CN115368919A - Method and system for pyrolysis coupling gasification treatment of oily sludge - Google Patents

Method and system for pyrolysis coupling gasification treatment of oily sludge Download PDF

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Publication number
CN115368919A
CN115368919A CN202211051643.XA CN202211051643A CN115368919A CN 115368919 A CN115368919 A CN 115368919A CN 202211051643 A CN202211051643 A CN 202211051643A CN 115368919 A CN115368919 A CN 115368919A
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flue gas
pyrolysis
treatment
oil
temperature flue
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阳绍军
刘璐
刘嘉鹏
刘文洲
夏双全
张南竹
刘姣姣
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Zhongke Hefei Coal Gasification Technology Co ltd
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Zhongke Hefei Coal Gasification Technology Co ltd
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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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0027—Condensation of vapours; Recovering volatile solvents by condensation by direct contact between vapours or gases and the cooling medium
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/10—Treatment of sludge; Devices therefor by pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
    • 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
    • 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
    • C10B57/10—Drying
    • C—CHEMISTRY; METALLURGY
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • 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)
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/06—Sludge reduction, e.g. by lysis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/24—Separation of coarse particles, e.g. by using sieves or screens
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/26—Reducing the size of particles, liquid droplets or bubbles, e.g. by crushing, grinding, spraying, creation of microbubbles or nanobubbles
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • 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

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
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  • General Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Treatment Of Sludge (AREA)

Abstract

The invention relates to the technical field of hazardous waste treatment, and provides a method and a system for pyrolysis coupling gasification treatment of oily sludge. According to the invention, oily sludge is sequentially subjected to pretreatment, drying and pyrolysis, pyrolytic carbon, mixed gas and second low-temperature flue gas are obtained through pyrolysis, wherein the pyrolytic carbon is gasified to obtain gasified gas, the mixed gas is condensed to obtain pyrolysis gas, the gasified gas and the pyrolysis gas both have certain heat values, and the gasified gas and the pyrolysis gas can be used as heat sources after combustion. The method provided by the invention further recycles the pyrolytic carbon and the mixed gas obtained after pyrolysis, not only can realize the reduction of the oily sludge, but also improves the recycling level of the system, reduces the treatment cost, improves the project income and has better development prospect. The system provided by the invention has the advantages of small floor area, skid-mounted type, low investment and low operation cost, and is suitable for treating different types of oily sludge such as oil sludge on the ground, oil-based drilling cuttings, refinery three-sludge and the like.

Description

Method and system for pyrolysis coupling gasification treatment of oily sludge
Technical Field
The invention relates to the technical field of hazardous waste treatment, in particular to a method and a system for pyrolysis coupling gasification treatment of oily sludge.
Background
The oily sludge is one of main pollutants generated in the petroleum production and processing process, has complex components and large pollution degree, and contains a large amount of colloids, asphaltenes, benzene series, anthracene, phenol, pyrene and other toxic and harmful substances. The environmental protection improvement force of China is gradually increased, and stricter requirements are put forward on the high-efficiency treatment of oily sludge pollutants. In order to reduce the pollution of the oily sludge to the environment and the influence on human health, the efficient treatment method of the oily sludge becomes a key breakthrough object in the whole petroleum industry.
The existing oil-containing sludge treatment technologies can be roughly divided into physicochemical treatment methods and biological treatment methods. Among them, the physicochemical treatment methods include a landfill method, an incineration method, an extraction method, a pyrolysis method, a concentration or drying method, an ultrasonic treatment method, a freeze-melting method, a conditioning-mechanical separation method, and the like. The biological treatment method mainly comprises a composting method, a microorganism strengthening method, a biological flotation method and the like. Since the oily sludge belongs to hazardous waste, the incineration method and the pyrolysis method have high harmless level and remarkable reduction level, and thus the oily sludge is widely applied to the field of oily sludge treatment.
The incineration method is that the oily sludge after the pre-treatment of dehydration and concentration is put into an incinerator at the temperature of 800-1200 ℃ and the mineral oil and other organic pollutants in the oily sludge are burnt and decomposed by using the excess air, the auxiliary fuel and the combustible crude oil substances in the sludge to be converted into CO 2 And H 2 O and other small molecules, thereby removing harmful components in the sludge and achieving the aim of harmless treatment. The sludge treatment speed by the incineration method is high, long-term storage and long-distance transportation are not needed, the sludge can be incinerated on the spot, the heat energy generated by combustion can be used for power supply and heating supply, the waste residue after combustion can be used for building base materials or greening road repair, but the problems that the treatment process occupies large area, the treatment cost is high, crude oil cannot be recycled and the like exist, in addition, dioxin and SO can be generated by organic matter incineration 2 And highly toxic substances such as CO influence the healthy life of human beings.
The pyrolysis method is characterized in that under the condition of air isolation and high temperature, heavy hydrocarbon substances, colloid and asphaltene contained in the oily sludge are volatilized, cracked, condensed and the like to be converted into light components through medium-high temperature pyrolysis, the light components and water are separated in a condensation mode, the resource recycling is realized, and the residual solid slag also meets the requirement of direct landfill. The pyrolysis method has the advantages of rapid and efficient treatment, simple process, large treatment capacity and the like, but has large occupied area, high investment and high operation cost. Because the pyrolytic carbon obtained after the oily sludge is subjected to pyrolysis treatment still has a certain calorific value, the common pyrolysis process does not effectively utilize the pyrolytic carbon, so that the process reduction and the resource level are low, and the large-scale popularization and application are not facilitated.
Disclosure of Invention
In view of this, the invention provides a method and a system for pyrolysis-coupled gasification treatment of oily sludge. The invention relates to a method for preparing a high-performance composite material. The method provided by the invention adopts a pyrolysis coupling gasification method to treat the oily sludge, and can gasify and utilize the pyrolytic carbon while effectively treating the oily sludge, thereby reducing the treatment cost, improving the project income and having better development prospect.
In order to achieve the above object, the present invention provides the following technical solutions:
a method for pyrolysis coupling gasification treatment of oily sludge comprises the following steps:
pretreating the oily sludge to obtain pretreated oil sludge and impurities;
drying the pretreated oil sludge to obtain dried oil sludge, water vapor and first low-temperature flue gas;
performing pyrolysis treatment on the dried oil sludge to obtain pyrolytic carbon, mixed gas and second low-temperature flue gas;
gasifying the pyrolytic carbon to obtain gasified gas and solid residues;
condensing the mixed gas to obtain an oil-water mixture and pyrolysis gas;
carrying out oil-water separation on the oil-water mixture to obtain recovered oil, condensed water and sewage;
and carrying out flue gas purification treatment on the first low-temperature flue gas and the second low-temperature flue gas to obtain the flue gas reaching the standard.
Preferably, the liquid content of the oily sludge is 30-80 wt%, and the solid content is 20-70 wt%; the liquid content of the pretreated oil sludge is 35-85 wt%, the solid content is 15-65 wt%, and the particle size of solid particles in the pretreated oil sludge is less than 20mm; the pretreatment mode comprises one or more of sorting, crushing and screening.
Preferably, the drying treatment temperature is 300-450 ℃, and the time is 20-40 min; the dried oil sludge has a liquid content of 5-30 wt% and a solid content of 70-95 wt%.
Preferably, the temperature of the pyrolysis treatment is 450-750 ℃, and the time is 20-30 min; the heat value of the pyrolytic carbon is 2500-5500 kcal/kg, and the particle size is less than 10mm.
Preferably, the temperature of the gasification treatment is 850-1050 ℃; the gasification agent adopted in the gasification treatment is the water vapor obtained by the drying treatment; the calorific value of the gasified gas is 900 to 1800kcal/Nm 3 。
Preferably, the condensation treatment adopts a direct heat exchange mode, and the oil-water separation adopts a standing separation mode; and the condensation treatment adopts the condensed water obtained by the oil-water separation as a heat exchange medium.
Preferably, after obtaining the pyrolysis gas and the gasification gas, the method further comprises:
carrying out first combustion treatment on the pyrolysis gas to obtain first high-temperature flue gas, wherein the first high-temperature flue gas is used as a heat source for the drying treatment;
performing second combustion treatment on the gasified gas to obtain second high-temperature flue gas, wherein the second high-temperature flue gas is used as a heat source for pyrolysis treatment;
the temperature of the first high-temperature flue gas is 850-1100 ℃, and the residence time of the flue gas is more than 2s; the temperature of the second high-temperature flue gas is 850-1100 ℃, and the residence time of the flue gas is more than 2s.
The invention also provides a system for the pyrolysis coupling gasification treatment of the oily sludge, which comprises a pretreatment device 1; the pretreatment device 1 is provided with an oily sludge inlet, a pretreated oily sludge outlet and a sundry outlet;
a drying machine 2; the dryer 2 is provided with a pretreated oil sludge inlet, a first high-temperature flue gas inlet, a dried oil sludge outlet, a first low-temperature flue gas outlet and a water vapor outlet, wherein the pretreated oil sludge inlet is connected with the pretreated oil sludge outlet of the pretreatment device 1;
a pyrolysis furnace 3; the pyrolysis furnace 3 is provided with a dried oil sludge inlet, a second high-temperature flue gas inlet, a pyrolytic carbon outlet, a mixed gas outlet and a second low-temperature flue gas outlet, wherein the dried oil sludge inlet is connected with the dried oil sludge outlet of the dryer 2;
a fluidized bed gasification furnace 4; the fluidized bed gasification furnace 4 is provided with a pyrolytic carbon inlet, a steam inlet, a gasified gas outlet and a solid residue outlet, wherein the pyrolytic carbon inlet is connected with the pyrolytic carbon outlet of the pyrolysis furnace 3, and the steam inlet is connected with the steam outlet of the drier 2;
a condensation treatment device 5; the condensation treatment device 5 is provided with a mixed gas inlet, a condensed water inlet, an oil-water mixture outlet and a pyrolysis gas outlet, wherein the mixed gas inlet is connected with the mixed gas outlet of the pyrolysis furnace 3;
an oil-water separation device 6; the oil-water separation device 6 is provided with an oil-water mixture inlet, a condensed water outlet, a sewage outlet and a recovered oil outlet, wherein the oil-water mixture inlet is connected with the oil-water mixture outlet of the condensation treatment device 5, and the condensed water outlet is connected with the condensed water inlet of the condensation treatment device 5;
a first combustion device 7; the first combustion device 7 is provided with a pyrolysis gas inlet, a first natural gas inlet, a first combustion air inlet and a first high-temperature flue gas outlet, wherein the pyrolysis gas inlet is connected with the pyrolysis gas outlet of the condensation processing device 5, and the first high-temperature flue gas outlet is connected with the first high-temperature flue gas inlet of the drying machine 2;
the second combustion device 8; the second combustion device 8 is provided with a gasified gas inlet, a second natural gas inlet, a second combustion air inlet and a second high-temperature flue gas outlet, wherein the gasified gas inlet is communicated with the gasified gas outlet of the fluidized bed gasification furnace 4, and the second high-temperature flue gas outlet is connected with the second high-temperature flue gas inlet of the pyrolysis furnace 3;
a flue gas purification device 9; the flue gas purification device 9 is provided with a first low-temperature flue gas inlet, a second low-temperature flue gas inlet and a standard flue gas outlet, the first low-temperature flue gas inlet is connected with the first low-temperature flue gas outlet of the drying machine 2, and the second low-temperature flue gas inlet is connected with the second low-temperature flue gas outlet of the pyrolysis furnace 3.
Preferably, the drier 2 is a single-shaft drier or a double-shaft drier; the pyrolysis furnace 3 is a single-shaft pyrolysis furnace or a double-shaft pyrolysis furnace; the fluidized bed gasification furnace 4 is a bubbling fluidized bed gasification furnace or a circulating fluidized bed gasification furnace.
Preferably, the flue gas purification device 9 comprises one or a combination of a desulfurization device, a denitrification device and a bag-type dust remover.
Compared with the prior art, the invention has the following beneficial effects:
(1) According to the invention, oily sludge is sequentially subjected to pretreatment, drying and pyrolysis, pyrolytic carbon, mixed gas and second low-temperature flue gas are obtained through pyrolysis, wherein the pyrolytic carbon is gasified to obtain gasified gas, the mixed gas is condensed to obtain pyrolysis gas, the gasified gas and the pyrolysis gas both have certain heat values, and the gasified gas and the pyrolysis gas can be used as heat sources after combustion. The method provided by the invention further recycles the pyrolytic carbon and the mixed gas obtained after pyrolysis, not only can further realize the reduction of the oily sludge, but also improves the resource level of the system, reduces the treatment cost, improves the project profit, and has better development prospect.
(2) Furthermore, as the oily sludge may contain impurities such as stones, iron blocks or wood, if pretreatment is not performed, subsequent system blockage and furnace shutdown maintenance can be caused, and continuous and stable operation of the system is influenced. The method provided by the invention is characterized in that the oily sludge is pretreated to remove impurities in the oily sludge, and the particle size of solid particles in the pretreated oily sludge is controlled to be less than 20mm, so that the running stability of a subsequent drier can be ensured, and a better heat transfer effect is achieved.
(3) Furthermore, the method provided by the invention controls the drying temperature to be 300-450 ℃ and the drying time to be 20-40 min, so that the pretreatment oil sludge can be completely dried in a drying machine, most water is evaporated out, and the evaporation of petroleum hydrocarbon components is reduced.
(4) Furthermore, the method provided by the invention controls the temperature of pyrolysis treatment at 450-750 ℃ and the time at 20-30 min, so that high-calorific-value pyrolysis carbon can be obtained, and the calorific value of the pyrolysis carbon is 2500-5500 kcal/kg. In order to ensure the feeding requirement of the subsequent gasification treatment, the particle size of the pyrolytic carbon is controlled to be less than 10mm.
(5) Furthermore, the method provided by the invention controls the temperature of gasification treatment to be 850-1050 ℃, can obtain high-calorific-value gasified gas, ensures complete gasification of the pyrolytic carbon, and ensures that the oil content of the obtained solid residue is less than 0.3%, so that the method meets national and industrial standards, does not generate tar and has better environmental protection property. Meanwhile, the gasifying agent adopted by the gasification treatment is the water vapor obtained by the drying treatment, so that the water utilization rate of the system and the calorific value of the gasified gas can be further improved.
(6) Furthermore, in the method provided by the invention, the condensation treatment adopts a direct heat exchange mode, so that the oil and water in the mixed gas can be rapidly condensed, the condensation effect of direct heat exchange is better compared with indirect heat exchange, and the problem of tar blockage is avoided. Because the density of the oil is different from that of the water, the oil with smaller density can be collected at the upper layer, and the water with larger density can be collected at the lower layer, so the oil-water separation adopts a standing separation mode, and the upper recovered oil is convenient to collect. Meanwhile, in order to save water, improve the water circulation utilization rate of the system and reduce the operation cost, the method provided by the invention takes the condensed water obtained by oil-water separation as the heat exchange medium for condensation treatment, and the redundant sewage is sent to a sewage treatment plant for treatment.
(7) Furthermore, in order to improve the heat utilization rate of the system and reduce the operation cost, the method provided by the invention takes the first high-temperature flue gas as a heat source for drying treatment and takes the second high-temperature flue gas as a heat source for pyrolysis treatment, and simultaneously controls the temperature of the first high-temperature flue gas to be 850-1100 ℃, the residence time of the flue gas to be more than 2s, the temperature of the second high-temperature flue gas to be 850-1100 ℃ and the residence time of the flue gas to be more than 2s, so that the generation of dioxin can be avoided, and the environmental protection property is better.
(8) The system provided by the invention has a good treatment effect on the oily sludge, can recycle high-value pyrolytic carbon, has small floor area, low investment and low operation cost, can be skid-mounted, and is suitable for treating different types of oily sludge such as ground oil sludge, oil-based drilling cuttings, refinery three-sludge and the like.
Drawings
FIG. 1 is a process flow diagram of the process for pyrolysis coupled gasification treatment of oily sludge according to the present invention;
fig. 2 is a schematic structural diagram of a system for pyrolysis coupling gasification treatment of oily sludge, wherein: 1-a pretreatment device, 2-a drier, 3-a pyrolysis furnace, 4-a fluidized bed gasification furnace, 5-a condensation treatment device, 6-an oil-water separation device, 7-a first combustion device, 8-a second combustion device and 9-a flue gas purification device.
Detailed Description
The invention provides a method for pyrolysis coupling gasification treatment of oily sludge, which comprises the following steps:
pretreating the oily sludge to obtain pretreated oil sludge and impurities;
drying the pretreated oil sludge to obtain dried oil sludge, water vapor and first low-temperature flue gas;
performing pyrolysis treatment on the dried oil sludge to obtain pyrolytic carbon, mixed gas and second low-temperature flue gas;
gasifying the pyrolytic carbon to obtain gasified gas and solid residues;
condensing the mixed gas to obtain an oil-water mixture and pyrolysis gas;
carrying out oil-water separation on the oil-water mixture to obtain recovered oil, condensed water and sewage;
and carrying out flue gas purification treatment on the first low-temperature flue gas and the second low-temperature flue gas to obtain the flue gas reaching the standard.
The invention has no special requirements on the source and the type of the oily sludge, and the oily sludge known by the technical personnel in the field can be harmlessly treated by using the method of the invention, in particular to different types of oily sludge such as oil sludge on the ground, oil-based drill cuttings, three sludge in a refinery and the like.
The invention pretreats the oily sludge to obtain the pretreated oil sludge and impurities. In the invention, the liquid content of the oily sludge is preferably 30-80 wt%, more preferably 40-70 wt%, and the solid content is preferably 20-70 wt%, preferably 30-60 wt%; the pretreatment mode preferably comprises one or a combination of sorting, crushing and screening, and in the specific embodiment of the invention, the pretreatment mode is preferably crushing, or a combination of crushing and screening, or a combination of sorting, crushing and screening; in the embodiment of the invention, when the oily sludge contains metal (iron blocks, iron wires and the like) and non-metal impurities (stones, wood and the like), the metal impurities in the oily sludge are preferably sorted by sorting, the waste metal impurities are crushed into small-particle-size impurities by crushing, and finally the impurities which are difficult to crush are filtered out by screening. In the invention, the liquid content of the pretreated oil sludge is preferably 35 to 85wt%, preferably 45 to 80wt%, the solid content is preferably 15 to 65wt%, more preferably 20 to 50wt%, and the particle size of the solid particles in the pretreated oil sludge is preferably less than 20mm, more preferably less than 15mm. If the particle size of the impurities or the oily sludge is too large, the impurities or the oily sludge directly enter the drying machine to cause blockage, and the service life of the spiral shaft is influenced. The method provided by the invention controls the particle size of solid particles in the oil sludge to be less than 20mm through pretreatment, and can ensure the stability and continuity of feeding.
After the pretreated oil sludge is obtained, drying treatment is carried out on the pretreated oil sludge to obtain dried oil sludge, water vapor and first low-temperature flue gas. In the invention, the temperature of the drying treatment is preferably 300-450 ℃, more preferably 350-400 ℃, and the time of the drying treatment is preferably 20-40 min, more preferably 25-35 min. In the present invention, the dried sludge preferably has a liquid content of 5 to 30wt%, more preferably 10 to 25wt%, and a solid content of 70 to 95wt%, more preferably 80 to 90wt%. The liquid content of the oily sludge is high, so that the cost of subsequent pyrolysis treatment can be increased, the pretreated oil sludge is dried firstly, the liquid content of the pretreated oil sludge is reduced, the energy consumption of the subsequent pyrolysis treatment can be reduced, and the lowest cost is realized.
After the dried oil sludge is obtained, the dried oil sludge is subjected to pyrolysis treatment to obtain pyrolytic carbon, mixed gas and second low-temperature flue gas. In the invention, the thermal value of the pyrolytic carbon is 2500-5500 kcal/kg, and the particle size is less than 10mm; the temperature of the pyrolysis treatment is preferably 450 to 750 ℃, more preferably 500 to 700 ℃, and the time of the pyrolysis treatment is preferably 20 to 30min, more preferably 22 to 25min. The invention controls the temperature and time of pyrolysis in the range, and can obtain the pyrolytic carbon with high heat value and particle size meeting the requirement.
After the pyrolytic carbon is obtained, the invention gasifies the pyrolytic carbon to obtain gasified gas and solid residues. In the invention, the temperature of the gasification treatment is preferably 850-1050 ℃, and more preferably 900-1000 ℃; the heat value of the gasified gas is 900-1800 kcal/Nm 3 . The invention controls the temperature of gasification treatment within the range, and can ensure that the obtained heat value is 900-1800 kcal/Nm 3 The gasified gas and the pyrolytic carbon can be completely gasified, and the oil content of the obtained solid residue is less than 0.3wt%, thereby meeting the national and industrial environmental protection standards. In order to improve the water utilization rate of the system and the calorific value of gasified gas, in the invention, the gasifying agent adopted by the gasification treatment is the water vapor obtained by the drying treatment.
After the mixed gas is obtained, the mixed gas is condensed to obtain a pyrolysis gas and oil-water mixture. The invention separates the pyrolysis gas and the oil-water mixture through condensation treatment; the condensation treatment adopts a direct heat exchange mode, the used heat exchange medium is condensed water, and the temperature of the condensed water is 20-40 ℃; the invention adopts a direct heat exchange mode for condensation treatment, can quickly condense oil and water in the mixed gas, has better condensation effect of direct heat exchange compared with indirect heat exchange, and avoids the problem of tar blockage.
In the invention, the oil-water mixture obtained by condensation is subjected to oil-water separation to obtain recovered oil, condensed water and sewage. In the invention, the oil-water separation preferably adopts a standing separation mode, light oil is on the upper layer, and water is on the lower layer, so that recovered oil is convenient to collect; in a specific embodiment of the invention, the bottom of the device for standing separation is preferably provided with two water pumping pipes, one water pumping pipe is communicated with the condensing device, the pumped water is taken out as condensed water, and the rest water is taken out as sewage through the other water pumping pipe and sent to a sewage treatment plant for further treatment. In order to save water, improve the water circulation utilization rate of the system and reduce the operation cost, the method provided by the invention takes the condensed water obtained by oil-water separation as the heat exchange medium of the condensation treatment.
After obtaining the pyrolysis gas, the invention preferably carries out the first combustion treatment on the pyrolysis gas to obtain the first high-temperature flue gas. In the invention, the first combustion treatment is preferably carried out under the conditions of fuel gas and combustion-supporting gas, wherein the fuel gas is preferably natural gas (recorded as first natural gas), and the combustion-supporting gas is preferably air (recorded as first combustion-supporting air); the first high-temperature flue gas is used as a heat source for the drying treatment, so that the heat utilization rate of the system is improved, and the operation cost is reduced. When the first high-temperature flue gas is adopted for drying treatment, the temperature of the first high-temperature flue gas is controlled to be 850-1100 ℃, and the residence time of the flue gas is more than 2s, so that the generation of dioxin is avoided, and the environment friendliness is better.
After obtaining the gasified gas, the invention preferably carries out a second combustion treatment on the gasified gas to obtain a second high-temperature flue gas. In the invention, the second combustion treatment is preferably carried out under the conditions of fuel gas and combustion-supporting gas, the fuel gas is preferably natural gas (recorded as second natural gas), and the combustion-supporting gas is preferably air (recorded as second combustion-supporting air); the second high-temperature flue gas is used as a heat source for pyrolysis treatment, so that the heat utilization rate of the system is improved, and the operation cost is reduced. When the second high-temperature flue gas is used for pyrolysis treatment, the temperature of the second high-temperature flue gas is controlled to be 850-1100 ℃, and the residence time of the flue gas is more than 2s, so that the generation of dioxin is avoided, and the environmental protection performance of the system is improved.
After the first low-temperature flue gas and the second low-temperature flue gas are obtained, the first low-temperature flue gas and the second low-temperature flue gas are subjected to flue gas purification treatment so as to obtain the flue gas reaching the standard. In the invention, the temperature of the first low-temperature flue gas and the second low-temperature flue gas is preferably controlled to be 200-300 ℃ so as to ensure that the heat in the flue gas is utilized as much as possible and improve the heat utilization rate of the system.
The invention also provides a system for the pyrolysis coupling gasification treatment of the oily sludge, which comprises a pretreatment device 1, a drier 2, a pyrolysis furnace 3, a fluidized bed gasification furnace 4, a condensation treatment device 5, an oil-water separation device 6, a first combustion device 7, a second combustion device 8 and a flue gas purification device 9.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a pretreatment device 1. In the invention, the pretreatment device 1 comprises one or a combination of a plurality of sorting devices, crushing devices and screening devices; the pretreatment device 1 is provided with an oily sludge inlet, a pretreated oily sludge outlet and a sundries outlet.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a drier 2. In the invention, the drier 2 is provided with a pretreated oil sludge inlet, a first high-temperature flue gas inlet, a dried oil sludge outlet, a first low-temperature flue gas outlet and a water vapor outlet, wherein the pretreated oil sludge inlet is connected with a pretreated oil sludge outlet of the pretreatment device 1; the drier 2 is preferably a single-shaft drier or a double-shaft drier; in the specific embodiment of the invention, when the liquid content of the oily sludge is less than 50%, the drying requirement can be met by adopting a single-shaft type drying machine, and when the liquid content of the oily sludge is more than or equal to 50wt%, because the liquid content is higher, a double-shaft type drying machine is preferably adopted to realize rapid dehydration. The invention adopts a single-shaft or double-shaft type drying machine, the shaft is arranged in a hollow way, and hot flue gas, steam or heat conducting oil is filled in the shaft, so that the drying efficiency can be improved.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a pyrolysis furnace 3. In the invention, the pyrolysis furnace 3 is provided with a dried oil sludge inlet, a second high-temperature flue gas inlet, a pyrolytic carbon outlet, a mixed gas outlet and a second low-temperature flue gas outlet, wherein the dried oil sludge inlet is connected with the dried oil sludge outlet of the dryer 2. In the present invention, the pyrolysis furnace 3 is preferably a single-shaft pyrolysis furnace or a twin-shaft pyrolysis furnace; in the specific embodiment of the invention, when the liquid content of the dried oil sludge is less than 15wt%, the pyrolysis requirement can be met by adopting a single-shaft pyrolysis furnace, and when the liquid content of the dried oil sludge is more than or equal to 15wt%, the double-shaft pyrolysis furnace is preferably adopted to realize rapid pyrolysis due to higher liquid content. The pyrolysis treatment is endothermic reaction, the invention adopts a single-shaft or double-shaft pyrolysis furnace, the shaft is arranged in a hollow way, and the shaft is filled with hot flue gas, thus reducing the energy consumption of the pyrolysis treatment.
In the invention, the drier 2 is preferably arranged right above the pyrolysis furnace 3, the pretreated oil sludge inlet of the drier 2 is preferably arranged at the same side with the pyrolysis carbon outlet of the pyrolysis furnace 3, and the dried oil sludge outlet of the drier 2 is preferably arranged at the same side with the dried oil sludge inlet of the pyrolysis furnace 3; through the arrangement, the occupied area can be reduced, and the skid-mounted equipment is facilitated.
In the invention, the distance between the dried oil sludge outlet of the drier 2 and the dried oil sludge inlet of the pyrolysis furnace 3 is preferably 40-80 cm, and the dried oil sludge outlet and the dried oil sludge inlet are preferably connected by adopting a stainless steel pipeline, and the stainless steel pipeline is wrapped by a heat insulation material; the invention controls the distance between the dried oil sludge outlet of the drier 2 and the dried oil sludge inlet of the pyrolysis furnace 3 within the range, can avoid the problem of blockage of tar, dust and the like caused by overlong distance, adopts the stainless steel pipeline for connection, can prevent a medium from corroding the pipeline, wraps a heat insulation material outside the stainless steel pipeline, can prevent heat loss and improves the heat utilization rate.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a fluidized bed gasification furnace 4. In the invention, the fluidized bed gasification furnace 4 is provided with a pyrolytic carbon inlet, a water vapor inlet, a gasified gas outlet and a solid residue outlet, wherein the pyrolytic carbon inlet is connected with the pyrolytic carbon outlet of the pyrolysis furnace 3, and the water vapor inlet is connected with the water vapor outlet of the drying machine 2. In the present invention, the fluidized-bed gasification furnace is preferably a bubbling fluidized-bed gasification furnace or a circulating fluidized-bed gasification furnace; the fluidized bed gasification furnace has the advantages of low gasification efficiency and poor environmental protection, and can improve the gasification efficiency and has good environmental protection.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a condensation treatment device 5. In the invention, the condensation treatment device 5 is provided with a mixed gas inlet, a condensed water inlet, an oil-water mixture outlet and a pyrolysis gas outlet, wherein the mixed gas inlet is connected with the mixed gas outlet of the pyrolysis furnace 3. In the present invention, the condensation treatment apparatus is preferably a spray tower.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises an oil-water separation device 6; the oil-water separation device 6 is provided with an oil-water mixture inlet, a condensed water outlet, a sewage outlet and a recovered oil outlet, wherein the oil-water mixture inlet is connected with the oil-water mixture outlet of the condensation treatment device 5, and the condensed water outlet is connected with the condensed water inlet of the condensation treatment device 5. In the present invention, the oil-water separation device is preferably a static separation type oil-water separation device.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a first combustion device 7. In the invention, the first combustion device 7 is provided with a pyrolysis gas inlet, a first natural gas inlet, a first combustion air inlet and a first high-temperature flue gas outlet, wherein the pyrolysis gas inlet is connected with the pyrolysis gas outlet of the condensation treatment device 5, and the first high-temperature flue gas outlet is connected with the first high-temperature flue gas inlet of the drying machine 2. In the present invention, the first combustion device is preferably a gas furnace.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a second combustion device 8. In the invention, the second combustion device 8 is provided with a gasified gas inlet, a second natural gas inlet, a second combustion air inlet and a second high-temperature flue gas outlet, wherein the gasified gas inlet is communicated with the gasified gas outlet of the fluidized bed gasification furnace 4, and the second high-temperature flue gas outlet is connected with the second high-temperature flue gas inlet of the pyrolysis furnace 3. In the present invention, the second combustion means is preferably a gas furnace.
The system for the pyrolysis coupling gasification treatment of the oily sludge comprises a flue gas purification device 9. In the invention, the flue gas purification device 9 is provided with a first low-temperature flue gas inlet, a second low-temperature flue gas inlet and a standard flue gas outlet, the first low-temperature flue gas inlet is connected with the first low-temperature flue gas outlet of the drying machine 2, and the second low-temperature flue gas inlet is connected with the second low-temperature flue gas outlet of the pyrolysis furnace 3. In the present invention, the flue gas purification device 9 comprises one or a combination of several of a desulfurization device, a denitrification device and a bag-type dust collector.
When the system provided by the invention is used for carrying out pyrolysis coupling gasification treatment on the oily sludge, the control conditions of each step are consistent with the scheme, and the detailed description is omitted.
FIG. 1 is a process flow diagram of the process for pyrolysis coupled gasification treatment of oily sludge according to the present invention; FIG. 2 is a schematic structural diagram of a system for pyrolysis-coupled gasification treatment of oily sludge according to the present invention.
The method and system of the present invention are described in detail below with reference to FIGS. 1-2: sending the oily sludge into a pretreatment device 1 for pretreatment to obtain pretreated oil sludge and impurities; sending the pretreated oil sludge into a drier 2 for drying treatment to obtain dried oil sludge, water vapor and first low-temperature flue gas, wherein the water vapor is introduced into a gasification treatment device to be used as a gasification agent; feeding the dried oil sludge into a pyrolysis furnace 3 for pyrolysis treatment to obtain pyrolysis carbon, mixed gas and second low-temperature flue gas; sending the pyrolytic carbon into a fluidized bed gasification furnace 4 for gasification treatment to obtain gasified gas and solid residues; sending the mixed gas into a condensation treatment device 5 for condensation treatment to obtain an oil-water mixture and pyrolysis gas; sending the oil-water mixture into an oil-water separation device 6 for oil-water separation to obtain recovered oil, condensed water and sewage, and introducing the condensed water into a condensation treatment device to serve as a cooling medium; feeding the pyrolysis gas into a first combustion device 7, and performing first combustion treatment under the action of first natural gas and first combustion-supporting air to obtain first high-temperature flue gas, wherein the first high-temperature flue gas is introduced into a drier 2 to be used as a heat source; sending the gasified gas into a second combustion device 8, and carrying out second combustion treatment under the action of second natural gas and second combustion-supporting air to obtain second high-temperature flue gas, wherein the second high-temperature flue gas is introduced into the pyrolysis furnace 3 to be used as a heat source; and sending the first low-temperature flue gas and the second low-temperature flue gas into a flue gas purification device 9 for flue gas purification treatment to obtain the flue gas reaching the standard.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
Example 1
The method is characterized in that the oily sludge falling to the ground is treated by adopting a system for the pyrolysis coupling gasification treatment of the oily sludge, the component analysis of the oily sludge is shown in table 1, wherein the process flow of the pyrolysis coupling gasification treatment of the oily sludge is shown in fig. 1, and the structural schematic diagram of the system is shown in fig. 2. The specific treatment process comprises the following steps:
TABLE 1 analysis of the composition of oily sludge
Item Liquid content Solid content
Unit of wt％ wt％
Numerical value 30 70
Sending the oily sludge with the liquid content of 30wt% and the solid content of 70wt% into a pretreatment device 1 for pretreatment to obtain pretreated oil sludge and impurities with the liquid content of 35wt% and the solid content of 65 wt%. The pretreatment is crushing and screening, the particle size of solid particles in the pretreated oil sludge is 15mm, and the impurities are stones and wood.
And sending the pretreated oil sludge into a drier 2 for drying treatment to obtain dried oil sludge with a liquid content of 5wt% and a solid content of 95wt%, water vapor and first low-temperature flue gas. The drying treatment temperature is 300 ℃, the drying treatment time is 20min, a single-shaft drying machine is adopted in the drying treatment, and the temperature of the first low-temperature flue gas is 250 ℃.
And sending the dried oil sludge into a pyrolysis furnace 3 for pyrolysis treatment to obtain pyrolytic carbon, mixed gas and second low-temperature flue gas. The pyrolysis treatment temperature is 450 ℃, the pyrolysis treatment time is 20min, the pyrolysis treatment adopts a single-shaft pyrolysis furnace, the calorific value of the obtained pyrolysis carbon is 3000kcal/kg, the particle size is less than 10mm, and the temperature of the second low-temperature flue gas is 250 ℃.
And sending the pyrolytic carbon into a fluidized bed gasification furnace 4 for gasification treatment to obtain gasified gas and solid residues. The fluidized bed is a bubbling fluidized bed, and the temperature of the gasification treatment is 850 ℃. The gasification agent adopted in the gasification treatment is the water vapor obtained by the drying treatment, and the calorific value of the gasified gas is 1200kcal/Nm 3 The oil content of the solid residue was 0.2% by weight.
And sending the mixed gas into a condensation treatment device 5 for condensation treatment to obtain an oil-water mixture and pyrolysis gas, and sending the oil-water mixture into an oil-water separation device 6 for oil-water separation to obtain recovered oil, condensed water and sewage. The condensation treatment adopts a direct heat exchange mode, the oil-water separation adopts a standing separation mode, and the condensation treatment adopts condensed water obtained by the oil-water separation as a heat exchange medium.
And the pyrolysis gas is sent into a first combustion device 7, and is subjected to first combustion treatment under the action of natural gas and combustion-supporting air to obtain first high-temperature flue gas. And (3) sending the gasified gas into a second combustion device 8, and carrying out second combustion treatment under the action of natural gas and combustion-supporting air to obtain second high-temperature flue gas. And introducing the first high-temperature flue gas into the drier 2 as a heat source for drying treatment, and introducing the second high-temperature flue gas into the pyrolysis furnace 3 as a heat source for pyrolysis treatment. The temperature of the first high-temperature flue gas is 850 ℃, and the residence time of the flue gas in the drier 2 is 2.5s; the temperature of the second high-temperature flue gas is 850 ℃, and the residence time of the flue gas in the pyrolysis furnace 3 is 2.5s.
Feeding the first low-temperature flue gas and the second low-temperature flue gas into a flue gas purification device 9 for flue gas purification treatment to obtain standard flue gas; the flue gas purification device 8 consists of a desulfurization device and a denitrification device, and finally realizes harmless, quantitative reduction and resource utilization of the oily sludge.
Example 2
The system for pyrolysis coupling gasification treatment of the oily sludge is used for treating the oily sludge of oil-based drill cuttings in Xinjiang, and the component analysis of the oily sludge is shown in Table 2, wherein the process flow of the pyrolysis coupling gasification treatment of the oily sludge is shown in figure 1, and the structural schematic diagram of the system is shown in figure 2. The specific treatment process comprises the following steps:
TABLE 2 analysis of the composition of oily sludge (mass fraction)
Item Liquid content Solid content
Unit wt％ wt％
Numerical value 50 50
Sending the oily sludge with the liquid content of 50wt% and the solid content of 50wt% into a pretreatment device 1 for pretreatment to obtain pretreated oil sludge and impurities with the liquid content of 55wt% and the solid content of 45 wt%. The pretreatment mode is crushing, the particle size of solid particles in the pretreated oil sludge is 18mm, and the impurities are stones.
And sending the pretreated oil sludge into a drier 2 for drying treatment to obtain dried oil sludge with a liquid content of 14wt% and a solid content of 86wt%, water vapor and first low-temperature flue gas. The drying treatment temperature is 350 ℃, the drying treatment time is 25min, a single-shaft type drying machine is adopted for drying treatment, and the temperature of the first low-temperature flue gas is 300 ℃.
And sending the dried oil sludge into a pyrolysis furnace 3 for pyrolysis treatment to obtain pyrolytic carbon, mixed gas and second low-temperature flue gas. The temperature of the pyrolysis treatment is 550 ℃, the time is 23min, and the pyrolysis treatment adopts a single-shaft pyrolysis furnace. The obtained pyrolytic carbon has a calorific value of 2500kcal/kg, a particle size of less than 10mm, and a temperature of the second low-temperature flue gas of 300 ℃.
And sending the pyrolytic carbon into a fluidized bed gasification furnace 4 for gasification treatment to obtain gasified gas and solid residues. The fluidized bed is a bubbling fluidized bed, and the temperature of the gasification treatment is 900 ℃. And the gasifying agent adopted by the gasification treatment is the water vapor obtained by the drying treatment. The calorific value of the gasification gas is 900kcal/Nm 3 The oil content of the solid residue was 0.15% by weight.
And sending the mixed gas into a condensation treatment device 5 for condensation treatment to obtain an oil-water mixture and pyrolysis gas, and sending the oil-water mixture into an oil-water separation device 6 for oil-water separation to obtain recovered oil, condensed water and sewage. The condensation treatment adopts a direct heat exchange mode, the oil-water separation adopts a standing separation mode, and the condensation treatment adopts condensed water obtained by the oil-water separation as a heat exchange medium.
And feeding the pyrolysis gas into a first combustion device 7, and performing first combustion treatment under the action of natural gas and combustion-supporting air to obtain first high-temperature flue gas. And sending the gasified gas into a second combustion device, and carrying out second combustion treatment under the action of natural gas and combustion-supporting air to obtain second high-temperature flue gas. And sending the first high-temperature flue gas into a drier to be used as a heat source for drying treatment, and sending the second high-temperature flue gas into a pyrolysis furnace to be used as a heat source for pyrolysis treatment. Wherein the temperature of the first high-temperature flue gas is 900 ℃, and the residence time of the flue gas in the drier is 2.5s; the temperature of the second high-temperature flue gas is 900 ℃, and the residence time of the flue gas in the pyrolysis furnace is 2.5s.
And sending the first low-temperature flue gas and the second low-temperature flue gas into a flue gas purification device 9 for flue gas purification treatment to obtain the flue gas reaching the standard. The flue gas purification device 8 is composed of a desulfurization device, a denitration device and a bag-type dust collector, and finally realizes harmless, reduction and resource utilization of the oily sludge.
Example 3
The system for pyrolysis coupling gasification treatment of the oily sludge is used for treating the oily sludge generated by a certain refinery, the composition analysis of the oily sludge is shown in table 3, wherein the process flow of the pyrolysis coupling gasification treatment of the oily sludge is shown in fig. 1, and the structural schematic diagram of the used system is shown in fig. 2. The specific treatment process comprises the following steps:
TABLE 3 analysis of the composition of oily sludge
Item Liquid content Solid content
Unit wt％ wt％
Numerical value 60 40
Sending the oily sludge with the liquid content of 60wt% and the solid content of 40wt% into a pretreatment device 1 for pretreatment to obtain pretreated oil sludge and impurities with the liquid content of 65wt% and the solid content of 35 wt%. The pretreatment comprises sorting, crushing and screening, the particle size of solid particles in the pretreated oil sludge is 10mm, and the impurities are stones, wood and iron blocks.
And sending the pretreated oil sludge into a drier 2 for drying treatment to obtain dried oil sludge with a liquid content of 20wt% and a solid content of 80wt%, water vapor and first low-temperature flue gas. The drying treatment temperature is 400 ℃, the drying treatment time is 30min, a double-shaft type drying machine is adopted for drying treatment, and the temperature of the first low-temperature flue gas is 200 ℃.
And sending the dried oil sludge into a pyrolysis furnace 3 for pyrolysis treatment to obtain pyrolytic carbon, mixed gas and second low-temperature flue gas. The temperature of the pyrolysis treatment is 650 ℃, the time is 28min, and the pyrolysis treatment adopts a double-shaft pyrolysis furnace. The obtained pyrolytic carbon has a calorific value of 4500kcal/kg, a particle size of less than 10mm, and a temperature of the second low-temperature flue gas of 200 ℃.
And sending the pyrolytic carbon into a fluidized bed gasification furnace 4 for gasification treatment to obtain gasified gas and solid residues. The fluidized bed is a circulating fluidized bed, and the temperature of the gasification treatment is 1000 ℃. The gasifying agent adopted in the gasification treatment is the steam obtained by the drying treatment. The calorific value of the gasification gas is 1600kcal/Nm 3 The oil content of the solid residue was 0.2% by weight.
And sending the mixed gas into a condensation treatment device 5 for condensation treatment to obtain an oil-water mixture and pyrolysis gas, and sending the oil-water mixture into an oil-water separation device 6 for oil-water separation to obtain recovered oil, condensed water and sewage. The condensation treatment adopts a direct heat exchange mode, the oil-water separation adopts a standing separation mode, and the condensation treatment adopts condensed water obtained by the oil-water separation as a heat exchange medium.
And feeding the pyrolysis gas into a first combustion device 7, and performing first combustion treatment under the action of natural gas and combustion-supporting air to obtain first high-temperature flue gas. And (3) sending the gasified gas into a second combustion device 8, and carrying out second combustion treatment under the action of natural gas and combustion-supporting air to obtain second high-temperature flue gas. The first high-temperature flue gas is sent into a drier to be used as a heat source for drying treatment, and the second high-temperature flue gas is sent into a pyrolysis furnace to be used as a heat source for pyrolysis treatment. Wherein the temperature of the first high-temperature flue gas is 980 ℃, and the residence time of the flue gas in the drier is 2.5s; the temperature of the second high-temperature flue gas is 980 ℃, and the residence time of the flue gas in the pyrolysis furnace is 2.5s.
And sending the first low-temperature flue gas and the second low-temperature flue gas into a flue gas purification device 9 for flue gas purification treatment to obtain the flue gas reaching the standard. The flue gas purification device 8 consists of a desulfurization device, a denitrification device and a bag-type dust collector, and finally realizes harmless, quantitative reduction and resource utilization of the oily sludge.
Example 4
The system for pyrolysis coupling gasification treatment of the oily sludge is used for treating the oily sludge of oil sludge at the bottom of a certain plant tank, the component analysis of the oily sludge is shown in table 4, wherein the process flow of the pyrolysis coupling gasification treatment of the oily sludge is shown in fig. 1, and the structural schematic diagram of the used system is shown in fig. 2. The specific treatment process comprises the following steps:
TABLE 4 analysis of the composition of oily sludge
Item Liquid content Solid content
Unit of wt％ wt％
Numerical value 80 20
The oily sludge with the liquid content of 80wt% and the solid content of 20wt% is sent into a pretreatment device 1 for pretreatment, and pretreated oil sludge and impurities with the liquid content of 85wt% and the solid content of 15wt% are obtained. The pretreatment is crushing and screening, the particle size of solid particles in the pretreated oil sludge is 16mm, and the impurities are stones and wood.
And sending the pretreated oil sludge into a drier 2 for drying treatment to obtain dried oil sludge with a liquid content of 30wt% and a solid content of 70wt%, water vapor and first low-temperature flue gas. The drying treatment temperature is 450 ℃, the drying treatment time is 40min, the drying treatment adopts a double-shaft type drying machine, and the temperature of the first low-temperature flue gas is 300 ℃.
And (3) feeding the dried oil sludge into a pyrolysis furnace 3 for pyrolysis treatment to obtain pyrolysis carbon, mixed gas and second low-temperature flue gas. The temperature of the pyrolysis treatment is 750 ℃, the time is 30min, and the pyrolysis treatment adopts a double-shaft pyrolysis furnace. The obtained pyrolytic carbon has a calorific value of 5500kcal/kg, a particle size of less than 10mm, and a temperature of the second low-temperature flue gas of 300 ℃.
And sending the pyrolytic carbon into a fluidized bed gasification furnace 4 for gasification treatment to obtain gasified gas and solid residues. The gasification treatment adopts a fluidized bed gasification mode, the fluidized bed is a circulating fluidized bed, and the temperature of the gasification treatment is 1050 ℃. And the gasifying agent adopted by the gasification treatment is the water vapor obtained by the drying treatment. The calorific value of the gasification gas is 1800kcal/Nm 3 The oil content of the solid residue was 0.18% by weight.
And sending the mixed gas into a condensation treatment device 5 for condensation treatment to obtain an oil-water mixture and pyrolysis gas, and sending the oil-water mixture into an oil-water separation device 6 for oil-water separation to obtain recovered oil, condensed water and sewage. The condensation treatment adopts a direct heat exchange mode, the oil-water separation adopts a standing separation mode, and the condensation treatment adopts condensed water obtained by the oil-water separation as a heat exchange medium.
And feeding the pyrolysis gas into a first combustion device 7, and performing first combustion treatment under the action of natural gas and combustion-supporting air to obtain first high-temperature flue gas. And (3) sending the gasified gas into a second combustion device 8, and carrying out second combustion treatment under the action of natural gas and combustion-supporting air to obtain second high-temperature flue gas. The first high-temperature flue gas is sent into a drier to be used as a heat source for drying treatment, and the second high-temperature flue gas is sent into a pyrolysis furnace to be used as a heat source for pyrolysis treatment. Wherein the temperature of the first high-temperature flue gas is 1100 ℃, and the residence time of the flue gas in the drier is 2.5s; the temperature of the second high-temperature flue gas is 1100 ℃, and the residence time of the flue gas in the pyrolysis furnace is 2.5s.
And sending the first low-temperature flue gas and the second low-temperature flue gas into a flue gas purification device 9 for flue gas purification treatment to obtain the flue gas reaching the standard. The flue gas purification device 8 is composed of a desulfurization device, a denitration device and a bag-type dust collector, and finally realizes harmless, reduction and resource utilization of the oily sludge.
The embodiment shows that the method provided by the invention can recover oil products in the oily sludge, has good economic benefit, simultaneously realizes the reduction and harmless treatment of the oily sludge, can obtain solid residues with the oil content less than 0.3wt%, can meet the national standard requirements, and is easy for industrialized popularization and application; the system provided by the invention has the advantages of small floor area, skid-mounted type, low investment and low operation cost, and is suitable for treating different types of oily sludge such as oil sludge on the ground, oil-based drilling cuttings, refinery three-sludge and the like.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.

Claims (10)

1. A method for pyrolysis coupling gasification treatment of oily sludge is characterized by comprising the following steps:
pretreating the oily sludge to obtain pretreated oil sludge and impurities;
drying the pretreated oil sludge to obtain dried oil sludge, water vapor and first low-temperature flue gas;
performing pyrolysis treatment on the dried oil sludge to obtain pyrolytic carbon, mixed gas and second low-temperature flue gas;
gasifying the pyrolytic carbon to obtain gasified gas and solid residues;
condensing the mixed gas to obtain an oil-water mixture and pyrolysis gas;
carrying out oil-water separation on the oil-water mixture to obtain recovered oil, condensed water and sewage;
and carrying out flue gas purification treatment on the first low-temperature flue gas and the second low-temperature flue gas to obtain the flue gas reaching the standard.
2. The method for the pyrolysis coupling gasification treatment of the oily sludge according to claim 1, wherein the liquid content of the oily sludge is 30-80 wt%, and the solid content is 20-70 wt%; the liquid content of the pretreated oil sludge is 35-85 wt%, the solid content is 15-65 wt%, and the particle size of solid particles in the pretreated oil sludge is less than 20mm; the pretreatment mode comprises one or more of sorting, crushing and screening.
3. The method for the pyrolysis coupling gasification treatment of the oily sludge according to claim 1, wherein the drying treatment is carried out at a temperature of 300-450 ℃ for 20-40 min; the dried oil sludge has a liquid content of 5-30 wt% and a solid content of 70-95 wt%.
4. The method for the pyrolysis coupling gasification treatment of the oily sludge according to claim 1, wherein the temperature of the pyrolysis treatment is 450-750 ℃ and the time is 20-30 min; the heat value of the pyrolytic carbon is 2500-5500 kcal/kg, and the particle size is less than 10mm.
5. The method for the pyrolysis-coupled gasification treatment of the oil-containing sludge according to claim 1, wherein the temperature of the gasification treatment is 850-1050 DEG C(ii) a The gasification agent adopted in the gasification treatment is the water vapor obtained by the drying treatment; the heat value of the gasified gas is 900-1800 kcal/Nm 3 。
6. The method for the pyrolysis coupling gasification treatment of the oily sludge according to claim 1, wherein the condensation treatment adopts a direct heat exchange mode, and the oil-water separation adopts a standing separation mode; and the condensation treatment adopts condensed water obtained by the oil-water separation as a heat exchange medium.
7. The method for the pyrolysis coupling gasification treatment of the oily sludge according to claim 1, wherein after obtaining the pyrolysis gas and the gasification gas, the method further comprises:
carrying out first combustion treatment on the pyrolysis gas to obtain first high-temperature flue gas, wherein the first high-temperature flue gas is used as a heat source for the drying treatment;
performing second combustion treatment on the gasified gas to obtain second high-temperature flue gas, wherein the second high-temperature flue gas is used as a heat source for pyrolysis treatment;
the temperature of the first high-temperature flue gas is 850-1100 ℃, and the residence time of the flue gas is more than 2s; the temperature of the second high-temperature flue gas is 850-1100 ℃, and the residence time of the flue gas is more than 2s.
8. The system for the pyrolysis coupling gasification treatment of the oily sludge is characterized by comprising a pretreatment device (1); the pretreatment device (1) is provided with an oily sludge inlet, a pretreated oil sludge outlet and a sundry outlet;
a drying machine (2); the drier (2) is provided with a pretreated oil sludge inlet, a first high-temperature flue gas inlet, a dried oil sludge outlet, a first low-temperature flue gas outlet and a water vapor outlet, wherein the pretreated oil sludge inlet is connected with the pretreated oil sludge outlet of the pretreatment device (1);
a pyrolysis furnace (3); the pyrolysis furnace (3) is provided with a dried oil sludge inlet, a second high-temperature flue gas inlet, a pyrolytic carbon outlet, a mixed gas outlet and a second low-temperature flue gas outlet, wherein the dried oil sludge inlet is connected with a dried oil sludge outlet of the drying machine (2);
a fluidized bed gasification furnace (4); the fluidized bed gasification furnace (4) is provided with a pyrolytic carbon inlet, a water vapor inlet, a gasified gas outlet and a solid residue outlet, wherein the pyrolytic carbon inlet is connected with the pyrolytic carbon outlet of the pyrolysis furnace (3), and the water vapor inlet is connected with the water vapor outlet of the drier (2);
a condensation processing device (5); the condensation treatment device (5) is provided with a mixed gas inlet, a condensed water inlet, an oil-water mixture outlet and a pyrolysis gas outlet, wherein the mixed gas inlet is connected with the mixed gas outlet of the pyrolysis furnace (3);
an oil-water separation device (6); the oil-water separation device (6) is provided with an oil-water mixture inlet, a condensed water outlet, a sewage outlet and a recovered oil outlet, wherein the oil-water mixture inlet is connected with the oil-water mixture outlet of the condensation treatment device (5), and the condensed water outlet is connected with the condensed water inlet of the condensation treatment device (5);
a first combustion device (7); the first combustion device (7) is provided with a pyrolysis gas inlet, a first natural gas inlet, a first combustion air inlet and a first high-temperature flue gas outlet, wherein the pyrolysis gas inlet is connected with the pyrolysis gas outlet of the condensation treatment device (5), and the first high-temperature flue gas outlet is connected with the first high-temperature flue gas inlet of the drying machine (2);
a second combustion device (8); the second combustion device (8) is provided with a gasified gas inlet, a second natural gas inlet, a second combustion air inlet and a second high-temperature flue gas outlet, wherein the gasified gas inlet is communicated with the gasified gas outlet of the fluidized bed gasification furnace (4), and the second high-temperature flue gas outlet is connected with the second high-temperature flue gas inlet of the pyrolysis furnace (3);
a flue gas purification device (9); flue gas purification device (9) are provided with first low temperature flue gas entry, second low temperature flue gas entry and flue gas outlet up to standard, first low temperature flue gas entry with the first low temperature flue gas outlet of mummification machine (2) links to each other, second low temperature flue gas entry with the second low temperature flue gas outlet of pyrolysis oven (3) links to each other.
9. The system for the pyrolysis coupling gasification treatment of the oily sludge according to claim 8, wherein the drier (2) is a single-shaft drier or a double-shaft drier; the pyrolysis furnace (3) is a single-shaft pyrolysis furnace or a double-shaft pyrolysis furnace; the fluidized bed gasification furnace (4) is a bubbling fluidized bed gasification furnace or a circulating fluidized bed gasification furnace.
10. The system for the pyrolysis and coupling gasification treatment of the oily sludge according to claim 8, wherein the flue gas purification device (9) comprises one or a combination of a desulfurization device, a denitrification device and a bag-type dust remover.
CN202211051643.XA 2022-08-30 2022-08-30 Method and system for pyrolysis coupling gasification treatment of oily sludge Pending CN115368919A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116970411A (en) * 2023-09-12 2023-10-31 亚德（上海）环保系统有限公司 Sludge treatment device and working method thereof

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116970411A (en) * 2023-09-12 2023-10-31 亚德（上海）环保系统有限公司 Sludge treatment device and working method thereof

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