CN111718084A - Oily sludge treatment method - Google Patents
Oily sludge treatment method Download PDFInfo
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- CN111718084A CN111718084A CN202010397892.9A CN202010397892A CN111718084A CN 111718084 A CN111718084 A CN 111718084A CN 202010397892 A CN202010397892 A CN 202010397892A CN 111718084 A CN111718084 A CN 111718084A
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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
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- 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
- B01D53/14—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 by absorption
- B01D53/1418—Recovery of products
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- 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
- B01D53/14—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 by absorption
- B01D53/1487—Removing organic compounds
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- 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
- B01D53/14—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 by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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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
- C02F11/008—Sludge treatment by fixation or solidification
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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
- C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
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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
- C02F11/12—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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- 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
- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
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- 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
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing
Abstract
The invention provides a method for treating oily sludge, which comprises the following steps that sludge is divided into light matters and heavy matters by a cyclone separator; the light materials are transported into a buffer tank, and the heavy materials are transported into a sludge storage tank; carrying out gas-liquid separation by using a buffer tank; the gas phase is transmitted to a spray tower; contacting the gas phase with spray water, and cooling by water to obtain oily sewage; carrying out oil-water separation on the oily sewage to obtain condensed water and light organic matters; cooling the condensed water, returning the cooled condensed water to the top of the spray tower, and enriching the light organic matters and then discharging the light organic matters; carrying out pressurization separation and drying post-treatment on the non-condensable gas in the gas phase; conveying the heavy material to a preheating tank for preheating; conveying the heavy material to a reaction tank, stirring and cooling; compressing and dehydrating the heavy material by using a compressor; preparing the heavy material into the sewage peat with uniform particle size; transporting the sludge carbon to a drying furnace for drying; conveying the heavy material to a carbonization furnace for high-temperature carbonization to obtain carbon; the charcoal is subjected to reburning pyrolysis. The invention has the beneficial effects that: high resource recovery and utilization rate and high processing cost ratio.
Description
Technical Field
The invention relates to sludge treatment, in particular to a method for treating oily sludge.
Background
Sewage and sludge are two systems that are equally important and closely related to solve the problem of water pollution. The sludge treatment is a guarantee that the sewage treatment can be finally implemented, and in economically developed countries, the sludge treatment is an extremely important link, and the investment of the sludge treatment accounts for about 50-70% of the total investment of sewage treatment plants. In the main method for sludge treatment and disposal in China, the water content of activated sludge in a sewage field can still reach about 80% after dehydration treatment in the current stage of coal chemical industry, and after being conveyed to the current cinder field by an automobile for airing, the activated sludge is transferred to a hazardous waste center for incineration and landfill treatment or airing and carbonization.
The innovation points of the invention are as follows: 1, re-burning the carbonized sludge again, transferring heat to heat conducting oil by the biomass charcoal after re-burning, recycling the heat of the heat conducting oil, and 3, finely processing different substances contained in the sludge.
Disclosure of Invention
In order to solve the technical problems, the invention discloses a method for treating oily sludge, which is implemented by the following steps:
a method for treating oily sludge is characterized by comprising the following steps: s1: transporting sludge into a cyclone separator, wherein the cyclone separator separates the sludge into light matters and heavy matters; s2: transporting the light materials into a buffer tank, and transporting the heavy materials into a sludge storage tank; s3: the buffer tank heats the light substances to perform gas-liquid separation, and gas phase and liquid phase are separated; s4: pressurizing the liquid phase by an oil transfer pump and then discharging the liquid phase, and transmitting the gas phase into a spray tower; s5: the saturated steam in the gas phase is in reverse contact with the spray water from top to bottom at the top of the spray tower from bottom to top, and the oil-containing sewage is obtained after water cooling; s6: the oily sewage is discharged from the bottom of the spray tower, is lifted by a circulating water pump and then enters an oil-water separator for oil-water separation to obtain condensed water and light organic matters; s7: the condensed water is conveyed to an air cooler for cooling and then returned to the top of the spray tower for recycling, and the light organic matters are enriched in the oil-water separator and then discharged; s8: carrying out pressurization, separation and drying post-treatment on the non-condensable gas in the gas phase; s9: conveying the heavy material to a preheating tank for preheating; s10: conveying the heavy material to a reaction tank, stirring and cooling; s11: compressing and dehydrating the heavy material by using a compressor; s12: preparing the heavy material into sewage peat with uniform particle size; s13: conveying the sludge carbon to a drying furnace for drying; s14: conveying the heavy material to a carbonization furnace for high-temperature carbonization to obtain carbon; s15: and conveying the carbon to a reburning furnace for reburning pyrolysis.
Preferably, the pressure in the buffer tank is-3 kPa to 3kPa, the pressure of the gas phase discharged from the top of the spray tower is-17 kPa to-23 kPa, the temperature of oily sewage discharged from the bottom of the spray tower is 98 ℃ to 102 ℃ by steam spraying.
Preferably, the liquid level of the buffer tank and the variable frequency of the oil transfer pump are provided with interlocking alarm; or/and the oil outlet end of the oil-water separator is fixedly communicated, a second electric regulating valve is fixedly arranged on the pipeline, and the liquid level of the spray tower and the opening degree of the second electric regulating valve are interlocked to give an alarm; or/and the inlet pressure of the compressor and the frequency conversion of the compressor are provided with interlocking alarm; and/or a third electric regulating valve is arranged on a pipeline between the circulating spray water air cooler and the liquid inlet end of the spray tower, and the temperature of the spray tower and the opening degree of the third electric regulating valve are provided with interlocking alarm.
Preferably, the buffer tank is provided with a high-liquid-level bleed control loop; or/and a steam overload control loop is arranged at the temperature of a gas phase outlet at the top of the spraying tower; or/and the screw compressor is provided with an overtemperature protection control loop.
Preferably, the temperature in the reaction tank is controlled to be 100-350 ℃, and the pressure is controlled to be 5-25 Mpa.
Preferably, the reaction time of the reaction tank is not less than 10 min-12 min.
Preferably, it further comprises S17: introducing the flue gas obtained in S14 and S15 and the waste heat of the main furnace into a flue gas pipeline by a fan to exchange heat energy with heat conduction oil, wherein the temperature of the heat conduction oil is raised to 280-350 ℃, and then the heat conduction oil is divided into three parts for use: 20 to 35 percent of heat conducting oil is directly used for preheating the sludge in the S9; 30-45% of heat conducting oil is directly used for heating reaction of a reaction tank in S10; 40% -55% of heat conducting oil and water with the temperature of 15-25 ℃ are subjected to heat exchange in an exchanger, and the water is changed into high-temperature steam with the temperature of 180-200 ℃ and is transferred to a dryer to dry sludge.
Preferably, the temperature of the heat conduction oil obtained after heat exchange between the heat conduction oil and the biomass charcoal is lower than 350 ℃.
Preferably, the heat required by the preheating reaction and the reaction of the reaction tank only needs to be supplied with power for heating when the biomass charcoal is started, the heat required after the biomass charcoal is started passes through the preheating reaction and the heat conduction oil with the temperature of 280-350 ℃ obtained after the heat exchange of the heat conduction oil and the biomass charcoal is provided through the heat exchange.
Preferably, the heat generated during S14, S15 is transferred to a genset for power generation.
The technical scheme of the invention can solve the technical problems of low neutral cost ratio and low resource recovery rate in the prior art; by implementing the technical scheme of the invention, the technical effects of high resource recycling rate and high cost performance treatment can be realized.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only one embodiment of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a process flow diagram of a process for treating oily sludge.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In a specific embodiment, as shown in fig. 1, a method for treating oily sludge is characterized in that: s1: transporting sludge into a cyclone separator, wherein the cyclone separator separates the sludge into light matters and heavy matters; s2: transporting the light materials into a buffer tank, and transporting the heavy materials into a sludge storage tank; s3: the buffer tank heats the light substances to perform gas-liquid separation, and gas phase and liquid phase are separated; s4: pressurizing the liquid phase by an oil transfer pump and then discharging the liquid phase, and transmitting the gas phase into a spray tower; s5: the saturated steam in the gas phase is in reverse contact with the spray water from top to bottom at the top of the spray tower from bottom to top, and the oil-containing sewage is obtained after water cooling; s6: the oily sewage is discharged from the bottom of the spray tower, is lifted by a circulating water pump and then enters an oil-water separator for oil-water separation to obtain condensed water and light organic matters; s7: the condensed water is conveyed to an air cooler for cooling and then returned to the top of the spray tower for recycling, and the light organic matters are enriched in the oil-water separator and then discharged; s8: carrying out pressurization, separation and drying post-treatment on the non-condensable gas in the gas phase; s9: conveying the heavy material to a preheating tank for preheating; s10: conveying the heavy material to a reaction tank, stirring and cooling; s11: compressing and dehydrating the heavy material by using a compressor; s12: preparing the heavy material into sewage peat with uniform particle size; s13: conveying the sludge carbon to a drying furnace for drying; s14: conveying the heavy material to a carbonization furnace for high-temperature carbonization to obtain carbon; s15: and conveying the carbon to a reburning furnace for reburning pyrolysis.
In this particular embodiment, S1-S8: the gas phase at 95-105 ℃ after the gas-liquid separation of the buffer tank is reversely and directly contacted and condensed with the tower top circulating spray water at 55-60 ℃ in the spray tower 3 by an air cooler. Condensing the steam and the light oil component in the gas phase into oily sewage, removing oil from the oily sewage by an oil-water separator to obtain condensed water at the temperature of 80-90 ℃, cooling the condensed water to the temperature of 55-60 ℃ by a circulating spray water air cooler, and recycling the condensed water as the tower top circulating spray water of the spray tower; the light oil and the steam condensate in the oily sewage are respectively recovered and collected by independent pipelines, so that the problem of heat exchange efficiency reduction caused by the enrichment of the light oil in a circulating system can be effectively solved, and the steam condensate and the light oil can be recycled to generate economic benefit. Meanwhile, the one-pump type circulating cooling system is adopted, compared with a conventional air cooling system, the wave-resistant capacity of the system can be greatly improved, the impact of the throughput development produced liquid quantity, steam quantity and temperature change on the system can be better responded, and the stability of the pressure and temperature of the whole system is further ensured.
S9-S5 may be: conveying sludge in a sludge storage tank to be treated to a carbonization tank for preheating treatment by transportation and device, and preheating the sludge to 100 ℃ by electric heating; and (3) conveying the preheated sludge to a reaction tank for stirring reaction for 10min for dehydration, wherein a large amount of waste gas is generated in the reaction tank, and the waste gas is transferred to a waste gas device for treatment. Conveying the sludge after reaction to a cooling tank, stirring for 1h, and cooling to 80 ℃; the cooled sludge is finely crushed, mixed and uniformly granulated in a presser, the finely crushed and uniformly mixed sludge is transferred to a dryer for drying and then is conveyed to a carbonization kiln for carbonization to obtain carbon; the carbonized carbon with the temperature of more than 4000 kilocalories is rapidly re-burned in a biomass furnace at 400-500 ℃, the carbonized carbon with the temperature of less than 4000 kilocalories is re-burned in the biomass furnace at 250-300 ℃, the re-burned high-temperature biomass carbon is conducted in a heat exchanger 1 to exchange heat with heat conduction oil with the temperature of 25-30 ℃, the biomass carbon is cooled to room temperature, the heat conduction oil takes away the heat in the biomass carbon, the heat conduction oil has higher heat at the moment, the temperature reaches 280-300 ℃, the heat conduction oil with the temperature of 280-300 ℃ is used for the following three purposes, wherein, 20-35 percent of the heat conduction oil is directly used for preheating sludge, the sludge reaches 100 ℃, the heat conduction oil with the temperature of 280-300 ℃ and the heat conduction oil with the temperature of 25-30 ℃ are firstly mixed until the temperature of the heat conduction oil is 150 ℃ and then the sludge is preheated, the temperature of the heat conduction oil is reduced to 25-30 ℃, the heat conduction oil is recovered, 1, the biomass charcoal is used again for cooling the high-temperature biomass charcoal to obtain granular biomass charcoal without color odor, and the granular biomass charcoal is packaged and delivered out of a factory. 30% -45% of heat conduction oil with the temperature of about 280-300 ℃ is directly used for heating reaction of the reaction tank, so that the temperature of the reaction tank is controlled, the reaction is carried out at 250 ℃, the temperature of the heat conduction oil is reduced to 25-30 ℃, the heat conduction oil is recovered and transferred to a heat exchanger again, and the heat exchanger 1 is used for cooling the high-temperature biomass charcoal again; the heat conducting oil with the temperature of 40-55% and the temperature of 280-300 ℃ is transferred into an exchanger to exchange heat with water with the temperature of 15-25 ℃, the water is changed into water vapor, the partial water vapor is transferred to a dryer to dry sludge in the dryer, the process may need to firstly mix the heat conducting oil with the temperature of 280-300 ℃ with the heat conducting oil with the temperature of 25-30 ℃ for heat conduction, the oil temperature is reduced to 200 ℃, then the water is heated, the cooled heat conducting oil with the temperature of 25-30 ℃ is recycled and transferred to the heat exchanger 1 to be used for cooling high-temperature biomass again, and the condensed water with the temperature of 15-25 ℃ is transferred to the water exchanger again for recycling.
S9-S15 can also be: conveying sludge in a sludge storage tank to be treated to a carbonization tank through a conveying device for preheating treatment, and preheating the sludge to 100 ℃ by utilizing electric heating; the preheated sludge is conveyed to a reaction tank to be stirred and react for 10min for dehydration, at the moment, a large amount of waste gas is generated in the reaction tank, the waste gas is transferred to waste, and a gas device is used for treatment. Conveying the sludge after reaction to a cooling tank, stirring for 1h, and cooling to 80 ℃; the cooled sludge is finely crushed, mixed and uniformly granulated in a presser, the finely crushed and uniformly mixed sludge is transferred to a dryer for drying and then is conveyed to a carbonization kiln for carbonization to obtain carbon; the carbonized carbon with the temperature of more than 4000 kilocalories is rapidly reburned in a biomass furnace at 400-500 ℃, the carbonized carbon with the temperature of less than 4000 kilocalories is reburned in the biomass furnace at 250-300 ℃, the reburned high-temperature biomass carbon is conducted in a heat exchanger 1 to exchange heat with heat conduction oil with the temperature of 25-30 ℃, the biomass carbon is cooled to room temperature, the heat conduction oil takes away the biomass carbon, the heat in the biomass carbon, the heat conduction oil has higher heat, the temperature reaches 280-300 ℃, the heat conduction oil with the temperature of 280-300 ℃ is used for the following three purposes, wherein, 20-35 percent of the heat conduction oil is directly used for preheating sludge, the sludge reaches 100 ℃, the heat conduction oil with the temperature of 280-300 ℃ and the heat conduction oil with the temperature of 25-30 ℃ are firstly mixed until the temperature of the heat conduction oil is 150 ℃ and then the sludge is preheated, the temperature of the heat conduction oil is reduced to 25-30 ℃, the heat conduction oil is recovered, 1, the biomass charcoal is used again for cooling the high-temperature biomass charcoal to obtain granular biomass charcoal without color odor, and the granular biomass charcoal is packaged and delivered out of a factory. 30% -45% of heat conduction oil with the temperature of about 280-300 ℃ is directly used for heating reaction of the reaction tank, so that the temperature of the reaction tank is controlled, the reaction is carried out at 250 ℃, the temperature of the heat conduction oil is reduced to 25-30 ℃, the heat conduction oil is recovered and transferred to a heat exchanger again, and the heat exchanger 1 is used for cooling the high-temperature biomass charcoal again; the heat conducting oil with the temperature of 40-55% and the temperature of 280-300 ℃ is transferred into an exchanger to exchange heat with water with the temperature of 15-25 ℃, the water is changed into water vapor, the partial water vapor is transferred to a dryer to dry sludge in the dryer, the process may need to firstly mix the heat conducting oil with the temperature of 280-300 ℃ with the heat conducting oil with the temperature of 25-30 ℃ for heat conduction, the oil temperature is reduced to 200 ℃, then the water is heated, the cooled heat conducting oil with the temperature of 25-30 ℃ is recycled and transferred to the heat exchanger 1 to be used for cooling high-temperature biomass again, and the condensed water with the temperature of 15-25 ℃ is transferred to the water exchanger again for recycling.
In a preferred embodiment, the pressure in the buffer tank is-3 kPa to 3kPa, the pressure of the gas phase discharged from the top of the spray tower is-17 kPa to-23 kPa, the temperature of the oily sewage discharged from the bottom of the spray tower is 98 ℃ to 102 ℃ by steam spraying.
In a preferred embodiment, the liquid level of the buffer tank and the frequency conversion of the oil transfer pump are provided with interlocking alarms; or/and the oil outlet end of the oil-water separator is fixedly communicated, a second electric regulating valve is fixedly arranged on the pipeline, and the liquid level of the spray tower and the opening degree of the second electric regulating valve are interlocked to give an alarm; or/and the inlet pressure of the compressor and the frequency conversion of the compressor are provided with interlocking alarm; and/or a third electric regulating valve is arranged on a pipeline between the circulating spray water air cooler and the liquid inlet end of the spray tower, and the temperature of the spray tower and the opening degree of the third electric regulating valve are provided with interlocking alarm.
In a preferred embodiment, the buffer tank is provided with a high level bleed control loop; or/and a steam overload control loop is arranged at the temperature of a gas phase outlet at the top of the spraying tower; or/and the screw compressor is provided with an overtemperature protection control loop.
In a preferred embodiment, the temperature in the reaction tank is controlled to be 100-350 ℃, and the pressure is controlled to be 5-25 MPa.
In a preferred embodiment, the reaction time of the reaction tank is not less than 10 min-12 min.
In a preferred embodiment, the method further comprises the step of S17: introducing the flue gas obtained in S14 and S15 and the waste heat of the main furnace into a flue gas pipeline by a fan to exchange heat energy with heat conduction oil, wherein the temperature of the heat conduction oil is raised to 280-350 ℃, and then the heat conduction oil is divided into three parts for use: 20 to 35 percent of heat conducting oil is directly used for preheating the sludge in the S9; 30-45% of heat conducting oil is directly used for heating reaction of a reaction tank in S10; 40% -55% of heat conducting oil and water with the temperature of 15-25 ℃ are subjected to heat exchange in an exchanger, and the water is changed into high-temperature steam with the temperature of 180-200 ℃ and is transferred to a dryer to dry sludge.
In a preferred embodiment, the temperature of the heat conduction oil obtained after the heat exchange between the heat conduction oil and the biomass charcoal is lower than 350 ℃; the heat required by the preheating reaction and the reaction of the reaction tank only needs to be supplied with power for heating when the biomass charcoal is started, the heat required after the biomass charcoal is started passes through the heat transfer oil, and the heat transfer oil with the temperature of 280-350 ℃ obtained after the heat exchange of the heat transfer oil and the biomass charcoal is provided through the heat exchange.
In a preferred embodiment, the heat generated during S14 and S15 is transferred to a generator set for power generation, thereby effectively utilizing the heat therein.
It should be understood that the above-described embodiments are merely exemplary of the present invention, and are not intended to limit the present invention, and that any modification, equivalent replacement, or improvement made without departing from the spirit and principle of the present invention shall fall within the protection scope of the present invention.
Claims (10)
1. A method for treating oily sludge is characterized by comprising the following steps:
s1: transporting sludge into a cyclone separator, wherein the cyclone separator separates the sludge into light matters and heavy matters;
s2: transporting the light materials into a buffer tank, and transporting the heavy materials into a sludge storage tank;
s3: the buffer tank heats the light substances to perform gas-liquid separation, and gas phase and liquid phase are separated;
s4: pressurizing the liquid phase by an oil transfer pump and then discharging the liquid phase, and transmitting the gas phase into a spray tower;
s5: the saturated steam in the gas phase is in reverse contact with the spray water from top to bottom at the top of the spray tower from bottom to top, and the oil-containing sewage is obtained after water cooling;
s6: the oily sewage is discharged from the bottom of the spray tower, is lifted by a circulating water pump and then enters an oil-water separator for oil-water separation to obtain condensed water and light organic matters;
s7: the condensed water is conveyed to an air cooler for cooling and then returned to the top of the spray tower for recycling, and the light organic matters are enriched in the oil-water separator and then discharged;
s8: carrying out pressurization, separation and drying post-treatment on the non-condensable gas in the gas phase;
s9: conveying the heavy material to a preheating tank for preheating;
s10: conveying the heavy material to a reaction tank, stirring and cooling;
s11: compressing and dehydrating the heavy material by using a compressor;
s12: preparing the heavy material into sewage peat with uniform particle size;
s13: conveying the sludge carbon to a drying furnace for drying;
s14: conveying the heavy material to a carbonization furnace for high-temperature carbonization to obtain carbon;
s15: and conveying the carbon to a reburning furnace for reburning pyrolysis.
2. The method for treating oily sludge according to claim 1, wherein: the pressure in the buffer tank is-3 kPa to 3kPa, the pressure of the gas phase discharged from the top of the spray tower is-17 kPa to-23 kPa, steam is sprayed, and the temperature of the oily sewage discharged from the bottom of the spray tower is 98 ℃ to 102 ℃.
3. The method for treating oily sludge according to claim 1, wherein: the liquid level of the buffer tank and the variable frequency of the oil transfer pump are provided with interlocking alarm; or/and the oil outlet end of the oil-water separator is fixedly communicated, a second electric regulating valve is fixedly arranged on the pipeline, and the liquid level of the spray tower and the opening degree of the second electric regulating valve are interlocked to give an alarm; or/and the inlet pressure of the compressor and the frequency conversion of the compressor are provided with interlocking alarm; and/or a third electric regulating valve is arranged on a pipeline between the circulating spray water air cooler and the liquid inlet end of the spray tower, and the temperature of the spray tower, the third electric and the opening degree of the electric regulating valve are provided with linkage alarm.
4. The method for treating oily sludge according to claim 1, wherein: the buffer tank is provided with a high liquid level discharge control loop; or/and a steam overload control loop is arranged at the temperature of a gas phase outlet at the top of the spraying tower; or/and the screw compressor is provided with an overtemperature protection control loop.
5. The method for treating oily sludge according to claim 1, wherein: the temperature in the reaction tank is controlled to be 100-350 ℃, and the pressure is controlled to be 5-25 Mpa.
6. The method for treating oily sludge according to claim 1, wherein: the reaction time of the reaction tank is not less than 10 min-12 min.
7. The method for treating oily sludge according to claim 1, wherein: further comprising S17: introducing the flue gas obtained in S14 and S15 and the waste heat of the main furnace into a flue gas pipeline by a fan to exchange heat energy with heat conduction oil, wherein the temperature of the heat conduction oil is raised to 280-350 ℃, and then the heat conduction oil is divided into three parts for use: 20 to 35 percent of heat conducting oil is directly used for preheating the sludge in the S9; 30-45% of heat conducting oil is directly used for heating reaction of a reaction tank in S10; 40% -55% of heat conducting oil and water with the temperature of 15-25 ℃ are subjected to heat exchange in an exchanger, and the water is changed into high-temperature steam with the temperature of 180-200 ℃ to be transferred to a dryer to dry sludge.
8. The method for treating oily sludge according to claim 7, wherein: the temperature of the heat conduction oil obtained after heat exchange between the heat conduction oil and the biomass charcoal is lower than 350 ℃.
9. The method for treating oily sludge according to claim 7, wherein: the heat required by the preheating reaction and the reaction of the reaction tank only needs to be supplied with power for heating when the biomass charcoal is started, the heat required after the biomass charcoal is started passes through the heat transfer oil, and the heat transfer oil with the temperature of 280-350 ℃ obtained after the heat exchange of the heat transfer oil and the biomass charcoal is provided through the heat exchange.
10. The method for treating oily sludge according to claim 7, wherein: the heat generated during S14, S15 is transferred to a genset for power generation.
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| CN106904814A (en) * | 2017-04-24 | 2017-06-30 | 上海梵煦环境科技有限公司 | A kind of method of sludge carbonization resintering |
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| CN101239770A (en) * | 2008-03-20 | 2008-08-13 | 张贺新 | Dirty oil mud separating method and device |
| CN103449701A (en) * | 2013-08-14 | 2013-12-18 | 湖州宜可欧环保科技有限公司 | Method and device for refinery sludge carbonization treatment and carbon recovery |
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Application publication date: 20200929 |