CN114907876A - Method and apparatus for solvent recovery - Google Patents
Method and apparatus for solvent recovery Download PDFInfo
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- CN114907876A CN114907876A CN202110181661.9A CN202110181661A CN114907876A CN 114907876 A CN114907876 A CN 114907876A CN 202110181661 A CN202110181661 A CN 202110181661A CN 114907876 A CN114907876 A CN 114907876A
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/30—Controlling or regulating
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
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- Extraction Or Liquid Replacement (AREA)
Abstract
The invention relates to the technical field of petrochemical industry, in particular to a method and a device for recovering a solvent, wherein the method comprises the following steps: (1) heating the mixed solution containing the extraction oil and the solvent to obtain a heated mixed solution; (2) carrying out phase separation on the heated mixed solution to obtain a recovered solvent and an extract oil-containing material flow; (3) heating and separating the extract oil-containing material flow to obtain an extract oil-rich material flow; wherein step (2) and step (3) are each independently performed in a supercritical state. The method makes the temperature of the extracted oil-containing material flow higher than that of the heated mixed liquid by heating and separating the extracted oil-containing material flow, reduces the solvent content in the extracted oil-rich material flow, and simultaneously reduces the feeding temperature of the mixed liquid, thereby effectively reducing the energy consumption and investment, and simultaneously reducing the temperature and the heat exchange capacity of the recovered solvent.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a method and a device for recovering a solvent.
Background
Under the conditions of increasing shortage of crude oil, increasing deterioration of imported crude oil and increasing oil product demand in China, the role of the solvent deasphalting technology in processing heavy and poor oil is highlighted. The development and the perfection of the solvent deasphalting technology have positive effects on the aspects of reasonably and fully utilizing petroleum resources and bringing economic benefits and social benefits to enterprises.
The solvent recovery part of the solvent deasphalting occupies most of the equipment investment and energy consumption of the whole device. Solvent recovery can generally be achieved by evaporation and supercritical solvent recovery. Unlike evaporation methods, which provide a large amount of latent heat for recovering the phase change of the solvent, supercritical solvent recovery is that under supercritical conditions, the solvent is changed from a liquid state to a supercritical fluid state, and the solubility of the deasphalted oil in the solvent is gradually reduced and separated from the solvent. In the whole process, 85-90% of the solvent is not subjected to phase change, so that most of energy consumption is saved, and the energy consumption is greatly reduced compared with that of an evaporation method.
The solvent deasphalting device newly built at present adopts the supercritical technology to recover the solvent, and the supercritical solvent recovery tower adopts isothermal operation in most cases. The solvent recovered in the supercritical state has a low density (100-200 kg/m) 3 ) And a large amount of heat exchange area is needed for heat exchange and heat energy recovery. Compared with the distillation technology commonly used in industry, the solvent deasphalting technology still has the problems of high energy consumption, large investment and the like.
CN107177373A discloses a supercritical residual oil and/or catalytic slurry oil treatment system, which extracts residual oil and/or catalytic slurry oil under subcritical condition, and then recovers solvent under supercritical condition; CN105400545A discloses a heavy oil separation method and a processing system thereof, wherein an extraction tower with a plurality of packing sections in the upper region is adopted, a distributor is arranged between adjacent packing sections, and a supercritical solvent from a supercritical solvent recovery tower is introduced through the distributor, so as to further separate heavy components in the deasphalted oil phase at the upper part of the extraction tower; CN102690678A discloses a processing method of inferior heavy crude oil, which uses the atmospheric residue of the inferior heavy crude oil as the raw material of a solvent extraction device, and separates the crude oil by a solvent extraction process under a supercritical state.
The supercritical solvent recovery process employed in the above process is operated isothermally, and to reduce the solvent content of the bottoms stream, the supercritical solvent recovery column employs a relatively high feed temperature, resulting in relatively high energy consumption, such as 949.1MJ/t for a typical ROSE process integration.
Disclosure of Invention
The invention aims to solve the problems of high feeding temperature of mixed liquid, high temperature of recovered solvent, high energy consumption, high investment and the like caused by isothermal operation of a solvent recovery tower in the supercritical solvent recovery method in the prior art, and provides a method and a device for recovering a solvent.
In order to achieve the above object, a first aspect of the present invention provides a method for recovering a solvent, the method comprising the steps of:
(1) heating the mixed liquid containing the extraction oil and the solvent to obtain the heated mixed liquid;
(2) carrying out phase separation on the heated mixed solution to obtain a recovered solvent and an extract oil-containing material flow;
(3) heating and separating the extract oil-containing material flow to obtain an extract oil-rich material flow;
wherein step (2) and step (3) are each independently performed in a supercritical state.
In a second aspect, the present invention provides an apparatus for solvent recovery, the apparatus comprising: the device comprises a heater and a solvent recovery tower, wherein a filler section, a distributor and a heat exchange component are sequentially arranged in the solvent recovery tower from top to bottom;
the heater is arranged in the middle of the solvent recovery tower, is communicated with the distributor and is used for heating mixed liquid containing extraction oil and a solvent, and the obtained heated mixed liquid is uniformly distributed in the solvent recovery tower through the distributor and flows upwards to enter the filler section;
the filler section is used for carrying out phase separation on the heated mixed solution in a supercritical state to obtain a recovered solvent and an extract oil-containing material flow, wherein the extract oil-containing material flow flows downwards to enter the heat exchange part;
the heat exchange part is used for heating and separating the extract oil-containing material flow in a supercritical state to obtain an extract oil-rich material flow.
Compared with the prior art, the invention has the following advantages:
(1) according to the method provided by the invention, the temperature of the extract oil-containing material flow is higher than that of the heated mixed liquid in a manner of heating and separating the extract oil-containing material flow, so that the feeding temperature of the mixed liquid is reduced while the content of the solvent in the extract oil-rich material flow is reduced, the energy consumption and the investment are effectively reduced, and the temperature and the heat exchange amount of the recovered solvent are also reduced;
(2) according to the device provided by the invention, the filling section, the heat exchange part and the distributor are arranged in the solvent recovery tower, and particularly, the heat exchange part is arranged at the lower part of the solvent recovery tower, namely, the temperature of the tower bottom material flow can be controlled in a local heat exchange mode, so that the lower part temperature of the solvent recovery tower is higher than the upper part temperature, the energy consumption waste caused by the traditional isothermal operation is avoided, and the equipment investment and the device floor area are effectively reduced.
Drawings
FIG. 1 is a schematic diagram of a solvent recovery apparatus according to the present invention;
FIG. 2 is a schematic structural diagram of a heat exchange component provided by the present invention;
FIG. 3 is a top view of a heat exchange member provided by the present invention;
FIG. 4 is a schematic structural view of another heat exchange member provided by the present invention;
fig. 5 is a top view of another heat exchange member provided by the present invention.
Description of the reference numerals
1. Mixed liquid 2, heat exchanger 3, heater 4 and solvent recovery tower
5. A packing section 6, a heat exchange part 7, an extract oil-rich material flow 8 and a heat exchange medium inlet
9. Heat exchange medium outlet 10, recovered solvent 11, heat exchange branch pipe 12 and heat exchange main pipe
13. U-shaped heat exchange tube 14, vertical connecting tube 15 and distributor
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For numerical ranges, each range between its endpoints and individual point values, and each individual point value can be combined with each other to give one or more new numerical ranges, and such numerical ranges should be construed as specifically disclosed herein.
In the present invention, the "top" of the container means 0 to 10% of the container from the top to the bottom, unless otherwise specified; the upper part of the container means 10 to 30 percent of the container from top to bottom; the lower part of the container is 60-90% of the container from top to bottom; the "bottom" of the container means 90-100% of the container from top to bottom.
In a first aspect the present invention provides a method of solvent recovery comprising the steps of:
(1) heating the mixed solution containing the extraction oil and the solvent to obtain a heated mixed solution;
(2) carrying out phase separation on the heated mixed solution to obtain a recovered solvent and an extracted oil-containing material flow;
(3) heating and separating the extract oil-containing material flow to obtain an extract oil-rich material flow;
wherein step (2) and step (3) are each independently performed in a supercritical state.
The inventor of the invention researches and finds that: in a supercritical state, the temperature of the material flow containing the extraction oil can be controlled by separating the mixed liquid containing the extraction oil and the solvent and heating and separating the obtained material flow containing the extraction oil, particularly by adjusting the temperature of a heat exchange medium, so that the residual solvent in the material flow containing the extraction oil is separated, the feeding temperature and the energy consumption of the mixed liquid are reduced, the content range of the solvent in the material flow rich in the extraction oil is reduced, and the heat load of the recovered solvent is reduced.
In the present invention, the mixed liquid containing the extracted oil and the solvent is an extract phase of the heavy oil, and the solvent is an extraction solvent of the heavy oil.
In the present invention, the temperature of the heated mixed liquid corresponds to the feed temperature of the mixed liquid, unless otherwise specified.
According to the present invention, it is preferable that the temperature of the heated mixed solution is higher than the critical temperature of the solvent.
In some embodiments of the present invention, the temperature of the heated mixed solution is preferably 5 to 50 ℃ higher than the critical temperature of the solvent, preferably 10 to 35 ℃. And adopting the optimal conditions to ensure the phase separation efficiency of the mixed liquid while reducing the solubility of the solvent.
According to the present invention, preferably, in the mixed solution, the weight ratio of the extraction oil to the solvent is 1: 1-15, preferably 1: 1-10. Adopt preferred condition, be favorable to improving the feeding distribution effect of mixed liquid, reduce and distribute and block up the risk to improve the separation effect of mixed liquid.
In the present invention, there is a wide range of options for the manner of heating in step (1). As long as the temperature range of the heated mixed solution is 5 to 50 ℃ higher than the critical temperature of the solvent.
In the present invention, the heat load of the recovered solvent is effectively utilized in order to reduce energy consumption. Preferably, the recovered solvent in step (2) is heat exchanged with the mixed solution before the heating.
In some embodiments of the present invention, preferably, the weight ratio of the recovery solvent to the mixed solution is 1: 1.2-2, preferably 1: 1.3-1.5.
According to the invention, the temperature of the recovered solvent after heat exchange is preferably 1-20 ℃ higher than the temperature of the mixed solution, preferably 5-15 ℃.
According to the present invention, preferably, the extraction oil is a deasphalted oil.
In some embodiments of the present invention, it is preferred that the asphaltene content is less than or equal to 1 wt% and the metal content is less than or equal to 50 μ g/g, based on the total weight of the deasphalted oil.
According to the present invention, preferably, the extracted oil is extracted from at least one heavy oil selected from the group consisting of residual oil, vacuum residual oil, heavy oil of poor quality and oil sand.
In the present invention, there is a wide selection range of the solvent as long as the solvent and the extraction oil are phase-separated in a supercritical state. Preferably, the solvent is at least one of C4-C6 alkanes, for example, selected from n-butane, isobutane, n-pentane, isopentane, neopentane, cyclopentane, n-hexane, isohexane, and the like; preferably at least one selected from the group consisting of mixed hydrocarbons of C4 alkanes, mixed hydrocarbons of C4-C5 alkanes, mixed hydrocarbons of C5 alkanes, mixed hydrocarbons of C5-C6 alkanes and mixed hydrocarbons of C6 alkanes.
In the present invention, the supercritical state depends on the kind of the solvent, for example, when the solvent is propane, the supercritical state includes: the temperature is more than or equal to 96.75 ℃, and the pressure is more than or equal to 4.26 MPa; when the solvent is n-butane, the supercritical state comprises: the temperature is more than or equal to 152.0 ℃, and the pressure is more than or equal to 3.8 MPa; when the solvent is n-pentane, the supercritical state comprises: the temperature is more than or equal to 196.5 ℃, and the pressure is more than or equal to 3.38 MPa. In the present invention, the pressure refers to gauge pressure unless otherwise specified.
The invention utilizes the fact that the density of the solvent in the mixed liquid is obviously reduced under the supercritical state, and the value is close to the density of gas phase, thereby obtaining good separation effect by utilizing the density difference of the solvent and the extracted oil in the mixed liquid, namely, at the final set temperature, the extracted oil is practically insoluble in the solvent, thereby generating phase separation.
In the present invention, the phase separation is to separate the extraction oil and the solvent in the mixed solution in a supercritical state due to a density difference caused by the decrease of the solubility of the solvent and the precipitation of the extraction oil. Preferably, the conditions for phase separation include: the temperature is 5-50 ℃ higher than the critical temperature of the solvent, and preferably 10-35 ℃; the pressure is 0.5-2MPa, preferably 0.5-1MPa, above the critical pressure of the solvent. Preferred conditions are used to further facilitate the separation efficiency of the recovered solvent and to reduce the solvent content of the extract oil-containing stream.
In the invention, in order to further ensure that the solvent content in the extract oil-containing material flow reaches the standard, the solvent content in the extract oil-rich material flow is reduced by heating and separating the extract oil-containing material flow in a supercritical state.
According to the present invention, preferably, the conditions for the thermal separation include: the temperature is 10-30 ℃ higher than the temperature of the phase separation, preferably 15-25 ℃; the pressure is 0.5-2MPa, preferably 0.5-1MPa, above the critical pressure of the solvent. Preferably, conditions are used to further facilitate the reduction of solvent content in the extract oil-rich stream.
In some embodiments of the present invention, it is preferred that the solvent be present in the extract oil-rich stream in an amount of 50 wt.% or less, preferably in the range of 25 to 35 wt.%.
According to the present invention, preferably, the heating separation process includes: and exchanging heat between the extract oil-containing material flow and a heat exchange medium, and separating the extract oil-containing material flow after heat exchange.
According to the present invention, preferably, the inlet temperature of the heat exchange medium is 250-350 ℃, preferably 280-320 ℃; the outlet temperature of the heat exchange medium is 200-330 ℃, and preferably 270-310 ℃. The heating temperature of the extract oil-containing stream is strictly controlled by controlling the flow rate of the heat exchange medium, thereby controlling the solvent content in the extract oil-rich stream.
According to the present invention, preferably, the heat exchange medium is selected from steam and/or thermal oil. Wherein the heat transfer oil is selected from alkyl biphenyl type heat transfer oil, preferably heat transfer oil synthesized by isopropyl group spacer, antipode (isomer) and biphenyl.
According to a particularly preferred embodiment of the invention, the method comprises: (1) exchanging heat between the mixed solution containing the deasphalted oil and the solvent and the recovered solvent, and heating the obtained mixed solution after heat exchange to obtain a heated mixed solution; (2) carrying out phase separation on the heated mixed solution to obtain a recovered solvent and an extracted oil material flow; (3) heating and separating the extract oil-containing material flow and a heat exchange medium to obtain an extract oil-rich material flow; wherein step (2) and step (3) are each independently performed in a supercritical state.
In a second aspect, the present invention provides an apparatus for solvent recovery, the apparatus comprising: the device comprises a heater and a solvent recovery tower, wherein a filling section, a distributor and a heat exchange part are sequentially arranged in the solvent recovery tower from top to bottom;
the heater is arranged in the middle of the solvent recovery tower, is communicated with the distributor and is used for heating mixed liquid containing extraction oil and a solvent, and the obtained heated mixed liquid is uniformly distributed in the solvent recovery tower through the distributor and flows upwards to enter the filler section;
the filler section is used for carrying out phase separation on the heated mixed solution in a supercritical state to obtain a recovered solvent and an extract oil-containing material flow, wherein the extract oil-containing material flow flows downwards to enter the heat exchange part;
the heat exchange part is used for heating and separating the extract oil-containing material flow in a supercritical state to obtain an extract oil-rich material flow.
The device for recovering the solvent provided by the invention is characterized in that the heating part is arranged at the lower part of the solvent recovery tower, and the temperature of the bottom of the solvent recovery tower is controlled, so that the feeding temperature of the mixed solution and the temperature of the recovered solvent are reduced while the content of the solvent in the bottom material flow (namely the rich extracted oil material flow) is ensured to reach the standard.
According to a preferred apparatus of the present invention, the packing section is disposed at an upper portion of the solvent recovery column; the heat exchange component is arranged at the lower part of the solvent recovery tower; the distributor is arranged between the filling section and the heat exchange part.
The present invention provides a preferred solvent recovery apparatus, as shown in fig. 1, comprising: the device comprises a heater 3 and a solvent recovery tower 4, wherein a filling section 5, a distributor 15 and a heat exchange part 6 are sequentially arranged in the solvent recovery tower 4 from top to bottom; the heater 3 is arranged in the middle of the solvent recovery tower 4, is communicated with the distributor 15, and is used for heating the mixed liquid 1 containing the extraction oil and the solvent, and uniformly distributing the obtained heated mixed liquid in the solvent recovery tower 4 through the distributor 15, and enabling the heated mixed liquid to flow upwards to enter the filling section 5; the filler section 5 is configured to perform phase separation on the heated mixed solution in a supercritical state to obtain a recovered solvent 10 and an extract oil-containing material stream, wherein the extract oil-containing material stream flows downward and enters the heat exchange component 6; the heat exchange part 6 is used for heating and separating the extract oil-containing material flow in a supercritical state to obtain an extract oil-rich material flow 7.
According to the invention, preferably, the filler section is provided with a coalescing filler. The purpose of the coalescent filler is to enable small-droplet deasphalted oil carried in the solvent to be gathered into large droplets to flow downwards, and the quality of the solvent recovered at the top of the tower is ensured.
According to the invention, preferably, the specific surface area of the coalescing filler is greater than or equal to 80m 2 /m 3 Preferably 90 to 200m 2 /m 3 (ii) a The porosity is not less than 0.9, preferably 0.92-0.98. Promoting the heated mixture under preferred conditionsThe phase separation is carried out under the supercritical state, and the yield of the recovered solvent is improved.
According to the invention, preferably, the manner of the coalescing packing is selected from random packing and/or structured packing; the coalescing packing is preferably selected from non-open cell grid packing and/or plate corrugated packing.
According to the present invention, preferably, the heat exchange component comprises a heat exchange medium inlet, a heat exchange main pipe, a heat exchange branch pipe and a heat exchange medium outlet which are sequentially communicated, and the heat exchange medium inlet and the heat exchange medium outlet are respectively and independently arranged on the tower wall of the solvent recovery tower.
In the present invention, in order to improve the heat exchange efficiency between the extract oil-containing stream and the heat exchange medium, preferably, the heat exchange medium inlet is located below the heat exchange medium outlet. That is, the temperature of the extract oil-containing stream is raised by countercurrent contact between the extract oil-containing stream and a heat exchange medium, so that the residual solvent and the extract oil in the extract oil-containing stream are separated due to density difference, and an extract oil-rich stream is obtained.
According to the invention, preferably, the heat exchange branched pipes are at least one heat exchange pipe which is arranged in parallel in multiple rows or in series and arranged in multiple layers.
According to the present invention, preferably, the inner diameter of the heat exchange tube is 10 to 30mm, preferably 15 to 25 mm.
According to a preferred embodiment of the present invention, the heat exchange sub-tubes are at least one heat exchange tube arranged in parallel in multiple rows, and the heat exchange sub-tubes are arranged along the longitudinal direction.
As shown in fig. 2, the heat exchange component 6 includes a heat exchange medium inlet 8, a heat exchange main pipe 12, a heat exchange branch pipe 11, and a heat exchange medium outlet 9, which are sequentially communicated, and the heat exchange medium inlet 8 and the heat exchange medium outlet 9 are respectively and independently arranged on a tower wall of the solvent recovery tower 4, and the heat exchange medium inlet 8 is located below the heat exchange medium outlet 9; the heat exchange branched pipes 11 are at least one heat exchange pipe arranged in parallel in multiple rows, and the heat exchange branched pipes 11 are arranged longitudinally.
The top view of the heat exchange component provided by the invention is shown in fig. 3, wherein the heat exchange branched tubes 11 are at least one heat exchange tube arranged in parallel in multiple rows, and the heat exchange branched tubes 11 are arranged along the longitudinal direction.
In some embodiments of the present invention, preferably, when the heat exchange tubes are arranged in multiple parallel rows, the distance between two adjacent heat exchange tubes in each row is 5-40mm, preferably 10-30 mm; the distance between two adjacent rows of the heat exchange branched pipes is 30-100mm, and preferably 40-80 mm.
According to another preferred embodiment of the present invention, preferably, the heat exchange branched pipe is at least one heat exchange pipe arranged in a plurality of layers in series, and the heat exchange branched pipe is arranged in a transverse direction and in an inclined manner.
According to the invention, the inclination angle of the heat exchange branch pipe is preferably 10-60 degrees, and is preferably 20-45 degrees.
As shown in fig. 4, the heat exchange component 6 includes a heat exchange medium inlet 8, at least one U-shaped heat exchange tube 13, at least one vertical connection tube 14, and a heat exchange medium outlet 9, which are sequentially connected, and the heat exchange medium inlet 8 and the heat exchange medium outlet 9 are respectively and independently disposed on a tower wall of the solvent recovery tower 4, the heat exchange medium inlet 8 is located below the heat exchange medium outlet 9, and the U-shaped heat exchange tubes 13 are arranged in a transverse direction.
The top view of the heat exchange component provided by the invention is shown in fig. 5, wherein the heat exchange branched tubes 11 are at least one heat exchange tube arranged in series and in multiple layers, and the heat exchange branched tubes 11 are arranged in the transverse direction.
In some embodiments of the present invention, preferably, when the heat exchange branched pipes are arranged in a series of multiple layers, the distance between two adjacent heat exchange branched pipes in each layer is 10-80mm, preferably 20-60 mm; the height between two adjacent layers of the heat exchange branch pipes is 50-1000mm, and preferably 100-400 mm.
According to the present invention, preferably, the apparatus further comprises a heat exchanger.
Further preferably, an inlet of the heat exchanger is connected to the top of the solvent recovery tower, and an outlet of the heat exchanger is connected to an inlet of the heater, and is configured to exchange heat between the mixed solution and the recovered solvent, and heat the obtained mixed solution after heat exchange.
The present invention will be described in detail below by way of examples.
Example 1
Solvent recovery deviceAs shown in fig. 1 and 2, the apparatus includes: the system comprises a heat exchanger 2, a heater 3 and a solvent recovery tower 4 which are communicated, wherein a filling section 5, a heat exchange part 6 and a distributor 15 are arranged in the solvent recovery tower 4; wherein the heater 3 is arranged in the middle of the solvent recovery tower 4 and communicated with the distributor 15; the packing section 5 is arranged at the upper part of the solvent recovery tower 4, and the packing section 5 is provided with a grid packing (the specific surface area is 95 m) without holes 2 /m 3 Void fraction 0.94), the heat exchange means 6 is disposed at the lower portion of the solvent recovery column 4, and the distributor 15 is disposed between the packing section 5 and the heat exchange means 6; the heat exchange component 6 comprises a heat exchange medium inlet 8, a heat exchange medium outlet 9, a heat exchange main pipe 12 and heat exchange branch pipes 11, wherein the heat exchange branch pipes 11 are at least one heat exchange pipe which is arranged in parallel in multiple rows, and the inner diameter of each heat exchange pipe is 15 mm; the distance between every two adjacent heat exchange tubes in each row is 20 mm; the distance between two adjacent rows of heat exchange tubes is 50 mm.
Method for recovering solventThe method comprises the following steps:
1) exchanging heat between a mixed solution containing deasphalted oil (properties are shown in table 1) and a solvent (propane, the critical temperature is 96.75 ℃, and the critical pressure is 4.26MPa) and a recovered solvent, and heating the mixed solution after heat exchange to obtain a heated mixed solution, wherein the temperature is 105 ℃, the weight ratio of the deasphalted oil to the propane is 1:8.5, the temperature of the mixed solution is 70 ℃, and the pressure is 5 MPa; the temperature of the recovered solvent is 85 ℃ after heat exchange;
2) and under a supercritical state, carrying out phase separation on the heated mixed solution to obtain a recovered solvent and a deasphalted oil-containing material flow, wherein the phase separation conditions comprise: the temperature is 108 ℃, and the pressure is 4.8 MPa;
3) heating and separating the deasphalted oil-containing material flow from steam under a supercritical state to obtain a deasphalted oil-rich material flow S1, wherein the inlet temperature of the steam is 280 ℃, and the outlet temperature of the steam is 260 ℃; the conditions for the thermal separation include: the temperature is 120 ℃ and the pressure is 4.8 MPa.
Wherein the supercritical solvent recovery is 95.4% and the solvent content in the deasphalted oil-rich stream S1 is 28 wt%.
Based on 100 ten thousand tons/year residual oil treatment capacity (8400 h of start-up in a year) and 37.3 percent of quality yield of deasphalted oil products, the required heat exchange amount and heating amount calculated by the flow simulation software in the example 1 are shown in the table 2.
Comparative example 1
The apparatus for solvent recovery as provided in example 1 was carried out except that the apparatus did not include a heat exchange unit in the solvent recovery column, i.e., the temperatures at the top and bottom of the column were the same.
Method for recovering solventThe method comprises the following steps:
1) exchanging heat between a mixed solution containing deasphalted oil (properties are shown in table 1) and a solvent (propane, the critical temperature is 96.75 ℃, and the critical pressure is 4.26MPa) and a recovered solvent, and heating the mixed solution after heat exchange to obtain a heated mixed solution, wherein the temperature is 120 ℃, the weight ratio of the deasphalted oil to the propane is 1:8.5, the temperature of the mixed solution is 70 ℃, and the pressure is 5 MPa; the temperature of the recovered solvent is 85 ℃ after heat exchange;
2) subjecting the heated mixture to phase separation under supercritical conditions to obtain a recovered solvent and a deasphalted oil-rich stream D1, wherein the phase separation conditions include: the temperature is 120 ℃, and the pressure is 4.8 MPa;
wherein the supercritical solvent recovery is 95.2% and the solvent content in the deasphalted oil-rich stream D1 is 29 wt%.
The heat exchange amount and the heating amount required by the calculation of the flow simulation software in the comparative example 1 are shown in the table 2, wherein the residual oil treatment amount is 100 ten thousand tons/year (8400 h for annual start-up), and the quality yield of the deasphalted oil product is 37.3%.
Example 2
Solvent recovery deviceAs shown in fig. 1 and 4, the apparatus includes: the heat exchanger 2, the heater 3 and the solvent recovery tower 4 are communicated, and a filler section 5, a heat exchange part 6 and a distributor 15 are arranged in the solvent recovery tower 4; wherein the heater 3 is arranged atThe middle part of the solvent recovery tower 4 is communicated with the distributor 15; the packing section 5 is arranged at the upper part of the solvent recovery tower 4, and the packing section 5 is provided with a grid packing (the specific surface area is 100 m) without holes (the size is not more than one hundred centimeters) 2 /m 3 Void fraction 0.95), the heat exchange member 6 is disposed at the lower portion of the solvent recovery column 4, and the distributor 15 is disposed between the packing section 5 and the heat exchange member 6; the heat exchange component 6 comprises a heat exchange medium inlet 8, a heat exchange medium outlet 9, a heat exchange main pipe 12 and a heat exchange branch pipe 11, wherein the heat exchange branch pipe 11 is at least one heat exchange pipe which is arranged in a series multilayer mode, and the inner diameter of each heat exchange pipe is 20 mm; the distance between every two adjacent heat exchange branch pipes in each layer is 60 mm; the height between two adjacent layers of the heat exchange branched pipes is 120 mm.
Method for recovering solventThe method comprises the following steps:
1) exchanging heat between a mixed solution of deasphalted oil (properties are shown in table 1) and a solvent (n-butane, the critical temperature is 152.0 ℃, and the critical pressure is 3.8MPa) and a recovered solvent, and heating the mixed solution after heat exchange to obtain a heated mixed solution, wherein the temperature is 180 ℃, the weight ratio of the deasphalted oil to the n-butane is 1:3.9, the temperature of the mixed solution is 130 ℃, and the pressure is 4.7 MPa; the temperature of the recovered solvent after heat exchange is 145 ℃;
2) and under a supercritical state, carrying out phase separation on the heated mixed solution to obtain a recovered solvent and a deasphalted oil-containing material flow, wherein the phase separation conditions comprise: the temperature is 185 ℃, and the pressure is 4.5 MPa;
3) under a supercritical state, heating and separating the deasphalted oil-containing material flow and heat conducting oil to obtain an deasphalted oil-rich material flow S2, wherein the inlet temperature of the heat conducting oil is 320 ℃, and the outlet temperature of the heat conducting oil is 280 ℃; the conditions for the thermal separation include: the temperature was 200 ℃ and the pressure was 4.5 MPa.
Wherein the supercritical solvent recovery is 91.0% and the solvent content in the deasphalted oil rich stream S2 is 26 wt%.
Based on the 200 ten thousand tons/year residual oil treatment capacity (8400 h of start-up), the yield of deasphalted oil products is 61.0 percent, and the required heat exchange amount and the heating amount calculated by the flow simulation software in the example 2 are shown in the table 2.
Comparative example 2
The apparatus for solvent recovery as provided in example 2 was followed except that the apparatus did not include heat exchange means in the solvent recovery column, i.e., the temperatures at the top and bottom of the column were the same.
Method for recovering solventThe method comprises the following steps:
1) exchanging heat between a mixed solution containing deasphalted oil (properties are shown in table 1) and a solvent (n-butane, the critical temperature is 152.0 ℃, and the critical pressure is 3.8MPa) and a recovered solvent, and heating the mixed solution after heat exchange to obtain a heated mixed solution, wherein the temperature is 200 ℃, the weight ratio of the deasphalted oil to the n-butane is 1:3.9, the temperature of the mixed solution is 130 ℃, and the pressure is 4.7 MPa; the temperature of the recovered solvent after heat exchange is 145 ℃;
2) subjecting the heated mixture to phase separation under supercritical conditions to obtain a recovered solvent and a deasphalted oil-rich stream D2, wherein the phase separation conditions include: the temperature is 200 ℃, and the pressure is 4.5 MPa;
wherein the supercritical solvent recovery was 90.0% and the solvent content in the deasphalted oil-rich stream D2 was 28 wt%.
The heat exchange amount and the heating amount required by the calculation of the process simulation software in the comparative example 2 are shown in the table 2 according to the residual oil treatment amount of 200 ten thousand tons/year (8400 h for starting every year) and the deasphalted oil product yield of 61.0%.
Example 3
Solvent recovery deviceAs shown in fig. 1 and 4, the apparatus includes: the system comprises a heat exchanger 2, a heater 3 and a solvent recovery tower 4 which are communicated, wherein a filling section 5, a heat exchange part 6 and a distributor 15 are arranged in the solvent recovery tower 4; wherein, the heater 3 is arranged in the middle of the solvent recovery tower 4 and is communicated with the distributor 15; the packing section 5 is arranged at the upper part of the solvent recovery tower 4, and the packing section 5 is provided with a grid packing (the specific surface area is 100 m) without holes (the size is not more than one hundred centimeters) 2 /m 3 Void fraction 0.95), the heat exchange means 6 is provided at the lower part of the solvent recovery column 4, and the distributor 15 is provided between the packing section 5 and the heat exchange means 6; the heat exchange component 6 comprises a heat exchange medium inlet 8, a heat exchange medium outlet 9, a heat exchange main pipe 12 and a heat exchange branch pipe 11, wherein the heat exchange branch pipe 11 is at least one heat exchange pipe which is arranged in series and in multiple layers, and the interior of the heat exchange pipeThe diameter is 20 mm; the distance between every two adjacent heat exchange branch pipes in each layer is 50 mm; the height between two adjacent layers of heat exchange branched pipes is 200 mm.
Method for recovering solventThe method comprises the following steps:
1) exchanging heat between a mixed solution of deasphalted oil (properties are shown in table 1) and a solvent (n-pentane, the critical temperature is 196.5 ℃, and the critical pressure is 3.38MPa) and a recovered solvent, and heating the mixed solution after heat exchange to obtain a heated mixed solution, wherein the temperature is 220 ℃, the weight ratio of the deasphalted oil to the n-pentane is 1:3, the temperature of the mixed solution is 175 ℃, and the pressure of the mixed solution is 4.2 MPa; the temperature of the recovered solvent is 190 ℃ after heat exchange;
2) and under a supercritical state, carrying out phase separation on the heated mixed solution to obtain a recovered solvent and a deasphalted oil-containing material flow, wherein the phase separation conditions comprise: the temperature is 225 ℃, and the pressure is 4 MPa;
3) under a supercritical state, heating and separating the deasphalted oil-containing material flow and heat conducting oil to obtain an deasphalted oil-rich material flow S3, wherein the inlet temperature of the heat conducting oil is 320 ℃, and the outlet temperature of the heat conducting oil is 290 ℃; the conditions for the thermal separation include: the temperature was 240 ℃ and the pressure was 4 MPa.
Wherein the supercritical solvent recovery was 85.7% and the solvent content in the deasphalted oil-rich stream S3 was 30 wt%.
Based on the residual oil treatment capacity of 200 ten thousand tons/year (8400 h of start-up per year) and the deasphalted oil product quality yield of 79.0 percent, the required heat exchange amount and the heating amount calculated by the flow simulation software in the example 3 are shown in the table 2.
Comparative example 3
The apparatus for solvent recovery as provided in example 3 was followed except that the apparatus did not include heat exchange means in the solvent recovery column, i.e., the temperatures at the top and bottom of the column were the same.
Method for recovering solventThe method comprises the following steps:
1) exchanging heat between a mixed solution containing deasphalted oil (properties are shown in table 1) and a solvent (n-pentane, the critical temperature is 196.5 ℃, the critical pressure is 3.38MPa) and the recovered solvent, and heating the mixed solution after heat exchange to obtain a heated mixed solution, wherein the temperature is 240 ℃, the weight ratio of the deasphalted oil to the n-pentane is 1:3, the temperature of the mixed solution is 175 ℃, and the pressure is 4.2 MPa; the temperature of the recovered solvent after heat exchange is 190 ℃;
2) subjecting the heated mixture to phase separation under supercritical conditions to obtain a recovered solvent and a deasphalted oil-rich stream D3, wherein the phase separation conditions include: the temperature is 240 ℃ and the pressure is 4 MPa;
wherein the supercritical solvent recovery is 82.1% and the solvent content in the deasphalted oil-rich stream D3 is 35 wt%.
The heat exchange amount and the heating amount required by the calculation of the flow simulation software in the comparative example 3 are shown in the table 2, wherein the residual oil treatment amount is 200 ten thousand tons/year (8400 h for annual start-up), and the quality yield of the deasphalted oil product is 79.0%.
Example 4
The apparatus and process of example 1 were followed except that the apparatus did not include a heat exchanger, i.e., the mixture of deasphalted oil and solvent was directly heated, and the same procedure was followed to obtain an extract-rich oil stream S4, wherein the solvent content in the extract-rich oil S4 was 28 wt%.
Based on 100 ten thousand tons/year residual oil treatment capacity (8400 h of start-up in a year) and 37.3 percent of quality yield of deasphalted oil products, the required heat exchange amount and heating amount calculated by the flow simulation software in example 4 are shown in the table 2.
Example 5
The apparatus and process of example 1 was followed except that the temperature of the mixed liquor was replaced with 103 ℃ after heating in the same process, and an extract-rich stream S5 was obtained in which the recovered solvent exhibited trace amounts of deasphalted oil, 1% of the total deasphalted oil feed, with a 95.1% supercritical solvent recovery and 29.5 wt% solvent in the extract-rich S5.
Based on 100 ten thousand tons/year residual oil treatment capacity (8400 h per year), the deasphalted oil product quality yield is 37.3 percent, and the required heat exchange amount and the heating amount are calculated by the flow simulation software in example 5 and are shown in the table 2.
Example 6
The apparatus and process of example 1 were followed except that in the process, a mixed liquor booster pump was added to boost the pressure of the feed mixed liquor from 5MPa to 6.7MPa and the pressure of the phase separation and heat separation was 6.5 MPa; the rest steps are the same, and an extract oil-rich material flow S6 is obtained, wherein deasphalted oil appears in the recovered solvent, the deasphalted oil accounts for 1.5% of the total deasphalted oil feeding material, the supercritical solvent recovery rate is 95.1%, and the solvent content in the extract oil-rich S6 is 29.8 wt%.
Based on 100 ten thousand tons/year residual oil treatment capacity (8400 h per year), the deasphalted oil product quality yield is 37.3 percent, and the required heat exchange amount and the heating amount are calculated by the flow simulation software in example 6 and are shown in the table 2.
TABLE 1
TABLE 2
| Example 1 | Comparative example 1 | Example 2 | Comparative example 2 | Example 3 | |
| Heat exchange amount/kW | 16743 | 23119 | 32568 | 39947 | 26855 |
| Heating power/kW | 8368 | 8539 | 20086 | 20093 | 23673 |
TABLE 2
| Comparative example 3 | Example 4 | Example 5 | Example 6 | |
| Heat exchange amount/kW | 34304 | 0 | 16743 | 9521 |
| Heating power/kW | 23702 | 25111 | 8218 | 7125 |
As can be seen from the data in Table 2, by adopting the method for recovering the solvent, provided by the invention, the solvent-containing material flow and the heat exchange medium are heated and separated, so that the solvent content of the tower bottom material flow is ensured to reach the standard while the temperature of the recovered solvent is reduced, the feeding temperature of the solvent recovery tower is reduced, the effects of reducing the heat exchange quantity and the heating heat load of the recovered solvent are achieved, the energy consumption is reduced, and the investment and the occupied area of the device are reduced.
Specifically, comparing example 1 with comparative example 1, it can be seen that, by adopting the method of the present invention, the heat exchange amount required by the solvent recovery method of example 1 is reduced by 6376kW and the heating amount is reduced to some extent, compared with the solvent recovery method of comparative example 1, based on 100 ten thousand tons/year residual oil treatment amount (8400 h per year operation) and the deasphalted oil product quality yield of 37.3%; comparing example 2 with comparative example 2, it can be seen that, in terms of 200 ten thousand tons/year residual oil treatment capacity (8400 h of start-up per year) and the deasphalted oil product quality yield of 61.0%, by adopting the method of the present invention, the heat exchange amount required by example 2 is reduced by 7379kW compared with the solvent recovery method of comparative example 2, and the heating amount is reduced; comparing example 3 with comparative example 3, it can be seen that, by adopting the method of the present invention, the heat exchange amount required by example 3 is reduced by 7449kW compared with the solvent recovery method of comparative example 3, and the heating amount is reduced to some extent, in terms of 200 ten thousand tons/year residual oil treatment amount (8400 h of start-up per year) and the deasphalted oil product quality yield of 79.0%; comparing example 1 with example 4, it can be seen that, based on 100 ten thousand tons/year residual oil treatment capacity (8400 h per year), the deasphalted oil product quality yield is 37.3%, by adopting the method of the invention, the solvent heat load recovered in example 1 is 16743kW, and the heating amount is reduced, so that the energy consumption is reduced; comparing example 1 with example 5, it can be seen that the quality yield of deasphalted oil product is 37.3% based on 100 ten thousand tons/year residual oil treatment (8400 h/year start), although the heating amount of example 5 is reduced, the recovered solvent contains trace amount of deasphalted oil, and slight pollution is generated; comparing example 1 with example 6, it can be seen that, based on 100 ten thousand tons/year residual oil treatment capacity (8400 h per year), the deasphalted oil product quality yield is 37.3%, in example 6, the phase separation and heating separation are performed under higher pressure, the heat exchange amount is reduced by 7222kW, the heating amount is reduced by 1243kW, but the separation effect of the solvent recovery tower is poor, the recovered solvent contains deasphalted oil, which causes serious pollution, affects the extraction effect of the solvent, and increases the energy consumption of the booster pump and the equipment investment of the solvent recovery tower due to the increase of the operating pressure.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (10)
1. A method of solvent recovery, comprising the steps of:
(1) heating the mixed solution containing the extraction oil and the solvent to obtain a heated mixed solution;
(2) carrying out phase separation on the heated mixed solution to obtain a recovered solvent and an extract oil-containing material flow;
(3) heating and separating the extract oil-containing material flow to obtain an extract oil-rich material flow;
wherein step (2) and step (3) are each independently performed in a supercritical state.
2. The method of claim 1, wherein the temperature of the heated mixed liquor is above the critical temperature of the solvent;
preferably, the temperature of the heated mixed solution is 5-50 ℃ higher than the critical temperature of the solvent, and is preferably 10-35 ℃;
preferably, in the mixed solution, the weight ratio of the extraction oil to the solvent is 1: 1-15, preferably 1: 1-10;
preferably, the recovered solvent in step (2) is subjected to heat exchange with the mixed solution before the heating;
preferably, the weight ratio of the recovery solvent to the mixed solution is 1: 1.2-2, preferably 1: 1.3-1.5;
preferably, the temperature of the recovered solvent after heat exchange is 1-20 ℃ higher than the temperature of the mixed solution, and preferably 5-15 ℃.
3. The process of claim 1 or 2, wherein the extracted oil is a deasphalted oil;
preferably, the content of asphaltene is less than or equal to 1 wt% and the content of metal is less than or equal to 50 [ mu ] g/g based on the total weight of the deasphalted oil;
preferably, the extracted oil is extracted from at least one heavy oil selected from the group consisting of atmospheric residue, vacuum residue, heavy oil of poor quality and oil sand;
preferably, the solvent is at least one of C4-C6 alkanes, preferably at least one selected from the group consisting of mixed hydrocarbons of C4 alkanes, mixed hydrocarbons of C4-C5 alkanes, mixed hydrocarbons of C5 alkanes, mixed hydrocarbons of C5-C6 alkanes, and mixed hydrocarbons of C6 alkanes.
4. The method of any of claims 1-3, wherein the conditions for phase separation comprise: the temperature is 5-50 ℃ higher than the critical temperature of the solvent, preferably 10-35 ℃; the pressure is 0.5-2MPa higher than the critical pressure of the solvent, preferably 0.5-1 MPa;
preferably, the conditions for the thermal separation include: the temperature is 10-30 ℃ higher than the temperature of the phase separation, preferably 15-25 ℃; the pressure is 0.5-2MPa, preferably 0.5-1MPa, above the critical pressure of the solvent.
5. A process according to any one of claims 1 to 4, wherein the solvent is present in the extract oil-rich stream in an amount of 50 wt.% or less, preferably in an amount of 25 to 35 wt.%;
preferably, the process of heating separation comprises: exchanging heat between the extract oil-containing material flow and a heat exchange medium, and separating the extract oil-containing material flow after heat exchange;
preferably, the inlet temperature of the heat exchange medium is 250-350 ℃, preferably 280-320 ℃; the outlet temperature of the heat exchange medium is 200-330 ℃, preferably 270-310 ℃;
preferably, the heat exchange medium is selected from steam and/or thermal oil.
6. An apparatus for solvent recovery, the apparatus comprising: the device comprises a heater and a solvent recovery tower, wherein a filler section, a distributor and a heat exchange component are sequentially arranged in the solvent recovery tower from top to bottom;
the heater is arranged in the middle of the solvent recovery tower, is communicated with the distributor and is used for heating mixed liquid containing extraction oil and a solvent, and the obtained heated mixed liquid is uniformly distributed in the solvent recovery tower through the distributor and flows upwards to enter the filler section;
the filler section is used for carrying out phase separation on the heated mixed solution in a supercritical state to obtain a recovered solvent and an extract oil-containing material flow, wherein the extract oil-containing material flow flows downwards to enter the heat exchange part;
the heat exchange part is used for heating and separating the extract oil-containing material flow in a supercritical state to obtain an extract oil-rich material flow.
7. The apparatus of claim 6, wherein the filler section is provided with coalescing filler;
preferably, the specific surface area of the coalescing filler is more than or equal to 80m 2 /m 3 Preferably 90 to 200m 2 /m 3 (ii) a The porosity is more than or equal to 0.9, preferably 0.92-0.98;
preferably, the manner of the coalescent packing is selected from random packing and/or structured packing, and the coalescent packing is preferably selected from non-open-cell grid packing and/or plate corrugated packing.
8. The device of claim 6 or 7, wherein the heat exchange component comprises a heat exchange medium inlet, a heat exchange header pipe, a heat exchange branch pipe and a heat exchange medium outlet which are communicated in sequence, and the heat exchange medium inlet and the heat exchange medium outlet are respectively and independently arranged on the tower wall of the solvent recovery tower;
preferably, the heat exchange medium inlet is located below the heat exchange medium outlet.
9. The apparatus of claim 8, wherein the heat exchange sub-tubes are at least one heat exchange tube arranged in parallel in a plurality of rows, and the heat exchange sub-tubes are arranged in a longitudinal direction;
preferably, when the heat exchange branched pipes are arranged in multiple parallel rows, the distance between every two adjacent heat exchange branched pipes in each row is 5-40mm, and preferably 10-30 mm; the distance between two adjacent rows of heat exchange branched pipes is 30-100mm, preferably 40-80 mm;
preferably, the heat exchange branched pipes are at least one heat exchange pipe which is arranged in a series multilayer manner, and the heat exchange branched pipes are arranged along the transverse direction and in an inclined manner;
preferably, the inclination angle of the heat exchange branch pipe is 10-60 degrees, preferably 20-45 degrees;
preferably, when the heat exchange branched pipes are arranged in a plurality of layers in series, the distance between every two adjacent heat exchange branched pipes in each layer is 10-80mm, and preferably 20-60 mm; the height between two adjacent layers of the heat exchange branch pipes is 50-1000mm, and preferably 100-400 mm.
10. The apparatus of any one of claims 6-9, wherein the apparatus further comprises a heat exchanger;
preferably, an inlet of the heat exchanger is connected to the top of the solvent recovery tower, and an outlet of the heat exchanger is connected to an inlet of the heater, and is configured to exchange heat between the mixed solution and the recovered solvent, and heat the obtained mixed solution after heat exchange.
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| CN105400545A (en) * | 2014-09-10 | 2016-03-16 | 中国石油大学(北京) | Heavy oil separation method and treatment system thereof |
| WO2017137912A1 (en) * | 2016-02-10 | 2017-08-17 | University Of Kwazulu-Natal | Supercritical extraction process |
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| US4305814A (en) * | 1980-06-30 | 1981-12-15 | Kerr-Mcgee Refining Corporation | Energy efficient process for separating hydrocarbonaceous materials into various fractions |
| US4784753A (en) * | 1985-10-17 | 1988-11-15 | Institut Francais Du Petrole | Deasphalting process comprising power recovery from the stage of separating deasphalted oil from the deasphalting solvent |
| GB8711349D0 (en) * | 1986-05-14 | 1987-06-17 | Inst Francais Du Petrole | Deasphalting process |
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