CN102343205B - Centralized purification treatment process and device of waste gas in spandex production process - Google Patents
Centralized purification treatment process and device of waste gas in spandex production process Download PDFInfo
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- CN102343205B CN102343205B CN201110200129.3A CN201110200129A CN102343205B CN 102343205 B CN102343205 B CN 102343205B CN 201110200129 A CN201110200129 A CN 201110200129A CN 102343205 B CN102343205 B CN 102343205B
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Abstract
The purpose of the invention is to provide a process and a device for the purification treatment of waste gas generated during spandex production. Waste gas generated during spandex production of the invention is introduced into an absorption tower by a blower, orderly passes through a composite solution absorption unit and an organic acid solution absorption unit, and is discharged from the top part of the absorption tower; the total content of harmful gas in the discharged gas is less than 0.5 mg/m3. During the process, the composite solution absorption unit is firstly used to absorb gas easily dissolved in water and alkali liquor in the waste gas, such as dimethylformamide, dimethylacetamide, acetic acid, formaldehyde, and the like, and part of dimethylamine and ammonia gas are also absorbed; then the organic acid solution absorption unit is used for reabsorption so as to remove remaining harmful gas which is alkaline and is easily dissolved in water; and the tail gas discharge reaches the standard. The absorption process thoroughly removes harmful components in waste gas generated in spandex production industry, thus effectively prevents ambient air pollution, and has an economically feasible treatment process.
Description
Invention field
The present invention relates to technique and the device of purified treatment in spandex production process exhaust gas centralized.
Background technology
Polyurethane elastomeric fiber, claims Spandex (Spandex) abroad, and the trade name of China is spandex.Spandex has the incomparable elasticity of other any fibers, and its elongation at break is greater than 400%, conventionally 500%～700%, reaches as high as more than 800%, and elastic restoration ratio when deformation 300% reaches more than 95%, has good fatigue performance.From manufacturing process, polyurethane fibre industry spinning production line has four kinds, i.e. dry spinning, wet spinning, reaction method spinning and fusion method spinning at present.First three solvent of planting spin processes use is DMF and DMAc, and wherein dry spinning production capacity accounts for aggregated capacity 86.39%, in leading position.
The production procedure of dry spinning is: solution
-spinning pump (filtration)
-drying box (100 ℃ of hot blasts are blown over, and make solution evaporation)
-spinning
-winding shaping.Concrete operation is as follows:
Polyethers and vulcabond form prepolymer with the mol ratio of 1: 2 under certain reaction temperature and time conditions, prepolymer is after solvent is dissolved, add again dimethylamine to carry out chain propagation reaction, form block copolymer solution, through operations such as mixing, filtration, deaerations, make the spinning solution of performance uniformity again.Then with measuring pump quantitative and even be pressed into spinneret.Under the effect of pressure, spinning solution is extruded and forms strand thread from spinneret pore, and enters path.In path, be filled with hot-air, the solvent in strand thread volatilized rapidly, and taken away by air, strand concentration improves constantly until solidify, and meanwhile strand thread is stretched and attenuates, and is finally wound into certain web-like.
Spandex is produced chemical industry and textile of chemical fibre a lot of contents and the feature in producing that combine, and it is chemical process that polymerization workshop section, heat medium system, assembly clean and refine workshop section etc., and spinning, is wound as typical synthetic fiber spinning production technology.Due to the technology of spandex production at present and the material characteristic of use, cause the whole production process from raw material storage to product output all to have toxic emission.Especially in the path gas of high temperature spray silk process, except most of air, steam, also contain the toxic organic compounds such as dimethylamine, formaldehyde, acetic acid, dimethylacetylamide (DMAc), dimethyl formamide (DMF), ammonia, methyl alcohol, if their directly emptying, will be to serious environment pollution.
At present, the method for processing waste gas in spandex production process is generally directly emptying, and the harm therefore environment of production plant area and periphery being caused is self-evident.
Summary of the invention
The object of this invention is to provide new technology and the device of purified treatment in a kind of spandex production process exhaust gas centralized, as shown in Figure 1.The present invention sets up upper and lower two absorptive units in same absorption tower body, wherein lower unit is composite solution absorptive unit, upper unit is organic acid soln absorptive unit, through after the absorption of these two unit, pernicious gas content in processed gas will can meet relevant environmental requirement completely, reaches the object of cleaner production.
Object of the present invention can realize by following technical solution:
A kind of spandex production process waste gas absorption tower, its structure is as shown in the absorption tower T-1 in Fig. 1, in absorption tower body, set up upper and lower two absorptive units, wherein lower unit is composite solution absorptive unit, upper unit is organic acid solution absorptive unit, between composite solution absorptive unit and organic acid solution absorptive unit, have vapour-liquid spacer assembly M-1 that Unit two are separated, and gas can enter into from the composite solution absorptive unit of bottom the organic acid solution absorptive unit on top, gas distributor A-1 is arranged at the bottom of composite solution absorptive unit, exhaust inlet pipe outside gas distributor A-1 and tower joins, the middle part of composite solution absorptive unit is GAS ABSORPTION district, this district can load with filler or column plate, liquid distribution trough Q-1 is arranged at the top of composite solution absorptive unit, liquid distribution trough Q-1 is connected with fluid flowmeter FM-1 by centrifugal pump P-2 with the composite solution storage tank V-3 outside tower, composite solution absorptive unit bottom has pipeline 2 to communicate with composite solution storage tank V-3, forms composite solution closed circuit, organic acid solution absorptive unit bottom is vapour-liquid spacer assembly M-1, gas enters organic acid solution absorptive unit by vapour-liquid spacer assembly M-1, the middle part of organic acid solution absorptive unit is GAS ABSORPTION district, this district can load with filler or column plate, liquid distribution trough Q-2 is arranged at the top of organic acid solution absorptive unit, liquid distribution trough Q-2 is connected with fluid flowmeter FM-2 by centrifugal pump P-3 with the organic acid solution storage tank V-5 outside tower, organic acid solution absorptive unit bottom has pipeline 5 to communicate with organic acid solution storage tank V-5, form organic acid cycle loop, waste gas outlet after purified treatment is arranged at organic acid solution absorptive unit top.
Above-mentioned spandex production process waste gas absorption tower, described gas-liquid spacer assembly M-1 is that (its cross section is rectangle by one or more riser, circle or other shape) form with liquid-blocking cap, gas phase rises by riser from lower unit, and overflow from surrounding along the gap between riser and liquid-blocking cap, and the liquid phase of upper unit is stopped inflow upper unit bottom by liquid-blocking cap in dropping process, and flow out via pipeline 5.
Purification process technique in a kind of spandex production process exhaust gas centralized, as shown in Figure 1, it comprises the following steps: its flow process
(content of main harmful components is respectively 1-500mg/m to the gas that step 1. is discharged each vacuum pump outlet of the outfits such as spandex production process polymerization workshop section, Pen Si workshop section, refining workshop section, solvent recovery workshop section
3dimethylacetylamide (DMAc), 1-2000mg/m
3dimethyl formamide (DMF), 1-1000mg/m
3dimethylamine, 1-500mg/m
3ammonia, 1-2000mg/m
3formaldehyde and 1--4000mg/m
3acetic acid steam) collect, enter gas reservoir V-1, then by air blast P-1 and pipeline 1, gas is concentrated to the gas distributor A-1 of the composite solution absorptive unit bottom that is delivered to absorption tower T-1, enter absorption tower T-1,
According to the content of each waste gas component in gas reservoir V-1, the spray flux of controlling composite solution by fluid flowmeter FM-1, makes to be down to respectively 0.1mg/m by the content of formaldehyde and acetic acid in the gas after the T-1 composite solution absorptive unit of absorption tower
3below,
In the time of the increased content of harmful components in gas phase, the concentration of composite solution and internal circulating load are all heightened corresponding,
Composite solution in the T-1 composite solution absorptive unit of step 3. absorption tower is in circulation, the composite solution partially absorbing after waste gas is discharged from pipeline 7, valve F-3 and pipeline 10, remove biochemical treatment tank, the amount of discharge is determined according to the online basicity that detects composite solution; Recycling composite solution storage tank V-2 supplements the fresh composite solution of equivalent to composite solution storage tank V-3 by valve F-1, make the liquid level in composite solution storage tank V-3 keep constant, the volume of composite solution storage tank V-3 was determined by internal circulating load and the time of staying of composite solution.
The top organic acid solution absorptive unit that the gas of step 4. after the T-1 composite solution absorptive unit of absorption tower enters into absorption tower T-1 by the vapour-liquid spacer assembly M-1 at T-1 composite solution absorptive unit top, absorption tower absorbs, the gas vent of vapour-liquid spacer assembly M-1 is above organic acid solution liquid level, prevent that organic acid solution from entering into composite solution absorptive unit, this absorptive unit can load with filler or column plate, its concrete height and specification are determined by concrete commercial scale
In the time of the increased content of harmful components in gas phase, the concentration of organic acid soln and internal circulating load are all heightened corresponding.
Organic acid solution in the organic acid absorptive unit of T-1 top, step 6. absorption tower is in circulation, the organic acid solution partially absorbing after waste gas is discharged from pipeline 8, valve F-4 and pipeline 10, remove biochemical treatment tank, the amount of discharge is determined according to the online basicity that detects organic acid solution; Utilize organic acid absorption liquid storage tank V-4, by valve F-2, organic acid absorption liquid storage tank V-5 is carried out to equivalent supplements simultaneously, make the liquid level in organic acid absorption liquid storage tank V-5 keep constant, the volume of organic acid absorption liquid storage tank V-5 was determined by internal circulating load and the time of staying of absorption liquid
The last gas of step 7., from organic acid absorptive unit top, T-1 top, absorption tower, is discharged by valve F-5 and pipeline 9, and in the gas of discharge, the quality percentage total content of pernicious gas is less than 0.5mg/m
3.
Purification process technique in above-mentioned spandex production process exhaust gas centralized, the gas distributor A-1 of the composite solution absorptive unit bottom of the absorption tower T-1 described in step 1 can be arranged on below the liquid level of composite solution of the composite solution absorptive unit bottom of absorption tower T-1.
The present invention innovates the technique of purified treatment in conventional spandex production process exhaust gas centralized, and the pernicious gas in gas reservoir V-1 comprises: dimethylacetylamide (DMAc), dimethyl formamide (DMF), acetic acid, formaldehyde, dimethylamine, ammonia.By controlling the spray flux of two absorptive units, gas is by after the composite solution absorptive unit and organic acid absorptive unit of absorption tower T-1, and the content of dimethylacetylamide (DMAc), dimethyl formamide (DMF), acetic acid, formaldehyde steam, dimethylamine and ammonia is less than 0.5 mg/m
3, and any single gas phase content be all less than 0.1 mg/m
3.In the time that equipment material allows, can adopt the not volatile inorganic acid solution such as dilute sulfuric acid, sulfonic acid, and should not may cause with hydrochloric acid and nitric acid etc. the volatile solvent soln of secondary pollution.
Technique of the present invention has the following advantages: (1) is integrated upper and lower two absorptive units in same seat tower, have saved space, have simplified flow process; (2) adopt vapour-liquid spacer assembly that the unimpeded liquid of two sections gas circuit is not communicated; (3) in composite solution absorptive unit, utilize alkali lye and sour gas generation neutralization reaction to produce stable compound, in rare organic acid absorptive unit, use nontoxic pollution-free organic acid weak solution and alkaline gas generation neutralization reaction to produce stable compound, thereby avoid being discharged in air, prevented the pollution of pernicious gas to environment.
Accompanying drawing explanation
Fig. 1 is schematic flow sheet of the present invention.Wherein:
T-1 is absorption tower, and P-1 is air blast, and P-2, P-3 are fluid delivery pump, V-1 is waste gas storage tank, V-2 is that pure water storage tank, V-3, V-5 are absorption liquid storage tank, and V-4 is rare organic acid storage tank, and F-1, F-2, F-3, F-4, F-5 are valve, Q-1, Q-2 liquid distribution trough, A-1 is gas distributor, FM-1, FM-2 are fluid flowmeter, M-1 is vapour-liquid spacer assembly, and 1,2,3,4,5,6,7,8,9,10 is pipeline.
The specific embodiment
Further illustrate by the following examples the present invention.
embodiment 1: produce waste gas absorption in 3kt spandex production process take dimethylacetylamide (DMAc) as solvent per year
Spandex workshop waste gas absorption method operating procedure is as shown in accompanying drawing one.This system is mainly made up of equipment such as absorption tower, pure water storage tank, rare organic acid absorption liquid storage tanks.Be provided with metering and control instrument and pipeline at each equipment room.The waste gas of collecting in waste gas storage tank V-1 (is contained to 5 mg/m
3dimethylacetylamide steam, 20 mg/m
3acetic acid steam, 40 mg/m
3formaldehyde, 56 mg/m
3dimethylamine gas and 13 mg/m
3ammonia) pass into the composite solution absorptive unit (composite solution of the NaOH that composite solution is 0.1M and 0.3M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1, according to the content of the exhaust gas constituents in gas, and exhaust-gas treatment amount, the spray flux of controlling composite solution with flowmeter FM-1, the liquid spraying density of the present embodiment is 45m
3/ m
2h, makes the quality percentage composition of acetic acid in the gas after composite solution absorptive unit be down to 0.04 mg/m
3, content of formaldehyde is reduced to 0.07 mg/m
3.By absorb waste gas composite solution by pipeline 7 by valve F-3 with 0.2m
3the speed of/d is discharged, enter biochemical treatment tank, utilize composite solution storage tank V-2 by valve F-1, composite solution storage tank V-3 to be supplemented the fresh composite solution of equivalent simultaneously, make the liquid level in composite solution storage tank V-3 keep constant, the volume of composite solution storage tank V-3 is 80m
3.Now in gas, still contain 42 mg/m
3dimethylamine gas and 8mg/m
3ammonia, again gas is entered to the rare organic acid liquid absorptive unit of absorption tower T-1 by vapour-liquid spacer assembly M-1, utilize the benzene sulfonic acid solution of 0.1M to absorb, regulating the sprinkle density of spray flux the present embodiment of benzene sulfonic acid liquid according to the content of dimethylamine in gas and ammonia is 36m
3/ m
2h, makes dimethylamine gas and ammonia in waste gas substantially be completely absorbed, and last, the gas after being cleaned is emptying by valve F-5 and pipeline 9, and gas total content harmful in emptying gas is down to 0.25 mg/m
3, absorb organic acid soln after waste gas from pipeline 8, valve F-4 and pipeline 10 with 0.2m
3the speed of/d is discharged, and removes biochemical treatment tank; Utilize organic acid absorption liquid storage tank V-4, by valve F-2, organic acid absorption liquid storage tank V-5 is carried out to equivalent simultaneously and supplement, make the liquid level in organic acid absorption liquid storage tank V-5 keep constant, the volume of organic acid absorption liquid storage tank V-5 is 30m
3.
embodiment 2: produce waste gas absorption in 5kt spandex production process take dimethylacetylamide (DMAc) as solvent per year
Spandex workshop waste gas absorption method operating procedure is as shown in accompanying drawing one.This system is mainly made up of equipment such as absorption tower, pure water storage tank, rare organic acid absorption liquid storage tanks.Be provided with metering and control instrument and pipeline at each equipment room.The waste gas of collecting in waste gas storage tank V-1 (is contained to 25 mg/m
3dimethylacetylamide steam, 12 mg/m
3formaldehyde, 120 mg/m
3acetic acid steam, 45 mg/m
3dimethylamine gas and 16 mg/m
3ammonia) pass into the composite solution absorptive unit (composite solution of the sodium carbonate that composite solution is 0.4M and 0.5M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1, according to the content of the exhaust gas constituents in gas, and exhaust-gas treatment amount, the spray flux of controlling composite solution with flowmeter FM-1, the sprinkle density of the present embodiment is 25m
3/ m
2h, makes the quality percentage composition of acetic acid in the gas after composite solution absorptive unit be down to 0.090mg/m
3below, formaldehyde is reduced to 0.08 mg/m
3below, by absorb waste gas composite solution by pipeline 7 by valve F-3 with 0.4m
3the speed of/d is discharged, enter biochemical treatment tank, utilize composite solution storage tank V-2 by valve F-1, composite solution storage tank V-3 to be supplemented the fresh composite solution of equivalent simultaneously, make the liquid level in composite solution storage tank V-3 keep constant, the volume of composite solution storage tank V-3 is 40m
3.Now in gas, still contain 25mg/m
3dimethylamine gas and 9 mg/m
3ammonia, again gas is entered to the rare organic acid solution absorptive unit of absorption tower T-1 by vapour-liquid spacer assembly M-1, utilize the tartaric weak solution of 1.2M to absorb, (sprinkle density is 18m to regulate rare tartaric spray flux according to the content of dimethylamine in gas and ammonia
3/ m
2h), make dimethylamine gas and ammonia in waste gas substantially be completely absorbed, last, the gas after being cleaned is emptying by valve F-5 and pipeline 9, and in emptying gas, dimethylamine content is 0.05 mg/m
3, ammonia level is 0.01 mg/m
3, harmful gas total content is lower than 0.3 mg/m
3.The tartaric acid solution absorbing after waste gas will be from pipeline 8, valve F-4 and pipeline 10 with 0.3m
3the speed of/d is discharged, and removes biochemical treatment tank; Utilize organic acid absorption liquid storage tank V-4, by valve F-2, organic acid absorption liquid storage tank V-5 is carried out to equivalent simultaneously and supplement, make the liquid level in organic acid absorption liquid storage tank V-5 keep constant, the volume of organic acid absorption liquid storage tank V-5 is 27m
3.
embodiment 3: produce waste gas absorption in 10kt spandex production process take dimethylacetylamide (DMAc) as solvent per year
Mode of operation is as embodiment 1.The waste gas of collecting in waste gas storage tank V-1 (is contained to dimethylacetylamide steam, 31 mg/m of 50mg/m3
3formaldehyde, the acetic acid steam of 400mg/m3, the dimethylamine gas of 100mg/m3 and the ammonia of 5mg/m3) pass into the composite solution absorptive unit (composite solution of the sodium acid carbonate that solution is 3.0M and 3.5M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1, according to the content of the exhaust gas constituents in gas and exhaust-gas treatment amount, the spray flux of controlling composite solution with flowmeter FM-1, the sprinkle density of the present embodiment is 8m
3/ m
2h), make the content of acetic acid in the gas after composite solution absorptive unit be down to 0.01 mg/m
3, and content of formaldehyde is down to 0.02 mg/m
3.By absorb waste gas composite solution by pipeline 7 by valve F-3 with 0.4m
3/ d discharges and enters biochemical treatment tank, utilizes composite solution storage tank V-2 by valve F-1, composite solution storage tank V-3 to be supplemented the fresh composite solution of equivalent simultaneously, makes the liquid level in composite solution storage tank V-3 keep constant, and the volume of composite solution storage tank V-3 is 15m
3.Now in gas, still contain 49mg/m
3dimethylamine gas and 3.25mg/m
3ammonia, again gas is entered to the rare organic acid solution absorptive unit of absorption tower T-1 by vapour-liquid spacer assembly M-1, utilize the weak solution of the lactic acid of 3.0M to absorb, regulate the spray flux of rare lactic acid according to the content of dimethylamine in gas and ammonia, the sprinkle density of the present embodiment is 15m
3/ m
2h, makes dimethylamine gas and ammonia in waste gas substantially be completely absorbed, and last, the gas after being cleaned is emptying by valve F-5 and pipeline 9, and gas total content harmful in emptying gas is down to 0.3mg/m
3, and the content of single gas phase is all lower than 0.1 mg/m
3.The organic acid soln absorbing after waste gas will be from pipeline 8, valve F-4 and pipeline 10 with 0.45m
3/ d discharges, and removes biochemical treatment tank; Utilize organic acid absorption liquid storage tank V-4, by valve F-2, organic acid absorption liquid storage tank V-5 is carried out to equivalent simultaneously and supplement, make the liquid level in organic acid absorption liquid storage tank V-5 keep constant, the volume of organic acid absorption liquid storage tank V-5 is 25m
3.
embodiment 4: produce waste gas absorption in 20kt spandex production process take dimethylacetylamide (DMAc) as solvent per year
Mode of operation is as embodiment 1.The waste gas of collecting in waste gas storage tank V-1 (is contained to 20mg/m
3dimethylacetylamide steam, 33mg/m
3formaldehyde, 156mg/m
3acetic acid steam, 12mg/m
3dimethylamine gas and 58mg/m
3ammonia) pass into the composite solution absorptive unit (composite solution of the NaOH that composite solution is 5.0M and 5.0M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1, according to the exhaust gas constituents content in gas and exhaust-gas treatment amount, control the spray flux of rare composite solution with flowmeter FM-1, the sprinkle density of the present embodiment is 15m
3/ m
2h, makes the content of acetic acid and formaldehyde in the gas after composite solution absorptive unit be down to 0.045 mg/m
3below.By absorb waste gas composite solution by pipeline 7 by valve F-3 with 0.5m
3the speed of/d is discharged, enter biochemical treatment tank, utilize composite solution storage tank V-2 by valve F-1, composite solution storage tank V-3 to be supplemented the fresh composite solution of equivalent simultaneously, make the liquid level in composite solution storage tank V-3 keep constant, the volume of composite solution storage tank V-3 is 35m
3.Now in system, still contain 8mg/m
3dimethylamine gas and 26mg/m
3ammonia, again gas is entered to the rare organic acid liquid absorptive unit of absorption tower T-1 by vapour-liquid spacer assembly M-1, utilize the weak solution of the citric acid of 5.0M to absorb, the spray flux that regulates citric acid solution according to the content of dimethylacetylamide, dimethylamine and ammonia in gas, the sprinkle density of the present embodiment is 18m
3/ m
2h, makes them substantially be completely absorbed, last, and the gas after being cleaned is emptying by valve F-5 and pipeline 9, and gas total content harmful in emptying gas is down to 0.25mg/m
3below.The citric acid solution absorbing after waste gas will be from pipeline 8, valve F-4 and pipeline 10 with 0.4m
3the speed of/d is discharged, and removes biochemical treatment tank; Utilize organic acid absorption liquid storage tank V-4, by valve F-2, organic acid absorption liquid storage tank V-5 is carried out to equivalent simultaneously and supplement, make the liquid level in organic acid absorption liquid storage tank V-5 keep constant, the volume of organic acid absorption liquid storage tank V-5 is 27m
3.
embodiment 5: produce waste gas absorption in 5kt spandex production process take dimethyl formamide (DMF) as solvent per year
Mode of operation is as embodiment 1.The waste gas of collecting in waste gas storage tank V-1 (containing dimethyl formamide steam, the formaldehyde steam of 46mg/m3, the dimethylamine gas of 20mg/m3 and the ammonia of 16.5mg/m3 of 23mg/m3) is passed into the composite solution absorptive unit (composite solution of the NaOH that composite solution is 1.8M and 0.1M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1, according to the content of the exhaust gas constituents in gas and exhaust-gas treatment amount, the spray flux of controlling composite solution with flowmeter FM-1, the sprinkle density of the present embodiment is 20m
3/ m
2h, makes the total content of formaldehyde and dimethyl formamide in the gas after composite solution absorptive unit be down to 0.1 mg/m
3below.By absorb waste gas composite solution by pipeline 7 by valve F-3 with 0.25m
3the speed of/d is discharged, enter biochemical treatment tank, utilize composite solution storage tank V-2 by valve F-1, composite solution storage tank V-3 to be supplemented the fresh composite solution of equivalent simultaneously, make the liquid level in composite solution storage tank V-3 keep constant, the volume of composite solution storage tank V-3 is 40m
3.Now in gas, still contain 16mg/m
3dimethylamine gas and 9mg/m
3ammonia, again gas is entered to the rare organic acid liquid absorptive unit of absorption tower T-1 by vapour-liquid spacer assembly M-1, utilize the weak solution of the citric acid of 1.1M to absorb, regulate the spray flux of rare citric acid according to the content of dimethylamine in gas and ammonia, the sprinkle density of the present embodiment is 18m
3/ m
2h, makes the content of dimethylamine gas and ammonia in waste gas be down to respectively 0.08mg/m
3below.Finally, the gas after being cleaned is emptying by valve F-5 and pipeline 9, and gas total content harmful in emptying gas is down to 0.3mg/m
3below.The organic acid soln absorbing after waste gas will be from pipeline 8, valve F-4 and pipeline 10 with 0.3m
3the speed of/d is discharged, and removes biochemical treatment tank; Utilize organic acid absorption liquid storage tank V-4, by valve F-2, organic acid absorption liquid storage tank V-5 is carried out to equivalent simultaneously and supplement, make the liquid level in organic acid absorption liquid storage tank V-5 keep constant, the volume of organic acid absorption liquid storage tank V-5 is 25m
3.
embodiment 6: produce 10kt spandex workshop waste gas absorption take dimethyl formamide (DMF) as solvent per year
Mode of operation is as embodiment 1.The waste gas of collecting in waste gas storage tank V-1 (is contained to 55mg/m
3dimethyl formamide steam, 216mg/m
3formaldehyde steam, 117mg/m
3dimethylamine gas and 5mg/m
3ammonia) pass into the composite solution absorptive unit (composite solution of the NaOH that composite solution is 0.5M and 1.5M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1, according to the content of the exhaust gas constituents in gas and exhaust-gas treatment amount, control the spray flux of rare composite solution with flowmeter FM-1, the sprinkle density of the present embodiment is 28m
3/ m
2h, makes the total content of formaldehyde and dimethyl formamide in the gas after composite solution absorptive unit be down to 0.1 mg/m
3below.By absorb waste gas composite solution by pipeline 7 by valve F-3 with 0.35m
3the speed of/d is discharged, enter biochemical treatment tank, utilize composite solution storage tank V-2 by valve F-1, composite solution storage tank V-3 to be supplemented the fresh composite solution of equivalent simultaneously, make the liquid level in composite solution storage tank V-3 keep constant, the volume of composite solution storage tank V-3 is 48m
3.Now in gas, still contain 78mg/m
3dimethylamine gas and 2.6mg/m
3ammonia, again gas is entered to the rare organic acid liquid absorptive unit of absorption tower T-1 by vapour-liquid spacer assembly M-1, utilize the weak solution of the citric acid of 1.2 M to absorb, (sprinkle density is 20m to regulate the spray flux of rare citric acid according to the content of dimethylamine in gas and ammonia
3/ m
2.h), make the content of dimethylamine gas and ammonia in waste gas be down to respectively 0.08mg/m
3below.Finally, the gas after being cleaned is emptying by valve F-5 and pipeline 9, and gas total content harmful in emptying gas is down to 0.4mg/m
3below.The organic acid soln absorbing after waste gas will be from pipeline 8, valve F-4 and pipeline 10 with 0.35m
3the speed of/d is discharged, and removes biochemical treatment tank; Utilize organic acid absorption liquid storage tank V-4, by valve F-2, organic acid absorption liquid storage tank V-5 is carried out to equivalent simultaneously and supplement, make the liquid level in organic acid absorption liquid storage tank V-5 keep constant, the volume of organic acid absorption liquid storage tank V-5 is 30m
3.
Claims (4)
1. the technique of purified treatment in a spandex production process exhaust gas centralized, it is characterized in that adopting spandex production process waste gas absorption tower, in spandex production process waste gas absorption tower body, set up upper and lower two absorptive units, wherein lower unit is composite solution absorptive unit, upper unit is organic acid solution absorptive unit, between composite solution absorptive unit and organic acid solution absorptive unit, have vapour-liquid spacer assembly (M-1) that Unit two are separated, and gas can enter into from the composite solution absorptive unit of bottom the organic acid solution absorptive unit on top, gas distributor (A-1) is arranged at the bottom of composite solution absorptive unit, gas distributor (A-1) joins with the exhaust inlet pipe outside tower, the middle part of composite solution absorptive unit is GAS ABSORPTION district, filler or column plate filling for this district, liquid distribution trough (Q-1) is arranged at the top of composite solution absorptive unit, liquid distribution trough (Q-1) is connected with fluid flowmeter (FM-1) by centrifugal pump (P-2) with the composite solution storage tank (V-3) outside tower, composite solution absorptive unit bottom has pipeline (2) to communicate with composite solution storage tank (V-3), form composite solution closed circuit, organic acid solution absorptive unit bottom is vapour-liquid spacer assembly (M-1), gas enters organic acid solution absorptive unit by vapour-liquid spacer assembly (M-1), the middle part of organic acid solution absorptive unit is GAS ABSORPTION district, filler or column plate filling for this district, liquid distribution trough (Q-2) is arranged at the top of organic acid solution absorptive unit, liquid distribution trough (Q-2) is connected with fluid flowmeter (FM-2) by centrifugal pump (P-3) with the organic acid solution storage tank (V-5) outside tower, organic acid solution absorptive unit bottom has pipeline (5) to communicate with organic acid solution storage tank (V-5), form organic acid cycle loop, waste gas outlet after purified treatment is arranged at organic acid solution absorptive unit top, the concrete steps of described purification process technique are as follows:
The gas that step 1. is discharged each vacuum pump outlet of the outfits such as spandex production process polymerization workshop section, Pen Si workshop section, refining workshop section, solvent recovery workshop section is collected, enter gas reservoir (V-1), then gas is concentrated to the gas distributor (A-1) of the composite solution absorptive unit bottom that is delivered to absorption tower (T-1) by air blast (P-1) and pipeline (1), enter absorption tower (T-1)
Step 2. is in the composite solution absorptive unit of absorption tower (T-1), extract composite solution by centrifugal pump (P-2) out by composite solution storage tank (V-3), through piping (3) and fluid flowmeter (FM-1), from absorption tower, the liquid distribution trough (Q-1) at (T-1) composite solution absorptive unit top sprays downwards, absorb to remove acids and the formaldehyde material in gas, then from absorption tower, (T-1) composite solution absorptive unit bottom passes back into composite solution storage tank (V-3), described composite solution is the solution that contains alkali and salt, alkali in composite solution is NaOH or Na
2cO
3or NaHCO3, or adopt Ca (OH)
2,or other inorganic and organic basic material, wherein the concentration of alkali lye is between 0.1M ~ 5M, salt in composite solution is natrium nitrosum, its concentration is about between 0.1M ~ 5M, this absorptive unit can load with filler or column plate, and its concrete height and specification are determined by concrete commercial scale, according to the content of each waste gas component in gas reservoir (V-1), controlled the spray flux of composite solution by fluid flowmeter (FM-1)
Composite solution in the composite solution absorptive unit of step 3. absorption tower (T-1) is in circulation, the composite solution partially absorbing after waste gas is discharged from pipeline (7), valve (F-3) and pipeline (10), remove biochemical treatment tank, the amount of discharge is determined according to the online basicity that detects composite solution; Recycling composite solution storage tank (V-2) supplements the fresh composite solution of equivalent to composite solution storage tank (V-3) by valve (F-1), make the liquid level in composite solution storage tank (V-3) keep constant, the volume of composite solution storage tank (V-3) was determined by internal circulating load and the time of staying of composite solution
The top organic acid solution absorptive unit that the gas of step 4. after the composite solution absorptive unit of absorption tower (T-1) enters into absorption tower (T-1) by the vapour-liquid spacer assembly (M-1) at composite solution absorptive unit top, absorption tower (T-1) absorbs, the gas vent of vapour-liquid spacer assembly (M-1) is above organic acid solution liquid level, prevent that organic acid solution from entering into composite solution absorptive unit, this absorptive unit can load with filler or column plate, its concrete height and specification are determined by concrete commercial scale
Centrifugal pump for step 5. (P-3) is extracted the liquid in organic acid absorption liquid storage tank (V-5) out, through fluid flowmeter (FM-2) and pipeline (6), enter packing layer or the column plate of the top organic acid solution absorptive unit on absorption tower (T-1) by organic acid solution absorptive unit top liquid distribution trough (Q-2) ejection, adverse current waste gas is upwards carried out to reactive absorption, then from absorption tower, the bottom of (T-1) top organic acid solution absorptive unit passes back into organic acid absorption liquid storage tank (V-5), and the organic acid of use comprises citric acid, lactic acid, tartaric acid or benzene sulfonic acid; The concentration of organic acid absorption liquid is between 0.1M-5.0M,
Organic acid solution in the organic acid absorptive unit of top, step 6. absorption tower (T-1) is in circulation, the organic acid solution partially absorbing after waste gas is discharged from pipeline (8), valve (F-4) and pipeline (10), remove biochemical treatment tank, the amount of discharge is determined according to the online basicity that detects organic acid solution; Utilize organic acid absorption liquid storage tank (V-4), by valve (F-2), organic acid absorption liquid storage tank (V-5) is carried out to equivalent supplements simultaneously, make the liquid level in organic acid absorption liquid storage tank (V-5) keep constant, the volume of organic acid absorption liquid storage tank (V-5) was determined by internal circulating load and the time of staying of absorption liquid
Step 7. is last, and gas is organic acid absorptive unit top, (T-1) top from absorption tower, discharges by valve (F-5) and pipeline (9), and in the gas of discharge, the quality percentage total content of pernicious gas is less than 0.5mg/m
3, the fluid discharge that pipeline (10) is discharged focuses on to biochemistry pool.
2. purification process technique in exhaust gas centralized according to claim 1, is characterized in that: the organic acid that step 5 is used is citric acid, the concentration of organic acid absorption liquid is between 0.4M-1.5M.
3. purification process technique in exhaust gas centralized according to claim 1, is characterized in that: the composite solution described in step 2, in the time of the increased content of harmful components in gas phase, the concentration of composite solution and internal circulating load are all heightened corresponding.
4. purification process technique in exhaust gas centralized according to claim 1, is characterized in that: the organic acid absorption liquid described in step 5, in the time of the increased content of harmful components in gas phase, the concentration of organic acid soln and internal circulating load are all heightened corresponding.
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