CN112573784A - Method for treating oily sludge by utilizing atmospheric and vacuum distillation/cracking device - Google Patents
Method for treating oily sludge by utilizing atmospheric and vacuum distillation/cracking device Download PDFInfo
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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
- C02F11/002—Sludge treatment using liquids immiscible with water
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- 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
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
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- 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
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
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- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/365—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds from petrochemical industry (e.g. refineries)
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- 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
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Abstract
The invention discloses a method for treating oily sludge by utilizing an atmospheric and vacuum distillation/cracking device, belonging to the technical field of petrochemical production. The disposal method comprises the following steps: firstly, carrying out drying separation on pretreated oily sludge, enabling gas phase generated in the separation process to enter a condenser, enabling liquid phase collected by the condenser to enter an oil-water separator, discharging water phase collected by the condenser into an oily sewage pipeline, and enabling non-condensable gas in the condenser to be merged into an atmospheric and vacuum distillation/cracking device; then, adding an extracting agent into a solid phase generated by drying separation and an oil phase obtained by separation of an oil-water separator, sending a mixed substance into a solid-liquid separator after extraction is finished, sending the separated solid phase into an evaporator, returning the evaporated oil phase to the oil-water separator, and discharging the evaporated residual solid phase up to the standard; and finally, the liquid phase obtained by the separation of the solid-liquid separator enters an atmospheric and vacuum distillation/cracking device. The invention utilizes the existing conditions of the refining enterprises to fully recover the valuable components in the sludge, and the disposal process can not cause secondary pollution.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry production, and particularly relates to a method for treating oily sludge by using an atmospheric and vacuum distillation device/a catalytic cracking device/a hydrocracking device, which is particularly suitable for oily sludge generated in the refining and wastewater treatment processes of petroleum in an oil refinery.
Background
Oily sludge (HW08, HW11, etc.) was listed in the national records of hazardous waste for 2016, incorporated into hazardous waste management. At present, the oil-containing sludge generates about 100 million tons every year, the sludge has complex components, high viscosity and high water content, and the treatment is not suitable. The hazardous waste generated by the state-regulated enterprises must be treated by a third party with the capital of hazardous waste treatment, thereby greatly increasing the burden of the enterprises and the environment.
The oil-containing sludge generation is mainly concentrated in the refining industry, and many researchers put forward their ideas on how to treat a large amount of oil-containing sludge. Most of treatment equipment, technologies and processes are only considered from the perspective of recycling and harmlessness of hazardous wastes, but have the problems of high treatment cost, long process flow, complex operation, non-ideal effect, narrow application range and the like, and cannot treat sludge by utilizing the existing conditions of enterprises from the practical perspective of the enterprises.
The prior art reports on the research related to the treatment of oily sludge mainly include:
US4666585 discloses a technical route for treating oily sludge in a coking device, which comprises stirring and mixing the fraction oil of coking with the oily sludge to obtain slurry oil, and feeding the slurry oil into the coking device. This process can introduce more moisture and ash, affect the normal operation of the coker, and can limit the capacity of the coker. The technology is only suitable for the production device of the product coke as fuel coke, and is not suitable for the production device of the product coke as electrode coke.
CN1488591A discloses a method for treating oily sludge, which comprises the steps of mechanically dehydrating the oily sludge, mixing with an extracting agent, preheating, homogenizing, carrying out thermal extraction-dehydration treatment, carrying out solid-liquid separation, feeding a liquid phase into a coking device, and taking a solid phase as a fuel. In the technology, the oily sludge is only mechanically dehydrated before extraction, the dehydration degree is low, oil-water-solid in the dehydrated oily sludge is still a stable system, the extraction is not thorough, the extracted residues can meet the requirement of harmlessness only by burning, the extraction temperature is high (100-150 ℃), and the energy consumption in the treatment process is high.
CN208532564U discloses an oily sludge treatment system, and the system contains pretreatment systems, fatlute separation system, silt separation system, mud-water separation system, film curing system, full cycle dry distillation system, heating system, clear water system sewage case and oil storage tank. Because the system is relatively independent and lacks the cooperation of an external system to the system, the substances processed in each link need to be stored and disposed separately, and the overall processing system has long flow and is complex.
CN102050556B discloses a method for treating oil-containing sludge, which comprises the steps of dehydrating the oil-containing sludge, drying, separating partial oil and water from the oil-containing sludge, extracting and drying the dried solid phase, wherein the slag phase meets the discharge standard of common solid wastes, and extracting the liquid phase to enter a delayed coking device. However, the method needs to separately establish a set of waste gas treatment device, so that the cost is increased; meanwhile, the method is realized by recycling valuable components in the oil sludge to the delayed coking device, and the popularization degree of the domestic delayed coking device is not as good as that of an atmospheric and vacuum distillation device at present, so that the application range is limited.
In view of the foregoing, the prior art is yet to be further improved.
Disclosure of Invention
The invention aims to provide a method for treating oily sludge by using an atmospheric and vacuum distillation/cracking device, which is used for fully recovering valuable components in the sludge by using the existing conditions of refining enterprises from the viewpoint of reduction of the oily sludge and does not cause secondary pollution in the treatment process.
The technical solution comprises:
a method for disposing oily sludge by utilizing an atmospheric and vacuum distillation/cracking device sequentially comprises the following steps:
s1, drying and separating the pretreated oily sludge, feeding a gas phase generated in the separation process into a condenser, feeding a liquid phase collected by the condenser into an oil-water separator, discharging a water phase collected by the condenser into an oily sewage pipeline, and merging non-condensable gas in the condenser into the atmospheric and vacuum distillation/cracking device;
s2, adding an extracting agent into the solid phase generated by drying and separating in the step S1 and the oil phase obtained by separating in the oil-water separator for extraction reaction, after extraction is finished, sending the mixed substance into a solid-liquid separator, sending the solid phase obtained by separating in the solid-liquid separator into an evaporator, returning the oil phase evaporated by the evaporator to the oil-water separator in the step S1, and discharging the evaporated residual solid phase up to the standard;
s3, feeding the liquid phase separated by the solid-liquid separator into an atmospheric and vacuum distillation/cracking device.
Further, in step S1, the pretreatment is to dehydrate the oily sludge by simple machinery, and the water content of the oily sludge is not less than 50%.
Further, in step S1, drying separation is performed in a drying separator, and the relevant process conditions of the drying separation are as follows: the pressure is 50-105KPa, the temperature is 100-250 ℃, and the processing time is 60-90 minutes.
Further, in step S1, the cracking device is a catalytic cracking device or a hydrocracking device, and when the non-condensable gas in the condenser is merged into the atmospheric and vacuum distillation device, the non-condensable gas is specifically merged into a three-top gas recovery system arranged in the atmospheric and vacuum distillation device, and is introduced into a heating furnace as a fuel for digestion; when the non-condensable gases in the condenser are incorporated into the catalytic cracking unit, they are specifically incorporated into the off-gas treatment unit of the catalytic cracking unit; when the non-condensable gas in the condenser is merged into the hydrocracking device, the non-condensable gas in the condenser and the flue gas generated by a heating furnace of the hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney.
Further, in step S2, the extraction reaction temperature is 20-80 ℃, the extraction time is 10-30 minutes, and the solid-liquid mass ratio is 1-100: 1; the extractant is crude light oil produced by atmospheric and vacuum distillation or light oil produced by a catalytic cracking unit or raw oil of a hydrocracking unit.
Further, in step S2, the evaporator is evaporated for 60-90 minutes at an evaporation temperature of 105-200 ℃ and an absolute pressure of 50-105 KPa.
Preferably, in step S3, the liquid phase separated by the solid-liquid separator enters an electric desalting tank of an atmospheric and vacuum distillation apparatus, and then the reaction is carried out according to the operating conditions of the atmospheric and vacuum distillation process; or the liquid phase obtained by the separation of the solid-liquid separator enters a reaction-regeneration system in the catalytic cracking device, and then the reaction is carried out according to the operating conditions of the reaction-regeneration system; or the liquid phase obtained by the separation of the solid-liquid separator enters the raw oil in the hydrocracking device, the subsequent reaction is carried out according to the hydrocracking process operation conditions, and valuable components in the oily sludge are recycled to the hydrocracking device.
Further preferably, the crude light oil produced by the atmospheric and vacuum distillation unit comprises crude gasoline, gas oil, crude kerosene or naphtha.
Further preferably, the light oil produced by the catalytic cracking unit is gasoline, diesel oil or kerosene.
More preferably, the raw material oil of the hydrocracking unit is crude gasoline, gas oil, vacuum distillate, wax oil or gas oil.
Preferably, the oily sludge comprises oil-containing sludge produced in oil field exploitation and refining enterprises in petroleum refining and wastewater treatment processes, such as ground sludge, tank cleaning sludge, scum bottom sludge, three-separator sludge, oil-overflowing sludge produced in production accidents, and oil sludge in oil interceptors, flotation tanks, residual activated sludge, crude oil dehydration tanks, oil storage tanks and oil sludge tanks.
Compared with the prior art, the invention has the following beneficial technical effects:
in the method for treating the oily sludge, part of the process is directly embedded into an atmospheric and vacuum distillation device, a catalytic cracking device or a hydrocracking device, so that the clean production of sludge reduction is realized, the sludge treatment process is simple, the treatment effect is good, the equipment construction cost is low, the operation energy consumption is low, the maintenance is easy, and the application range is wide.
All heating and heat preservation processes related to the oily sludge treatment process can be heated by a thermal system of an atmospheric and vacuum distillation device or other thermal systems, and when the temperature does not meet the operation conditions, the equipment is started to self-heat.
All the heating and heat preservation processes related to the oily sludge treatment process can be heated by using a thermal system of a catalytic cracking unit or other thermal systems, and when the temperature does not meet the operation condition, the equipment is started to self-heat.
All temperature rising and heat preservation processes related to the oily sludge treatment process can utilize the recovered waste heat of the hydrocracking device, and when the temperature does not meet the operation conditions, the device is started to self-heat.
Drawings
The invention is further described below with reference to the accompanying drawings:
FIG. 1 is a flow diagram of the process of the present invention embedded in an atmospheric and vacuum distillation unit;
FIG. 2 is a flow diagram of the process of the present invention as inserted into a catalytic cracking unit;
FIG. 3 is a flow diagram of the process of the present invention as it is inserted into a hydrocracking unit.
Detailed Description
The invention provides a method for treating oily sludge by utilizing an atmospheric and vacuum distillation/cracking device, and in order to make the advantages and technical scheme of the invention clearer and clearer, the invention is described in detail by combining specific examples.
The cracking device mainly comprises a catalytic cracking device and a hydrocracking device;
the atmospheric and vacuum distillation device, the catalytic cracking device and the hydrocracking device are all the devices in the prior art, no special modification is needed, the specific structure can be realized by referring to the prior art, and detailed description is omitted.
The method for disposing the oily sludge is embedded into an atmospheric and vacuum distillation device and is explained by combining figure 1 and examples 1-6.
Example 1:
oily sludge (with the water content of 80.3 wt%, the oil content of 15.4 wt% and the solid content of 4.3 wt%) generated by a certain refinery is sent into a drying separator (the pressure is 50KPa at absolute pressure and the temperature is 250 ℃ for drying treatment for 80 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser is merged into a three-top gas recovery system arranged by atmospheric and vacuum distillation, and the condensed gas is introduced into a heating furnace to be used as fuel for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 15 minutes, and the solid-liquid ratio is 80: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to the oil-water separator, evaporating at 130 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into an electric desalting tank in an atmospheric and vacuum distillation device, subsequently reacting according to the operating conditions of the atmospheric and vacuum distillation process, and recycling the valuable components in the oily sludge to the atmospheric and vacuum distillation device. The detection result of the slag phase is shown in the table 1, and the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution is met.
Example 2:
oily sludge (with water content of 68.4 wt%, oil content of 17.6 wt% and solid content of 14.0 wt%) generated in a certain refinery is sent into a drying separator (under the pressure of 65KPa at the absolute pressure and at the temperature of 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to oil-water separation, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser is merged into a three-top gas recovery system arranged by atmospheric and vacuum distillation, and the condensed gas is introduced into a heating furnace to be used as fuel for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 80: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 180 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into an electric desalting tank in an atmospheric and vacuum distillation device, subsequently reacting according to the operating conditions of the atmospheric and vacuum distillation process, and recycling the valuable components in the oily sludge to the atmospheric and vacuum distillation device. The detection result of the slag phase is shown in the table 1, and the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution is met.
Example 3:
oily sludge (with water content of 72.8 wt%, oil content of 19.8 wt% and solid content of 7.4 wt%) generated in a certain refinery is sent into a drying separator (under the absolute pressure of 60KPa and at the temperature of 200 ℃ for drying treatment for 80 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser is merged into a three-top gas recovery system arranged by atmospheric and vacuum distillation, and the condensed gas is introduced into a heating furnace to be used as fuel for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 50 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 90: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 200 ℃ and 50KPa absolute pressure for 60 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into an electric desalting tank in an atmospheric and vacuum distillation device, subsequently reacting according to the atmospheric and vacuum distillation process conditions, and recycling the valuable components in the oily sludge to the atmospheric and vacuum distillation device. The detection result of the slag phase is shown in the table 1, and the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution is met.
Example 4:
oily sludge (with the water content of 65.3 wt%, the oil content of 20.3 wt% and the solid content of 14.4 wt%) generated by a certain refinery is sent into a drying separator (the pressure is 90KPa at absolute pressure and the temperature is 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser is merged into a three-top gas recovery system arranged by atmospheric and vacuum distillation, and the condensed gas is introduced into a heating furnace to be used as fuel for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 60 ℃, the extraction time is 30 minutes, and the solid-liquid ratio is 95: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 200 ℃ and 50KPa absolute pressure for 70 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into an electric desalting tank in an atmospheric and vacuum distillation device, subsequently reacting according to the operating conditions of the atmospheric and vacuum distillation process, and recycling the valuable components in the oily sludge to the atmospheric and vacuum distillation device. The detection result of the slag phase is shown in the table 1, and the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution is met.
Example 5:
oily sludge (with the water content of 80.3 wt%, the oil content of 15.4 wt% and the solid content of 4.3 wt%) generated by a certain refinery is sent into a drying separator (the pressure is 50KPa at absolute pressure and the temperature is 250 ℃ for drying treatment for 80 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser is merged into a three-top gas recovery system arranged by atmospheric and vacuum distillation, and the condensed gas is introduced into a heating furnace to be used as fuel for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (naphtha) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 15 minutes, and the solid-liquid ratio is 90: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to the oil-water separator, evaporating at 130 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive naphtha and valuable components in the oily sludge) separated by the solid-liquid separator into an electric desalting tank in an atmospheric and vacuum distillation device, subsequently reacting according to the operating conditions of the atmospheric and vacuum distillation process, and recycling the valuable components in the oily sludge to the atmospheric and vacuum distillation device. The detection result of the slag phase is shown in the table 1, and the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution is met.
Example 6:
oily sludge (with water content of 68.4 wt%, oil content of 17.6 wt% and solid content of 14.0 wt%) generated in a certain refinery is sent into a drying separator (under the pressure of 65KPa at the absolute pressure and at the temperature of 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to oil-water separation, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser is merged into a three-top gas recovery system arranged by atmospheric and vacuum distillation, and the condensed gas is introduced into a heating furnace to be used as fuel for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude kerosene) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 85: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 180 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive crude kerosene and valuable components in the oily sludge) separated by the solid-liquid separator into an electric desalting tank in an atmospheric and vacuum distillation device, subsequently reacting according to the operating conditions of a reaction-regeneration system, and recycling the valuable components in the oily sludge to the atmospheric and vacuum distillation device. The detection result of the slag phase is shown in the table 1, and the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution is met.
TABLE 1 slag phase analysis results
The method for disposing the oily sludge according to the invention is embedded in a catalytic cracking unit and is explained in connection with fig. 2 and examples 7-12.
Example 7:
oily sludge (with the water content of 80.3 wt%, the oil content of 15.4 wt% and the solid content of 4.3 wt%) generated by a certain refinery is sent to a drying separator (the pressure is 50KPa at the absolute pressure and the temperature is 250 ℃ for drying treatment for 80 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to oil-water separation, separated water phase is discharged into an oily sewage pipeline, and non-condensable gas in the condenser is sent to a catalytic cracking waste gas treatment device for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (gasoline) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 15 minutes, and the solid-liquid ratio is 80: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to the oil-water separator, evaporating at 130 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into a reaction-regeneration system in the catalytic cracking device, subsequently reacting according to the operating conditions of the reaction-regeneration system, and recycling the valuable components in the oily sludge to the catalytic cracking device. The detection results of the slag phase are shown in the table 2, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 8:
oily sludge (with water content of 68.4 wt%, oil content of 17.6 wt% and solid content of 14.0 wt%) generated in a certain refinery is sent to a drying separator (under the pressure of 65KPa at the absolute pressure and at the temperature of 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to oil-water separation, separated water phase is discharged into an oily sewage pipeline, and non-condensable gas in the condenser is sent to a catalytic cracking waste gas treatment device for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (gasoline) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 80: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 180 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into a reaction-regeneration system in the catalytic cracking device, subsequently reacting according to the operating conditions of the reaction-regeneration system, and recycling the valuable components in the oily sludge to the catalytic cracking device. The detection results of the slag phase are shown in the table 2, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 9:
oily sludge (water content 72.8 wt%, oil content 19.8 wt% and solid content 7.4 wt%) generated in a certain refinery is sent to a drying separator (drying treatment is carried out for 80 minutes at 200 ℃ under the absolute pressure of 60 KPa) while the sludge is dried, gas phase generated during drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, and non-condensable gas in the condenser is sent to a catalytic cracking waste gas treatment device for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (gasoline) enter an extraction reactor for extraction (the operation temperature is 50 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 90: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 200 ℃ and 50KPa absolute pressure for 60 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into a reaction-regeneration system in the catalytic cracking device, subsequently reacting according to the operating conditions of the reaction-regeneration system, and recycling the valuable components in the oily sludge to the catalytic cracking device. The detection results of the slag phase are shown in the table 2, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 10:
oily sludge (with the water content of 65.3 wt%, the oil content of 20.3 wt% and the solid content of 14.4 wt%) generated by a certain refinery is sent to a drying separator (the pressure is 90KPa at absolute pressure and the temperature is 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to oil-water separation, separated water phase is discharged into an oily sewage pipeline, and non-condensable gas in the condenser is sent to a catalytic cracking waste gas treatment device for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (gasoline) enter an extraction reactor for extraction (the operation temperature is 60 ℃, the extraction time is 30 minutes, and the solid-liquid ratio is 95: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 200 ℃ and 50KPa absolute pressure for 70 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into a reaction-regeneration system in the catalytic cracking device, subsequently reacting according to the operating conditions of the reaction-regeneration system, and recycling the valuable components in the oily sludge to the catalytic cracking device. The detection results of the slag phase are shown in the table 2, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 11:
oily sludge (with the water content of 80.3 wt%, the oil content of 15.4 wt% and the solid content of 4.3 wt%) generated by a certain refinery is sent to a drying separator (the pressure is 50KPa at the absolute pressure and the temperature is 250 ℃ for drying treatment for 80 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to oil-water separation, separated water phase is discharged into an oily sewage pipeline, and non-condensable gas in the condenser is sent to a catalytic cracking waste gas treatment device for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (diesel oil) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 15 minutes, and the solid-liquid ratio is 90: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to the oil-water separator, evaporating at 130 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into a reaction-regeneration system in the catalytic cracking device, subsequently reacting according to the operating conditions of the reaction-regeneration system, and recycling the valuable components in the oily sludge to the catalytic cracking device. The detection results of the slag phase are shown in the table 2, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 12:
oily sludge (with water content of 68.4 wt%, oil content of 17.6 wt% and solid content of 14.0 wt%) generated in a certain refinery is sent to a drying separator (under the pressure of 65KPa at the absolute pressure and at the temperature of 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to oil-water separation, separated water phase is discharged into an oily sewage pipeline, and non-condensable gas in the condenser is sent to a catalytic cracking waste gas treatment device for digestion;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extracting agent (kerosene) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 85: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 180 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into a reaction-regeneration system in the catalytic cracking device, subsequently reacting according to the operating conditions of the reaction-regeneration system, and recycling the valuable components in the oily sludge to the catalytic cracking device. The detection results of the slag phase are shown in Table 2, and the detection results accord with the concentration limit value of harmful components (no organic matter content exceeds standard) in the GB 5085.3-2007 leaching solution
TABLE 2 slag phase analysis results
The method for disposing the oily sludge according to the invention is inserted into a hydrocracking device and is explained by combining with figure 3 and examples 13-18.
Example 13:
oily sludge (with the water content of 80.3 wt%, the oil content of 15.4 wt% and the solid content of 4.3 wt%) generated by a certain refinery is sent into a drying separator (the pressure is 50KPa at absolute pressure and the temperature is 250 ℃ for drying treatment for 80 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser and flue gas generated by a heating furnace of a hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 15 minutes, and the solid-liquid ratio is 80: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to the oil-water separator, evaporating at 130 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into the raw oil in the hydrocracking device, reacting according to the hydrocracking process operation conditions, and recycling the valuable components in the oily sludge to the hydrocracking device. The detection results of the slag phase are shown in the table 3, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 14:
oily sludge (with water content of 68.4 wt%, oil content of 17.6 wt% and solid content of 14.0 wt%) generated by a certain refinery is sent into a drying separator (under the pressure of 65KPa and at the temperature of 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser and flue gas generated by a heating furnace of a hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 80: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 180 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into the raw oil in the hydrocracking device, reacting according to the hydrocracking process operation conditions, and recycling the valuable components in the oily sludge to the hydrocracking device. The detection results of the slag phase are shown in the table 3, and the detection results accord with the limit value of concentration of harmful components (no organic matter content exceeds the standard) in the GB 5085.3-2007 leaching solution.
Example 15:
oily sludge (water content 72.8 wt%, oil content 19.8 wt% and solid content 7.4 wt%) generated in a certain refinery is sent into a drying separator (drying treatment is carried out for 80 minutes at 200 ℃ under the absolute pressure of 60 KPa) while the sludge is dried, gas phase generated during drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser and flue gas generated by a heating furnace of a hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 50 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 90: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 200 ℃ and 50KPa absolute pressure for 60 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into the raw oil in the hydrocracking device, reacting according to hydrocracking process conditions, and recycling the valuable components in the oily sludge to the hydrocracking device. The detection results of the slag phase are shown in the table 3, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 16:
oily sludge (with the water content of 65.3 wt%, the oil content of 20.3 wt% and the solid content of 14.4 wt%) generated by a certain refinery is sent into a drying separator (the pressure is 90KPa at absolute pressure and the temperature is 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser and flue gas generated by a heating furnace of a hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (crude gasoline) enter an extraction reactor for extraction (the operation temperature is 60 ℃, the extraction time is 30 minutes, and the solid-liquid ratio is 95: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 200 ℃ and 50KPa absolute pressure for 70 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gasoline and valuable components in the oily sludge) separated by the solid-liquid separator into the raw oil in the hydrocracking device, reacting according to the hydrocracking process operation conditions, and recycling the valuable components in the oily sludge to the hydrocracking device. The detection results of the slag phase are shown in the table 3, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 17:
oily sludge (with the water content of 80.3 wt%, the oil content of 15.4 wt% and the solid content of 4.3 wt%) generated by a certain refinery is sent into a drying separator (the pressure is 50KPa at absolute pressure and the temperature is 250 ℃ for drying treatment for 80 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser and flue gas generated by a heating furnace of a hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (gas oil) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 15 minutes, and the solid-liquid ratio is 90: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to the oil-water separator, evaporating at 130 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gas oil and valuable components in the oily sludge) separated by the solid-liquid separator into the raw oil in the hydrocracking device, subsequently reacting according to the hydrocracking process operation conditions, and recycling the valuable components in the oily sludge to the hydrocracking device. The detection results of the slag phase are shown in the table 3, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
Example 18:
oily sludge (with water content of 68.4 wt%, oil content of 17.6 wt% and solid content of 14.0 wt%) generated by a certain refinery is sent into a drying separator (under the pressure of 65KPa and at the temperature of 200 ℃ for drying treatment for 60 minutes), gas phase generated during sludge drying enters a condenser, liquid phase collected by the condenser is subjected to an oil-water separator, separated water phase is discharged into an oily sewage pipeline, non-condensable gas in the condenser and flue gas generated by a heating furnace of a hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney;
the solid phase separated by the drying separator, the oil phase separated by the oil-water separator and the newly added extractant (gas oil) enter an extraction reactor for extraction (the operation temperature is 40 ℃, the extraction time is 20 minutes, and the solid-liquid ratio is 85: 1); after extraction, sending the mixed substance into a solid-liquid separator, separating out a solid phase, sending the solid phase into an evaporator, returning the evaporated oil phase to an oil-water separator, evaporating at 180 ℃ and 80KPa (absolute pressure) for 50 minutes, wherein the residue phase left after evaporation meets the general solid waste discharge standard;
and (3) sending the liquid phase (containing excessive gas oil and valuable components in the oily sludge) separated by the solid-liquid separator into the raw oil in the hydrocracking device, subsequently reacting according to the operating conditions of a reaction-regeneration system, and recycling the valuable components in the oily sludge to the hydrocracking device. The detection results of the slag phase are shown in the table 3, and the detection results accord with the concentration limit value (no organic matter content exceeds the standard) of harmful components in the GB 5085.3-2007 leaching solution.
TABLE 3 slag phase analysis results
The parts which are not described in the invention can be realized by taking the prior art as reference.
It should be noted that: any equivalents or obvious modifications thereof which may occur to persons skilled in the art and which are given the benefit of this description are deemed to be within the scope of the invention.
Claims (11)
1. A method for disposing oily sludge by utilizing an atmospheric and vacuum distillation/cracking device is characterized by sequentially comprising the following steps:
s1, drying and separating the pretreated oily sludge, feeding a gas phase generated in the separation process into a condenser, feeding a liquid phase collected by the condenser into an oil-water separator, discharging a water phase collected by the condenser into an oily sewage pipeline, and merging non-condensable gas in the condenser into the atmospheric and vacuum distillation/cracking device;
s2, adding an extracting agent into the solid phase generated by drying and separating in the step S1 and the oil phase obtained by separating in the oil-water separator for extraction reaction, after extraction is finished, sending the mixed substance into a solid-liquid separator, sending the solid phase obtained by separating in the solid-liquid separator into an evaporator, returning the oil phase evaporated by the evaporator to the oil-water separator in the step S1, and discharging the evaporated residual solid phase up to the standard;
s3, feeding the liquid phase separated by the solid-liquid separator into an atmospheric and vacuum distillation/cracking device.
2. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 1, which is characterized in that: in step S1, the pretreatment is to dehydrate the oily sludge through simple machinery, and the water content of the oily sludge is more than or equal to 50%.
3. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 1, which is characterized in that: in step S1, drying separation is performed in a drying separator, and the relevant process conditions of drying separation are as follows: the pressure is 50-105KPa, the temperature is 100-250 ℃, and the processing time is 60-90 minutes.
4. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 1, which is characterized in that: in the step S1, the cracking device is a catalytic cracking device or a hydrocracking device, when the non-condensable gas in the condenser is merged into the atmospheric and vacuum distillation device, the non-condensable gas is specifically merged into a three-top gas recovery system arranged in the atmospheric and vacuum distillation device, and is introduced into a heating furnace as a fuel for digestion; when the non-condensable gases in the condenser are incorporated into the catalytic cracking unit, they are specifically incorporated into the off-gas treatment unit of the catalytic cracking unit; when the non-condensable gas in the condenser is merged into the hydrocracking device, the non-condensable gas in the condenser and the flue gas generated by a heating furnace of the hydrocracking device enter a waste heat boiler through a combined flue to recover waste heat, and the waste heat is directly discharged into the atmosphere through a chimney.
5. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 4, wherein: in step S2, the extraction reaction temperature is 20-80 ℃, the extraction time is 10-30 minutes, and the solid-liquid mass ratio is 1-100: 1; the extractant is crude light oil produced by atmospheric and vacuum distillation or light oil produced by a catalytic cracking unit or raw oil of a hydrocracking unit.
6. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 4, wherein: in step S2, the evaporation temperature of the evaporator is 105-200 ℃, the pressure is 50-105KPa, and the evaporation time is 60-90 minutes.
7. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 4, wherein: in step S3, the liquid phase separated by the solid-liquid separator enters an electric desalting tank of an atmospheric and vacuum distillation device, and then the reaction is carried out according to the operating conditions of the atmospheric and vacuum distillation process; or the liquid phase obtained by the separation of the solid-liquid separator enters a reaction-regeneration system in the catalytic cracking device, and then the reaction is carried out according to the operating conditions of the reaction-regeneration system; or the liquid phase obtained by the separation of the solid-liquid separator enters the raw oil in the hydrocracking device, the subsequent reaction is carried out according to the hydrocracking process operation conditions, and valuable components in the oily sludge are recycled to the hydrocracking device.
8. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 5, wherein: the crude light oil produced by the atmospheric and vacuum distillation device comprises crude gasoline, gas oil, crude kerosene or naphtha.
9. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 5, wherein: the light oil produced by the catalytic cracking unit is gasoline, diesel oil or kerosene.
10. The method for disposing the oily sludge by using the atmospheric and vacuum distillation/cracking device according to claim 5, wherein: the raw material oil of the hydrocracking device is crude gasoline, gas oil, vacuum distillate oil, wax oil or crude diesel oil.
11. A method for disposing oily sludge by using an atmospheric and vacuum distillation/cracking unit according to any one of claims 1 to 10, characterized in that: the oil-containing sludge comprises ground oil sludge, tank cleaning oil sludge, floating slag bottom sludge, three-separator oil sludge and oil spilling sludge generated in production accidents in the oil refining and wastewater treatment processes of oil field exploitation and refining enterprises, and oil sludge in an oil separation tank, a flotation tank, residual activated sludge, a crude oil dehydration tank, an oil storage tank and a sump oil tank.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113233725A (en) * | 2021-06-24 | 2021-08-10 | 陕西延长石油（集团）有限责任公司 | Device and method for flotation and extraction coupling treatment of oily sludge |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070090022A1 (en) * | 2003-05-13 | 2007-04-26 | Szu-Jen Chien | Method of separating oil slurry from the crude oil |
| CN101823824A (en) * | 2009-03-04 | 2010-09-08 | 中国石油天然气股份有限公司 | Treatment process of oily sludge |
| CN103058471A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Method for treatment of oil sludge by thermal treatment-supercritical extraction |
| CN103979757A (en) * | 2014-05-27 | 2014-08-13 | 陕西延长石油（集团）有限责任公司 | Method for treating oily sludge through multistage extraction-splitting coupling of supercritical fluid |
| CN108675589A (en) * | 2018-07-23 | 2018-10-19 | 哈尔滨金源伟业环保科技有限公司 | A kind of continous way greasy filth pyrolysis treatment systems and pyrolysis treating method |
| CN109777454A (en) * | 2019-01-29 | 2019-05-21 | 浙江百能科技有限公司 | It a kind of pyrolyzing sludge liquefaction and its is mixed with coal dust and burns combined apparatus and technique |
-
2019
- 2019-09-29 CN CN201910929590.9A patent/CN112573784A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20070090022A1 (en) * | 2003-05-13 | 2007-04-26 | Szu-Jen Chien | Method of separating oil slurry from the crude oil |
| CN101823824A (en) * | 2009-03-04 | 2010-09-08 | 中国石油天然气股份有限公司 | Treatment process of oily sludge |
| CN103058471A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Method for treatment of oil sludge by thermal treatment-supercritical extraction |
| CN103979757A (en) * | 2014-05-27 | 2014-08-13 | 陕西延长石油（集团）有限责任公司 | Method for treating oily sludge through multistage extraction-splitting coupling of supercritical fluid |
| CN108675589A (en) * | 2018-07-23 | 2018-10-19 | 哈尔滨金源伟业环保科技有限公司 | A kind of continous way greasy filth pyrolysis treatment systems and pyrolysis treating method |
| CN109777454A (en) * | 2019-01-29 | 2019-05-21 | 浙江百能科技有限公司 | It a kind of pyrolyzing sludge liquefaction and its is mixed with coal dust and burns combined apparatus and technique |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113233725A (en) * | 2021-06-24 | 2021-08-10 | 陕西延长石油（集团）有限责任公司 | Device and method for flotation and extraction coupling treatment of oily sludge |
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