CN103203167A - Exhaust gas recovery method - Google Patents
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- CN103203167A CN103203167A CN2012104170017A CN201210417001A CN103203167A CN 103203167 A CN103203167 A CN 103203167A CN 2012104170017 A CN2012104170017 A CN 2012104170017A CN 201210417001 A CN201210417001 A CN 201210417001A CN 103203167 A CN103203167 A CN 103203167A
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- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The invention relates to an exhaust gas recovery method which comprises the following steps: (1) allowing exhaust gas to pass through an exhaust gas recovery system and dissolving the exhaust gas in water in a spraying manner so as to form recovery liquid with a certain concentration, wherein the temperature of the liquid is 20 to 50 DEG C; and (2) subjecting the prepared recovery liquid to distillation and condensation through a waste liquid rectification system, wherein a heat source of a shell layer of the waste liquid rectification system is normal pressure steam with a temperature of 100 to 140 DEG C, recovery waste liquid is allowed to pass through the interior of a pipe layer of the waste liquid rectification system, the interior of the pipe layer is in a negative pressure state through pumping by a vacuum pump, and the negative pressure state can accelerate separation of a solvent and water in the waste liquid under the action of the external heat source of the shell layer. According to the invention, an exhaust gas recovery rectification apparatus recovers exhaust gas produced in industrial production through spraying and multiple distillations and has high efficiency; the exhaust gas is recovered and then reutilized, so energy saving and environmental protection are realized, the problem of exhaust gas treatment is effectively overcome and influence of irritant gas on the health of operation personnel can be substantially reduced.
Description
Technical field
The present invention relates to the chemical industry field, set and relate to a kind of gas recovery method.
Background technology
When engineering resins such as production immersion coating polyimides, need use a large amount of intensive polar solvents, obtain impregnated fabric after the oven dry of drying case, solvent ratios reaches more than 60%, directly be discharged in the air and can cause certain pollution to environment, general mode or the gas sampling recycling of burning that adopt.And relevant environmental protection equipment is invested 1,000,000 yuan, and is very expensive, therefore is restricted aspect recycling.These solvents all have certain volatility in addition, environment to production site has very big influence, in the excitant environment, work for a long time and can damage human body, therefore need a cover waste gas acquisition system to collect the gas that contains solvent that drying is come out, intensive polar solvent such as DMF etc. are soluble in water, and boiling point and water difference are bigger, about 45 degree, therefore can adopt the mode of water spray to collect, obtain certain density recovery liquid, reclaim by distillation then.
Summary of the invention
Technical problem to be solved by this invention provides and a kind ofly can effectively reclaim the gas recovery method that waste gas carries out cycling and reutilization.
For solving the problems of the technologies described above, the invention provides a kind of gas recovery method, comprise the steps:
(1) waste gas is passed through gas recovery system, with the mode of spray that waste gas is soluble in water, form certain density recovery liquid, fluid temperature is 20-50 ℃;
The recovery liquid that (2) will make is by waste liquor rectification system distillation condensation, and the shell thermal source of described waste liquor rectification system is atmospheric steam, and temperature is 100-140 ℃; The logical waste liquid that reclaims extracts by vavuum pump in the pipe layer in the pipe layer of described waste liquor rectification system, is negative pressure state, and negative pressure state can be accelerated waste liquid under the effect of shell external heat source, and solvent separates with water.
Described gas recovery method also comprises: the cloth of immersion solvent is dried, and bake out temperature is higher than the boiling point of solvent, produces waste gas in the drying course, and collects waste gas by the gas collection exhaust system.
Use the waste gas of above-mentioned gas recovery method to reclaim rectifier unit, comprising: dipping drying system, gas collection exhaust system, gas recovery system, waste liquor rectification system.
Described dipping drying system comprises: the resin glue stock tank, the liquid level that links to each other with the resin glue stock tank pipeline of making up the difference, with the liquid level cloth apparatus that soaks that pipeline is connected of making up the difference, the lifting side picking device that bottom soaking cloth apparatus, links to each other, be located at the electrical heating drying room that soaks the cloth apparatus top, be located at the many groups fabric guide roll in the electrical heating drying room, be located at the exhaust outlet on electrical heating drying room top, the impregnation drying system adopts Liquid level compensator self filler mode, pass through induction level, by-pass valve control is opened, implement filling up of glue, reduce labour intensity greatly, stable dipping liquid level can improve the uniformity of the coating of resin.
Described gas collection exhaust system comprises: gas exhaust piping, gas storage terminal and low speed air-introduced machine, described gas exhaust piping comprises that one vertically arranges and bottom port circular arc pipe down, the edge of the bottom port of this circular arc pipe bends to the center, and form an annular groove, described annular groove is used for collecting the condensed fluid on the circular arc pipe, anti-pipeline condensate liquid passes back into the electrical heating drying room, and the oven dry operation of impregnated fabric is had a negative impact, the inner ring of this annular groove is connected with the exhaust outlet of electrical heating drying room, this annular groove bottom is connected with for the sewage draining exit of getting rid of condensed fluid, be connected with the blowdown control piper on this sewage draining exit, described gas storage terminal links to each other with gas exhaust piping, the output of described gas storage terminal links to each other with the low speed air-introduced machine, the bottom of described gas storage terminal is provided with valve, is used for the condensed fluid in the periodic cleaning pipeline.
Described gas recovery system links to each other with the low speed air-introduced machine of gas collection exhaust system, and described gas recovery system comprises: S shape or arch horizontal positioned in order to prevent that liquid level in the gas recovery system from replenishing the air inlet pipe of overflowing when excessive and the recovery tower that links to each other with this air inlet pipe.
Described waste liquor rectification system comprises: the temperature control igniter, burner with temperature control igniter control igniting, the steam oven that links to each other with burner, with first alembic, after-fractionating jar, the 3rd alembic and the drainer that steam oven links to each other successively by steam pipework, the vavuum pump that links to each other with drainer.
Described recovery tower bottom is provided with first accumulator tank and second accumulator tank, described first accumulator tank is located at the top of second accumulator tank, this first accumulator tank links to each other with air inlet pipe and links to each other with second accumulator tank by collecting switching valve, described first accumulator tank top is provided with first packing layer, the first spray district, interlayer, second packing layer, the second spray district successively, the described first spray district links to each other with first accumulator tank by circulation line, water pump with the second spray district, be used for the recovery liquid of first accumulator tank is carried out circulated sprinkling, make recovery liquid concentration higher.
Described recovery tower top is provided with a plurality of moisturizing cycling switch, be used for to collect the condensed water that the waste liquor rectification system produces and recycle, the outside of described first accumulator tank and second accumulator tank is connected with liquid level gauge respectively, be used for showing the liquid level of first accumulator tank and second accumulator tank and control that described second accumulator tank links to each other with the waste liquor rectification system by water pump.
Described first alembic, the after-fractionating jar, the 3rd alembic, drainer includes shell and pipe layer, described pipe layer comprises upper tube layer and lower tube layer, described waste liquid import by pipeline successively with the after-fractionating jar, the lower tube layer of first alembic links to each other, the lower tube layer of described first alembic links to each other with the upper tube layer, and first alembic, the after-fractionating jar, the 3rd alembic, the upper tube layer of drainer links to each other successively, when passing through the lower tube layer of three alembics, can utilize the thermal energy differential of shell and pipe layer that waste liquid is carried out preheating, improve energy utilization rate, when entering the first rectifying jar, waste liquid has had certain temperature, can accelerate the time of rectifying, improve rectification efficiency, waste liquid passes through first alembic successively through the upper tube layer then, the after-fractionating jar, the distillation of the 3rd alembic.
Be equipped with valve between the pipe layer of described first alembic and after-fractionating jar, after-fractionating jar and the 3rd alembic, described valve is manual or electrically operated valve, can realize interface operation according to rectifying speed designs flow size and pressure, reduce the operation easier of recovery system.
The bottom of described after-fractionating jar, the bottom of the 3rd alembic, the middle part of drainer is equipped with the waste water accumulator tank, described waste water accumulator tank all links to each other with the pipe layer of described corresponding tank body, and described waste water accumulator tank links to each other with first accumulator tank of recovery tower by water pump respectively, described after-fractionating jar, the middle part of the 3rd alembic is equipped with tank, described two tanks link to each other with second condensing unit of drainer lower end by pipeline, described second cooling device is externally connected with cooling water pipe, described second cooling device links to each other by first cooling device of pipeline with the drainer upper end, the input of described first condensing unit links to each other with the 3rd alembic, and the described first cooling device output links to each other with back pool.
The middle part of described first alembic, after-fractionating jar, the 3rd alembic is equipped with pan tank, and described three pan tanks link to each other successively, and the output of the pan tank of described the 3rd alembic links to each other with the finished product jar through water pump.
Described steam oven links to each other with the shell of first alembic, after-fractionating jar, the 3rd alembic respectively by the road, what flow out in the described steam oven is water at atmospheric pressure steam, temperature is 100-140 ℃, because temperature is higher than the boiling point of water in the rectifier unit pipeline, progressively makes in water and the liquid solvent and separates.
Described steam oven is provided with steam pressure release valve, when the steam oven internal pressure is too high, can open steam pressure release valve and carry out step-down, described steam pipe is provided with temp controlled meter, temp controlled meter links to each other with the temperature control igniter by signal picker, pass through signals collecting, the realization burner is lighted a fire automatically, keep the outer vapor (steam) temperature of shell, be equipped with liquid level gauge on described three alembics, finished product jar, the drainer, by modes such as weight induction or liquid level inductions, form the recovery system liquid level alarm device, the alert rectifying liquid that in time circulates.
Described vavuum pump links to each other with the pipe layer of drainer, the steam that is used for extraction waste liquid pipeline enters condensation in the drainer, make the waste liquid pipeline be negative pressure state, accelerate waste liquid under the effect of shell external heat source solvent and moisture from, partial solvent is along with steam is siphoned away by negative pressure, for improving rectification effect, its condensation need be got off, therefore vavuum pump links to each other with the pipe layer of condensation hat, flue gas is cooled off, because the condensation temperature of solvent is different with water, earlier the waste liquid condensation is reclaimed, steam cools off recovery along with negative pressure device enters in second condensing unit, and gets back to continuation use in the solvent recovery unit by water pump.
Technique effect of the present invention: gas recovery method of the present invention reclaims the waste gas that produces in the industrial production by the mode of spray, repeatedly distillation, efficient is higher, carry out recycling after the recovery, energy-conserving and environment-protective, solve the problem of exhaust-gas treatment effectively, can reduce irritative gas greatly to operating personnel's health effect.
Description of drawings
For the present invention can clearerly be understood, below in conjunction with the drawings and specific embodiments the present invention is described in further detail:
Fig. 1 is the structural representation that waste gas of the present invention reclaims rectifier unit;
Fig. 2 is the partial enlarged drawing of described dipping drying system and gas collection exhaust system;
Fig. 3 is the partial enlarged drawing of described gas recovery system;
Fig. 4 is the partial enlarged drawing of described waste liquor rectification system;
Fig. 5 is the partial enlarged drawing that described gas collection exhaust system is connected with the dipping drying system.
Specific embodiment
As Fig. 1-4, a kind of gas recovery method of present embodiment comprises the steps:
(1) waste gas is passed through gas recovery system, with the mode of spray that waste gas is soluble in water, form certain density recovery liquid, fluid temperature is 20-50 ℃;
The recovery liquid that (2) will make is by waste liquor rectification system distillation condensation, and the shell thermal source of described waste liquor rectification system is atmospheric steam, and temperature is 100-140 ℃; The logical waste liquid that reclaims extracts by vavuum pump in the pipe layer in the pipe layer of described waste liquor rectification system, is negative pressure state, and negative pressure state can be accelerated waste liquid under the effect of shell external heat source, and solvent separates with water.
Described gas recovery method also comprises: the cloth of immersion solvent is dried, and bake out temperature is 160 ℃, produces waste gas in the drying course, and collects waste gas by the gas collection exhaust system.
A kind of waste gas of above-mentioned gas recovery method that uses reclaims rectifier unit, comprising: dipping drying system 1, gas collection exhaust system 2, gas recovery system 3, waste liquor rectification system 4.
Described dipping drying system 1 comprises: resin glue stock tank 1-1, the liquid level that links to each other with the resin glue stock tank 1-1 pipeline 1-2 that makes up the difference, soak cloth apparatus 1-3 with liquid level makes up the difference that pipeline is connected, the lifting side picking device 1-4 that bottom soaking cloth apparatus 1-3, links to each other, be located at the electrical heating drying room 1-5 that soaks cloth apparatus 1-3 top, be located at the many groups fabric guide roll 1-6 in the electrical heating drying room 1-5, be located at the exhaust outlet 1-7 on electrical heating drying room 1-5 top, impregnation drying system 1 adopts Liquid level compensator self filler mode, pass through induction level, by-pass valve control is opened, implement filling up of glue, reduce labour intensity greatly, stable dipping liquid level can improve the uniformity of the coating of resin.
Described gas collection exhaust system 2 comprises: gas exhaust piping 2-1, gas storage terminal 2-2 and low speed air-introduced machine 2-3, described gas exhaust piping 2-1 comprises that one vertically arranges and bottom port circular arc pipe 2-4 down, the edge of the bottom port of this circular arc pipe 2-4 bends to the center, and form an annular groove 2-11, the inner ring of this annular groove 2-11 is connected with the exhaust outlet 1-7 of electrical heating drying room 1-5, this annular groove 2-11 bottom is connected with for the sewage draining exit of getting rid of condensed fluid, be connected with blowdown control piper 2-12 on this sewage draining exit, described annular groove 2-11 is used for collecting the condensed fluid on the circular arc pipe 2-4, anti-pipeline condensate liquid passes back into electrical heating drying room 1-5, and the oven dry operation of impregnated fabric is had a negative impact, described gas storage terminal 2-2 links to each other with gas exhaust piping 2-1, the output of described gas storage terminal 2-2 links to each other with low speed air-introduced machine 2-3, the bottom of described gas storage terminal 2-2 is provided with valve 2-21, is used for the condensed fluid in the periodic cleaning pipeline.
Described gas recovery system 3 links to each other with the low speed air-introduced machine 2-3 of gas collection exhaust system 2, and described gas recovery system 2 comprises: S shape or arch horizontal positioned in order to prevent that liquid levels in the gas recovery system 3 from replenishing the air inlet pipe 3-1 that overflows when excessive and the recovery tower 3-2 that links to each other with this air inlet pipe 3-1.
Described waste liquor rectification system 4 comprises: temperature control igniter 4-1, burner 4-2 with temperature control igniter control igniting, the steam oven 4-3 that links to each other with burner, the first alembic 4-4, the after-fractionating jar 4-5, the 3rd alembic 4-6 that link to each other by steam pipework with steam oven 4-3, the drainer 4-7 that links to each other with the 3rd alembic 4-6, the vavuum pump 4-8 that links to each other with drainer 4-7.
Described recovery tower 3-2 bottom is provided with the first accumulator tank 3-21 and the second accumulator tank 3-22, the described first accumulator tank 3-21 is located at the top of the second accumulator tank 3-22, this first accumulator tank 3-21 links to each other with air inlet pipe 3-1 and links to each other with the second accumulator tank 3-22 by collecting switching valve 3-23, described first accumulator tank 3-21 top is provided with the first packing layer 3-24 successively, the first spray district 3-25, interlayer 3-26, the second packing layer 3-27, the second spray district 3-28, the described first spray district 3-25 and the second spray district 3-27 pass through circulation line, water pump links to each other with the first accumulator tank 3-21, be used for the recovery liquid of the first accumulator tank 3-21 is carried out circulated sprinkling, make recovery liquid concentration higher.
Described recovery tower 3-2 top is provided with a plurality of moisturizing cycling switch 3-28, be used for collecting the condensed water of waste liquor rectification system 4 generations and recycling, the outside of the described first accumulator tank 3-21 and the second accumulator tank 3-22 is connected with liquid level gauge respectively, be used for showing the liquid level of first accumulator tank and second accumulator tank and control that the described second accumulator tank 3-22 links to each other with waste liquor rectification system 4 by water pump.
The described first alembic 4-4, after-fractionating jar 4-5, the 3rd alembic 4-6, drainer 4-7 includes shell and pipe layer, described pipe layer comprises upper tube layer and lower tube layer, described waste liquid import by pipeline successively with after-fractionating jar 4-5, the lower tube layer of the first alembic 4-4 links to each other, the lower tube layer of the described first alembic 4-4 links to each other with the upper tube layer, and the first alembic 4-4, after-fractionating jar 4-5, the 3rd alembic 4-6, the upper tube layer of drainer 4-7 links to each other successively, when passing through the lower tube layer of three alembics, can utilize the thermal energy differential of shell and pipe layer that waste liquid is carried out preheating, improve energy utilization rate, when entering the first rectifying jar, waste liquid has had certain temperature, can accelerate the time of rectifying, improve rectification efficiency, waste liquid passes through the first alembic 4-4 successively through the upper tube layer then, after-fractionating jar 4-5, the 3rd alembic 4-6 distillation.
Be equipped with valve between the pipe layer of the described first alembic 4-4 and after-fractionating jar 4-5, after-fractionating jar 4-5 and the 3rd alembic 4-6, described valve is manual or electrically operated valve, can be according to rectifying speed designs flow size and pressure, realize interface operation, reduce the operation easier of recovery system.
The bottom of described after-fractionating jar 4-5, the bottom of the 3rd alembic 4-6, the middle part of drainer 4-7 is equipped with the waste water accumulator tank, described waste water accumulator tank all links to each other with the pipe layer of described corresponding tank body, and the output of described waste water accumulator tank links to each other with the first accumulator tank 3-21 of recovery tower by water pump respectively, described after-fractionating jar 4-5, the middle part of the 3rd alembic 4-6 is equipped with condensate draining, described two condensate drainings link to each other with the second condensing unit 4-72 of drainer lower end by pipeline, the described second cooling device 4-72 is externally connected with cooling water pipe, the described second cooling device 4-72 links to each other by the first cooling device 4-71 of pipeline with drainer 4-7 upper end, the input of the described first condensing unit 4-71 links to each other with the 3rd alembic 4-6, and the described first cooling device 4-71 output links to each other with back pool.
The middle part of the described first alembic 4-4, after-fractionating jar 4-5, the 3rd alembic 4-6 is equipped with pan tank, and described three pan tanks link to each other successively, and the output of the pan tank of described the 3rd alembic 4-6 links to each other with the finished product jar through water pump.
Described steam oven 4-3 links to each other with the shell of the first alembic 4-4, after-fractionating jar 4-5, the 3rd alembic 4-6 respectively by the road, what flow out among the described steam oven 4-3 is water at atmospheric pressure steam, temperature is 100-140 ℃, because temperature is higher than the boiling point of water in the rectifier unit pipeline, progressively makes in water and the liquid solvent and separate.
Described steam oven 4-3 is provided with steam pressure release valve 4-31, when the steam oven internal pressure is too high, can open steam pressure release valve 4-31 and carry out step-down, described steam pipe is provided with temp controlled meter, temp controlled meter links to each other with temperature control igniter 4-1 by signal picker, pass through signals collecting, the realization burner is lighted a fire automatically, keep the outer vapor (steam) temperature of shell, be equipped with liquid level gauge on described three alembics, finished product jar, the drainer, by modes such as weight induction or liquid level inductions, form the recovery system liquid level alarm device, the alert rectifying liquid that in time circulates.
Described vavuum pump 4-8 links to each other with the pipe layer of drainer 4-7, the steam that is used for extraction waste liquid pipeline enters condensation among the drainer 4-7, make the waste liquid pipeline be negative pressure state, accelerate waste liquid under the effect of shell external heat source solvent and moisture from, partial solvent is along with steam is siphoned away by negative pressure, for improving rectification effect, its condensation need be got off, therefore vavuum pump 4-8 links to each other with the pipe layer of drainer 4-7, flue gas is cooled off, because the condensation temperature of solvent is different with water, earlier the waste liquid condensation is reclaimed, steam cools off recovery along with negative pressure device enters in the second condensing unit 4-72, and gets back to continuation use in the solvent recovery unit by water pump.
Obviously, above-described embodiment only is for example of the present invention clearly is described, and is not to be restriction to embodiments of the present invention.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here need not also can't give all embodiments exhaustive.And these belong to apparent variation or the change that spirit of the present invention extended out and still are among protection scope of the present invention.
Claims (10)
1. a gas recovery method is characterized in that comprising the steps:
(1) waste gas is passed through gas recovery system, with the mode of spray that waste gas is soluble in water, form certain density recovery liquid, reclaiming liquid temp is 20-50 ℃;
The recovery liquid that (2) will make is by the distillation condensation of waste liquor rectification system; The logical waste liquid that reclaims extracts by vavuum pump in the pipe layer in the pipe layer of described waste liquor rectification system, is negative pressure state.
2. gas recovery method as claimed in claim 1, it is characterized in that: described gas recovery method also comprises: the cloth of immersion solvent is dried, and bake out temperature is higher than the boiling point of solvent, and the waste gas that produces in the drying course is collected by the gas collection exhaust system.
3. one kind is used the waste gas of aforesaid right requirement 1 or 2 described gas recovery methods to reclaim rectifier unit, it is characterized in that comprising: dipping drying system, gas collection exhaust system, gas recovery system, waste liquor rectification system;
Described dipping drying system comprises: resin glue stock tank, the liquid level that links to each other with the resin glue stock tank make up the difference pipeline, with liquid level make up the difference that pipeline is connected soak cloth apparatus, with soak lifting side picking device that the cloth apparatus bottom links to each other, be located at the electrical heating drying room that soaks above the cloth apparatus, be located at many groups fabric guide roll in the electrical heating drying room, be located at the exhaust outlet on electrical heating drying room top;
Described gas collection exhaust system comprises: gas exhaust piping, gas storage terminal and low speed air-introduced machine, described gas exhaust piping comprises that one vertically arranges and bottom port circular arc pipe down, the edge of the bottom port of this circular arc pipe bends to the center, and form an annular groove, the inner ring of this annular groove is connected with the exhaust outlet of electrical heating drying room, this annular groove bottom is connected with for the sewage draining exit of getting rid of condensed fluid, be connected with the blowdown control piper on this sewage draining exit, described gas storage terminal links to each other with gas exhaust piping, the output of described gas storage terminal links to each other with the low speed air-introduced machine, and the bottom of described gas storage terminal is provided with valve;
Described gas recovery system links to each other with the low speed air-introduced machine of gas collection exhaust system, and described gas recovery system comprises: S shape or arch horizontal positioned in order to prevent that liquid level in the gas recovery system from replenishing the air inlet pipe of overflowing when excessive and the recovery tower that links to each other with this air inlet pipe;
Described waste liquor rectification system comprises: the temperature control igniter, burner with temperature control igniter control igniting, the steam oven that links to each other with burner, first alembic, after-fractionating jar, the 3rd alembic that link to each other by steam pipework with steam oven, the drainer that links to each other with the 3rd alembic, the vavuum pump that links to each other with drainer, the bottom of described the 3rd alembic is provided with the waste liquid import, and this waste liquid import links to each other by pipeline with the output of recovery tower.
4. waste gas as claimed in claim 3 reclaims rectifier unit, it is characterized in that: described recovery tower bottom is provided with first accumulator tank and second accumulator tank, described first accumulator tank is located at the top of second accumulator tank, this first accumulator tank links to each other with air inlet pipe and links to each other with second accumulator tank by collecting switching valve, described first accumulator tank top is provided with first packing layer, the first spray district, interlayer, second packing layer, the second spray district successively, and the described first spray district links to each other with first accumulator tank by circulation line, water pump with the second spray district.
5. waste gas as claimed in claim 4 reclaims rectifier unit, it is characterized in that: described recovery tower top is provided with a plurality of moisturizing cycling switch, the outside of described first accumulator tank and second accumulator tank is connected with liquid level gauge respectively, and described second accumulator tank links to each other with the waste liquor rectification system by water pump.
6. waste gas as claimed in claim 5 reclaims rectifier unit, it is characterized in that: described first alembic, after-fractionating jar, the 3rd alembic, drainer include shell and pipe layer, described pipe layer comprises upper tube layer and lower tube layer, described waste liquid import links to each other with the lower tube layer of after-fractionating jar, first alembic successively by pipeline, the lower tube layer of described first alembic links to each other with the upper tube layer, and the upper tube layer of first alembic, after-fractionating jar, the 3rd alembic, drainer links to each other successively;
Be equipped with valve between the upper tube layer of described first alembic and after-fractionating jar, after-fractionating jar and the 3rd alembic, described valve is manually-operated gate;
Or, being equipped with valve between the pipe layer of described first alembic and after-fractionating jar, after-fractionating jar and the 3rd alembic, described valve is electrically operated valve.
7. waste gas as claimed in claim 6 reclaims rectifier unit, it is characterized in that: the bottom of described after-fractionating jar, the bottom of the 3rd alembic, the middle part of drainer is equipped with the waste water accumulator tank, described waste water accumulator tank all links to each other with the pipe layer of described corresponding tank body, and described waste water accumulator tank links to each other with first accumulator tank of recovery tower by water pump respectively, described after-fractionating jar, the middle part of the 3rd alembic is equipped with tank, described two tanks link to each other with second condensing unit of drainer lower end by pipeline, described second cooling device is externally connected with cooling water pipe, described second cooling device links to each other by first cooling device of pipeline with the drainer upper end, the input of described first condensing unit links to each other with the 3rd alembic, and the described first cooling device output links to each other with back pool.
8. waste gas as claimed in claim 7 reclaims rectifier unit, it is characterized in that: the middle part of described first alembic, after-fractionating jar, the 3rd alembic is equipped with pan tank, described three pan tanks link to each other successively, and the output of the pan tank of described the 3rd alembic links to each other with the finished product jar through water pump.
9. waste gas as claimed in claim 8 reclaims rectifier unit, it is characterized in that: described steam oven links to each other with the shell of first alembic, after-fractionating jar, the 3rd alembic respectively by the road, what flow out among the described steam oven 4-3 is water at atmospheric pressure steam, and temperature is 100-140 ℃.
10. waste gas as claimed in claim 9 reclaims rectifier unit, it is characterized in that: described steam oven is provided with steam pressure release valve, described steam pipe is provided with temp controlled meter, temp controlled meter links to each other with the temperature control igniter by signal picker, is equipped with liquid level gauge on described three alembics, finished product jar, the drainer; Described vavuum pump and drainer.
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| CN2012104170017A CN103203167A (en) | 2012-10-26 | 2012-10-26 | Exhaust gas recovery method |
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| CN2012104170017A CN103203167A (en) | 2012-10-26 | 2012-10-26 | Exhaust gas recovery method |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102989188A (en) * | 2012-10-26 | 2013-03-27 | 镇江铁科橡塑制品有限公司 | Exhaust gas recovery and rectification device |
| CN104208977A (en) * | 2014-01-28 | 2014-12-17 | 北京华晟环能科技有限公司 | Organic working medium purifying and recycling system |
| CN107149835A (en) * | 2017-06-06 | 2017-09-12 | 石泰山 | Concentration and processing method of a kind of low concentration containing volatile organic compounds |
| CN108928983A (en) * | 2018-07-25 | 2018-12-04 | 山东鑫蓝新能源科技有限公司 | A kind of sewage low temperature distillation processing system |
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| CN102989188A (en) * | 2012-10-26 | 2013-03-27 | 镇江铁科橡塑制品有限公司 | Exhaust gas recovery and rectification device |
| CN202860155U (en) * | 2012-10-26 | 2013-04-10 | 镇江铁科橡塑制品有限公司 | Waste gas recycle and rectification device |
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| GB756892A (en) * | 1953-06-18 | 1956-09-12 | Philips Nv | Improvements in low temperature gas rectification columns |
| CN101274153A (en) * | 2008-04-02 | 2008-10-01 | 南京工业大学 | Method for synthetically reutilizing ammonia and hydrogen in tail gas discharged from indigo production |
| CN102161534A (en) * | 2011-01-26 | 2011-08-24 | 上海凯展环保科技有限公司 | Device for processing dimethylamine exhaust gas and wastewater |
| CN202283419U (en) * | 2012-02-01 | 2012-06-27 | 淄博鲁华同方化工有限公司 | Device for separating and purifying mono-olefin from C5 |
| CN102989188A (en) * | 2012-10-26 | 2013-03-27 | 镇江铁科橡塑制品有限公司 | Exhaust gas recovery and rectification device |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102989188A (en) * | 2012-10-26 | 2013-03-27 | 镇江铁科橡塑制品有限公司 | Exhaust gas recovery and rectification device |
| CN104208977A (en) * | 2014-01-28 | 2014-12-17 | 北京华晟环能科技有限公司 | Organic working medium purifying and recycling system |
| CN104208977B (en) * | 2014-01-28 | 2016-04-06 | 北京华晟环能科技有限公司 | Organic working medium purifying and recycling system |
| CN107149835A (en) * | 2017-06-06 | 2017-09-12 | 石泰山 | Concentration and processing method of a kind of low concentration containing volatile organic compounds |
| CN107149835B (en) * | 2017-06-06 | 2019-01-18 | 石泰山 | A kind of concentration and processing method of the low concentration containing volatile organic compounds |
| CN108928983A (en) * | 2018-07-25 | 2018-12-04 | 山东鑫蓝新能源科技有限公司 | A kind of sewage low temperature distillation processing system |
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Application publication date: 20130717 |