WO2020041917A1 - 高浓度石油污泥绿色清洗-热脱附集成技术处理方法与处理系统 - Google Patents

高浓度石油污泥绿色清洗-热脱附集成技术处理方法与处理系统 Download PDF

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Publication number
WO2020041917A1
WO2020041917A1 PCT/CN2018/000319 CN2018000319W WO2020041917A1 WO 2020041917 A1 WO2020041917 A1 WO 2020041917A1 CN 2018000319 W CN2018000319 W CN 2018000319W WO 2020041917 A1 WO2020041917 A1 WO 2020041917A1
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Prior art keywords
sludge
thermal desorption
oil
tank
thermal
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PCT/CN2018/000319
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English (en)
French (fr)
Inventor
杨崎峰
宋海农
周永信
林宏飞
黎秋君
廖长君
黄祖浩
王爱
李智华
赵志勇
曹斐姝
黄锦孙
谢湉
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广西博世科环保科技股份有限公司
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Priority to CA3090902A priority Critical patent/CA3090902A1/en
Publication of WO2020041917A1 publication Critical patent/WO2020041917A1/zh

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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
    • C02F11/00—Treatment of sludge; Devices therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/06—Spray cleaning
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/38—Removing components of undefined structure
    • B01D53/40—Acidic components
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/79—Injecting reactants
    • 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
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/06—Sludge reduction, e.g. by lysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/10—Energy recovery
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the invention relates to the technical field of sludge treatment, in particular to a method and system for processing high-concentration petroleum sludge with green cleaning and thermal desorption.
  • oily sludge contains a large amount of odorous and toxic substances such as benzene, anthracene, phenols, and gadolinium. If oily sludge is not treated in time, it will cause varying degrees of damage to the production area and the surrounding environment.
  • high-concentration petroleum sludge oil sludge with an oil content of more than 15% is referred to as high-concentration petroleum sludge.
  • thermochemical cleaning for high-concentration petroleum sludge.
  • the thermochemical cleaning method is used, and the sludge after cleaning is still The high residual oil content cannot meet the standards for direct discharge or utilization. If direct thermal thermal desorption is used to directly detoxify high-concentration petroleum sludge, there will be greater hidden safety hazards, as well as shortcomings such as high energy consumption and waste of petroleum resources.
  • the object of the present invention is to provide a high-concentration petroleum sludge green cleaning-thermal desorption integrated technology processing method and processing system, which adopts a combination of cleaning technology and thermal desorption technology to process high-concentration petroleum Sludge can not only recover resources, but also safely detoxify sludge.
  • the invention provides a high-concentration petroleum sludge green cleaning-thermal desorption integrated technology processing method, which includes the following processing steps:
  • Solid-liquid separation and oil-water separation The solid-liquid separation is performed by a high-efficiency solid-liquid separator to reduce the oil content of the separated sludge to 3% to 6% and the water content to 60% to 70%. Then, the sludge is transported to The sludge temporary storage area is temporarily stored or directly sent to the sludge dryer, the sewage separated by the high-efficiency solid-liquid separator is sent to the oil-water separator, and the oil separated by the oil-water separator is sent to the recovered oil tank.
  • the sewage separated by the oil-water separator is sent to an integrated sewage treatment system for processing, and the treated water is stored in a water storage tank and reused in a chemical thermal washing tank;
  • Sludge drying and condensation recovery treatment Dry the sludge sent to the sludge dryer to a moisture content below 20%, and send the steam generated during the drying process to the condensation recovery system for condensation, oil and water After condensation, the condensate is sent to an oil-water separator for oil-water separation;
  • Oil sludge thermal desorption treatment and high temperature combustion oxidation treatment The oily sludge treated by the sludge dryer is sent to the thermal desorption system, and the temperature of the thermal desorption chamber of the thermal desorption system is controlled at 300-750 ° C. And ensure that the thermal desorption chamber is in a slight negative pressure state, at the same time, the sludge transportation direction is opposite to the flow direction of the flue gas, and ensure that the sludge is desorbed and cracked under anoxic conditions;
  • Tail gas cooling and dust removal treatment The intermediate temperature tail gas from the waste heat boiler is sent to the quench tower, and the tail gas temperature is reduced to below 200 ° C through the quench tower, and then the temperature is reduced by dust removal and spraying of lye to remove acid gas. The tail gas is treated After reaching the standard, it is discharged into the atmosphere through the chimney.
  • step (6) the high-temperature combustion oxidation system uses natural gas to open fire, the working temperature is in the range of 850 to 1100 ° C, and the residence time is 1.5 to 2 seconds to ensure the complete harmless elimination of organic components and prevent the dioxin produce.
  • step (6) the high-temperature exhaust gas from the high-temperature combustion oxidation system is about 1000 ° C, which is sent to a waste heat boiler for waste heat recovery and then reduced to 500 ° C intermediate-temperature exhaust gas.
  • the invention relates to a high-concentration petroleum sludge green cleaning-thermal desorption integrated technology processing system, which is mainly composed of a sludge chemical hot washing system and a sludge harmless thermal desorption system.
  • the sludge chemical hot washing system is composed of sludge Mass tank 1, chemical hot wash tank 2, high-efficiency solid-liquid separator 3, oil-water separator 4, integrated sewage treatment system 6, water storage tank 23 are connected in sequence through pipelines.
  • the top oil outlet of chemical hot wash tank 2 and The oil outlet of the oil-water separator 4 is respectively connected to the recovery oil tank 5 through a pipeline, and the bottom of the chemical thermal washing tank 2 is connected to the high-efficiency solid-liquid separator 3 through a pipeline.
  • the liquid outlet of the high-efficiency solid-liquid separator 3 is separated from oil-water.
  • Device 4 is connected;
  • the sludge harmless heat desorption system consists of a sludge dryer 10, a condensation recovery system 11, a thermal desorption feed system 7, a thermal desorption system 8, a high temperature combustion oxidation system 9, and a waste heat boiler 13.
  • the exhaust gas cooling and dust removal treatment system and the discharge system are composed.
  • the solid discharge port of the high-efficiency solid-liquid separator 3 is connected to the feed inlet of the sludge dryer 10.
  • the steam outlet of the sludge dryer 10 is condensed and recovered.
  • the non-condensable gas outlet of 11 is connected to the high-temperature combustion oxidation system 9 through a pipeline, and the condensate outlet of the condensation recovery system 11 is connected to an oil-water separator 4 through a pipeline; the solid discharge port of the sludge dryer 10 and the thermal desorption feed system 7 Are connected, the thermal desorption feed system 7 is connected with the thermal desorption system 8, the thermal desorption flue gas outlet 83 of the thermal desorption system 8 is connected with the flue gas inlet 91 of the high temperature combustion oxidation system 9, and the thermal desorption system The discharge port of 8 is connected to the discharge system.
  • the exhaust gas outlet 93 of the high-temperature combustion oxidation system 9 is connected to the waste heat boiler 13.
  • the steam outlet of the waste heat boiler 13 is connected to the chemical heat washing tank 2 and the sludge dryer 10 through the pipeline.
  • the waste heat boiler The flue gas outlet is connected to the exhaust gas cooling and dust removal treatment system, and the exhaust gas is discharged into the atmosphere after being processed by the exhaust gas cooling and dust removal treatment system.
  • the oil-water separator 4 is composed of a buffer tank 41, a reaction tank 42, an oil storage tank 44 and a water outlet tank 43.
  • the buffer tank 41, the reaction tank 42 and the water outlet tank 43 are arranged in order.
  • the oil storage tank 44 is located in the reaction tank 42. In the upper part, the oil storage tank 44 is connected to the recovery oil tank 5 through a pipeline, and the buffer tank 41 is connected to the liquid outlet of the high-efficiency solid-liquid separator 3 through a pipeline.
  • the thermal desorption sludge feeding system 7 is composed of a feeding silo 71, a belt conveyor 72, and a metering hopper 73.
  • the feeding silo 71 is located at the entrance of the belt conveyor 72
  • the metering hopper 73 is located at The outlet of the belt conveyor 72 and the outlet of the metering hopper 73 are connected to the inlet of the thermal desorption system 8.
  • the thermal desorption system 8 of the present invention includes a thermal desorption chamber coated with a refractory material.
  • a series of thermal desorption burners 82 are installed on the top of the thermal desorption chamber, and a stainless steel crawler belt is arranged below the thermal desorption burner 82.
  • a feed inlet is provided at one end of the thermal desorption chamber, and a discharge propeller 84 is provided at the other end.
  • a thermal desorption flue gas outlet 83 is provided at the top of the thermal desorption chamber.
  • the high-temperature combustion oxidation system 9 of the present invention includes a high-temperature combustion chamber.
  • One end of the high-temperature combustion chamber is provided with a flue gas inlet 91 and a high-temperature burner 92, and the other end is provided with an exhaust gas outlet 93.
  • the exhaust gas outlet 93 is connected to the waste heat boiler 13.
  • the exhaust gas cooling and dedusting treatment system includes a quench tower 14, a spray tower 15, a settling tower 16, an induced draft fan 17, and a chimney 18, the spray tower 15 is connected to the settling tower 16, and the quench tower 14 is connected to the spray tower via a pipeline 15 is connected, the outlet of the sedimentation tower 16 is connected to the chimney 18 through a pipeline, and an induced draft fan 17 is installed on the pipeline.
  • the discharging system is composed of a discharging hopper 19, a dual-axis spiral unloader 20, and a discharging bin 21.
  • the discharging hopper 19 is located at the entrance of the dual-axis spiral unloader 20, and the discharging bin 21 is located in the double
  • the outlet of the shaft screw unloader 20 the outer layer of the double shaft screw unloader 20 is wrapped with a layer of cooling water, and the top of the discharge bin 21 is equipped with a spray device to reduce the temperature and dust in the silo. .
  • the present invention has the following advantages:
  • the cleaning agent adopted by the present invention is green and environmentally friendly, and has a significant cleaning effect. After washing, the oil-water-solid three-phase layering efficiency is fast and the oil recovery rate is high.
  • the thermal desorption system of the present invention adopts high temperature and corrosion resistant stainless steel crawler transmission, which directly heats sludge by flame method, has high desorption efficiency, large processing capacity, and can achieve high operating temperature and residence time.
  • the length of the high-temperature combustion chamber used is long enough, the residence time is long enough, the supplementary air is excessive, and the combustion temperature is high enough to achieve 3T incineration to ensure the complete combustion of organic gases, which can effectively prevent the generation of dioxins.
  • FIG. 1 is a process flow chart of a method for processing a high-concentration petroleum sludge green cleaning-thermal desorption integrated technology according to the present invention.
  • FIG. 2 is a schematic structural diagram of a high-concentration petroleum sludge green cleaning-thermal desorption integrated technology processing system according to the present invention.
  • sludge homogenization tank 1 chemical hot wash tank 2, high-efficiency solid-liquid separator 3, oil-water separator 4, sewage buffer tank 41, reaction tank 42, oil storage tank 44, water outlet tank 43, recovery oil tank 5, sewage Integrated processing system 6, thermal desorption feed system 7, feed silo 71, belt conveyor 72, metering hopper 73, thermal desorption system 8, stainless steel track 81, thermal desorption burner 82, thermal desorption With flue gas outlet 83, discharge thruster 84, high temperature combustion oxidation system 9, flue gas inlet 91, high temperature burner 92, high temperature exhaust gas outlet 93, sludge dryer 10, condensation recovery system 11, condensation pump 12, waste heat Boiler 13, quench tower 14, spray tower 15, settling tower 16, induced draft fan 17, chimney 18, discharge hopper 19, biaxial screw conveyor 20, discharge silo 21, dosing system 22, water storage tank 23 , The first mud pump 24, the second mud pump 25, the sewage pump 26, and the grille 27.
  • the high-concentration petroleum sludge green cleaning-thermal desorption integrated technology processing method of the present invention includes the following processing steps:
  • (1) Homogeneous and impurity-removing pretreatment The sludge is subjected to quenching and tempering and dispersing pretreatment. During the quenching and tempering process, a sludge dispersant can be added to adjust the dispersibility of the sludge, so that the colored strip cloth woven bag fragments in the sludge slurry and labor protection supplies , Weeds, brick tiles, iron wire and other garbage ⁇ 10 mm size are intercepted by the grille, and the debris intercepted by the grille is regularly cleaned.
  • Chemical hot-washing treatment send the sludge after homogeneous impurity-removing treatment to a chemical hot-washing tank containing hot water (60-80 ° C) and cleaning agents (such as lye, surfactant, etc.),
  • the chemical thermal washing tank is equipped with a dosing system for adding cleaning agents.
  • the green environmental protection cleaning agent and hot water and sludge are forced to be fully stirred by the stirring blades in the tank, so that the crude oil is separated from the sludge, and the separated oil is removed from the chemical.
  • the top of the hot-wash tank is scraped out and stored in a recovery oil tank.
  • the solid phase after chemical heat-washing is discharged from the bottom of the chemical hot-wash tank and sent to a high-efficiency solid-liquid separator.
  • Solid-liquid separation and oil-water separation The solid-liquid separation is performed by a high-efficiency solid-liquid separator to reduce the oil content of the separated sludge to 3% to 6% and the water content to 60% to 70%.
  • the separated sludge is sent to the sludge temporary storage area for temporary storage or directly into the sludge dryer, and the sewage separated by the high-efficiency solid-liquid separator is sent to the oil-water separator, and the oil separated by the oil-water separator is sent to Into the recovery tank, and the sewage separated by the oil-water separator is sent to the integrated sewage treatment system (the structure of this equipment can adopt the "Heavy Metal Wastewater Complete Treatment Equipment" disclosed by Chinese Patent No. ZL201220225085.X, and other sewage can also be implemented Treatment equipment), the treated water is stored in a water storage tank, and then reused in a chemical thermal washing tank.
  • the dewatered sludge has a moisture content of about 60% and cannot be directly entered into the thermal desorption system. Therefore, the sludge sent to the sludge dryer needs to be dried to a moisture content of 20
  • the heat source of the sludge dryer mainly comes from the heat recovered by the electricity and waste heat boilers.
  • the steam generated during the drying process is sent to the condensation recovery system for condensation.
  • the condensate is sent to the oil-water separator. Oil-water separation is performed.
  • the recovered oil is collected and shipped to the treatment station for processing.
  • the separated water enters the integrated sewage treatment system for reuse by the sludge chemical thermal washing tank.
  • Non-condensable light components that is, non-condensable gas
  • the high-temperature combustion oxidation system performs complete combustion oxidation to ensure that the flue gas is fully purified.
  • Oil sludge thermal desorption treatment and high temperature combustion oxidation treatment The oily sludge treated by the sludge dryer is fed into the thermal desorption system through the feeding system.
  • the continuous feeding of the sludge makes the feeding port form a " Soil plug "can reduce the amount of air entering the thermal desorption system, and effectively block the thermal desorption system from the atmosphere, ensuring that the thermal desorption chamber is in a state of slight negative pressure.
  • the sludge is transported through the stainless steel crawler in the thermal desorption chamber.
  • the sludge flow direction is opposite to the flue gas flow.
  • the sludge is heated by a series of thermal desorption burners on the top of the thermal desorption system.
  • the entire process Strictly control the amount of air entering to ensure that the sludge is desorbed and cracked in the absence of oxygen.
  • the temperature of the thermal desorption chamber can be set between 300 and 750 ° C to ensure that the various hydrocarbon fractions in the sludge are completely desorbed.
  • the thermal desorption flue gas from the thermal desorption system enters the high-temperature combustion oxidation system.
  • the high-temperature combustion oxidation system uses natural gas to burn.
  • the operating temperature is in the range of 850 to 1100 ° C and the residence time is 1.5 to 2 seconds to ensure that it never condenses.
  • the organic components such as petroleum hydrocarbons in the gas are completely harmlessly eliminated, and the production of dioxins is prevented.
  • Tail gas cooling and dust removal treatment The intermediate temperature tail gas from the waste heat boiler is sent to the quench tower, and the temperature of the tail gas is reduced from 500 ° C to less than 200 ° C within 1 s through the quench tower to avoid the re-generation of dioxins, and then pass through Cooling and dust removal and spraying of lye to remove acid gas, the exhaust gas is discharged to the atmosphere through the chimney after being treated to the standard.
  • the treatment system of the present invention includes two parts: a sludge chemical heat washing system and a sludge harmless thermal desorption system.
  • the sludge chemical thermal washing system is composed of a sludge homogeneous tank 1, a chemical thermal washing tank 2, a high-efficiency solid-liquid separator 3, an oil-water separator 4, an integrated sewage treatment system 6, and a water storage tank 23, which are connected in sequence through a pipeline.
  • the sludge homogenization tank 1 is provided with a grille 27, and the discharge opening of the sludge homogenization tank 1 is connected to the inlet of the chemical thermal washing tank 2 through a first sludge pump 24.
  • the chemical thermal washing tank 2 is provided with a cleaning agent for adding In the chemical dosing system 22, a stirring slurry is provided in the chemical thermal washing tank 2.
  • the top oil outlet of the chemical thermal washing tank 2 is connected to the recovery oil tank 5 through a pipeline, and the bottom outlet of the chemical thermal washing tank 2 passes through the second
  • the sludge pump 25 is connected to the inlet of the high-efficiency solid-liquid separator 3, the solid outlet of the high-efficiency solid-liquid separator 3 is connected to the feed inlet of the sludge dryer 10, and the liquid outlet of the high-efficiency solid-liquid separator 3 is
  • the sewage pump 26 is connected to the inlet of the oil-water separator 4, the water outlet of the oil-water separator 4 is connected to the water inlet of the integrated sewage treatment system 6, and the water outlet of the integrated sewage treatment system 6 is connected to the inlet of the water storage tank 23 After being connected, the water in the water storage tank 23 is finally returned to the chemical heat washing tank 2 for reuse.
  • the sludge innocuous heat desorption system consists of a sludge dryer 10, a condensation recovery system 11, a thermal desorption feed system 7, a thermal desorption system 8, a high-temperature combustion oxidation system 9, a waste heat boiler 13, and exhaust gas cooling and dust removal.
  • the treatment system and the discharge system are composed of the steam outlet of the sludge dryer 10 and the condensation recovery system 11.
  • the non-condensable gas outlet of the condensation recovery system 11 is connected to the high temperature combustion oxidation system 9 through a pipeline for recycling and condensation recovery.
  • the condensate outlet of the system 11 is connected to the oil-water separator 4 via a pipeline, and a condensate pump 12 is installed on the pipeline; the solid discharge port of the sludge dryer 10 is connected to the thermal desorption feed system 7 for thermal desorption
  • the feeding system 7 includes a feeding hopper 71, a belt conveyor 72, and a metering hopper 73.
  • the feeding hopper 71 is located at the entrance end of the belt conveyor 72, and the metering hopper 73 is located at the exit end of the belt conveyor 72.
  • the feed silo 71 is connected to the solid discharge port of the sludge dryer 10.
  • the metering hopper 73 of the thermal desorption feed system 7 is installed at the inlet of the thermal desorption system 8, and the thermal desorption system 8 Including thermal desorption chamber coated with refractory, top of thermal desorption chamber A series of thermal desorption burners 82 are evenly scattered on both sides of the centerline. A stainless steel crawler conveyor belt 81 is arranged below the thermal desorption burner 82. One end of the thermal desorption chamber is provided with a feed inlet and the other end A discharge propeller 84 is provided, and a thermal desorption flue gas outlet 83 is provided on the top of the thermal desorption chamber.
  • the discharge propeller 84 is connected to a discharge system, which is discharged by a discharge hopper 19 and a dual-axis spiral discharge.
  • the feeder 20 and the discharge bin 21 are formed.
  • the discharge hopper 19 is located at the entrance of the dual-axis spiral unloader 20, the discharge bin 21 is located at the exit of the dual-axis spiral unloader 20, and the The outer layer is wrapped with a layer of cooling water, and the top of the discharge bin 21 is provided with a spray device to reduce the temperature and dust of the slag in the bin; the thermal desorption flue gas outlet 83 and the high temperature combustion oxidation system 9 flue gas
  • the air inlet 91 is connected.
  • the high-temperature combustion oxidation system 9 includes a high-temperature combustion chamber.
  • the high-temperature combustion chamber is horizontally installed and coated with refractory around the room.
  • One end of the high-temperature combustion chamber is provided with a flue gas inlet 91 and a high-temperature burner 92.
  • An exhaust gas outlet 93 is provided at one end, and the exhaust gas outlet 93 is connected to the waste heat boiler 13
  • the heat source outlet of the waste heat boiler 13 is connected to the chemical hot wash tank 2 and the sludge dryer 10 through a pipeline.
  • the flue gas outlet of the waste heat boiler is connected to the exhaust gas cooling and dust removal treatment system, and the exhaust gas is discharged to the atmosphere after being processed by the exhaust gas cooling and dust removal treatment system. in.
  • the oil-water separator 4 is composed of a buffer tank 41, a reaction tank 42, an oil storage tank 44 and a water outlet tank 43.
  • the buffer tank 41, the reaction tank 42 and the water outlet tank 43 are arranged in order.
  • the oil storage tank 44 is located in the reaction tank 42. In the upper part, the oil storage tank 44 is connected to the recovery oil tank 5 through a pipeline, and the buffer tank 41 is connected to the liquid outlet of the high-efficiency solid-liquid separator 3 through a pipeline.
  • the exhaust gas cooling and dedusting treatment system includes a quench tower 14, a spray tower 15, a settling tower 16, an induced draft fan 17, and a chimney 18, the spray tower 15 and the settling tower 16 are sequentially penetrated, and the quench tower 14 passes the pipeline and the spray tower 15 is connected, and the outlet of the sedimentation tower 16 is connected to the chimney 18 through a pipeline.
  • An induced draft fan 17 is installed on the pipeline. The exhaust gas is finally processed and discharged to the atmosphere through the chimney 18 under the action of the induced draft fan 17.
  • the metering hopper 73 of the thermal desorption sludge feeding system 7 according to the present invention adopts a biaxial spiral feeding method, and a soil plug is formed through a bottom diameter reduction design to reduce outside air from entering the thermal desorption system 8.
  • the sludge is sent to the sludge homogenization tank 1.
  • the outlet of the sludge homogenization tank 1 is equipped with a grille 27.
  • a sludge dispersant can be added to adjust the dispersibility of the sludge and make the color stripe cloth in the sludge slurry.
  • Garbage debris with a size of ⁇ 10 mm, such as woven bag fragments, labor protection supplies, weeds, brick tiles, and iron wires, are intercepted by the grille 21, and the debris intercepted by the grille 27 is regularly cleaned.
  • the quenched and tempered sludge is pumped into the chemical thermal washing tank 2 through the action of the first mud pump 24.
  • the chemical thermal washing tank 2 is equipped with a dosing system 22, and the stirring blades in the tank put green cleaning agents and hot water and sludge Force sufficient stirring to separate the crude oil from the sludge, and the detached oil is scraped off from the top of the chemical thermal washing tank 2 and stored in the recovery oil tank 5; the solid phase after chemical thermal washing is from the chemical thermal washing tank 2
  • the bottom of the tank enters the high-efficiency solid-liquid separator 3 through the action of the second mud pump 25.
  • the oil content of the sludge separated by the high-efficiency solid-liquid separator 3 is reduced to 3% to 6%, and the water content is about 60% to 70%.
  • the small sludge truck is used to transport the separated sludge to the sludge temporary storage area for temporary storage or direct storage. It is sent to the sludge dryer 10, and the separated sewage enters the oil-water separator 4 through the sewage pump 26.
  • the sewage first enters the buffer tank 41 and then flows into the reaction tank 42 for aeration to separate the oil and water.
  • the oil flows into the oil storage tank 44 and the separated water enters the integrated sewage treatment system 6 from the water outlet tank 43 for processing.
  • the treated water is stored in the water storage tank 23 and used for chemical thermal washing tank 2 in.
  • the moisture content of the dewatered sludge is too high to directly enter the thermal desorption system, so it needs to be dried in the sludge dryer 10 to reduce the moisture content to less than 20%.
  • the drying heat source of the sludge dryer 10 mainly comes from the heat recovered by industrial electricity and waste heat boiler 13.
  • the steam generated during the drying process enters the condensation recovery system 11 for condensation, the oil and water are condensed, and the condensate enters the oil-water separation.
  • Device 4 the recovered oil enters the recovered oil tank 5 and is then transported to a treatment station for processing.
  • the water separated by the oil-water separator 4 enters the integrated sewage treatment system 6 for reuse by the chemical thermal washing tank 2.
  • the non-condensable The light components ie, non-condensable gases
  • the high-temperature burner 92 of the high-temperature combustion oxidation system 9 for complete combustion oxidation, ensuring that the flue gas is fully purified.
  • the oily sludge that has been dried by the sludge dryer 10 is sent to the metering hopper 73 on the top of the thermal desorption system 8 through the feed conveyor 7.
  • the sludge forms a "soil" in the metering hopper 73. Plugging ”can reduce the amount of air entering the thermal desorption system 8 and effectively block the thermal desorption chamber of the thermal desorption system 8 from the atmosphere to ensure that the thermal desorption chamber is in a state of slight negative pressure.
  • Sludge is transported through the stainless steel track 81 in the thermal desorption chamber. The flow direction of the sludge is opposite to the flow direction of the flue gas.
  • a series of thermal desorption burners 82 on the top of the thermal desorption chamber achieve heating of the sludge.
  • the process strictly controls the amount of air entering to ensure that the sludge is desorbed and cracked in the absence of oxygen.
  • the 1000 ° C high-temperature exhaust gas from the high-temperature combustion oxidation system 9 is sent to a waste heat boiler 13 for waste heat recovery, and the superheated steam generated is used by the chemical cleaning tank 2 and the sludge dryer 10.
  • the temperature of the exhaust gas recovered through the waste heat boiler 13 is reduced to below 500 ° C., so that the heat is fully recovered and utilized, the heat is fully recovered and reused, and dioxin is prevented from being regenerated.
  • the intermediate temperature exhaust gas from the waste heat boiler is sent to the quench tower 14 to reduce the temperature of the exhaust gas from 500 ° C to less than 200 ° C within 1 s to avoid the re-generation of dioxin.
  • the cooled exhaust gas enters the spray tower 15 and the sedimentation tower 16 again. Cooling and dust removal and spraying of lye to remove acid gas, and the exhaust gas is discharged to the atmosphere through the chimney after being treated to the standard.
  • the slag treated by the thermal desorption system 8 falls on the discharge hopper 19 under the action of the discharge propeller 84, and is then transported to the discharge bin 21 for storage by the biaxial screw unloader 20, and the biaxial spiral
  • the outer layer of the unloader is wrapped with a layer of cooling water to prevent the discharge temperature from being too high or too high to affect the equipment's operating life.
  • the discharge bin 21 is sealed and the top of the warehouse is equipped with a spray device to reduce the amount of slag in the bin. Temperature and dust, to prevent dust from escaping.
  • the water content is 50%, the oil content is 18%, and the average particle size is less than 5mm.
  • the water content of the sludge is 65%, and the oil content of the sludge is reduced to 6%; after drying, the water content of the sludge is reduced to 20%, and the dried sludge is sent by the feeding system.
  • control the temperature of the sludge in the thermal desorption chamber is 500-700 ° C, the residence time is 20 minutes, and the temperature of the high temperature combustion chamber is controlled at 1100 ° C. 2s.
  • the oil content of the slag after thermal desorption is 220mg / kg, and the removal rate is 99.69%.
  • the dioxin content in the flue gas after the thermal desorption tail gas is purified by high temperature combustion is less than 0.1TEQng / Nm 3 , and all indexes are processed by the exhaust gas treatment system. Meet the emission standards of the Comprehensive Emission Standards for Air Pollutants.
  • the water content is 40%, the oil content is 15%, and the average particle size is less than 10mm.
  • the crude oil recovery rate after cleaning is 80%.
  • the water content of the sludge is 60% to 65%, and the oil content of the sludge is reduced to 3%.
  • the water content of the sludge is reduced to 19%.
  • the dried sludge is fed by the feeding system. It is sent to the metering hopper and falls on the stainless steel track in the thermal desorption system.
  • the temperature range of the sludge in the thermal desorption chamber is 300-500 ° C, and the residence time is 18 minutes.
  • the temperature of the high temperature combustion chamber is controlled at 850 ° C. Stay for 1.5s.
  • the oil content of the slag after thermal desorption is 200mg / kg, and the removal rate is 99.62%.
  • the dioxin content in the flue gas after the thermal desorption exhaust gas is purified by high temperature combustion is less than 0.1TEQng / Nm 3 , and the indicators are processed by the exhaust gas treatment system. Meet the emission standards of the Comprehensive Emission Standards for Air Pollutants.
  • the water content is 55%, the oil content is 25%, and the average particle size is less than 10mm.
  • the water content of the sludge is 60% to 65%, and the oil content of the sludge is reduced to 5%.
  • the water content of the sludge is reduced to 18%.
  • the dried sludge is fed by the feeding system. It is sent to the metering hopper and falls on the stainless steel track in the thermal desorption system.
  • the temperature range of the sludge in the thermal desorption chamber is 400 ⁇ 550 °C, and the residence time is 20min.
  • the temperature of the high temperature combustion chamber is controlled at 950 °C. Stays for 1.8s.
  • the oil content of the slag after thermal desorption is 180mg / kg, and the removal rate is 99.71%.
  • the dioxin content in the flue gas after the thermal desorption tail gas is purified by high temperature combustion is less than 0.1TEQng / Nm 3 , and the indicators are processed by the exhaust gas treatment system. Meet the emission standards of the Comprehensive Emission Standards for Air Pollutants.

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  • Environmental & Geological Engineering (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Water Supply & Treatment (AREA)
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Abstract

一种高浓度石油污泥绿色清洗-热脱附集成技术处理方法及处理系统，该方法包括均质除杂预处理、化学热洗处理、固液分离与油水分离、油泥热脱附及高温燃烧氧化、热交换及尾气降温除尘的处理步骤；该系统包括油泥化学热洗系统和油泥无害化热脱附系统，油泥化学热洗系统由油泥均质槽(1)、油泥化学热洗罐(2)、高效固液分离器(3)、油水分离器(4)、污水一体化处理系统(6)、储水罐(23)依次连接组成，油泥无害化热脱附系统主要由污泥烘干机(10)、冷凝回收系统(11)、热脱附进料系统(7)、热脱附系统(8)、高温燃烧氧化系统(9)、余热锅炉(13)及出料系统组成。该方法采用化学热洗技术与热脱附技术联合运用，可同时实现石油类物质和热量等资源回收利用、含油污泥减量化、无害化等多重功效。

Description

高浓度石油污泥绿色清洗-热脱附集成技术处理方法与处理系统 技术领域
本发明涉及油泥治理技术领域，具体是一种高浓度石油污泥绿色清洗-热脱附集成技术处理方法与处理系统。
背景技术
作为一种化学能源，石油在开采、运输、储存、加工等过程中不可避免地会产生大量的废渣、废水和废气，给社会环境与人类安全带来巨大的潜在威胁。尤其是高浓度的含油污泥含有大量的苯系物、蒽、酚类、芘等有恶臭的有毒物质，含油污泥若得不到及时处理，将会对生产区域和周边环境造成不同程度的影响：含油污泥中的油气挥发，会使生产区域内空气质量总烃浓度超标；散落和堆放的含油污泥污染地表水甚至地下水，使水中COD、BOD和石油类严重超标；含油污泥含有大量的原油，造成土壤中石油类超标，土壤板结，使区域内的植被遭到破坏，草原退化，生态环境受到影响。由于原油中所含的某些烃类物质具有致癌、致畸、致突变作用，油田含油污泥已被列为危险固体废弃物(HW08)进行管理。
通常将含油率大于15％以上的油泥称之为高浓度石油污泥，目前针对高浓度石油污泥有采用热化学清洗的方法进行原油回收，但仅用热化学清洗法，清洗后的油泥依然残留较高的石油含量，无法达到直接排放或利用的标准。如果用直热式热脱附对高浓度的石油污泥直接进行无害化处理，又存在较大的安全隐患，而且存在能耗高和浪费石油资源等缺点。
发明内容
针对现有技术存在的缺点，本发明的目的在于提供一种高浓度石油污泥绿色清洗-热脱附集成技术处理方法与处理系统，它采用清洗技术与热脱附技术联合处理高浓度的石油污泥，既能回收资源，又能安全地对油泥进行无害化处理。
为实现上述目的，本发明采用的技术方案是：
本发明一种高浓度石油污泥绿色清洗-热脱附集成技术处理方法，包括如下处理步骤：
(1)均质除杂预处理：将油泥进行调质、分散处理，并去除油泥浆中的垃圾杂物；
(2)化学热洗处理：将经均质除杂处理后的油泥送入内有热水和清洗剂的化学热洗罐中，通过搅拌，使原油从油泥中脱离出来，脱离出来的油从化学热洗罐的顶部刮出来，存储于回收油罐中，化学热洗后的固相从化学热洗罐的罐底排出送入高效固液分离器中；
(3)固液分离与油水分离：通过高效固液分离器进行固液分离，使分离出的油泥含油率降至3％～6％，含水率为60％～70％，然后将油泥输送至油泥暂存区暂存或直接送入污泥烘干机中，将高效固液分离器分离出的污水送入油水分离器中，将通过油水分离器分离出的油送入回收油罐中，将油水分离器分离出的污水送入污水一体化处理系统中进行处理，将处理后的水储存于储水罐中，回用于化学热洗罐中；
(4)油泥干化及冷凝回收处理：将送入污泥烘干机中的油泥烘干至含水率在20％以下，将干化过程产生的蒸汽送入冷凝回收系统进行冷凝，油和水经冷凝后将冷凝液送入油水分离器进行油水分离；
(5)油泥热脱附处理及高温燃烧氧化处理：将污泥烘干机处理后的含油污泥送入热脱附系统，热脱附系统的热脱附室温度控制在300-750℃之间，并确保热脱附室处于微负压的状态，同时使油泥的输送方向与烟气的流动方向相反，并确保油泥在缺氧的状态下完成脱附裂解；
(6)热交换处理：将步骤(5)中热脱附系统产生的烟气以及步骤(4)中冷凝回收系统产生的不可冷凝的轻质组分输送至高温燃烧氧化系统进行完全燃烧氧化，再将从高温燃烧氧化系统中出来的高温尾气送入到余热锅炉进行余热回收，产生的过热蒸汽作为化学热洗罐和污泥烘干机的热源；
(7)尾气降温除尘处理：将从余热锅炉出来的中温尾气送入急冷塔，通过急冷塔使尾气温度降至200℃以下，再经降温除尘和喷淋碱液以去除酸性气体，尾气经处理达标后通过烟囱排放到大气中。
步骤(6)中，所述高温燃烧氧化系统采用天然气明火燃烧，工作温度在850～1100℃范围内，停留时间1.5～2秒，以确保有机成分彻底无害化消除，同时防止二噁英的产生。
步骤(6)中，高温燃烧氧化系统中出来的高温尾气约1000℃，将其送至余热锅炉进行余热回收后降为500℃的中温尾气。
本发明一种高浓度石油污泥绿色清洗-热脱附集成技术处理系统，主要由油泥化学热洗系统和油泥无害化热脱附系统两部分构成，所述油泥化学热洗系统由油泥均质槽1、化学热洗罐2、高效固液分离器3、油水分离器4、污水一体化处理系统6、储水罐23经管路 依次连接组成，化学热洗罐2的顶部出油口以及油水分离器4的出油口分别经管路与回收油罐5相连接，化学热洗罐2的底部经管路与高效固液分离器3相连接，高效固液分离器3的液体出口与油水分离器4相连接；所述油泥无害化热脱附系统由污泥烘干机10、冷凝回收系统11、热脱附进料系统7、热脱附系统8、高温燃烧氧化系统9、余热锅炉13、尾气降温除尘处理系统及出料系统组成，高效固液分离器3的固体出料口与污泥烘干机10的进料口相连接，污泥烘干机10的蒸汽出口与冷凝回收系统11相连接，冷凝回收系统11的不凝气出口经管路连接高温燃烧氧化系统9，冷凝回收系统11的冷凝液出口经管路连接油水分离器4；污泥烘干机10的固体出料口与热脱附进料系统7相连接，热脱附进料系统7与热脱附系统8相连接，热脱附系统8的热脱附烟气出口83与高温燃烧氧化系统9的烟气进口91相连接，热脱附系统8的出料口与出料系统相连接，高温燃烧氧化系统9的尾气出口93连接余热锅炉13，余热锅炉13的蒸汽出口经管路连接化学热洗罐2和污泥烘干机10，余热锅炉的烟气出口与尾气降温除尘处理系统相连接，尾气经尾气降温除尘处理系统处理后排放到大气中。
本发明所述油水分离器4由缓冲槽41、反应槽42、储油槽44以及出水槽43组成，缓冲槽41、反应槽42及出水槽43依次排布设置，储油槽44位于反应槽42的上部，储油槽44经管路与回收油罐5相连接，缓冲槽41经管路与高效固液分离器3的液体出口相连接。
本发明所述热脱附油泥进料系统7由进料料仓71、皮带输送机72和计量进料斗73组成，进料料仓71位于皮带输送机72的入口，计量进料斗73位于皮带输送机72的出口，计量进料斗73的出口连接热脱附系统8的入料口。
本发明所述热脱附系统8包括涂有耐火材料的热脱附室，热脱附室的顶部安装有一系列热脱附燃烧器82，热脱附燃烧器82的下方设有不锈钢履带式传送带81，热脱附室的一端设有入料口，另一端设有卸料推进器84，热脱附室的顶部设置热脱附烟气出口83。
本发明所述高温燃烧氧化系统9包括高温燃烧室，高温燃烧室的一端设置烟气进气口91以及高温燃烧器92，另一端设置尾气出口93，尾气出口93与余热锅炉13相接。
本发明所述尾气降温除尘处理系统包括急冷塔14、喷淋塔15、沉降塔16、引风机17和烟囱18，喷淋塔15与沉降塔16相贯通，急冷塔14经管路与喷淋塔15相连接，沉降塔16的出口经管路连接烟囱18，该管路上安装有引风机17。
本发明所述出料系统由出料料斗19、双轴螺旋卸料机20和出料料仓21组成，出料料 斗19位于双轴螺旋卸料机20的入口，出料料仓21位于双轴螺旋卸料机20的出口，双轴螺旋卸料机20的外层裹着一层降温水层，出料料仓21顶部设有喷淋装置，以降低料仓内渣土的温度和扬尘。
与现有技术相比，本发明具有以下优点：
(1)本发明采用的清洗药剂绿色环保，清洗效果显著，清洗后油水固三相分层效率快，油回收率高。
(2)本发明的热脱附系统采用耐高温耐腐蚀不锈钢履带传输，直接火焰方式加热油泥，脱附效率高，处理能力大，可以实现高操作温度和停留时间。
(3)本发明整个系统保持在微负压状态下，正常情况下可确保污染物和粉尘不外溢，防止二次污染。
(4)采用的高温燃烧室长度足够长，停留时间足够长，补充的空气过量，燃烧温度足够高，实现3T焚烧，确保有机气体完全燃烧，可有效防止二噁英产生。
(5)对整个系统的余热进行回收利用，节约能耗，降低能耗成本。
(6)采用化学热洗技术与热脱附技术联合运用，可同时实现石油类物质和热量等资源的回收利用、含油污泥减量化、无害化等多重功效。
附图说明
图1是本发明高浓度石油污泥绿色清洗-热脱附集成技术处理方法的工艺流程图。
图2是本发明高浓度石油污泥绿色清洗-热脱附集成技术处理系统的结构示意图。
图中：油泥均质槽1，化学热洗罐2，高效固液分离器3，油水分离器4，污水缓冲槽41，反应槽42，储油槽44，出水槽43，回收油罐5，污水一体式处理系统6，热脱附进料系统7，进料料仓71，皮带输送机72，计量进料斗73，热脱附系统8，不锈钢履带81，热脱附燃烧器82，热脱附烟气出口83，卸料推进器84，高温燃烧氧化系统9，烟气进口91，高温燃烧器92，高温尾气出口93，污泥烘干机10，冷凝回收系统11，冷凝泵12，余热锅炉13，急冷塔14，喷淋塔15，沉降塔16，引风机17，烟囱18，出料料斗19，双轴螺旋输送机20，出料料仓21，加药系统22，储水罐23，第一泥浆泵24，第二泥浆泵25，污水泵26，格栅27。
具体实施方式
下面结合附图对本发明的技术方案作进一步的说明。
如图1所示，本发明高浓度石油污泥绿色清洗-热脱附集成技术处理方法，包括如下处 理步骤：
(1)均质除杂预处理：将油泥进行调质、分散预处理，调质过程中可加入油泥分散剂来调节油泥的分散性，使油泥浆中的彩条布编织袋碎片、劳保用品、野草、砖头瓦块、铁丝等尺寸≥10毫米垃圾杂物被格栅拦截下来，并定期清理格栅拦截的杂物。
(2)化学热洗处理：将经均质除杂处理后的油泥送入内有热水(60～80℃)和清洗剂(如碱液、表面活性剂等)的化学热洗罐中，化学热洗罐配备有用于添加清洗剂的加药系统，通过罐内的搅拌桨把绿色环保的清洗剂和热水与油泥强制充分搅拌，使原油从油泥中脱离出来，脱离出来的油从化学热洗罐的顶部刮出来，存储于回收油罐中，化学热洗后的固相从化学热洗罐的罐底排出送入高效固液分离器中。
(3)固液分离与油水分离：通过高效固液分离器进行固液分离，使分离出的油泥含油率降至3％～6％，含水率为60％～70％，采用小型翻斗车将分离后的油泥输送至油泥暂存区暂存或直接送入污泥烘干机中，将高效固液分离器分离出的污水送入油水分离器中，将通过油水分离器分离出的油送入回收油罐中，将油水分离器分离出的污水送入污水一体化处理系统(该设备的结构可采用中国专利号ZL201220225085.X公开的《重金属废水成套处理设备》，也可以采用其它实现污水处理的设备)中进行处理，将处理后的水储存于储水罐中，回用于化学热洗罐中。
(4)油泥干化及冷凝回收处理：脱水后的污泥含水率60％左右，无法直接进入热脱附系统，故需将送入污泥烘干机中的油泥烘干至含水率在20％以下，污泥烘干机的热源主要来源于电和余热锅炉回收的热量，将干化过程产生的蒸汽送入冷凝回收系统进行冷凝，油和水经冷凝后将冷凝液送入油水分离器进行油水分离，回收的油收集后外运至处理站处理，分离的水进入污水一体化处理系统中，供油泥化学热洗罐再次利用，不可冷凝的轻质组分(即不凝气体)输送至高温燃烧氧化系统进行完全燃烧氧化，确保烟气得到充分净化处理。
(5)油泥热脱附处理及高温燃烧氧化处理：将污泥烘干机处理后的含油污泥通过进料系统送入热脱附系统，油泥的连续进料使进料口形成了一个“土塞”，可减少进入热脱附系统的空气量，并将热脱附系统与大气有效阻隔，确保热脱附室处于微负压的状态。油泥在热脱附室内通过不锈钢履带传送，油泥的流动方向与烟气流动方向相反，在传送的过程中，由热脱附系统顶部的一系列热脱附燃烧器实现对油泥的加热，整个过程严格控制空气的进入量，确保油泥在缺氧的状态下脱附裂解。根据油泥的类型以及含水率的不同，热 脱附室的温度可以设置在300至750℃之间，以确保油泥中的各种烃馏分完全脱附出来。热脱附系统出来的热脱附烟气进入到高温燃烧氧化系统中，高温燃烧氧化系统采用天然气明火燃烧，工作温度在850～1100℃范围内，停留时间1.5～2秒，以确保从不凝气中的石油烃等有机成分彻底无害化消除，同时防止二噁英的产生。
(6)热交换处理：将步骤(5)中热脱附系统产生的烟气以及步骤(4)中冷凝回收系统产生的不可冷凝的轻质组分输送至高温燃烧氧化系统进行完全燃烧氧化，再将从高温燃烧氧化系统中出来的约1000℃高温尾气送入到余热锅炉进行余热回收，经余热锅炉回收后降为500℃的中温尾气，同时将产生的过热蒸汽作为化学热洗罐和污泥烘干机的热源。
(7)尾气降温除尘处理：将从余热锅炉出来的中温尾气送入急冷塔，通过急冷塔使尾气温度从500℃在1s内降至200℃以下，避免二噁英的再次生成，然后再经降温除尘和喷淋碱液以去除酸性气体，尾气经处理达标后通过烟囱排放到大气中。
实施上述方法采用的处理系统结构如图2所示：
本发明处理系统包括油泥化学热洗系统与油泥无害化热脱附系统两部分。
所述油泥化学热洗系统是由油泥均质槽1、化学热洗罐2、高效固液分离器3、油水分离器4、污水一体化处理系统6、储水罐23经管路依次连接组成，所述油泥均质槽1内设格栅27，油泥均质槽1出料口通过第一污泥泵24与化学热洗罐2的进口相连接，化学热洗罐2配套有用于添加清洗剂的加药系统22，化学热洗罐2内设有搅拌浆，化学热洗罐2的顶部出油口经管路与回收油罐5相连接，化学热洗罐2的底部出料口通过第二污泥泵25与高效固液分离器3的进口相连接，高效固液分离器3的固体出料口与油泥烘干机10的进料口相连接，高效固液分离器3的液体出口则通过污水泵26与油水分离器4的进口相连接，油水分离器4的出水口与污水一体化处理系统6的进水口相连接，污水一体化处理系统6的出水口与储水罐23的进口相连接，储水罐23的水最终又回到化学热洗罐2中回用。
所述油泥无害化热脱附系统由污泥烘干机10、冷凝回收系统11、热脱附进料系统7、热脱附系统8、高温燃烧氧化系统9、余热锅炉13、尾气降温除尘处理系统及出料系统组成，污泥烘干机10的蒸汽出口与冷凝回收系统11相连接，冷凝回收系统11的不凝气体出口经管路连接高温燃烧氧化系统9，以进行回收利用，冷凝回收系统11的冷凝液出口经管路连接油水分离器4，该管路上安装有冷凝泵12；所述污泥烘干机10的固体出料口与热脱附进料系统7相连接，热脱附进料系统7包括进料料仓71、皮带输送机72和计量进 料斗73，进料料仓71位于皮带输送机72的入口端，计量进料斗73位于皮带输送机72的出口端，进料料仓71与污泥烘干机10的固体出料口相连接，热脱附进料系统7的计量进料斗73安装在热脱附系统8的入料口，热脱附系统8包括涂有耐火材料的热脱附室，热脱附室的顶部安装有均匀错落在中心线两侧的一系列热脱附燃烧器82，热脱附燃烧器82的下方设有不锈钢履带式传送带81，热脱附室的一端设有入料口，另一端设有卸料推进器84，热脱附室的顶部设置热脱附烟气出口83，卸料推进器84与出料系统相连接，所述出料系统由出料料斗19、双轴螺旋卸料机20和出料料仓21组成，出料料斗19位于双轴螺旋卸料机20的入口，出料料仓21位于双轴螺旋卸料机20的出口，双轴螺旋卸料机20的外层裹着一层降温水层，出料料仓21顶部设有喷淋装置，以降低料仓内渣土的温度和扬尘；热脱附烟气出口83与高温燃烧氧化系统9的烟气进气口91相连接，高温燃烧氧化系统9包括高温燃烧室，高温燃烧室水平安装并且在室内周围涂有耐火材料，高温燃烧室的一端设置烟气进气口91以及高温燃烧器92，另一端设置尾气出口93，尾气出口93与余热锅炉13相接，余热锅炉13的热源出口经管路连接化学热洗罐2和污泥烘干机10，余热锅炉的烟气出口与尾气降温除尘处理系统相连接，尾气经尾气降温除尘处理系统处理后排放到大气中。
本发明所述油水分离器4由缓冲槽41、反应槽42、储油槽44以及出水槽43组成，缓冲槽41、反应槽42及出水槽43依次排布设置，储油槽44位于反应槽42的上部，储油槽44经管路与回收油罐5相连接，缓冲槽41经管路与高效固液分离器3的液体出口相连接。
本发明所述尾气降温除尘处理系统包括急冷塔14、喷淋塔15、沉降塔16、引风机17和烟囱18，喷淋塔15与沉降塔16顺序贯通，急冷塔14经管路与喷淋塔15相连接，沉降塔16的出口经管路连接烟囱18，该管路上安装有引风机17，尾气最终经处理达标在引风机17作用下通过烟囱18排放到大气中。
本发明所述热脱附油泥进料系统7的计量进料斗73采用双轴螺旋进料方式，通过底部变径设计形成土塞，减少外界空气进入到热脱附系统8中。
本发明处理系统的工作过程如下：
将污泥送入油泥均质槽1，油泥均质槽1的出水口处装有格栅27，调质过程中可加入油泥分散剂来调节油泥的分散性，使油泥浆中的彩条布编织袋碎片、劳保用品、野草、砖头瓦块、铁丝等尺寸≥10毫米垃圾杂物被格栅21拦截下来，并定期清理格栅27拦截的杂 物。
将调质后的油泥经过第一泥浆泵24的作用泵入化学热洗罐2，化学热洗罐2配备了加药系统22，罐内的搅拌桨把绿色环保的清洗剂和热水与油泥强制充分搅拌，使原油从油泥中脱离出来，脱离出来的油从化学热洗罐2的顶部刮出来，存储于回收油罐5中；化学热洗后的固相则从化学热洗罐2的罐底通过第二泥浆泵25的作用下进入到高效固液分离器3中。
通过高效固液分离器3分离出的污泥含油率降至3％～6％，含水率60％～70％左右，采用小型翻斗车将分离后的油泥输送至油泥暂存区暂存或直接送入污泥烘干机10中，分离出的污水则经过污水泵26进入到油水分离器4中，污水先进入缓冲槽41，再流入到反应槽中42进行曝气使油水分离，分离出的油流入储油槽44中，分离出的水从出水槽43进入到污水一体化处理系统6中进行处理，经处理后的水储存于储水罐23中，并回用于化学热洗罐2中。
脱水后的污泥含水率太高，无法直接进入热脱附系统，故需置于污泥烘干机10中干化处理，使其含水率降至20％以下。污泥烘干机10的干化热源主要来源于工业用电和余热锅炉13回收的热量，干化过程产生的蒸汽进入冷凝回收系统11进行冷凝，油和水被冷凝下来，冷凝液进入油水分离器4，将回收的油进入回收油罐5后外运至处理站处理，经油水分离器4分离出的水进入污水一体化处理系统6中，供化学热洗罐2再次利用，不可冷凝的轻质组分(即不凝气体)输送至高温燃烧氧化系统9的高温燃烧器92进行完全燃烧氧化，确保烟气得到充分净化处理。
将经污泥烘干机10干化处理后的含油污泥通过进料输送机7送入热脱附系统8顶部的计量进料斗73，油泥在计量进料斗73内形成了一个“土塞”，可减少进入热脱附系统8的空气量，并将热脱附系统8的热脱附室与大气有效阻隔，确保热脱附室处于微负压的状态。油泥在热脱附室内通过不锈钢履带81传送，油泥的流动方向与烟气流动方向相反，在传送的过程中，热脱附室顶部的一系列热脱附燃烧器82实现对油泥的加热，整个过程严格控制空气的进入量，确保油泥在缺氧的状态下脱附裂解。将从高温燃烧氧化系统9中出来的1000℃高温尾气送入到余热锅炉13进行余热回收，产生的过热蒸汽供化学清洗罐2和污泥烘干机10使用。将经过余热锅炉13回收的尾气温度降至500℃以下，既充分回收利用热量，既充分回收利用热量，又避免二噁英重新生成。将从余热锅炉出来的中温尾气送入急冷塔14使尾气温度从500℃在1s内降至200℃以下，避免二噁英的再次生成，降 温后的尾气进入喷淋塔15和沉降塔16再次降温除尘和喷淋碱液除去酸性气体，尾气经处理达标后通过烟囱排放到大气中。
经热脱附系统8处理后的渣土在卸料推进器84的作用下，落到出料料斗19上，再由双轴螺旋卸料机20输送到出料料仓21储存，双轴螺旋卸料机外层裹着一层降温水层，防止出料温度过高过高影响设备运行寿命，出料料仓21采用密闭设置，仓库顶部设有喷淋装置，降低料仓内渣土的温度和扬尘，防止扬尘外逸。
以下是本发明的应用实例：
实例一：
以某油田的罐底油泥为处理对象，其含水率为50％，含油率为18％，平均颗粒粒径小于5mm，经调质后进入化学热洗罐清洗，清洗后原油回收率为66.7％，经高效固液分离器处理后污泥含水率为65％，污泥含油率降至6％；经烘干后污泥含水率降至20％，烘干后的污泥由进料系统送至计量进料斗，并落入热脱附系统中的不锈钢履带上，控制油泥在热脱附室的温度范围为500～700℃，停留时间20min，高温燃烧室的温度控制在1100℃，停留2s。热脱附后的渣土含油量为220mg/kg，去除率达99.69％，热脱附尾气经高温燃烧净化烟气中二噁英含量小于0.1TEQng/Nm 3，经尾气处理系统处理后各指标达到《大气污染物综合排放标准》的排放标准。
实例二：
以某油田的落地油泥为处理对象，其含水率为40％，含油率为15％，平均颗粒粒径小于10mm，经调质后进入化学热洗罐清洗，清洗后原油回收率为80％，经高效固液分离器处理后污泥含水率60％～65％，污泥含油率降至3％；经烘干后污泥含水率降至19％，烘干后的污泥由进料系统送至计量进料斗，并落入热脱附系统中的不锈钢履带上，控制油泥在热脱附室的温度范围为300～500℃，停留时间18min，高温燃烧室的温度控制在850℃，停留1.5s。热脱附后的渣土含油量为200mg/kg，去除率达99.62％，热脱附尾气经高温燃烧净化烟气中二噁英含量小于0.1TEQng/Nm 3，经尾气处理系统处理后各指标达到《大气污染物综合排放标准》的排放标准。
实例三：
以某油田的油泥砂为处理对象，其含水率为55％，含油率为25％，平均颗粒粒径小于10mm，经调质后进入化学热洗罐清洗，清洗后原油回收率为80％，经高效固液分离器处 理后污泥含水率60％～65％，污泥含油率降至5％；经烘干后污泥含水率降至18％，烘干后的污泥由进料系统送至计量进料斗，并落入热脱附系统中的不锈钢履带上，控制油泥在热脱附室的温度范围为400～550℃，停留时间20min，高温燃烧室的温度控制在950℃，停留1.8s。热脱附后的渣土含油量为180mg/kg，去除率达99.71％，热脱附尾气经高温燃烧净化烟气中二噁英含量小于0.1TEQng/Nm 3，经尾气处理系统处理后各指标达到《大气污染物综合排放标准》的排放标准。

Claims (10)

  1. 一种高浓度石油污泥绿色清洗-热脱附集成技术处理方法，其特征在于，它包括如下处理步骤：
    (1)均质除杂预处理：将油泥进行调质、分散处理，并去除油泥浆中的垃圾杂物；
    (2)化学热洗处理：将经均质除杂处理后的油泥送入内有热水和清洗剂的化学热洗罐中，通过搅拌，使原油从油泥中脱离出来，脱离出来的油从化学热洗罐的顶部刮出来，存储于回收油罐中，化学热洗后的固相从化学热洗罐的罐底排出送入高效固液分离器中；
    (3)固液分离与油水分离：先通过高效固液分离器进行固液分离，使分离出的油泥含油率降至3％～6％，含水率为60％～70％，然后将油泥输送至油泥暂存区暂存或直接送入污泥烘干机中，将高效固液分离器分离出的污水送入油水分离器中，通过油水分离器分离出的油送入回收油罐中，将油水分离器分离出的污水送入污水一体化处理系统中进行处理，将处理后的水储存于储水罐中，回用于化学热洗罐中；
    (4)油泥干化及冷凝回收处理：将送入污泥烘干机中的油泥烘干至含水率在20％以下，将干化过程产生的蒸汽送入冷凝回收系统进行冷凝，油和水经冷凝后将冷凝液送入油水分离器进行油水分离；
    (5)油泥热脱附处理及高温燃烧氧化处理：将污泥烘干机处理后的含油污泥送入热脱附系统，热脱附系统的热脱附室温度控制在300-750℃之间，并确保热脱附室处于微负压的状态，同时使油泥的输送方向与烟气的流动方向相反，并确保油泥在缺氧的状态下完成脱附裂解；
    (6)热交换处理：将步骤(5)中热脱附系统产生的烟气以及步骤(4)中冷凝回收系统产生的不可冷凝的轻质组分输送至高温燃烧氧化系统进行完全燃烧氧化，再将从高温燃烧氧化系统中出来的高温尾气送入到余热锅炉进行余热回收，产生的过热蒸汽作为化学热洗罐和污泥烘干机的热源；
    (7)尾气降温除尘处理：将从余热锅炉出来的中温尾气送入急冷塔，通过急冷塔使尾气温度降至200℃以下，再经降温除尘和喷淋碱液以去除酸性气体，尾气经处理达标后通过烟囱排放到大气中。
  2. 根据权利要求1所述浓度石油污泥绿色清洗-热脱附集成技术处理方法，其特征在于，步骤(6)中，所述高温燃烧氧化系统采用天然气明火燃烧，工作温度在850～1100℃ 范围内，停留时间1.5～2秒，以确保有机成分彻底无害化消除，同时防止二噁英的产生。
  3. 根据权利要求1或2所述浓度石油污泥绿色清洗-热脱附集成技术处理方法，其特征在于，步骤(6)中，高温燃烧氧化系统中出来的高温尾气约1000℃，将其送至余热锅炉进行余热回收后降为500℃的中温尾气。
  4. 一种高浓度石油污泥绿色清洗-热脱附集成技术处理系统，其特征在于，它主要由油泥化学热洗系统和油泥无害化热脱附系统两部分构成，所述油泥化学热洗系统由油泥均质槽(1)、化学热洗罐(2)、高效固液分离器(3)、油水分离器(4)、污水一体化处理系统(6)、储水罐(23)经管路依次连接组成，化学热洗罐(2)的顶部出油口以及油水分离器(4)的出油口分别经管路与回收油罐(5)相连接，化学热洗罐(2)的底部经管路与高效固液分离器(3)相连接，高效固液分离器(3)的液体出口与油水分离器(4)相连接；所述油泥无害化热脱附系统由污泥烘干机(10)、冷凝回收系统(11)、热脱附进料系统(7)、热脱附系统(8)、高温燃烧氧化系统(9)、余热锅炉(13)、尾气降温除尘处理系统及出料系统组成，高效固液分离器(3)的固体出料口与污泥烘干机(10)的进料口相连接，污泥烘干机(10)的蒸汽出口与冷凝回收系统(11)相连接，冷凝回收系统(11)的不凝气出口经管路连接高温燃烧氧化系统(9)，冷凝回收系统(11)的冷凝液出口经管路连接油水分离器(4)；污泥烘干机(10)的固体出料口与热脱附进料系统(7)相连接，热脱附进料系统(7)与热脱附系统(8)相连接，热脱附系统(8)的热脱附烟气出口(83)与高温燃烧氧化系统(9)的烟气进口(91)相连接，热脱附系统(8)的出料口与出料系统相连接，高温燃烧氧化系统(9)的尾气出口(93)连接余热锅炉(13)，余热锅炉(13)的蒸汽出口经管路连接化学热洗罐(2)和污泥烘干机(10)，余热锅炉的烟气出口与尾气降温除尘处理系统相连接，尾气经尾气降温除尘处理系统处理后排放到大气中。
  5. 根据权利要求4所述高浓度石油污泥绿色清洗-热脱附集成技术处理系统，其特征在于，所述油水分离器(4)由缓冲槽(41)、反应槽(42)、储油槽(44)以及出水槽(43)组成，缓冲槽(41)、反应槽(42)及出水槽(43)依次排布设置，储油槽(44)位于反应槽(42)的上部，储油槽(44)经管路与回收油罐(5)相连接，缓冲槽(41)经管路与高效固液分离器(3)的液体出口相连接。
  6. 根据权利要求4或5所述高浓度石油污泥绿色清洗-热脱附集成技术处理系统，其特征在于，所述热脱附油泥进料系统(7)由进料料仓(71)、皮带输送机(72)和计量进料斗(73)组成，进料料仓(71)位于皮带输送机(72)的入口，计量进料斗(73)位于 皮带输送机(72)的出口，计量进料斗(73)的出口连接热脱附系统(8)的入料口。
  7. 根据权利要求4或5所述高浓度石油污泥绿色清洗-热脱附集成技术处理系统，其特征在于，所述热脱附系统(8)包括涂有耐火材料的热脱附室，热脱附室的顶部安装有一系列热脱附燃烧器(82)，热脱附燃烧器(82)的下方设有不锈钢履带式传送带(81)，热脱附室的一端设有入料口，另一端设有卸料推进器(84)，热脱附室的顶部设置热脱附烟气出口(83)。
  8. 根据权利要求4或5所述高浓度石油污泥绿色清洗-热脱附集成技术处理系统，其特征在于，所述高温燃烧氧化系统(9)包括高温燃烧室，高温燃烧室的一端设置烟气进气口(91)以及高温燃烧器(92)，另一端设置尾气出口(93)，尾气出口(93)与余热锅炉(13)相接。
  9. 根据权利要求4或5所述高浓度石油污泥绿色清洗-热脱附集成技术处理系统，其特征在于，所述尾气降温除尘处理系统包括急冷塔(14)、喷淋塔(15)、沉降塔(16)、引风机(17)和烟囱(18)，喷淋塔(15)与沉降塔(16)相贯通，急冷塔(14)经管路与喷淋塔(15)相连接，沉降塔(16)的出口经管路连接烟囱(18)，该管路上安装有引风机(17)。
  10. 根据权利要求4或5所述高浓度石油污泥绿色清洗-热脱附集成技术处理系统，其特征在于，所述出料系统由出料料斗(19)、双轴螺旋卸料机(20)和出料料仓(21)组成，出料料斗19位于双轴螺旋卸料机20的入口，出料料仓21位于双轴螺旋卸料机20的出口，双轴螺旋卸料机(20)的外层裹着一层降温水层，出料料仓(21)顶部设有喷淋装置，以降低料仓内渣土的温度和扬尘。
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CN117534282A (zh) * 2023-12-11 2024-02-09 蓬莱荣洋钻采环保服务有限公司 一种油田中油泥的热解处理装置
CN117534282B (zh) * 2023-12-11 2024-05-17 蓬莱荣洋钻采环保服务有限公司 一种油田中油泥的热解处理装置

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