CN102343205A - 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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- CN102343205A CN102343205A CN2011102001293A CN201110200129A CN102343205A CN 102343205 A CN102343205 A CN 102343205A CN 2011102001293 A CN2011102001293 A CN 2011102001293A CN 201110200129 A CN201110200129 A CN 201110200129A CN 102343205 A CN102343205 A CN 102343205A
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- 239000002912 waste gas Substances 0.000 title claims abstract description 66
- 229920002334 Spandex Polymers 0.000 title claims abstract description 34
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 34
- 239000004759 spandex Substances 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 24
- 238000000746 purification Methods 0.000 title claims abstract description 10
- 238000010521 absorption reaction Methods 0.000 claims abstract description 152
- 239000007789 gas Substances 0.000 claims abstract description 149
- 239000002131 composite material Substances 0.000 claims abstract description 129
- 150000007524 organic acids Chemical class 0.000 claims abstract description 96
- 239000003513 alkali Substances 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims description 128
- 238000003860 storage Methods 0.000 claims description 94
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 claims description 45
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- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 24
- 239000007921 spray Substances 0.000 claims description 20
- 230000004907 flux Effects 0.000 claims description 15
- 125000006850 spacer group Chemical group 0.000 claims description 14
- 239000002904 solvent Substances 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 11
- 239000012071 phase Substances 0.000 claims description 11
- 239000000945 filler Substances 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 238000009826 distribution Methods 0.000 claims description 9
- KEAYESYHFKHZAL-UHFFFAOYSA-N Sodium Chemical compound [Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 claims description 8
- 238000005516 engineering process Methods 0.000 claims description 8
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 claims description 8
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 5
- 230000000505 pernicious effect Effects 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- SRSXLGNVWSONIS-UHFFFAOYSA-N benzenesulfonic acid Chemical compound OS(=O)(=O)C1=CC=CC=C1 SRSXLGNVWSONIS-UHFFFAOYSA-N 0.000 claims description 4
- 229940092714 benzenesulfonic acid Drugs 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 claims description 4
- 238000001514 detection method Methods 0.000 claims description 4
- 238000011049 filling Methods 0.000 claims description 4
- 239000004310 lactic acid Substances 0.000 claims description 4
- 235000014655 lactic acid Nutrition 0.000 claims description 4
- 238000012856 packing Methods 0.000 claims description 4
- 150000003839 salts Chemical class 0.000 claims description 4
- FEWJPZIEWOKRBE-UHFFFAOYSA-N Tartaric acid Natural products [H+].[H+].[O-]C(=O)C(O)C(O)C([O-])=O FEWJPZIEWOKRBE-UHFFFAOYSA-N 0.000 claims description 3
- 239000006096 absorbing agent Substances 0.000 claims description 3
- 238000006116 polymerization reaction Methods 0.000 claims description 3
- 239000011975 tartaric acid Substances 0.000 claims description 3
- FEWJPZIEWOKRBE-JCYAYHJZSA-N Dextrotartaric acid Chemical compound OC(=O)[C@H](O)[C@@H](O)C(O)=O FEWJPZIEWOKRBE-JCYAYHJZSA-N 0.000 claims description 2
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- 239000007791 liquid phase Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 238000007670 refining Methods 0.000 claims description 2
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 2
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 2
- 235000002906 tartaric acid Nutrition 0.000 claims description 2
- 235000015165 citric acid Nutrition 0.000 claims 1
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 abstract description 52
- ROSDSFDQCJNGOL-UHFFFAOYSA-N Dimethylamine Chemical compound CNC ROSDSFDQCJNGOL-UHFFFAOYSA-N 0.000 abstract description 51
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 48
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 5
- WSFSSNUMVMOOMR-NJFSPNSNSA-N methanone Chemical compound O=[14CH2] WSFSSNUMVMOOMR-NJFSPNSNSA-N 0.000 abstract description 3
- 230000009102 absorption Effects 0.000 abstract 7
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 abstract 1
- 238000003915 air pollution Methods 0.000 abstract 1
- 239000012080 ambient air Substances 0.000 abstract 1
- 230000009103 reabsorption Effects 0.000 abstract 1
- 229910021529 ammonia Inorganic materials 0.000 description 29
- WFKAJVHLWXSISD-UHFFFAOYSA-N isobutyramide Chemical compound CC(C)C(N)=O WFKAJVHLWXSISD-UHFFFAOYSA-N 0.000 description 13
- 238000009987 spinning Methods 0.000 description 9
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 8
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- 239000000835 fiber Substances 0.000 description 5
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
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- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
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- 229920002635 polyurethane Polymers 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
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- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 229920001400 block copolymer Polymers 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
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- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 150000007530 organic bases Chemical class 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 238000007500 overflow downdraw method Methods 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
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- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
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Images
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- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
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 spandex production process waste gas and concentrate the technology and the device of purified treatment.
Background technology
Polyurethane elastomeric fiber is claimed Spandex (Spandex) abroad, and the trade name of China is a spandex.Spandex has the incomparable elasticity of other any fibers, and its elongation at break, reaches as high as more than 800% usually 500%～700% greater than 400%, and the elastic restoration ratio during deformation 300% reaches more than 95%, has good fatigue performance.From manufacturing process, route is produced in polyurethane fibre industry spinning at present has four kinds, i.e. dry spinning, wet spinning, reaction method spinning and fusion method spinning.The solvent that the first three spin processes is used is DMF and DMAc, and wherein the dry spinning production capacity accounts for aggregated capacity 86.39%, is 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 following:
Polyethers and vulcabond form prepolymer with 1: 2 mol ratio under certain reaction temperature and time condition; Prepolymer is after the solvent dissolving; Add dimethylamine again and carry out chain propagation reaction; Form block copolymer solution; Through operations such as mixing, filtration, deaerations, process the spinning solution of performance uniformity again.Then with the measuring pump quantitative and even be pressed into spinneret.Under the effect of pressure, spinning solution is extruded from the spinneret pore and forms the strand thread, and gets into the path.Be filled with hot-air in the path, the solvent in the strand thread volatilized rapidly, and taken away by air, strand concentration improves constantly until solidifying, and meanwhile the strand thread is stretched and attenuates, and is wound into certain web-like at last.
Spandex production combines chemical industry and textile of chemical fibre a lot of contents and the characteristics in producing, and polymerization workshop section, heating agent system, assembly clean and make with extra care workshop section etc. and be chemical process, and spinning, is wound as typical chemical fibre spinning production technology.Because the technology of spandex production at present and the material characteristic of use cause the whole process of production from raw material storage to the product output that toxic emission is all arranged.Especially in the path gas of high temperature spray silk process; Except that most of air, steam; Also contain toxic organic compounds such as dimethylamine, formaldehyde, acetate, dimethylacetylamide (DMAc), dimethyl formamide (DMF), ammonia, methyl alcohol, they will be to serious environment pollution as if directly emptying.
At present, the method for handling waste gas in the spandex production process generally is direct emptying, and therefore the harm that the environment of production plant area and periphery is caused is self-evident.
Summary of the invention
The purpose of this invention is to provide a kind of spandex production process waste gas and concentrate the new technology and the device of purified treatment, shown in accompanying drawing 1.The present invention sets up two absorptive units up and down in same absorption tower body; Wherein lower unit is the composite solution absorptive unit; Upper unit is the organic acid soln absorptive unit; Through after the absorption of these two unit; The pernicious gas content that is processed in the gas will can satisfy relevant environmental requirement fully, reaches the purpose of cleaner production.
The object of the invention can be realized through following technical solution:
One kinds of spandex production process gas absorption tower, the structure in Figure 1 shows the absorption tower T-1, the upper and lower absorber established within the absorption unit, wherein the lower unit is a complex solution absorption unit, the upper unit is a liquid absorbing acid element, and an organic acid complex solution absorption cell between the liquid absorbing units vapor - liquid isolating means M-1 of the two units are separated from the lower part of the gas absorption cell complex solution into the organic liquid to the upper part of the absorption cell; compound Solution absorption cell with gas sparger at the bottom of A-1, A-1 gas sparger outside the tower inlet gas phase, the complex solution in the middle of the gas absorption cell absorption zone, the area can be filled with a filler material or trays, complex solution absorption unit on top of one liquid distributor Q-1, Q-1 liquid distributor outside the tower complex solution storage tank V-3 by the pump P-2 and FM-1 is connected to liquid flow, the absorption cell complex solution the bottom of the pipe 2 and the composite solution storage tank V-3 interlinked to form a composite solution circulation loop; organic fluid vapor absorption unit bottom - liquid isolation device M-1, the gas by steam - liquid isolation device M-1 into the organic liquid absorption unit, an organic acid solution in the middle of the gas absorption cell absorption zone, the area can be filled with a filler material or trays, organic liquid absorbing units on top of one liquid distributor Q-2, Q-2 liquid distributor outside the tower organic liquid storage tank V-5 by pump P-3 and FM-2 connected to the liquid flow, organic liquid absorbing unit 5 and the bottom of the pipe storage tank V-5 organic liquid is connected, forming organic liquid circulation circuit, organic liquid absorption unit at the top of the exhaust gas purification exports.
Above-mentioned spandex production process waste gas absorption tower equipment; Described gas-liquid spacer assembly M-1 is that (its cross section is a rectangle by one or more riser; Circle or other shape) form with liquid-blocking cap; Gas phase rises through riser from lower unit; And along the gap between riser and the liquid-blocking cap from around overflow; And the liquid phase of upper unit is stopped inflow upper unit bottom by liquid-blocking cap in dropping process, and flows out via pipeline 5.
A kind of spandex production process waste gas is concentrated purification process technique, its flow process as shown in Figure 1, it comprises the following steps:
(content of main harmful components is respectively 1-500mg/m to the gas that each vacuum pump outlet of outfits such as step 1. pair spandex production process polymerization workshop section, spray silk workshop section, refining workshop section, solvent recovery workshop section is discharged
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, get into gas reservoir V-1, with pipeline 1 gas is concentrated the gas distributor A-1 of the composite solution absorptive unit bottom that is delivered to absorption tower T-1 through air blast P-1 then, entering absorption tower T-1,
According to the content of each waste gas component in the gas reservoir V-1,, make and reduce to 0.1mg/m respectively through the content of formaldehyde and acetate in the gas behind the T-1 composite solution absorptive unit of absorption tower by the spray flux of fluid flowmeter FM-1 control composite solution
3Below,
When the content of harmful components in the gas phase increased, the concentration of composite solution and internal circulating load were all heightened corresponding,
Composite solution in the T-1 composite solution absorptive unit of step 3. absorption tower is in circulation; The composite solution that partially absorbs behind the waste gas is discharged from pipeline 7, valve F-3 and pipeline 10; Remove biochemical treatment tank, the amount of discharge is then confirmed according to the basicity of online detection composite solution; Utilize composite solution storage tank V-2 composite solution storage tank V-3 to be replenished the fresh composite solution of equivalent through valve F-1 again; Make the liquid level among the composite solution storage tank V-3 keep constant, the volume of composite solution storage tank V-3 is by the internal circulating load and the time of staying decision of composite solution.
The top organic acid solution absorptive unit that the vapour-liquid spacer assembly M-1 of the gas of step 4. after through absorption tower T-1 composite solution absorptive unit through T-1 composite solution absorptive unit top, absorption tower enters into absorption tower T-1 absorbs; The gas vent of vapour-liquid spacer assembly M-1 is above the organic acid solution liquid level; Prevent that organic acid solution from entering into the composite solution absorptive unit; This absorptive unit can be with filler or column plate filling; Its concrete height and specification are by concrete commercial scale decision
When the content of harmful components in the gas phase increased, the concentration of organic acid soln and internal circulating load were 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 that partially absorbs behind the waste gas is discharged from pipeline 8, valve F-4 and pipeline 10; Remove biochemical treatment tank, the amount of discharge is then confirmed according to the basicity of online detection organic acid solution; Utilizing organic acid absorption liquid storage tank V-4 through valve F-2 organic acid absorption liquid storage tank V-5 to be carried out equivalent simultaneously replenishes; Make the liquid level among the organic acid absorption liquid storage tank V-5 keep constant; The volume of organic acid absorption liquid storage tank V-5 is by the internal circulating load and the time of staying decision of absorption liquid
The last gas of step 7. is T-1 top organic acid absorptive unit top from the absorption tower, discharges through valve F-5 and pipeline 9, and the quality percentage total content of pernicious gas is less than 0.5mg/m in the gas of discharge
3
Above-mentioned spandex production process waste gas is concentrated purification process technique, and the gas distributor A-1 of the composite solution absorptive unit of the absorption tower T-1 described in the step 1 bottom can be arranged on below the liquid level of composite solution of composite solution absorptive unit bottom of absorption tower T-1.
The present invention concentrates the technology of purified treatment to innovate to conventional spandex production process waste gas, and the pernicious gas among the gas reservoir V-1 comprises: dimethylacetylamide (DMAc), dimethyl formamide (DMF), acetate, formaldehyde, dimethylamine, ammonia.Through controlling the spray flux of two absorptive units; Gas is through behind the composite solution absorptive unit and organic acid absorptive unit of absorption tower T-1, and the content of dimethylacetylamide (DMAc), dimethyl formamide (DMF), acetate, formaldehyde steam, dimethylamine and ammonia is less than 0.5 mg/m
3, and any single gas phase content all less than 0.1 mg/m
3When equipment material allows, not volatile inorganic acid solutions such as dilute sulfuric acid, sulfonic acid can be adopted, and the volatile solvent soln of secondary pollution should not be possibly caused with hydrochloric acid and nitric acid etc.
Technology of the present invention has the following advantages: (1) is integrated two absorptive units up and down in same seat tower, have practiced thrift the space, have simplified flow process; (2) adopt the vapour-liquid spacer assembly to make the unimpeded liquid of two sections gas circuit then not communicate; (3) in the composite solution absorptive unit, utilize alkali lye and sour gas generation neutralization reaction to produce stable compound; In the 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 the air, prevented the pollution of pernicious gas environment.
Description of drawings
Fig. 1 is a schematic flow sheet of the present invention.Wherein:
T-1 is the absorption tower, and P-1 is an air blast, and P-2, P-3 are the fluid delivery pump; V-1 is the waste gas storage tank; V-2 is that pure water storage tank, V-3, V-5 are the absorption liquid storage tank, and V-4 is the 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 are gas distributor, and FM-1, FM-2 are fluid flowmeter; M-1 is the vapour-liquid spacer assembly, and 1,2,3,4,5,6,7,8,9,10 is pipeline.
The specific embodiment
Below further specify the present invention through embodiment.
Embodiment 1: with dimethylacetylamide (DMAc) is that solvent is produced waste gas absorption in the 3kt spandex production process per year
Spandex workshop waste gas absorption process operating procedure is shown in accompanying drawing one.This system mainly is 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 among the waste gas storage tank V-1 (is contained 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) feed the composite solution absorptive unit (composite solution is the NaOH of 0.1M and the composite solution of 0.3M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1; Content according to the exhaust gas constituents in the gas; And exhaust-gas treatment amount; With the spray flux of flowmeter FM-1 control composite solution, the liquid spraying density of present embodiment is 45m
3/ m
2H makes and reduces to 0.04 mg/m through the quality percentage composition of acetate in the gas behind the composite solution absorptive unit
3, content of formaldehyde is reduced to 0.07 mg/m
3With the composite solution of absorbing waste gas through pipeline 7 by valve F-3 with 0.2m
3The speed of/d is discharged; Get into biochemical treatment tank; Utilize composite solution storage tank V-2 through valve F-1 composite solution storage tank V-3 to be replenished the fresh composite solution of equivalent simultaneously, make that the liquid level among the composite solution storage tank V-3 keeps constant, the volume of composite solution storage tank V-3 is 80m
3Still contain 42 mg/ms in the gas this moment
3Dimethylamine gas and 8mg/m
3Ammonia; Again gas is got into the rare organic acid liquid absorptive unit of absorption tower T-1 through vapour-liquid spacer assembly M-1; Utilize the benzene sulfonic acid solution of 0.1M to absorb, the sprinkle density of regulating the spray flux present embodiment of benzene sulfonic acid liquid according to the content of dimethylamine in the gas and ammonia is 36m
3/ m
2H makes that dimethylamine gas and ammonia are absorbed basically fully in the waste gas, and last, the gas after being cleaned is through valve F-5 and pipeline 9 emptyings, and the gas total content that is harmful in the gas of emptying is reduced to 0.25 mg/m
3, the organic acid soln after the absorbing 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 through valve F-2 organic acid absorption liquid storage tank V-5 to be carried out equivalent simultaneously and replenish, make that the liquid level among the organic acid absorption liquid storage tank V-5 keeps constant, the volume of organic acid absorption liquid storage tank V-5 is 30m
3
Embodiment 2: with dimethylacetylamide (DMAc) is that solvent is produced waste gas absorption in the 5kt spandex production process per year
Spandex workshop waste gas absorption process operating procedure is shown in accompanying drawing one.This system mainly is 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 among the waste gas storage tank V-1 (is contained 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) feed the composite solution absorptive unit (composite solution is the sodium carbonate of 0.4M and the composite solution of 0.5M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1; Content according to the exhaust gas constituents in the gas; And exhaust-gas treatment amount; With the spray flux of flowmeter FM-1 control composite solution, the sprinkle density of present embodiment is 25m
3/ m
2H makes and reduces to 0.090mg/m through the quality percentage composition of acetate in the gas behind the composite solution absorptive unit
3Below, formaldehyde is reduced to 0.08 mg/m
3Below, with the composite solution of absorbing waste gas through pipeline 7 by valve F-3 with 0.4m
3The speed of/d is discharged; Get into biochemical treatment tank; Utilize composite solution storage tank V-2 through valve F-1 composite solution storage tank V-3 to be replenished the fresh composite solution of equivalent simultaneously, make that the liquid level among the composite solution storage tank V-3 keeps constant, the volume of composite solution storage tank V-3 is 40m
3Still contain 25mg/m in the gas this moment
3Dimethylamine gas and 9 mg/m
3Ammonia; Again gas is got into the rare organic acid solution absorption unit of absorption tower T-1 through 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 the gas and ammonia
3/ m
2H), make that dimethylamine gas and ammonia are absorbed basically fully in the waste gas, last, the gas after being cleaned is through valve F-5 and pipeline 9 emptyings, and dimethylamine content is 0.05 mg/m in the gas of emptying
3, ammonia level is 0.01 mg/m
3, harmful gas total content is lower than 0.3 mg/m
3Tartaric acid solution after the absorbing 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 through valve F-2 organic acid absorption liquid storage tank V-5 to be carried out equivalent simultaneously and replenish, make that the liquid level among the organic acid absorption liquid storage tank V-5 keeps constant, the volume of organic acid absorption liquid storage tank V-5 is 27m
3
Embodiment 3: with dimethylacetylamide (DMAc) is that solvent is produced waste gas absorption in the 10kt spandex production process per year
Mode of operation such as embodiment 1.With waste gas (the dimethylacetylamide steam, 31 mg/m that contain 50mg/m3 that collect among the waste gas storage tank V-1
3Formaldehyde; The dimethylamine gas of the acetic acid steam of 400mg/m3,100mg/m3 and the ammonia of 5mg/m3) with the composite solution absorptive unit (solution be the sodium acid carbonate of 3.0M and composite solution that 3.5M natrium nitrosum form) of air blast P-1 through piping 1 and gas distributor A-1 feeding absorption tower T-1; Content and exhaust-gas treatment amount according to the exhaust gas constituents in the gas; With the spray flux of flowmeter FM-1 control composite solution, the sprinkle density of present embodiment is 8m
3/ m
2H), feasible content through acetate in the gas behind the composite solution absorptive unit is reduced to 0.01 mg/m
3, and content of formaldehyde is reduced to 0.02 mg/m
3With the composite solution of absorbing waste gas through pipeline 7 by valve F-3 with 0.4m
3/ d discharges and gets into biochemical treatment tank, utilizes composite solution storage tank V-2 through valve F-1 composite solution storage tank V-3 to be replenished the fresh composite solution of equivalent simultaneously, makes that the liquid level among the composite solution storage tank V-3 keeps constant, and the volume of composite solution storage tank V-3 is 15m
3Still contain 49mg/m in the gas this moment
3Dimethylamine gas and 3.25mg/m
3Ammonia; Again gas is got into the rare organic acid solution absorption unit of absorption tower T-1 through vapour-liquid spacer assembly M-1; Utilize the weak solution of the lactic acid of 3.0M to absorb, according to the spray flux that the content of dimethylamine in the gas and ammonia is regulated rare lactic acid, the sprinkle density of present embodiment is 15m
3/ m
2H makes that dimethylamine gas and ammonia are absorbed basically fully in the waste gas, and last, the gas after being cleaned is through valve F-5 and pipeline 9 emptyings, and the gas total content that is harmful in the gas of emptying is reduced to 0.3mg/m
3, and the content of single gas phase all is lower than 0.1 mg/m
3Organic acid soln after the absorbing 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 through valve F-2 organic acid absorption liquid storage tank V-5 to be carried out equivalent simultaneously and replenish, make that the liquid level among the organic acid absorption liquid storage tank V-5 keeps constant, the volume of organic acid absorption liquid storage tank V-5 is 25m
3
Embodiment 4: with dimethylacetylamide (DMAc) is that solvent is produced waste gas absorption in the 20kt spandex production process per year
Mode of operation such as embodiment 1.The waste gas of collecting among the waste gas storage tank V-1 (is contained 20mg/m
3Dimethylacetylamide steam, 33mg/m
3Formaldehyde, 156mg/m
3Acetic acid steam, 12mg/m
3Dimethylamine gas and 58mg/m
3Ammonia) feed the composite solution absorptive unit (composite solution is the NaOH of 5.0M and the composite solution of 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 exhaust gas constituents content in the gas and exhaust-gas treatment amount; Control the spray flux of rare composite solution with flowmeter FM-1, the sprinkle density of present embodiment is 15m
3/ m
2H makes and reduces to 0.045 mg/m through the content of acetate and formaldehyde in the gas behind the composite solution absorptive unit
3Below.With the composite solution of absorbing waste gas through pipeline 7 by valve F-3 with 0.5m
3The speed of/d is discharged; Get into biochemical treatment tank; Utilize composite solution storage tank V-2 through valve F-1 composite solution storage tank V-3 to be replenished the fresh composite solution of equivalent simultaneously, make that the liquid level among the composite solution storage tank V-3 keeps constant, the volume of composite solution storage tank V-3 is 35m
3Still contain 8mg/m in the system this moment
3Dimethylamine gas and 26mg/m
3Ammonia; Again gas is got into the rare organic acid liquid absorptive unit of absorption tower T-1 through vapour-liquid spacer assembly M-1; Utilize the weak solution of the citric acid of 5.0M to absorb; According to the spray flux that the content of dimethylacetylamide, dimethylamine and ammonia in the gas is regulated citric acid solution, the sprinkle density of present embodiment is 18m
3/ m
2H makes them absorbed fully basically, and is last, and the gas after being cleaned is through valve F-5 and pipeline 9 emptyings, and gas total content harmful in the gas of emptying is reduced to 0.25mg/m
3Below.Citric acid solution after the absorbing 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 through valve F-2 organic acid absorption liquid storage tank V-5 to be carried out equivalent simultaneously and replenish, make that the liquid level among the organic acid absorption liquid storage tank V-5 keeps constant, the volume of organic acid absorption liquid storage tank V-5 is 27m
3
Embodiment 5: with dimethyl formamide (DMF) is that solvent is produced waste gas absorption in the 5kt spandex production process per year
Mode of operation such as embodiment 1.The waste gas of collecting among the waste gas storage tank V-1 (containing the dimethyl formamide steam of 23mg/m3, the formaldehyde steam of 46mg/m3, the dimethylamine gas of 20mg/m3 and the ammonia of 16.5mg/m3) is fed the composite solution absorptive unit (composite solution is the NaOH of 1.8M and the composite solution that the 0.1M natrium nitrosum is formed) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1; Content and exhaust-gas treatment amount according to the exhaust gas constituents in the gas; With the spray flux of flowmeter FM-1 control composite solution, the sprinkle density of present embodiment is 20m
3/ m
2H makes and reduces to 0.1 mg/m through the total content of formaldehyde and dimethyl formamide in the gas behind the composite solution absorptive unit
3Below.With the composite solution of absorbing waste gas through pipeline 7 by valve F-3 with 0.25m
3The speed of/d is discharged; Get into biochemical treatment tank; Utilize composite solution storage tank V-2 through valve F-1 composite solution storage tank V-3 to be replenished the fresh composite solution of equivalent simultaneously, make that the liquid level among the composite solution storage tank V-3 keeps constant, the volume of composite solution storage tank V-3 is 40m
3Still contain 16mg/m in the gas this moment
3Dimethylamine gas and 9mg/m
3Ammonia; Again gas is got into the rare organic acid liquid absorptive unit of absorption tower T-1 through vapour-liquid spacer assembly M-1; Utilize the weak solution of the citric acid of 1.1M to absorb, according to the spray flux that the content of dimethylamine in the gas and ammonia is regulated rare citric acid, the sprinkle density of present embodiment is 18m
3/ m
2H makes that the content of dimethylamine gas and ammonia is reduced to 0.08mg/m respectively in the waste gas
3Below.At last, the gas after being cleaned is through valve F-5 and pipeline 9 emptyings, and gas total content harmful in the gas of emptying is reduced to 0.3mg/m
3Below.Organic acid soln after the absorbing 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 through valve F-2 organic acid absorption liquid storage tank V-5 to be carried out equivalent simultaneously and replenish, make that the liquid level among the organic acid absorption liquid storage tank V-5 keeps constant, the volume of organic acid absorption liquid storage tank V-5 is 25m
3
Embodiment 6: with dimethyl formamide (DMF) is that solvent is produced the absorption of 10kt spandex workshop waste gas per year
Mode of operation such as embodiment 1.The waste gas of collecting among the waste gas storage tank V-1 (is contained 55mg/m
3Dimethyl formamide steam, 216mg/m
3Formaldehyde steam, 117mg/m
3Dimethylamine gas and 5mg/m
3Ammonia) feed the composite solution absorptive unit (composite solution is the NaOH of 0.5M and the composite solution of 1.5M natrium nitrosum composition) of absorption tower T-1 through piping 1 and gas distributor A-1 with air blast P-1; Content and exhaust-gas treatment amount according to the exhaust gas constituents in the gas; Control the spray flux of rare composite solution with flowmeter FM-1, the sprinkle density of present embodiment is 28m
3/ m
2H makes and reduces to 0.1 mg/m through the total content of formaldehyde and dimethyl formamide in the gas behind the composite solution absorptive unit
3Below.With the composite solution of absorbing waste gas through pipeline 7 by valve F-3 with 0.35m
3The speed of/d is discharged; Get into biochemical treatment tank; Utilize composite solution storage tank V-2 through valve F-1 composite solution storage tank V-3 to be replenished the fresh composite solution of equivalent simultaneously, make that the liquid level among the composite solution storage tank V-3 keeps constant, the volume of composite solution storage tank V-3 is 48m
3Still contain 78mg/m in the gas this moment
3Dimethylamine gas and 2.6mg/m
3Ammonia; Again gas is got into the rare organic acid liquid absorptive unit of absorption tower T-1 through 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 the gas and ammonia
3/ m
2.h), make that the content of dimethylamine gas and ammonia is reduced to 0.08mg/m respectively in the waste gas
3Below.At last, the gas after being cleaned is through valve F-5 and pipeline 9 emptyings, and gas total content harmful in the gas of emptying is reduced to 0.4mg/m
3Below.Organic acid soln after the absorbing 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 through valve F-2 organic acid absorption liquid storage tank V-5 to be carried out equivalent simultaneously and replenish, make that the liquid level among the organic acid absorption liquid storage tank V-5 keeps constant, the volume of organic acid absorption liquid storage tank V-5 is 30m
3
Claims (7)
1 A spandex manufacturing process gas absorber, characterized in that: the absorption body up and down two absorption unit, wherein the lower unit is a complex solution absorption unit, the upper unit is an organic acid solution absorption cell, the absorption cell and an organic acid complex solution between the liquid absorbing unit vapor - liquid isolating means (M-1) of the two elements separated from the lower part of the gas absorption cell complex solution into the organic liquid to the upper part of the absorption cell; complex solution at the bottom of a gas absorption cell Distribution device (A-1), gas sparger (A-1) and the exhaust gas outside the tower inlet phase, absorption cell complex solution in the middle of gas absorption zone, the area filled with a filler material or trays, absorption unit complex solution the top of the liquid distribution device (Q-1), a liquid distribution device (Q-1) and the tower of the complex solution storage tank (V-3) by the pump (P-2) and a liquid flow meter (FM-1) connected to the bottom of the absorption unit complex solution pipe (2) and compound solution tank (V-3) connected to form a composite solution circulation loop; organic liquid absorption cell bottom vapor - liquid isolating means (M-1), the gas through vapor - liquid isolating means (M-1) into the organic liquid absorption unit, an organic acid solution in the middle of the gas absorption cell absorption zone, the area or trays filled with a filler, an organic acid liquid absorbing units on top of one liquid distributor ( Q-2), a liquid distribution device (Q-2) and the tower of the organic solution storage tank (V-5) by the pump (P-3) and a liquid flow meter (FM-2) connected to the organic liquid absorbing the bottom of the pipe element (5) with an organic acid solution storage tank (V-5) is connected, forming organic liquid circulation circuit, the top organic liquid absorbing unit after purification of exhaust gas outlet.
2. spandex production process waste gas absorption tower according to claim 1; It is characterized in that: described gas-liquid spacer assembly (M-1) is made up of one or more riser and liquid-blocking cap; Gas phase rises through riser from the composite solution absorptive unit; And along the gap between riser and the liquid-blocking cap from around overflow; And the liquid phase of organic acid solution absorptive unit is stopped by liquid-blocking cap in dropping process; Flow into organic acid solution absorptive unit bottom, and flow out via pipeline (5).
3. spandex production process waste gas absorption tower according to claim 1 and 2; It is characterized in that: two absorber portions up and down of described absorption tower (T-1) are filled with filler or column plate; Wherein column plate comprises sieve plate column plate, valve plate, bubble cap plate, and filler comprises structured packing and dumped packing.
4. the technology of the concentrated purified treatment of spandex production process waste gas is characterized in that adopting the described spandex production process of claim 1 waste gas absorption tower, and concrete steps are following:
The gas that each vacuum pump outlet of outfits such as step 1. pair spandex production process polymerization workshop section, spray silk workshop section, refining workshop section, solvent recovery workshop section is discharged is collected; Get into gas reservoir V-1; Gas is concentrated the gas distributor (A-1) of the composite solution absorptive unit bottom that is delivered to absorption tower (T-1) through air blast (P-1) and pipeline (1) then; Get into absorption tower (T-1)
Step 2. is in the composite solution absorptive unit of absorption tower (T-1); Extract composite solution through centrifugal pump (P-2) out by composite solution storage tank (V-3); Through piping (3) and fluid flowmeter (FM-1); The liquid distribution trough (Q-1) at (T-1) composite solution absorptive unit top sprays downwards from the absorption tower; Absorption is to remove acids and the formaldehyde material in the gas; (T-1) composite solution absorptive unit bottom passes back into composite solution storage tank (V-3) from the absorption tower then; Composite solution is the solution that contains alkali and salt, and the alkali in the composite solution is NaOH or Na
2CO
3Or NaHCO3, perhaps adopt Ca (OH)
2,Or other inorganic and organic basic material; Wherein the concentration of alkali lye is between 0.1M ~ 5M; Salt in the composite solution is natrium nitrosum; Its concentration is about between 0.1M ~ 5M; This absorptive unit can be with filler or column plate filling, and its concrete height and specification are by concrete commercial scale decision, according to the content of each waste gas component in the gas reservoir (V-1); Spray flux by fluid flowmeter (FM-1) control composite solution
Composite solution in the composite solution absorptive unit of step 3. absorption tower (T-1) is in circulation; The composite solution that partially absorbs behind the waste gas is discharged from pipeline (7), valve (F-3) and pipeline (10); Remove biochemical treatment tank, the amount of discharge is then based on the basicity of online detection composite solution and confirm; Utilize composite solution storage tank (V-2) composite solution storage tank (V-3) to be replenished the fresh composite solution of equivalent through valve (F-1) again; Make the liquid level in the composite solution storage tank (V-3) keep constant, the volume of composite solution storage tank (V-3) is by the internal circulating load and the time of staying decision of composite solution;
Step 4. is through the absorption tower; (T-1) gas behind the composite solution absorptive unit passes through the absorption tower; (T-1) the vapour-liquid spacer assembly at composite solution absorptive unit top; (M-1) enter into the absorption tower; (T-1) top organic acid solution absorptive unit absorbs; The vapour-liquid spacer assembly; (M-1) gas vent is above the organic acid solution liquid level; Prevent that organic acid solution from entering into the composite solution absorptive unit; This absorptive unit can be with filler or column plate filling; Its concrete height and specification are by concrete commercial scale decision
Step 5. is extracted the liquid in the organic acid absorption liquid storage tank (V-5) out with centrifugal pump (P-3); Through fluid flowmeter (FM-2) and pipeline (6); Get into the packing layer or the column plate of the top organic acid solution absorptive unit on absorption tower (T-1) through organic acid solution absorptive unit top liquid distribution trough (Q-2) ejection; The waste gas that adverse current is made progress reacts absorption; The bottom of (T-1) top organic acid solution absorptive unit passes back into organic acid absorption liquid storage tank (V-5) from the absorption tower then, 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 the 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 that partially absorbs behind the waste gas is discharged from pipeline (8), valve (F-4) and pipeline (10); Remove biochemical treatment tank, the amount of discharge is then confirmed according to the basicity of online detection organic acid solution; Utilizing organic acid absorption liquid storage tank (V-4) through valve (F-2) organic acid absorption liquid storage tank (V-5) to be carried out equivalent simultaneously replenishes; Make the liquid level in the organic acid absorption liquid storage tank (V-5) keep constant; The volume of organic acid absorption liquid storage tank (V-5) is by the internal circulating load and the time of staying decision of absorption liquid
Step 7. is last, and gas is organic acid absorptive unit top, (T-1) top from the absorption tower, discharges through valve (F-5) and pipeline (9), and the quality percentage total content of pernicious gas is less than 0.5mg/m in the gas of discharge
3, the fluid discharge that pipeline (10) is discharged focuses on to biochemistry pool.
5. waste gas according to claim 4 is concentrated purification process technique, it is characterized in that: the organic acid that step 5 is used is a citric acid, and the concentration of organic acid absorption liquid is between 0.4M-1.5M.
6. waste gas according to claim 4 is concentrated purification process technique, it is characterized in that: the described composite solution of step 2, when the content of harmful components in the gas phase increased, the concentration of composite solution and internal circulating load were all heightened corresponding.
7. waste gas according to claim 4 is concentrated purification process technique, it is characterized in that: the described organic acid absorption liquid of step 5, when the content of harmful components in the gas phase increased, the concentration of organic acid soln and internal circulating load were all heightened corresponding.
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