim 1, is characterized in that: in described container for evaporation (10), on liquid level (A), liquid material recycle system terminal part is provided with packing layer (12); Described hot gas delivery system comprises admission passage (31) and is attached thereto the thermal source transfer lime (32) connecing, blower fan (33) is set in the space more than packing layer (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320282969.3U CN203428945U (en) | 2013-05-22 | 2013-05-22 | Mechanical ventilation forced-circulation evaporation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320282969.3U CN203428945U (en) | 2013-05-22 | 2013-05-22 | Mechanical ventilation forced-circulation evaporation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203428945U true CN203428945U (en) | 2014-02-12 |
Family
ID=50057996
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320282969.3U Expired - Fee Related CN203428945U (en) | 2013-05-22 | 2013-05-22 | Mechanical ventilation forced-circulation evaporation device |
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| Country | Link |
|---|---|
| CN (1) | CN203428945U (en) |
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2013
- 2013-05-22 CN CN201320282969.3U patent/CN203428945U/en not_active Expired - Fee Related
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140212 Termination date: 20160522 |