CN108623082A - A kind of recycling processing method of gas field output water - Google Patents
A kind of recycling processing method of gas field output water Download PDFInfo
- Publication number
- CN108623082A CN108623082A CN201710179194.XA CN201710179194A CN108623082A CN 108623082 A CN108623082 A CN 108623082A CN 201710179194 A CN201710179194 A CN 201710179194A CN 108623082 A CN108623082 A CN 108623082A
- Authority
- CN
- China
- Prior art keywords
- water
- gas field
- reverse osmosis
- mvr
- high pressure
- 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.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/10—Nature of the water, waste water, sewage or sludge to be treated from quarries or from mining activities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
- C02F5/08—Treatment of water with complexing chemicals or other solubilising agents for softening, scale prevention or scale removal, e.g. adding sequestering agents
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
The present invention relates to a kind of recycling processing methods of gas field output water.This method is used except as hard as the filter reverse osmosis MVR techniques of catalytic ozonation A/O/MBR high pressures, effectively remove hardness, suspended matter, organic matter, salt and the ammonia nitrogen in waste water, solve the problems, such as that the indexs such as hardness, suspended matter, organic matter, ammonia nitrogen, chloride are excessively high during the output water recycling treatment of gas field, waste water reinjection amount is effectively reduced, realizes the recycling treatment of gas field output water.Finally obtained high pressure reverse osmosis produced water and MVR evaporation production water are back to circulating cooling make-up water, MVR mother liquor re-injections.Except the process combination as hard as filter catalytic ozonation A/O/MBR in the present invention, it is suitable for handling high rigidity, the gas field output water of high organic matter；The reverse osmosis combination with MVR techniques of high pressure realizes the most depth concentration of gas field output water, reduces the re-injection amount of gas field output water to greatest extent, and realize the recycling of waste water under the early period for reducing operating cost.
Description
Technical field
The present invention relates to field of industrial waste water treatment, specifically a kind of recycling processing method of gas field output water.Especially
Refer to using except as hard as filter-catalytic ozonation-A/O/MBR- high pressures it is reverse osmosis-mechanical steam recompression (MVR) technical finesse
The recycling processing method of gas field output water.
Background technology
With the continuous improvement of socio-economic development and living standards of the people, demand for energy is increasingly increased, gas field is opened
The amount of adopting increases year by year.In the exploitation in gas field, especially in the middle and later periods of gas field development, since water flooding can be along tomography and construction
Crack invades gas reservoir, into shaft bottom, gas reservoir energy loss is made to increase, and well head pressure reduces, and band outlet capacity is deteriorated, and gas well is caused to subtract
Production or water logging stop production.To maintain the steady production of natural gas, gas field to carry out water drainage-gas recovery technology energetically so that the water yield of gas well
It increases sharply, many gas wells are forced closing well because extracted waste water can not handle, and affect normal gas production production.
While causing problem to gas field production, caused social concern also appears undoubtedly gas field output water, to certainly
Right environment causes a large amount of extracted waste waters generated during huge pressure, especially mining area of southwest China gas-field exploitation, the waste water
In addition to containing a large amount of hydrogen sulfide and sulfide, also contain a large amount of salt, organic matter, ammonia nitrogen and suspended matter etc..If cannot have
Effect processing can not only generate environment serious pollution, can also generate heavy corrosion to waterline, there are serious safety is hidden
Suffer from.
Processing for gas field output water mainly has provided after standard discharge or advanced treating after reinjection into reservoir, processing at present
Source by etc. in the way of.For existing treatment process, presently mainly carry out re-injection after reasonable sanding, in standard discharge and
It is rarely reported in terms of recycling treatment.Current main recycling whereabouts is to be used for circulating cooling make-up water, is mended according to recirculated water
The reuse standard of water, for the output water recycling treatment of gas field, main processing target is most of salt in water removal
Point, organic matter, suspended matter and ammonia nitrogen.
Invention content
In view of the deficiencies in the prior art, at the purpose of the present invention is to provide a kind of recycling of gas field output water
Reason method, using except as hard as the reverse osmosis-MVR techniques of filter-catalytic ozonation-A/O/MBR- high pressures, effectively removing in waste water
Hardness, suspended matter, organic matter, salt and ammonia nitrogen solve hardness during the output water recycling treatment of gas field, suspended matter, organic
The excessively high problem of the indexs such as object, ammonia nitrogen and chloride effectively reduces waste water reinjection amount, at the recycling for realizing gas field output water
Reason.
To achieve the above objectives, the technical solution adopted by the present invention is that：
A kind of recycling processing method of gas field output water, includes the following steps：The first step, using except being gone as hard as filtering technology
Most of hardness in degasification field produced water and suspended matter；Second step, using catalytic ozonation removal except as hard as filtering out in water
Hardly degraded organic substance；Third walks, using the easily biodegradable organics and ammonia in the removal catalytic ozonation water outlet of A/O/MBR techniques
Nitrogen；4th step concentrates A/O/MBR Process for Effluent, by most of salt in A/O/MBR Process for Effluent using high pressure reverse osmosis separation
Class removes, and forms high pressure reverse osmosis produced water and high pressure reverse osmosis concentrated water；5th step, using MVR techniques by high pressure reverse osmosis concentrated water
Further concentration forms MVR evaporations production water and MVR mother liquors, and MVR mother liquors carry out reinjection technology, and high pressure reverse osmosis produced water and MVR steam
Hair production water reuse.
Based on the above technical solution, following steps are specifically included：
Step 1, gas field output water, which enters, removes hard filter element, is added and removes hard medicament, reaction enters clarification after a certain period of time
Pond carries out clarification filtration, is formed except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
Step 2, it except ozone catalytic oxidation unit is entered as hard as filtering out water, stops after a certain period of time, forms ozone catalytic oxygen
Dissolve water；
Step 3, catalytic ozonation water outlet enters A/O/MBR units, respectively in A sections of anoxic, aerobic O sections and MBR membrane cisterna
It stops after a certain period of time, forms MBR and produce water；
Step 4, MBR, which produces water and enters high pressure reverse osmosis units, carries out separation concentration, forms high pressure reverse osmosis produced water and high pressure
Reverse osmosis concentrated water, high pressure reverse osmosis produced water reuse；
Step 5, high pressure reverse osmosis concentrated water enters MVR units evaporation and concentration, forms MVR mother liquors and MVR evaporation production water, MVR
Mother liquor carries out reinjection technology, MVR evaporation production water reuses.
Based on the above technical solution, in step 1, the main water quality characteristic of the gas field output water is：Inlet flow-patterm
7~8,10000~22000mg/L of total dissolved solid, 300~1500mg/L of suspended matter, 0~20mg/L of oil content, ammonia nitrogen 50
~200mg/L, total hardness (CaCO3Meter) 1500~3000mg/L, total alkalinity (CaCO3Meter) 550-950mg/L, Na+4000~
10000mg/L, Cl-5000~12000mg/L, SO4 2-800~1500mg/L, COD1500~3000mg/L.
Based on the above technical solution, through step 1~5 treated gas field output waters, in MVR mother liquors, oil content
＜ 5mg/L, suspended matter ＜ 1mg/L meet gas field re-injection water quality standard；High pressure reverse osmosis produced water and MVR evaporation production water conductivities ＜
1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, total oil ＜ 0.5mg/L, meet circulating cooling make-up water
Reuse standard.
Based on the above technical solution, in step 1, the hard medicament that removes except in hard filter element is sodium hydroxide
And sodium carbonate, except the proportioning of hard medicament is sodium hydroxide：Sodium carbonate is 6~8:1, the medicament reaction time is 15~30min, except hard
PH controls are 10.8~11.5, and except the hard rear clarifying basin that enters filters, the residence time is 30min~90min.
Based on the above technical solution, in step 2, except as hard as filtering out before water enters ozone catalytic oxidation unit,
Pipeline dosing pump is set, and medicament is sodium hypochlorite；When except 50mg/L is higher than as hard as the ammonia-nitrogen content filtered out in water, time chlorine is added
Sour sodium, dosage is ammonia nitrogen in waste water and sodium hypochlorite mass ratio is 1：8~9.
Based on the above technical solution, the inlet flow-patterm of ozone catalytic oxidation unit described in step 2 is 7~8, is stopped
Time is 1~2h, ozone concentration 125-135mg/L；Ozone dosage is 800~1500mg/L.
Based on the above technical solution, A/O/MBR units described in step 3, the A sections of residence times of anoxic are 4~6h,
Aerobic O sections and MBR membrane cisterna 27~32h of total residence time, sludge reflux amount 300~400%, sludge volume 1~2%, sludge concentration
10~12g/L；
With this condition, the control of MBR membrane fluxs is in 10~12L/m2·h。
Based on the above technical solution, high pressure reverse osmosis units described in step 4 uses disc tube reverse osmosis (dt-ro) film group
Part, membrane module form are that multiple disc-type diaphragms are connected on composition disc-type film column on a central tube；High pressure reverse osmosis units
Service condition be：Operating pressure is 5~7MPa, and inlet flow-patterm is 7~10.
With this condition, the membrane flux of high pressure reverse osmosis units is controlled in 7~10L/m2H, high pressure reverse osmosis concentrated water
TDS (dissolvability solid amount) is 40000~60000mg/L.
Based on the above technical solution, MVR units described in step 5 uses existing commercially available MVR evaporators, MVR female
The TDS controls of liquid are back to circulating cooling make-up water after 150000mg/L, MVR evaporations production water and the mixing of high pressure reverse osmosis produced water.
The recycling processing method of gas field output water of the present invention, using except as hard as filter-catalytic ozonation-A/O/
Reverse osmosis-MVR the techniques of MBR- high pressures effectively remove hardness, suspended matter, organic matter, salt and the ammonia nitrogen in waste water, solve gas field
The excessively high problem of the indexs such as hardness, suspended matter, organic matter, ammonia nitrogen, chloride, effectively reduces during output water recycling treatment
Waste water reinjection amount realizes the recycling treatment of gas field output water.
The essential distinction of the present invention and the prior art is：For the technological deficiency of the prior art, the present invention is used and is removed
As hard as filter-catalytic ozonation-A/O/MBR- high pressures reverse osmosis-MVR process gas field output water.By using the technology,
Realize efficient, quick, the inexpensive recycling treatment of gas field output water.Compared to the prior art, technology of the present invention
Equipment is simple, operation and maintenance are easy, operating cost substantially reduces, and Technical Economy is good.For gas field output water, the present invention relates to
Resource treatment technique it is more economical, reasonable, feasible.
Advantageous effect：
1, the present invention by gas field output water except the most of hardness as hard as filter, eliminated in the output water of gas field, outstanding
Float and a small amount of organic matter, avoid the fouling of catalyst during follow-up catalytic ozonation, extend catalytic ozonation
The cleaning frequency of unit；
2, the present invention is removed using catalytic ozonation removal as hard as the hardly degraded organic substance filtered out in water, reduces follow-up A/
The processing load of O/MBR techniques, ensure that the producing water water quality of follow-up reverse osmosis membrane system, extend the cleaning frequency of membranous system,
It ensure that the operation steady in a long-term of membranous system；
3, the present invention removes easily biodegradable organics and ammonia nitrogen in waste water by using A/O/MBR techniques, has cultivated with high salt
Under the conditions of salt-durable microbe bacterium, improve the organic matter removal effect under high salt conditions；
4, it is suitable for processing high rigidity, height except the process combination as hard as filter-catalytic ozonation-A/O/MBR in the present invention
The gas field output water of organic matter；
5, the present invention under the early period for reducing operating cost, is realized by using high pressure is reverse osmosis and the combination of MVR techniques
The most depth concentration of gas field output water, reduces the re-injection amount of gas field output water, and realize the money of waste water to greatest extent
Sourceization utilizes.
Description of the drawings
The present invention has following attached drawing：
The process flow chart of Fig. 1 present invention.
Specific implementation mode
Below in conjunction with attached drawing, invention is further described in detail.
As shown in Figure 1, a kind of recycling processing method of gas field output water of the present invention, includes the following steps：The
One step, using except the most of hardness and suspended matter removed as hard as filtering technology in the output water of gas field；Second step, using ozone catalytic
Oxidation removal is removed as hard as the hardly degraded organic substance filtered out in water；Third walks, and is gone out using A/O/MBR techniques removal catalytic ozonation
Easily biodegradable organics in water and ammonia nitrogen；4th step concentrates A/O/MBR Process for Effluent, by A/O/ using high pressure reverse osmosis separation
Most of salt removing in MBR Process for Effluent, forms high pressure reverse osmosis produced water and high pressure reverse osmosis concentrated water；5th step uses
MVR techniques further concentrate high pressure reverse osmosis concentrated water, form MVR evaporations production water and MVR mother liquors, and MVR mother liquors carry out at re-injection
Reason, high pressure reverse osmosis produced water and MVR evaporation production water reuses.
Based on the above technical solution, following steps are specifically included：
Step 1, gas field output water, which enters, removes hard filter element, is added and removes hard medicament, reaction enters clarification after a certain period of time
Pond carries out clarification filtration, is formed except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
Step 2, it except ozone catalytic oxidation unit is entered as hard as filtering out water, stops after a certain period of time, forms ozone catalytic oxygen
Dissolve water；
Step 3, catalytic ozonation water outlet enters A/O/MBR units, respectively in A sections of anoxic, aerobic O sections and MBR membrane cisterna
It stops after a certain period of time, forms MBR and produce water；
Step 4, MBR, which produces water and enters high pressure reverse osmosis units, carries out separation concentration, forms high pressure reverse osmosis produced water and high pressure
Reverse osmosis concentrated water, high pressure reverse osmosis produced water reuse；
Step 5, high pressure reverse osmosis concentrated water enters MVR units evaporation and concentration, forms MVR mother liquors and MVR evaporation production water, MVR
Mother liquor carries out reinjection technology, MVR evaporation production water reuses.
Based on the above technical solution, in step 1, the main water quality characteristic of the gas field output water is：Inlet flow-patterm
7~8,10000~22000mg/L of total dissolved solid, 300~1500mg/L of suspended matter, 0~20mg/L of oil content, ammonia nitrogen 50
~200mg/L, total hardness (CaCO3Meter) 1500~3000mg/L, total alkalinity (CaCO3Meter) 550-950mg/L, Na+4000~
10000mg/L, Cl-5000~12000mg/L, SO4 2-800~1500mg/L, COD1500~3000mg/L.
Based on the above technical solution, through step 1~5 treated gas field output waters, oil content ＜ in MVR mother liquors
5mg/L, suspended matter ＜ 1mg/L meet gas field re-injection water quality standard；High pressure reverse osmosis produced water and MVR evaporation production water conductivities ＜
1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, total oil ＜ 0.5mg/L, meet circulating cooling make-up water
Reuse standard.
Based on the above technical solution, except the hard medicament that removes in hard filter element is sodium hydroxide described in step 1
And sodium carbonate, except the proportioning of hard medicament is sodium hydroxide：Sodium carbonate is 6~8:1, the medicament reaction time is 15~30min, except hard
PH controls are 10.8~11.5, and except the hard rear clarifying basin that enters filters, the residence time is 30min~90min.
Based on the above technical solution, in step 2, except as hard as filtering out before water enters ozone catalytic oxidation unit,
Pipeline dosing pump is set, and medicament is sodium hypochlorite；When except 50mg/L is higher than as hard as the ammonia-nitrogen content filtered out in water, time chlorine is added
Sour sodium, dosage is ammonia nitrogen in waste water and sodium hypochlorite mass ratio is 1：8~9.
Based on the above technical solution, the inlet flow-patterm of ozone catalytic oxidation unit described in step 2 is 7~8, is stopped
Time is 1~2h, ozone concentration 125-135mg/L；Ozone dosage is 800~1500mg/L.
Based on the above technical solution, A/O/MBR units described in step 3, the A sections of residence times of anoxic are 4~6h,
Aerobic O sections and MBR membrane cisterna 27~32h of total residence time, sludge reflux amount 300~400%, sludge volume 1~2%, sludge concentration
10~12g/L；
With this condition, the control of MBR membrane fluxs is in 10~12L/m2·h。
Based on the above technical solution, high pressure reverse osmosis units described in step 4 uses disc tube reverse osmosis (dt-ro) film group
Part, membrane module form are that multiple disc-type diaphragms are connected on composition disc-type film column on a central tube；High pressure reverse osmosis units
Service condition be：Operating pressure is 5~7MPa, and inlet flow-patterm is 7~10.
With this condition, the reverse osmosis membrane flux of high pressure is controlled in 7~10L/m2The TDS of h, high pressure reverse osmosis concentrated water is
40000~60000mg/L.
Based on the above technical solution, MVR units described in step 5 uses existing commercially available MVR evaporators, MVR female
The TDS controls of liquid are back to circulating cooling make-up water after 150000mg/L, MVR evaporations production water and the mixing of high pressure reverse osmosis produced water.
It is specific embodiment below.
Embodiment 1
The main water quality characteristic of certain gas field output water is：Inlet flow-patterm 7, total dissolved solid 10000mg/L, suspended matter
300mg/L, ammonia nitrogen 50mg/L, total hardness (CaCO3Meter) 1500mg/L, total alkalinity (CaCO3Meter) 550mg/L, Na+4000mg/L,
Cl-5000mg/L, SO4 2-800mg/L, COD 1500mg/L.
Processing step is as follows：
Step 1, gas field output water, which enters, removes hard filter element, except hard medicament is sodium hydroxide and sodium carbonate, removes hard medicament
Proportioning is sodium hydroxide：Sodium carbonate is 6:1, the medicament reaction time is 15min, except hard pH controls are 10.8, is entered after removing firmly clear
Clear pond precipitation filtering, residence time 30min are formed except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
With this condition, except as hard as the water hardness is filtered out less than 100mg/L, total oil is less than 1mg/L；
Step 2, except ozone catalytic oxidation unit is entered as hard as filtering out water, catalytic ozonation water outlet is formed；Inlet flow-patterm is
7, residence time 1h, ozone concentration 125mg/L；
With this condition, ozone dosage 800mg/L；COD in catalytic ozonation water outlet is about 700mg/L, ammonia
Nitrogen is about 47mg/L.
Step 3, catalytic ozonation water outlet enters A/O/MBR units, forms MBR and produces water.Wherein, when anoxic A sections of stops
Between be 4h, aerobic O sections and MBR membrane cisterna total residence time 27h, sludge reflux amount 300%, sludge volume 1%, sludge concentration 10g/L；
With this condition, the control of MBR membrane fluxs is in 10L/m2·h；MBR produces water COD about 210mg/L, ammonia nitrogen about 25mg/L.
Step 4, MBR, which produces water and enters high pressure reverse osmosis units, carries out separation concentration, forms high pressure reverse osmosis produced water and high pressure
Reverse osmosis concentrated water, high pressure reverse osmosis produced water reuse；High pressure reverse osmosis units use disc tube reverse osmosis (dt-ro) membrane module, membrane module form
It is connected on composition disc-type film column on a central tube for multiple disc-type diaphragms；The service condition of high pressure reverse osmosis units is：
Operating pressure is 5MPa, inlet flow-patterm 7；
With this condition, the reverse osmosis membrane flux of high pressure is controlled in 7L/m2The TDS of h, high pressure reverse osmosis concentrated water is
40000mg/L；High pressure reverse osmosis produced water conductivity ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜
10mg/L, total oil are less than 0.5mg/L, meet circulating cooling make-up water reuse standard.
Step 5, high pressure reverse osmosis concentrated water enters MVR units evaporation and concentration, forms MVR mother liquors and MVR evaporation production water.MVR
Unit uses existing commercially available MVR evaporators, and in 150000mg/L, MVR evaporation production water also meets cycle for the TDS controls of MVR mother liquors
It is back to circulating cooling make-up water after water moisturizing standard and the mixing of high pressure reverse osmosis produced water；
By above-mentioned steps treated gas field output water, oil content ＜ 5mg/L, suspended matter ＜ 1mg/L in MVR mother liquors,
Meet gas field re-injection water quality standard；1200 μ S/cm, the COD ＜ 60mg/ of conductivity ＜ of high pressure reverse osmosis produced water and MVR evaporation production water
L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, total oil ＜ 0.5mg/L, meet circulating cooling make-up water reuse standard.
Embodiment 2
The main water quality characteristic of certain gas field output water is：Inlet flow-patterm 7.5, total dissolved solid 16000mg/L, suspended matter
700mg/L, oil content 10mg/L, ammonia nitrogen 120mg/L, total hardness (CaCO3Meter) 2000mg/L, total alkalinity (CaCO3Meter) 720mg/
L, Na+7000mg/L, Cl-9000mg/L, SO4 2-1100mg/L, COD 2200mg/L.
Processing step is as follows：
Step 1, gas field output water, which enters, removes hard filter element, except hard medicament is sodium hydroxide and sodium carbonate, removes hard medicament
Proportioning is sodium hydroxide：Sodium carbonate is 7:1, the medicament reaction time is 20min, except hard pH controls are 11, enters clarification after removing firmly
Pond precipitation filtering, residence time 60min are formed except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
With this condition, except as hard as the water hardness is filtered out less than 100mg/L, total oil is less than 1mg/L, ammonia nitrogen 120mg/L.
Step 2, except as hard as filtering out before water enters ozone catalytic oxidation unit, pipeline dosing pump is arranged in pipeline, and time chlorine is added
Remaining a small amount of ammonia nitrogen in sour sodium removal waste water, dosage are except as hard as the ammonia nitrogen and sodium hypochlorite mass ratio 1 filtered out in water：9.Add
Water outlet enters ozone catalytic oxidation unit after medicine, forms catalytic ozonation water outlet；Inlet flow-patterm is 7.5, residence time 1.5h,
Ozone concentration is 130mg/L；
With this condition, ozone dosage 1200mg/L；COD in catalytic ozonation water outlet is about 910mg/L, ammonia
Nitrogen is about 32mg/L.
Step 3, catalytic ozonation water outlet enters A/O/MBR units, forms MBR and produces water.Wherein, when anoxic A sections of stops
Between be 5h, aerobic O sections and MBR membrane cisterna total residence time 30h, sludge reflux amount 350%, sludge volume 1.5%, sludge concentration 11g/
L；
With this condition, the control of MBR membrane fluxs is in 11L/m2·h；MBR produces water COD about 300mg/L, ammonia nitrogen about 9mg/L.
Step 4, MBR, which produces water and enters high pressure reverse osmosis units, carries out separation concentration, forms high pressure reverse osmosis produced water and high pressure
Reverse osmosis concentrated water, high pressure reverse osmosis produced water reuse；High pressure reverse osmosis units use disc tube reverse osmosis (dt-ro) membrane module, membrane module form
It is connected on composition disc-type film column on a central tube for multiple disc-type diaphragms；The service condition of high pressure reverse osmosis units is：
Operating pressure is 6MPa, inlet flow-patterm 10；
With this condition, the reverse osmosis membrane flux of high pressure is controlled in 9L/m2The TDS of h, high pressure reverse osmosis concentrated water is
50000mg/L；High pressure reverse osmosis produced water conductivity ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜
10mg/L, total oil are less than 0.5mg/L, meet circulating cooling make-up water reuse standard.
Step 5, high pressure reverse osmosis concentrated water enters MVR units evaporation and concentration, forms MVR mother liquors and MVR evaporation production water.MVR
Unit uses existing commercially available MVR evaporators, and in 150000mg/L, MVR evaporation production water also meets cycle for the TDS controls of MVR mother liquors
It is back to circulating cooling make-up water after water moisturizing standard and the mixing of high pressure reverse osmosis produced water；
By above-mentioned steps treated gas field output water, oil content ＜ 5mg/L, suspended matter ＜ 1mg/L in MVR mother liquors,
Meet gas field re-injection water quality standard；1200 μ S/cm, COD ＜ 60mg/L of high pressure reverse osmosis produced water and MVR evaporation production water conductivities ＜,
Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, total oil ＜ 0.5mg/L, meet circulating cooling make-up water reuse standard.
Embodiment 3
The main water quality characteristic of gas field output water is：Inlet flow-patterm 8, total dissolved solid 22000mg/L, suspended matter
1500mg/L, oil content 20mg/L, ammonia nitrogen 200mg/L, total hardness (CaCO3Meter) 3000mg/L, total alkalinity (CaCO3Meter)
950mg/L, Na+10000mg/L, Cl-12000mg/L, SO4 2-1500mg/L, COD 3000mg/L.
Processing step is as follows：
Step 1, gas field output water, which enters, removes hard filter element, except hard medicament is sodium hydroxide and sodium carbonate, removes hard medicament
Proportioning is sodium hydroxide：Sodium carbonate is 8:1, the medicament reaction time is 30min, except hard pH controls are 11.5, is entered after removing firmly clear
Clear pond precipitation filtering, residence time 90min are formed except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
With this condition, except as hard as the water hardness is filtered out less than 100mg/L, total oil is less than 1mg/L, ammonia nitrogen 200mg/L.
Step 2, except as hard as filtering out before water enters ozone catalytic oxidation unit, pipeline dosing pump is arranged in pipeline, and time chlorine is added
Remaining a small amount of ammonia nitrogen in sour sodium removal waste water, dosage are except as hard as the ammonia nitrogen and sodium hypochlorite mass ratio 1 filtered out in water：8.Add
Water outlet enters ozone catalytic oxidation unit after medicine, forms catalytic ozonation water outlet；Inlet flow-patterm is 8, residence time 2h, ozone
A concentration of 135mg/L；
With this condition, ozone dosage 1500mg/L；COD in catalytic ozonation water outlet is about 1050mg/L,
Ammonia nitrogen is about 62mg/L.
Step 3, catalytic ozonation water outlet enters A/O/MBR units, forms MBR and produces water.Wherein, when anoxic A sections of stops
Between be 6h, aerobic O sections and MBR membrane cisterna total residence time 32h, sludge reflux amount 400%, sludge volume 2%, sludge concentration 12g/L；
With this condition, the control of MBR membrane fluxs is in 12L/m2·h；MBR produces water COD about 470mg/L, ammonia nitrogen about 18mg/L.
Step 4, MBR, which produces water and enters high pressure reverse osmosis units, carries out separation concentration, forms high pressure reverse osmosis produced water and high pressure
Reverse osmosis concentrated water, high pressure reverse osmosis produced water reuse；High pressure reverse osmosis units use disc tube reverse osmosis (dt-ro) membrane module, membrane module form
It is connected on composition disc-type film column on a central tube for multiple disc-type diaphragms；The service condition of high pressure reverse osmosis units is：
Operating pressure is 7MPa, inlet flow-patterm 9；
With this condition, the reverse osmosis membrane flux of high pressure is controlled in 10L/m2The TDS of h, high pressure reverse osmosis concentrated water is
60000mg/L；High pressure reverse osmosis produced water conductivity ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜
10mg/L, total oil are less than 0.5mg/L, meet circulating cooling make-up water reuse standard.
Step 5, high pressure reverse osmosis concentrated water enters MVR units evaporation and concentration, forms MVR mother liquors and MVR evaporation production water.MVR
Unit uses existing commercially available MVR evaporators, and in 150000mg/L, MVR evaporation production water also meets cycle for the TDS controls of MVR mother liquors
It is back to circulating cooling make-up water after water moisturizing standard and the mixing of high pressure reverse osmosis produced water；
By above-mentioned steps treated gas field output water, oil content ＜ 5mg/L, suspended matter ＜ 1mg/L in MVR mother liquors,
Meet gas field re-injection water quality standard；1200 μ S/cm, COD ＜ 60mg/L of high pressure reverse osmosis produced water and MVR evaporation production water conductivities ＜,
Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, total oil ＜ 0.5mg/L, meet circulating cooling make-up water reuse standard.
The foregoing is merely the preferable possible embodiments of the present invention, not thereby limit to the scope of the claims of the present invention, therefore all
It is to be both contained in protection scope of the present invention with equivalence changes made by description of the invention and accompanying drawing content.
The content not being described in detail in this specification belongs to the prior art well known to professional and technical personnel in the field.
Claims (9)
1. a kind of recycling processing method of gas field output water, it is characterised in that：Include the following steps：
Step 1, gas field output water enter remove hard filter element, be added remove hard medicament, reaction after a certain period of time enter clarifying basin into
Row clarification filtration is formed except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
Step 2, it except ozone catalytic oxidation unit is entered as hard as filtering out water, stops after a certain period of time, forms catalytic ozonation and go out
Water；
Step 3, catalytic ozonation water outlet enters A/O/MBR units, is stopped respectively in A sections of anoxic, aerobic O sections and MBR membrane cisterna
After a certain period of time, it forms MBR and produces water；
Step 4, MBR, which produces water and enters high pressure reverse osmosis units, carries out separation concentration, forms high pressure reverse osmosis produced water and high pressure reverse osmosis
Saturating concentrated water, high pressure reverse osmosis produced water reuse；
Step 5, high pressure reverse osmosis concentrated water enters MVR units evaporation and concentration, forms MVR mother liquors and MVR evaporation production water, MVR mother liquors
Carry out reinjection technology, MVR evaporation production water reuses.
2. the recycling processing method of gas field output water according to claim 1, it is characterised in that：In step 1, the gas
The main water quality characteristic of field produced water is：Inlet flow-patterm 7~8,10000~22000mg/L of total dissolved solid, suspended matter 300~
1500mg/L, 0~20mg/L of oil content, 50~200mg/L of ammonia nitrogen, 1500~3000mg/L of total hardness, total alkalinity 550-
950mg/L, Na+4000~10000mg/L, Cl-5000~12000mg/L, SO4 2-800~1500mg/L, COD 1500~
3000mg/L。
3. the recycling processing method of gas field output water according to claim 1, it is characterised in that：Through step 1~5 processing
Gas field output water afterwards, in MVR mother liquors, oil content ＜ 5mg/L, suspended matter ＜ 1mg/L meet gas field re-injection water quality standard；High pressure
Reverse osmosis produced water and MVR evaporation production water conductivities ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/
L, total oil ＜ 0.5mg/L, meets circulating cooling make-up water reuse standard.
4. the recycling processing method of gas field output water according to claim 1, it is characterised in that：It is described to remove in step 1
The hard medicament that removes in hard filter element is sodium hydroxide and sodium carbonate, except the proportioning of hard medicament is sodium hydroxide：Sodium carbonate be 6~
8:1, the medicament reaction time is 15~30min, and entering clarifying basin except hard pH controls are 10.8~11.5, after removing firmly filters, stop
Time is 30min~90min.
5. the recycling processing method of gas field output water according to claim 1, it is characterised in that：In step 2, except hard
Before filtering water outlet enters ozone catalytic oxidation unit, pipeline dosing pump is set, and medicament is sodium hypochlorite；When except as hard as filtering out in water
Ammonia-nitrogen content when being higher than 50mg/L, sodium hypochlorite is added, dosage is ammonia nitrogen in waste water and sodium hypochlorite mass ratio is 1：8
~9.
6. the recycling processing method of gas field output water according to claim 5, it is characterised in that：It is smelly described in step 2
The inlet flow-patterm of oxygen catalytic oxidation unit is 7~8, and the residence time is 1~2h, ozone concentration 125-135mg/L；Ozone dosage
For 800~1500mg/L.
7. the recycling processing method of gas field output water according to claim 1, it is characterised in that：A/ described in step 3
O/MBR units, the A sections of residence times of anoxic are 4~6h, aerobic O sections and MBR membrane cisterna 27~32h of total residence time, sludge reflux amount
300~400%, sludge volume 1~2%, 10~12g/L of sludge concentration；
With this condition, the control of MBR membrane fluxs is in 10~12L/m2·h。
8. the recycling processing method of gas field output water according to claim 1, it is characterised in that：It is high described in step 4
It is that multiple disc-type diaphragms are connected on a central tube to press reverse osmosis units to use disc tube reverse osmosis (dt-ro) membrane module, membrane module form
Upper composition disc-type film column；The service condition of high pressure reverse osmosis units is：Operating pressure is 5~7MPa, and inlet flow-patterm is 7~10；
With this condition, the membrane flux of high pressure reverse osmosis units is controlled in 7~10L/m2H, the dissolubility of high pressure reverse osmosis concentrated water
Solid amount is 40000~60000mg/L.
9. the recycling processing method of gas field output water according to claim 1, it is characterised in that：MVR described in step 5
Unit uses MVR evaporators, and in 150000mg/L, MVR evaporations production water and high pressure are anti-for the dissolvability solid amount control of MVR mother liquors
It is back to circulating cooling make-up water after infiltration production water mixing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710179194.XA CN108623082A (en) | 2017-03-23 | 2017-03-23 | A kind of recycling processing method of gas field output water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710179194.XA CN108623082A (en) | 2017-03-23 | 2017-03-23 | A kind of recycling processing method of gas field output water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN108623082A true CN108623082A (en) | 2018-10-09 |
Family
ID=63707251
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710179194.XA Pending CN108623082A (en) | 2017-03-23 | 2017-03-23 | A kind of recycling processing method of gas field output water |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108623082A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109851162A (en) * | 2019-01-18 | 2019-06-07 | 中国石油工程建设有限公司 | A kind of oil gas field brine waste treatment process up to standard |
| CN112897763A (en) * | 2019-12-04 | 2021-06-04 | 中国石油天然气股份有限公司 | Gas field water treatment method and system |
| CN113149341A (en) * | 2021-03-25 | 2021-07-23 | 中化环境科技工程有限公司 | Advanced treatment method for high-salinity wastewater |
| CN113371895A (en) * | 2021-07-05 | 2021-09-10 | 中石化石油工程技术服务有限公司 | Process method and system for resourceful treatment of oil and gas field produced water |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101851046A (en) * | 2010-06-21 | 2010-10-06 | 吴静璇 | Device for deep treatment and complete recovery of coking wastewater and application method thereof |
| CN102372375A (en) * | 2010-08-27 | 2012-03-14 | 中国石油化工股份有限公司 | Advanced wastewater hardness removal method |
| CN102603092A (en) * | 2011-01-20 | 2012-07-25 | 四川仁智石化科技有限责任公司 | Treating method for desalting high-salt-content waste water in oil and gas field |
| CN103304104A (en) * | 2013-07-02 | 2013-09-18 | 中国石油集团工程设计有限责任公司 | Zero-sewage discharge novel process for development of natural gas fields |
| KR20150085990A (en) * | 2014-01-17 | 2015-07-27 | 코웨이 주식회사 | Water and wastewater treatment system and metho of the same |
| CN104876403A (en) * | 2015-06-11 | 2015-09-02 | 武汉钢铁(集团)公司 | Process and device for advanced treatment and reuse of coking wastewater |
| CN105906149A (en) * | 2016-06-02 | 2016-08-31 | 内蒙古君正氯碱化工技术研究院 | Chlor-alkali plant strong brine zero-discharge treatment system and treatment method |
-
2017
- 2017-03-23 CN CN201710179194.XA patent/CN108623082A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101851046A (en) * | 2010-06-21 | 2010-10-06 | 吴静璇 | Device for deep treatment and complete recovery of coking wastewater and application method thereof |
| CN102372375A (en) * | 2010-08-27 | 2012-03-14 | 中国石油化工股份有限公司 | Advanced wastewater hardness removal method |
| CN102603092A (en) * | 2011-01-20 | 2012-07-25 | 四川仁智石化科技有限责任公司 | Treating method for desalting high-salt-content waste water in oil and gas field |
| CN103304104A (en) * | 2013-07-02 | 2013-09-18 | 中国石油集团工程设计有限责任公司 | Zero-sewage discharge novel process for development of natural gas fields |
| KR20150085990A (en) * | 2014-01-17 | 2015-07-27 | 코웨이 주식회사 | Water and wastewater treatment system and metho of the same |
| CN104876403A (en) * | 2015-06-11 | 2015-09-02 | 武汉钢铁(集团)公司 | Process and device for advanced treatment and reuse of coking wastewater |
| CN105906149A (en) * | 2016-06-02 | 2016-08-31 | 内蒙古君正氯碱化工技术研究院 | Chlor-alkali plant strong brine zero-discharge treatment system and treatment method |
Non-Patent Citations (1)
| Title |
|---|
| 梁兵等: "蒸发结晶分离处理气田水技术在川东地区的应用前景展望", 《天然气勘探与开发》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109851162A (en) * | 2019-01-18 | 2019-06-07 | 中国石油工程建设有限公司 | A kind of oil gas field brine waste treatment process up to standard |
| CN112897763A (en) * | 2019-12-04 | 2021-06-04 | 中国石油天然气股份有限公司 | Gas field water treatment method and system |
| CN112897763B (en) * | 2019-12-04 | 2022-08-05 | 中国石油天然气股份有限公司 | Gas field water treatment method and system |
| CN113149341A (en) * | 2021-03-25 | 2021-07-23 | 中化环境科技工程有限公司 | Advanced treatment method for high-salinity wastewater |
| CN113371895A (en) * | 2021-07-05 | 2021-09-10 | 中石化石油工程技术服务有限公司 | Process method and system for resourceful treatment of oil and gas field produced water |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101979344B (en) | Nano catalytic electrolysis technology and membrane technology-based leather wastewater treatment and recycling method | |
| CN101857328B (en) | Spinning printing and dyeing waste water reclamation method, device and application thereof | |
| CN102452760B (en) | Treatment method for recycle of oil field produced water | |
| CN101462801B (en) | Steel composite wastewater recycle-water double-membrane demineralization system and technique | |
| CN102942279A (en) | Treatment method for circulating water sewerage and reverse osmosis concentrated water and equipment thereof | |
| CN102020392B (en) | Dyeing reclaimed water recycling process and equipment | |
| CN103922537B (en) | System for recycling wastewater from circulating cooling water by adopting membrane process | |
| CN108623082A (en) | A kind of recycling processing method of gas field output water | |
| CN103102049B (en) | High-nitrogen-concentration organic wastewater treatment method | |
| CN105016577A (en) | Advanced treatment system for process sewage and advanced treatment method for sewage | |
| CN106745981A (en) | A kind of system and method for high-salt wastewater treatment for reuse | |
| CN208814790U (en) | A kind of concentration strong brine softening of steel wastewater removes hard processing unit | |
| CN104030483A (en) | Treatment method for recycling power plant circulating water sewage | |
| CN107445377A (en) | A kind of biochemical waste water Zero-discharge treating process and processing system | |
| CN112047553A (en) | PTA high-salinity wastewater treatment, reuse and zero-discharge system and method | |
| CN109912068A (en) | Blowdown water purification circuit and purification process based on reverse osmosis deaslination processing | |
| CN108623083A (en) | A kind of advanced treatment and reclamation method of gas field output water | |
| CN108623084A (en) | A kind of advanced treatment and reclamation method of gas field output water | |
| CN202865053U (en) | Processing device for wastewater form circulating cooling water and reverse osmosis concentrated water | |
| CN108328836B (en) | Water inlet control system based on high-salt-content wastewater reduction process | |
| CN206437968U (en) | A kind of system of high-salt wastewater treatment for reuse | |
| CN206538318U (en) | A kind of device for handling the high organic wastewater of industrial high salt | |
| CN202576135U (en) | Device for producing drinking water through coal mine water | |
| CN106746130A (en) | A kind of high-salt concentrated water zero-discharge treatment system and process | |
| CN108623081A (en) | A kind of gas field output water reduces reuse method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |