CN1058251C - Sulfur-containing organic waste water treatment method and special gas purifying equipment-gas balancer - Google Patents
Sulfur-containing organic waste water treatment method and special gas purifying equipment-gas balancer Download PDFInfo
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- CN1058251C CN1058251C CN 95103356 CN95103356A CN1058251C CN 1058251 C CN1058251 C CN 1058251C CN 95103356 CN95103356 CN 95103356 CN 95103356 A CN95103356 A CN 95103356A CN 1058251 C CN1058251 C CN 1058251C
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 12
- 239000011593 sulfur Substances 0.000 title abstract description 5
- 229910052717 sulfur Inorganic materials 0.000 title abstract description 5
- 238000004065 wastewater treatment Methods 0.000 title description 5
- 239000010815 organic waste Substances 0.000 title description 2
- 239000002351 wastewater Substances 0.000 claims abstract description 60
- 238000000034 method Methods 0.000 claims abstract description 38
- 238000000926 separation method Methods 0.000 claims abstract description 24
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 14
- 230000023556 desulfurization Effects 0.000 claims abstract description 14
- 238000006243 chemical reaction Methods 0.000 claims abstract description 9
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 111
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- 238000010521 absorption reaction Methods 0.000 claims description 24
- 230000008569 process Effects 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 14
- 238000007254 oxidation reaction Methods 0.000 claims description 14
- 239000008394 flocculating agent Substances 0.000 claims description 13
- 238000012545 processing Methods 0.000 claims description 12
- 230000003647 oxidation Effects 0.000 claims description 11
- 238000010926 purge Methods 0.000 claims description 10
- 230000008929 regeneration Effects 0.000 claims description 10
- 238000011069 regeneration method Methods 0.000 claims description 10
- 238000005189 flocculation Methods 0.000 claims description 8
- 230000016615 flocculation Effects 0.000 claims description 8
- 230000029087 digestion Effects 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 7
- 229920002521 macromolecule Polymers 0.000 claims description 7
- 239000002912 waste gas Substances 0.000 claims description 7
- 229930182555 Penicillin Natural products 0.000 claims description 6
- JGSARLDLIJGVTE-MBNYWOFBSA-N Penicillin G Chemical compound N([C@H]1[C@H]2SC([C@@H](N2C1=O)C(O)=O)(C)C)C(=O)CC1=CC=CC=C1 JGSARLDLIJGVTE-MBNYWOFBSA-N 0.000 claims description 6
- 229940049954 penicillin Drugs 0.000 claims description 6
- 238000002203 pretreatment Methods 0.000 claims description 6
- 241000186541 Desulfotomaculum Species 0.000 claims description 5
- 239000005864 Sulphur Substances 0.000 claims description 5
- 229920006395 saturated elastomer Polymers 0.000 claims description 5
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical class [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 claims description 4
- 241000282326 Felis catus Species 0.000 claims description 4
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 4
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 4
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 4
- 229920002401 polyacrylamide Polymers 0.000 claims description 4
- 238000013461 design Methods 0.000 claims description 3
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 3
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 239000004094 surface-active agent Substances 0.000 claims description 3
- 239000002699 waste material Substances 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 2
- 229910052782 aluminium Inorganic materials 0.000 claims description 2
- 125000000129 anionic group Chemical group 0.000 claims description 2
- 125000002091 cationic group Chemical group 0.000 claims description 2
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 2
- 239000011790 ferrous sulphate Substances 0.000 claims description 2
- 238000002955 isolation Methods 0.000 claims description 2
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 229920001495 poly(sodium acrylate) polymer Polymers 0.000 claims description 2
- NNMHYFLPFNGQFZ-UHFFFAOYSA-M sodium polyacrylate Chemical compound [Na+].[O-]C(=O)C=C NNMHYFLPFNGQFZ-UHFFFAOYSA-M 0.000 claims description 2
- QTENRWWVYAAPBI-YCRXJPFRSA-N streptomycin sulfate Chemical compound OS(O)(=O)=O.OS(O)(=O)=O.OS(O)(=O)=O.CN[C@H]1[C@H](O)[C@@H](O)[C@H](CO)O[C@H]1O[C@@H]1[C@](C=O)(O)[C@H](C)O[C@H]1O[C@@H]1[C@@H](N=C(N)N)[C@H](O)[C@@H](N=C(N)N)[C@H](O)[C@H]1O.CN[C@H]1[C@H](O)[C@@H](O)[C@H](CO)O[C@H]1O[C@@H]1[C@](C=O)(O)[C@H](C)O[C@H]1O[C@@H]1[C@@H](N=C(N)N)[C@H](O)[C@@H](N=C(N)N)[C@H](O)[C@H]1O QTENRWWVYAAPBI-YCRXJPFRSA-N 0.000 claims description 2
- 210000000056 organ Anatomy 0.000 claims 2
- 230000003068 static effect Effects 0.000 claims 2
- 238000003113 dilution method Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 abstract description 5
- 241000894006 Bacteria Species 0.000 abstract description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 abstract 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 abstract 1
- 239000006227 byproduct Substances 0.000 abstract 1
- 230000003750 conditioning effect Effects 0.000 abstract 1
- 230000004060 metabolic process Effects 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 9
- 238000012856 packing Methods 0.000 description 3
- 239000002244 precipitate Substances 0.000 description 3
- 241001074903 Methanobacteria Species 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000010790 dilution Methods 0.000 description 2
- 239000012895 dilution Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 229920001131 Pulp (paper) Polymers 0.000 description 1
- 240000004808 Saccharomyces cerevisiae Species 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 159000000009 barium salts Chemical class 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 235000003599 food sweetener Nutrition 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000003765 sweetening agent Substances 0.000 description 1
- 231100000167 toxic agent Toxicity 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 235000019156 vitamin B Nutrition 0.000 description 1
- 239000011720 vitamin B Substances 0.000 description 1
- 235000019154 vitamin C Nutrition 0.000 description 1
- 239000011718 vitamin C Substances 0.000 description 1
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Abstract
The invention relates to a method for treating sulfur-containing organic wastewater and a gas balancer of special gas purification equipment. Firstly, the wastewater is pretreated by conditioning to improve the bacteria reduction metabolism condition of sulfate in the wastewater, and then the wastewater passes through an anaerobic desulfurization reactor to ensure that more than 90 percent of SO in the wastewater2-Is converted into H2S, conversion of most of the organics to acetic acid and CO2/H2. The effluent of anaerobic desulfurization contains a large amount of S2-、HS-And H2S, more than 95% of sulfide in the wastewater is recycled into a sulfur byproduct through a sulfide separation and purification system, and the desulfurized effluent is subjected to anaerobic and aerobic biochemical treatment to purify the wastewater. The invention also provides a special gas purifying device and a gas balancer. Compared with the prior art, the invention has the advantages of high efficiency and economy.
Description
The present invention relates to a kind of disposal method of sulfur-contained organic and gas sweetening specific equipment-gaseous equilibrium device.
Chinese patent CN1012358B discloses a kind of " method for the treatment of penicillin waste water ", it mainly is before biochemical treatment waste water to be carried out flocculation separation and precipitate the desulfurization processing, at first in waste water, add inorganic flocculating agent and macromolecule organic flocculating agent and carry out flocculation separation, add the soluble barium salt then in the supernatant liquor after flocculation separation and precipitate desulfurization.This method has been controlled demulsifying agent in the waste water, SO effectively by add the chemical agent approach in waste water
4 2-Deng the inhibition influence of a class toxicant to methanobacteria, waste water is handled by anaerobism and aerobic biochemical and is reached good effects of purification quality.But because this method is to SO in the waste water
4 2-Adopt problems such as chemical treatment method, the storing burden of sweetening agent and reagent cost take, bring difficulty for the operation of large-scale penicillin wastewater processing plant.
The objective of the invention is at above-mentioned weak point of the prior art, and a kind of efficient, economic disposal method of sulfur-contained organic is provided.Another object of the present invention provides the employed gas sweetening specific equipment one gaseous equilibrium device of a kind of this treatment process.
The object of the present invention is achieved like this:
A. waste water at first passes through modified pre-treatment:
The soluble ferric iron salt that in waste water, adds 50-450ppm;
B, anaerobism desulfurization
Carry out desulfotomaculum bacteria through pretreated waste water by an anaerobism desulphurization reactor, the pH7.0-7.5 of control waste water, temperature is 35-39 ℃, by the reflux dilution way, and the water outlet after the part stripping process returned the anaerobism desulphurization reactor, with S in the controlling reactor
2-Inhibition influence to desulfotomaculum bacteria.
C. the isolation of purified system of sulfide:
Biochemical liquid after the anaerobism desulfurization enters gas stripping column and carries out the stripping processing, the stripping gas that blasts from the gas stripping column bottom is from the anaerobism desulfidation tail gas and purify the anaerobism desulfidation tail gas that absorbs after handling, the residence time of waste water in gas stripping column is 10-60 minute, water-gas ratio is 1: 5-30, stripping intensity is 10-35m
3/ m
2The time, after stripping process, make 95% above H in the waste water
2S changes gas phase over to, and the anaerobism desulphurization reactor is returned in the water part after stripping process, and unnecessary waste water goes anaerobic biological to handle, and the waste gas of discharging from the gas stripping column top enters gas treating system;
D. anaerobism and aerobic biochemical are handled:
Waste water after stripping process is admitted to anaerobic digestion reaction vessel and carries out the anaerobic biological processing, and anaerobic effluent is sent into the aerobic bio-contact oxidation pond, carries out bio-oxidation and handles.
At the modified pretreatment stage of waste water, for containing polymeric surface active agent and a large amount of mycelium penicillin wastewater and Streptomycin sulphate mycelia waste liquid, also need to add macromolecule organic flocculating agent and inorganic flocculating agent, carry out flocculation separation, the pH6.8-9.5 of control waste water, temperature is 25-65 ℃.
Macromolecule organic flocculating agent is selected any in the following kind in flocculation separation:
(1) molecular weight is the polyacrylamide cationic high-molecular organic floculant (PAMC) more than 4,000,000, add-on 1.5-20ppm;
(2) molecular weight is the polyacrylamide anionic macromolecule organic flocculating agent (PHP) more than 5,000,000, add-on 1.5-10ppm;
(3) sodium polyacrylate: add-on 2-10ppm;
Inorganic flocculating agent is selected any in the following kind:
(1) bodied ferric sulfate: add-on 25-250ppm;
(2) polymeric aluminum: add-on 20-250ppm.
In the modified pre-treatment of waste water, the molysite of adding solubility is selected any in the following kind for use:
(1) ferrous sulfate
(2) iron trichloride
(3) bodied ferric sulfate
Gas treating system is made up of absorption tower, gaseous equilibrium device, oxidation regeneration device and settling bath, and the waste gas of discharging from the gas stripping column top is at first sent into the absorption tower, the H that 95% in the waste gas is above
2S is cleaned absorption, the Purge gas that cat head is discharged is sent back to gas stripping column behind the gaseous equilibrium device, and remaining Purge gas enters atmosphere by the gaseous equilibrium device, the saturated absorption liquid of discharging from the bottom, absorption tower enters the oxidation regeneration device, make saturated absorption liquid obtain oxidation regeneration, gas H in absorption, oxidative regeneration process
2S is converted into elemental sulfur, sends to after by settling bath sulphur mud being collected and is processed into sulphur, and the absorption liquid behind oxidation regeneration is sent back to the absorption tower.
Gas sweetening specific equipment-gaseous equilibrium device is by tank 22, bell jar 26, gas stop means 13, inlet pipe 24 and escape pipe 23 are formed, bell jar 26 floats on the water surface in the tank 22, inlet pipe 24 and escape pipe 23 pass tank 22 and stretch in the bell jar 26, gas stop means 13 is by gas baffling pipe 28, gas-water separation pipe 30, residual air ingress pipe 27 and residual air delivery line 25 are formed, residual air delivery line 25 penetrates from tank 22 bottom centre, its height is contour with tank 22, gas baffling pipe 28 is positioned at bell jar longitudinal axis position, its height is contour with bell jar, its top and bell jar are fixedly connected, its lower end is enclosed within on the residual air delivery line 25, gas-water separation pipe 30 is enclosed within the bottom of gas baffling pipe 28, end closure and be fixedly connected on it with gas baffling pipe 28 outer walls, the top that is positioned at the gas baffling pipe 28 of gas-water separation pipe 30 has gas flow guiding window 29, be provided with residual air ingress pipe 27 in the bottom of gas-water separation pipe 30, the distance h between the lower surface of the lower surface of the vertical component of residual air ingress pipe 27 and gas baffling pipe 28
1Be 20-200mm, the height h of residual air ingress pipe 27
2=(0.3-0.95) h
0, h
0Design pressure for bell jar.Be provided with purging valve 31 in the upper end of gas baffling pipe 28.The quantity of residual air ingress pipe 27 is 1-6.
Below in conjunction with drawings and Examples the present invention is further described:
Fig. 1 is a process flow sheet of the present invention.
Fig. 2 is a gaseous equilibrium device structural representation.
Fig. 3 is the gas stop means of gaseous equilibrium device.
Process explanation is as follows: (referring to Fig. 1)
1, the modified pre-treatment of waste water:
Refinement waste acid water distillate by penicillin factory discharges at first enters regulating tank 1, with saturated milk of lime, H
2SO
4Or H
3PO
4Control waste water PH6.5-9.5,20-65 ℃ of temperature control, in waste water, add the FeSO4 (or FeCl3) of 50-450ppm by test tank 2, waste water is sent into settling bath 4 continuously, under continuous stirring condition, slowly in waste water, add macromolecule organic flocculating agent and inorganic flocculating agent by test tank 3.Concrete add-on sees attached list 1.By the charged poly-effect and the bridging action of flocculation agent, make suspended solid, colloid thing and the molecules surfactant of most of bio-refractory in the waste water, separate from waste water with the form of flocculent precipitate, supernatant liquor enters anaerobism desulphurization reactor 7.When not containing objectionable impuritiess such as a large amount of suspended solidss and tensio-active agent in the waste water, this pre-treatment mainly is to add a certain amount of soluble ferric iron salt in waste water.
2, anaerobism desulfurization:
Through pretreated waste water, deliver to the bottom of anaerobism desulphurization reactor 7 continuously by circulation groove 5 and pump 6, control reaction temperature 25-39 ℃, PH7-7.5, the S of the method controlling reactor by reflux dilution
2-Concentration suppressing below the range of influence.By the effect of sulfatereducting bacteria in the reactor and acid-producing bacteria, make the above SO of 85-95% in the waste water
4 2-, SO
3 2-, S
2O
4 2-Be converted into H Deng material
2S, most of organism is converted into acetate and CO
2/ H
2, through containing a large amount of sulfide in the water outlet after the anaerobism desulfurization processing.This will be to methane fermentation process toxigenicity, and waste water is sent to gas stripping column 8 and carries out the stripping processing.
3, waste water stripping process:
The S that contains by 7 discharges of anaerobism desulphurization reactor
2-Waste water injects gas stripping column 8 continuously, and the top of its gas stripping column 8 is provided with water distribution and Despumation device.Packing medium is housed in the tower, is rich in CO
2Purification stripping gas feed by gas stripping column 8 bottoms continuously by blower fan 9.Its source of the gas is from anaerobism desulphurization reactor 7 tail gas that generates and the anaerobism desulfidation tail gas that purifies after absorption is handled.Control gas stripping column 8 retention time of sewage 10-60 minutes, stripping intensity 10-35m
3/ m
2. the time.Neutralization and gas by stripping gas in the tower are proposed effect, make in the waste water most of sulfide with H
2The S form is brought in the stripping tail gas.S in the water outlet after stripping process
2-Content be about 10mg/l.Delivering to anaerobic digestion reaction vessel 18 by overflow groove 5 and intercepting basin 16 and pump 17 carries out methanation and handles.The stripping tail gas that discharge at gas stripping column 8 tops is delivered to H
2The S absorption system.
4, anaerobic digestion and aerobic biochemical are handled:
The stripping of being discharged by gas stripping column 8 bottoms purifies water outlet, delivers to anaerobic digestion reaction vessel 18, control reaction temperature 35-37 ℃, hydraulic load 1-6m by overflow groove 5 and intercepting basin 16 and pump 17
3/ m
2. the time.In anaerobic reactor 18, by the effect of methanobacteria, make that the organism of 75-80% is converted into biogas in the waste water, its biogas is made for fuel after by ferric oxide dry desulfurization device 19 purifying treatment.Remaining a small amount of organic pollutant in the anaerobic effluent is handled and follow-up materialization processing through the bio-oxidation in aerobic bio-contact oxidation pond 20, and waste water can reach the purification requirement, makes the total clearance of COD in the waste water reach 85-90%, BOD
5Total clearance is more than 95%.
5, H
2The S gas cleaning is handled
The stripping tail gas of discharging from gas stripping column 8 tops, H
2S content reaches 5-12g/m approximately
3, CO
2Content is about 40-50%.Sulphur-containing exhaust gas is at first sent into an absorption tower 10, is filled with packing medium in the tower.Absorption liquid sprays into from cat head continuously by pump 15, contains H
2S waste gas feeds at the bottom of by tower, in packing layer, the abundant contact reacts of gas-liquid two-phase, through absorb, H after the purifying treatment
2H in the S gas more than 95%
2S is cleaned absorption.Purge gas, H that cat head is discharged
2S content reaches 1mg/m approximately
3About.Return the stripping process system through gaseous equilibrium device 11 and blower fan 9.Gas is put forward, is absorbed residue Purge gas that circulating treatment procedure produces and enters atmosphere by gaseous equilibrium device and a specific gas stop means 13 being located at its inside, or mixes with biogas after the purifying treatment and to be used as fuel.
6, about gas sweetening specific equipment-gaseous equilibrium device: (referring to Fig. 2,3)
Gas sweetening specific equipment-gaseous equilibrium device is by tank 22, bell jar 26, inlet pipe 24 and escape pipe 23 are formed, bell jar 26 floats on the water surface in the tank 22, inlet pipe 24 and escape pipe 23 pass tank 22 and stretch in the bell jar 26, gas stop means 13 is by gas baffling pipe 28, gas-water separation pipe 30, residual air ingress pipe 27 and residual air delivery line 25 are formed, residual air delivery line 25 penetrates from tank 22 bottom centre, its height is contour with tank 22, gas baffling pipe 28 is positioned at bell jar longitudinal axis position, its height is contour with bell jar, its top and bell jar are fixedly connected, its lower end is enclosed within on the residual air delivery line 25, gas-water separation pipe 30 is enclosed within the bottom of gas baffling pipe 28, end closure and fixedly connected on it with gas baffling pipe 28 outer walls, the top that is positioned at the gas baffling pipe 28 of gas-water separation pipe 30 has gas flow guiding window 29, be provided with residual air ingress pipe 27 in the bottom of gas-water separation pipe 30, the distance h between the lower surface of the lower surface of the vertical component of residual air ingress pipe 27 and gas baffling pipe 28
1Be 20-200mm, the height h of residual air ingress pipe 27
2=(0.3-0.95) h
0, h
0Design pressure for bell jar.Be provided with purging valve 31 in the upper end of gas baffling pipe 28.The quantity of residual air ingress pipe 27 is 1-6.
7, put forward, absorb the balance of circulating treating system gas about gas:
The equilibrium process of circulating treating system gas is carried, absorbed to gas in the waste water treatment process of the present invention in conjunction with Fig. 2, Fig. 3 is described in detail:
Gas after the purifying treatment enters gaseous equilibrium device 11 continuously by inlet pipe 24, by the effect of blower fan among Fig. 19, returns constantly by escape pipe 23 that gas is carried, the absorption cleaning treatment system.In the technological process, along with gas in the anaerobism desulphurization reactor is constantly imported to gaseous equilibrium device 11.Gas increases gradually in the gaseous equilibrium device 11, causes bell jar 26 constantly to rise, and liquid level descends in the bell jar 26.When the residual air ingress pipe 27 of gas stop means 13 surfaced, gas superfluous in the bell jar entered gas-water separation pipe 30 by residual air ingress pipe 27.Branch water effect by gas-water separation pipe 30, the fluid-tight water that residual air ingress pipe 27 is brought into enters in the tank 22 of gas-water separation pipe 30 bottoms, gas by the gas flow guiding window 29 on the gas-water separation pipe 30, gas baffling pipe 28 and residual air delivery line 25 deliver to other with the gas system or directly the purging valve 31 by gas baffling pipe 28 tops drain into atmosphere.After residual gas was discharged, gas-circulating system restored balance.Along with liquid level in the bell jar 26 descends, residual air ingress pipe 27 immerses in the water, by the water seal effect residual air ingress pipe 27 and bell jar is separated, and outwards exhaust stops; When gas in the bell jar is superfluous once more, repeats above-mentioned exhaust process, thereby make the recycle gas treatment system remain equilibrium state.
The present invention to the penicillin wastewater treatment effect is:
SO
4 2-Clearance: 90% H2S absorptivity: 95%
COD clearance: 90% BOD5Clearance: 95%
Wherein anaerobism desulfurization:
Influent COD: 10000-20000mg/l
Water inlet SO4 2-：2000-5000mg/l
SO
4 2-Conversion ratio: 85-95%
SO
4 2-Remove load: 3.5-10kg SO4 2-/m
3. day
COD clearance: 30-40%
Anaerobic digestion:
Influent COD: 7000-12000mg/l
COD clearance: 70-80%
COD removes load: 8-20KgCOD/m3. day
Aerobic treatment:
Influent COD: 600-1200mg/l
COD clearance: 50-75%
Hydraulic detention time: 4 hours
The present invention is to the treatment effect of streptomysin waste water:
S0
4 2-Clearance: 90%H2S absorptivity: 95%
COD clearance: 92%BOD5Clearance: 96.5%
Wherein anaerobism desulfurization:
Influent COD: 6000-13000mg/l
Water inlet BOD5：2500-5000mg/l
Water inlet SO4 2-：700-1500mg/l
SO
4 2-Conversion ratio-: 90-95%
COD clearance: 30-40%
Anaerobic digestion:
Water inlet COD:4200-7800mg/l
COD clearance: 75-82%
COD removes load: 8-20KgCOD/m
3. day
Aerobic biochemical is handled:
Water inlet COD:525-663mg/l
Water inlet BOD
5: 200-300mg/l
Hydraulic detention time: 4 hours
COD clearance: 45-55%
BOD
5Clearance: 80-85%
Because the present invention adopted desulfotomaculum bacteria technology, and successfully solved anaerobism desulfurization mesophytization and suppressed to influence problem, therefore used present method to handle sulfur-containing waste water and have efficient, economic advantage than known similar method of wastewater treatment.Present method not only is suitable for the waste water treatment of all mycillin production plants, is equally applicable to vitamins C, vitamins B
12, industrial organic waste water such as starch, yeast, cotton pulp, wood pulp processing processing, the especially processing of high density sulfur-bearing organic wastewater.
Claims (8)
1, a kind of disposal method of sulfur-contained organic is characterized in that:
A, waste water at first pass through modified pre-treatment:
The soluble ferric iron salt that in waste water, adds 50-450ppm;
B, anaerobism desulfurization:
Carry out desulfotomaculum bacteria through pretreated waste water by an anaerobism desulphurization reactor, the pH7.0-7.5 of control waste water, temperature is 35-39 ℃, by the reflux dilution method, and the water outlet after the part stripping process returned the anaerobism desulphurization reactor, with S in the controlling reactor
2-Inhibition influence to desulfotomaculum bacteria.
The isolation of purified system of c, sulfide:
Biochemical liquid after the anaerobism desulfurization enters gas stripping column and carries out the stripping processing, the stripping gas that blasts from the gas stripping column bottom is from the anaerobism desulfidation tail gas and purify the anaerobism desulfidation tail gas that absorbs after handling, the residence time of waste water in gas stripping column is 10-60 minute, water-gas ratio is 1: 5-30, stripping intensity is 10-35m
3/ m
2The time, after stripping process, make the H more than 95% in the waste water
2S changes gas phase over to, and the anaerobism desulphurization reactor is returned in the water part after stripping process, and unnecessary waste water goes anaerobic biological to handle, and the waste gas of discharging from the gas stripping column top enters gas treating system;
D, anaerobism and aerobic biochemical are handled:
Waste water after stripping process is admitted to anaerobic digestion reaction vessel and carries out the anaerobic biological processing, and anaerobic effluent is sent into the aerobic bio-contact oxidation pond, carries out bio-oxidation and handles.
2, treatment process according to claim 1, it is characterized in that the modified pretreatment stage of waste water, for containing polymeric surface active agent and a large amount of mycelium penicillin wastewater and Streptomycin sulphate mycelia waste liquid, also need to add macromolecule organic flocculating agent and inorganic flocculating agent, carry out flocculation separation, the pH6.8-9.5 of control waste water, temperature is 25-65 ℃.
3, treatment process according to claim 2 is characterized in that in flocculation separation macromolecule organic flocculating agent selects any in the following kind:
(1) molecular weight is the cationic high score of polyacrylamide more than 4,000,000
Sub-organic floculant (PAMC), add-on 1.5-20ppm;
(2) molecular weight is the polyacrylamide anionic high score more than 5,000,000
Sub-organic floculant (PHP), add-on 1.5-10ppm;
(3) sodium polyacrylate: add-on 2-10ppm;
Inorganic flocculating agent is selected any in the following kind:
(1) bodied ferric sulfate: add-on 25-250ppm;
(2) polymeric aluminum: add-on 20-250ppm.
4,, it is characterized in that the soluble ferric iron salt of adding is selected any in the following kind for use in the modified pre-treatment of waste water according to claim 1 or 3 described treatment processs:
(1) ferrous sulfate,
(2) iron trichloride,
(3) bodied ferric sulfate
5, treatment process according to claim 4 is characterized in that gas treating system is made up of absorption tower, gaseous equilibrium device, oxidation regeneration device and settling bath, and the waste gas of discharging from the gas stripping column top is at first sent into the absorption tower, the H that 95% in the waste gas is above
2S is cleaned absorption, the Purge gas that cat head is discharged is sent back to gas stripping column behind the gaseous equilibrium device, and remaining Purge gas enters atmosphere by the gaseous equilibrium device, the saturated absorption liquid of discharging from the bottom, absorption tower enters the oxidation regeneration device, make saturated absorption liquid obtain oxidation regeneration, gas H in absorption, oxidative regeneration process
2S is converted into elemental sulfur, sends to after by settling bath sulphur mud being collected and is processed into sulphur, and the absorption liquid behind oxidation regeneration is sent back to the absorption tower.
6, a kind of gas sweetening specific equipment-gaseous equilibrium device, it is characterized in that it is by tank (22), bell jar (26), gas stop means (13), inlet pipe (24) and escape pipe (23) are formed, bell jar (26) floats on the water surface of tank (22), inlet pipe (24) and escape pipe (23) pass tank (22) and stretch in the bell jar (26), gas stop means (13) is by gas baffling pipe (28), gas-water separation pipe (30), residual air ingress pipe (27) and residual air delivery line (25) are formed, residual air delivery line (25) penetrates from tank (22) bottom centre, its height is contour with tank (22), gas baffling pipe (28) is positioned at bell jar longitudinal axis position, its height is contour with bell jar, its top and bell jar are fixedly connected, its lower end is enclosed within on the residual air delivery line (25), gas-water separation pipe (30) is enclosed within the bottom of gas baffling pipe (28), end closure and be fixedly connected on it with gas baffling pipe (28) outer wall, the top that is positioned at the gas baffling pipe (28) of gas-water separation pipe (30) has gas flow guiding window (29), be provided with residual air ingress pipe (27) in the bottom of gas-water separation pipe (30), the distance h between the lower surface of the lower surface of the vertical component of residual air ingress pipe (27) and gas baffling pipe (28)
1Be 20-200mm, the height h of residual air ingress pipe (27)
2=(0.3-0.95) h
0, h
0Design pressure for bell jar.
7, static organ according to claim 6 is characterized in that being provided with purging valve (31) in the upper end of gas baffling pipe (28).
8, static organ according to claim 6, the quantity that it is characterized in that residual air ingress pipe (27) are 1-6.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 95103356 CN1058251C (en) | 1995-04-25 | 1995-04-25 | Sulfur-containing organic waste water treatment method and special gas purifying equipment-gas balancer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 95103356 CN1058251C (en) | 1995-04-25 | 1995-04-25 | Sulfur-containing organic waste water treatment method and special gas purifying equipment-gas balancer |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1120023A CN1120023A (en) | 1996-04-10 |
| CN1058251C true CN1058251C (en) | 2000-11-08 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 95103356 Expired - Fee Related CN1058251C (en) | 1995-04-25 | 1995-04-25 | Sulfur-containing organic waste water treatment method and special gas purifying equipment-gas balancer |
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| CN (1) | CN1058251C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE10314893A1 (en) * | 2003-04-01 | 2004-11-04 | Cristallo Holdings Inc., Edmonton | Process for surface activation and / or surface decarburization of sulfur-crosslinked rubber particles |
| CN101250393B (en) * | 2008-04-01 | 2010-06-02 | 中国石油天然气股份有限公司 | Treating agent containing polymer produced liquid |
| US9157100B2 (en) * | 2012-06-15 | 2015-10-13 | Coskata, Inc. | Integrated processes for bioconverting syngas to oxygenated organic compound with sulfur supply |
| CN108975619B (en) * | 2018-08-09 | 2019-12-20 | 广东鼎丰纸业有限公司 | Comprehensive treatment device and method for heavy-pollution condensate water in pulping process |
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1995
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| Publication number | Publication date |
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