WO2021169912A1 - Dispositif et procédé de traitement des eaux usées organiques contenant du soufre par oxydation humide - Google Patents

Dispositif et procédé de traitement des eaux usées organiques contenant du soufre par oxydation humide Download PDF

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WO2021169912A1
WO2021169912A1 PCT/CN2021/077225 CN2021077225W WO2021169912A1 WO 2021169912 A1 WO2021169912 A1 WO 2021169912A1 CN 2021077225 W CN2021077225 W CN 2021077225W WO 2021169912 A1 WO2021169912 A1 WO 2021169912A1
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liquid
pipe
gas
inlet
shell
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PCT/CN2021/077225
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English (en)
Chinese (zh)
Inventor
杨强
许萧
王俊杰
钱运东
王磊
王志强
孟敏
李裕东
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华东理工大学
上海米素环保科技有限公司
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Publication of WO2021169912A1 publication Critical patent/WO2021169912A1/fr

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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
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • 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
    • C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
    • 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
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/101—Sulfur compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/10—Biological treatment of water, waste water, or sewage

Definitions

  • the invention belongs to the technical field of wet oxidation, and specifically relates to a device and method for wet oxidation treatment of sulfur-containing organic wastewater.
  • Wet oxidation technology namely Wet Air Oxidation (WAO)
  • WAO Wet Air Oxidation
  • the oxygen in the air is used to oxidize the sulfide in the waste lye into sodium thiosulfate or sulfate to eliminate the odor; in the liquid phase
  • the applicable organic pollutant concentration is between the incineration treatment concentration and the biochemical treatment concentration.
  • the wet oxidation reaction is a free radical reaction, including four stages: induction period, proliferation period, degradation period and end period.
  • induction period molecular oxygen reacts with organic matter to generate hydrocarbyl radicals.
  • hydrocarbyl radicals continue to react with molecular oxygen, and the resulting ester radicals react with organic substances to generate low-molecular acids and hydroxyl radicals.
  • Molecular acid decomposes into ether radicals, hydroxyl radicals and hydrocarbyl radicals. Hydroxyl radicals have strong oxidizing properties, and then deoxidize organic pollutants.
  • the energy between the free radicals is combined and the reaction stops.
  • the problems encountered in the treatment of wastewater by wet oxidation reactions include the presence of hydrocarbon oil in the wastewater, low oxidation efficiency, difficulty in degassing reaction products, and failure to meet the standard for closed slag discharge.
  • the hydrocarbons from the alkaline washing process and the butter produced in the alkaline washing tower are entrained in the waste lye.
  • the waste lye with oil causes the temperature and pressure of the oxidation reactor to fluctuate, causing the reactor to fly , Coking occurs, and even the residual oxygen content at the outlet of the reactor drops sharply.
  • the violent fluctuations caused serious entrainment of gas mist at the outlet of the reactor, which made the on-line oxygen meter malfunction.
  • the lye and oil system is very easy to emulsify, the current common methods such as inclined plate sedimentation, cyclone separation, and filter element coalescence cannot meet the requirements of long-period, high-efficiency lye degreasing.
  • the wet oxidation reactor contains a large number of fine-sized bubbles.
  • the smaller bubbles in the reaction product have higher fluid followability.
  • the fine bubbles are difficult to peel off from the liquid phase, and the vapor phase mist entrainment is serious.
  • the volume of the gas-liquid separator cannot be too large, which poses new challenges to the traditional sedimentation gas-liquid separation technology.
  • the liquid phase product will produce a certain amount of sludge precipitation after neutralization, which needs to be discharged regularly.
  • the reaction pressure of wet oxidation is usually greater than 1 MPa, containing acid, alkali, and toxic organic components. Under the trend of increasingly stringent environmental protection and safety requirements, higher requirements are put forward on the technology of airtight cleaning of sludge.
  • the present invention provides a wet oxidation treatment device for sulfur-containing organic wastewater, and a method for achieving this effect.
  • a device for wet oxidation treatment of sulfur-containing organic wastewater includes a coalescing and degreasing unit, an oxidation reaction unit, a cyclone degassing unit and a closed sludge discharge unit;
  • the coalescing and degreasing unit includes a coalescer, and the coalescer includes a first shell and an oil removing device in the first shell; the top surface of the first shell is provided with a liquid inlet and oil Phase outlet; the bottom of the first shell below the oil phase outlet is provided with a first drain;
  • the oxidation reaction unit includes a reactor, the reactor includes a second shell, a partition is fixed in the second shell, and more than one fractal internals are fixed on the partition;
  • the second shell is provided with a gas inlet and a liquid inlet, the liquid inlet is communicated with the first liquid outlet, and the upper part of the second shell is provided with a first gas-liquid outlet;
  • the fractal inner piece It includes a cylinder body, a bottom plate is fixed at the bottom of the cylinder body, a liquid inlet is opened on the cylinder body above the bottom plate, and an air inlet pipe pointing to the bottom plate is fixed on the side wall of the cylinder body.
  • the bottom of the air inlet pipe is sealed, the air inlet pipe is provided with a plurality of aeration micropores, the liquid inlet and the air inlet pipe are both located below the partition, and the top of the cylinder is a second air-liquid outlet ;
  • the cyclone degassing unit includes a third housing and a cyclone deaerator in the third housing, a gas-liquid two-phase inlet is provided on the side of the third housing, and the gas-liquid two-phase inlet Communicating the cyclone deaerator and the second gas-liquid outlet, a second liquid discharge port is provided at the bottom of the third casing, and a gas phase discharge port is provided on the top of the third casing;
  • the airtight mud drain unit includes a fourth shell and a mud drain provided at the bottom of the fourth shell.
  • the fourth shell is provided with a liquid inlet and a mud outlet, and the liquid inlet It is in communication with the second liquid discharge port, and the sludge discharger is in communication with the sludge discharge port.
  • the oil removal device includes a fluid rectifier, an X-shaped fiber layer and a corrugated plate layer which are sequentially arranged between the liquid inlet and the oil phase outlet.
  • the X-type fiber layer includes lipophilic and hydrophobic fibers and hydrophilic and oleophobic fibers, wherein the lipophilic and hydrophobic fibers are made of polyimide, polytetrafluoroethylene or polyparaphenylene. Phthalamide, the hydrophilic and oleophobic fiber material is 316 alloy, 321 alloy or 20 alloy.
  • the corrugated plate layer includes a plurality of zigzag corrugated plates arranged side by side, the distance between adjacent corrugated plates is 5-25mm, and the wave crest is provided with a circular hole with a diameter of 5-10mm.
  • the spacing between the holes is 50 to 300 mm.
  • the present invention is further provided that a throat is fixed in the second gas-liquid outlet, the middle of the throat is a through hole with a small middle and two large ends, and the minimum inner diameter of the throat is 6-100 mm.
  • the present invention is further provided that a circulating pump is provided on the outside of the reactor, and two ends of the circulating pump are respectively connected to the inside of the reactor located above and below the partition.
  • the upper part of the fourth housing is provided with a liquid discharge outlet;
  • the sludge discharger includes a main pipe, a branch pipe, and a sludge discharge pipe connected in sequence; and the fourth housing is provided with high-pressure water Inlet, the main pipeline is connected to the high-pressure water inlet, the sludge discharge pipe is connected to the sludge discharge port;
  • the sub-pipe is connected with an open blocking plate, and the opening of the blocking plate is connected with an ejector Nozzle, the axis of the ejection nozzle and the sub-pipe are coincident;
  • the ejection nozzle and the main pipe are connected with a mud mixing nozzle outside the sub-pipe, and the ejection nozzle and the mud discharge
  • the sub-pipe between the pipes is provided with a mud-inducing chamber, and the sub-pipe between the ejection nozzle and the mud-inducing chamber is communicated with an umbrella-shaped suction cup.
  • the present invention is further provided that more than one sub-pipe is connected between the main pipe and the sludge discharge pipe, and the cross-sectional area of the main pipe is the sum of the cross-sectional areas of all the sub-pipes.
  • the diameter of the sub-pipe is 20-200 mm
  • the mud mixing nozzle and the sub-pipe have an included angle of 30-80°
  • the umbrella-shaped suction cup has an expansion angle of 90-160 degrees.
  • the top of the umbrella-shaped suction cup has a hole, and a straight pipe with a diameter of 30-100 mm is welded to the opening of the sub-pipe, and the length of the straight pipe is 50-80 mm.
  • the present invention is further provided that the high-pressure water inlet is communicated with a booster pump.
  • the present invention also provides a method for wet oxidation treatment of sulfur-containing organic wastewater using the above-mentioned device.
  • the core steps include the degreasing of the raw material liquid, the enhancement of gas-liquid reaction mass transfer, the improvement of the gas-liquid separation efficiency of the reaction product, and the closed slag discharge, including the following step:
  • the formed sludge enters the fourth housing through the liquid inlet, and is discharged from the sludge outlet through the sludge discharger.
  • the present invention is further configured that, in step (1), the temperature of the sulfur-containing organic wastewater is 4 to 210 degrees Celsius, and the oil content after treatment is reduced to 0.1 to 20 mg/L.
  • the present invention is further provided that the gas-liquid ratio in the fractal internals is 0.1-30, the apparent gas velocity is 0.001-0.1 m/s, the bubble diameter is 0.02-20 mm, and the liquid phase residence time is 1.5-2.5 hours.
  • the present invention is further configured that, in step (4), a booster pump is used to provide sufficient power to the high-pressure water inlet, and the booster pump has a pressure of 0.2-2 MPa.
  • the present invention has the following beneficial effects:
  • reaction feed After the coalescing and degreasing unit treatment, the reaction feed has a good degreasing protection effect, and it is not easy to coke and fly over temperature.
  • the bubbles in the reactor are finer, which is beneficial to speed up the oxidation speed and deepen the reaction accuracy.
  • Figure 1 is a schematic diagram of the overall structure of the present invention.
  • Figure 2 is a schematic diagram of the structure of the fractal internals
  • Figure 3 is a schematic diagram of the structure of a cyclone degasser
  • Figure 4A is a schematic diagram of the structure of the mud discharging device (single mud discharging device);
  • Figure 4B is a schematic diagram of the structure of the sludge discharging device (the sludge discharging device is installed in parallel);
  • Figure 5 is a schematic diagram of the structure of the oxidation reaction unit (with a circulating pump);
  • Fig. 6 is a schematic diagram of a partial structure of the corrugated board layer.
  • 1 coalescing and degreasing unit 1-1 fluid rectifier; 1-2X type fiber layer; 1-3 corrugated board layer; 1-3-1 corrugated board;
  • Cyclone degassing unit 3 Cyclone degassing unit; 3-1 Cyclone deaerator; 3-1-1 liquid and gas inlet; 3-1-2 column cavity; 3-1-3 liquid phase outlet; 3-1-4 overflow pipe Conical port; 3-1-5 first overflow pipe column cavity; 3-1-6 secondary liquid outlet; 3-1-7 annular slot; 3-1-8 second overflow pipe column cavity;
  • 4 Closed mud discharge unit 4-1 mud discharge device; 4-1-1 ejection nozzle; 4-1-2 mud mixing nozzle; 4-1-3 umbrella-shaped suction cup; 4-1-4 mud chamber; 4 -1-5 main pipeline; 4-1-6 branch pipeline; 4-1-7 mud channel;
  • a device for wet oxidation treatment of sulfur-containing organic wastewater includes a coalescing and degreasing unit 1, an oxidation reaction unit 2, a cyclone degassing unit 3, and a closed sludge discharge unit 4, see figure 1.
  • the coalescing and degreasing unit includes a coalescer, and the coalescer includes a first housing and a degreasing device in the first housing.
  • the top surface of the first shell is provided with a liquid inlet and an oil phase outlet; the bottom of the first shell below the oil phase outlet is provided with a first liquid outlet.
  • the oil removal device includes a fluid rectifier 1-1, an X-shaped fiber layer 1-2 and a corrugated plate layer 1-3 arranged in sequence between the liquid inlet and the oil phase outlet.
  • the corrugated board layer 1-3 includes a plurality of zigzag corrugated boards 1-3-1 arranged side by side, the distance between adjacent corrugated boards 1-3-1 is 5-25mm, and the wave crest has a diameter of 5-10mm. The distance between the round holes is 50 ⁇ 300mm.
  • the structure of the X-type fiber layer 1-2 in the present invention is consistent with the structure of the X-type fiber layer in the patent CN201410211202.0.
  • the X-type fiber layer 1-2 includes lipophilic and hydrophobic fibers and hydrophilic and oleophobic fibers.
  • the lipophilic and hydrophobic fibers are made of polyimide, polytetrafluoroethylene or poly(p-phenylene terephthalamide).
  • the hydrophilic and oleophobic fiber material is 316 alloy, 321 alloy or 20 alloy.
  • the treatment process of the coalescing and degreasing unit is: after the sulfur-containing organic wastewater enters the coalescer, the wastewater is rectified by the fluid rectifier 1-1, so that the fluid is evenly distributed in the radial cross section of the fluid flow; the rectified wastewater is uniform Into the X-shaped braided layer 1-2 formed by the interlaced weaving of lipophilic and hydrophobic fibers and hydrophilic and oleophobic fibers, in the X-shaped braid 1-2, oil droplets are captured, coalesced and grown, and a trace oil-in-water emulsion is formed Demulsification and separation; the coalesced and separated oil and water enter the corrugated sheet layer 1-3 for rapid growth and separation of oil droplets; after the process of separation, the oil content in the wastewater is reduced to 0.1-20mg/L.
  • the oxidation reaction unit includes a reactor. See Fig. 2.
  • the reactor includes a second shell.
  • a partition 2-2 is fixed in the second shell, and more than one fractal inner part 2-1 is fixed on the partition 2-2.
  • the fractal internals 2-1 can be fixed in parallel.
  • a gas inlet and a liquid inlet are provided on the second shell located under the partition 2-2, the liquid inlet is connected with the first liquid discharge port, and the upper part of the second shell is provided with a first gas-liquid outlet.
  • the fractal inner part 2-1 includes a cylinder, the bottom of the cylinder is fixed with a bottom plate 2-1-8, the cylinder above the bottom plate 2-1-8 is provided with a liquid inlet 2-1-7, and the side wall of the cylinder An intake pipe pointing to the bottom plate 2-1-8 is fixed on the top.
  • the bottom of the intake pipe can be sealed by an intake plug 2-1-4.
  • There are multiple aeration micropores 2-1-3, the liquid inlet 2-1-7 and the air inlet 2-1-6 are located under the partition 2-2, and the top of the cylinder is the second gas-liquid outlet 2. -1-1.
  • the minimum flow channel size of the fractal inner part 2-1 is 1.2-12mm. Runner refers to all circulation areas except equipment.
  • a throat pipe 2-1-2 is fixed in the second gas-liquid outlet 2-1-1, and the middle of the throat pipe 2-1-2 is a through hole with a small middle and two large ends, and the minimum inner diameter of the throat pipe is 6 ⁇ 100mm.
  • the present invention also provides a circulating feed system for the oxidation reaction unit.
  • a circulating pump 7 is provided on the outside of the reactor, and the two ends of the circulating pump 7 are respectively connected to the inside of the reactor located above and below the partition plate 2-2.
  • the reacted product part is injected into the fractal inner part 2-1 again through the circulating pump 7, so that the reacted liquid phase reacts with fresh air for a second time, so as to achieve the purpose of improving the oxidation efficiency.
  • the treatment process of the oxidation reaction unit is: the sulfur-containing organic wastewater after coalescing and degreasing is pressurized by the booster pump and then enters the liquid inlet of the fractal inner part 2-1. At the same time, fresh air enters the inlet pipe through the compressor. Port 2-1-6 is blown into the fractal inner part 2-1. After the gas enters the air inlet pipe, bubbles are generated through the aeration micropores 2-1-3.
  • the bubbles and sulfur-containing organic wastewater are fully uniform in the mixing chamber 2-1-5 After mixing, it is sprayed out through the throat 2-1-2, and the oxygen in the fractal bubble fully reacts with the sulfide in the sulfur-containing organic waste water to oxidize it into sodium thiosulfate or sulfate.
  • All equipment parts in the reactor are large-sized channels and static parts. There is no flow dead zone in the device, which can avoid a large amount of potential fouling deposits in the oxidation reaction.
  • the waste lye and compressed air are used as kinetic energy sources, and the water contained in the upper cavity of the partition is a continuous phase fluid, which causes the gas-liquid to mix with the existing liquid in the upper cavity of the partition, so that the temperature of the device is more uniform.
  • most of the gas size is small, which prevents the gas from rising rapidly due to its low density relative to the surrounding liquid. This smaller bubble lengthens the contact time between the gas and the liquid, and greatly improves the oxygen utilization rate.
  • the swirling flow degassing unit includes a third shell and a swirling flow deaerator 3-1 in the third shell (the structure of the swirling flow deaerator 3-1 is similar to the use of swirling or centrifugal field in the patent CN201310037577.5 It is consistent with the structure of the pressure gradient field coupling device for liquid degassing), the side of the third shell is provided with a gas-liquid two-phase inlet, and the gas-liquid two-phase inlet communicates with the cyclone degasser 3-1 and the second gas-liquid Outlet 2-1-1, a second liquid discharge port is provided at the bottom of the third casing, and a gas-phase discharge port is provided on the top of the third casing.
  • the processing process of the cyclone degassing unit is: combined with the cyclonic deaerator in Figure 3, the reacted gas-liquid mixture enters the device from the liquid gas inlet 3-1-1 under a certain pressure, and under the action of the centrifugal field,
  • the gas in the liquid migrates to the center position of the column cavity 3-1-2, generating a pressure gradient field, and the gas dissolved in the inlet liquid migrates to the center axis position of the column cavity 3-1-2 under the action of the pressure gradient field, and
  • the gas separated from the centrifugal field at the 3-1-4 section of the conical port at the end of the first overflow pipe is mixed and discharged through the first overflow pipe column cavity 3-1-5, and the liquid entrained by the gas is discharged through the second overflow
  • the annular slot 3-1-7 on the column cavity 3-1-8 performs secondary separation, and the purified gas is discharged from the upper opening of the second overflow pipe column cavity 3-1-8, entraining the recovered secondary liquid It is discharged through the secondary
  • the closed mud discharge unit includes a fourth shell and a mud drain 4-1 arranged at the bottom of the fourth shell.
  • the fourth shell is provided with a liquid inlet and a mud outlet, and the liquid inlet and the second The two liquid discharge ports are connected, and the mud discharging device 4-1 is connected to the mud discharging port, see Figure 4A.
  • the upper part of the fourth shell is provided with a liquid discharge outlet;
  • the sludge discharger includes a main pipe 4-1-5, a sub-pipe 4-1-6, and a sludge discharge pipe 4-1-7 that are connected in sequence;
  • the fourth shell The body is provided with a high-pressure water inlet, the main pipeline is connected to the high-pressure water inlet, the high-pressure water inlet is connected to the booster pump 5, and the mud discharge pipe 4-1-7 is connected to the mud discharge port;
  • the sub-pipe 4-1-6 is connected with an opening The ejection nozzle 4-1-1 is connected to the opening of the blocking plate.
  • the axis of the ejection nozzle 4-1-1 and the sub-pipe 4-1-6 coincide; the ejection nozzle 4-1-1 and The branch pipe 4-1-6 between the main pipe 4-1-5 is connected with the mud mixing nozzle 4-1-2, the ejection nozzle 4-1-1 and the mud pipe 4-1-7 are connected with each other.
  • the pipe 4-1-6 is provided with a mud-inducing chamber 4-1-4, and the sub-pipe 4-1-6 between the ejection nozzle 4-1-1 and the mud-inducing chamber 4-1-4 is connected with an umbrella outside. Suction cup 4-1-3.
  • the closed sludge discharging unit of the present invention can be further equipped with a parallel installation mode of sludge discharging devices to increase the processing capacity.
  • a parallel installation mode of sludge discharging devices to increase the processing capacity.
  • the diameter of the sub-pipe 4-1-6 is 20-200mm, the mud mixing nozzle 4-1-2 and the sub-pipe are at an angle of 30-80°; the expansion angle of the umbrella-shaped suction cup 4-1-3 is 90-160 degrees.
  • Umbrella suction cup 4-1-3 has a hole on the top, and a straight pipe with a diameter of 30-100mm is welded to the opening of the sub-pipe 4-1-6, and the length of the straight pipe is 50-80mm.
  • the treatment process of the closed sludge discharge unit is: the liquid phase feed and neutralization reaction after degassing by the cyclone degassing unit.
  • the neutralization reaction can be carried out in the mixer 6 or artificially added and adjusted, and the neutralized liquid enters the closed discharge In the mud unit, after gravity sedimentation, the treated waste liquid is discharged, and the sludge is deposited on the bottom and needs to be discharged regularly.
  • the booster pump When the mud is discharged, the booster pump is turned on, the high-pressure water flows into the main pipe 4-1-5, one water flow is sprayed out through the mud mixing nozzle 4-1-2 to loosen the deposited mud, and the other water flow passes through the ejection nozzle 4-1 -1 is ejected, and negative pressure is formed in the pipeline when the high-pressure water jet is sprayed.
  • the loose mud is sucked into the pipeline through the umbrella-shaped suction cup 4-1-3, and is discharged after being mixed with the high-pressure water flow in the mud discharge channel 4-1-7.
  • the method of the present invention for wet oxidation treatment of sulfur-containing organic wastewater using the above-mentioned device can be summarized as follows: firstly, the sulfur-containing organic wastewater is subjected to high-efficiency degreasing treatment, and the sulfide is chemically oxidized by the air oxidation method, and the reaction product enters the cyclone. Degasser for deep gas-liquid separation. The desulfurized wastewater is neutralized, and the neutralized waste liquid flows to the closed sludge discharge unit to precipitate out suspended solids and some colloids. The sludge settled at the bottom is regularly discharged through the sludge discharger. Specifically, it includes the following steps:
  • the degreasing wastewater enters the liquid inlet of the fractal internals, and air is filled into the intake pipe.
  • the gas-liquid ratio entering the fractal internals is 0.1-30, the apparent gas velocity is 0.001-0.1m/s, and the bubble diameter It is 0.02-20mm, and the liquid phase residence time is 1.5-2.5 hours.
  • the wastewater fully reacts with the oxygen in the air, and the reacted gas-liquid two-phase product is discharged from the first gas-liquid outlet into the cyclone degasser;
  • the formed sludge enters the fourth shell through the liquid inlet, and the high-pressure water is pumped into the bottom mud drain through the high-pressure water inlet by the booster pump (control pressure is 0.2 ⁇ 2MPa), after the high-pressure water enters the pipeline It is divided into two paths, one of which is sprayed out through mud mixing nozzle to make the sludge deposited at the bottom loose and uniform, and the other is through the ejection nozzle to generate a high-speed jet to form a vacuum in the sludge chamber, and the sludge at the bottom of the fourth shell passes through The mud chamber is sucked in, mixed with the high-speed jet in the pipeline and discharged.

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)
  • Physical Water Treatments (AREA)

Abstract

L'invention concerne un dispositif pour traiter les eaux usées organiques contenant du soufre au moyen d'une oxydation humide. Le dispositif comprend une unité d'élimination de l'huile d'agrégation (1), une unité de réaction d'oxydation (2), une unité de dégazage à cyclone (3), et une unité d'évacuation de boues fermée (4). L'invention concerne également un procédé de traitement des eaux usées organiques contenant du soufre par oxydation humide en utilisant le dispositif. Le procédé comprend : la réalisation d'un traitement d'élimination des huiles à haute efficacité sur les eaux usées organiques contenant du soufre, puis la réalisation d'un traitement d'oxydation chimique sur un sulfure en utilisant un procédé d'oxydation à l'air, la réalisation d'une séparation gaz-liquide profonde sur un produit de réaction qui entre dans l'unité de dégazage à cyclone (3), et l'évacuation hermétique des boues au moyen d'un dispositif d'évacuation des boues.
PCT/CN2021/077225 2020-02-28 2021-02-22 Dispositif et procédé de traitement des eaux usées organiques contenant du soufre par oxydation humide WO2021169912A1 (fr)

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CN202010126741.XA CN111362451B (zh) 2020-02-28 2020-02-28 一种湿式氧化处理含硫有机废水的装置和方法
CN202010126741.X 2020-02-28

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CN111362451B (zh) * 2020-02-28 2022-06-03 华东理工大学 一种湿式氧化处理含硫有机废水的装置和方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH05115887A (ja) * 1991-10-24 1993-05-14 Nippon Shokubai Co Ltd 無機の硫黄を含む化合物を含有する廃水の処理方法
CN102285729A (zh) * 2010-06-18 2011-12-21 中国石油化工股份有限公司 一种高温湿式氧化处理废碱液的方法
CN103964545A (zh) * 2014-05-19 2014-08-06 华东理工大学 一种对含低浓度污油的废水进行深度除油的方法及装置
CN105016552A (zh) * 2014-04-22 2015-11-04 中国石油化工股份有限公司 一种油品精制废碱液的处理方法
CN208151047U (zh) * 2018-02-07 2018-11-27 中国石油化工股份有限公司 脱硫废水氧化罐
CN111362451A (zh) * 2020-02-28 2020-07-03 华东理工大学 一种湿式氧化处理含硫有机废水的装置和方法

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10188119B2 (en) * 2001-07-16 2019-01-29 Foret Plasma Labs, Llc Method for treating a substance with wave energy from plasma and an electrical arc
US7666316B2 (en) * 2004-07-20 2010-02-23 Thinkvillage-Kerfoot, Llc Permanganate-coated ozone for groundwater and soil treatment with in-situ oxidation
CN103071318B (zh) * 2013-01-30 2015-04-15 华东理工大学 利用旋流或离心场与压力梯度场耦合进行液体脱气的装置
CN109020090A (zh) * 2018-09-12 2018-12-18 南京科莱恩环境工程有限公司 一种高浓度难降解有机废水处理装置及方法
CN110270282A (zh) * 2019-07-04 2019-09-24 华东理工大学 一种分形气泡构型可控式浆态床反应器

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH05115887A (ja) * 1991-10-24 1993-05-14 Nippon Shokubai Co Ltd 無機の硫黄を含む化合物を含有する廃水の処理方法
CN102285729A (zh) * 2010-06-18 2011-12-21 中国石油化工股份有限公司 一种高温湿式氧化处理废碱液的方法
CN105016552A (zh) * 2014-04-22 2015-11-04 中国石油化工股份有限公司 一种油品精制废碱液的处理方法
CN103964545A (zh) * 2014-05-19 2014-08-06 华东理工大学 一种对含低浓度污油的废水进行深度除油的方法及装置
CN208151047U (zh) * 2018-02-07 2018-11-27 中国石油化工股份有限公司 脱硫废水氧化罐
CN111362451A (zh) * 2020-02-28 2020-07-03 华东理工大学 一种湿式氧化处理含硫有机废水的装置和方法

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