JPH07286183A - Method for conversion of hydrocarbon bottom oil - Google Patents

Abstract

PURPOSE: To obtain light products of high quality by deasphalting a residual hydrocarbon oil and then, subjecting the deasphalted oil to thermal, cracking to efficiently carry out the conversion of the residual hydrocarbon oil.

CONSTITUTION: The conversion of a residual hydrocarbon oil is carried out by the steps of deasphalting a residual hydrocarbon oil such as a heavy asphaltene-containing hydrocarbon containing not less than 75 (wt.)% hydrocarbons having a boiling point of not lower than 520°C in a deasphalting zone 101 to obtain (i) a deasphalted oil (DAO) at a yield of at least 50%, preferably 60-90%, more preferably 65-85%, based on the total weight of residual hydrocarbon oil and (ii) an asphaltene fraction; and passing part or all of the DAO through a thermal cracking zone 102 to thermally crack it at a temperature of 350-600°C under a pressure of 1-100 bar at an average residence time of 0.5-60 min so that a 520°C+ conversion of at least 60%, preferably 70-90%, based on the total weight of materials having a boiling point of not lower than 520°C present in the DAO before thermal cracking is obtained.

COPYRIGHT: (C)1995,JPO

Description

Detailed Description of the Invention

[0001]

FIELD OF THE INVENTION The present invention relates to a hydrocarbon residue (resi).
The present invention relates to a conversion method of a dual hydrocarbon oil).

[0002]

Pyrolysis is a widely used method for converting hydrocarbon resids to lighter products.
This method typically involves preheating the feedstock to a suitable temperature, pyrolyzing the preheated feedstock, and fractionating the effluent. The effluent is often used to stop the decomposition reaction,
Quench before sorting. Fractionation can be carried out, for example, by atmospheric distillation alone or by a combination of atmospheric distillation and vacuum distillation. One of the undesirable phenomena that occurs during the pyrolysis of bottoms feedstocks at high conversion levels is the formation of insolubles that limit distillate formation. The formation of this insoluble material is mainly due to the heavy asphaltene component and to some extent also due to the large amount of aromatic components present in the feedstock. Insoluble matter is also produced from synthetic asphaltene formed during the condensation reaction that occurs in the thermal decomposition process. In particular, it is known that the formation of insoluble matter occurs under severe decomposition conditions. However, pyrolysis is a relatively simple method that requires relatively little investment and operating costs. Therefore, pyrolysis has become an attractive method from both a manufacturing and economic standpoint. for that reason,
Efforts are constantly being made to further improve the efficiency of pyrolysis. In the past, several methods have been proposed to achieve this goal. For example, NL-A-84000
No. 74 discloses a method for producing a hydrocarbon mixture from residual oil. This method consists of first deasphalting the residual oil and then subjecting the deasphalted oil to a cracking process to finally obtain one or more fractions.
The asphalt bitumen fraction is partially oxidized with oxygen to produce a gas mixture containing carbon monoxide and hydrogen, which gas mixture is then used in catalytic hydrocarbon synthesis to produce synthetic hydrocarbons. These synthetic hydrocarbons are then separated, preferably by atmospheric distillation, and then mixed with at least a portion of the fraction produced in the cracking of the deasphalted oil. The most suitable cracking process for deasphalted oil is a catalytic cracking process. It is described that the light naphtha produced by catalytic cracking has excellent quality. On the other hand, the light naphtha produced by pyrolysis must also be subjected to a further hydrogenation step in order to convert the diene into an olefin in order to obtain the desired quality of the light naphtha. EP-A-0,372,652 has the disadvantage of a method of the type described in NL-A-8400074 because the asphaltene removed from the residual oil in the deasphalting step no longer contributes to the formation of distillates. , The yield of distillate is not optimal.
Therefore, vacuum residual oil (vacuum resin)
The process described in EP-A-0,372,652 for converting heavy hydrocarbon feedstocks such as e) to lighter products is a method of first preheating a heavy feedstock and then a preheated feed. It involves the operation of passing the feedstock through a pyrolysis zone under conditions such that hydrocarbons with a boiling point of 520 ° C. or higher are converted to 35% or more, suitably 70% by weight. The effluent from the cracking zone is then separated into one or more fractions (which should be recovered as products) and a residual oil, and the residual oil is deasphalted to obtain asphalt and deasphalted oil. The deasphalted oil can also be further processed, for example by catalytic cracking, hydrotreating, hydrocracking or thermal cracking to obtain more useful fractions. Basically, this prior art process involves thermal cracking under relatively harsh conditions followed by deasphalting of the residual oil. However, this method also limits the final yield of the fraction due to the asphaltene present in the pyrolysis feedstock due to the formation of insoluble and / or coke materials, despite relatively severe cracking conditions. With the problem. Also, there is still a need to upgrade the deasphalted oil fraction obtained by deasphalting of the pyrolyzed residual oil in a further conversion process in order to achieve conversion to useful distillate products.

Thus, there is still room for improvement in the efficiency of conversion processes involving the pyrolysis of hydrocarbon resids. Therefore, as one of the objects, the present invention provides a method for converting a hydrocarbon residual oil into a light product of high efficiency and high quality in terms of cost and yield. In terms of cost efficiency (cost efficiency), the objective is to use as few devices as possible without affecting the production rate and the quality of the final product. Of course, this method must meet the appropriate safety and environmental requirements. The present invention is a variety of refinery configurations such as pyrolysis refineries, catalytic cracking refineries, hydrocracking refineries,
Alternatively, it is also an object to provide a method that can be appropriately incorporated in an oil refinery in which two or more of these oil refinery forms are combined.

According to the present invention, (a) a hydrocarbon residual oil is deasphalted, and (i)
50% by weight or more of the total weight of hydrocarbon residual oil, preferably 6
Deasphalted oi in a yield of 0 to 90% by weight, more preferably 65 to 85% by weight.
l = DAO), and (ii) obtaining an asphaltene fraction, and (b) passing a part or all of DAO through a pyrolysis zone to remove substances having a boiling point of 520 ° C. or higher existing in DAO before pyrolysis. 60% by weight or more of the total weight, preferably 70-90
Achieving a wt% 520 ° C + conversion. Thus, the process of the present invention basically involves the severe thermal cracking of deasphalted oil obtained in high yield from hydrocarbon resids. As used herein, the expression “520 ° C. + conversion” means the conversion of hydrocarbons present in the pyrolysis feedstock having a boiling point of 520 ° C. or higher. 5
20 ° C + conversion is wt% relative to pyrolysis feedstock or DAO
Is advantageously represented by the formula:

[Equation 1] It will be clear that “520 ° C. +” refers to the amount of hydrocarbons with a boiling point of 520 ° C. and above.

One of the advantages of the process of the present invention is that the deasphalting treatment removes heavy asphaltene from hydrocarbon resids prior to pyrolysis, which significantly reduces the formation of insolubles during pyrolysis. It is in. As a result, the maximum achievable conversion level is determined primarily by the formation of the synthetic asphaltene component formed by the condensation reaction that occurs during pyrolysis, rather than the asphaltene component present in the hydrocarbon residue prior to deasphalting. Will be done. This means that the process of the present invention can achieve higher conversion levels with higher distillate production rates as compared to subjecting the resid to severe pyrolysis without prior deasphalting. Another advantage of the process of the invention is that the quality of the cuts from the pyrolysis zone is very high. That is, these fractions have an excellent H / C ratio and a low content of sulfur- and nitrogen-containing impurities. The impurities present in the hydrocarbon residual oil feedstock are DA
It was found that it was mainly concentrated in the asphalt phase produced by the deasphalting treatment, not in O 2. Therefore, the impurities concentrated in the asphalt phase are DA
Fractions produced by the thermal decomposition of O can no longer be incorporated. Further, the method of the present invention shows great synergistic potential when incorporated into a thermal cracking refinery, a hydrocracking refinery or a catalytic cracking refinery, but when incorporated into an oil refinery combining two or more of the above refinery forms. , May exhibit even higher synergistic potential.
This will be described in detail later for each refinery configuration with reference to FIGS. 2, 3 and 4.

The hydrocarbon bottoms used as feedstock in the process of the present invention can in principle be any bottoms resulting from the fractionation process. Therefore, in each case, the hydrocarbon residual oil has a relatively high asphaltene content. Preferably, the hydrocarbon residual oil contains 3 hydrocarbons having a boiling point of 520 ° C. or higher.
It is a heavy asphaltene-containing hydrocarbon raw material containing 5 wt% or more, preferably 75 wt% or more, more preferably 90 wt% or more. Particularly suitable hydrocarbon feedstocks that meet this requirement are generally short residues.
It is also known as crude oil vacuum residue. Deasphalting the hydrocarbon residue prior to pyrolysis may be carried out by any conventional method, such as physical separation using membranes or adsorption techniques. However, in the present invention, it is preferable to use the well-known solvent deasphalting method.
In this method, hydrocarbon residue to be deasphalted,
It is usually treated countercurrently with an extraction medium consisting of a light hydrocarbon solvent containing paraffinic compounds. Commonly used paraffinic compounds include C _3-8 paraffinic hydrocarbons, suitably C ₃ -C ₅ paraffinic hydrocarbons such as propane, butane, isobutane, pentane, isopentane or two of these. It may be a mixture of two or more. However, in the present invention, it is preferable to use butane, pentane or a mixture thereof as the extraction solvent,
Most preferably, pentane is used. Generally, the extraction depth increases as the number of carbon atoms in the extraction solvent increases. It should be noted here that as the extraction depth increases, the total amount of heavy hydrocarbons extracted with light hydrocarbons from hydrocarbon residual oil also increases, while the asphaltene fraction decreases but heavier Therefore, the viscosity becomes high. Therefore, the extraction depth does not become too large. This is because an extremely heavy asphaltene fraction having an extremely high viscosity, which can be hardly further processed, is obtained.

The solvent deasphalting process may use a rotating disc contactor or plate column for the hydrocarbon residue introduced at the top and the extraction solvent introduced at the bottom. Comprehensive paraffinic solubility behavior present in hydrocarbon resids (overall paraffinic)
The lighter hydrocarbons with solvency behavior dissolve in the extraction solvent and are discharged from the top of the device. Asphaltene components that do not dissolve in the extraction solvent are discharged from the bottom of the device. The conditions under which deasphalting occurs are known to those skilled in the art. Deasphalting treatment is
Ratio of total extraction solvent to hydrocarbon residue 1.5-8 wt / wt,
A pressure of 1 to 50 bar and a temperature of 40 to 230 ° C. are suitable. As mentioned above, for the purposes of the present invention, the deasphalting of hydrocarbon residue is treated with 50% DAO.
It is carried out so as to obtain an extraction depth of not less than wt%, preferably 60 to 90 wt%, more preferably 65 to 85 wt%. The balance of 100% by weight consists of the asphalt fraction. "Extraction depth (extraction depth
h) ”means DAO after deasphalting by solvent extraction
Of the initial hydrocarbon residual oil before deasphalting and is expressed as a percentage by weight relative to the total weight of the initial hydrocarbon residual oil.

The thermal decomposition of DAO in the present invention can be carried out by a general thermal decomposition process. The exact conditions of pyrolysis may vary and one skilled in the art can select the temperature, pressure and residence time to produce the desired conversion. The same conversion can occur at high temperatures and short residence times and at low temperatures and long residence times. As required by the present invention, in order to achieve 520 ° C. + conversion of DAO of 60% by weight or more, the thermal decomposition of the deasphalted oil in the thermal decomposition zone is carried out at a temperature of 350 to 6
00 ° C, pressure 1-100 bar and average residence time 0.5
It is suitable to carry out in about 60 minutes. Residence times relate to low temperature feedstocks, i.e. room temperature cold oil feedstocks.
The effluent from the pyrolysis zone may be quenched prior to separation into one or more cuts and cracked resid. Quenching may be performed, for example, by contacting the effluent with a cooler quenching liquid. Suitable quench liquids include relatively light hydrocarbon oils, such as gasoline, or recirculating low temperature resids obtained from the effluent. After optional quenching, the effluent is suitably separated into one or more fractions and cracked bottoms, for example by atmospheric distillation and / or vacuum distillation. The cracked residual oil is rather viscous due to the presence of heavy asphaltene components, but its viscosity is considerably lower than that of the heavy asphalt phase separated from the hydrocarbon residual oil in the deasphalting step.

The present invention may also partially or fully recycle the cracked resids to the resid feed and / or DAO to maximize plant capacity and optimize distillate production rates. Characterize. The present invention further provides a cracked residual oil,
It is also characterized by blending with the higher viscosity asphalt fraction obtained as a result of deasphalting treatment and subjecting the resulting blend stream to partial oxidation (gasification). The blend ratio is adjusted so that the viscosity of the blend stream meets the viscosity specifications of the gasifier. The production of cracked residual oil that can be used as a diluent for the higher-viscosity asphalt fraction in the gasifier feedstock means that asphalt is produced with a viscosity that exceeds the viscosity specification of the gasifier feedstock during deasphalting treatment. to enable. This means that DAO can be produced in higher yields relative to hydrocarbon resids, thus leading to higher final yields of distillate from the pyrolysis step.
Gasification comprises any well-known oxidation process that consists of partially oxidizing a heavy hydrocarbon feedstock with oxygen in the presence of steam, usually high pressure steam, to obtain a clean gas after gassing. Is suitable. The clean gas can be used as a contaminant-free fuel gas, in a refinery, or at the same time as cogeneration of power and steam.
e.g.), hydrogen production and hydrocarbon synthesis processes.

In FIG. 1, a hydrocarbon residue (106), preferably a short residue, is passed through a deasphalting zone (101) resulting in DAO (107) and asphalt fraction (1).
19) and are generated. This asphalt fraction is also referred to as "pentane-asphalt". The DAO (107) is sent to the thermal decomposition zone (102) and heated to cause a decomposition reaction. The reaction zone (102) may suitably consist of a furnace alone or a combination of a furnace and one or more immersion vessels. When the "cracked DAO" (108) exits the reaction zone (102), it is passed through a cyclone (103), quenched, and cracked residual oil (110) and light fraction (109).
And separated. The light fraction (109) is the atmospheric pressure separator (1
04) in naphtha minus fraction (111), kerosene fraction (112), gas oil fraction (113) and bottom fraction (1)
14) and are separated. The bottom fraction (114) is blended with the cracked bottoms (110) described above and the resulting blended stream is sent to a vacuum distillation unit (105) where the vacuum gas oil fraction (115) and a light flash (flash).
d) Distillate (116) and heavy flash distillate (11)
7) and vacuum flash cracked residual oil (118) are fractionated. Flash distillates (116) and (117)
May be recovered as a product component, or for example further pyrolysis,
It may be converted to a higher grade material by hydrocracking or catalytic cracking followed by optional hydrotreating. As previously mentioned, the cracked resid (118) is partially or wholly hydrocarbon residue feed (10) to maximize utilization of plant capacity and optimize distillate production.
6) and / or may be recycled to DAO (107). These options are shown in dotted lines in FIG.

In FIG. 2, crude oil (211) is passed through an atmospheric distillation unit (201) and one or more fractions (21) including all fractions from naphtha minus to heavy gas oil.
2) and long residue (213)
And separated. The long residual oil (213) is further subjected to (high) vacuum distillation apparatus (202) with vacuum gas oil (214), light flash distillate (215), heavy flash distillate (216) and short residual oil (217). ) And separated. The flash distillates (215) and (216) merge and are sent to the distillate decomposer (207). The short residual oil (217) is deasphalted in the deasphalting zone (203) resulting in DAO (219) and pentane-asphalt (218). DAO (219) then undergoes severe pyrolysis (T) in the TC (pyrolysis) zone (206).
C) and after separation (distillation) a fraction (220) and a bottom product (221) are obtained. The distillate (220) is sent to the distillate decomposer (207) and the bottom product (22)
1) is sent to the vacuum flushing device (208) with the bottom product (222) produced in the distillate decomposer (207). The vacuum flashing device (208) separates into a pyrolysis flash distillate (223) and a vacuum flash cracking residual oil (224). The pyrolysis flash fraction (223) is sent to the distillate decomposition unit (207),
Vacuum flash cracked bottoms (224) is added to pentane-asphalt (218) as a diluent. The resulting blended stream meets the gasifier (204) viscosity specifications. A naphtha minus fraction (225) and a gas oil fraction (226) are also produced in the distillate decomposition unit (207), and these fractions are expensive after hydrodesulfurization in the hydrodesulfurization unit (209). Recovered as automotive gas oil and industrial gas oil component (227). The gasification of the blended stream (218/224) is performed by gasifying the blended stream, oxygen (228) and steam (229).
04), where partial oxidation of the heavy hydrocarbons present in the blend stream occurs to produce a gas mixture (230) predominantly of carbon monoxide and hydrogen. The mixture is then passed through a gas treatment device (20
Substantially purified in 5). The refined gas (231) may be partially or wholly recovered as clean fuel gas at the refinery, or may be used in cogeneration of power and steam, hydrogen production and / or hydrocarbon synthesis processes. Compared to a thermal conversion refinery that pyrolyzes a short residual oil without prior deasphalting treatment, the thermal conversion refinery of Figure 2 produces more distillate and less vacuum flash cracked residual oil. When pentane is used as the extraction solvent and the short residual oil is deasphalted at a high extraction depth, the amount of pentane-asphalt produced is relatively small. The low production of both vacuum flash cracked resid and pentane-asphalt means that less gasification capacity is required when the short resid is directly subjected to severe pyrolysis. This is a favorable advantage from both a refinery profit and investment perspective.

In the catalytic cracking refinery of FIG. 3, crude oil (31
0) is an atmospheric distillation unit (301), which is separated into one or more kinds of fractions (311) including all fractions from naphtha minus to heavy gas oil and long residual oil (312). ,
The long residual oil was further subjected to (high) vacuum distillation apparatus (302) and further vacuum gas oil (313) and light flash distillate (314).
And heavy flash distillate (315) and short residual oil (316)
And separated. The short residual oil (316) is then deasphalted in a deasphalting unit (303) resulting in pentane-asphalt (317) and DAO (31).
8) is obtained and the DAO is sent to the TC zone (306). Pyrolysis reaction occurs in the zone (after separation)
Naphtha Minus (319) and Gas Oil Fraction (320)
And a bottom product (321) is produced. The bottom product (321) is separated by a vacuum flushing device (307) into a pyrolysis flash distillate (322) and a vacuum flash cracking residual oil (323). Pyrolysis flash fraction (3
22) and the light and heavy flash distillates (314) and (315) are passed to a catalytic cracking zone (309) where the top (324), naphtha (325), kerosene (3).
26), light cycle oil and heavy cycle oil / clarified slurry oil (328) are produced. Light cycle oil (3
Both 27) and the gas oil fraction (320) are passed through a hydrodesulfurization unit (308) resulting in an expensive automotive and industrial gas oil component (329). Heavy cycle oil / clarified slurry oil (328), pentane-
The asphalt (317) and vacuum flash cracked bottoms (323) are blended and the resulting blend stream meets the gasifier (304) viscosity specifications. The blended stream, oxygen (330) and steam (331) are passed to a gasifier (304), where the heavy hydrocarbons are partially oxidized and a gas mixture (332) consisting primarily of carbon monoxide and hydrogen. ) Is produced and the gas mixture is then purified in a gas treatment unit (305). Purified gas (33
3) may be partly or wholly recovered as clean fuel gas at the refinery, or may be used for power and steam cogeneration, hydrogen production and / or hydrocarbon synthesis processes. Long residual oil catalytic cracking (long residue fluid)
(catalytic cracker = LRFCC)
Compared with refineries, flash distillate fluid catalytic cracker (flash distillate fluid)
(catalytic cracker = FDFCC)
The refinery (see FIG. 3), which has severe thermal decomposition of DAO, has the advantage of significant cost savings because FDFCC does not require catalyst cooling capacity. Also, unlike the LRFCC refinery, the metals present in the crude oil no longer come into contact with the FCC catalyst at the FDFCC refinery, thus reducing costs for FCC catalyst replacement, spent catalyst disposal or reactivation. Another advantage is the FDFCC
At the refinery lies in the fact that SOx emissions are significantly lower.
This is because the sulfur present in the long residual oil will be contained in the pentane-asphalt after deasphalting. Sulfur removal in this case is carried out in the gasifier gas treatment step after partial oxidation of the gasifier feed mixture.

In the process of the complex hydrocracking refinery shown in FIG. 4, all reference numbers (401) to (403) have the same meaning as the corresponding reference numbers (201) to (233) in FIG. The only difference between the process of FIG. 4 and FIG. 2 is that the flash distillates (415) and (416) are the flash distillates (215) and (216).
The distillate decomposer (40
7) instead of being passed through the hydrocracking zone (43
4). This hydrocracking zone (4
In 34) the flash distillates (415) and (416) are converted to a higher grade material, i.e. cracked and hydrotreated, top (435), naphtha (436),
Converted to kerosene (437), gas oil (438) and hydrowax (439). Hydrowax (439) can be suitably used as a feedstock for integrated chemical plants, for example for producing lower olefins.
Alternatively, the pyrolysis flash distillate (423) may be used partially or fully as a feedstock for the hydrocracking zone (434) instead of passing through the distillate cracking zone (407). Compared to a refinery (FD / DAO HCU) in which a feedstock consisting of a mixture of flash distillate and DAO is passed through a hydrocracker (HCU), the flash distillate of FIG. Hydrocracking refineries (FD / HCU + DAO / TC refineries) require less fluid pressure capacity for expensive high pressure HCU, and lower coal feed rates (combin) due to the lack of DAO feedstock.
It has the advantage that it can be operated in ed fed ratio). As a result, the reactor volume can be smaller,
Therefore, investment and operating costs are saved. Also, DAO
Metal contaminants and high Conradson carbon residues present in the feedstock (high Conradson Carbon)
Residue) Expensive high pressure guard beds needed to protect hydrocrackers from materials
d) No reactor is required. FD / HCU + DAO / in Figure 4
Another important advantage of TC refineries is that due to DAO upgrades through harsh pyrolysis, the optimal DAO yield for short resids is primarily due to meeting maximum viscosity specifications for gasifier feedstocks. Of pentane-asphalt with a vacuum flash cracked bottoms blend operation. This optimal DAO yield is greater than the optimal DAO yield for short resids for FD / D HCU. The latter is determined by the Maximum Guard Bed Reactor Conradson Carbon Residue Specification. Therefore, HCU including severe thermal decomposition of DAO
DAs that can be upgraded to expensive distillates at refineries
More O is obtained, resulting in less asphalt production and less capacity required in the gasifier, thus saving investment and operating costs.

[0014]

EXAMPLES The present invention will be described in more detail with reference to the following examples. Example 1 Using pentane as an extraction solvent, Arabian Heavy Short Resi (Arabian Heavy Short Resi)
(due = AHSR) is deasphalted, and AHSR
70% by weight of DAO (AHSR C5-DAO) was obtained. Extraction is based on a total solvent / feedstock ratio of 2.0 (wt / w
t), feedstock predilution 0.5 (wt / wt), temperature 193 ° C. and pressure 40 bar. AHSR C
5-DAO is then pressure 5.0 bar, out (out)
let) temperature 470 ° C., 480 ° C., 490 ° C. and 500
Subjected to severe pyrolysis at ° C. Comparative Example 1 The same AHSR used in Example 1 was used at a pressure of 5.0.
Subjected to pyrolysis at bar. Outlet temperature is 460 ° C, 465
C, 470 C and 461 C. AHSR C5-
Analytical data for DAO and AHSR are shown in Table I.
The abbreviations used are as follows: "% w" stands for wt% and "CSt" stands for centistoke. The results of pyrolysis of AHSR C5-DAO and AHSR at various outlet temperatures are shown in Tables II and III, respectively.

[0015]

[Table 1]

[0016]

[Table 2]

[0017]

[Table 3]

At insoluble matter contents above about 0.5% by weight,
It was found that the pyrolysis pilot plant malfunctions due to the deposition of insoluble matter. Therefore, it was impossible to further decompose at higher conversion levels. on the other hand,
Using the DAO-TC route of Example 1, 500 ° C
At the outlet temperature as well, it has an insoluble matter content of only 0.03% by weight, so there is still the possibility of further decomposition at higher conversion levels without impairing the functioning of the pilot plant due to insoluble matter accumulation 350 ° C + Residual oil was obtained. Also, as is clear from a comparison of the 520 ° C. + conversion level with the AHSR feedstocks shown in Tables II and III,
The process of the invention described in Example 1 allows a higher degree of conversion and thus a higher distillate yield, without the malfunction of the pyrolysis unit due to the insoluble matter formed.

[Brief description of drawings]

1 is an illustration of typical steps of the method of the present invention.

FIG. 2 is an explanatory diagram of a process of a pyrolysis refinery.

FIG. 3 is an explanatory diagram of a process of a catalytic cracking refinery.

FIG. 4 is an explanatory diagram of steps in a hydrocracking refinery.

[Explanation of symbols]

 101 Deasphalting zone 102 Pyrolysis zone 103 Cyclone 104 Normal pressure fractionator 105 Vacuum distillation apparatus

Claims (13)

[Claims] 1. A method of deasphalting a hydrocarbon residue (a) to obtain 50% by weight or more, preferably 60 to 90% by weight, more preferably 65% by weight of the total weight of (i) the hydrocarbon residue.
Deasphalted oil (DAO) in a yield of ~ 85% by weight,
(Ii) obtaining an asphaltene fraction, and (b) passing a part or all of DAO through a pyrolysis zone to obtain 60 wt% of the total weight of substances having a boiling point of 520 ° C. or higher present in DAO before pyrolysis. Or more, preferably 70 to 90
Achieving a weight percent 520 ° C. + conversion of a hydrocarbon residue. 2. The method according to claim 1, wherein the hydrocarbon residual oil is a heavy asphaltene-containing hydrocarbon raw material containing 75% by weight or more of a hydrocarbon having a boiling point of 520 ° C. or higher. 3. The method according to claim 2, wherein the heavy asphaltene-containing hydrocarbon feedstock is a vacuum residual oil of crude oil. 4. The method according to claim 1, wherein the deasphalting treatment is carried out by solvent extraction using butane, pentane or a mixture thereof as an extraction solvent. 5. The method according to claim 4, wherein pentane is used as the extraction solvent. 6. The method according to claim 1, wherein the deasphalting treatment is carried out at a ratio of total extraction solvent to hydrocarbon residual oil of 1.5 to 8 wt / wt, a pressure of 1 to 50 bar, and a temperature of 160 to 230 ° C. The method described in paragraph 1. 7. The pyrolysis of DAO in the pyrolysis zone is carried out at a temperature of 350 to 600 ° C., a pressure of 1 to 100 bar and an average residence time of 0.5 to 60 minutes. The method described in. 8. The cracked residual oil finally obtained from the thermal cracking zone is partially or wholly recycled to a hydrocarbon residual oil feedstock for deasphalting treatment and / or DAO. The method according to paragraph 1. 9. A blend of at least a portion of the cracked resid finally obtained from the thermal cracking zone and the asphaltene fraction obtained by deasphalting, and then subjecting the resulting blend stream to gasification. Item 9. The method according to any one of items 1 to 8. 10. A heat conversion refinery incorporating the method of any one of claims 1-9. 11. A catalytic cracking refinery incorporating the method of any one of claims 1-9. 12. A hydrocracking refinery incorporating the method of any one of claims 1-9. 13. A refinery comprising a combination of two or more refinery configurations according to claims 10-12.