CN111410982A - Oil residue fractional separation full-recycling system - Google Patents
Oil residue fractional separation full-recycling system Download PDFInfo
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- 238000000926 separation method Methods 0.000 title claims abstract description 69
- 238000004064 recycling Methods 0.000 title claims abstract description 22
- 239000007787 solid Substances 0.000 claims abstract description 40
- 238000002156 mixing Methods 0.000 claims abstract description 38
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 239000007791 liquid phase Substances 0.000 claims abstract description 22
- 238000005191 phase separation Methods 0.000 claims abstract description 16
- 239000002893 slag Substances 0.000 claims abstract description 15
- 238000011084 recovery Methods 0.000 claims description 27
- 238000001035 drying Methods 0.000 claims description 23
- 239000003795 chemical substances by application Substances 0.000 claims description 17
- 239000007790 solid phase Substances 0.000 claims description 11
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 9
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 6
- 238000005194 fractionation Methods 0.000 claims description 5
- 239000003502 gasoline Substances 0.000 claims description 4
- 239000012046 mixed solvent Substances 0.000 claims description 4
- 239000010865 sewage Substances 0.000 claims description 3
- 239000002283 diesel fuel Substances 0.000 claims description 2
- 239000000284 extract Substances 0.000 claims description 2
- 239000003350 kerosene Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 13
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract description 4
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 3
- 239000000446 fuel Substances 0.000 abstract description 3
- 229930195733 hydrocarbon Natural products 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 47
- 239000011269 tar Substances 0.000 description 30
- 238000000034 method Methods 0.000 description 17
- 238000000605 extraction Methods 0.000 description 16
- 238000003756 stirring Methods 0.000 description 15
- 239000002904 solvent Substances 0.000 description 8
- 239000011273 tar residue Substances 0.000 description 7
- 239000003245 coal Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 239000002699 waste material Substances 0.000 description 5
- 239000002131 composite material Substances 0.000 description 4
- 239000011259 mixed solution Substances 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 238000004821 distillation Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000007792 addition Methods 0.000 description 1
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- 239000010779 crude oil Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
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- 238000002309 gasification Methods 0.000 description 1
- -1 hydrocarbon organic compounds Chemical class 0.000 description 1
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- 238000000465 moulding Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
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- 238000000197 pyrolysis Methods 0.000 description 1
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- 238000000638 solvent extraction Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- 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
- 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
- C10G1/04—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by extraction
- C10G1/045—Separation of insoluble materials
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L5/00—Solid fuels
- C10L5/40—Solid fuels essentially based on materials of non-mineral origin
- C10L5/48—Solid fuels essentially based on materials of non-mineral origin on industrial residues and waste materials
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1003—Waste materials
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
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- Chemical Kinetics & Catalysis (AREA)
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- Extraction Or Liquid Replacement (AREA)
Abstract
The invention provides a full recycling system for oil residue fractional separation, which comprises a primary separation unit and a secondary separation unit; the first-stage separation unit comprises a first mixing device, a first solid-liquid separation device and a first liquid-phase separation device; the second-stage separation unit comprises a second mixing device, a second solid-liquid separation device and a second liquid-phase separation device. The solid slag obtained finally by the system has low content of volatile hydrocarbon and extremely low water content, can be used as an environment-friendly solid raw material or fuel without further processing, and is safe and environment-friendly in storage.
Description
Technical Field
The invention belongs to the field of oil residue treatment, relates to an oil residue recovery system, and particularly relates to an oil residue grading separation full-resource recovery system.
Background
The oil residue comprises tar residue obtained in the coal pyrolysis and gasification processes of coal chemical enterprises or liquefied residue obtained in the direct coal liquefaction process, and also comprises various waste oil, scum, tank bottom oil residue, oil sludge, sediment, activated sludge and other waste mineral oil residues generated in the crude oil refining process of petrochemical enterprises. Most of the oil residues belong to dangerous wastes in a dangerous waste list, and how to reasonably treat the solid wastes is a problem faced by the enterprises.
At present, most enterprises stack the oil residues randomly and cannot effectively treat and utilize the oil residues. Because a large amount of organic hydrocarbon compounds are doped in the formation process of the oil residues, the part of the organic hydrocarbon compounds can pollute underground water and soil due to permeation in the stacking process, the volatilization of the organic hydrocarbon compounds can also seriously pollute the atmospheric environment, and solid particles in the oil residues can scatter around along with long-term exposure and must be reasonably treated. Meanwhile, the hydrocarbon organic compounds in the oil residues can be used as chemical raw materials for high value-added utilization, and the granular solids can be recycled due to the high calorific value of the granular solids.
CN107557044B provides a tar residue recycling treatment process, which takes demulsification dehydration, solvent extraction and centrifugal separation as the core, adopts distillate oil of coal tar at 200-: coal tar 200-230 ℃ distillate oil 90-95 wt%, crude benzene 4.1-9.7 wt%, industrial naphthalene 0.3-0.9 wt%, under the conditions of demulsification dehydration temperature 35-55 ℃, extraction temperature 55-60 ℃, pressure 101.325kPa, pump circulation flow 15-20m3/h, extraction time 3-4h, centrifuge rotation speed 2500-3000r/min and the like, a process combining thermal extraction and centrifugation is adopted. Although the process can recover tar in tar residues, the process still has two problems, namely, the regeneration and recycling of the composite extracting agent are not considered, and a large amount (30-70% by mass) of the composite extracting agent and tar are adsorbed and adhered to the solid separated by the centrifugal machine, so that the boiling point of the composite extracting agent is high, the oil phase in the solid is difficult to recover by drying, and the dried solid still causes certain pollution to the environment.
CN110477938A discloses a method and a system for grading treatment of tar residues, which comprises the following steps: adding the tar residue into a composite solvent, stirring and dissolving to obtain a solid-liquid mixture; carrying out centrifugal separation on the solid-liquid mixture to obtain a first agent-oil mixed solution rich in tar and first solid residues; drying the first solid slag to recover the solvent and tar adsorbed and adhered in the first solid slag, and condensing and collecting gas escaped in the drying process to obtain a second agent-oil mixed solution; distilling the first agent-oil mixed solution and the second agent-oil mixed solution to obtain crude tar, a solvent and water; fractionating the crude tar to obtain light oil, heavy oil and bitumen; and (4) pressurizing and molding the second solid slag obtained after drying to obtain the molded coal. Although the regeneration of the solvent is considered in the process, the resource utilization of the solid slag is also considered, the first solid slag is dried (150-260 ℃), but because the selected main solvent is a component with a high boiling point, such as coal-based washing oil distillate oil, the recovery rate of the solvent and tar adsorbed and adhered to the solid slag is low at the drying temperature, and then the dried second solid slag is pressed and formed into the molded coal, so that not only can good benefits be obtained, but also the waste of resources is realized.
Disclosure of Invention
Aiming at the technical problems in the prior art, the invention provides an oil residue grading separation full-resource recovery system, which solves the problems of environmental protection and resource utilization of oil residue storage and further recovers a solvent adsorbed and adhered in solids separated by a centrifugal machine.
In order to achieve the purpose, the invention adopts the following technical scheme:
the invention provides a full recycling system for oil residue fractional separation, which comprises a primary separation unit and a secondary separation unit;
the first-stage separation unit comprises a first mixing device, a first solid-liquid separation device and a first liquid-phase separation device;
the second-stage separation unit comprises a second mixing device, a second solid-liquid separation device and a second liquid-phase separation device;
a feed inlet of the first mixing device is connected with the oil residue conveying pipeline, a discharge outlet of the first mixing device is connected with an inlet of the first solid-liquid separation device, and a liquid phase outlet of the first solid-liquid separation device is connected with an inlet of the first liquid-phase separation device;
the solid phase outlet of the first solid-liquid separation device is connected with the feed inlet of the second mixing device, the discharge outlet of the second mixing device is connected with the inlet of the second solid-liquid separation device, the liquid phase outlet of the second solid-liquid separation device is connected with the outlet of the second solid-liquid separation device, and the solid phase outlet of the second solid-liquid separation device is connected with a solid slag discharge pipeline.
As a preferable technical solution of the present invention, the first mixing device mixes and extracts the oil residue and the first extracting agent.
As a preferable technical scheme of the invention, the first extracting agent comprises a mixed solvent consisting of one or more of distillate oil with the temperature of 170-230 ℃, kerosene and light diesel oil in tar.
In a preferred embodiment of the present invention, the mass ratio of the first extractant to the oil residue is 0.5 to 3:1, for example, 0.8:1, 1:1, 1.5:1, 2:1, 2.5:1 or 2.8:1, but the present invention is not limited to the above-mentioned values, and other values not listed in the above-mentioned value range are also applicable.
Preferably, the mixing temperature of the first mixing device is 50 to 120 ℃, such as 55 ℃, 60 ℃, 65 ℃, 70 ℃, 75 ℃, 80 ℃, 85 ℃, 90 ℃, 95 ℃, 100 ℃, 105 ℃, 110 ℃ or 115 ℃, but not limited to the recited values, and other values not recited in the range of values are also applicable.
Preferably, the mixing time of the first mixing device is 0.5-3 h, such as 0.8h, 1h, 1.5h, 2h, 2.5h or 2.8h, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
As a preferable technical scheme of the invention, the first liquid phase separation device is provided with a sewage outlet, a crude tar outlet and a first extracting agent outlet, and the first extracting agent outlet and the oil residue conveying pipeline are mixed and extracted.
In a preferred embodiment of the present invention, the second mixing device connects the solid phase obtained by the first solid-liquid separation device and the second extractant.
As a preferred technical scheme of the invention, the second extracting agent comprises a mixed solvent consisting of one or more of industrial crude benzene, toluene and hydrogenated light gasoline.
Preferably, the boiling point range of the hydrogenated light gasoline is 65-130 ℃.
In the present invention, the boiling point of the second extractant is lower than the boiling point of the first extractant.
In a preferred embodiment of the present invention, the mass ratio of the second extractant to the solid phase obtained by the first solid-liquid separation device is 1 to 4:1, for example, 1.5:1, 2:1, 2.5:1, 3:1 or 3.5:1, but the present invention is not limited to the above-mentioned values, and other values not shown in the above-mentioned value range are also applicable.
Preferably, the mixing temperature of the first mixing device is 40 to 80 ℃, such as 45 ℃, 50 ℃, 55 ℃, 60 ℃, 65 ℃, 70 ℃ or 75 ℃, but not limited to the recited values, and other values not recited in the range of values are also applicable.
Preferably, the mixing time of the first mixing device is 0.5-3 h, such as 0.8h, 1h, 1.5h, 2h, 2.5h or 2.8h, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
As a preferable technical solution of the present invention, the second liquid phase separation device is provided with a crude tar outlet and a second extractant outlet, the second extractant outlet is connected to the inlet of the second mixing device, and the crude tar outlet is connected to the inlet of the first liquid phase separation device.
As a preferable technical scheme of the invention, a drying device is arranged on the solid slag discharge pipeline.
Preferably, the drying device is provided with a condensate outlet and a solid slag outlet, and the condensate outlet is connected with the inlet of the second liquid phase separation device.
Preferably, the drying temperature of the drying device is 100 to 250 ℃, such as 120 ℃, 150 ℃, 180 ℃, 200 ℃, 220 ℃ or 240 ℃, but not limited to the recited values, and other values not recited in the range of the values are also applicable.
Preferably, the drying pressure of the drying device is 10 to 80kPaA, such as 20kPaA, 30kPaA, 40kPaA, 50kPaA, 60kPaA or 70kPaA, but not limited to the recited values, and other values not recited in the range of values are also applicable.
Compared with the prior art, the invention at least has the following beneficial effects:
(1) the invention provides a full-recycling system for oil residue fractional separation, which solves the environmental protection problem and resource utilization problem of oil residue storage and further recycles a solvent adsorbed and adhered in solids separated by a centrifugal machine;
(2) the invention provides an oil residue fractional separation full-recycling system, which is characterized in that the volatile hydrocarbon content of solid residues finally obtained by the system is low, the water content is extremely low, the solid residues can be used as environment-friendly solid raw materials or fuels without further processing, and the storage is safe and environment-friendly.
Drawings
FIG. 1 is a schematic structural diagram of a fractional oil-residue separation full-recycling system provided in example 1 of the present invention;
in the figure: 1-a first extraction stirring tank, 2-a first centrifuge, 3-a first extractant recovery tower, 4-a second extraction stirring tank, 5-a second centrifuge, 6-a second extractant recovery tower and 7-a drying device.
The present invention is described in further detail below. The following examples are merely illustrative of the present invention and do not represent or limit the scope of the claims, which are defined by the claims.
Detailed Description
The technical scheme of the invention is further explained by the specific implementation mode in combination with the attached drawings.
To better illustrate the invention and to facilitate the understanding of the technical solutions thereof, typical but non-limiting examples of the invention are as follows:
example 1
The present embodiment provides a system for oil residue fractionation and recycling of full resources, which has a structure as shown in fig. 1, and the system includes a primary separation unit and a secondary separation unit;
the primary separation unit comprises a first extraction stirring tank, a first centrifuge and a first extractant recovery tower;
the second-stage separation unit comprises a second extraction stirring tank, a second centrifugal machine and a second extractant recovery tower;
a feed inlet of the first extraction stirring tank is connected with the oil residue conveying pipeline, a discharge outlet of the first extraction stirring tank is connected with an inlet of the first centrifuge, and a liquid phase outlet of the first centrifuge is connected with an inlet of the first extractant recovery tower;
the solid phase outlet of the first centrifuge is connected with the feed inlet of the second extraction stirring tank, the discharge outlet of the second extraction stirring tank is connected with the inlet of the second centrifuge, the liquid phase outlet of the second centrifuge is connected with the outlet of the second extractant recovery tower, and the solid phase outlet of the second extractant recovery tower is connected with a solid residue discharge pipeline;
the first extractant recovery tower is provided with a sewage outlet, a crude tar outlet and a first extractant outlet, and the first extractant outlet is connected with the oil residue conveying pipeline;
the second extraction stirring tank is used for mixing and extracting the solid phase obtained by the first centrifuge and the second extractant;
the second extractant recovery tower is provided with a crude tar outlet and a second extractant outlet, the second extractant outlet is connected with the inlet of the second extraction stirring tank, and the crude tar outlet is connected with the inlet of the first extractant recovery tower;
and a drying device is arranged on the solid slag discharge pipeline, the drying device is provided with a condensate outlet and a solid slag outlet, and the condensate outlet is connected with an inlet of the second extractant recovery tower.
Example 2
This example provides a method for performing fractional oil-residue separation and total recycling by using the fractional oil-residue separation and total recycling system provided in example 1, the method comprising:
firstly, adding the oil residue and a first extracting agent into a first extraction stirring tank, stirring and dissolving to obtain a solid-liquid mixture, allowing the solid-liquid mixture to enter a first centrifuge for centrifugal separation to obtain a centrifugal liquid rich in tar, and conveying the obtained centrifugal liquid rich in the tar to a first extracting agent recovery tower for distillation to obtain crude tar, the first extracting agent and water. And adding a first-stage centrifugal dry phase obtained by centrifugal separation of the first centrifugal machine and a second extracting agent into a second extraction stirring tank, stirring and dissolving to obtain a solid-liquid mixture, adding the solid-liquid mixture into the second centrifugal machine for second-stage centrifugal separation, sending the obtained centrifugate to a second extracting agent recovery tower for distillation to obtain crude tar and second extraction, wherein the crude tar contains a small amount of the first extracting agent, and sending the crude tar to the first extracting agent recovery tower for further distillation and recovery of the first extracting agent. And (3) adsorbing and adhering a second extractant and a small amount of first extractant and tar in the secondary centrifugal dry phase, conveying the second extractant and the tar to a drying device, condensing the gas escaping in the drying process, collecting the gas, conveying the gas to a second extractant recovery tower to further recover the second extractant, and applying the solid residue formed after drying as an environment-friendly solid raw material or fuel.
Example 3
A certain gasified tar residue (55.38% in solid content, 12.7% in water content, and 31.92% in tar content) was recovered by using the system for fractional separation and total recycling of oil residue provided in example 1 and the method for fractional separation and total recycling of oil residue provided in example 2, and the main parameters are shown in table 1.
TABLE 1
The residual amounts of tar and extractant in the solid residue treated in this example were 12.8%, and the water content was 0.25%.
Example 4
A certain coker tar residue (38.32% solids, 8.70% water, 52.98% tar) was recovered using the system and method for fractional separation and total recycling of oil residue provided in example 1, and the main parameters are shown in Table 2.
TABLE 2
The residual amounts of tar and extractant in the solid residue treated in this example were 8.2%, and the water content was 0.30%.
Example 5
The system for fractional separation and total recycling of oil residue provided in example 1 and the method for fractional separation and total recycling of oil residue provided in example 2 were used to recycle a coal-liquefied oil residue (solid content 48.32%, water content 0.20%, tar content 51.48%), and the main parameters are shown in table 3.
TABLE 3
The residual amounts of tar and extractant in the solid residue treated in this example were 10.4%, and the water content was 0.27%
Example 6
A semi-coke tar residue (40.12% in solid content, 4.0% in water content, and 55.88% in tar content) was recovered by using the system for fractional separation and total recycling of oil residue provided in example 1 and the method for fractional separation and total recycling of oil residue provided in example 2, and the main parameters are shown in table 4.
TABLE 4
The residual amounts of tar and extractant in the solid residue treated in this example were 9.3%, and the water content was 0.29%.
The applicant declares that the present invention illustrates the detailed structural features of the present invention through the above embodiments, but the present invention is not limited to the above detailed structural features, that is, it does not mean that the present invention must be implemented depending on the above detailed structural features. It should be understood by those skilled in the art that any modifications of the present invention, equivalent substitutions of selected components of the present invention, additions of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.
The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
Claims (10)
1. The oil residue grading separation full resource recovery system is characterized by comprising a primary separation unit and a secondary separation unit;
the first-stage separation unit comprises a first mixing device, a first solid-liquid separation device and a first liquid-phase separation device;
the second-stage separation unit comprises a second mixing device, a second solid-liquid separation device and a second liquid-phase separation device;
a feed inlet of the first mixing device is connected with the oil residue conveying pipeline, a discharge outlet of the first mixing device is connected with an inlet of the first solid-liquid separation device, and a liquid phase outlet of the first solid-liquid separation device is connected with an inlet of the first liquid-phase separation device;
the solid phase outlet of the first solid-liquid separation device is connected with the feed inlet of the second mixing device, the discharge outlet of the second mixing device is connected with the inlet of the second solid-liquid separation device, the liquid phase outlet of the second solid-liquid separation device is connected with the outlet of the second solid-liquid separation device, and the solid phase outlet of the second solid-liquid separation device is connected with a solid slag discharge pipeline.
2. The oil residue fractionation and total recycling system according to claim 1, wherein the first mixing device is used for mixing and extracting the oil residue with the first extracting agent.
3. The oil residue fractional separation full resource recovery system of claim 2, wherein the first extractant is a mixed solvent composed of one or more of distillate oil at 170-230 ℃, kerosene and light diesel oil in tar.
4. The oil residue fractional separation full resource recovery system of claim 1, wherein the mass ratio of the first extractant to the oil residue is 0.5-3: 1;
preferably, the mixing temperature of the first mixing device is 50-120 ℃;
preferably, the mixing time of the first mixing device is 0.5-3 h.
5. The oil residue stage separation full recycling system according to claim 1, wherein said first liquid phase separation device is provided with a sewage outlet, a crude tar outlet and a first extractant outlet, said first extractant outlet is connected with said oil residue delivery pipeline.
6. The oil residue fractionation and total recycling system according to claim 1, wherein the second mixing device mixes and extracts the solid phase obtained by the first solid-liquid separation device and the second extractant.
7. The oil residue fractionation full resource recovery system according to claim 6, wherein the second extractant is a mixed solvent composed of one or more of industrial crude benzene, toluene and hydrogenated light gasoline;
preferably, the boiling point range of the hydrogenated light gasoline is 65-130 ℃.
8. The oil residue fractional separation full resource recovery system of claim 1, wherein the mass ratio of the second extractant to the solid phase obtained by the first solid-liquid separation device is 1-4: 1;
preferably, the mixing temperature of the first mixing device is 40-80 ℃;
preferably, the mixing time of the first mixing device is 0.5-3 h.
9. The oil residue fractionation full resource recovery system according to claim 1, wherein the second liquid phase separation device is provided with a crude tar outlet and a second extractant outlet, the second extractant outlet is connected to the inlet of the second mixing device, and the crude tar outlet is connected to the inlet of the first liquid phase separation device.
10. The oil residue fractional separation full resource recovery system of claim 1, wherein a drying device is arranged on the solid residue discharge pipeline;
preferably, the drying device is provided with a condensate outlet and a solid slag outlet, and the condensate outlet is connected with the inlet of the second liquid phase separation device;
preferably, the drying temperature of the drying device is 100-250 ℃;
preferably, the drying pressure of the drying device is 10-80 kPaA.
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962560A (en) * | 2010-09-29 | 2011-02-02 | 神华集团有限责任公司 | Extraction method of direct coal liquefaction residues and application of extracts |
| CN103275754A (en) * | 2013-05-30 | 2013-09-04 | 神华集团有限责任公司 | Method for separating liquefied heavy oil and asphalt substrate from direct coal liquefaction residues |
| CN104845652A (en) * | 2015-06-10 | 2015-08-19 | 神华集团有限责任公司 | Treatment method for direct coal liquefaction residues |
| CN107557044A (en) * | 2017-10-24 | 2018-01-09 | 西北大学 | A kind of tar slag recycling treatment process |
| CN108251153A (en) * | 2017-12-26 | 2018-07-06 | 中国石油天然气集团公司 | A kind of dehydrating aging process for purification and its system |
| CN110295053A (en) * | 2019-08-12 | 2019-10-01 | 胜帮科技股份有限公司 | A kind of recycling processing method of coal chemical industry oil-containing solid slag |
-
2020
- 2020-04-13 CN CN202010284587.9A patent/CN111410982A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101962560A (en) * | 2010-09-29 | 2011-02-02 | 神华集团有限责任公司 | Extraction method of direct coal liquefaction residues and application of extracts |
| CN103275754A (en) * | 2013-05-30 | 2013-09-04 | 神华集团有限责任公司 | Method for separating liquefied heavy oil and asphalt substrate from direct coal liquefaction residues |
| CN104845652A (en) * | 2015-06-10 | 2015-08-19 | 神华集团有限责任公司 | Treatment method for direct coal liquefaction residues |
| CN107557044A (en) * | 2017-10-24 | 2018-01-09 | 西北大学 | A kind of tar slag recycling treatment process |
| CN108251153A (en) * | 2017-12-26 | 2018-07-06 | 中国石油天然气集团公司 | A kind of dehydrating aging process for purification and its system |
| CN110295053A (en) * | 2019-08-12 | 2019-10-01 | 胜帮科技股份有限公司 | A kind of recycling processing method of coal chemical industry oil-containing solid slag |
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