CN108623066A - 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 PDF

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Publication number
CN108623066A
CN108623066A CN201710178632.0A CN201710178632A CN108623066A CN 108623066 A CN108623066 A CN 108623066A CN 201710178632 A CN201710178632 A CN 201710178632A CN 108623066 A CN108623066 A CN 108623066A
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China
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water
gas
reverse osmosis
mvr
hard
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CN201710178632.0A
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Chinese (zh)
Inventor
张新妙
彭海珠
郭智
张建华
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中国石油化工股份有限公司
中国石油化工股份有限公司北京化工研究院
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Priority to CN201710178632.0A priority Critical patent/CN108623066A/en
Publication of CN108623066A publication Critical patent/CN108623066A/en

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    • 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
    • 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
    • C02F1/78—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
    • 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
    • C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents

Abstract

The present invention relates to a kind of recycling processing methods of gas field output water.This method is using efficiently except as hard as the filter reverse osmosis MVR techniques of catalytic ozonation high pressure, 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.

Description

A kind of recycling processing method of gas field output water

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 efficiently except as hard as filter-catalytic ozonation-high pressure it is reverse osmosis-mechanical steam recompression (MVR) technical finesse gas field The recycling processing method of 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, and the stock is useless Water also contains a large amount of salt, organic matter, ammonia nitrogen and suspended matter etc. in addition to containing a large amount of hydrogen sulfide and sulfide.If cannot get It is effectively treated, serious pollution can be not only generated to environment, 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 the hardness efficiently except as hard as the reverse osmosis-MVR techniques of filter-catalytic ozonation-high pressure, effectively removed in waste water, Suspended matter, organic matter, salt and ammonia nitrogen solve hardness, suspended matter, organic matter, ammonia during the output water recycling treatment of gas field The excessively high problem of the indexs such as nitrogen and chloride effectively reduces waste water reinjection amount, realizes the recycling treatment of gas field output water.

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 efficiently except hard filterer Skill removes most of hardness and suspended matter in the output water of gas field；Second step, using catalytic ozonation removal except as hard as filtering out Most of organic matter in water；Third walks, using the concentration catalytic ozonation water outlet of high pressure reverse osmosis separation, by ozone catalytic oxygen Most of salt removing in water is dissolved, high pressure reverse osmosis produced water and high pressure reverse osmosis concentrated water are formed；4th step, using MVR works Skill further concentrates high pressure reverse osmosis concentrated water, forms MVR evaporations production water and MVR mother liquors.MVR mother liquors carry out reinjection technology, high Press reverse osmosis produced water and MVR evaporation production water reuses.

A kind of recycling processing method of gas field output water, specifically includes following steps：

Step 1, gas field output water, which enters, efficiently removes hard filter element, is added and removes hard medicament, reaction after a certain period of time, carries out Membrane filtration is formed efficiently except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；

Step 2, it efficiently stops after a certain period of time except ozone catalytic oxidation unit is entered as hard as filtering out water, forms ozone and urge Change oxidation water outlet；

Step 3, catalytic ozonation water outlet carries out separation concentration into high pressure reverse osmosis units, and it is reverse osmosis produced to form high pressure Water and high pressure reverse osmosis concentrated water；High pressure reverse osmosis produced water reuse；

Step 4, 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, the main water quality characteristic of the gas field output water is：Inlet flow-patterm 7~8, always 10000~22000mg/L of soluble solid, 300~1500mg/L of suspended matter, 0~20mg/L of oil content, 50~150mg/ of ammonia nitrogen L, total hardness (CaCO3Meter) 1500~3000mg/L, total alkalinity (CaCO3Meter) 550-950mg/L, Na+4000~10000mg/L, Cl-5000~12000mg/L, SO4 2-500~1200mg/L of 800~1500mg/L, COD.

Based on the above technical solution, through step 1~4 treated gas field output waters, oil contains in the MVR mother liquors ＜ 5mg/L are measured, 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 recirculated water benefit Water reuse standard.

Based on the above technical solution, the hard medicament that removes efficiently removed described in step 1 in hard filter element is hydrogen-oxygen Change sodium and sodium carbonate, except hard dosages distribution is sodium hydroxide：Sodium carbonate is 6~8:1, the medicament reaction time is 15~30min, is removed Hard pH controls carry out Gore membrane filtration 10.8~11.5, except firmly rear, and the membrane material of membrane filtration is polytetrafluoroethylene (PTFE), and membrane aperture is 0.15~0.25 μm；The membrane flux of membrane filtration is controlled in 150~250L/m2·h。

Based on the above technical solution, efficiently except as hard as filtering out before water enters ozone catalytic oxidation unit, setting Pipeline dosing pump, medicament are sodium hypochlorite, and when except 50mg/L is higher than as hard as the ammonia-nitrogen content filtered out in water, hypochlorous acid is added Sodium, dosing dosage are except being 1 as hard as the ammonia nitrogen and sodium hypochlorite mass ratio filtered out in water：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 600~1200mg/L.

Based on the above technical solution, high pressure reverse osmosis units described in step 3 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, the control of the membrane fluxs of high pressure reverse osmosis units 7~ 10L/m2H, TDS (dissolvability solid amount) is 40000~60000mg/L in high pressure reverse osmosis concentrated water.

Based on the above technical solution, MVR units described in step 4 uses existing commercially available MVR evaporators, MVR female Liquid TDS controls 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 efficiently except as hard as filter-catalytic ozonation- Reverse osmosis-MVR the techniques of high pressure effectively remove hardness, suspended matter, organic matter, salt and the ammonia nitrogen in waste water, solve gas field output The excessively high problem of the indexs such as hardness, suspended matter, organic matter, ammonia nitrogen, chloride, effectively reduces waste water in recycling of water resource processing procedure Re-injection 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 using high Effect is except as hard as filter-catalytic ozonation-high pressure 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, technical equipment of the present invention Simply, operation and maintenance are easy, operating cost substantially reduces, and Technical Economy is good.For gas field output water, money of the present invention Source treatment technology is more economical, reasonable, feasible.

Advantageous effect：

1, the present invention by gas field output water efficiently except the most of hardness as hard as filter, removed in the output water of gas field, Suspended matter and a small amount of organic matter, avoid the fouling of catalyst during follow-up catalytic ozonation, extend ozone catalytic oxygen Change the cleaning frequency of unit；

2, the present invention using gore film processing high suspended matter content waste water advantage, by using Ge Er organic membrane filters, Will remove as hard as filter it is integrated, eliminate intermediate clarifier, reduce occupation area of equipment, improve treatment effeciency, solve and remove The filtration problem of high suspended matter content water outlet after hard；

3, the present invention handles the waste water of high suspended matter content by using gore film, avoids using other forms membrane filtration High flow rate operational mode, reduce operating cost, and membrane flux is high, the cycle of operation is long；

4, the present invention is removed using catalytic ozonation removal as hard as the most of organic matter filtered out in water, reduces follow-up height Reverse osmosis processing load is pressed, ensure that the producing water water quality of follow-up reverse osmosis membrane system, extends the cleaning frequency of membranous system, is protected The operation steady in a long-term of membranous system is demonstrate,proved；

5, the process combination as hard as filter-reverse osmosis-MVR of catalytic ozonation-high pressure is efficiently removed in the present invention, is suitable for place Manage high rigidity, the gas field output water of low organic matter；

6, 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 gas field output to greatest extent The recycling of water.

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.

A kind of recycling processing method of gas field output water of the present invention, includes the following steps：The first step, using height Effect is except the most of hardness and suspended matter removed as hard as filtering technology in the output water of gas field；Second step is gone using catalytic ozonation Except except as hard as the most of organic matter filtered out in water；Third walks, and is discharged using high pressure reverse osmosis separation concentration catalytic ozonation, Most of salt removing during catalytic ozonation is discharged, forms high pressure reverse osmosis produced water and high pressure reverse osmosis concentrated water；4th Step, is further concentrated high pressure reverse osmosis concentrated water using MVR techniques, forms MVR evaporations production water and MVR mother liquors.MVR mother liquors carry out Reinjection technology, high pressure reverse osmosis produced water and MVR evaporation production water reuses.

A kind of recycling processing method of gas field output water, specifically includes following steps：

Step 1, gas field output water, which enters, efficiently removes hard filter element, is added and removes hard medicament, reaction after a certain period of time, carries out Membrane filtration is formed efficiently except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；

Step 2, it efficiently stops after a certain period of time except ozone catalytic oxidation unit is entered as hard as filtering out water, forms ozone and urge Change oxidation water outlet；

Step 3, catalytic ozonation water outlet carries out separation concentration into high pressure reverse osmosis units, and it is reverse osmosis produced to form high pressure Water and high pressure reverse osmosis concentrated water；High pressure reverse osmosis produced water reuse；

Step 4, 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, the main water quality characteristic of the gas field output water is：Inlet flow-patterm 7~8, always 10000~22000mg/L of soluble solid, 300~1500mg/L of suspended matter, 0~20mg/L of oil content, 50~150mg/ of ammonia nitrogen L, total hardness (CaCO3Meter) 1500~3000mg/L, total alkalinity (CaCO3Meter) 550-950mg/L, Na+4000~10000mg/L, Cl-5000~12000mg/L, SO4 2-500~1200mg/L of 800~1500mg/L, COD.

Based on the above technical solution, through step 1~4 treated gas field output waters, oil contains in the MVR mother liquors ＜ 5mg/L are measured, suspended matter ＜ 1mg/L meet gas field re-injection water quality standard；The conductance of high pressure reverse osmosis produced water and MVR evaporation production water Rate ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, total oil ＜ 0.5mg/L, meet recirculated water Moisturizing reuse standard.

Based on the above technical solution, the hard medicament that removes efficiently removed described in step 1 in hard filter element is hydrogen-oxygen Change sodium and sodium carbonate, except hard dosages distribution is sodium hydroxide：Sodium carbonate is 6~8:1, the medicament reaction time is 15~30min, is removed Hard pH controls carry out Gore membrane filtration 10.8~11.5, except firmly rear, and the membrane material of membrane filtration is polytetrafluoroethylene (PTFE), and membrane aperture is 0.15~0.25 μm；The membrane flux of membrane filtration is controlled in 150~250L/m2·h。

Based on the above technical solution, efficiently except as hard as filtering out before water enters ozone catalytic oxidation unit, setting Pipeline dosing pump, medicament are sodium hypochlorite, and when except 50mg/L is higher than as hard as the ammonia-nitrogen content filtered out in water, hypochlorous acid is added Sodium, dosing dosage are except being 1 as hard as the ammonia nitrogen and sodium hypochlorite mass ratio filtered out in water：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 600~1200mg/L.

Based on the above technical solution, high pressure reverse osmosis units described in step 3 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, the control of the membrane fluxs of high pressure reverse osmosis units 7~ 10L/m2H, TDS is 40000~60000mg/L in high pressure reverse osmosis concentrated water.

Based on the above technical solution, MVR units described in step 4 uses existing commercially available MVR evaporators, MVR female Liquid TDS controls 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 several specific embodiments 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 500mg/L.

Processing step is as follows：

Step 1, gas field output water, which enters, efficiently removes hard filter element, except hard medicament is sodium hydroxide and sodium carbonate, except hard Dosages distribution is sodium hydroxide：Sodium carbonate is 6:1, the medicament reaction time is 15min, except hard pH controls are 10.8, except hard laggard Row Gore membrane filtration, the membrane material of membrane filtration are polytetrafluoroethylene (PTFE), 0.15 μm of membrane aperture, are formed efficiently except as hard as filtering out water；Filter Outward transport processing is concentrated after slag class is cured.

With this condition, the membrane flux of membrane filtration is controlled in 250L/m2·h；What is formed after membrane filtration efficiently removes as hard as filter It is discharged SS and is less than 0.5mg/L, efficiently except as hard as the water hardness is filtered out less than 100mg/L, total oil is less than 1mg/L；

Step 2, efficiently catalytic ozonation water outlet is formed except ozone catalytic oxidation unit is entered as hard as filtering out water；Water inlet PH 7, residence time 1h, ozone concentration 125mg/L；

With this condition, ozone dosage 600mg/L；COD in catalytic ozonation water outlet is about 90mg/L, ammonia nitrogen About 47mg/L；

Step 3, catalytic ozonation water outlet carries out separation concentration into high pressure reverse osmosis units, and it is reverse osmosis produced to form high pressure 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, film Kit form is that multiple disc-type diaphragms are connected on composition disc-type film column on a central tube；The operation of high pressure reverse osmosis units Condition is：Operating pressure is 5MPa, inlet flow-patterm 7.

With this condition, the membrane flux of high pressure reverse osmosis units is controlled in 7L/m2H, high pressure reverse osmosis concentrated water TDS 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 4, 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, MVR mother liquors TDS controls also to meet recirculated water in 150000mg/L, MVR evaporation production water It is back to circulating cooling make-up water after moisturizing standard and the mixing of high pressure reverse osmosis produced water；

By oil content ＜ 5mg/L in above-mentioned steps treated MVR mother liquors, suspended matter ＜ 1mg/L meet gas field re-injection Water quality standard；MVR evaporation production water conductivities ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, always Oily ＜ 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 100mg/L, total hardness (CaCO3Meter) 2000mg/L, total alkalinity (CaCO3Meter) 720mg/ L, Na+7000mg/L, Cl-9000mg/L, SO4 2-1100mg/L, COD 800mg/L.

Processing step is as follows：

Step 1, gas field output water, which enters, efficiently removes hard filter element, except hard medicament is sodium hydroxide and sodium carbonate, except hard Dosages distribution is sodium hydroxide：Sodium carbonate is 7:1, the medicament reaction time is 20min, except hard pH controls are 11, is carried out after removing firmly Gore membrane filtration, the membrane material of membrane filter unit are polytetrafluoroethylene (PTFE), 0.2 μm of membrane aperture, are formed efficiently except as hard as filtering out water；Filter Outward transport processing is concentrated after slag class is cured.

With this condition, the membrane flux of membrane filtration is controlled in 200L/m2·h；What is formed after membrane filtration efficiently removes as hard as filter It is discharged SS and is less than 0.5mg/L, efficiently except as hard as the water hardness is filtered out less than 100mg/L, total oil is less than 1mg/L, ammonia nitrogen 100mg/L；

Step 2, efficiently except as hard as filtering out before water enters ozone catalytic oxidation unit, pipeline dosing pump is arranged in pipeline, is added Sodium hypochlorite removes remaining a small amount of ammonia nitrogen in waste water, and dosage is except as hard as the ammonia nitrogen and sodium hypochlorite mass ratio 1 filtered out in water： 8.Water outlet enters ozone catalytic oxidation unit after dosing, forms catalytic ozonation water outlet；Inlet flow-patterm 7.5, residence time be 1.5h, ozone concentration 130mg/L；

With this condition, ozone dosage 900mg/L；COD in catalytic ozonation water outlet is about 120mg/L, ammonia Nitrogen is about 23mg/L；

Step 3, catalytic ozonation water outlet carries out separation concentration into high pressure reverse osmosis units, and it is reverse osmosis produced to form high pressure 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, film Kit form is that multiple disc-type diaphragms are connected on composition disc-type film column on a central tube；The operation of high pressure reverse osmosis units Condition is：Operating pressure is 6MPa, inlet flow-patterm 10.

With this condition, the membrane flux of high pressure reverse osmosis units is controlled in 9L/m2H, high pressure reverse osmosis concentrated water TDS 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 4, 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, MVR mother liquors TDS controls also to meet recirculated water in 150000mg/L, MVR evaporation production water It is back to circulating cooling make-up water after moisturizing standard and the mixing of high pressure reverse osmosis produced water；

By oil content ＜ 5mg/L in above-mentioned steps treated MVR mother liquors, suspended matter ＜ 1mg/L meet gas field re-injection Water quality standard；MVR evaporation production water conductivities ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, always Oily ＜ 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 150mg/L, total hardness (CaCO3Meter) 3000mg/L, total alkalinity (CaCO3Meter) 950mg/L, Na+10000mg/L, Cl-12000mg/L, SO4 2-1500mg/L, COD 1200mg/L.

Processing step is as follows：

Step 1, gas field output water, which enters, efficiently removes hard filter element, except hard medicament is sodium hydroxide and sodium carbonate, except hard Dosages distribution is sodium hydroxide：Sodium carbonate is 8:1, the medicament reaction time is 30min, except hard pH controls are 11.5, except hard laggard Row Gore membrane filtration, the membrane material of membrane filter unit are polytetrafluoroethylene (PTFE), 0.25 μm of membrane aperture, are formed efficiently except as hard as filtering out Water；Outward transport processing is concentrated after filter residue class is cured.

With this condition, the membrane flux of membrane filtration is controlled in 150L/m2·h；What is formed after membrane filtration efficiently removes as hard as filter It is discharged SS and is less than 0.5mg/L, efficiently except as hard as the water hardness is filtered out less than 80mg/L, total oil is less than 1mg/L, ammonia nitrogen 150mg/L；

Step 2, efficiently except as hard as filtering out before water enters ozone catalytic oxidation unit, pipeline dosing pump is arranged in pipeline, is added Sodium hypochlorite removes remaining a small amount of ammonia nitrogen in waste water, and dosage is except as hard as the ammonia nitrogen and sodium hypochlorite mass ratio 1 filtered out in water： 9.Water outlet enters ozone catalytic oxidation unit after dosing, forms catalytic ozonation water outlet；Inlet flow-patterm 8, residence time 2h, Ozone concentration is 135mg/L；

With this condition, ozone dosage 1200mg/L；COD in catalytic ozonation water outlet is about 150mg/L, ammonia Nitrogen is about 25mg/L；

Step 3, catalytic ozonation water outlet carries out separation concentration into high pressure reverse osmosis units, and it is reverse osmosis produced to form high pressure 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, film Kit form is that multiple disc-type diaphragms are connected on composition disc-type film column on a central tube；The operation of high pressure reverse osmosis units Condition is：Operating pressure is 7MPa, inlet flow-patterm 9.

With this condition, the membrane flux of high pressure reverse osmosis units is controlled in 10L/m2H, high pressure reverse osmosis concentrated water TDS 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 4, 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, MVR mother liquors TDS controls also to meet recirculated water in 150000mg/L, MVR evaporation production water It is back to circulating cooling make-up water after moisturizing standard and the mixing of high pressure reverse osmosis produced water；

By oil content ＜ 5mg/L in above-mentioned steps treated MVR mother liquors, suspended matter ＜ 1mg/L meet gas field re-injection Water quality standard；MVR evaporation production water conductivities ＜ 1200 μ S/cm, COD ＜ 60mg/L, Cl-＜ 200mg/L, ammonia nitrogen ＜ 10mg/L, always Oily ＜ 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：Specifically include following steps：
Step 1, gas field output water, which enters, efficiently removes hard filter element, is added and removes hard medicament, reaction after a certain period of time, carries out film mistake Filter is formed efficiently except as hard as filtering out water；Outward transport processing is concentrated after filter residue class is cured；
Step 2, it efficiently stops after a certain period of time except ozone catalytic oxidation unit is entered as hard as filtering out water, forms ozone catalytic oxygen Dissolve water；
Step 3, catalytic ozonation water outlet enters high pressure reverse osmosis units and carries out separation concentration, formed high pressure reverse osmosis produced water with High pressure reverse osmosis concentrated water；High pressure reverse osmosis produced water reuse；
Step 4, 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 as described in claim 1, it is characterised in that：The master of the gas field output water The water quality characteristic is wanted to be：Inlet flow-patterm 7~8,10000~22000mg/L of total dissolved solid, 300~1500mg/L of suspended matter, oil 0~20mg/L of content, 50~150mg/L of ammonia nitrogen, 1500~3000mg/L of total hardness, total alkalinity 550-950mg/L, Na+ 4000 ~10000mg/L, Cl-5000~12000mg/L, SO4 2-500~1200mg/L of 800~1500mg/L, COD.
3. the recycling processing method of gas field output water as described in claim 1, it is characterised in that：Through step 1~4 treated Gas field output water, oil content ＜ 5mg/L in the MVR mother liquors, suspended matter ＜ 1mg/L meet gas field re-injection water quality standard；High pressure is anti- Infiltration production 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.
4. the recycling processing method of gas field output water as described in claim 1, it is characterised in that：It is efficiently removed described in step 1 The hard medicament that removes in hard filter element is sodium hydroxide and sodium carbonate, except hard dosages distribution is sodium hydroxide：Sodium carbonate is 6~8: 1, the medicament reaction time is 15~30min, and except hard pH controls are 10.8~11.5, Gore membrane filtration, membrane filtration are carried out after removing firmly Membrane material be polytetrafluoroethylene (PTFE), membrane aperture be 0.15~0.25 μm；The membrane flux of membrane filtration is controlled in 150~250L/m2· h。
5. the recycling processing method of gas field output water as described in claim 1, it is characterised in that：Efficiently except as hard as filtering out water Into before ozone catalytic oxidation unit, pipeline dosing pump is set, medicament is sodium hypochlorite, when except containing as hard as the ammonia nitrogen filtered out in water When amount is higher than 50mg/L, sodium hypochlorite is added, dosing dosage is except being as hard as the ammonia nitrogen and sodium hypochlorite mass ratio filtered out in water 1：8~9.
6. the recycling processing method of gas field output water as claimed in claim 5, it is characterised in that：Ozone described in step 2 is urged The inlet flow-patterm for changing oxidation unit is 7~8, and the residence time is 1~2h, ozone concentration 125-135mg/L；Ozone dosage is 600~1200mg/L.
7. the recycling processing method of gas field output water as described in claim 1, it is characterised in that：High pressure described in step 3 is anti- It is that multiple disc-type diaphragms are connected on structure on a central tube that permeation unit, which uses disc tube reverse osmosis (dt-ro) membrane module, membrane module form, At disc-type film column.
8. the recycling processing method of gas field output water as claimed in claim 7, it is characterised in that：The high pressure reverse osmosis units Service condition be：Operating pressure is 5~7MPa, and inlet flow-patterm is 7~10, the control of the membrane fluxs of high pressure reverse osmosis units 7~ 10L/m2H, the dissolvability solid amount in high pressure reverse osmosis concentrated water are 40000~60000mg/L.
9. the recycling processing method of gas field output water as described in claim 1, it is characterised in that：MVR units described in step 4 Using existing commercially available MVR evaporators, the dissolvability solid amount control of MVR mother liquors is in 150000mg/L, MVR evaporations production water and height It is back to circulating cooling make-up water after pressure reverse osmosis produced water mixing.
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