CN1120023A - Disposal method of sulfur-contained organic effluent and gas purifying special equipment-gas balancing apparatus - Google Patents
Disposal method of sulfur-contained organic effluent and gas purifying special equipment-gas balancing apparatus Download PDFInfo
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- CN1120023A CN1120023A CN 95103356 CN95103356A CN1120023A CN 1120023 A CN1120023 A CN 1120023A CN 95103356 CN95103356 CN 95103356 CN 95103356 A CN95103356 A CN 95103356A CN 1120023 A CN1120023 A CN 1120023A
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Abstract
The process for treating organic waste water containing sulfur includes such steps as modifying pretreatment for improving bacterial reduction metabolism condition in sulfate, anaerobic desulfurizing reaction to treansform over 90% of SO4(2-) into H2S and most of organic matter into acetic acid and CO2/H2, sulfide seperation and clarification to recover over 95% of sulfide as sulfur by-product, and anaerobic and aerobic biological treating to obtain clarified water. A special apparatus for gas clarification, named gas equalizer, is disclosed.
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 chemical treatment method, problems such as the storing burden of sweetening agent and reagent cost expense 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 of a kind of this treatment process-gaseous equilibrium device.
The object of the present invention is achieved like this:
A, waste water at first pass through modified pre-treatment:
The soluble ferric iron salt that in waste water, adds 50-450ppm, but to improve anaerobic waste water desulfurization biochemical character;
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 ℃, simultaneously by S in reflux dilution way (promptly the water outlet after stripping process being returned in the anaerobism desulphurization reactor by the certain reflux ratio) controlling reactor
2-Concentration in span of control, the anaerobism desulfurization makes the above SO of 85-95% in the waste water
4 2-, SO
3 2-, S
2O
4 2-Transfer H to Deng material
2S, most of organism transfers acetate and CO to
2/ H
2
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 rear portion 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 water outlet after stripping process is returned the anaerobism desulphurization reactor by certain reflux ratio, 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:
Be admitted to anaerobic digestion reaction vessel through the waste water after stripping process and carry out the anaerobic biological processing, anaerobic effluent is sent into the aerobic bio-contact oxidation pond, carry out bio-oxidation and handle.
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 ℃, and containing soluble ferric iron salt is 50-450ppm.
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 cationic high-molecular organic floculant (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 for use:
(1) bodied ferric sulfate: add-on 25-250ppm,
(2) polymeric aluminum: add-on 20-250ppm.
In the modified pre-treatment of waste water, the soluble ferric iron salt of adding 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, temperature is controlled 20-65 ℃, adds the FeSO of 50-450ppm in waste water by test tank 2
4(or FeCl
3), waste water is sent into settling bath 4 continuously, under continuous stirring condition, slowly adds the macromolecule organic flocculating agent of 1.5-5ppm by test tank 3 in waste water.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-Transfer H to Deng material
2S, most of organism transfers acetate and CO to
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 tower 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.Anaerobism desulfidation tail gas, control gas stripping column after the tail gas that its source of the gas generates from anaerobism desulphurization reactor 7 is handled with the purification absorption 8 retention time of sewage 10-60 minutes, stripping intensity 10-35m
3/ m
2The 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.Deliver to anaerobic digestion reaction vessel 18 by overflow groove 5 and intercepting basin 16 and pump 17, carry out methanation and handle.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
2The time.In anaerobic digestion reaction vessel 18, by the effect of methanobacteria, make the organism of 75-80% in the waste water be transferred to biogas, 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 reaches 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
2The about 1mg/m of S content
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, 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.
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% H
2S specific absorption: 95%
COD clearance: 90% BOD
5Clearance: 95%
Wherein anaerobism desulfurization:
Water inlet COD:10000-20000mg/l
Water inlet SO
4 2-: 2000-5000mg/l
SO
4 2-Transformation efficiency: 85-95%
SO
4 2-Remove load: 3.5-10KgSO
4 2-/ m
3Day
COD clearance: 30-40%
Anaerobic digestion:
Water inlet COD:7000-12000mg/l
COD clearance: 70-80%
COD removes load: 8-20KgCOD/m
3Day
Aerobic biochemical is handled:
Water inlet COD:600-1200mg/l
COD clearance: 50-75%
Hydraulic detention time: 4 hours
The present invention is to the treatment effect of Streptomycin sulphate waste water:
SO
4 2-Clearance: 90% H
2S specific absorption: 95%
COD clearance: 92% BOD
5Clearance: 96.5%
Wherein anaerobism desulfurization:
Water inlet COD:6000-13000mg/l
Water inlet BOD
5: 2500-5000mg/l
Water inlet SO
4 2-: 700-1500mg/l
SO
4 2-Transformation efficiency: 90-95%
COD clearance: 30-40%
Anaerobic digestion:
Water inlet COD:4200-7800mg/l
COD clearance: 75-82%
COD removes load: 8-20Kg/m
3Day
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 has adopted desulfotomaculum bacteria technology, and has successfully solved anaerobism The desulfurization mesophytization suppresses to affect problem, and it is organic useless therefore to use this method to process sulfur-bearing Water has efficient, economic advantage than known similar method of wastewater treatment. We Method not only is suitable for the waste water treatment of all mycillin production plants, same being suitable for In vitamin C, Cobastab12, the worker such as starch, yeast, cotton pulp, wood pulp processing Processing, the especially waste water of high-concentration sulfur-containing organic wastewater of industry 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, but to improve anaerobic waste water desulfurization biochemical character;
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 ℃, simultaneously by S in reflux dilution way (promptly the water outlet after stripping process being returned in the anaerobism desulphurization reactor by the certain reflux ratio) controlling reactor
2-Concentration in span of control, the anaerobism desulfurization makes the above SO of 85-95% in the waste water
4 2-, SO
3 2-, S
2O
4 2-Transfer H to Deng material
2S, most of organism transfers acetate and CO to
2/ H
2
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 rear portion 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 water outlet after stripping process is returned the anaerobism desulphurization reactor by certain reflux ratio, 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 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 ℃, containing soluble ferric iron salt is 50-450ppm.
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 polyacrylamide cationic high-molecular organic floculant (PAMC) more than 4,000,000, add-on 1.5-20ppm,
(2) molecular weight is the polyacrylamide cationic high-molecular organic floculant (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 for use:
(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 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.
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 | Disposal method of sulfur-contained organic effluent and gas purifying special equipment-gas balancing apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 95103356 CN1058251C (en) | 1995-04-25 | 1995-04-25 | Disposal method of sulfur-contained organic effluent and gas purifying special equipment-gas balancing apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1120023A true CN1120023A (en) | 1996-04-10 |
| CN1058251C CN1058251C (en) | 2000-11-08 |
Family
ID=5074674
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 95103356 Expired - Fee Related CN1058251C (en) | 1995-04-25 | 1995-04-25 | Disposal method of sulfur-contained organic effluent and gas purifying special equipment-gas balancing apparatus |
Country Status (1)
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|---|---|
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100355821C (en) * | 2003-04-01 | 2007-12-19 | 克瑞斯特罗控股有限公司 | Process for surface activation and/or devulcanisation of sulphur-vulcanised 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 extraction liquid |
| CN104540953A (en) * | 2012-06-15 | 2015-04-22 | 科斯卡塔公司 | Integrated processes for bioconverting syngas to oxygenated organic compound with sulfur supply |
| CN108975619A (en) * | 2018-08-09 | 2018-12-11 | 广东鼎丰纸业有限公司 | A kind of slurrying weight foul condensate Integrated Processing Unit and method |
-
1995
- 1995-04-25 CN CN 95103356 patent/CN1058251C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100355821C (en) * | 2003-04-01 | 2007-12-19 | 克瑞斯特罗控股有限公司 | Process for surface activation and/or devulcanisation of sulphur-vulcanised 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 extraction liquid |
| CN104540953A (en) * | 2012-06-15 | 2015-04-22 | 科斯卡塔公司 | Integrated processes for bioconverting syngas to oxygenated organic compound with sulfur supply |
| CN108795995A (en) * | 2012-06-15 | 2018-11-13 | 赛纳塔生物有限公司 | With sulphur supply by synthesis gas bioconversion at the integrated processes of oxygen-containing organic compound |
| CN108975619A (en) * | 2018-08-09 | 2018-12-11 | 广东鼎丰纸业有限公司 | A kind of slurrying weight foul condensate Integrated Processing Unit and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1058251C (en) | 2000-11-08 |
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