KR900000861B1 - Treating process of petroleum - Google Patents

Abstract

A reformed oil is produced by introducing a petroleum heavy oil preheated in a preheater to 450-550≰C into the top of a heatinsulated cracking device where the oil flows down in the form of plug flow straigtened by multistage horizontal perforated plates and low speed horizontal stirring at 390-450≰C and abov 1 atm. for 1-5 hrs. residence time in the cracking device. 30-65 Wt.% of the component having above 500 ≰C b.pt. in the heavy oil is converted to a lower boiling component having below 500 ≰C b.pt. and cracked gaseous prod. generated by cracking rises upward counter-currently to the downward liq. flow together with purging steam introduced in the bottom of the cracking device.

Description

Treatment method of petroleum heavy oil

1 is a flowchart illustrating an example of the method of the present invention.

* Explanation of symbols for main parts of the drawings

2: preheater 4: pyrolysis

7: mixer 9: first separation column

11: second separation tower 14: third separation tower

21: separator 24: separator

The present invention relates to a method for treating petroleum heavy oil. More specifically, the present invention relates to a treatment method for obtaining an active ingredient which is essentially free of asphaltenes and heavy metals from petroleum heavy oils.

Many treatments have been proposed for separating and recovering active ingredients contained in petroleum heavy oils, including the use of catalysts or hydrogen under high pressure. However, such methods were not completely satisfactory. For example, a method of treating petroleum heavy oil using a catalyst usually causes catalyst deterioration over time. This degradation is usually due to heavy metals and asphaltenes present in large quantities in the heavy streams. The process of treating petroleum heavy oil by hydrogenation under high pressure is uneconomical, especially when consuming a large amount of hydrogen.

As a result of the above drawbacks associated with catalysis and hydrocracking, other methods, including thermal cracking and solvent extraction, have been proposed and put into use as alternatives for treating petroleum heavy oils. These methods do not require the use of a catalyst or hydrogen and thus avoid the problems encountered by the above methods. Known pyrolysis methods include, for example, visbreaking methods such as those described in US Pat. No. 4,454,023, and delayed coking methods, both of which have been widely used for pyrolysis of heavy oils.

However, even these alternative pyrolysis methods do not completely solve the problem. For example, in the bisbreaking method for treating heavy oil, heat treatment is performed under mild conditions because of the specific use of the product to be obtained, so that only a small part of the total macromolecular components in the raw heavy oil are decomposed. On the other hand, in the delayed coking process, since the heat treatment is performed under severe conditions, coking and dehydrogenation of the hydrocarbon component in the raw heavy oil is unnecessary. Thus, these two methods represent the extremes of pyrolysis.

Solvent extraction has also been proposed. However, using such a method alone can recover only a limited amount of the effective milk product. This is especially true when this raw material contains a high content of heavy metals. In view of the efficient use of resources and energy, further improvements are needed in the treatment of petroleum heavy oils.

Large quantities of asphaltenes and heavy metals by a novel combination of reliable and simple processes that convert economical and efficient crude oils into high value components, removing asphaltenes and heavy metals from them and keeping loss of active ingredients to a minimum A method of treating petroleum heavy oil raw materials containing petroleum is developed.

More specifically, the present invention relates to a novel and improved process for treating petroleum heavy oil feedstocks. The novel and improved process of the present invention is to introduce the raw petroleum heavy oil preheated to a temperature of about 450 ° C. to 550 ° C. in the preheater on top of the thermal cracker in adiabatic state. Preheated crude petroleum heavy oil flows downwardly through the pyrolyzer under plug-flow conditions using multistage horizontal perforated plates spaced throughout the pyrolyzer. The operating conditions in the pyrolyzer are temperatures of about 390 ° C to 450 ° C, pressures above atmospheric pressure and residence times of about 1 to about 5 hours.

Since the petroleum-based heavy oil raw material flows downward through the pyrolyzer, the distillation vapor and gaseous products formed by the pyrolysis of the petroleum-based heavy oil raw material are removed by steam introduced at the bottom of the pyrolyzer. The system flows upward in the countercurrent to heavy oil feedstock. Under the above conditions, 30 to 65% of the components of the petroleum-based heavy oil raw material having a boiling point exceeding about 500 ° C are converted to a component having a boiling point of less than about 500 ° C. The cracked bottom oil is recovered from the bottom of the pyrolyzer, which is similar to the liquid pitch. The bottom oil containing asphaltenes, heavy metals and active milk powder is mixed with a solvent and the mixture is solvent extracted. Solvent extraction is carried out at temperatures and pressures at or near the critical point of the solvent and above the softening point of asphaltenes. Under such conditions, the mixture of asphaltenes and heavy metals is rapidly and efficiently separated from the active milk powder in the above bottom oil.

1 is a flowchart illustrating an example of the method of the present invention.

The novel method of the present invention consists of a series of processes, thereby improving the overall yield and quality of the effective milk powder. These processes result in the selective pyrolysis of petroleum-based heavy oil feedstocks such as atmospheric or vacuum distillation column bottoms (i.e. atmospheric or vacuum residues). This selective pyrolysis is carried out under conditions in which the polymer hydrocarbon component is limited to decomposition in the raw material in which the decomposition of the petroleum heavy oil raw material is only relatively easily decomposed. During this selective pyrolysis process, the separation and recovery of the light hydrocarbons formed is facilitated by simultaneous steam stripping. Simultaneous steam stripping can minimize further decomposition of the formed hard hydrocarbon components and thus avoid unnecessary ejection of gaseous by-products. Then, the pyrolyzed petroleum heavy oil recovered from the bottom of the pyrolyzer is subjected to the highly efficient critical solvent extraction-separation treatment constituting the second step of the process of the present invention. By the use of a critical solvent extraction-separation process, most of the active milk remaining in the pyrolyzed heavy oil is recovered.

In carrying out the method of the present invention, the operating conditions applied to the pyrolysis process and the critical solvent extraction-separation process are selected according to the components of the petroleum heavy oil raw material to maximize the overall yield and quality of the recovered effective milk powder. The yields and qualities described above when run under optimum conditions are much higher than those obtained from conventional methods such as catalysis, hydrocracking, bisbreaking, delayed coking or solvent extraction. It is also a high fluidized bed, such as heavy metals containing asphaltenes recovered from the bottoms oil or bottom oil solvent extraction-separation processes recovered from the pyrolysis process of the process. The high flowability of these materials makes them easier to handle than recovered from the conventional methods described above.

In the process of the present invention, the operating conditions used for pyrolysis are those conditions which facilitate the selective concentration of nickel, vanadium and other heavy metals in the petroleum heavy oil feedstock to the asphaltene of pyrolyzed heavy oil recovered from the tower of the pyrolyzer. to be. In this regard, at least about 30% by weight, preferably at least about 40% by weight, of components of petroleum-based heavy oil raw materials having an atmospheric boiling point above about 500 ° C. It has been found that the pyrolysis treatment should be carried out to such an extent that it decomposes to components below the atmospheric boiling point of about 500 ° C. However, in order to avoid excessive dehydrogenation and ejection of gaseous fractions and to maximize the overall yield of the active milk powder, at least about 65% by weight, preferably about 60% by weight, of components of petroleum-based heavy oil raw materials having an atmospheric boiling point above about 500 ° C. The degree of decomposition is limited in the pyrolysis process of the method of the present invention so that the above does not decompose into components having an atmospheric boiling point of less than about 500 ° C.

On the other hand, in the non-breaking method, it is carried out under a pressure of 10 to 30 kg / cm 2 and a residence time of about 10 to 40 minutes. Only about 15 to 25% by weight of the component having an atmospheric boiling point above 500 ° C. in the raw material has an atmospheric boiling point below 500 ° C. Decomposes into ingredients.

The importance of the upper limit described above with respect to the degree of decomposition carried out in the pyrolysis process is closely related to the overall economics and the stable operation of the process constituting the present invention. For example, if the thermal decomposition degree exceeds the above upper limit, a large amount of inexpensive gaseous product will occur and at the same time the formation of coke will greatly increase. In addition, when the amount of coke in the pyrolysed heavy oil recovered from the pyrolyzer is increased, the final residual oil or asphaltenes separated and recovered during the extraction process of the process of the present invention is cured into a material that is difficult to handle, not a liquid state. In such a case, the separation, recovery, and release of the final residual oil or asphaltenes are extremely difficult and complicated apparatus is required to accomplish this. Thus, the pyrolysis degree in the first process of the present invention limits the pyrolysed heavy residues recovered therefrom to contain a minimum amount of coke. As a result, the final residual oil or asphaltenes extracted during the extraction process of the present invention is highly fluid at the process temperature. Such high fluidity facilitates separation, recovery and the like and simplifies the apparatus used and its arrangement. U.S. Patent Nos. 4,435,276 and 4,443,328 further describe operating conditions, apparatus, and the like for performing such selective pyrolysis or the first process of the method of the present invention. These patents are incorporated herein by reference.

The pyrolyzed heavy oil or column bottom oil recovered from the pyrolyzer is subjected to the critical solvent extraction-separation constituting the second process of the present invention. The heavy oil pyrolyzed in this second process is mixed with the critical solvent. The mixture is then subjected to temperature and pressure conditions which are higher than the softening point of asphaltene in the pyrolyzed residue and preferably close to the critical point of the solvent. Under these conditions, asphaltenes are less soluble in critical solvents than active powders, and rapid separation of asphaltenes from the mixture proceeds. After removing the separated asphaltenes, it is further heated to raise the temperature of the remaining mixture of the critical solvent and the effective milk (or to reduce the pressure), thereby lowering the solubility of the active ingredient in the solvent, thereby separating the effective milk from the solvent. Be sure to Upon recovery of the separated effective milk powder, the solvent is readily recovered and reused for the extraction of the bottom oil from the pyrolyzer used in the first step of the process of the invention. US Patent No. 2,940,920; 2,967,818; 2,980,602; 3,003,945; 3,003,946; 3,003,947; 3,005,769; 4,125,459; 4,239,616 and 4,273,644 describe specific operating conditions, such as the temperature, pressure, and materials available for the extraction solvent used in the second process of the present invention. These patents are described herein for reference.

In FIG. 1, petroleum heavy oil raw materials, such as atmospheric pressure or distillation column bottom oil, are introduced into preheater 2 through tube 1. In preheater 2, the petroleum heavy oil raw material is heated to a temperature above about 450 to 550 ° C under pressure in the range of about 1 to about 10 kg / cm 2. To avoid coking of the raw material it passes through preheater 2 at a speed of about 2 to about 20 m / sec.

Then, the preheated raw material is transferred from the preheater 2 to the upper portion of the cylindrical pyrolyzer 4 through the tube 3. Steam, preferably superheated steam, is introduced into the bottom of pyrolyzer 4 via tube 18 and steam distributor 18 '. This superheat steam flows countercurrently to the upwardly flowing and downwardly reacting feedstock. The overheated steam flowing in countercurrent facilitates the evaporation and removal of cracker light component oil from the downwardly reacting heat reacting feedstock, thus eliminating the need to apply reduced pressure distillation to the pyrolyzed residues from which pyrolysis is recovered from 4. The amount of superheat steam introduced into the pyrolyzer 4 through the tube 18 and bonsai device 18 'to evaporate and remove the decomposed light component oil is in the range of about 5 to 20% by weight of the feed stream undergoing thermal reaction in the pyrolyzer 4.

In general, pyrolyzer 4 is operated at atmospheric pressure and at temperatures from about 390 ° C. up to the temperature of the preheated raw material introduced. The residence time of the raw material in the pyrolysis machine 4 is two times or more, that is, about 1 to about 10 hours, compared with that of the visbreaking method.

In carrying out the process of the invention, the crude oil to be thermally reacted must be descended through pyrolyzer 4 in essentially plug-flow form, preferably not stagnant at or near the inner surface of pyrolyzer 4. When the plug-flow cannot be maintained, heat-reacting crude oil forms passages and eddys in the descending column. Such a passage and circumference once formed provides a passage through which a portion of the crude oil passes quickly through the pyrolyzer 4. Shorter residence times of these parts of the pyrolysed feedstock in pyrolyzer 4 lower the overall conversion of crude oil to a more valuable powdered milk product, which is undesirable.

In order to maintain the plug-flow of the pyrolyzing crude oil flowing downward and to prevent stagnation, the multi-stage horizontal porous distribution plates 4a to 4j are installed in the pyrolyzer 4.

The pyrolyzer 4 also has a drive shaft 38 which is operated by a motor 40. The drive shaft 38 is equipped with a multi-stage horizontal scraper blade, only two of which 38a and 38b are shown in the drawing. The horizontal scraper blade attached to the drive shaft 38 is located immediately adjacent to each of the multistage horizontal porous distribution plates 4a to 4h and extends from the drive shaft 38 to the outside near the inner surface of the pyrolyzer 4. The purpose of the drive shaft 38 and the multi-stage horizontal scraper blade attached thereto is to distribute the meso-phase coke precursor produced as part of the pyrolysis reaction evenly throughout the downwardly flowing thermal reaction crude oil. By distributing these meso-phase coke precursors evenly throughout the descending reaction flow, it is possible to fundamentally prevent agglomeration of these precursors and consequently the accumulation of coke in the pyrolyzer 4.

The mixture of cracked light oil steam, a small amount of cracked gas and steam flows upward through the pyrolyzer 4 and the multi-stage horizontal porous plate 4a to 4g against the descending thermal reaction crude oil. The mixture is then discharged from the top of pyrolyzer 4 through tube 19 and passed through condenser 20 to separator 21. This mixture is separated in the separator 21 into cracked gas streams, condensate streams and cracked light streams, which are conveyed from separator 21 via tubes 22, 23 and 34, respectively.

Inductive pyrolysis residue is conveyed from the bottom of pyrolyzer 4. This fluidized bottom oil is sent directly from the pyrolyzer 4 to the mixer 7 by means of a pump 5 through a tube 6. In mixer 7, this flowable residual oil is mixed with a suitable solvent introduced into mixer 7 via tube 33 in a volume ratio of about 1: 8 to about 1:12. The mixture of pyrolyzed bottoms bottoms and solvent is then passed through a tube 8 to the first separation column 9 where the temperature of the mixture is maintained at an elevated temperature near the critical temperature of the solvent and the pressure of the mixture at the temperature near the vapor pressure of the solvent. It is maintained at an elevated pressure. In the first separation column 9, the above mixture of the bottoms bottom oil and the solvent pyrolyzed at the operating temperature in the first separation column 9 is composed of a resinous component, an active powder and a solvent, and a fluid first heavy phase containing asphaltene and heavy metals. Separated by. The first flowable hard phase is withdrawn from the first separation tower 9 via tube 10 and conveyed to the second separation tower 11 via heater 27. By heater 27 the first flowable hard phase is heated to a temperature higher than the temperature in the first separation column.

The fluid first heavy phase containing asphaltenes, heavy metals and some solvent is withdrawn from the bottom of the first separation column 9 and introduced into the separator 24 via a tube 12 with a pressure reducing valve 35. Further depressurization in separator 24 allows the solvent to evaporate. Solvent is recovered from separator 24 through tube 26. The recovered solvent can then be circulated to mixer 7 through the corresponding condenser 30, pump 32 and tube 33. The asphaltenes during evaporation and recovery of the solvent in separator 24 are recovered and recovered from the separator in a high flow bed through tube 25.

The first hard phase is withdrawn from the first separation tower 9 and heated in a heater 27 to a temperature higher than the temperature in the first separation tower and then transported to the second separation tower 11. In the second separation column 11, the first hard phase is separated into a second fluid hard phase containing an active milk powder and a solvent and a fluid second heavy phase containing a resin component and some solvent. The second flowable hard phase is withdrawn from the column top of the second separation column 11 via tube 13 and heated in a heater 28 above the critical temperature of the solvent and then introduced into the third separation column 14. The fluid second heavy phase containing the resin component is discharged in a fluid state from the bottom of the second separation column 11 through a tube 15 degrees, recovered or recycled to the preheater 2, mixed with fresh raw oil, and decomposed in the pyrolyzer 4.

In a third separation column 14 in which the solvent is in a supercritical state, the second hard phase separates into a third hard phase and a desired third heavy phase containing deasphalted oil. The product is withdrawn from the column bottom of the third separation column 14 through tube 16. The third hard phase containing the original extractant is withdrawn from the top of the third separation column 14 via tube 17 and recycled to mixer 7 via the corresponding coolers 29 and pump 31. A replenishment solvent is supplied to mixer 7 by pump 36 via tube 37 to replenish a small amount of solvent lost from the apparatus, where asphaltenes, resins and active powders are separated and recovered.

The method of the invention is illustrated by the following examples which in no way limit the scope of the invention.

EXAMPLE

A crude oil consisting of mixed vacuum distillation tower bottoms (reduced bottom oil) obtained from Middle Eastern crude oil and containing 83 ppm nickel and 272 ppm vanadium was preheated to 480 ° C. and introduced into the top of a pyrolyzer having a 10 stage horizontal porous cracker. . Under the reaction conditions at atmospheric pressure and decomposition tower temperature of 420 ° C., the residue under reduced pressure flows downward of the pyrolyzer. The residence time of the thermally reacted vacuum residue in the pyrolyzer was about 120 minutes. As the vacuum residue reacted thermally flowed downward through the pyrolyzer, steam was supplied to the bottom of the pyrolyzer so that the ratio of steam to residual oil was about 10% by weight. Under these conditions, 55% by weight of the component having a boiling point above 500 ° C in the vacuum residue crude oil was converted to a component having a boiling point below 500 ° C.

A steamy mixed effluent consisting of 4% by weight of cracked gaseous products and 51% by weight of pyrolysis light oil vapor relative to the weight of steam and the original vacuum residue was obtained from the top of the pyrolyzer. In addition, a fluid effluent was recovered from the bottom of the pyrolyzer. This flowable effluent consisted of pyrolyzed bottoms, representing the remaining 45% by weight of the starting vacuum residue. This pyrolytic flowable residue had a softening point of 150 ° C. and an asphaltene content of 40% by weight according to the ring and ball tests.

The pyrolysis fluid residue was fed from the bottom of the pyrolyzer to the mixer, mixed with cyclohexane so that the capacity ratio of the residue to solvent was 1: 10, and then introduced into the first of three successive separation columns. The first separation column had a temperature of 282 ° C. and a pressure of 53.7 kg / cm 2 (52 atm). Under these conditions, the mixture is separated in the first separation column into an asphaltene containing heavy fluidized bed and a hard fluidized bed which is a mixture of resinous component oils, light fractions and cyclohexane solvents. The asphaltene-containing heavy fluid phase containing about 30% of the cyclohexane solvent was withdrawn from the bottom of the first separation column and depressurized to atmospheric pressure to flash and recover the solvent therefrom. About 98% of the cyclohexane contained in this heavy fluid phase is recovered leaving a fluid product rich in asphaltenes, yielding 45% by weight relative to the weight of the pyrolyzed fluid residue feedstock to the first separation column. This asphaltene-rich fluid component contained 460 ppm nickel and 1500 ppm vanadium and had a softening point of 240 ° C. measured according to ring and ball tests.

A hard liquid phase consisting of a mixture of a resin oil, a lighter oil component and a cyclohexane solvent is recovered from the top of the first separation column and heated. The heated hard liquid phase is then introduced to a second separation column operated at an internal temperature of 290 ° C. and an internal pressure of 51.6 kg / cm 2 (50 atm). Under these conditions, the mixture is separated into a second heavy fluid phase containing resin oil and a second hard liquid phase consisting of a mixture of a lighter oil component and a cyclohexane solvent. The second heavy fluid phase containing the resin component oil was discharged and recovered from the bottom of the second separation tower in a yield of 10% by weight relative to the pyrolysis fluid residual material for the first distillation column.

The second hard liquid phase was recovered from the top of the second separation column and further heated before being introduced into the third separation column. The third separation column was operated at an internal temperature of 316 ° C. and an internal pressure of 50.6 kg / cm 2 (49 atm) to separate lighter oil components from the cyclohexane solvent. The lighter oil component was discharged from the bottom of the third separation column and the cyclohexane solvent was withdrawn from the top. The withdrawn cyclohexane solvent was then cooled and recycled to the mixer for reuse.

The lighter oil recovered from the third separation tower had a 45 wt% yield with respect to the pyrolysis fluid residual material for the first distillation column, with 0.5 wt% asphaltene content, 10 ppm nickel and 20 ppm vanadium content.

The combined yield of light pyrolysed light oil recovered directly from the pyrolyzer and lighter oil components extracted and separated by solvent was 71.25% by weight and the removal rate of heavy metals in the initial pyrolysis fluid residue was 98.3%. The amount of cyclohexane solvent consumed during the extraction and separation process was 0.05% by weight relative to the weight of the residual oil feed to the pyrolyzer.

[Comparative Example]

The same reduced pressure residual oil raw material as used in the above example was preheated to 450 ° C. and fed to the same pyrolyzer as the above example. In the pyrolyzer, the reduced pressure residual oil raw material is pyrolyzed without steam stripping under conditions of 14.8 atm, 430 ° C., and a residence time of 10 minutes. Under these conditions similar to those used in conventional bisbreaking methods, only 20% of the components with boiling points above 500 ° C. were converted to components with boiling points below 500 ° C.

The mixture obtained by withdrawing the pyrolyzed fluid residue from the bottom of the pyrolyzer and mixing with pentane in a mixer at a ratio of 10: 1 of solvent to residual oil was obtained at an internal temperature of 177 ° C and an internal pressure of 43.4 kg / cm2 (42 atm). It was introduced into a first separation column operated. Under these conditions, the mixture in the first separation column is separated into a hard liquid phase comprising a mixture of asphaltene containing heavy fluid phase and resin oil, lighter oil component and pentane solvent.

The asphaltene-containing heavy fluid phase containing some pentane exited the bottom of the first separation column and the pressure was reduced to atmospheric pressure, so that the solvent pentane was evaporated and separated off through flashing. The asphaltene rich fluid product was recovered in 50% yield by weight of the pyrolysis fluid resid feed to the first separation tower. This asphaltene-rich fluid product contained 111 ppm nickel and 363 ppm vanadium.

A light liquid phase consisting of a resin oil, a lighter oil component and a pentane solvent is discharged from the top of the first separation column and introduced into a second separation column operated at an internal temperature of 200 ° C. and an internal pressure of 47.5 kg / cm 2 (46 atm). It became. In the second separation column, the hard liquid phase is separated into the second heavy fluid phase of the resin component oil, which is discharged from the bottom of the second separation column and recovered in a yield of 10% by weight relative to the weight of the pyrolysis fluid residue raw material introduced into the first distillation column. do.

The second hard liquid phase was taken out from the top of the second separation column and heated, and then introduced into a third separation column operated at an internal temperature of 227 ° C. and an internal pressure of 45.4 kg / cm 2 (44 atm). In the third separation column, the lighter oil component was separated into the solvent. The lighter oil component is discharged from the bottom of the third distillation column while the solvent is discharged from the top and circulated in the mixer for reuse after cooling. The lighter oil components recovered in the third separation column were obtained in a yield of 40% by weight relative to the weight of the pyrolysis fluid residues feed to the first distillation column, with an asphaltene content of 0.1% by weight or less, a nickel content of 42ppm and a vanadium content of 136ppm. .

The combined yield of lighter oil components extracted and separated by pyrolysis light oil recovered directly from the pyrolysis solvent was only 52% by weight. This yield is fundamentally lower than 71.25% of the previous example. The removal rate of the heavy metal present in the fluid residual oil raw material in the starting heat of this comparative example was only 80%, whereas that of the previous example was 98.3%. The amount of pentane solvent used in this comparative example was 0.5% by weight relative to the weight of the pyrolyzer reduced pressure residual oil raw material, whereas that of the previous example was only 0.05%.

While the invention has been described in connection with preferred embodiments thereof, variations or modifications are not intended to depart from the spirit and scope of the invention as defined in the claims.

Claims (9)

A method for treating petroleum heavy oil, consisting of: preheating the petroleum heavy residue containing heavy metal to about 450 ° C to about 550 ° C; Introducing the preheated residue into an adiabatic pyrolysis tank having an upper portion and a lower portion, wherein the preheated residue is introduced into an upper portion of the pyrolysis vessel to flow in a plug-flow state through the pyrolysis vessel toward the lower portion; Pyrolyzing the residue flowing downward in the pyrolysis tank by maintaining the above residue at an elevated temperature of about 390 ° C to about 450 ° C under a pressure of at least 1 atmosphere; At the same time introducing steam into the bottom of the pyrolysis tank, the steam flowing countercurrently to the downstream flowing downwards; Flowing cracked gas and light oil vapor and steam from the top of the pyrolysis tank and fluid residues pyrolyzed from the bottom; Mixing the pyrolyzed fluid residues with the extractant to form a mixture and introducing the mixture into the extraction bath; Maintaining the mixture at elevated temperature and pressure in the extraction bath to separate the mixture into a heavy fluid phase containing heavy metals and a light fluid phase containing resinous oils, light oil components and solvents; The separated heavy fluid phase containing the heavy metal and asphaltene powder and the light phase containing the resin component oil, the light oil component and the solvent are respectively recovered. The process of claim 1 further comprising: introducing a light fluid phase containing a resin oil, a light oil component, and a solvent into a second extraction tank; The hard fluid phase is maintained under elevated temperature and pressure in the second extraction tank so that the hard fluid phase is converted into a second heavy fluid phase containing resin component oil and a second hard fluid phase containing light oil component and solvent. To separate; The separated second heavy fluid phase and the second hard liquid phase are respectively recovered. The method of claim 2, further comprising: introducing a second hard fluid phase containing the light oil component and a solvent into a third extraction tank; Maintaining the second light fluid phase under elevated temperature and pressure in the third extraction tank to separate the second light fluid phase into a fluid light oil component and a solvent phase; The separated fluid light oil phase and the solvent phase are each recovered. 2. The process of claim 1 wherein the residence time of the petroleum heavy oil in the thermal insulation cracking tank is from about 1 hour to about 10 hours. The process of claim 1 wherein about 30 to about 65 weight percent of the component having an atmospheric boiling point above about 550 ° C. in the petroleum heavy oil causing pyrolysis in the adiabatic pyrolysis tank is decomposed into a component having an atmospheric boiling point below about 500 ° C. 5. The process of claim 1 wherein the amount of steam introduced at the bottom of the thermal insulation pyrolysis tank is from about 5 to about 20 weight percent of the preheated residual oil introduced at the top of the thermal insulation pyrolysis tank. The process of claim 1 wherein the pyrolyzed fluid residue is mixed with the extractant in a volume ratio of about 1: 8 to about 1:12. The method of claim 1 wherein the mixture is maintained at an elevated temperature near the critical temperature of the solvent. The method of claim 8, wherein the mixture is maintained at an elevated pressure that is at least near the vapor pressure of the solvent at the temperature at which the mixture is maintained.

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