CN101219319A - Device for recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method - Google Patents
Device for recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method Download PDFInfo
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- CN101219319A CN101219319A CNA2007100096273A CN200710009627A CN101219319A CN 101219319 A CN101219319 A CN 101219319A CN A2007100096273 A CNA2007100096273 A CN A2007100096273A CN 200710009627 A CN200710009627 A CN 200710009627A CN 101219319 A CN101219319 A CN 101219319A
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Abstract
The invention relates to a device for recycling waste gas generated by viscose through an alkali cleaning-absorbing condensation method, which relates to the equipment for recycling waste gas generated by industries. The device for recycling waste gas generated by viscose through an alkali cleaning-absorbing condensation method has relatively good processing effects and can recycle useful resources in the waste gas with high efficiency. The device is equipped with a waste gas filter, an alkaline tower, a solution transfer pump, a storing tank of sodium hydrosulfide, an air compressor, a washer, a recycle pump, an adsorption tank, an air heater, a heater, a storing tank of carbon bisulfide, a gear transfer pump, a flowmeter, a solution separator, a magnetic levitation ball liquid level switch, a condenser, a water pump, a cooling tower, a draft fan, a vacuum pump, a concentration analyzer of H2S and CS2, an adsorption tank, a cooler and a pneumatic ball valve. Sulfureted hydrogen gas in the waste gas is transformed into sodium hydrosulfide liquid and carbon bisulfide gas in the waste gas is transformed into carbon bisulfide liquid through washing, absorbing, condensing and separating. The carbon bisulfide liquid is employed as raw materials and is directly sent back to the production of the viscose.
Description
Technical field
The present invention relates to a kind of industrial production waste gas reclaimer, especially relate to a kind of device that adopts alkali cleaning and adsorption condensing method to reclaim the viscose rayon process gas.
Background technology
Viscose rayon is to be that raw material adds industrial chemicals such as caustic soda, sulfuric acid, carbon disulfide, zinc sulfate with the natural polymer cellulose, the regenerated celulose fibre of making through a series of chemistry and physical change.In process of production, can produce a certain amount of CS
2And H
2Pernicious gases such as S cause the pollution to environment.How reducing this pollution, is one of major subjects of present domestic viscose rayon enterprise.Existing processing method mainly adopts incinerating method to handle, and is about to CS
2And H
2S waste gas places the incinerator incineration oxidation to become SO
2, the mist after the burning contains 5%～6%SO
2And water (water is by H
2S generates during burning), the heat that the burning back produces can utilize, and the high-temperature gas during burning enters SO
2Reburner is reacted into SO at reburner through catalyst action
3, SO
3Generate gaseous sulfuric acid, SO after condensation with steam reaction again
3Become dilute sulfuric acid with water, with its simmer down to liquid sulfuric acid, tail gas is removed remaining SO through alkali cleaning at last
2Waste gas.
Notification number is that the patent of invention of CN1070129 discloses a kind of process and complexes thereof that viscose rayon is produced waste gas pollution control and treatment that are used for.It is by acid bath degas system, H
2S is converted into sulfur system and CS
2The absorption recovery system constitutes.In the acid bath degas system, adopt the board-like degassing tower that is provided with gas cylinder to carry out vacuum outgas, at H
2S is converted into sulfur system with base catalysis doctor solution circulation catalysis, at CS
2The absorption recovery system reclaims with the cylindricality adsorbents adsorb.
Notification number is degasser and the application thereof that the patent of invention of CN1186878 discloses a kind of double effect intermittent cooling type, comprises that economic benefits and social benefits degassing design and the indirect-cooling cool exchanger with two special efficient degassing tank series connection carries out condensation process.Can be with the H in the liquid of viscose rayon quantity-produced coagulating bath
2S and CS
2Content be reduced to below the 6mg/l, have the degassing efficiency height, save heat energy and water source, reduce the effect of polluting and improving the viscose rayon quality.
Summary of the invention
The objective of the invention is directly to discharge at waste gas in the existing production process of viscose fiber, or the exhaust-gas treatment effect is relatively poor, discharging is difficult for up to standard or problems such as waste gas treatment process complexity, operating cost height, provide a kind of treatment effect better, and can be from waste gas the recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method device of high efficiente callback useful resources.
Technical scheme of the present invention is the CS of discharging in producing at viscose rayon
2And H
2S waste gas is collected it, through washing, absorption, condensation, separation, the hydrogen sulfide gas in the waste gas is converted into NaHS liquid, and the carbon disulfide gas in the waste gas is converted into carbon disulfide liquid.Carbon disulfide liquid can be used as the raw material direct reuse in viscose rayon production, and NaHS has been widely used industrial.
The present invention is provided with waste gas filter, caustic wash tower, solution transfer pump, NaHS storage tank, air compressor machine, scrubbing tower, circulating pump, adsorption tanks, air-heater, heater, carbon disulfide storage tank, gear infusion pump, flowmeter, solution separator, magnetic floating-ball level switch, condenser, water pump, cooling tower, air-introduced machine, vavuum pump, H
2S and CS
2Concentration analyzer, adsorption tanks, cooler, pneumatic ball valve and pipeline thereof.
The external H of cooler input
2S and CS
2Waste gas, cooler outlet is taken over the filter air intake, the filter gas outlet connects the caustic wash tower air intake, the gas outlet of being located at the caustic wash tower top connects the scrubbing tower air intake, the liquid outlet of being located at the caustic wash tower bottom connects the solution transfer pump inlet by pneumatic operated valve, the solution transfer pump liquid outlet connects NaHS storage tank inlet, and the inlet on caustic wash tower top connects circulating-pump outlet by shutoff valve and control valve, and the inlet on caustic wash tower top inserts NaOH solution by a three-way connection through control valve and shutoff valve.The scrubbing tower liquid outlet connects pump entry, and the gas outlet of being located at the scrubbing tower top connects each adsorption tanks air intake of first adsorption zone, and NaOH solution is inserted on the top of scrubbing tower, and scrubbing tower top liquid inlet connects the circulating pump liquid outlet by shutoff valve and control valve.Steam is inserted in each adsorption tanks steam inlet, and the nitrogen inlet of each adsorption tanks inserts nitrogen, and each adsorption tanks exhaust outlet all connects the air-introduced machine air intake vent, and fan out draft connects chimney.The second adsorption zone adsorption tanks air intake connects the first adsorption zone adsorption tanks gas outlet, and each adsorption tanks top is equipped with steam outlet.All the liquid outlet of adsorption tanks bottom connects the condenser liquid inlet by pneumatic operated valve, filter, and all adsorption tanks all have an air inlet to connect air compressor machine gas outlet and air-heater air outlet by shutoff valve, control valve, filter.The air-heater air intake vent connects the heater air outlet, and the condenser liquid outlet connects solution separator liquid inlet, and solution separator liquid outlet connects gear infusion pump liquid inlet by pneumatic operated valve, flowmeter, and gear infusion pump liquid outlet connects carbon disulfide storage tank inlet.The cooling tower delivery port is by shutoff valve, filter water pump water inlet, and pump outlet connects condenser water inlet and cooler water inlet, and the cooling tower water inlet connects condenser delivery port and cooler delivery port.
Caustic wash tower is provided with magnetic floating-ball level switch, cylindrical shell, overcurrent plate, filler, shower, manhole, exhaust gas entrance, liquid outlet, slag-drip opening, inlet and exhaust outlet.The magnetic floating-ball level switch is located on the NaHS on the cylindrical shell bottom, the overcurrent plate is located in the cylindrical shell, filler is located on the overcurrent plate, shower is located at cylindrical shell top, and manhole is located on the housing of cylindrical shell, and exhaust gas entrance is located at cylindrical shell bottom one side, liquid inlet is located at cylindrical shell bottom one side, slag-drip opening is located at the cylindrical shell bottom, and inlet is located at cylindrical shell top one side, and exhaust outlet is located at the cylindrical shell top.
Scrubbing tower is provided with magnetic floating-ball level switch, cylindrical shell, overcurrent plate, demister, shower, filler, manhole, exhaust gas entrance, overfall, slag-drip opening, circulation solution outlet, circulation solution import, exhaust outlet, inlet and circulation infusion pump.The magnetic floating-ball level switch is located on the liquid of cylindrical shell bottom, the overcurrent plate is located at bottom in the cylindrical shell, demister is located at the cylindrical shell internal upper part, shower is located at the demister below, filler is located on the overcurrent plate, manhole is located at cylinder shell one side, exhaust gas entrance is located at cylindrical shell bottom one side, overfall is located at cylindrical shell bottom one side and is positioned at the exhaust gas entrance below, and slag-drip opening is located at cylindrical shell bottom one side, and cylindrical shell bottom one side is located in the circulation solution outlet, the circulation solution import is located at cylindrical shell top one side and is joined with shower, the circulation solution outlet is connected with the circulation solution import through the circulation infusion pump, and exhaust outlet is located at the cylindrical shell top, and inlet is located at cylindrical shell top one side and is joined with shower.
Adsorption tanks are provided with body, overcurrent plate, coarse particles layer, active carbon layer, manhole, exhaust gas inlet, slag-drip opening, liquid outlet, cold and hot wind inlet, nitrogen inlet/vacuum draw mouth, suction and exhaust ports, pure qi (oxygen) outlet, steam outlet and steam inlet again.The overcurrent plate is located at bottom in the body, the coarse particles layer is located on the overcurrent plate, active carbon layer is located at coarse particles layer top, manhole is located at body top one side, exhaust gas inlet and cold and hot wind inlet all are located at body bottom one side, slag-drip opening and liquid outlet all are located at the body bottom, and nitrogen inlet/vacuum draw mouth and steam inlet all are located at bodies top one side, and suction and exhaust ports, pure qi (oxygen) outlet and steam outlet all are located at bodies top again.
Waste gas enters caustic wash tower, the CS that produces after filtering by cooler cooling and filter after alkali cleaning
2Gas enters adsorption tanks.Adsorption tanks are provided with at least 2, are in air inlet absorption, desorption and holding state successively in turn.When entering adsorption tanks, waste gas adsorbs CS by active carbon layer
2, absorption is closed all valves of adsorption tanks when saturated, aspirates out jar an interior air, moves for next step inflated with nitrogen provides the safe buffering of a totally-enclosed, charges into nitrogen then, for next step feeding steam provides safe action.Feed steam, the CS that is adsorbed by active carbon layer
2Desorption is separated from active carbon.Contain CS behind the desorption
2Steam solution enters condenser.After desorption finished, the steam off valve was opened the emptying valve, and residue vapor in the adsorption tanks is emitted.Feed hot blast again in adsorption tanks, expeling is adsorbed on moisture in the active carbon, makes active carbon obtain drying.Feed compressed air to drying after the higher active carbon of temperature cool off, adsorption tanks continue exhaust, for next one circulation absorption ready.Enter the CS that contains of condenser
2Steam solution, through heat exchange by water cooling, condensing soln enters the solution separator, the solution separator according to hydrometer method with CS
2Solution is separated from steam solution, by the gear infusion pump it is extracted into the carbon disulfide storage tank, uses for workshop.
The present invention adopts PCL man-machine interface automation operating system, and realizes whole collection control with the viscose rayon workshop, the parameter at each control point all gather automatically and can be effectively controlled from computer, show, warning, record, printing etc.All thermometric instruments are all selected the bimetallic thermometer of protection type band corrosion-resistant finishes for use, and temperature teletransmission measuring instrument adopts the Pt of resistant material
100Thermal resistance.Manometer is selected the anti-corrosion type bourdon gauges for use, and intelligent transducer is adopted in the pressure teletransmission.The liquid level gauge that shows adopts magnetic turnover panel double colored indicator on the spot, and the liquid level teletransmission becomes to send adopts differential pressure levelmeter, magnetic floating-ball level switch.The portion gas flow adopts metal floater flowmeter (the charged remote transmission device of flowmeter when needing teletransmission), and electromagnetic flowmeter is adopted in the conducting liquid flow measurement, and the large pipeline gas flow measurement adopts the plug-in type vortex-shedding meter.Fluid flowmeter adopts the digital display target type meter.Executing agency adopts pneumatic control valve, shutoff valve, pneumatic base-plate valve, butterfly valve etc.
Through experiment, the technical parameter after the processing is as follows: H
2S clearance 99.7%, CS
2Clearance 97%, H
2S concentration of emission 13.6mg/m3, CS
2Concentration of emission 156.4mg/m3, total S clearance 99.7%.
CS after collecting
2And H
2S waste gas at first is cooled to waste gas about 25 ℃ by cooler, filters out waste gas in collection process behind the entrained foreign material through filter again, and waste gas enters caustic wash tower, the H more than 97% in the waste gas after alkali cleaning
2S changes into NaHS liquid, liquid NaHS income storage tank.The H that do not react in the waste gas this moment
2S, its concentration is below 100ppm, and then, waste gas enters scrubbing tower and NaOH further reacts, Na
2S solution is handled through the alkali cleaning again that circulates, the waste gas H that comes out from scrubbing tower
2S concentration drops to below the 10ppm, and this moment, the waste gas main component was CS
2CS
2Be introduced into adsorption tanks, CS
2In adsorption tanks, adsorbed, when absorption reaches capacity state, charge into nitrogen replacement in the adsorption tanks and go out air, and then feed Steam Heating CS by active carbon layer
2From active carbon layer, desorb.Absorption between each adsorption tanks, to find time, fill nitrogen, desorb be follow procedure and carry out continuously.Separate the CS that contains of sucking-off
2Steam become and contain CS through condenser condenses
2The aqueous solution, again through the solution separator with CS
2With moisture from, CS
2Solution enters storage tank, continues to supply with to produce and uses.Water is discharged into water treating pond, and the water purification after the processing flows back to cooling tower and recycles.
The reaction equation of exhaust-gas treatment is: H
2S+2NaOH=Na
2S+2H
2O, H
2S+Na
2S=2NaHS.
Description of drawings
Fig. 1 is structure composition, corollary equipment and the pipeline annexation schematic diagram of the embodiment of the invention.Pictorial representation in Fig. 1 is as follows :-a-sodium hydroxide solution ,-b-compressed air ,-c-carbon disulfide liquid,-d-nitrogen,-e-secondary suction ,-f-hydrogen sulfide, carbon disulfide waste gas ,-g-hot blast,-h-NaHS, the discharging of-j-pure qi (oxygen) ,-k-sodium sulfide solution ,-n-carbon disulfide gas,-s-cooling water ,-z-steam.
Fig. 2 is the caustic wash tower structural representation of the embodiment of the invention.
Fig. 3 is the scrubbing tower structural representation of the embodiment of the invention.
Fig. 4 is the adsorption tanks structural representation of the embodiment of the invention.
The specific embodiment
Referring to Fig. 1～4, the present invention is provided with waste gas filter 1, caustic wash tower 2, solution transfer pump 3, NaHS storage tank 4, air compressor machine 5, scrubbing tower 6, circulating pump 7, adsorption tanks 8, air-heater 9, heater 10, carbon disulfide storage tank 11, gear infusion pump 12, flowmeter 13, solution separator 14, magnetic floating-ball level switch 15, condenser 16, water pump 17, cooling tower 18, air-introduced machine 19, vavuum pump 20, H
2S and CS
2Concentration analyzer 21, adsorption tanks 22, cooler 23, difference gauge, traffic analyzer, pneumatic ball valve, pipeline etc.The external H of the input of cooler 22
2S, CS
2Waste gas, the air intake of filter 1 is taken in cooler 22 outlets, the gas outlet of filter 1 connects caustic wash tower 2 air intakes, the gas outlet of being located at caustic wash tower 2 tops connects scrubbing tower 6 air intakes, the liquid outlet of being located at caustic wash tower 2 bottoms connects solution transfer pump 3 inlets by pneumatic operated valve, solution transfer pump 3 liquid outlets connect NaHS storage tank 4 inlets, the inlet on caustic wash tower 2 tops connects circulating pump 7 outlets by shutoff valve and control valve, and the inlet on caustic wash tower top inserts NaOH solution by a three-way connection through control valve and shutoff valve.The liquid outlet of scrubbing tower 6 connects circulating pump 7 inlets, and gas outlet, scrubbing tower 6 top connects the air intake of each adsorption tanks 8 of first adsorption zone, and NaOH solution is inserted on the top of scrubbing tower 6, and the top liquid inlet of scrubbing tower 6 connects the liquid outlet of circulating pump 7 by shutoff valve and control valve.Steam is received the steam inlet of each adsorption tanks, and nitrogen is received the nitrogen inlet of each adsorption tanks, and the exhaust outlet of each adsorption tanks 8 all connects the air intake vent of air-introduced machine 19, and air-introduced machine 19 air outlets connect chimney.The air intake of the second adsorption zone adsorption tanks 22 connects the gas outlet of the first adsorption zone adsorption tanks 8, and the top of each adsorption tanks 22 is equipped with steam outlet.All the liquid outlet of adsorption tanks bottom connects the liquid inlet of condenser 16 by pneumatic operated valve, filter 1, and all adsorption tanks all have an air inlet to connect air compressor machine 6 gas outlets and air-heater 9 air outlets by shutoff valve, control valve, filter.The air intake vent of air-heater 9 connects heater 10 air outlets, condenser 16 liquid outlets connect solution separator 14 liquid inlets, solution separator 14 liquid outlets connect gear infusion pump 12 liquid inlets by pneumatic operated valve, flowmeter 13, and gear infusion pump 12 liquid outlets connect carbon disulfide storage tank 11 inlets.Cooling tower 18 delivery ports are by shutoff valve, filter water pump 17 water inlets, and water pump 17 delivery ports connect condenser 16 water inlets and cooler 23 water inlets, and cooling tower 18 water inlets connect condenser 16 delivery ports and cooler 23 delivery ports.
Workshop is drawn into EGT of the present invention and surpasses 30 ℃, cooler is set the waste gas hotbed is reduced to below 25 ℃, is convenient to the chemical reaction of waste gas.The waste gas that collect the production scene can suck some particulate foreign material unavoidably, and the employing filter medium is that the filter of non-woven fibre cotton filters out foreign material, avoids CS
2And H
2S waste gas contains other foreign material.Alkali cleaning is according to CS
2And H
2The chemical feature of S element carries out, i.e. CS
2Be not melted into water, and H
2S is water-soluble, sprays into NaOH solution to caustic wash tower, with H
2The S reaction produces NaHS solution, and NaHS solution is directly used by solution transfer pump suction storage tank, the H after alkali cleaning
2S gas 95% is converted into NaHS.CS
2Gas sucks scrubbing tower, uses NaOH solution to CS
2Gas further washs, and makes CS
2Gas improves purity, removes impurity.Cleaning solution obtains to recycle by circulating pump 7, and unified the processing discharged in the solution overflow after the washing.
Referring to Fig. 2, caustic wash tower is provided with magnetic floating-ball level switch 201, cylindrical shell 202, overcurrent plate 203, filler 204, shower 205, manhole 206, exhaust gas entrance 207, liquid outlet 208, slag-drip opening 209, inlet 210, exhaust outlet 211 etc.Magnetic floating-ball level switch 201 is located on the NaHS on cylindrical shell 202 bottoms, overcurrent plate 203 is located in the cylindrical shell 202, filler 204 is located on the overcurrent plate 203, shower 205 is located at cylindrical shell 202 tops, and manhole 206 is located on the housing of cylindrical shell 202, and exhaust gas entrance 207 is located at cylindrical shell bottom one side, liquid inlet 208 is located at cylindrical shell bottom one side, slag-drip opening 209 is located at the cylindrical shell bottom, and inlet 210 is located at cylindrical shell top one side, and exhaust outlet 211 is located at the cylindrical shell top.CS
2And H
2S waste gas is up suction in caustic wash tower cylindrical shell 202, with reverse the colliding of NaOH solution of shower 205 ejections, central H
2S waste gas and NaOH solution obtain abundant haptoreaction by filler 204, overcurrent plate 203, produce NaHS and fall at the bottom of the tower, by solution transfer pump 3 input NaHS storage tanks 4, CS
2Toward the top motion, suck the exhaust gas entrance of scrubbing tower through filler overcurrent plate 203, filler 204 by exhaust outlet.The overcurrent plate is provided with a plurality of holes in the 203 whole planes, and filler 204 adopts the becket of corrosion resistance or pottery to embrace earrings, and magnetic floating-ball level switch 201 is used for control and keeps cylindrical shell 202 bottoms level.
Referring to Fig. 3, scrubbing tower is provided with magnetic floating-ball level switch 31, cylindrical shell 32, overcurrent plate 33, demister 34, shower 35, filler 36, manhole 37, exhaust gas entrance 38, overfall 39, slag-drip opening 310, circulation solution outlet 311, circulation solution import 312, exhaust outlet 313, inlet 314 and circulation infusion pump 315.Magnetic floating-ball level switch 31 is located on the liquid of cylindrical shell 32 bottoms, overcurrent plate 33 is located at middle and lower part in the cylindrical shell, demister 34 is located at the cylindrical shell internal upper part, shower 35 is located at the below of demister 34, filler 36 is located on the overcurrent plate 33, manhole 37 is located at cylinder shell one side, exhaust gas entrance 38 is located at cylindrical shell bottom one side, overfall 39 is located at cylindrical shell bottom one side and is positioned at exhaust gas entrance 38 belows, slag-drip opening 310 is located at cylindrical shell bottom one side, cylindrical shell bottom one side is located in circulation solution outlet 311, circulation solution import 312 is located at cylindrical shell top one side and is joined with shower, circulation solution outlet 311 is connected with circulation solution import 312 by circulation infusion pump 315, and exhaust outlet 313 is located at the cylindrical shell top, and inlet 314 is located at cylindrical shell top one side and is joined with shower 35.CS
2Waste gas enters in the cylindrical shell 32 from exhaust gas entrance 38, and by upwards suction of air-introduced machine, through filler 36, with reverse the colliding of NaOH solution from shower 35 ejections, fully contact is thoroughly cleaned, and by removing the particulate water droplet through demister 34 before the exhaust outlet 313, makes CS
2Waste gas is further purified and is taken out toward adsorption tanks 8.Magnetic floating-ball level switch 31 is used to control the liquid level of cleaning solution, and the overcurrent plate is provided with a plurality of holes in the 33 whole planes, and filler 36 adopts the becket of corrosion resistance or pottery to embrace earrings, and shower 35 is used for the NaOH solution spraying, and slag-drip opening 310 is used for cleaning in the tower.
Referring to Fig. 4, adsorption tanks are provided with body 41, overcurrent plate 42, coarse particles layer 43, active carbon layer 44, manhole 45, exhaust gas inlet 46, slag-drip opening 47, liquid outlet 48, cold and hot wind inlet 49, nitrogen inlet/vacuum draw mouth 410, suction and exhaust ports 411, pure qi (oxygen) outlet 412, steam outlet 413 and steam inlet 414 again.Overcurrent plate 42 is located at bottom in the body 41, coarse particles layer 43 is located on the overcurrent plate 42, active carbon layer 44 is located on the coarse particles layer 43, manhole 45 is located at body 41 tops one side, exhaust gas inlet 46 and cold and hot wind inlet 49 all are located at body 41 bottoms one side, slag-drip opening 47 and liquid outlet 48 all are located at body 41 bottoms, nitrogen inlet/vacuum draw mouth 410 and steam inlet 414 all are located at body 41 tops one side, and suction and exhaust ports 411, pure qi (oxygen) outlet 412 and steam outlet 413 all are located at body 41 tops again.At CS
2Gas enters before the body 41, and the active carbon layer in the body 41 is removed moisture by the hot-air seasoning that is blown into from cold and hot wind inlet 49; Then feed cold wind from cold and hot wind inlet again, the active carbon layer temperature is cooled to below 30 ℃; Next step is CS
2Gas enters body 41 bottoms from exhaust gas inlet 46, passes overcurrent plate 42 with holes, is adsorbed by active carbon layer 44 in upwards flowing; When absorption reaches capacity, valve-off, from vacuum draw mouth 410 by vavuum pump with the shape that is evacuated in the tank body, charge into nitrogen in order to one step of back; After charging into nitrogen, open steam valve and feed 110～130 ℃ of steam, steam leads to coarse particles layer 43, all compresses into into active carbon layer 44, the CS that is adsorbed by active carbon layer
2Gas desorption comes out, this moment steam lowered the temperature, condensation, obtain CS
2--water vapor mixture, flow to condenser 16 by liquid outlet 48 through pneumatic operated valve, this is the desorption stage.After desorption finished, the steam off valve was opened suction and exhaust ports again, allow as yet inhale, desorption contain surplus CS
2Gas enter the second adsorption zone adsorption tanks 22, inhale once more, desorption process.Desorption is opened 413 pairs of adsorption tanks releases of steam outlet earlier after finishing, close complete steam valve, opens 412 exhausts of pure qi (oxygen) outlet again.And then in adsorption tanks, be blown into hot blast, carry out next one circulation.Each adsorption tanks is all by above order execution, and also hockets in order between each adsorption tanks, thus realize absorption, desorption, standby process successively.Manhole 45 on the adsorption tanks body 41 is used to load and unload active carbon layer usefulness, and coarse particles layer 43 can adopt stone, active carbon layer is had other gas of pollution in order to absorption.Slag-drip opening 47 is used for the adsorption tanks internal cleaning and uses.
Claims (5)
1. the recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method device is characterized in that being provided with waste gas filter, caustic wash tower, solution transfer pump, NaHS storage tank, air compressor machine, scrubbing tower, circulating pump, adsorption tanks, air-heater, heater, carbon disulfide storage tank, gear infusion pump, flowmeter, solution separator, magnetic floating-ball level switch, condenser, water pump, cooling tower, air-introduced machine, vavuum pump, H
2S and CS
2Concentration analyzer, adsorption tanks, cooler, pneumatic ball valve and pipeline thereof;
The external H of cooler input
2S and CS
2Waste gas, cooler outlet is taken over the filter air intake, the filter gas outlet connects the caustic wash tower air intake, the gas outlet of being located at the caustic wash tower top connects the scrubbing tower air intake, the liquid outlet of being located at the caustic wash tower bottom connects the solution transfer pump inlet by pneumatic operated valve, the solution transfer pump liquid outlet connects NaHS storage tank inlet, the inlet on caustic wash tower top connects circulating-pump outlet by shutoff valve and control valve, the inlet on caustic wash tower top inserts NaOH solution by a three-way connection through control valve and shutoff valve, the scrubbing tower liquid outlet connects pump entry, the gas outlet of being located at the scrubbing tower top connects each adsorption tanks air intake of first adsorption zone, NaOH solution is inserted on the top of scrubbing tower, scrubbing tower top liquid inlet connects the circulating pump liquid outlet by shutoff valve and control valve, steam is inserted in each adsorption tanks steam inlet, the nitrogen inlet of each adsorption tanks inserts nitrogen, each adsorption tanks exhaust outlet all connects the air-introduced machine air intake vent, fan out draft connects chimney, the second adsorption zone adsorption tanks air intake connects the first adsorption zone adsorption tanks gas outlet, each adsorption tanks top is equipped with steam outlet, all the liquid outlet of adsorption tower bottom passes through pneumatic operated valve, filter connects the condenser liquid inlet, all adsorption tanks all have an air inlet to pass through shutoff valve, control valve, filter connects air compressor machine gas outlet and air-heater air outlet, the air-heater air intake vent connects the heater air outlet, the condenser liquid outlet connects solution separator liquid inlet, solution separator liquid outlet passes through pneumatic operated valve, flowmeter connects gear infusion pump liquid inlet, gear infusion pump liquid outlet connects carbon disulfide storage tank inlet, the cooling tower delivery port passes through shutoff valve, filter water pump water inlet, pump outlet connects condenser water inlet and cooler water inlet, and the cooling tower water inlet connects condenser delivery port and cooler delivery port.
2. recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method device as claimed in claim 1 is characterized in that caustic wash tower is provided with magnetic floating-ball level switch, cylindrical shell, overcurrent plate, filler, shower, manhole, exhaust gas entrance, liquid outlet, slag-drip opening, inlet and exhaust outlet; The magnetic floating-ball level switch is located on the NaHS on the cylindrical shell bottom, the overcurrent plate is located in the cylindrical shell, filler is located on the overcurrent plate, shower is located at cylindrical shell top, and manhole is located on the housing of cylindrical shell, and exhaust gas entrance is located at cylindrical shell bottom one side, liquid inlet is located at cylindrical shell bottom one side, slag-drip opening is located at the cylindrical shell bottom, and inlet is located at cylindrical shell top one side, and exhaust outlet is located at the cylindrical shell top.
3. recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method device as claimed in claim 1 is characterized in that scrubbing tower is provided with magnetic floating-ball level switch, cylindrical shell, overcurrent plate, demister, shower, filler, manhole, exhaust gas entrance, overfall, slag-drip opening, circulation solution outlet, circulation solution import, exhaust outlet, inlet and circulation infusion pump; The magnetic floating-ball level switch is located on the liquid of cylindrical shell bottom, the overcurrent plate is located at middle and lower part in the cylindrical shell, demister is located at the cylindrical shell internal upper part, shower is located at the below of demister, filler is located on the overcurrent plate, manhole is located at cylinder shell one side, exhaust gas entrance is located at cylindrical shell bottom one side, overfall is located at cylindrical shell bottom one side and is positioned at the exhaust gas entrance below, slag-drip opening is located at cylindrical shell bottom one side, cylindrical shell bottom one side is located in the circulation solution outlet, the circulation solution import is located at cylindrical shell top one side and is joined with shower, the circulation solution outlet is connected with the circulation solution import by the circulation infusion pump, and exhaust outlet is located at the cylindrical shell top, and inlet is located at cylindrical shell top one side and is joined with shower.
4. recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method device as claimed in claim 1, it is characterized in that adsorption tanks are provided with body, the overcurrent plate, the coarse particles layer, active carbon layer, manhole, exhaust gas inlet, slag-drip opening, liquid outlet, cold and hot wind inlet, nitrogen inlet and vacuum draw mouth, suction and exhaust ports again, the pure qi (oxygen) outlet, steam outlet and steam inlet, the overcurrent plate is located at bottom in the body, the coarse particles layer is located on the overcurrent plate, active carbon layer is located on the coarse particles layer, manhole is located at body top one side, exhaust gas inlet and cold and hot wind inlet all are located at body bottom one side, slag-drip opening and liquid outlet all are located at the body bottom, nitrogen inlet and vacuum draw mouth and steam inlet all are located at bodies top one side, suction and exhaust ports again, pure qi (oxygen) outlet and steam outlet all are located at bodies top.
5. recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method device as claimed in claim 1 is characterized in that the coarse particles layer is the stone layer.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2007100096273A CN101219319A (en) | 2007-09-30 | 2007-09-30 | Device for recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method |
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|---|---|---|---|
| CNA2007100096273A CN101219319A (en) | 2007-09-30 | 2007-09-30 | Device for recovering viscose fiber production exhaust-gas with soda washing-adsorption condensing method |
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Cited By (20)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102743969A (en) * | 2012-07-16 | 2012-10-24 | 北京绿创环保设备股份有限公司 | Treatment method for mixed waste gas containing H2S and CS2 |
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