CN103265091A - Mechanical ventilation forced circulation evaporation device and liquid material evaporation method - Google Patents
Mechanical ventilation forced circulation evaporation device and liquid material evaporation method Download PDFInfo
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- CN103265091A CN103265091A CN2013101938861A CN201310193886A CN103265091A CN 103265091 A CN103265091 A CN 103265091A CN 2013101938861 A CN2013101938861 A CN 2013101938861A CN 201310193886 A CN201310193886 A CN 201310193886A CN 103265091 A CN103265091 A CN 103265091A
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Abstract
The invention provides a mechanical ventilation forced circulation evaporation device and a liquid material evaporation method which are used for improving the operation reliability of an evaporation system and reducing the energy consumption and the operation cost. The mechanical ventilation forced circulation evaporation device comprises an evaporation container (10), a liquid material circulation system, a hot air conveying system and a tail gas collecting discharging system, wherein the evaporation container (10) is sealed, and a discharging pipe (11) is arranged at the bottom of the evaporation container (10); the initialing end and the terminal end of the liquid material circulation system are respectively positioned below and above a liquid level (A) inside the evaporation container (10); the terminal end of the air conveying system is communicated with a cavity of the evaporation container (10); and the initialing end of the tail gas collecting discharging system is communicated with a cavity above the liquid level (A) in the evaporation container (10).
Description
Technical field
The present invention relates to liquid material evaporation unit and method of evaporating, can be used for the processing of liquid material evaporation concentration or trade effluent.
Background technology
For used water difficult to degradate (the B/C value is lower than 0.3), high-salt wastewater (salinity is higher than 0.5%wt in sodium-chlor), at present main treatment technology has that evaporation, film are handled, advanced oxidation, enters generate subsequent chemical industry section through above-mentioned processed waste water (less salt, can be biochemical) and handles.
For evaporation technique, the theoretical steam of present single-action, economic benefits and social benefits, triple effect, quadruple effect consumes about 1.10,0.57,0.40,0.30 tons of steam/ton water, about 242 yuan, 125 yuan, 88 yuan, 66 yuan of corresponding ton wastewater treatment steam costs are if add that actual motion costs such as recirculated cooling water, electrical consumption further go up.In addition, common tubular type heating chamber+separate chamber's evaporation technique is because the heating tube burn into stops up causes such as (salt crystallization, greasy dirt, calcium foulings etc.), the more difficult steady running of evaporation equipment.As for mechanical vapour recompression (MVR), mechanical vapour recompression type evaporating, concentrating and crystallizing (MVC) evaporation technique, because vaporization temperature generally is higher than 60 ℃, the steam consumption is equivalent to 7～12 imitates, and direct operating cost all is not less than 45 yuan of/ton waste water, and running cost descends to some extent.But MVR, MVC evaporation technique still face problems such as flow passage components burn into heating tube (interchanger) obstruction, general liquid, and 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, and it is higher with after service cost to cause one-time investment to rise violently.Concentrate similar to above-mentioned trade effluent evaporation process situation for adopting evaporation to carry out material.
For membrane technology, domestic main production microfiltration membrane (MF), ultra-filtration membrane (UF) are that colloid or suspension class material are more effective and economical to the waste water composition at present, and be 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 product heavy industrialization of domestic production producer is used and need be checked by putting into practice.NF, RO film are directly handled high-concentration waste water (or in advance suspended substance, wet goods being carried out pre-treatment) and are still faced irreversible blockage problem, and the flux decay of film is very fast.Simultaneously, the dense water of NF, RO (organic content 0.5%wt above, salinity be higher than 1.0%wt in sodium-chlor) still needs further to handle, and can't solve all waste water fully.
For high-level oxidation technology, domestic many employing hydrogen peroxide catalytic oxidations (as Fenton), electrolytic oxidation, ozone oxidation, photochemical catalytic oxidation etc. at present.Because oxidation technology selective oxidation difficulty can not realize the preferential oxidation hardly degraded organic substance, the oxidant consumption amount is bigger, and running cost is still higher.Even according to hydrogen peroxide (30%wt) or 50～100ppm ozone (ozone 10%wt, the oxygen 90%wt) dosage of 1.0%wt, only the cost of oxygenant is all at 20 yuan/ton more than the waste water (the power set running cost that the oxygen-free agent adds).
In addition, high-level oxidation technology can not solve the problem of salt, the high problem of salinity is still unresolved in the follow-up biochemical device even the waste water after oxidation improves wastewater biodegradability, its steady running is difficulty (the salinity fluctuation of trade effluent causes the interior solvency concentration of cytolemma of bacterium to change, and bacterial activity is subjected to suppressing more by force).After common solution was high-salt wastewater process advanced oxidation at present, follow-up thin up was reduced to biochemistry with salinity and accepts scope, caused water resource waste thus and pollute total amount increasing the pollution emission reduction difficulty along with the increase of extension rate.Domestic tap water price is greatly about 2.0～10.0 yuan/ton, the cost of wastewater dilution and extension rate linear dependence.In addition, the whole operation stability of device is subject to into water fluctuation, and the operation stability fluctuation of oxidation unit water outlet and biochemical device water outlet is all bigger.
How solving domestic industry waste water (or material concentrates) running cost height, installing problems such as operation stability is relatively poor, the whole production domesticization of device is key issues that this patent quasi-solution is determined.
Summary of the invention
Technical problem to be solved by this invention provides a kind of power ventilation forced circulation evaporation device, with the serviceability of effective increase vapo(u)rization system, cuts down the consumption of energy and running cost.
The present invention solves the technical scheme that above technical problem adopts: a kind of power ventilation forced circulation evaporation device of the present invention 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 the container for evaporation under the liquid level, on; The terminal of hot gas delivery system and the intracavity inter-connection of container for evaporation; Cavity in the initiating terminal of exhaust collection blowdown system and the container for evaporation on the liquid level is connected.
Another technical problem to be solved by this invention provides a kind of liquid material method of evaporating that uses above-mentioned power ventilation forced circulation evaporation device, this method comprises the steps: 1. pending liquid material to be conveyed in the container for evaporation, and carries out pump circulation by the liquid material recycle system; 2. feed hot gas in the container for evaporation or suction hot gas evaporates through the hot gas delivery system; 3. by the exhaust collection blowdown system with the collection and confinement of gases in the container for evaporation upper space to container for evaporation; 4. be delivered to outside the container for evaporation by the settling of drainage conduit with the container for evaporation bottom.
The invention has the beneficial effects as follows, because vaporization temperature is lower and move near normal pressure, liquid material in the container for evaporation (the especially stickiness material after the 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 the device capital cost; Because the source of evaporation thermal source is ambient air, technology waste gas, general facilities waste gas, recirculated cooling water, steam condensate etc., has solved existing evaporation unit energy consumption problem of higher effectively, and running cost is reduced significantly.
Description of drawings
This specification sheets comprises following two width of cloth accompanying drawings:
Fig. 1 is the structural representation of a kind of power ventilation forced circulation evaporation of the present invention device embodiment 1;
Fig. 2 is the structural representation of a kind of power ventilation forced circulation evaporation of the present invention device embodiment 2.
Member and corresponding mark among the 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
The present invention is further described below in conjunction with drawings and Examples.
With reference to Fig. 1, a kind of power ventilation forced circulation evaporation device of the present invention, 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 in the container for evaporation 10 under the liquid level A, on; The intracavity inter-connection of the terminal of hot gas delivery system and container for evaporation 10; Cavity in the initiating terminal of exhaust collection blowdown system and the container for evaporation 10 on the liquid level A is connected.
This device 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 the container for evaporation 10, and carries out pump circulation by the liquid material recycle system.
2. feed hot gas in the container for evaporation 10 or suction hot gas evaporates through the hot gas delivery system.The temperature of hot gas is 5～300 ℃ (but fixed with the calorific value of supplying heat source), but the volume ratio of institute's hot gas that feeds and container for evaporation 10 liquid material internal circulating loads is 10～15000:1(with the calorific value of supplying heat source calmly, m
3.h
-1/ m
3.h
-1).At least a from general facilities waste gas, technology waste gas, ambient air, recirculated cooling water, steam condensate, steam, the electrically heated of thermal source.
3. by the exhaust collection blowdown system with the collection and confinement of gases in container for evaporation 10 upper spaces to container for evaporation 10.The tail gas condensation then can directly be discharged by detection is qualified, perhaps phlegma is transported to the subsequent wastewater treatment system and handles, and perhaps tail gas (or the non-condensable gas after the aforementioned condensation) is as the treated qualified back discharging of waste gas.
4. the enriched material that will be deposited on container for evaporation 10 bottoms by drainage conduit 11 is delivered to outside the container for evaporation 10.The enriched material of Industrial Wastewater Treatment needs the test according to GB5085.1-3, presses Hazardous wastes, general waste treatment according to qualification result, or carries out resource reutilization according to its value.
With reference to Fig. 1, the described liquid material recycle system comprises liquid material circulation line 21 and setting pump 22 and liquid-inlet pipe 23 thereon, 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 the above cavity of 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.
The filler of also can packing in the container for evaporation 10, filler can adopt a kind of or combination in the wrong filler of oblique, honeycomb filler, S ripple filler, the trapezoidal filler etc., and filling ratio (filler volume and container for evaporation 10 volume ratios) is 10～80%.With reference to Fig. 2, in the 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 that connects, in the space of packing layer more than 12 blower fan 33 is set.
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, directly hot blast is fed in the container for evaporation 10.At least a from general facilities waste gas, technology waste gas, ambient air, recirculated cooling water, steam condensate, steam, the electrically heated of thermal source, gas then derives from ambient air, industrial gaseous waste, the general facilities waste gas at least a.
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 that connects.
Embodiment 1:
40 tons/hour (chemical oxygen demand (COD) 0.5～30%wt, inorganic salt 1.0～30.0%wt, oil-contg 0.01～1.2%wt) belong to Hazardous wastes according to " national Hazardous wastes catalogue " this waste water to certain project daily output saliferous used water difficult to degradate.If handle according to Hazardous wastes, its processing cost is up to 172～2,880,000/sky, and the direct processing cost of unit waste water is 1800～3000 yuan/ton.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 (not containing the waste treatment cost), the direct processing cost of unit waste water is 140～210 yuan/ton.But the device start soon, and situations such as fouling, heating tube obstruction, general liquid appear in this device successively, and the effluent quality fluctuation greatly causes heavy burden to follow-up biochemical system.Simultaneously, owing 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, the water outlet chemical oxygen demand (COD) between 0.2～3.0%wt, go out salinity water between 0.2～1.5%wt.Simultaneously, for ease of the operation discharging of dope, the evaporation dope shifts from vaporizer when reaching 7～15% solid contents, and the execute-in-place condition is more abominable.
With reference to Fig. 1, for solving the unstable situation of said apparatus and the high problem of working cost, this project has adopted power ventilation forced circulation evaporation device and liquid material method of evaporating.Concrete technical measures are as follows:
The 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 2500-3000m for the recirculated cooling water amount
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 the aerobic aeration oxygen source.Refuse after concentrating is solid-state (water ratio is 40～50%), regularly migrates out vapo(u)rization system.No longer have the dope problem of three-effect evaporation and condensation, the execute-in-place environment significantly takes a turn for the better.Because vaporization temperature is normal temperature substantially, evaporation unit changes to the glass reinforced plastic 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 operation did not continuously run into fouling, obstruction, the general liquid problem of triple effect evaporation device in 3 months again except the day-to-day operation of blower fan and pump is safeguarded.The running cost of this engineering is mainly from blower fan and waste water recycle pump electric power consumption, and the day operation cost is 384～960 yuan (do not contain the waste treatment cost, investigated the result in 3 months through steady running), and the direct processing cost of unit waste water is 0.4～1.2 yuan/ton.The result who waste gas is carried out condensation test shows that its phlegma chemistry oxygen requirement is that 0.1～0.2%wt, salinity (in 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, the 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, in establish the wrong filler (filling ratio is 60%) of oblique, design evaporator room temperature is 28 ± 3 ℃.Device exhaust stimulates the menstrual flow and enters waste water station after the condensation and further handle, and non-condensable gas further enters follow-up exhaust treatment system.Refuse after concentrating is solid-state (water ratio is 40～50%), regularly migrates out vapo(u)rization system.The continous-stable operation did not run into general liquid, fouling, the blockage problem of three-effect evaporation and condensation in 1 year.The running cost of this engineering is mainly from blower fan, waste water recycle pump electric power, vent gas treatment and phlegma biochemical treatment with fixed attention.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 the waste treatment cost).Phlegma chemistry oxygen requirement is that 0.06～0.15%wt, salinity (in sodium-chlor) are 0.02～0.1%wt.
Claims (9)
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 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 setting pump (22) and liquid-inlet pipe (23) thereon, 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), and 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 1, it 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) that connects.
5. a kind of power ventilation forced circulation evaporation device as claimed in claim 1 is characterized in that: in the 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) that connects, blower fan (33) is set in the space more than packing layer (12).
6. a kind of power ventilation forced circulation evaporation device as claimed in claim 1, it is characterized in that: described hot gas delivery system also comprises interchanger (34), thermal source transfer lime (32) is connected with admission passage (31) by interchanger (34).
7. adopt the liquid material method of evaporating as a kind of power ventilation forced circulation evaporation device as described in any claim of claim 1 to 6, comprise the steps:
1. pending liquid material is conveyed in the container for evaporation (10), and carries out pump circulation by the liquid material recycle system;
2. feed hot gas in the container for evaporation (10) or suction hot gas evaporates through the hot gas delivery system;
3. pass through the exhaust collection blowdown system collection and confinement of gases that container for evaporation (10) upper space is interior to container for evaporation (10);
4. the enriched material that will be deposited on container for evaporation (10) bottom by drainage conduit (11) is delivered to outside the container for evaporation (10).
8. liquid material method of evaporating as claimed in claim 7, it is characterized in that: described step 2. in, the temperature that enters the hot gas of vapor vessel (10) is 5～300 ℃, the volume ratio of the hot gas that feeds and container for evaporation (10) liquid material internal circulating load be 10～15000:1.
9. liquid material method of evaporating as claimed in claim 7, it is characterized in that: described step 2. in, at least a from general facilities waste gas, technology waste gas, ambient air, recirculated cooling water, steam condensate, steam, the electrically heated of thermal source, gas source are at least a in ambient air, industrial gaseous waste, the general facilities waste gas.
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Cited By (6)
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| CN103848530A (en) * | 2014-03-03 | 2014-06-11 | 无锡市中岳石化设备有限公司 | DDISO-integrated synchronous oxidation and desalination device |
| CN103848464A (en) * | 2014-02-28 | 2014-06-11 | 长沙威保特环保科技有限公司 | Treatment method of low-temperature evaporation high-concentration sewage |
| CN104069643A (en) * | 2014-07-17 | 2014-10-01 | 魏华 | Gas cycling evaporation method and device |
| CN104826348A (en) * | 2015-04-13 | 2015-08-12 | 铜仁学院 | Extraction mixed liquor treatment method by recycling steam condensate waste heat |
| CN107964775A (en) * | 2017-11-10 | 2018-04-27 | 珠海格力电器股份有限公司 | A kind of heating system and method for laundry waste heat recovery |
| CN108285187A (en) * | 2018-01-26 | 2018-07-17 | 北京四方鼎泰环保科技有限公司 | The evaporation and crystallization system of high-efficient energy-saving environment friendly and application |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103848464A (en) * | 2014-02-28 | 2014-06-11 | 长沙威保特环保科技有限公司 | Treatment method of low-temperature evaporation high-concentration sewage |
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| CN104826348A (en) * | 2015-04-13 | 2015-08-12 | 铜仁学院 | Extraction mixed liquor treatment method by recycling steam condensate waste heat |
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| CN107964775A (en) * | 2017-11-10 | 2018-04-27 | 珠海格力电器股份有限公司 | A kind of heating system and method for laundry waste heat recovery |
| CN107964775B (en) * | 2017-11-10 | 2019-05-03 | 珠海格力电器股份有限公司 | A kind of heating system and method for the recycling of laundry waste heat |
| CN108285187A (en) * | 2018-01-26 | 2018-07-17 | 北京四方鼎泰环保科技有限公司 | The evaporation and crystallization system of high-efficient energy-saving environment friendly and application |
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Application publication date: 20130828 |