CN102091497A - Method for treating waste gas discharged from continuously running laboratory - Google Patents
Method for treating waste gas discharged from continuously running laboratory Download PDFInfo
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- CN102091497A CN102091497A CN2011100065731A CN201110006573A CN102091497A CN 102091497 A CN102091497 A CN 102091497A CN 2011100065731 A CN2011100065731 A CN 2011100065731A CN 201110006573 A CN201110006573 A CN 201110006573A CN 102091497 A CN102091497 A CN 102091497A
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Abstract
The invention relates to the technical field of air-exhaust waste gas treatment for chemical laboratory and solves the problem of efficiently treating the waste gas under the condition of low airflow resistance. By using the technical scheme of high-degree atomization and vortex separation, the purposes of boosting gas/liquid contact without using padding and meeting gas/liquid separation demand are achieved while the purpose of fully decreasing the airflow resistance of treating equipment is achieved; by using the technical scheme of spraying thinned alkali liquor and inertia high boiling point organic liquid at the same time, the technical problem of gathering and treating water-soluble exhaust gas and oil-soluble exhaust gas is solved; and by using an oil-water separator and a film short-range distiller bypass to generate a loop, the problem of continuous running and continuous generation of treated oil-soluble exhaust gas by using high boiling point organic liquid is solved.
Description
Technical field
The present invention relates to the air draft waste gas pollution control and treatment technical field that chemical laboratory is used, solve the efficient exhaust-gas treatment scheme problem under the low-flow resistance condition.
Background technology
In the time of chemical laboratory work, there is chemical contamination gas to occur, for making the laboratory user of service avoid the chemical contamination injury, need to implement air draft, in the air-flow that is excluded, usually owing to due to the polytropy characteristics of research contents, the water-soluble waste gas (such as dust, acid mist, water-miscible organic solvent volatile matter) and the oil-soluble waste gas (such as the oil-soluble organic solvent volatile matter) of uncertain ratio can occur.
Water or sig water spray mode is the main means that solve dust and acid mist pollution in the chemical laboratory exhaust system at present; But in traditional spray administration way, in order to increase the gas-liquid touch opportunity, all adopted the technological means of filler usually, liquid flows from above, dusty gas from following to up; This employing filler increases the technical scheme of gas-liquid touch opportunity, has in fact caused the air draft gas-flow resistance to increase severely, thereby has caused the power consumption sharp increase of exhaust blower and operation noise to increase severely.
At the oil-soluble waste gas in the chemical laboratory exhaust system, the most frequently used way is to adopt the charcoal absorption means at present; In fact not only adsorption capacity is limited for active carbon, replacing program complexity, the replacement cost costliness also can be owing to changing the untimely desorption secondary pollution that occurs, also cause the air draft gas-flow resistance to increase severely simultaneously, thereby caused the power consumption of exhaust blower to increase severely and the sharp increase of operation noise.
And in the chemical laboratory discharging waste gas, contain simultaneously under the situation of water-soluble waste gas and oil-soluble waste gas, unless use spray abatement equipment and active carbon abatement equipment simultaneously, otherwise can't once solve governing problem.
And use the gas-flow resistance of two equipment simultaneously, will up under the air draft gas-flow resistance situation that does not adopt abatement equipment more than 3 times.Huge gas-flow resistance and unsatisfactory waste gas pollution control and treatment effect, caused serious laboratory discharging waste gas to administer technology barrier, in fact many laboratory exhaust gas abatement equipment are for reaching the target that reduces gas-flow resistance, emptied filler and active carbon wherein by the user, become pendulum decorations.
In view of the defective that above-mentioned existing waste gas pollution control and treatment technology exists, in the face of chemical laboratory waste gas pollution control and treatment target, we need a kind of technical scheme, can satisfy following several performance requirements simultaneously:
The low-flow resistance, efficient governance efficiency once solves the management goal of water-soluble waste gas and oil-soluble waste gas, and solves the continuous improvement running technology problem of oil-soluble waste gas.
Summary of the invention
The present invention intends providing a kind of low-flow resistance, high waste gas is imitated governance efficiency, once solve water-soluble waste gas and oil-soluble waste gas management goal simultaneously, and solve the uninterrupted continuously laboratory discharging waste gas processing method of administering the technical scheme problem of operation of oil-soluble waste gas.
The present invention realizes that the technical scheme that its technical performance target is adopted is such:
1. the laboratory discharging waste gas processing method of a continuously-running, one of its feature is to have adopted the mode of the atomization of liquid of liquid delivery pump/pipeline and fog-spray nozzle, in the passage of laboratory discharging waste gas, with sig water and inertia higher boiling organic liquid, fully atomizing respectively, the sig water that water-soluble waste gas in the discharging waste gas of laboratory is fully atomized captures neutralization, and the inertia higher boiling organic liquid dissolving that the oil-soluble waste gas in the discharging waste gas of laboratory is fully atomized absorbs; Two of its feature also is to have adopted double-entry cyclone separator, with the sig water and the inertia higher boiling organic liquid mixed airflow of described laboratory discharging waste gas and described abundant atomizing, finishes gas-liquid separation in described double-entry cyclone separator; Three of its feature also is to have adopted oil water separator, and sig water and inertia higher boiling liquid organic mixture with discharging in the described double-entry cyclone separator obtain layering in described oil water separator; Four of its feature also has been to adopt the thin-membrane short-range distiller of bypass connected mode, can will from described oil water separator, compile, dissolving has absorbed the inertia higher boiling organic liquid of oil-soluble waste gas in the too much laboratory discharging waste gas, distillation removes described oil-soluble waste gas continuously, drops into circular flow then; Five of its feature also is described sig water after neutralization consumes, and can adopt the mode of replenishing alkali to keep acid-base value.
2. described waste gas processing method, the working method that it is characterized in that described sig water and inertia higher boiling organic liquid operating path and waste gas pollution control and treatment is such: pending laboratory discharging waste gas, by the whirlwind porch of blower fan high-speed pushing to double-entry cyclone separator; Described sig water, inertia higher boiling organic liquid are driven by liquid delivery pump respectively, in the whirlwind porch of double-entry cyclone separator, by the fog-spray nozzle high atomisation; Pending laboratory discharging waste gas is being carried sig water and the inertia higher boiling organic liquid that is atomized, and together enters in the whirlwind cylinder folder chamber of double-entry cyclone separator, air-flow takes place circle round, and occurs gas-liquid separation simultaneously; Air-flow after being removed water-soluble waste gas and having removed oil-soluble waste gas upwards overflows from the bottom of the center pipe of described double-entry cyclone separator, and sig water and inertia higher boiling organic liquor mixed liquor can be discharged from the bottom pipe of double-entry cyclone separator; The end that described sig water and inertia higher boiling organic liquor mixture enter oil water separator; Another liquid at oil water separator flows to end head, the sig water of layering, inertia higher boiling organic liquid are compiled respectively by overflow pipe, driven respectively by liquid delivery pump once more, carry the whirlwind porch that arrives double-entry cyclone separator by pipeline, constitute the elementary path of administering circular flow; On pipeline before and after the liquid delivery pump that drives inertia higher boiling organic liquor, a bypass circulation is arranged, the thin-membrane short-range distiller of a bypass connected mode in parallel, dissolved under the situation that has absorbed the oil-soluble waste gas in a large amount of laboratory discharging waste gas at inertia higher boiling organic liquid, can control by valve, from the outlet conduit of described liquid delivery pump, partly shunt inertia higher boiling organic liquor and enter thin-membrane short-range distiller, the mode that adopts continuous distillation to remove oil-soluble waste gas is regenerated, inertia higher boiling organic liquid after the regeneration, be directed to by pipeline in the suction inlet pipeline of described liquid delivery pump, constitute regeneration cycle; The collection that is condensed of described oil-soluble waste gas.
3. described waste gas processing method is characterized in that described double-entry cyclone separator, be one will be with one air-flow, through in the shunting every, be split into two strands of air-flows, the cut-in manner in opposite directions with 180 degree enters the whirlwind cylindrical cavity in two whirlwind porch of described cyclone separator; Its feature also is to have arranged atomization of liquid fog-spray nozzle in the whirlwind porch.
4. described waste gas processing method is characterized in that described oil water separator, is a casing that has the polylith dividing plate, dividing plate quantity greater than 2 less than 50; The arrangement of dividing plate constitutes the reciprocal trend of liquid stream; The liquid that flows out from described double-entry cyclone separator bottom flows to end head from a liquid and enters, after flowing to multiple stroke by a plurality of liquid, oil-water separation interface appears in other a upright end, flow out respectively, reenter liquid delivery pump, be admitted to aforesaid liquid spray head, reenter the exhaust-gas treatment circulation after the atomizing.
5. described waste gas processing method is characterized in that described film distillator, is a continuous still equipment of going up charging, bottom discharge; Dissolving has absorbed the inertia higher boiling organic liquid of oil-soluble waste gas in the too much laboratory discharging waste gas, enter from last charging aperture, flow downward with filminess along heated wall, lower boiling oil-soluble waste gas is evaporated, and condenses on condenser wall, and the oil-soluble waste gas that condensation compiles is compiled discharge, after inertia higher boiling organic liquid obtains regeneration by distillation, flow out thin-membrane short-range distiller, led back to suction inlet pipeline, finish the regeneration cycle of bypass into described liquid delivery pump by pipeline.
6. described waste gas processing method is characterized in that in the described sig water, and contained alkali can be NaOH, sodium carbonate; Its feature also is described inertia higher boiling organic liquid, can be atoleine, chlorocosanes, ethylene glycol phenyl ether, alkyd resins.
Be described further below in conjunction with accompanying drawing.
Description of drawings
Fig. 1 is the compound mode schematic perspective view of described double-entry cyclone separator and atomization of liquid fog-spray nozzle, wherein:
A is the top board of described double-entry cyclone separator;
B is the central circular airflow line of described double-entry cyclone separator;
C is the peripheral side plate of described double-entry cyclone separator;
D is the median septum of described double-entry cyclone separator, also is the peripheral circumferential plate of gyration airflow;
The air-flow import pipe of the described double-entry cyclone separator of G;
H is the shunting zone base plate of described double-entry cyclone separator;
I is the cylindrical cavity periphery wall that circles round of described double-entry cyclone separator;
J is the cylindrical cavity rounded bottom of circling round of described double-entry cyclone separator;
K is the liquid outlet down of described double-entry cyclone separator;
E is the one group of fog-spray nozzle that is placed on the whirlwind porch of described double-entry cyclone separator;
F is the other one group of fog-spray nozzle that is placed on the whirlwind porch of described double-entry cyclone separator;
Fig. 2 is the vertical view of described double-entry cyclone separator, wherein:
B is the central circular airflow line of described double-entry cyclone separator;
C is the peripheral side plate of described double-entry cyclone separator;
D is the median septum of described double-entry cyclone separator, also is the peripheral circumferential plate of gyration airflow;
The air-flow import pipe of the described double-entry cyclone separator of G;
K is the liquid outlet down of described double-entry cyclone separator;
E is the one group of fog-spray nozzle that is placed on the whirlwind porch of described double-entry cyclone separator;
F is the other one group of fog-spray nozzle that is placed on the whirlwind porch of described double-entry cyclone separator;
Fig. 3 is the Knock-Down Component figure of described double-entry cyclone separator, wherein:
A is the top board of described double-entry cyclone separator;
B is the central circular airflow line of described double-entry cyclone separator;
C is the peripheral side plate of described double-entry cyclone separator;
D is the median septum of described double-entry cyclone separator, also is the peripheral circumferential plate of gyration airflow;
The air-flow import pipe of the described double-entry cyclone separator of G;
H is the shunting zone base plate of described double-entry cyclone separator;
I is the cylindrical cavity periphery wall that circles round of described double-entry cyclone separator;
J is the cylindrical cavity rounded bottom of circling round of described double-entry cyclone separator;
K is the liquid outlet down of described double-entry cyclone separator;
E be placed on described double-entry cyclone separator the whirlwind porch-group fog-spray nozzle;
F is the other one group of fog-spray nozzle that is placed on the whirlwind porch of described double-entry cyclone separator;
Fig. 4 is described double-entry cyclone separator and described oil water separator, at the operation combining form schematic diagram that does not insert under the thin-membrane short-range distiller situation of bypass connected mode, wherein:
L is the outer wall of described oil water separator;
M is described dividing plate;
N is the profit handing-over interface under the profit layering situation;
O is the manifold trunk of upper strata inertia higher boiling organic liquid;
P is the manifold trunk of lower floor's sig water;
Q is the liquid delivery pump of inertia higher boiling organic liquid;
R is the liquid delivery pump of sig water;
S is the delivery pump outlet conduit of inertia higher boiling organic liquid;
T is the delivery pump outlet conduit of sig water;
U is the arm that inertia higher boiling organic liquid enters double-entry cyclone separator;
V is the arm that sig water enters double-entry cyclone separator;
Fig. 5 is the operation combining form schematic diagram under the described thin-membrane short-range distiller situation of inserting the bypass connected mode, wherein:
L is the outer wall of described oil water separator;
M is described dividing plate;
O is the manifold trunk of upper strata inertia higher boiling organic liquid;
P is the manifold trunk of lower floor's sig water;
Q is the liquid delivery pump of inertia higher boiling organic liquid;
R is the liquid delivery pump of sig water;
S is the delivery pump outlet conduit of inertia higher boiling organic liquid;
T is the delivery pump outlet conduit of sig water;
W is a thin-membrane short-range distiller;
W-1 is the vacuum pipe that thin-membrane short-range distiller is used
Fig. 6 is the connected mode that constitutes bypass circulation between described thin-membrane short-range distiller and described oil water separator and the liquid delivery pump, wherein:
L is the outer wall of described oil water separator;
M is the described dividing plate of described oil water separator;
N is the profit layering interfaces of described oil water separator;
O is the manifold trunk of upper strata inertia higher boiling organic liquid;
P is the manifold trunk of lower floor's sig water;
Q is the liquid delivery pump of inertia higher boiling organic liquid;
R is the liquid delivery pump of sig water;
S is the delivery pump outlet conduit of inertia higher boiling organic liquid;
T is the delivery pump outlet conduit of sig water;
W is a thin-membrane short-range distiller;
W-1 is the vacuum pipe that described thin-membrane short-range distiller is used;
W-2 is the conduction oil delivery channel of the heating interlayer used of described thin-membrane short-range distiller;
W-3 is the heat conductive oil inlet conduit of the heating interlayer used of described thin-membrane short-range distiller;
W-4 is the cooling liquid inlet conduit that described thin-membrane short-range distiller is used;
W-5 is the cooling liquid outlet conduit that described thin-membrane short-range distiller is used;
W-6 is the condensate liquid outlet of the low boiling oil-soluble waste gas of described thin-membrane short-range distiller;
Y is the arm valve on the delivery pump outlet conduit of described inertia higher boiling organic liquid;
X is the ingress pipe of described thin-membrane short-range distiller regeneration liquid to be separated.
The circulation of experimental laboratory air exhausting waste gas pollution control and treatment:
With water-soluble waste gas and oil-soluble waste gas, from the experimental laboratory air exhausting air-flow, catch, will remove then the experimental laboratory air exhausting air-flow of water-soluble waste gas and oil-soluble waste gas, be discharged into the process in the environment, be exactly the governance process for experimental laboratory air exhausting waste gas, referred to herein as administering circulation.
Governance process can be accomplished by following equipment scheme and system operation mode:
Adopt as shown in Figure 3 component structural and general assembly orbution, and according to constructional aspect after Fig. 1, the general assembly shown in Figure 2, build up described double-entry cyclone separator.
Such as Fig. 4, shown in Figure 5, with inertia higher boiling organic liquid and described sig water, be placed among the described oil water separator L, in the left side of the oil water separator end, respectively there are respectively a pipeline O and P in upper strata and lower floor, by liquid delivery pump Q and R, carry described inertia higher boiling organic liquid and sig water to three described double-entry cyclone separators.
As shown in Figure 1 and Figure 2, drive inertia higher boiling organic liquid and the sig water of coming by liquid delivery pump, by fog-spray nozzle E and fog-spray nozzle F, after high atomisation, follow the pending laboratory discharging waste gas that imports by airduct G, be divided into two-way by described dividing plate D, the in opposite directions form with 180 degree enters described two-way cyclone separator whirlwind entrance.
Because the cause of high atomisation, huge specific area (the big and isopyknic filler total surface area of total surface area) appears in sig water, water-soluble waste gas in the pending laboratory discharging waste gas contacts with described atomizing sig water occurrence of large-area, and most water-soluble waste gas will fully be absorbed neutralization by sig water; Same because the cause of high atomisation, huge specific area appears in described inertia higher boiling organic liquid, oil-soluble waste gas in the pending laboratory discharging waste gas contacts with described atomizing inertia higher boiling organic liquid occurrence of large-area, and nearly all oil-soluble waste gas will dissolve in the higher boiling organic liquid.
Through the laboratory discharging waste gas that sig water had washed and passed through the washing of inertia higher boiling organic liquid, finished purification treatment, through the air-flow that purifies, by described double-entry cyclone separator center pipe B, from bottom to top discharging.
As shown in Figure 4, compile sig water and the inertia higher boiling organic liquid of the mixing that obtains by the cyclone separator bottom pipe, entered the low order end of described oil water separator by the pipeline guiding; The mixed liquor of sig water and inertia higher boiling organic liquid moves ahead in the reciprocal liquid that a plurality of dividing plate M of described oil water separator consist of flows away the corridor, flow to the high order end of described oil water separator always; Finish the profit delaminating process in the process that back and forth flows of described mixing material left, when arriving high order end, upper strata inertia higher boiling organic liquid is collected by manifold trunk O, enters liquid delivery pump Q, is driven by liquid delivery pump and enters new circulation; The sig water of lower floor, P collects by manifold trunk, enters liquid delivery pump R, is driven by liquid delivery pump then and enters new circulation.
Inertia higher boiling organic liquid regeneration cycle:
Dissolve, received the inertia higher boiling organic liquid of too much oil-soluble waste gas, from the outlet conduit of liquid delivery pump Q
Among the S,, be diverted to described thin-membrane short-range distiller W by arm X and flow control valve Y, through continuous still, after removing most oil-soluble waste gas, return the process among the suction inlet pipeline O of delivery pump Q, be called as the regeneration cycle of inertia higher boiling organic liquid here.
As shown in Figure 5, on the outlet conduit S of liquid delivery pump Q, an arm X is arranged, on the X arm, a control valve Y is arranged.The aperture of control valve Y just can be regulated total output flow ratio that the inertia higher boiling organic liquid of exporting enters flow and the liquid delivery pump Q of arm X from liquid delivery pump Q.
As shown in Figure 6, described thin-membrane short-range distiller has a vacuum tube W-1, connects water towards pump, for described thin-membrane short-range distiller provides vacuum environment; Described thin-membrane short-range distiller also has a deep fat input pipe W-3, deep fat efferent duct W-2, and described thin-membrane short-range distiller has a coolant inlet pipe W-5, cooling fluid efferent duct W-4.
Come by arm X and control valve Y shunting, the inertia higher boiling organic liquid that has been full of oil-soluble waste gas, through behind the described thin-membrane short-range distiller, the oil-soluble waste gas that is dissolved in the inertia higher boiling organic liquid is distilled/the condensation enrichment, discharges by the W-6 pipeline; Removed the inertia higher boiling organic liquid of oil-soluble waste gas, returned suction inlet pipeline, finished regeneration cycle into liquid delivery pump Q through piping Z.
Continuously or the use regeneration cycle of intermittence:
Above-mentioned whole regeneration cycle can be one and follow and administer the process that circulation is carried out simultaneously continuously, also can be according to oil-soluble waste gas in inertia higher boiling organic liquid the adsorbance degree and regeneration cycle process that clearance-type starts.
To sum up, above-mentioned technical scheme is exactly:
Adopted high atomisation to add the technical scheme that whirlwind separates, reached the target of exempting to promote gas/liquid touch opportunity and gas/liquid separation requirement, reached the purpose of the gas-flow resistance of abundant reduction abatement equipment simultaneously with filler; The technical scheme that has adopted sig water and inertia higher boiling organic liquid to spray simultaneously, technical problem is administered in the capture that has solved water-soluble waste gas and oil-soluble waste gas simultaneously; Adopted the bypass regenerative circuit mode of oil water separator and thin-membrane short-range distiller, solved the higher boiling organic liquid and administered the continuous operation of the oil-soluble waste gas problem of uninterruptedly regenerating.
The specific embodiment 1
Adopt chlorocosanes as inertia higher boiling organic liquid; The sodium hydrate aqueous solution that adopts 10% concentration is as sig water.
Adopt continuous regeneration cycle mode, when administering periodic duty, implement regeneration cycle incessantly: the aperture of control valve Y, the shunting ratio of employing be liquid delivery pump Q total output flow 15%, flow to described thin-membrane short-range distiller W by arm X.
Vacuum pipe W-1 connects water towards pump, and the vacuum environment of 10～20mm water column is provided for described thin-membrane short-range distiller W;
To hot oil temperature～180 degree of W-3 input, less than the boiling point of inertia higher boiling organic liquid; Coolant temperature to coolant inlet pipe W-5 input is-10 degree.
The method of operation that the cyclic regeneration of describing through present embodiment circulates can guarantee that 99% water-soluble waste gas is caught eliminating by sig water; 99% oil-soluble waste gas can be caught by the dissolving of inertia higher boiling organic liquid, and by continuous regeneration cycle system, enrichment is also reclaimed out 99% oil-soluble waste gas.
The operation gas-flow resistance of whole system is reduced to and adopts 1/40 of conventional fillers formula spray system and active carbon governing system simultaneously, has only 50～70 handkerchiefs.
Owing to exempt to have used filler, so the equipment of the laboratory exhaust gas treating capacity of same scale, operating weight reduces to 1/5 of the weight of equipment that adopts the conventional fillers mode.
Because the method for having exempted to use active carbon to administer oil-soluble waste gas causes whole system can administer circular flow continuously, continuous regeneration cycle operation, and need not the problem that system's abatement functions has to suspend to occur because change active carbon.
The specific embodiment 2
Adopt paraffin oil as inertia higher boiling organic liquid; The aqueous sodium carbonate that adopts 15% concentration is as sig water.
Adopt the regeneration cycle mode in gap, when administering the circulation continuous operation, according to the oil-soluble waste gas degree of saturation situation in the output liquid of described liquid delivery pump Q, and (judge index of present embodiment is: in the discharging waste gas of laboratory to discharge oil-soluble exhaust gas concentration situation in the air-flow after the improvement of laboratory air draft waste gas, do not enter the preceding oil-soluble exhaust gas concentration of abatement equipment and be assumed to be 1 measurement unit, then through and improvement in the later discharge air-flow, same oil-soluble exhaust gas constituents content, if reached 1% measurement unit), then need intermittence ground to start the regeneration cycle of described inertia higher boiling organic liquid:
The aperture of control valve Y, the shunting ratio of employing be liquid delivery pump Q total output flow 50%, flow to described thin-membrane short-range distiller W by arm X.
Vacuum pipe W-1 connects water towards pump, for described thin-membrane short-range distiller provides～vacuum environment of 15mm water column;
To hot oil temperature～200 degree of W-3 input, less than the boiling point of inertia higher boiling organic liquid; Coolant temperature to coolant inlet pipe W-5 input is-5 degree.
The method of operation that the cyclic regeneration of describing through present embodiment circulates can guarantee that 99% water-soluble waste gas is caught eliminating by sig water; 99% oil-soluble waste gas can be caught by the dissolving of inertia higher boiling organic liquid, and be passed through the regeneration cycle system in gap, and enrichment is also reclaimed out 99% oil-soluble waste gas.
The operation gas-flow resistance of whole system is reduced to and adopts 1/40 of conventional fillers formula spray system and active carbon governing system simultaneously, has only 50～70 handkerchiefs.
Owing to exempt to have used filler, so the equipment of the laboratory exhaust gas treating capacity of same scale, operating weight reduces to 1/5 of the weight of equipment that adopts the conventional fillers mode.
Because the method for having exempted to use active carbon to administer oil-soluble waste gas causes whole system can administer circular flow continuously, regeneration cycle continuous or intermittence is moved, and need not the problem that system's abatement functions has to suspend to occur because change active carbon.
The specific embodiment 3
The mixed liquor that adopts ethylene glycol phenyl ether and alkyd resins is as inertia higher boiling organic liquid, and both volume ratios reach 1: 1; The sodium hydrate aqueous solution that adopts 15% concentration is as sig water.
Adopt the regeneration cycle mode in gap, when administering the circulation continuous operation, according to the oil-soluble waste gas degree of saturation situation in the output liquid of described liquid delivery pump Q, and (judge index of present embodiment is: in the discharging waste gas of laboratory to discharge oil-soluble exhaust gas concentration situation in the air-flow after the improvement of laboratory air draft waste gas, do not enter the preceding oil-soluble exhaust gas concentration of abatement equipment and be assumed to be 1 measurement unit, then through and improvement in the later discharge air-flow, same oil-soluble exhaust gas constituents content, if reached 1% measurement unit), then need intermittence ground to start the regeneration cycle of described inertia higher boiling organic liquid:
The aperture of control valve Y, the shunting ratio of employing be liquid delivery pump Q total output flow 50%, flow to described thin-membrane short-range distiller W by arm X.
Vacuum pipe W-1 connects water towards pump, for described thin-membrane short-range distiller provides～vacuum environment of 15mm water column;
To hot oil temperature～200 degree of W-3 input, less than the boiling point of inertia higher boiling organic liquid; Coolant temperature to coolant inlet pipe W-5 input is-5 degree.
The method of operation that the cyclic regeneration of describing through present embodiment circulates can guarantee that 99% water-soluble waste gas is caught eliminating by sig water; 99% oil-soluble waste gas can be caught by the dissolving of inertia higher boiling organic liquid, and be passed through the regeneration cycle system in gap, and enrichment is also reclaimed out 99% oil-soluble waste gas.
The operation gas-flow resistance of whole system is reduced to and adopts 1/40 of conventional fillers formula spray system and active carbon governing system simultaneously, has only 50～70 handkerchiefs.
Owing to exempt to have used filler, so the equipment of the laboratory exhaust gas treating capacity of same scale, operating weight reduces to 1/5 of the weight of equipment that adopts the conventional fillers mode.
Because the method for having exempted to use active carbon to administer oil-soluble waste gas causes whole system can administer circular flow continuously, regeneration cycle continuous or intermittence is moved, and need not the problem that system's abatement functions has to suspend to occur because change active carbon.
Claims (6)
1. the laboratory discharging waste gas processing method of a continuously-running, one of its feature is to have adopted the mode of the atomization of liquid of liquid delivery pump/pipeline and fog-spray nozzle, in the passage of laboratory discharging waste gas, with sig water and inertia higher boiling organic liquid, fully atomizing respectively, the sig water that water-soluble waste gas in the discharging waste gas of laboratory is fully atomized captures neutralization, and the inertia higher boiling organic liquid dissolving that the oil-soluble waste gas in the discharging waste gas of laboratory is fully atomized absorbs; Two of its feature also is to have adopted double-entry cyclone separator, with the sig water and the inertia higher boiling organic liquid mixed airflow of described laboratory discharging waste gas and described abundant atomizing, finishes gas-liquid separation in described double-entry cyclone separator; Three of its feature also is to have adopted oil water separator, and sig water and inertia higher boiling liquid organic mixture with discharging in the described double-entry cyclone separator obtain layering in described oil water separator; Four of its feature also has been to adopt the thin-membrane short-range distiller of bypass connected mode, can will from described oil water separator, compile, dissolving has absorbed the inertia higher boiling organic liquid of oil-soluble waste gas in the too much laboratory discharging waste gas, distillation removes described oil-soluble waste gas continuously, drops into circular flow then; Five of its feature also is described sig water after neutralization consumes, and can adopt the mode of replenishing alkali to keep acid-base value.
2. waste gas processing method according to claim 1, the working method that it is characterized in that described sig water and inertia higher boiling organic liquid operating path and waste gas pollution control and treatment is such: pending laboratory discharging waste gas, by the whirlwind porch of blower fan high-speed pushing to double-entry cyclone separator; Described sig water, inertia higher boiling organic liquid are driven by liquid delivery pump respectively, in the whirlwind porch of double-entry cyclone separator, by the fog-spray nozzle high atomisation; Pending laboratory discharging waste gas is being carried sig water and the inertia higher boiling organic liquid that is atomized, and together enters in the whirlwind cylinder folder chamber of double-entry cyclone separator, air-flow takes place circle round, and occurs gas-liquid separation simultaneously; Air-flow after being removed water-soluble waste gas and having removed oil-soluble waste gas upwards overflows from the bottom of the center pipe of double-entry cyclone separator, and sig water and inertia higher boiling organic liquor mixed liquor can be discharged from the bottom pipe of double-entry cyclone separator; The end that described sig water and inertia higher boiling organic liquor mixture enter oil water separator; Another liquid at oil water separator flows to end head, the sig water of layering, inertia higher boiling organic liquid are compiled respectively by overflow pipe, driven respectively by liquid delivery pump once more, carry the whirlwind porch that arrives double-entry cyclone separator by pipeline, constitute the elementary path of administering circular flow; On pipeline before and after the liquid delivery pump that drives inertia higher boiling organic liquor, a bypass circulation is arranged, the thin-membrane short-range distiller of a bypass connected mode in parallel, dissolved under the situation that has absorbed the oil-soluble waste gas in a large amount of laboratory discharging waste gas at inertia higher boiling organic liquid, can control by valve, from the outlet conduit of described liquid delivery pump, partly shunt inertia higher boiling organic liquor and enter thin-membrane short-range distiller, the mode that adopts continuous distillation to remove oil-soluble waste gas is regenerated, inertia higher boiling organic liquid after the regeneration, be directed to by pipeline in the suction inlet pipeline of described liquid delivery pump, constitute regeneration cycle; The collection that is condensed of described oil-soluble waste gas.
3. waste gas processing method according to claim 1, it is characterized in that described double-entry cyclone separator, be one will be with one air-flow, through in the shunting every, be split into two strands of air-flows, cut-in manner in opposite directions with 180 degree enters the whirlwind cylindrical cavity in two whirlwind porch of described cyclone separator; Its feature also is to have arranged atomization of liquid fog-spray nozzle in the whirlwind porch.
4. waste gas processing method according to claim 1 is characterized in that described oil water separator, is a casing that has the polylith dividing plate, dividing plate quantity greater than 2 less than 50; The arrangement of dividing plate constitutes the reciprocal trend of liquid stream; The liquid that flows out from described double-entry cyclone separator bottom flows to end head from a liquid and enters, after flowing to multiple stroke by a plurality of liquid, oil-water separation interface appears in other a upright end, flow out respectively, reenter liquid delivery pump, be admitted to aforesaid liquid spray head, reenter the exhaust-gas treatment circulation after the atomizing.
5. waste gas processing method according to claim 1 is characterized in that described film distillator, is a continuous still equipment of going up charging, bottom discharge; The inertia higher boiling organic liquid that dissolving has absorbed oil-soluble waste gas in the too much laboratory discharging waste gas enters from last charging aperture, flow downward with filminess along heated wall, lower boiling oil-soluble waste gas is evaporated, on condenser wall, condense, the oil-soluble waste gas that condensation compiles is compiled discharge, and inertia higher boiling organic liquid flows out thin-membrane short-range distiller after obtaining regeneration by distillation, led back to suction inlet pipeline by pipeline, finish the regeneration cycle of bypass into described liquid delivery pump.
6. waste gas processing method according to claim 1 is characterized in that in the described sig water, and contained alkali can be NaOH, sodium carbonate; Its feature also is described inertia higher boiling organic liquid, can be atoleine, chlorocosanes, ethylene glycol phenyl ether, alkyd resins.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011100065731A CN102091497A (en) | 2011-01-13 | 2011-01-13 | Method for treating waste gas discharged from continuously running laboratory |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN2011100065731A CN102091497A (en) | 2011-01-13 | 2011-01-13 | Method for treating waste gas discharged from continuously running laboratory |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103785274A (en) * | 2012-10-29 | 2014-05-14 | 中国石油化工集团公司 | Method for processing waste gases and waste liquids in laboratory |
| CN107162080A (en) * | 2017-05-25 | 2017-09-15 | 胡国兴 | A kind of carburetion system |
| CN111298588A (en) * | 2020-03-06 | 2020-06-19 | 复旦大学 | Ship flue gas condensation cyclone purification device and method |
| CN112090119A (en) * | 2020-09-29 | 2020-12-18 | 云南农业大学 | Distributed multi-cyclone gas-water separation recycling device for tea fermentation |
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| CN2403483Y (en) * | 2000-01-18 | 2000-11-01 | 朱尊德 | Smoke dust purifier |
| US20030050004A1 (en) * | 2001-09-06 | 2003-03-13 | Mzander Facility Engineering Gmbh | Device and method for exhaust air processing, in particular, for clean room devices |
| CN2764470Y (en) * | 2005-07-01 | 2006-03-15 | 熊宇 | Exhaust gas absorption system for chemical laboratory |
| CN201182965Y (en) * | 2007-11-09 | 2009-01-21 | 范维林 | Combined lab waste gas purification processing unit |
| CN101780372A (en) * | 2010-01-29 | 2010-07-21 | 华南理工大学 | Method and device for processing laboratory exhaust gas |
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| CN2403483Y (en) * | 2000-01-18 | 2000-11-01 | 朱尊德 | Smoke dust purifier |
| US20030050004A1 (en) * | 2001-09-06 | 2003-03-13 | Mzander Facility Engineering Gmbh | Device and method for exhaust air processing, in particular, for clean room devices |
| CN2764470Y (en) * | 2005-07-01 | 2006-03-15 | 熊宇 | Exhaust gas absorption system for chemical laboratory |
| CN201182965Y (en) * | 2007-11-09 | 2009-01-21 | 范维林 | Combined lab waste gas purification processing unit |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103785274A (en) * | 2012-10-29 | 2014-05-14 | 中国石油化工集团公司 | Method for processing waste gases and waste liquids in laboratory |
| CN103785274B (en) * | 2012-10-29 | 2015-12-16 | 中国石油化工集团公司 | A kind of method for laboratory exhaust gas liquid waste processing |
| CN107162080A (en) * | 2017-05-25 | 2017-09-15 | 胡国兴 | A kind of carburetion system |
| CN107162080B (en) * | 2017-05-25 | 2023-09-15 | 深圳国兴鸿泰实业发展有限责任公司 | Vaporization system |
| CN111298588A (en) * | 2020-03-06 | 2020-06-19 | 复旦大学 | Ship flue gas condensation cyclone purification device and method |
| CN112090119A (en) * | 2020-09-29 | 2020-12-18 | 云南农业大学 | Distributed multi-cyclone gas-water separation recycling device for tea fermentation |
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Application publication date: 20110615 |