CN103880202B - Sulfuric acid gas field gas production waste water reinjection treatment process - Google Patents
Sulfuric acid gas field gas production waste water reinjection treatment process Download PDFInfo
- Publication number
- CN103880202B CN103880202B CN201210537451.XA CN201210537451A CN103880202B CN 103880202 B CN103880202 B CN 103880202B CN 201210537451 A CN201210537451 A CN 201210537451A CN 103880202 B CN103880202 B CN 103880202B
- Authority
- CN
- China
- Prior art keywords
- waste water
- sulfuric acid
- production waste
- gas production
- acid gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention discloses sulfuric acid gas field gas production waste water reinjection treatment process.This sulfuric acid gas field gas production waste water reinjection treatment process, comprise the steps: that coagulation and flocculation treatment, precipitation, sterilization, two medium filter filter, fiber bundle filter filters by sulfuric acid gas field gas production waste water successively through oil removal and oil removal treatment, aeration sulphur removal, chemical oxidation sulphur removal, ultrafiltration and corrosion-mitigation scale-inhibition.Present invention also offers a kind of corrosion inhibiting and descaling agent, it comprises: 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid, sodium sulfonate and benzotriazole.Gas production waste water reinjection processing technological flow of the present invention is easy, running cost is lower, management is simple, effectively can process sulfuric acid gas field gas production waste water, and water outlet reaches the A3 standard in People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index.
Description
Technical field
The present invention relates to sulfuric acid gas field gas production waste water reinjection treatment process.
Background technology
The shortage of water resources causes the concern of international community already, and there is more than 100 national lack of water in the whole world, comprising China.The gross amount of water resources of China is considerable, occupies the 4th, the world, but water resources comes the 109th, the world per capita.The annual blowdown flow rate about 30,000,000,000 tons in the whole nation.Each big city, whole nation underground water is polluted in various degree.78 trunk rivers in the whole nation have 54 to be polluted. the large water system of China seven: the Changjiang river, the Zhujiang River, Song Hua River, the Yellow River, Huaihe River, Haihe River, the Liaohe River.Have half section to be polluted in seven large water systems, 86% section, city is polluted and is exceeded standard, and more serious has: the Yellow River, Huaihe River, the Liaohe River, Taihu Lake, Chaohu, the rivers and lakes such as Dian Chi.
In China, natural gas source is the important lifeblood of national economy, Oil And Gas Exploration And Development project is while giving the Social benefit and economic benefit that social creativity is huge, cause certain pollution and destruction also to the ecotope of surrounding, the construction of natural gas fields can cause complicated and diversified impact to the air in exploratory development region, water body, soil, biology.The pollution of construction of natural gas fields activity to water resources is the most serious.Water is lifespring, the pollution of water can directly cause soil and crop pollution, the pollution of crop promotes again the enrichment of toxic substance in domestic animal, poultry and human body, finally jeopardizes the health of people in whole food chain, and therefore the process of Sweet natural gas gas production waste water reinjection strictly should process and prevent outer row.
In gas recovery, generally carry out gas production waste water reinjection.According to the characteristic of gas field gas production water re-injection layer position, should be noted that following problem:
1) inject water should not carry a large amount of suspended substance, organic sludge, oil and emulsion, with prevent block water injection well, stratum venturi, layer gap.
2) inject water stratum stop slime bacteria and saprophytic microorganism growth, prevent from therefore blocking water filling path.
3) adopt full-closed system water filling, injecting water should anoxybiotic as far as possible, to prevent many oxide from generating, and particularly Fe
3+precipitation.
4) inject water and should not be with corrosive medium as far as possible, to prevent the corrosion to water treating equipment, water pipe and well casing.
5) inject water and do not answer fouling, to prevent damage equipment and to reduce water-injection capability.
Therefore strict effectively process must be carried out to reinjected water, in prior art, now a lot of for sulfuric acid gas field gas production waste water reinjection treatment process method, mainly comprising Physical, chemical method, biological process and physico-chemical processes, generally taking array mode for reaching target processing effect.Wherein, Physical, chemical method, physical chemistry for this kind of strong toxicity and the large waste water that fluctuates have treatment effect stablize be easy to regulate function.Although biological process processing cost is low, for this type of feature waste water its be easily hit and even collapse, need cycle of recovering long, affect the safety and stability process of waste water.For the existing general treatment process using oxidation sulphur removal+coagulating sedimentation+single filter of sulfuric acid gas field gas production waste water reinjection treatment process, effluent quality situation after process is generally: SS is 60 ~ 100mg/L, median particle size 15 μm ~ 20 μm, oil 10mg/L ~ 25mg/L, sulphur 18mg/L ~ 55mg/L, 100, SRB bacterium/mL ~ 500/mL, 3000, TGB bacterium/mL ~ 8000/mL, iron bacteria 3000/mL ~ 5000/mL, total iron 5mg/L ~ 20mg/L, erosion rate 0.180mm/a ~ 0.850mm/a.Processed waste water water quality difficulty reaches the A3 standard in SY/T5329-94 petroclastic rock reservoir water water quality proposed standard as stated above.If be above standard water filling for a long time, can damage water injecting pipeline, affect the work-ing life of water injection well, even can affect groundwater quality, this present situation is urgently to be resolved hurrily.
Summary of the invention
Technology to be solved by this invention is, be difficult to reach the A3 standard in SY/T5329-94 petroclastic rock reservoir water water quality proposed standard to overcome in prior art the technique processing sulfuric acid gas field gas production waste water, finally cause damaging water injecting pipeline, affect the work-ing life of water injection well, even can affect the defect of groundwater quality, and a kind of sulfuric acid gas field gas production waste water reinjection treatment process is provided.Gas production waste water reinjection processing technological flow of the present invention is easy, running cost is lower, management is simple, effectively can process sulfuric acid gas field gas production waste water, and water outlet reaches the A3 standard in People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index.
The invention provides sulfuric acid gas field gas production waste water reinjection treatment process, it to comprise the steps: sulfuric acid gas field gas production waste water successively through oil removal and oil removal treatment, aeration sulphur removal, chemical oxidation sulphur removal, coagulation and flocculation treatment, precipitation, sterilization, two medium filter filter, fiber bundle filter filters, ultrafiltration and corrosion-mitigation scale-inhibition; In described corrosion-mitigation scale-inhibition, the corrosion inhibiting and descaling agent of employing comprises 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid, sodium sulfonate and benzotriazole.
Described sulfuric acid gas field gas production waste water is the sulfuric acid gas field gas production waste water described in the routine of this area, general SS is 200 ~ 800mg/L, median particle size 45 μm ~ 120 μm, oil 48mg/L ~ 125mg/L, 10000, sulphur 118mg/L ~ 1250mg/L, SRB bacterium/mL ~ 30000/mL, 100000, TGB bacterium/mL ~ 800000/mL, iron bacteria 100000/mL ~ 500000/mL, total iron 25mg/L ~ 70mg/L, erosion rate 2.250mm/a ~ 9.560mm/a.
In the present invention, described oil removing and oil removal process can be oil removing and the oil removal process of this area routine, are preferably through air-dissolving air-float process.
Described air-dissolving air-float process preferably adopts the process of nitrogen air-dissolving air-float.The device of the device preferred nitrogen air-dissolving air-float of described air-dissolving air-float.
The processing parameter that the processing parameter of described nitrogen dissolved air flotation device can refer to conventional nitrogen dissolved air flotation device is selected.
The described nitrogen air-dissolving air-float residence time preferred 10s ~ 20s.
The treatment temp of the device of described nitrogen air-dissolving air-float preferably 10 DEG C ~ 70 DEG C.
In described nitrogen air-dissolving air-float process, the preferred 0.3MPa ~ 0.4MPa of pressure of the molten gas of nitrogen.
In described nitrogen air-dissolving air-float process, the preferred 15m/s ~ 20m/s of molten gas velocity in nitrogen air dissolving system molten gas releasing tube.
In described nitrogen air-dissolving air-float process, the preferred 0.5m/s ~ 1.0m/s of nitrogen air dissolving system release head release flow velocity.
In described nitrogen air-dissolving air-float process, the diameter preferably 30 μm ~ 50 μm of nitrogen air dissolving system release bubble.
In the present invention, described aeration sulphur removal can be the aeration sulphur removal of this area routine, and its device, condition and step all can conveniently be selected.
The device of described aeration sulphur removal is preferably a closed unit and is connected with spray-type hydrogen sulfide absorption tower.
The each processing parameter of device of described aeration sulphur removal is as described in routine.
The residence time preferred 2h ~ 3h of the device of described aeration sulphur removal.
Gas-water ratio preferably (20:1) ~ (100:1) of the aeration rate of described aeration sulphur removal.
Preferred 2m/s ~ the 5m/s of gas flow rate of described spray-type hydrogen sulfide absorption tower air inlet.
Described spray-type hydrogen sulfide absorption tower preferably adopts volution nozzle.
In described spray-type hydrogen sulfide absorption tower, fogdrop diameter preferably 100 μm ~ 200 μm.
In described spray-type hydrogen sulfide absorption tower, add the gas medicine of sodium hydroxide than preferred 1m
3: (20g ~ 100g).
In described spray-type hydrogen sulfide absorption tower, add the gas medicine of clorox than preferred 1m
3: (50g ~ 500g).
In described spray-type hydrogen sulfide absorption tower, the preferred 100m of specific liquid rate
3/ m
2﹒ h ~ 160m
3/ m
2﹒ h.
In the present invention, described chemical oxidation sulphur removal can be the chemical oxidation sulphur removal of this area routine, and its each processing condition and step all can be selected by the routine of this area.
In described chemical oxidation sulphur removal, pharmacy optimization clorox used.
In described chemical oxidation sulphur removal, described clorox is preferably the clorox of 10% available chlorine containing massfraction, the preferred 2500mg/L ~ 30000mg/L of its dosage.Described available chlorine refers to oxidation state chlorine contained in chlorine-containing compound.
The residence time preferred 0.2h ~ 0.5h of described chemical oxidation sulphur removal.
In described chemical oxidation sulphur removal, agent mixer preferred pipeline formula mixing tank.In described pipeline mixer, the preferred 2m of mixinglength.
In the present invention, described coagulation and flocculation can be coagulation and the flocculation of this area routine, and its each processing condition and step all can refer to routine and select.
In described coagulation and flocculation treatment, generally first carry out coagulation and flocculate again.
In described coagulation and flocculation treatment, coagulating agent preferential oxidation aluminium content used is the polymerize aluminum chloride of 30%, and described percentage ratio is mass percent.Preferred 80mg/L ~ the 300mg/L of dosage of described polymer alumina.
In described coagulation and flocculation treatment, the reaction times preferred 20min ~ 30min of coagulation.
In described coagulation and flocculation treatment, flocculation agent preferred cationic flocculation agent.Described cationic flocculant optimization polypropylene acid amides.Preferred 1mg/L ~ the 4mg/L of dosage of described polyacrylamide.
In described coagulation and flocculation treatment, flocculation reaction time preferred 5min ~ 10min.
Described precipitation is generally carried out in settling vessel.Generally tube settling is adopted in described settling vessel.
The time preferred 1h ~ 2h of described precipitation.
The preferred 1m of surface load of described tube settling
3/ m
2﹒ h ~ 2m
3/ m
2﹒ h.
In the present invention, the process of described sterilization can be the sterilization process of this area routine, and its processing step and condition all can be selected by the routine of this area.
The preferred clorox of described sterilant.Preferred 5mg/l ~ the 10mg/l/ of dosage of described sterilant.
It is 10% available chlorine that described clorox preferably contains massfraction.Described available chlorine refers to oxidation state chlorine contained in chlorine-containing compound.
In the present invention, the two medium filters adopted during described two medium filters filter can be two medium filters of this area routine, and its processing condition and step all can conveniently be selected.
The filtrate upper strata of described two medium filters is preferably hard coal, and lower floor is preferably quartz sand.
The filtering velocity of described two medium filters is preferably 5.0m/h ~ 17.0m/h.
In the filler of described two medium filters, the preferred 0.4mm ~ 0.65mm of particle diameter (nonuniformity coefficient < 2) of quartz sand.
In the filler of described two medium filters, the preferred 0.8mm ~ 1.6mm of anthracitic particle diameter (nonuniformity coefficient < 2).
In the present invention, the fiber bundle filter used during described fiber bundle filter filters can be the fiber bundle filter of this area routine, and its processing condition and step all can conveniently be selected.
The filtering velocity of described fiber bundle filter is preferably 10.0m/h ~ 15.0m/h.
The filtrate filament diameter of described fiber bundle filter preferably 20 μm.
In the present invention, described ultrafiltration preferably uses ultrafiltration membrance filter.
The membrane pore size of described ultra-filtration membrane preferably 0.1 μm ~ 0.001 μm, unit surface water production rate 25L/m
2h.
Preferred 0.10MPa ~ 0.25MPa is pressed in the operation of described ultrafiltration.
In the present invention, described corrosion-mitigation scale-inhibition process can be the corrosion-mitigation scale-inhibition process of this area routine, and its processing condition and step all can be selected according to this area routine.
In described corrosion-mitigation scale-inhibition, the preferred 9.0mg/L-14.0mg/L of dosage of described 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid.
In described corrosion-mitigation scale-inhibition, the preferred 21.0mg/L-26.0mg/L of dosage of described sodium sulfonate.
In described corrosion-mitigation scale-inhibition, the preferred 2.5mg/L-3.5mg/L of dosage of described benzotriazole.
Present invention also offers a kind of corrosion inhibiting and descaling agent, it comprises 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid, sodium sulfonate and benzotriazole.
In described corrosion inhibiting and descaling agent, the preferred 9.0mg/L-14.0mg/L of dosage of described 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid.
In described corrosion inhibiting and descaling agent, the preferred 21.0mg/L-26.0mg/L of dosage of described sodium sulfonate.
In described corrosion inhibiting and descaling agent, the preferred 2.5mg/L-3.5mg/L of dosage of described benzotriazole.
Agents useful for same of the present invention and raw material except specified otherwise all commercially.
In the present invention, without prejudice to the field on the basis of common sense, above-mentioned each technical characteristic optimum condition arbitrary combination can obtain preferred embodiments.
Positive progressive effect of the present invention is: sulfuric acid gas field gas production waste water reinjection processing technological flow of the present invention is easy, Construction and operation cost is lower, management is simple, effectively can process sulfuric acid gas field gas production waste water, and realize water outlet and reach A3 standard in People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index.This technique extends the duration of service of reinjection well greatly, guarantees that non-wastewater discharge is to water body; This technique is simply easy to apply, and has fabulous application prospect.
Accompanying drawing explanation
Fig. 1 is sulfuric acid gas field gas production waste water reinjection processing technological flow schematic diagram in embodiment 1.
Embodiment
Mode below by embodiment further illustrates the present invention, but does not therefore limit the present invention among described scope of embodiments.The experimental technique of unreceipted actual conditions in the following example, conventionally and condition, or selects according to catalogue.
The Water-quality control of sulfuric acid gas field gas production waste water reinjection process is according to the A3 standard in People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index and analytical procedure: SS≤3.0mg/L, median particle size≤2.0 μm, oil≤8.0mg/L, sulphur≤6.0mg/L, SRB bacterium≤25/mL, TGB bacterium≤1000/mL, iron bacteria≤1000/mL, total iron≤0.5mg/L, erosion rate≤0.076mm/a.
In following embodiment, the detection method of SS, median particle size, oil, sulphur, SRB bacterium, TGB bacterium, iron bacteria, always iron and erosion rate is all by People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index and analytical procedure.
Embodiment 1
Carry out producing test (see accompanying drawing 1) as a trial, this system design water yield 360m to certain gas field gas production waste water
3/ d, water inlet (most of data) index is: general SS is 230 ~ 680mg/L, median particle size 55 μm ~ 115 μm, oil 55mg/L ~ 100mg/L, 10000, sulphur 250mg/L ~ 1200mg/L, SRB bacterium/mL ~ 30000/mL, 300000, TGB bacterium/mL ~ 800000/mL, iron bacteria 100000/mL ~ 400000/mL, total iron 25mg/L ~ 60mg/L, erosion rate 2.350mm/a ~ 9.500mm/a.
Described all treating processess are in encloses container carries out, technical process used is: by acid gas field gas production waste water through oil removing and suspended substance, then through aeration sulphur removal, again through chemical oxidation sulphur removal, laggard settling vessel again through coagulation carries out mud-water separation, then carries out sterilization two medium filter of going forward side by side and filter, then enters fiber bundle filter and filter, again through ultrafiltration membrance filter, finally carry out re-injection after corrosion-mitigation scale-inhibition process.
The treatment temp of described nitrogen dissolved air flotation device is 20 DEG C ~ 35 DEG C;
The described nitrogen air-dissolving air-float residence time is 15s ~ 20s;
Molten gas velocity 15m/s ~ 20m/s in described nitrogen high pressure air dissolving system molten gas releasing tube;
Described nitrogen high pressure air dissolving system release head release flow velocity is 0.5m/s ~ 1.0m/s;
The diameter 30 μm ~ 50 μm of described nitrogen high pressure air dissolving system release bubble.
The described aeration desulfurizing device residence time is 2.0h ~ 2.5h;
The gas-water ratio of the aeration rate of described aeration sulphur removal is 50:1 ~ 100:1;
Described spray-type hydrogen sulfide absorption tower adopts volution nozzle, fogdrop diameter 100 μm ~ 200 μm;
Gas flow rate 2m/s ~ the 5m/s of described spray-type hydrogen sulfide absorption tower air inlet;
Sodium hydroxide gas medicine is added than being 1m in described spray-type hydrogen sulfide absorption tower
3: 20g ~ 100g and clorox gas medicine compare 1m
3: 50g ~ 500g;
Described specific liquid rate is 100m
3/ m
2﹒ h ~ 160m
3/ m
2﹒ h.
Described chemical oxidation sulfur elimination clorox dosage is 3700mg/L ~ 25000mg/L.
The polymerize aluminum chloride that the coagulating agent that described coagulating sedimentation uses is alumina content 30%, flocculation agent is cationic flocculant;
The dosage of the coagulating agent that described coagulating sedimentation uses is 80mg/L ~ 300mg/L;
The flocculation agent that described coagulating sedimentation uses is polyacrylamide, and dosage is 1mg/L ~ 3.5mg/L;
The described coagulating sedimentation reaction times is 20min ~ 30min;
The described flocculation reaction time is 5min ~ 8min;
The sedimentation time of described coagulating sedimentation is 1h ~ 2h;
The surface load of described tube settling is 1m
3/ m
2﹒ h ~ 1.5m
3/ m
2﹒ h.
Described two medium filter filtrate upper stratas are hard coal, and lower floor is quartz sand;
Described two medium filter filtering velocitys are 10.0m/h ~ 15.0m/h;
Described two medium filter filler quartz sand 0.4mm ~ 0.65mm (nonuniformity coefficient < 2), hard coal 0.8mm ~ 1.6mm (nonuniformity coefficient < 2).
Described fiber bundle filter filtering velocity is 11.0m/h ~ 14.0m/h;
Described fiber bundle filter filtrate filament diameter 20 μm.
Described ultra-filtration membrane membrane pore size 0.1 μm ~ 0.01 μm, unit surface water production rate 25L/m
2h.
The composite medicine of described corrosion inhibiting and descaling agent is: 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid dosage 12.0mg/L, sodium sulfonate dosage 24.0mg/L, benzotriazole 3.0mg/L.
Start-up and functionning result shows, and this system run all right, treatment effect is fine.
After testing, effluent quality: SS≤3mg/L, median particle size≤2.0 μm, oil≤3.0mg/L, sulphur≤2.0mg/L, SRB≤100, TGB≤100, iron bacteria≤100, total iron≤0.1mg/L, erosion rate≤0.010mm/a, water quality meets People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index and analytical procedure.
Embodiment 2
Carry out producing test (see accompanying drawing 1) as a trial, this system design water yield 150m to certain gas field gas production waste water
3/ d.Water inlet (most of data) index is: general SS is 200 ~ 650mg/L, median particle size 45 μm ~ 100 μm, oil 50mg/L ~ 95mg/L, sulphur 120mg/L ~ 1200mg/L, 10000, SRB bacterium/mL ~ 30000/300000, mL, TGB bacterium/mL ~ 700000/mL, iron bacteria 300000/mL ~ 400000/mL, total iron 25mg/L ~ 50mg/L, erosion rate 2.350mm/a ~ 8.950mm/a.
Described all treating processess are in encloses container carries out, technical process used is: by acid gas field gas production waste water through oil removing and suspended substance, then through aeration sulphur removal, again through chemical oxidation sulphur removal, laggard settling vessel again through coagulation carries out mud-water separation, then carries out sterilization two medium filter of going forward side by side and filter, then enters fiber bundle filter and filter, again through ultrafiltration membrance filter, finally carry out re-injection after corrosion-mitigation scale-inhibition process.
The treatment temp of described nitrogen dissolved air flotation device is 20 DEG C ~ 35 DEG C;
The described nitrogen air-dissolving air-float residence time is 15s ~ 20s;
Molten gas velocity 15m/s ~ 20m/s in described nitrogen high pressure air dissolving system molten gas releasing tube;
Described nitrogen high pressure air dissolving system release head release flow velocity is 0.5m/s ~ 1.0m/s;
The diameter 30 μm ~ 50 μm of described nitrogen high pressure air dissolving system release bubble.
The described aeration desulfurizing device residence time is 2.0h ~ 3.0h;
The gas-water ratio of the aeration rate of described aeration sulphur removal is 50:1 ~ 80:1;
Described spray-type hydrogen sulfide absorption tower adopts volution nozzle, fogdrop diameter 100 μm ~ 200 μm;
Gas flow rate 2m/s ~ the 4m/s of described spray-type hydrogen sulfide absorption tower air inlet;
Sodium hydroxide gas medicine is added than being 1m in described spray-type hydrogen sulfide absorption tower
3: 20g ~ 80g and clorox gas medicine compare 1m
3: 50g ~ 450g;
Described specific liquid rate is 100m
3/ m
2﹒ h ~ 130m
3/ m
2﹒ h.
Described chemical oxidation sulfur elimination clorox dosage is 3400mg/L ~ 24000mg/L.
The polymerize aluminum chloride that the coagulating agent that described coagulating sedimentation uses is alumina content 30%, flocculation agent is cationic flocculant;
The dosage of the coagulating agent that described coagulating sedimentation uses is 80mg/L ~ 250mg/L;
The flocculation agent that described coagulating sedimentation uses is polyacrylamide, and dosage is 1.5mg/L ~ 3.0mg/L;
The described coagulating sedimentation reaction times is 20min ~ 30min;
The described flocculation reaction time is 5min ~ 10min;
The sedimentation time of described coagulating sedimentation is 1h ~ 2h;
The surface load of described tube settling is 1.5m
3/ m
2﹒ h ~ 2.0m
3/ m
2﹒ h.
Described two medium filter filtrate upper stratas are hard coal, and lower floor is quartz sand;
Described two medium filter filtering velocitys are 10.0m/h ~ 14.0m/h;
Described two medium filter filler quartz sand 0.4mm ~ 0.65mm (nonuniformity coefficient < 2), hard coal 0.8mm ~ 1.6mm (nonuniformity coefficient < 2).
Described fiber bundle filter filtering velocity is 11.0m/h ~ 14.0m/h;
Described fiber bundle filter filtrate filament diameter 20 μm.
Described ultra-filtration membrane membrane pore size 0.1 μm ~ 0.01 μm, unit surface water production rate 25L/m
2h.
The composite medicine of described corrosion inhibiting and descaling agent is: 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid dosage 13.0mg/L, sodium sulfonate dosage 23.0mg/L, benzotriazole 3.5mg/L.
Start-up and functionning result shows, and this system run all right, treatment effect is fine.
After testing, effluent quality: SS≤3mg/L, median particle size≤2.0 μm, oil≤3.0mg/L, sulphur≤2.0mg/L, SRB≤100, TGB≤1000, iron bacteria≤100, total iron≤0.1mg/L, erosion rate≤0.020mm/a, water quality meets People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index and analytical procedure.
Embodiment 3
Carry out producing test (see accompanying drawing 1) as a trial, this system design water yield 120m to certain gas field gas production waste water
3/ d.Water inlet (most of data) index is: general SS is 240 ~ 760mg/L, median particle size 55 μm ~ 120 μm, oil 55mg/L ~ 80mg/L, sulphur 200mg/L ~ 800mg/L, 10000, SRB bacterium/mL ~ 30000/300000, mL, TGB bacterium/mL ~ 800000/mL, iron bacteria 300000/mL ~ 400000/mL, total iron 25mg/L ~ 50mg/L, erosion rate 1.350mm/a ~ 8.550mm/a.
Described all treating processess are in encloses container carries out, technical process used is: by acid gas field gas production waste water through oil removing and suspended substance, then through aeration sulphur removal, again through chemical oxidation sulphur removal, laggard settling vessel again through coagulation carries out mud-water separation, then carries out sterilization two medium filter of going forward side by side and filter, then enters fiber bundle filter and filter, again through ultrafiltration membrance filter, finally carry out re-injection after corrosion-mitigation scale-inhibition process.
The treatment temp of described nitrogen dissolved air flotation device is 20 DEG C ~ 35 DEG C;
The described nitrogen air-dissolving air-float residence time is 15S ~ 20S;
Molten gas velocity 15m/s ~ 20m/s in described nitrogen high pressure air dissolving system molten gas releasing tube;
Described nitrogen high pressure air dissolving system release head release flow velocity is 0.5m/s ~ 1.0m/s;
The diameter 30 μm ~ 50 μm of described nitrogen high pressure air dissolving system release bubble.
The described aeration desulfurizing device residence time is 2.0h ~ 2.6h;
The gas-water ratio of the aeration rate of described aeration sulphur removal is 60:1 ~ 80:1;
Described spray-type hydrogen sulfide absorption tower adopts volution nozzle, fogdrop diameter 100 μm ~ 200 μm;
Gas flow rate 2m/s ~ the 3m/s of described spray-type hydrogen sulfide absorption tower air inlet;
Sodium hydroxide gas medicine is added than being 1m in described spray-type hydrogen sulfide absorption tower
3: 30g ~ 90g and clorox gas medicine compare 1m
3: 40g ~ 400g;
Described specific liquid rate is 100m
3/ m
2﹒ h ~ 150m
3/ m
2﹒ h.
Described chemical oxidation sulfur elimination clorox dosage is 3500mg/L ~ 28000mg/L.
The polymerize aluminum chloride that the coagulating agent that described coagulating sedimentation uses is alumina content 30%, flocculation agent is cationic flocculant;
The dosage of the coagulating agent that described coagulating sedimentation uses is 80mg/L ~ 200mg/L;
The flocculation agent that described coagulating sedimentation uses is polyacrylamide, and dosage is 2.0mg/L ~ 3.5mg/L;
The described coagulating sedimentation reaction times is 20min ~ 30min;
The described flocculation reaction time is 5min ~ 10min;
The sedimentation time of described coagulating sedimentation is 1h ~ 2h;
The surface load of described tube settling is 1.5m
3/ m
2﹒ h ~ 2.0m
3/ m
2﹒ h.
Described two medium filter filtrate upper stratas are hard coal, and lower floor is quartz sand;
Described two medium filter filtering velocitys are 10.0m/h ~ 15.0m/h;
Described two medium filter filler quartz sand 0.4mm ~ 0.65mm (nonuniformity coefficient < 2), hard coal 0.8mm ~ 1.6mm (nonuniformity coefficient < 2).
Described fiber bundle filter filtering velocity is 11.0m/h ~ 14.0m/h;
Described fiber bundle filter filtrate filament diameter 20 μm.
Described ultra-filtration membrane membrane pore size 0.1 μm ~ 0.01 μm, unit surface water production rate 25L/m
2h.
The composite medicine of described corrosion inhibiting and descaling agent is: 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid dosage 11.0mg/L, sodium sulfonate dosage 22.0mg/L, benzotriazole 2.0mg/L.
Start-up and functionning result shows, and this system run all right, treatment effect is fine.
After testing, effluent quality: SS≤3mg/L, median particle size≤2.0 μm, oil≤3.0mg/L, sulphur≤2.0mg/L, SRB≤100, TGB≤100, iron bacteria≤100, total iron≤0.1mg/L, erosion rate≤0.015mm/a, water quality meets People's Republic of China (PRC) oil and gas industry standard SY/T5329-94 petroclastic rock reservoir water water quality fertilizer index and analytical procedure.
Claims (11)
1. sulfuric acid gas field gas production waste water reinjection treatment process, it is characterized in that comprising the steps: that coagulation and flocculation treatment, precipitation, sterilization, two medium filter filter, fiber bundle filter filters by sulfuric acid gas field gas production waste water successively through oil removing and oil removal process, aeration sulphur removal, chemical oxidation sulphur removal, ultrafiltration and corrosion-mitigation scale-inhibition; Described oil removing and oil removal process adopt the process of nitrogen air-dissolving air-float; In described corrosion-mitigation scale-inhibition, the corrosion inhibiting and descaling agent of employing is made up of 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid, sodium sulfonate and benzotriazole; The dosage of described 1-Hydroxy Ethylidene-1,1-Diphosphonic Acid is 9.0mg/L ~ 14.0mg/L; The dosage of described sodium sulfonate is 21.0mg/L ~ 26.0mg/L; The dosage of described benzotriazole is 2.5mg/L ~ 3.5mg/L; In described sulfuric acid gas field gas production waste water, SS is 200 ~ 800mg/L, median particle size 45 μm ~ 120 μm, oil 48mg/L ~ 125mg/L, 10000, sulphur 118mg/L ~ 1250mg/L, SRB bacterium/mL ~ 30000/mL, 100000, TGB bacterium/mL ~ 800000/mL, iron bacteria 100000/mL ~ 500000/mL, total iron 25mg/L ~ 70mg/L, erosion rate 2.250mm/a ~ 9.560mm/a.
2. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: the residence time of described nitrogen air-dissolving air-float is 10s ~ 20s; The treatment temp of the device of described nitrogen air-dissolving air-float is 10 DEG C ~ 70 DEG C; In described nitrogen air-dissolving air-float process, the pressure of the molten gas of nitrogen is 0.3MPa ~ 0.4MPa; In described nitrogen air-dissolving air-float process, in nitrogen air dissolving system molten gas releasing tube, molten gas velocity is 15m/s ~ 20m/s; In described nitrogen air-dissolving air-float process, nitrogen air dissolving system release head release flow velocity is 0.5m/s ~ 1.0m/s; In described nitrogen air-dissolving air-float process, the diameter of nitrogen air dissolving system release bubble is 30 μm ~ 50 μm.
3. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: the device of described aeration sulphur removal is a closed unit and is connected with spray-type hydrogen sulfide absorption tower; The residence time of the device of described aeration sulphur removal is 2h ~ 3h; The gas-water ratio of the aeration rate of described aeration sulphur removal is (20:1) ~ (100:1); The gas flow rate of described spray-type hydrogen sulfide absorption tower air inlet is 2m/s ~ 5m/s; Described spray-type hydrogen sulfide absorption tower adopts volution nozzle; In described spray-type hydrogen sulfide absorption tower, fogdrop diameter is 100 μm ~ 200 μm; In described spray-type hydrogen sulfide absorption tower, add the gas medicine of sodium hydroxide than being 1m
3: (20g ~ 100g); In described spray-type hydrogen sulfide absorption tower, add the gas medicine of clorox than being 1m
3: (50g ~ 500g); In described spray-type hydrogen sulfide absorption tower, specific liquid rate is 100m
3/ m
2﹒ h ~ 160m
3/ m
2﹒ h.
4. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, it is characterized in that: in described chemical oxidation sulphur removal, medicament used is clorox; Described clorox is be the clorox of 10% available chlorine containing massfraction, and its dosage is 2500mg/L ~ 30000mg/L; The residence time of described chemical oxidation sulphur removal is 0.2h ~ 0.5h; In described chemical oxidation sulphur removal, agent mixer is pipeline mixer; In described pipeline mixer, mixinglength is 2m.
5. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: in described coagulation and flocculation treatment, first carry out coagulation and flocculate; In described coagulation and flocculation treatment, coagulating agent used to be alumina content be 30% polymerize aluminum chloride, described percentage ratio is mass percent; The dosage of described polymer alumina is 80mg/L ~ 300mg/L; Described coagulation is with in flocculation, and the reaction times of coagulation is 20min ~ 30min.
6. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: in described coagulation and flocculation treatment, flocculation agent is cationic flocculant; Described cationic flocculant is polyacrylamide; The dosage of described polyacrylamide is 1mg/L ~ 4mg/L; Described coagulation is with in flocculation, and the flocculation reaction time is 5min ~ 10min.
7. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: described being deposited in settling vessel is carried out; Tube settling is adopted in described settling vessel; The time of described precipitation is 1h ~ 2h; The surface load of described tube settling is 1m
3/ m
2﹒ h ~ 2m
3/ m
2﹒ h.
8. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: the sterilant adopted in described sterilization is clorox; The dosage of described sterilant is 5mg/l ~ 10mg/l; It is 10% available chlorine that described clorox contains massfraction.
9. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: the filtrate upper strata of described two medium filters is hard coal, and lower floor is quartz sand; The filtering velocity of described two medium filters is 5.0m/h ~ 17.0m/h; In the filler of described two medium filters, the particle diameter of quartz sand is 0.4mm ~ 0.65mm, nonuniformity coefficient < 2; In the filler of described two medium filters, anthracitic particle diameter is 0.8mm ~ 1.6mm, nonuniformity coefficient < 2.
10. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: the filtering velocity of described fiber bundle filter is 10.0m/h ~ 15.0m/h; The filtrate filament diameter of described fiber bundle filter is 20 μm.
11. sulfuric acid gas field gas production waste water reinjection treatment process as claimed in claim 1, is characterized in that: described ultrafiltration ultrafiltration membrance filter; The membrane pore size of described ultra-filtration membrane is 0.1 μm ~ 0.001 μm, unit surface water production rate 25L/m
2h; The operation pressure of described ultrafiltration is 0.10MPa ~ 0.25MPa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210537451.XA CN103880202B (en) | 2012-12-12 | 2012-12-12 | Sulfuric acid gas field gas production waste water reinjection treatment process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210537451.XA CN103880202B (en) | 2012-12-12 | 2012-12-12 | Sulfuric acid gas field gas production waste water reinjection treatment process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103880202A CN103880202A (en) | 2014-06-25 |
| CN103880202B true CN103880202B (en) | 2015-11-25 |
Family
ID=50949375
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210537451.XA Active CN103880202B (en) | 2012-12-12 | 2012-12-12 | Sulfuric acid gas field gas production waste water reinjection treatment process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103880202B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106256780A (en) * | 2015-06-18 | 2016-12-28 | 中国石油化工股份有限公司 | A kind of reinjection treatment method up to standard of the wastewater with high concentration of sulfide of oil gas field |
| CN105174581B (en) * | 2015-09-02 | 2017-09-15 | 中国石油化工股份有限公司 | A kind of sulfur Gas Fields produced water treatment technique |
| CN106698733A (en) * | 2015-11-12 | 2017-05-24 | 中国石油化工股份有限公司 | Deep desulfurization method for high-sulfur-containing wastewater of oil and gas field |
| CN106854020B (en) * | 2015-12-09 | 2020-02-14 | 中国石油天然气股份有限公司 | Method for recycling sulfur-containing gas production wastewater |
| CN107285505B (en) * | 2016-04-11 | 2020-02-18 | 中国石油化工股份有限公司 | Method for emission of high-sulfur-content wastewater of oil and gas field by reducing injection and reaching standard |
| CN107285503B (en) * | 2016-04-11 | 2020-02-18 | 中国石油化工股份有限公司 | Method for discharging high-sulfur-content wastewater of oil and gas field after injection reduction and reaching standards |
| CN106673265B (en) * | 2017-02-09 | 2020-01-31 | 陕西延长石油(集团)有限责任公司研究院 | Treatment method of oil-gas field high-sulfur-content sewage |
| CN107082506B (en) * | 2017-04-19 | 2020-07-28 | 陕西省石油化工研究设计院 | A kind of treatment method and technological process of oil field produced water |
| CN111285532A (en) * | 2019-12-24 | 2020-06-16 | 大庆油田有限责任公司 | Corrosion inhibitor-containing gas field water reinjection treatment device and process |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006043600A (en) * | 2004-08-05 | 2006-02-16 | Hakuto Co Ltd | Inhibitor of calcium carbonate scale by slaked lime suspension and method of inhibiting calcium carbonate scale |
| CN1789159A (en) * | 2005-12-05 | 2006-06-21 | 赵清顺 | Sterilization inhibitor for circulated cooling water treatment |
| JP2007039613A (en) * | 2005-08-05 | 2007-02-15 | Nippon Steel Corp | Gasification gas purification method and apparatus |
| CN101037271A (en) * | 2007-04-28 | 2007-09-19 | 阮文权 | Biological desulfurizing device for transforming sulfur-containing compound to elemental sulfur |
| CN101125717A (en) * | 2006-08-15 | 2008-02-20 | 中国石油天然气股份有限公司 | Ternary combination flooding produced liquid oil-containing sewage treatment process |
| CN101172726A (en) * | 2007-11-08 | 2008-05-07 | 长庆石油勘探局 | Method and technological process for treating sewage of oil recovery |
-
2012
- 2012-12-12 CN CN201210537451.XA patent/CN103880202B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006043600A (en) * | 2004-08-05 | 2006-02-16 | Hakuto Co Ltd | Inhibitor of calcium carbonate scale by slaked lime suspension and method of inhibiting calcium carbonate scale |
| JP2007039613A (en) * | 2005-08-05 | 2007-02-15 | Nippon Steel Corp | Gasification gas purification method and apparatus |
| CN1789159A (en) * | 2005-12-05 | 2006-06-21 | 赵清顺 | Sterilization inhibitor for circulated cooling water treatment |
| CN101125717A (en) * | 2006-08-15 | 2008-02-20 | 中国石油天然气股份有限公司 | Ternary combination flooding produced liquid oil-containing sewage treatment process |
| CN101037271A (en) * | 2007-04-28 | 2007-09-19 | 阮文权 | Biological desulfurizing device for transforming sulfur-containing compound to elemental sulfur |
| CN101172726A (en) * | 2007-11-08 | 2008-05-07 | 长庆石油勘探局 | Method and technological process for treating sewage of oil recovery |
Non-Patent Citations (2)
| Title |
|---|
| 含油污水中硫化物的处理技术;彭勃 等;《油气田环境保护》;20040930;第14卷(第3期);第10-11页 * |
| 高酸性油气田污水处理工艺;董正军;《石油化工应用》;20110430;第30卷(第4期);第70页第1节-第72页第5节 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103880202A (en) | 2014-06-25 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103880202B (en) | Sulfuric acid gas field gas production waste water reinjection treatment process | |
| CN104310628B (en) | A kind of reuse method of water-base fracturing flowback fluid | |
| US8734650B2 (en) | Method for recovering gas from shale reservoirs and purifying resulting produced water to allow the produced water to be used as drilling or frac water, or discharged to the environment | |
| CN102295359B (en) | Treatment method for deep-well polysulfide slurry drilling waste water | |
| CN105540947A (en) | Method and system for processing drilling wastewater | |
| CN101898854B (en) | Method and device for treatment of high-sulfur content and low-permeability oil reservoir produced wastewater | |
| CN106315903A (en) | Method for processing shale gas fracturing flowback fluid | |
| CN101891320A (en) | Treatment method realizing polymer-bearing produced wastewater resource utilization | |
| CN110255792A (en) | A kind of extra permeability oilfield recovered water stably reaching standard processing system and its treatment process | |
| CN102583816A (en) | Method for reusing and treating oily wastewater by adopting nitrogen gas floatation technology | |
| CN109937191A (en) | Method and apparatus for handling the output water from oil field and gas field | |
| CN107417019A (en) | A kind for the treatment of Technology for Petroleum Water Flooding | |
| KR100954571B1 (en) | Method of Preventing Manganese Oxide Formation in Backwashing Process of Membrane Filtration | |
| CN216711764U (en) | System for directly arrange outward after oil gas field water treatment | |
| CN105668845B (en) | Using offshore oilfield recovered water as the processing method of reinjected water | |
| CN101671091A (en) | Processing method for produced water for ultra-low permeable oil field reinjection | |
| CN106116022B (en) | A kind of ammonia nitrogen processing method in acid waste water containing heavy metal | |
| Bhatkar et al. | Modifications of petroleum industry effluent treatment Method: An approach for quality improvement of process water for ASP flooding and chemical EOR | |
| CN104370378B (en) | Method and device for fixed-point calcium scale removal of oilfield injection water | |
| CN207294436U (en) | A kind of device of thin oil oily wastewater pretreatment stabilizing water quality | |
| CN106430742A (en) | Method for pretreating petroleum fracturing liquid wastewater | |
| CA2939965A1 (en) | Tank gas bubbler | |
| CN111499040A (en) | Oil field fracturing flowback fluid reinjection treatment method | |
| CN205151850U (en) | Integrative pond is filtered in electrolysis | |
| CN106477758B (en) | A kind of fracturing outlet liquid process for reclaiming |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: SHANGHAI EMPEROR OF CLEANING TECH. CO., LTD. Free format text: FORMER OWNER: WANG WEI Effective date: 20150204 Free format text: FORMER OWNER: SHANGHAI EMPEROR OF CLEANING TECH. CO., LTD. Effective date: 20150204 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20150204 Address after: 200437 5F, B, Bai Shu Building, No. 1230, Bei Bei Road, Hongkou District, Shanghai, Zhongshan Applicant after: Shanghai Emperor of Cleaning Tech Co., Ltd. Address before: 200437 5F, B, Bai Shu Building, No. 1230, Bei Bei Road, Hongkou District, Shanghai, Zhongshan Applicant before: Wang Wei Applicant before: Shanghai Emperor of Cleaning Tech Co., Ltd. |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |