CN109867399B - Gas field wastewater desulfurization and desalination treatment system and method containing surfactant - Google Patents
Gas field wastewater desulfurization and desalination treatment system and method containing surfactant Download PDFInfo
- Publication number
- CN109867399B CN109867399B CN201711260181.1A CN201711260181A CN109867399B CN 109867399 B CN109867399 B CN 109867399B CN 201711260181 A CN201711260181 A CN 201711260181A CN 109867399 B CN109867399 B CN 109867399B
- Authority
- CN
- China
- Prior art keywords
- water outlet
- outlet
- treated water
- gas field
- separation
- 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
- 239000002351 wastewater Substances 0.000 title claims abstract description 81
- 239000004094 surface-active agent Substances 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 18
- 230000023556 desulfurization Effects 0.000 title claims abstract description 18
- 238000010612 desalination reaction Methods 0.000 title claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 190
- 239000007788 liquid Substances 0.000 claims abstract description 65
- 238000000926 separation method Methods 0.000 claims abstract description 58
- 238000001914 filtration Methods 0.000 claims abstract description 53
- 238000001179 sorption measurement Methods 0.000 claims abstract description 49
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 44
- 230000003647 oxidation Effects 0.000 claims abstract description 43
- 238000002425 crystallisation Methods 0.000 claims abstract description 34
- 230000008025 crystallization Effects 0.000 claims abstract description 34
- 238000005345 coagulation Methods 0.000 claims abstract description 29
- 230000015271 coagulation Effects 0.000 claims abstract description 29
- 150000003839 salts Chemical class 0.000 claims abstract description 20
- 239000007787 solid Substances 0.000 claims abstract description 14
- 239000012452 mother liquor Substances 0.000 claims abstract description 13
- 239000007789 gas Substances 0.000 claims description 82
- 238000001704 evaporation Methods 0.000 claims description 46
- 230000008020 evaporation Effects 0.000 claims description 44
- 239000010802 sludge Substances 0.000 claims description 40
- 238000005188 flotation Methods 0.000 claims description 32
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 30
- 238000003860 storage Methods 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 21
- 239000013078 crystal Substances 0.000 claims description 20
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical group [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 17
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 15
- 230000003197 catalytic effect Effects 0.000 claims description 14
- 238000004064 recycling Methods 0.000 claims description 13
- 239000000701 coagulant Substances 0.000 claims description 10
- 238000011033 desalting Methods 0.000 claims description 9
- 230000003009 desulfurizing effect Effects 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 6
- 239000008213 purified water Substances 0.000 claims description 6
- 239000012028 Fenton's reagent Substances 0.000 claims description 5
- 239000003463 adsorbent Substances 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 5
- 239000002455 scale inhibitor Substances 0.000 claims description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 4
- 238000005243 fluidization Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000012545 processing Methods 0.000 abstract description 6
- 230000002194 synthesizing effect Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 21
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 18
- 230000008569 process Effects 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 13
- 239000003345 natural gas Substances 0.000 description 9
- 239000000126 substance Substances 0.000 description 9
- 238000011161 development Methods 0.000 description 8
- 230000018109 developmental process Effects 0.000 description 8
- 239000012528 membrane Substances 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000010865 sewage Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 239000003344 environmental pollutant Substances 0.000 description 5
- 239000003672 gas field water Substances 0.000 description 5
- 150000002989 phenols Chemical class 0.000 description 5
- 231100000719 pollutant Toxicity 0.000 description 5
- 239000000498 cooling water Substances 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- 230000005484 gravity Effects 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 241000196324 Embryophyta Species 0.000 description 3
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 3
- 150000001298 alcohols Chemical class 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000007667 floating Methods 0.000 description 3
- 238000003973 irrigation Methods 0.000 description 3
- 230000002262 irrigation Effects 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000004659 sterilization and disinfection Methods 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 150000001299 aldehydes Chemical class 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 239000004088 foaming agent Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 239000003112 inhibitor Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000010413 mother solution Substances 0.000 description 2
- 230000033116 oxidation-reduction process Effects 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000011550 stock solution Substances 0.000 description 2
- 150000003568 thioethers Chemical class 0.000 description 2
- 231100000331 toxic Toxicity 0.000 description 2
- 230000002588 toxic effect Effects 0.000 description 2
- 241000251468 Actinopterygii Species 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 206010007269 Carcinogenicity Diseases 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 235000013162 Cocos nucifera Nutrition 0.000 description 1
- 244000060011 Cocos nucifera Species 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 206010019233 Headaches Diseases 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 206010028813 Nausea Diseases 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 206010043275 Teratogenicity Diseases 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 230000033558 biomineral tissue development Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 230000007670 carcinogenicity Effects 0.000 description 1
- 231100000260 carcinogenicity Toxicity 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 230000001684 chronic effect Effects 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000012217 deletion Methods 0.000 description 1
- 230000037430 deletion Effects 0.000 description 1
- 208000002173 dizziness Diseases 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 239000010408 film Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000008398 formation water Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003673 groundwater Substances 0.000 description 1
- 231100000869 headache Toxicity 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002484 inorganic compounds Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000003621 irrigation water Substances 0.000 description 1
- 239000004973 liquid crystal related substance Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000007726 management method Methods 0.000 description 1
- 239000013335 mesoporous material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000035772 mutation Effects 0.000 description 1
- 230000008693 nausea Effects 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000035515 penetration Effects 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 230000029553 photosynthesis Effects 0.000 description 1
- 238000010672 photosynthesis Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 235000015170 shellfish Nutrition 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 208000024891 symptom Diseases 0.000 description 1
- 231100000211 teratogenicity Toxicity 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 238000012384 transportation and delivery Methods 0.000 description 1
- 238000004148 unit process Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The utility model provides a gas field waste water desulfurization desalination processing system and method that contains surfactant, can be with the technique continuous treatment gas field waste water of synthesizing low energy consumption operation, including coagulation air supporting filtration pretreatment unit, mesoporous medium adsorption unit, evaporative crystallization unit and oxidation unit that connects gradually, evaporative crystallization unit includes heater, vapour-liquid separator, separation crystallizer and compressor, the heater has retrieval and utilization steam entry and eleventh processing water export, retrieval and utilization steam entry connection the compressed retrieval and utilization steam export of compressor, the compressor is connected the retrieval and utilization steam export of vapour-liquid separator, eleventh processing water export is connected the vapour-liquid separator, vapour-liquid separator has separation liquid export, first evaporative condensate export and mother liquor circulation entry, separation liquid export is connected the separation crystallizer, separation crystallizer has solid salt export and mother liquor circulation export, mother liquor circulation export is connected the mother liquor circulation entry.
Description
Technical Field
The invention relates to an advanced treatment technology of gas field produced water, namely gas field wastewater in natural gas field development, in particular to a surfactant-containing gas field wastewater desulfurization and desalination treatment system and method, which can continuously carry out omnibearing treatment on the gas field wastewater by a matched technology operated comprehensively with low energy consumption, are beneficial to environmental protection of a gas field development area and reduce or eliminate pollution of the gas field produced water to the environment.
Background
The gas field produced water is formation water produced to the surface along with the gas production operation. Because the pressure of the gas reservoir is continuously reduced during exploitation, underground water, crude oil and slurry gradually invade the gas reservoir and are extracted along with natural gas to form gas field produced water. The produced water of the gas field is gas field wastewater, and the wastewater point sources are dispersed due to the large number of gas well sites. The water yield of the produced water of the gas field increases along with the increase of the production time, and the composition of the water quality is complex and changeable due to different gas production regions. In general, the gas field wastewater has the characteristics of complex chemical components, high turbidity, high mineralization, high corrosiveness, oil-containing substances, high surfactant content, high COD concentration, poor biodegradability and the like, and simultaneously contains organic pollutants such as aldehydes, alcohols, phenols and the like, sulfides and heavy metal substances. Since field produced water is present and coexists with natural gas in the formation for a long period of time, many microorganisms and bacteria remain in the wastewater.
After the gas field produced water is discharged into the ground water body, a large amount of dissolved oxygen in the water can be consumed, so that the biochemical oxygen demand in the water body is increased sharply, the water body is blackened and odorized, and serious pollution is caused. The inventor finds that the gas field wastewater is wastewater with high surfactant content, and a large amount of foaming agents contained in the wastewater are difficult to degrade in the existing environment, have chronic toxic action and can cause long-term pollution to water bodies. Sulfide and heavy metal substances in gas field wastewater can increase the content of harmful metal elements in surface sediment, and have a certain toxic effect on organisms in water. The vast amount of suspended matters contained in the gas field wastewater easily cause turbidity of water bodies and influence photosynthesis of aquatic plants. The various petroleum hydrocarbons contained in the gas field wastewater are substances with carcinogenicity, mutation and teratogenicity, are difficult to degrade naturally after being discharged into water, can be enriched in aquatic animals and plants such as shellfish, fish, algae and the like, and cause harm to human bodies through food chains. Meanwhile, the gas field wastewater is high-chlorine wastewater, a large amount of chloride ions salinize soil, change the original physical and chemical properties of the soil and influence the growth environment of plants. The oil pollutants in the gas field wastewater such as phenol, benzene substances and the like can cause dizziness, nausea, headache and other symptoms, and have great influence on human health and serious harm. Along with the continuous expansion of the development scale of the natural gas and the gradual penetration of the development work of the natural gas, the water yield of the gas field produced water is gradually increased, and particularly, the large-scale application of various foaming agents, corrosion inhibitors, hydrate inhibitors, defoamers and other medicaments leads to the increasingly complex water quality composition of the gas field wastewater and the increasingly difficult treatment. Therefore, the natural gas enterprises provide a large amount of industrial raw materials and clean fuel and also bring serious environmental pollution problems. The inventors believe that if the gas field wastewater can be continuously treated in all directions by a complete technology which is operated with comprehensive low energy consumption, for example, desalination and desulfurization, disinfection and sterilization, degradation of organic matters, etc., waste can be turned into valuable, and the treated gas field wastewater becomes useful usable water, for example, the treated gas field wastewater can be reused as system circulating cooling water, other production water in the gas field, greening irrigation water, etc. In view of this, the present inventors have completed the present invention.
Disclosure of Invention
Aiming at the defects or shortcomings in the prior art, the invention provides a surfactant-containing gas field wastewater desulfurization and desalination treatment system and method, which can continuously carry out omnibearing treatment on the gas field wastewater by using a matched technology operated with comprehensive low energy consumption, are beneficial to environmental protection of a gas field development area and reduce or eliminate pollution of gas field produced water to the environment.
The technical scheme of the invention is as follows:
the utility model provides a gas field waste water desulfurization desalination processing system who contains surfactant, its characterized in that includes the coagulation air supporting filtration pretreatment unit, mesoporous medium adsorption unit, evaporative crystallization unit and the oxidation unit that connect gradually, coagulation air supporting filtration pretreatment unit has gas field waste water entry, the oxidation unit has the water purification delivery port, evaporative crystallization unit includes heater, vapour-liquid separator, separation crystallizer and compressor, the heater has retrieval and utilization steam entry and eleventh processing water export, retrieval and utilization steam entry connection the compressed retrieval and utilization steam export of compressor, the compressor is connected vapour-liquid separator's retrieval and utilization steam export, eleventh processing water export connection vapour-liquid separator, vapour-liquid separator has separation liquid export, first evaporative condensate outlet and mother liquor circulation entry, separation liquid export connection separation crystallizer has solid salt export and mother liquor circulation export, mother liquor circulation export connection mother liquor circulation entry.
The recycled steam is sucked into the compressor to be compressed to obtain the compressed recycled steam after pressurization and temperature rise, and the compressed recycled steam enters the heater through the recycled steam inlet to replace the initial steam when heating is started to form a recycled steam cycle, so that the initial steam is not needed.
The solid salt outlet is connected with a sludge storage tank.
The heater is connected with a tenth treated water outlet of the preheater, the preheater is connected with the first evaporation condensate water outlet, the preheater is provided with a second evaporation condensate water outlet, the second evaporation condensate water outlet is connected with the condenser, the condenser is connected with the condensate water tank through a condensate water outlet, and the condensate water tank is connected with the oxidation unit through a condensate water outlet.
The oxidation unit is an ozone catalytic oxidation unit.
The mesoporous medium adsorption unit comprises a precoated diatomite filter, an activated carbon adsorption filter and a second buffer tank, wherein the precoated diatomite filter is provided with a backwash water outlet and a seventh treated water outlet, the seventh treated water outlet is connected with the activated carbon adsorption filter, the activated carbon adsorption filter is provided with a backwash water outlet and an eighth treated water outlet, the eighth treated water outlet is connected with the second buffer tank, the second buffer tank is provided with a sludge outlet and a ninth treated water outlet, the ninth treated water outlet is connected with a preheater, a scale inhibitor adding device is arranged on a pipeline between the preheater and the ninth treated water outlet, and an ammonia nitrogen remover adding device is arranged on the preheater.
The coagulation air flotation filtering pretreatment unit comprises an oil separation tank, a storage tank, a first-stage air flotation device, a second-stage air flotation device, a first buffer tank and a multi-medium filter, wherein the oil separation tank is provided with a gas field wastewater inlet, a sludge outlet, a backwash water inlet and a first treated water outlet, the first treated water outlet is connected with the storage tank, the storage tank is provided with a sludge outlet and a second treated water outlet, the second treated water outlet is connected with the first-stage air flotation device, the first-stage air flotation device is provided with a sludge outlet and a third treated water outlet, the third treated water outlet is connected with the second-stage air flotation device, the second-stage air flotation device is provided with a sludge outlet and a fourth treated water outlet, the fourth treated water outlet is connected with the first buffer tank, the first buffer tank is provided with a sludge outlet and a fifth treated water outlet, the fifth treated water outlet is connected with the multi-medium filter, the multi-medium filter is provided with a backwash water outlet and a sixth treated water outlet, and the sixth treated water outlet is connected with the media adsorption unit.
The Fenton reagent adding device is arranged on a connecting pipeline of the second treated water outlet of the storage tank and the first-stage air flotation device, and the first-stage air flotation device is sequentially provided with an adsorbent adding device, a coagulant adding device and a coagulant aid adding device along the water flow direction.
A method for desulfurizing and desalting gas field wastewater containing a surfactant, comprising the step of treating the gas field wastewater containing the surfactant by: step 1 is coagulation air floatation filtering pretreatment, step 2 is mesoporous medium adsorption treatment, step 3 is evaporation crystallization treatment, step 4 is oxidation treatment, the oxidation treatment is ozone catalytic oxidation treatment, the evaporation crystallization treatment comprises preheating, heating, vapor-liquid separation, separation crystallization, condensation and compression pressurizing temperature rise of recycled steam, the recycled steam is formed in the vapor-liquid separation, the recycled steam is sucked into a compressor to be compressed to obtain compressed recycled steam after pressurizing and heating, and the compressed recycled steam enters a heater to replace the initial steam when heating is started to form recycling steam circulation, so that the initial steam is not needed; the waste water is subjected to vapor-liquid separation in a vapor-liquid separator, the precipitated crystal grains are suspended in liquid to perform fluidization movement, small crystal grains gradually rise, are discharged from the upper part along with the liquid, are sucked into a circulating pump through a pipeline, and enter a heater again to be heated and concentrated; the large crystals gradually sink, are discharged by a discharge pump and enter a separation crystallizer, the crystals are collected after centrifugal separation, namely solid salt, and the residual mother liquor is returned to a vapor-liquid separator for evaporation and crystallization; collecting condensate water generated in the vapor-liquid separator and entering a condensate water tank; condensed water in the condensed water tank is subjected to ozone catalytic oxidation treatment to become purified water.
The mesoporous medium adsorption treatment comprises precoated diatomite filtration treatment and activated carbon adsorption filtration treatment, and the coagulation air floatation filtration pretreatment adopts oil separation, air floatation and multi-medium filtration technology.
The invention has the following technical effects: the invention adopts the integration of four unit processes, namely coagulation air floatation filtration pretreatment, mesoporous medium adsorption filtration treatment, evaporation crystallization treatment and ozone catalytic oxidation treatment, so as to form a desulfurization and desalination deep comprehensive treatment process for the gas field wastewater containing the surfactant of the natural gas Tian Gao, and the process has the characteristics of good and stable treatment effect, simple and convenient operation, small occupied area of a MVR (mechanical vapor recompression) evaporator, small required space, low comprehensive energy consumption, low water treatment cost and the like.
The invention relates to a desulfurization and desalination treatment system and a desulfurization and desalination treatment method for gas field wastewater containing a surfactant, which can lead the effluent quality of the gas field wastewater after the whole course treatment to reach the first-level standard of the integrated wastewater discharge standard (GB 8978-1996), the design specification of industrial circulating cooling water treatment (GB 50050-2007) and the water quality standard of farm irrigation (GB 5084-2005). The water quality reaches the standard and can be recycled as system circulating cooling water, other production water in a gas field or greening and irrigation, the pollutants are separated out from the sewage in the form of crystalline salt, and the crystalline salt is subjected to landfill disposal or recycling.
The gas field wastewater enters a coagulation air floatation filtering pretreatment process unit through an oil separation tank, floating oil, partial suspended matters, partial organic matters and sulfides in the water are removed, the water enters a mesoporous medium adsorption filtration unit through lifting by a pump, the unit treatment water enters an evaporation crystallization unit through a feeding pump, the unit outlet condensed water enters a buffer tank through lifting by a pump and then enters an advanced oxidation unit through lifting by a pump, standard reaching water is reused as system circulating cooling water, other production water or greening and irrigation in the gas field, the pollutants are separated out from the sewage in the form of crystal salt, and the crystal salt is subjected to landfill treatment or recycling; the sludge generated by the coagulation air floatation filtering pretreatment unit and the evaporation crystallization unit is lifted to a sludge concentration tank through a pump, and after gravity concentration and mechanical dehydration, the dehydrated sludge is buried or incinerated.
The pretreatment process of the gas field wastewater adopts a coagulation air floatation filtering pretreatment process. The unit comprises an oil separation tank, a storage tank, a first-stage air floatation device, a second-stage air floatation device, a buffer tank and a multi-medium filter, and plays roles of homogenizing, removing oil, removing impurities, removing part of surfactant and removing sulfide. The unit oil has 90% of removal rate, 30% -50% of removal rate of COD (Chemical Oxygen Demand), 95% of removal rate of impurities, 25% -45% of removal rate of surfactant and 99.9% of removal rate of sulfur. The sludge generated by the unit is lifted to a sludge concentration tank through a pump, and after gravity concentration and mechanical dehydration, the dehydrated sludge is buried or incinerated.
The design for removing organic vapors such as high surfactant, phenols and the like in the gas field wastewater adopts a mesoporous medium adsorption filtration unit. The mesoporous medium adsorption unit consists of two adsorption devices, namely a precoated film diatomite adsorption filter and a coconut shell activated carbon adsorption filter. The COD removal rate of the unit is 60% -80% and the surfactant removal rate is 90%.
Desalination in gas field wastewater uses MVR (mechanical vapor recompression) evaporative crystallization techniques. The technology is that gas field wastewater treated by a mesoporous medium adsorption unit is conveyed to a preheater by a feed pump to be preheated and then enters a heater, a tube side exchanges heat with heating steam and then enters a vapor-liquid separator to be separated and evaporated, secondary steam obtained by separation is forcedly sucked into a heat pump compression device by a secondary steam pipeline at the top of a secondary separator, and the secondary steam is compressed, pressure and temperature rise, enthalpy increase and reenter the heater to heat the gas field wastewater. The whole set of device is evaporated at low temperature under the negative pressure condition. And (3) conveying the brine wastewater crystal slurry precipitated at the bottom of the liquid crystal separator to a crystallization separator, centrifuging, collecting and discharging separated solid salt, and enabling the centrifuged mother solution to enter an evaporation crystallization system again for evaporation crystallization concentration. The non-condensable gas in the surface condenser is separated in the form of water vapor, and is discharged into the atmosphere after being pumped out by a vacuum pump. The evaporated condensed water is collected and then enters the advanced oxidation unit.
The organic matters difficult to degrade in the wastewater are designed to adopt an advanced oxidation unit. The unit adopts an ozone catalytic oxidation advanced oxidation technology, and utilizes the oxidation-reduction potential of the OH free radical generated by ozone decomposition and the oxidation-reduction reaction which is non-selective to organic matters to remove COD.
Under the conditions that the national and environmental protection departments are gradually standardized for the water quality standard and management of the gas field water and the requirements are more and more stringent, a new technology for treating the gas field water is urgently needed to be explored and sustainable development is realized, and therefore, the invention provides a complete and effective series of technical solutions, namely a system and a method for desulfurizing and desalting the gas field wastewater containing the surfactant.
Drawings
FIG. 1 is a schematic diagram of a desulfurizing and desalting treatment system for gas field wastewater containing a surfactant, which is used for implementing the invention.
The reference numerals are listed below: 1-a gas field wastewater inlet; 2-an oil separation tank; 3-a first treated water outlet; 4-a sludge outlet; 5-backwash water inlet; 6-adjusting a storage tank; 7-a second treated water outlet; 8-Fenton reagent adding device (an oxidation system formed by hydrogen peroxide and a catalyst Fe2+ is commonly called as Fenton reagent); 9-an adsorbent adding device; 10-coagulant adding device; 11-coagulant aid adding device; 12-a first-stage air floatation device; 13-a third treated water outlet; 14-a second-stage air floatation device; 15-a fourth treated water outlet; 16-a first buffer tank; 17-a fifth treated water outlet; 18-a multi-media filter; 19-backwash water outlet; 20-a sixth treated water outlet; 21-a coagulation air floatation filtering pretreatment unit; 22-mesoporous medium adsorption units; 23-precoating a membrane diatomite filter; 24-seventh treated water outlet; 25-activated carbon adsorption filter; 26-eighth treated water outlet; 27-a second buffer tank; 28-a ninth treated water outlet; 29-an evaporative crystallization unit; 30-a scale inhibitor adding device; 31-a preheater; 32-ammonia nitrogen remover adding device; 33-a second evaporative condensate outlet; 34-tenth treated water outlet; 35-a heater; 36-a recycle steam inlet; 37-eleventh treated water outlet; 38-a vapor-liquid separator; 39-a first evaporative condensate outlet; 40-mother liquor circulation inlet; 41-a recycled steam outlet; 42-a separated liquid outlet; 43-separation crystallizer; 44-mother liquor circulation outlet; 45-a solid salt outlet; 46-a compressor; 47-compressed recycle steam outlet; 48-a condenser; 49-condensed water outlet; 50-a condensate water tank; 51-a condensate outlet; a 52-oxidation unit; 53-a purified water outlet; 54-a sludge storage tank.
Detailed Description
The invention is described below with reference to the accompanying drawings (fig. 1) and examples.
FIG. 1 is a schematic diagram of a desulfurizing and desalting treatment system for gas field wastewater containing a surfactant, which is used for implementing the invention. As shown in fig. 1, the gas field wastewater desulfurization and desalination treatment system containing a surfactant comprises a coagulation air flotation filtration pretreatment unit 21, a mesoporous medium adsorption unit 22, an evaporation crystallization unit 29 and an oxidation unit 52 which are sequentially connected, wherein the coagulation air flotation filtration pretreatment unit 21 is provided with a gas field wastewater inlet 1, the oxidation unit 52 is provided with a purified water outlet 53, the evaporation crystallization unit 29 comprises a heater 35, a vapor-liquid separator 38, a separation crystallizer 43 and a compressor 46, the heater 35 is provided with a recycling vapor inlet 36 and an eleventh treated water outlet 37, the recycling vapor inlet 36 is connected with a vapor outlet 47 for compression retraction of the compressor 46, the compressor 46 is connected with a recycling vapor outlet 41 of the vapor-liquid separator 38, the tenth treated water outlet 37 is connected with the vapor-liquid separator 38, the vapor-liquid separator 38 is provided with a separation liquid outlet 42, a first evaporation condensed water outlet 39 and a mother liquid circulation inlet 40, the separation liquid outlet 42 is connected with the separation crystallizer 43, the separation crystallizer 43 is provided with a solid salt outlet 45 and a circulation liquid outlet 44, and the mother liquid circulation outlet 44 is connected with the mother liquid circulation inlet 40. The recycle steam is drawn into the compressor 46 to be compressed to achieve pressurization and warming to form the compressed recycle steam, and the compressed recycle steam enters the heater 35 through the recycle steam inlet 36 to replace the initial steam when heating is started to form a recycle steam cycle, so that the initial steam is not needed. The solid salt outlet 45 is connected with a sludge storage tank 54.
The heater 35 is connected to the tenth treated water outlet 34 of the preheater 31, the preheater 31 is connected to the first evaporation condensate outlet 39, the preheater 31 has a second evaporation condensate outlet 33, the second evaporation condensate outlet 33 is connected to a condenser 48, the condenser 48 is connected to a condensate tank 50 through a condensate outlet 49, and the condensate tank 50 is connected to an oxidation unit 52 through a condensate outlet 51. The oxidation unit 52 is an ozone catalytic oxidation unit. The mesoporous medium adsorption unit 22 comprises a precoated diatomite filter 23, an activated carbon adsorption filter 25 and a second buffer tank 27, wherein the precoated diatomite filter 23 is provided with a backwash water outlet 19 and a seventh treated water outlet 24, the seventh treated water outlet 24 is connected with the activated carbon adsorption filter 25, the activated carbon adsorption filter 25 is provided with a backwash water outlet 19 and an eighth treated water outlet 26, the eighth treated water outlet 26 is connected with the second buffer tank 27, the second buffer tank 27 is provided with a sludge outlet 4 and a ninth treated water outlet 28, the ninth treated water outlet 28 is connected with a preheater 31, a scale inhibitor adding device 30 is arranged on a pipeline between the preheater 31 and the ninth treated water outlet 28, an ammonia nitrogen remover adding device 32 is arranged on the preheater 31, and the sludge outlet 4 of the second buffer tank 27 is connected with a sludge storage tank 54.
The coagulation air flotation filtration pretreatment unit 21 comprises an oil separation tank 2, a storage tank 6, a first-stage air flotation device 12, a second-stage air flotation device 14, a first buffer tank 16 and a multi-medium filter 18, wherein the oil separation tank 2 is provided with a gas field wastewater inlet 1, a sludge outlet 4, a backwash water inlet 5 and a first treated water outlet 3, the first treated water outlet 3 is connected with the storage tank 6, the storage tank 6 is provided with the sludge outlet 4 and a second treated water outlet 7, the second treated water outlet 7 is connected with the first-stage air flotation device 12, the first-stage air flotation device 12 is provided with the sludge outlet 4 and a third treated water outlet 13, the third treated water outlet 13 is connected with the second-stage air flotation device 14, the second-stage air flotation device 14 is provided with the sludge outlet 4 and a fourth treated water outlet 15, the fourth treated water outlet 15 is connected with the first buffer tank 16, the first buffer tank 16 is provided with the sludge outlet 4 and a fifth treated water outlet 17, the fifth treated water outlet 17 is connected with the multi-medium filter 18, and the multi-medium filter 20 is connected with the multi-medium filter 19. The Fenton reagent adding device 8 is arranged on a connecting pipeline between the second treated water outlet 7 of the storage tank 6 and the first-stage air floatation device 12, and the first-stage air floatation device 12 is sequentially provided with an adsorbent adding device 9, a coagulant adding device 10 and a coagulant aid adding device 11 along the water flow direction.
A method for desulfurizing and desalting gas field wastewater containing a surfactant, comprising the steps of treating the gas field wastewater containing the surfactant by: step 1 is coagulation air floatation filtering pretreatment, step 2 is mesoporous medium adsorption treatment, step 3 is evaporation crystallization treatment, step 4 is oxidation treatment, the oxidation treatment is ozone catalytic oxidation treatment, the evaporation crystallization treatment comprises preheating, heating, vapor-liquid separation, separation crystallization, condensation and compression pressurization heating of recycled steam, the recycled steam is formed in the vapor-liquid separation, the recycled steam is sucked into a compressor to be compressed to obtain compressed recycled steam after pressurization and heating, and the compressed recycled steam enters a heater to replace initial steam when heating is started to form recycling steam circulation, so that the initial steam is not needed; the waste water is subjected to vapor-liquid separation in a vapor-liquid separator, precipitated crystal grains are suspended in liquid to perform fluidization movement, small crystal grains gradually rise, are discharged from the upper part along with the liquid, are sucked into a circulating pump through a pipeline, and enter a heater again to be heated and concentrated; large crystals gradually sink, are discharged by a discharge pump and enter a separation crystallizer, the crystals are collected after centrifugal separation, namely solid salt, and the residual mother liquor returns to a vapor-liquid separator again for evaporation crystallization; the condensate water generated in the vapor-liquid separator is collected and enters a condensate water tank; condensed water in the condensed water tank is subjected to ozone catalytic oxidation treatment to become purified water. The mesoporous medium adsorption treatment comprises precoated diatomite filtration treatment and activated carbon adsorption filtration treatment, and the coagulation air floatation filtration pretreatment adopts oil separation, air floatation and multi-medium filtration technology.
The technical scheme adopted for solving the problems is a deep treatment process for desulfurizing and desalting gas field wastewater with high surfactant in natural gas field development, comprising the following steps: the gas field water sequentially enters a coagulation air floatation filtering pretreatment unit, a mesoporous medium adsorption unit, an evaporation unit and a high-grade oxidation unit.
(1) Coagulation air floatation filtering pretreatment unit: the pretreatment process adopts a coagulation air floatation filtration pretreatment process. Specifically, a process of 'storage adjustment buffering + secondary air floatation + primary fine filtration' is adopted. The oil removal rate in the gas field wastewater passing through the unit is 90%, the COD removal rate is 30% -50%, the impurity removal rate is 95%, the surfactant removal rate is 25% -45%, and the desulfurization rate is 99.9%. The sludge generated by the unit is lifted to a sludge concentration tank through a pump, and after gravity concentration and mechanical dehydration, the dehydrated sludge is buried or incinerated. The backwash water enters an oil separation tank.
(2) Mesoporous media adsorption filtration unit: the process adopts a mesoporous medium adsorption filter unit for removing organic vapors such as high surfactants, phenols, alcohols and the like in the gas field wastewater. The effluent of the coagulation air-float filtering pretreatment unit is lifted by a pump to enter a mesoporous medium adsorption filtration unit, a large amount of surfactant and organic steam such as phenols, alcohols and the like in the water are removed, the removal rate of the surfactant is 90 percent, and the COD removal rate is 60 to 80 percent
(3) An evaporation unit: the process adopts MVR evaporation crystallization technology to remove high salt from gas field wastewater with high surfactant content. The outlet water of the mesoporous medium adsorption filtration unit is pumped into the evaporation crystallization unit by a feed pump, condensed water at the outlet of the unit is lifted into a condensed water tank by the pump, pollutants are separated out from sewage in the form of crystalline salt, and the crystalline salt is subjected to landfill treatment or recycling.
(4) Advanced oxidation unit: the ozone catalytic oxidation advanced oxidation technology is adopted for the organic matters which are difficult to degrade in the gas field water. The condensed water at the outlet of the evaporation unit is lifted by a pump and enters the ozone catalytic oxidation advanced oxidation unit. The ozone catalytic oxidation has good rapid sterilization and disinfection properties, and has extremely high capability of oxidizing organic and inorganic compounds, removing organic matters which are difficult to degrade in water, and reducing COD.
A deep treatment process for desulfurizing and desalting gas field wastewater with high surfactant content for natural gas field development comprises the following specific steps:
step one, coagulation air floatation filtration: the gas field wastewater enters a storage tank through an oil separation tank, natural static settlement is carried out to remove floating oil, partial suspended matters and partial organic matters in the water, the effect of homogenizing the water is achieved at the same time, then a Fonton reagent is added into the wastewater, then an adsorbent, a coagulant and a coagulant aid are sequentially added into the wastewater, the wastewater is sequentially lifted into primary air flotation equipment and secondary air flotation equipment, the air flotation water enters a buffer tank, and then the wastewater is lifted into a multi-medium filter to remove floating oil, fine suspended matters, colloid, partial surfactant and sulfide in the water. The backwash water of the filter enters the oil separation tank. Sludge in the storage tank, scum of the secondary air floatation and sludge are collected in a sludge concentration tank, and after gravity concentration and mechanical dehydration, the dehydrated sludge is buried or incinerated. Air floatation working principle: the air can be dissolved in water under a certain pressure and is in a saturated state, then the pressure in the water is suddenly reduced, and the dissolved air is separated out from the water in the form of tiny bubbles, so that the dissolved air is adhered to solid particles with the particle diameter close to that of the water in the sewage, and the aim of removing impurities in the water is fulfilled.
Step two, mesoporous medium adsorption filtration: the process designs and adopts mesoporous medium adsorption filtration process to organic matters such as surfactant, phenols, aldehydes and the like remained in the gas field wastewater subjected to coagulation air floatation filtration pretreatment. The design principle of the unit mainly depends on the highly developed microporous structure of mesoporous materials and the large specific surface area to adsorb surface activity and organic substances so as to achieve the purpose of removing. Working principle of precoated diatomite filter: firstly, a layer of diatomite filter membrane is coated on the surface of the filter element, and the purposes of controlling oil and suspended matters are further achieved by utilizing the adsorption and interception performances of the filter membrane. The filtration pressure difference is increased along with the continuous increase of the pollutant adsorption and interception amount of the filter membrane, when the filtration pressure difference is larger than 1.5bar, the diatomite filter membrane is reversely blown down from the filter core by utilizing the reverse air explosion effect of compressed air, then the filter core is backwashed by purified sewage, and then the filter core is coated with the filter membrane for repeated use. The diatomite has the particle size of 200 mesh and the adding amount of 0.8Kg per square meter, and forms a filter membrane which filters sewage at the filtering speed of 3-5 m/h.
Step three, evaporating and crystallizing: desalting of the high-salt-content gas field wastewater adopts an MVR evaporation crystallization process. The evaporation temperature was 90℃and the compressor temperature was 16 ℃. MVR evaporation crystallization principle: the material is circulated in a falling film evaporator through a material circulating pump in a heating pipe. The primary steam is heated by fresh steam outside the pipe, the solution is heated and boiled to generate secondary steam, the generated secondary steam is sucked by a turbo-charging fan, the temperature of the secondary steam is increased after being pressurized, and the secondary steam is taken as a heating source to enter a heating chamber for circular evaporation. The MVR evaporation crystallization technology adopts electric energy to heat instead of steam, and has low power consumption, secondary steam generated by evaporation is compressed and fully utilized, the steam has almost no loss in the system, the output heat energy of each concentrated solution of condensed water is subjected to heat exchange with the stock solution, noncondensable gas is subjected to heat exchange with the stock solution, and the compressor motor adopts rotational speed frequency conversion control, so that the device has the characteristics of compact evaporation equipment, small occupied area, small required space and low energy consumption. The specific working mode is as follows: the evaporating device consists of a preheating device, a heating device, a vapor-liquid separator, a separation crystallizer and a condenser. Adding a scale inhibitor and an ammonia nitrogen remover into the wastewater treated by the mesoporous medium adsorption filtration unit in sequence, preheating, then entering a heater, performing heat exchange with steam at a specific flow rate under the action of a pump, performing vapor-liquid separation on the wastewater in a vapor-liquid separator, suspending precipitated crystal grains in liquid for fluidization movement, gradually rising small crystal grains, discharging the small crystal grains from the upper part along with the liquid, sucking the small crystal grains into a circulating pump through a pipeline, and performing heating concentration again entering the heater; the large crystals gradually sink, are discharged by a discharge pump and enter a separation crystallizer, most of crystal-solid salt is collected after centrifugal separation, and a small amount of mother solution is generated and returned to an evaporation system for evaporation crystallization; the generated steam is sucked by the turbine compressor, pressurized to raise the temperature and then enters the heater as a heating source for circular evaporation. The generated condensed water is collected into a condensed water tank.
Step four: advanced oxidation: the technology adopts heterogeneous ozone to catalyze, oxidize and degrade refractory organic matters. Activated carbon is used as a carrier to load transition metal and oxides thereof, ozone generates OH under the action of a catalyst, oxidation-reduction electric potential is up to 2.80V, OH free radical is used as a secondary oxidant to enable organic matters to be rapidly oxidized and decomposed into CO 2 And H 2 O and other nontoxic small molecular acids, thereby reducing the COD of the gas field water and the COD of the effluent water by 20-40 mg/L.
It is noted that the above description is helpful for a person skilled in the art to understand the present invention, but does not limit the scope of the present invention. Any and all such equivalent substitutions, modifications and/or deletions as may be made without departing from the spirit and scope of the invention.
Claims (5)
1. The gas field wastewater desulfurization and desalination treatment system containing the surfactant is characterized by comprising a coagulation air flotation filtration pretreatment unit, a mesoporous medium adsorption unit, an evaporation crystallization unit and an oxidation unit which are sequentially connected, wherein the coagulation air flotation filtration pretreatment unit is provided with a gas field wastewater inlet, the oxidation unit is provided with a purified water outlet, the evaporation crystallization unit comprises a heater, a vapor-liquid separator, a separation crystallizer and a compressor, the heater is provided with a recycling steam inlet and an eleventh treated water outlet, the recycling steam inlet is connected with a compressed recycling steam outlet of the compressor, the compressor is connected with a recycling steam outlet of the vapor-liquid separator, the eleventh treated water outlet is connected with the vapor-liquid separator, the vapor-liquid separator is provided with a separation liquid outlet, a first evaporation condensate outlet and a mother liquid circulation inlet, the separation liquid outlet is connected with the separation crystallizer, the separation crystallizer is provided with a solid salt outlet and a mother liquid circulation outlet, and the mother liquid circulation outlet is connected with the mother liquid circulation inlet;
the recycled steam of the vapor-liquid separator is sucked into the compressor to be compressed to obtain compressed recycled steam after pressurization and temperature rise, and the compressed recycled steam enters the heater through the recycled steam inlet to replace the initial steam when heating is started to form a recycled steam cycle, so that the initial steam is not needed;
the heater is connected with a tenth treated water outlet of the preheater, the preheater is connected with the first evaporation condensate water outlet, the preheater is provided with a second evaporation condensate water outlet, the second evaporation condensate water outlet is connected with the condenser, the condenser is connected with the condensate water tank through a condensate water outlet, and the condensate water tank is connected with the oxidation unit through a condensate water outlet;
the mesoporous medium adsorption unit comprises a precoated diatomite filter, an activated carbon adsorption filter and a second buffer tank, wherein the precoated diatomite filter is provided with a backwash water outlet and a seventh treated water outlet, the seventh treated water outlet is connected with the activated carbon adsorption filter, the activated carbon adsorption filter is provided with a backwash water outlet and an eighth treated water outlet, the eighth treated water outlet is connected with the second buffer tank, the second buffer tank is provided with a sludge outlet and a ninth treated water outlet, the ninth treated water outlet is connected with a preheater, a scale inhibitor adding device is arranged on a pipeline between the preheater and the ninth treated water outlet, an ammonia nitrogen remover adding device is arranged on the preheater, and the sludge outlet of the second buffer tank is connected with a sludge storage tank;
the coagulation air flotation filtering pretreatment unit comprises an oil separation tank, a storage tank, a first-stage air flotation device, a second-stage air flotation device, a first buffer tank and a multi-medium filter, wherein the oil separation tank is provided with a gas field wastewater inlet, a sludge outlet, a backwash water inlet and a first treated water outlet, the first treated water outlet is connected with the storage tank, the storage tank is provided with a sludge outlet and a second treated water outlet, the second treated water outlet is connected with the first-stage air flotation device, the first-stage air flotation device is provided with a sludge outlet and a third treated water outlet, the third treated water outlet is connected with the second-stage air flotation device, the second-stage air flotation device is provided with a sludge outlet and a fourth treated water outlet, the fourth treated water outlet is connected with the first buffer tank, the first buffer tank is provided with a sludge outlet and a fifth treated water outlet, the fifth treated water outlet is connected with the multi-medium filter, the multi-medium filter is provided with a backwash water outlet and a sixth treated water outlet, and the sixth treated water outlet is connected with the medium adsorption unit;
the gas field wastewater after the coagulation air floatation filtering pretreatment unit has 90% of oil removal rate, 30% -50% of COD removal rate, 95% of impurity removal rate, 25% -45% of surfactant removal rate and 99.9% of desulfurization rate;
the removal rate of the surfactant in the gas field wastewater after passing through the mesoporous medium adsorption and filtration unit is 90 percent, and the COD removal rate is 60-80 percent.
2. The surfactant-containing gas field wastewater desulfurization and desalination treatment system of claim 1, wherein the solid salt outlet is connected to a sludge storage tank.
3. The surfactant-containing gas field wastewater desulfurization desalination treatment system of claim 1, wherein the oxidation unit is an ozone catalytic oxidation unit.
4. The desulfurization and desalination treatment system for gas field wastewater containing a surfactant according to claim 1, wherein a Fenton reagent adding device is arranged on a connecting pipeline between a second treated water outlet of the storage tank and the first-stage air flotation device, and an adsorbent adding device, a coagulant adding device and a coagulant aid adding device are sequentially arranged on the first-stage air flotation device along the water flow direction.
5. A method for desulfurizing and desalting gas field wastewater containing a surfactant, comprising the step of treating the gas field wastewater containing the surfactant by: step 1 is coagulation air floatation filtering pretreatment, step 2 is mesoporous medium adsorption treatment, step 3 is evaporation crystallization treatment, step 4 is oxidation treatment, the oxidation treatment is ozone catalytic oxidation treatment, the evaporation crystallization treatment comprises preheating, heating, vapor-liquid separation, separation crystallization, condensation and compression pressurization heating of recycled steam, the recycled steam is formed in the vapor-liquid separation, the recycled steam is sucked into a compressor to be compressed to obtain compressed recycled steam after pressurization and heating, and the compressed recycled steam enters a heater to replace initial steam when heating is started to form recycling steam circulation, so that the initial steam is not needed; the waste water is subjected to vapor-liquid separation in a vapor-liquid separator, precipitated crystal grains are suspended in liquid to perform fluidization movement, small crystal grains gradually rise, are discharged from the upper part along with the liquid, are sucked into a circulating pump through a pipeline, and enter a heater again to be heated and concentrated; the large crystals gradually sink, are discharged by a discharge pump and enter a separation crystallizer, the crystals are collected after centrifugal separation, namely solid salt, and the residual mother liquor is returned to a vapor-liquid separator for evaporation and crystallization; collecting condensate water generated in the vapor-liquid separator and entering a condensate water tank; condensed water in the condensed water tank is subjected to ozone catalytic oxidation treatment to become purified water;
the mesoporous medium adsorption treatment comprises precoated diatomite filtration treatment and activated carbon adsorption filtration treatment, and the coagulation air floatation filtration pretreatment adopts oil separation, air floatation and multi-medium filtration processes;
the gas field wastewater after the coagulation air floatation filtering pretreatment unit has 90% of oil removal rate, 30% -50% of COD removal rate, 95% of impurity removal rate, 25% -45% of surfactant removal rate and 99.9% of desulfurization rate;
the removal rate of the surfactant in the gas field wastewater after passing through the mesoporous medium adsorption and filtration unit is 90 percent, and the COD removal rate is 60-80 percent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711260181.1A CN109867399B (en) | 2017-12-04 | 2017-12-04 | Gas field wastewater desulfurization and desalination treatment system and method containing surfactant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711260181.1A CN109867399B (en) | 2017-12-04 | 2017-12-04 | Gas field wastewater desulfurization and desalination treatment system and method containing surfactant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109867399A CN109867399A (en) | 2019-06-11 |
| CN109867399B true CN109867399B (en) | 2023-12-19 |
Family
ID=66915684
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711260181.1A Active CN109867399B (en) | 2017-12-04 | 2017-12-04 | Gas field wastewater desulfurization and desalination treatment system and method containing surfactant |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109867399B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112811686A (en) * | 2020-12-07 | 2021-05-18 | 德阳一铭科技发展有限公司 | Natural gas exploitation wastewater treatment process |
| CN115367939B (en) * | 2022-04-19 | 2024-04-16 | 北京万邦达环保技术股份有限公司 | Desulfurization high-salt wastewater treatment device and method |
Citations (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101041475A (en) * | 2007-03-09 | 2007-09-26 | 华南理工大学 | Fenton and air-float integral water treating method |
| CN101481186A (en) * | 2009-02-16 | 2009-07-15 | 中国石化集团石油工程西南有限公司油田工程服务分公司 | Process and apparatus for treating oil-gas field wastewater |
| CN201321416Y (en) * | 2008-10-14 | 2009-10-07 | 云南大学 | Combined equipment for treating organic wastewater with high salinity and high concentration |
| CN101555053A (en) * | 2008-04-11 | 2009-10-14 | 中国科学院广州地球化学研究所 | Compound coagulant used for treating rare-earth highly concentrated ammonian wastewater to recover industry ammonium chloride and treatment method |
| CN102320575A (en) * | 2011-08-26 | 2012-01-18 | 张小江 | The method of low-temperature evaporation Sodium Persulfate |
| CN102863097A (en) * | 2012-09-14 | 2013-01-09 | 濮阳市天地人环保工程技术有限公司 | Standardized treatment reinjection method of sulfur-containing waste liquid of high sulfur-containing oil and gas field |
| CN202924855U (en) * | 2012-12-10 | 2013-05-08 | 成都源创环保工程有限公司 | Car washing sewage reuse device |
| 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 |
| WO2013156002A1 (en) * | 2012-04-19 | 2013-10-24 | 波鹰(厦门)科技有限公司 | Nano catalyst electrolysis flocculation air flotation device |
| CN103880232A (en) * | 2013-03-25 | 2014-06-25 | 北京纬纶华业环保科技股份有限公司 | Treatment system and method for organic salt-containing wastewater |
| CN203890157U (en) * | 2014-05-16 | 2014-10-22 | 山西清泽环境科技有限公司 | Purification treatment device for industrial wastewater |
| CN104628185A (en) * | 2015-01-26 | 2015-05-20 | 许丽萍 | Oil and gas field fracturing flow-back fluid treatment process |
| CN204699440U (en) * | 2015-04-29 | 2015-10-14 | 中国石油天然气集团公司 | A kind of MVR evaporation and crystallization system of antiscaling, descaling |
| CN105198135A (en) * | 2015-10-27 | 2015-12-30 | 山东海吉雅环保设备有限公司 | Method for processing oil-field drilling-well and measure waste liquid for enabling water quality to reach standard and reusing water |
| CN105366868A (en) * | 2015-12-14 | 2016-03-02 | 四川阳森石油技术有限公司 | Up-to-standard discharge treatment technology of drilling wastewater from oil and gas fields |
| CN205473138U (en) * | 2016-01-11 | 2016-08-17 | 中国石油化工股份有限公司 | Comprehensive processing apparatus of alkaline residue waste liquid |
| CN106007094A (en) * | 2016-07-15 | 2016-10-12 | 武汉尚远环保股份有限公司 | Treatment method of oilfield waste water |
| CN205710248U (en) * | 2016-03-14 | 2016-11-23 | 尚鼎炉业科技（扬州）有限公司 | A kind of zero-discharge treatment system of dyeing waste water |
| CN205740622U (en) * | 2016-06-15 | 2016-11-30 | 广州市迈源科技有限责任公司 | A kind of percolate coagulating sedimentation, evaporation joint processing system |
| CN106348514A (en) * | 2016-11-07 | 2017-01-25 | 四川阳森石油技术有限公司 | Treatment process for gas field foam water up-to-standard discharge |
| CN106669207A (en) * | 2017-02-27 | 2017-05-17 | 江苏省环境科学研究院 | MVR (mechanical vapor recompression) evaporation crystallization system and method for high-salinity wastewater |
| CN207811478U (en) * | 2017-12-04 | 2018-09-04 | 北京沃特普特环境科技有限公司 | A kind of gas field wastewater desulfurization desalting processing system containing surfactant |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10252926B2 (en) * | 2015-08-31 | 2019-04-09 | Ecolab Usa Inc. | Wastewater treatment process for removing chemical oxygen demand |
-
2017
- 2017-12-04 CN CN201711260181.1A patent/CN109867399B/en active Active
Patent Citations (22)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101041475A (en) * | 2007-03-09 | 2007-09-26 | 华南理工大学 | Fenton and air-float integral water treating method |
| CN101555053A (en) * | 2008-04-11 | 2009-10-14 | 中国科学院广州地球化学研究所 | Compound coagulant used for treating rare-earth highly concentrated ammonian wastewater to recover industry ammonium chloride and treatment method |
| CN201321416Y (en) * | 2008-10-14 | 2009-10-07 | 云南大学 | Combined equipment for treating organic wastewater with high salinity and high concentration |
| CN101481186A (en) * | 2009-02-16 | 2009-07-15 | 中国石化集团石油工程西南有限公司油田工程服务分公司 | Process and apparatus for treating oil-gas field wastewater |
| CN102320575A (en) * | 2011-08-26 | 2012-01-18 | 张小江 | The method of low-temperature evaporation Sodium Persulfate |
| WO2013156002A1 (en) * | 2012-04-19 | 2013-10-24 | 波鹰(厦门)科技有限公司 | Nano catalyst electrolysis flocculation air flotation device |
| CN102863097A (en) * | 2012-09-14 | 2013-01-09 | 濮阳市天地人环保工程技术有限公司 | Standardized treatment reinjection method of sulfur-containing waste liquid of high sulfur-containing oil and gas field |
| CN202924855U (en) * | 2012-12-10 | 2013-05-08 | 成都源创环保工程有限公司 | Car washing sewage reuse device |
| CN103880232A (en) * | 2013-03-25 | 2014-06-25 | 北京纬纶华业环保科技股份有限公司 | Treatment system and method for organic salt-containing wastewater |
| 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 |
| CN203890157U (en) * | 2014-05-16 | 2014-10-22 | 山西清泽环境科技有限公司 | Purification treatment device for industrial wastewater |
| CN104628185A (en) * | 2015-01-26 | 2015-05-20 | 许丽萍 | Oil and gas field fracturing flow-back fluid treatment process |
| CN204699440U (en) * | 2015-04-29 | 2015-10-14 | 中国石油天然气集团公司 | A kind of MVR evaporation and crystallization system of antiscaling, descaling |
| CN105198135A (en) * | 2015-10-27 | 2015-12-30 | 山东海吉雅环保设备有限公司 | Method for processing oil-field drilling-well and measure waste liquid for enabling water quality to reach standard and reusing water |
| CN105366868A (en) * | 2015-12-14 | 2016-03-02 | 四川阳森石油技术有限公司 | Up-to-standard discharge treatment technology of drilling wastewater from oil and gas fields |
| CN205473138U (en) * | 2016-01-11 | 2016-08-17 | 中国石油化工股份有限公司 | Comprehensive processing apparatus of alkaline residue waste liquid |
| CN205710248U (en) * | 2016-03-14 | 2016-11-23 | 尚鼎炉业科技（扬州）有限公司 | A kind of zero-discharge treatment system of dyeing waste water |
| CN205740622U (en) * | 2016-06-15 | 2016-11-30 | 广州市迈源科技有限责任公司 | A kind of percolate coagulating sedimentation, evaporation joint processing system |
| CN106007094A (en) * | 2016-07-15 | 2016-10-12 | 武汉尚远环保股份有限公司 | Treatment method of oilfield waste water |
| CN106348514A (en) * | 2016-11-07 | 2017-01-25 | 四川阳森石油技术有限公司 | Treatment process for gas field foam water up-to-standard discharge |
| CN106669207A (en) * | 2017-02-27 | 2017-05-17 | 江苏省环境科学研究院 | MVR (mechanical vapor recompression) evaporation crystallization system and method for high-salinity wastewater |
| CN207811478U (en) * | 2017-12-04 | 2018-09-04 | 北京沃特普特环境科技有限公司 | A kind of gas field wastewater desulfurization desalting processing system containing surfactant |
Non-Patent Citations (5)
| Title |
|---|
| 基于蒸汽机械再压缩的硫酸铵蒸发结晶实验;韩东;彭涛;梁林;夏军;;化工进展(第S1期);全文 * |
| 杨贡林 ; 彭传丰 ; 符宇航 ; 刘昌辉 ; 李波 ; 牛翠英.气田废水多效蒸发脱盐综合利用的工艺研究.中国井矿盐.2016,第47卷(第001期),全文. * |
| 气田废水多效蒸发脱盐综合利用的工艺研究;杨贡林;彭传丰;符宇航;刘昌辉;李波;牛翠英;中国井矿盐;第47卷(第001期);全文 * |
| 浸没式粉末硅藻土预涂覆微滤装置过滤性能研究;丁兴江;;流体机械(第03期);全文 * |
| 高盐化工废水的处理和实践;张向阳;;江苏氯碱(第04期);全文 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109867399A (en) | 2019-06-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104529093B (en) | A kind of refuse pressing filtering liquid comprehensive wastewater processing equipment | |
| CN203568944U (en) | Coking wastewater reuse treatment system | |
| CN203307169U (en) | System for treating high-COD (Chemical Oxygen Demand) and high-salt content hard degradable wastewater | |
| CN101560045A (en) | Coal chemical wastewater treating technique | |
| CN108128983B (en) | Deep purification treatment process for high-sulfur and high-salt-content gas field produced water | |
| CN107304093A (en) | Containing formaldehyde, the integrated deep treatment method of methanol waste water and processing unit | |
| CN105084661A (en) | Coal-based ethylene glycol sewage treatment method and system | |
| CN107055927A (en) | A kind of high saliferous difficult degradation saccharin industrial wastewater waste gas processing method and device | |
| CN109867399B (en) | Gas field wastewater desulfurization and desalination treatment system and method containing surfactant | |
| CN104628065A (en) | Chemical pharmaceutical wastewater treatment system and method | |
| CN105417888B (en) | A kind of Clindamycin Hydrochloride waste water treatment process | |
| CN110885162A (en) | Zero-recharge treatment process for landfill leachate | |
| CN204454826U (en) | A kind of refuse pressing filtering liquid comprehensive wastewater treatment facility | |
| CN203360228U (en) | Tobacco wastewater treatment system | |
| CN108178446A (en) | high-concentration waste emulsion advanced treatment system | |
| CN207811478U (en) | A kind of gas field wastewater desulfurization desalting processing system containing surfactant | |
| CN204588911U (en) | A kind of stagewise water treatment recycling equipment | |
| CN207227223U (en) | A kind of processing of gasification of poor coal waste water and recycle device | |
| Nasr et al. | Introduction to “Cost-Efficient Wastewater Treatment Technologies: Engineered Systems” | |
| CN206279049U (en) | A kind of multi-stage sewage treatment device with recycling function | |
| CN206156979U (en) | High processing apparatus who contains salt difficult degradation saccharin industrial waste water waste gas | |
| CN205616731U (en) | Integrated advanced treatment unit who contains formaldehyde, methyl alcohol waste water | |
| CN104944638A (en) | Treatment method for high-salinity and low-pollution industrial wastewater | |
| CN104445719A (en) | Sewage treatment device | |
| CN104724881A (en) | Treatment method for high salinity industrial wastewater |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |