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    • 专利摘要:
    Distillates are produced from asphaltenes-containing hydrocarbon mixtures by a process comprising subjecting the hydrocarbon mixtures (101) to a catalytic hydrotreatment (106), and subjecting the distillation residue (102) of the hydroconverted product to a combination of solvent deasphalting (107) thermal cracking (108).
    公开号:SU1306479A3
    申请号:SU823520472
    申请日:1982-12-08
    公开日:1987-04-23
    发明作者:Хендрик Ван Донген Роберт；Роберт Ньюсам Джон
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to a method for producing hydrocarbon oil distillates from asphaltene-containing hydrocarbon mixtures and can be used in the petroleum refining industry.
    The aim of the invention is to increase the yield of distillate fractions and reduce gas formation.
    Figures 1-5 are flow diagrams illustrating the proposed method.
    The process is carried out in the scheme (Fig. I), which includes the Hydrotreating Zone (GO), the Deasphalting Zone 2 (YES) and the Thermal Cracking Zone (TK) in series, the Asfelten-containing hydrocarbon oil supplied through line 4 is subjected to
    GO, the product of which is divided into one or more distillate 5 fractions and residue 6, is subjected to flow 6, Stream 6 is subjected to YES, the product of which is separated into deasphalted oil 7 and asphalt bitumen 8, Stream 7 is subjected to TC, and the cracked product is divided into ONE or more distillate fractions 9 and a residue fraction 10,
    The process can be carried out according to the scheme (FIG. 2), including zone 1 GO, zone 3 TC and zone 2 YES, Asphaltene-containing hydrocarbon mixture 4 is subjected to GO, the product of which is divided into one or more distillate fractions 5 and residue fraction 6, Stream 6 expose to deasphalted oil 28 and asphalt bitumen 29 with solvent. The deasphalted oil 28 is mixed with atmospheric residue 30, and mixture 31 is subjected to thermal
    20 kings. Asphalt bitumen 29 is divided into two parts 32 and 33. The stream 33 is mixed with vacuum residue 34 to form a recycle stream 19, the product of thermal cracking 35 times
     atmospheric distillation is carried out on the gas fraction 36, atmospheric distillate 37 and atmospheric residue 38, which is divided into two parts 30 and 39, which is divided by vacuum distillation into 30 vacuum distillate 40 and vacuum residue 34,
    According to the flow chart of FIG. 4, the process is carried out in the sequence of the TC, and the cracked product is spatially including the GO zone, consisting of
    from a catalytic hydrotreating unit 11, a unit 12 for atmospheric distillation and a unit 13 for vacuum distillation II zone 14 DA and a TK zone consisting of block 15 for thermal cracking, a second block 16 for atmospheric distillation, a second block 41 for thermal cracking 41, the third unit 42 for atmospheric 45 distillation and the second unit 17 for vacuum distillation 17, the Asphaltene-containing hydrocarbon mixture 43 is mixed with vacuum residue 44 and the mixture 45 is subjected together with hydrogen 46 to catalytic hydrotreating, the resulting product 47 atm by atmospheric distillation is divided into gas fraction 48, atmospheric distillate 49 and atmospheric residue 50, This atmosphere
    divided into one or more distillate 9 fractions and residue 10 fraction; Stream 10 is subjected to YES, the product of which is separated into deasphalted oil 7 and asphalt bitumen 8; stream 7 is used as a component of the starting material for TC,
    Figures 3-5 show three detailed flow diagrams for the production of hydrocarbon oil distillates from asphaltene-containing hydrocarbon mixtures according to the proposed method.
    In accordance with the flow chart of FIG. 3, the process is carried out in series with a GO zone consisting of a unit 11 for catalytic hydroprocessing, a unit 12 for atmospheric distillation and a unit 13 for a wafer residue 50 vacuum distillation distillation 13, a zone 14 with the DATE section put on vacuum distillate
    and a TC zone consisting of a block 15 ter-51 and a vacuum residue 52, Vacuum
    mechanical cracking, second block 16 residual 52 by deasphalting
    for atmospheric distillation and second solvent are divided into deasphal 306479 2
    unit 17 for vacuum distillations, the Asphaltene-containing hydrocarbon mixture 18 is mixed with the recycle stream 19, and this mixture 20
    5 together with hydrogen 21 is subjected to catalytic hydrotreatment I Hydro treatment product 22 by atmospheric distillation is divided into gas fraction 23, atmospheric distillate 24 and atmospheric residue 25, This atmospheric residue 25 is separated by vacuum distillation into vacuum distillate 26 and vacuum residue 27. The latter is separated by deasphalting.
    15 with solvent for the deasphalted oil 28 and asphalt bitumen 29. The deasphalted oil 28 is mixed with the atmospheric residue 30, and the mixture 31 is subjected to thermal cracking. Asphalt bitumen 29 is divided into two parts 32 and 33, Stream 33 is mixed with vacuum residue 34 to form a recycle stream 19. Thermal cracking product is divided 35 times by atmospheric distillation into gas fraction 36, atmospheric distillate 37 and atmospheric residue 38 which is divided into two parts 30 and 39, which is vacuum distilled to divide 30 into a vacuum distillate 40 and a vacuum residue 34,
    According to the technological scheme according to FIG. 4, the process is carried out sequentially including the area of HE consisting of
    40
    from catalytic hydroprocessing unit 11, unit 12 for atmospheric distillation and unit 13 for vacuum distillation II zone 14 YES and TK zone consisting of unit 15 for thermal cracking, second unit 16 for atmospheric distillation, second unit 41 for thermal cracking 41 , the third unit 42 for atmospheric 45 distillation and the second unit 17 for vacuum distillation 17, the Asphaltene-containing hydrocarbon mixture 43 is mixed with vacuum residue 44 and the mixture 45 is subjected together with hydrogen 46 to catalytic hydrotreating, the resulting product 47 atm by spherical distillation, the gas fraction 48, the atmospheric distillate 49, and the atmospheric residue 50, This atmosphere
    Tizirovanny oil 53 and asphalt bitumen 54, Deasphalted oil 53 is mixed with atmospheric residue 55, and the mixture 56 is converted in the second thermal cracking unit into product 57, which is separated by atmospheric distillation into gas fraction 58, atmospheric distillate 59 and atmospheric the remainder 60, which is divided into two parts 55 and 61, is turned into asphalt bitumen 54 in the first thermal cracking unit into a product
    62, which is atmospheric distilled divided by atmospheric distillate
    63, gas fraction 64 and atmospheric residue 65, Gas fractions 58 and 64 are mixed to form a mixture 66. Atmospheric distillates 59 and 63 are mixed to form a mixture 67, Atmospheric residues 61 and 65 are mixed to form 68, which is separated by vacuum distillation into vacuum distillate 69 and vacuum residue 70, vacuum residue 70 divided
    into two parts 44 and 71, I
    In accordance with the flow chart of FIG. 5, the process is carried out sequentially including an FO zone consisting of a catalytic hydrotreatment unit 11, an atmospheric distillation unit 12 and a vacuum distillation unit 13, a TC zone consisting of a thermal cracking unit 15, a second atmospheric distillate unit 16 the second thermal cracking unit 41, the third atmospheric distillation unit 42 and the second vacuum distillation unit 17, and zone 14 YES, the Asphaltene-containing hydrocarbon mixture 72 is mixed with asphalt bitumen 73, and the mixture 74 is mixed with Ode 75 is subjected to catalytic hydrotreatment. The resulting product 76 is separated by atmospheric distillation into a gas fraction 77, atmospheric distillate 78 and atmospheric residue 79, Atmospheric residue 79 is vacuum distilled and divided into vacuum distillate 80 and vacuum residue 81, Vacuum residue 81 is thermally cracked and converted into product 82, which is separated by atmospheric distillation into a gas fraction 83, atmospheric distillate 84 and atmospheric residue 85, Atmospheric residue 85 is mixed with atmospheric residue 86, and this mixture 87 by vacuum distillation is divided into vacuum M0
    five
    0
    five
    0
    five
    The distillate and vacuum residue 89 are removed, the vacuum residue 89 is deactivated by solvent and the asphalt bitumen 91. The deasphalted oil 90 is mixed with atmospheric residue 92 and the mixture 93 is thermally cracked to form product 94, which is separated by atmospheric distillation into a gas fraction 95, atmospheric distillate 96 and atmospheric residue 97, Atmospheric residue 47 is divided into two parts 86 and 92, Gas fraction 83
    15 is mixed with gas fraction 95 to form mixture 98. Atmospheric distillates 84 and 96 are mixed to form mixture 99. Asphalt bitumen is divided into two parts 73 and 00,
    0
    Example 1. In the experiment according to
    The technological scheme (Fig. 3) uses an asphalt-containing hydrocarbon-5 mixture obtained as a residue by vacuum distillation of the atmospheric residue of crude Middle Eastern oil as a starting material. The boiling point of the vacuum residue is 520 ° C, the carbon content in it according to Remsbottom is 18.8 wt,% The initial mixture is subjected to hydrotreatment, KOTOP TO is carried out in two reactors, the first of which is filled with a Ni / V / SiO catalyst containing 0.5 May, h nickel and 2.0 May, h, vanadium at 100 May, h, silica, and the second of which is filled with a CoMoAl-O catalyst, containing 4 May, h. Kobapta and May 12, h. molybdenum at 100 May, h, alkyne oxide. Hydrotreating is carried out at a hydrogen pressure of 150 bar, the flow rate measured for both reactors, 0.5, (the ratio between hydrogen and raw materials is 1000 nl / kg) and at an average temperature of 41 0 ° C in the first reactor and 385 ° C in the second reactor. Subsequent deasphaltization is carried out at and at a pressure of 40 bar using n-butane as the solvent. The mass ratio between solvent and oil is 3: 1. Thermal cracking is carried out in a cracking coil at 480 ° C, a pressure of 20 bar and a flow rate of 0.4 kg of fresh feed per 1 liter of the cracking coil volume in 1 minute. The extent of recycling to the cracking coil (mass parts of
    tatka on bulk parts of fresh
    cf) equals 2.
    I
    100 May, h, a vacuum residue with a boiling point higher than 520 C, carbon content according to the Rambotosh 1808 wt.% Is mixed with 30.3 May, h, said circulation flow to obtain 130.3 May, h. mixtures with a carbon content according to Remsbottom 23.8 mas.%; The mixture is subjected to hydrotreatment under the indicated conditions and the resulting product (fraction Cg-, which contains carbon according to Pmbotto: 10.4 wt.%) Is separated by means of atmospheric distillation 15 to a gaseous fraction, 17.1 wt.h, Cj- () of atmospheric distillate and 106.0 May, h, of atmospheric residue. The atmospheric residue is separated by vacuum 20 distillation at 31.7 May, h. vacuum distillate with a boiling point of 350-520 ° C and 74.3 May, h, vacuum residue. The vacuum residue is subjected to a deaephalization with a solvent with the use of an organic substance, yielding 53.5 May, h, asphalt-freezing and 20.8 parts by weight of asphalt bitumen,
    The obtained deafaltisate (53.5 May, h,) is mixed with a part of the residual gas obtained from the subsequent thermal cracking during the operation. The thermally cracked product is then subjected to atmospheric distillation to obtain a gaseous fraction,
    20.0 May, h, C - 350 ° C of atmospheric Diethyl and Atmoofer Oetat,
    30.1 May, h. obtained atmoofer
    Comparing the total yield achieved in the case when the raw material is subjected to joint thermal cracking and hydrowashing, which provide about 50 May, h, 100 May, h of the starting material,
    The results of the experiment are summarized in Table 1. Table 1
    N ote, At 100 mph, feedstock (18) 100.0,
    Carbon content according to Remsbotto in the feedstock prior to treatment (stream 20) 23.8 May,%, 35 Stream 20 etoeite from 100 May, h, vacuum 18, 14.8 mAh, recirculated bitumen33; 15.5 wt.h. second vacuum chamber 34,
    The stream 31 consists of 28-43,5 м.ч. the residue is subjected to vacuum distilled 0 deasphalted oil 28 and ltion to obtain 14.6 May, h, vacuum, h ,; recycled diethyl
    It is 30 from distillation under atmospheric pressure, yielding 3.4 May, h, 350 ° (45–20.0 May, h, and the resultant of the distillation
    a smart distillate with a boiling point of 350-520 0 and 15.5 May, h, vacuum Residue (boiling at a temperature above 520 ° С), the resulting vacuum residue is returned to the hydrochloric etadiu, together with 14.8 wt.h, asphalt bitumen obtained at the stage of deasphalting by a solvent.
    C. - 36-37 at atmospheric pressure, 38 May 33.5, hours, of which 3.4 parts by weight, are recycled, and May 30.1, hours, subjected to atmospheric pressure, 38 May 33.5, hours, from which 3.4 parts by weight are recycled, and on May 30.1, hours, subjecting May 6, hours, the aphaltic bitumen is removed, 50 are vacuum distilled through stream 39.
    The total yield of the obtained atmospheric and vacuum distillates (together with separate mass portions of the streams 24, 26 and 40) is 83.4 May, h. at 100 May, h, a vacuum boiling point over 520 ° C, used as a starting material, which is a significant improvement, according to
    Comparing the total yield achieved in the case when the raw material is subjected to joint thermal cracking and hydrowashing, which provide about 50 May, h, 100 May, h of the starting material,
    The results of the experiment are summarized in Table 1. Table 1
    ZO
    N ote, At 100 mph, feedstock (18) 100.0,
    Carbon content according to Remsbotto in the feedstock prior to treatment (stream 20) 23.8 May,%, 35 Stream 20 etoeite from 100 May, h, vacuum 18, 14.8 mAh, recirculated bitumen33; 15.5 wt.h. second vacuum chamber 34,
    atmospheric receive-distillation
    C. - 36-37 at atmospheric pressure, 38 May 33.5, hours, of which 3.4 parts by weight are recycled, and May 30.1, hours, is subjected to vacuum distillation through stream 39
    55
    The combined yield of distillates obtained by distillation in vacuum and at atmospheric pressure, 83, wt.%,
    Example 2, According to the technological circuit (Fig, 4), the experiment was carried out using the same oil residue described in Example 1, but
    7 1306479 8
    characterized by a carbon content above 520 ° C, 21.2 May, h. obtained according to Remsbottom 14.5 wt.%. The residual vacuum residue is subjected to the same oil being treated as a circulation treatment, as in Example 1, however, the hydrotreating fluid stream and the rest of the cracking is carried out in two creams. yut. Obtained in a raking coil, and in the first of
    In this process, asphalt bitumen is subjected to thermal cracking with subsequent atmospheric distillation with the product thus obtained. The total amount of atmospheric distillates obtained after two stages of thermal cracking is 20.2 parts by weight.
    Total distillates (table 2
    they are maintained at a temperature of 460 ° C, and in the second 490 ° C.
    100 ma.ch. a vacuum residue boiling at a temperature above 520 C, with a carbon content of 14.5% by weight of carbon and a mixture of nitrogen and 21.2 May, h. circulation flow, to obtain 121.2, May, h. the mixture, the carbon content of Ramoubutoma — in which sotavl is 15 mospheric and vacuum), is 19.5% by weight. The mixture is subjected to hydraulics at 100. May, h, of the initial materi- al at the indicated areas X | a la, is 81.6 May, h. (taking into account the obtained product Sfraction C - which are 49, 67, 51 and 69 streams), which is characterized by the content of coal. The results of the experiment are given in a Lerod according to Rsbottom, 9.1 wt.%) Table-2 times, 20, is divided. by atmospheric distillation to a gaseous stream: 18.7 mAh, atmospheric distillate 350 ° C and 96.0 mAh, atmospheric residue. The atmospheric residue is subjected to vacuum distillation and 28.1 May, h, vacuum diethyl with a boiling point of 350-520 C and 67.9 May, h, vacuum diethil with a boiling point above 520 C are obtained. subjected to solvent deasphalting using the specified conditions to obtain 46.2 mue.ch4 of deaafaltisate and 21.7 May, h. asphalt bitumen, 35 I
    The asphalt-free oil is mixed with an e-indicated: atmospheric residue and the mixture is subjected to a second thermal cracking. The product of secondary thermal cracking (carried out at 490 ° C) is separated by atmospheric distillation into a gaseous fraction, atmospheric distillate and atmospheric residue. Part of the atmospheric residue is used together with asphalt-free oil as a raw material for secondary thermal cracking, and the rest is subjected vacuum distillation together with the atmospheric residue obtained after the atmospheric distillation of the product obtained as a result of thermal cracking at 460 ° C asphalt bitumen specified above. From the combined atmospheric residues, 14.6 May, h, vacuum distillate with a boiling point of 350-520 C are obtained, together with e 29.7 May, h, a vacuum residue with a boiling point of 40
    Note, At 100 May, h, 45 feedstock (40) 100.0.
    The content of carbon according to Ramotembto in the raw materials before the first treatment (stream 45) is 19.5 wt.%.
    The combined outputs of dietiltov, jjg obtained by distillation in vacuum and at atmospheric pressure, 81.6 wt.%
    EXAMPLE 3 The experiment was carried out according to the technological stage (Fig. 5) e j using the starting material described in Example 1, but with a carbon content according to Ramebottom of 17.1 wt.%. This material is processed under the conditions specified in
    In this process, asphalt bitumen is subjected to thermal cracking followed by atmospheric distillation with the product thus obtained. The total amount of atmospheric distillates obtained after two stages of thermal cracking is 20.2 parts by weight.
    The total amount of distillates (atmospheric and vacuum) obtained at 100. May, h, of the starting material, is 81.6 May, h. (taking into account the individual flows 49, 67, 51, and 69), The results of the experiment are presented in Table 2,
    table 2
    ), received a similar material - May, h. (including 9, 67, 51 and 69), are presented in
    40
    Note, At 100 May, h, 45 feedstock (40) 100.0.
    The content of carbon according to Ramotembto in the raw materials before the first treatment (stream 45) is 19.5 wt.%.
    The combined outputs of dietiltov, jjg obtained by distillation in vacuum and at atmospheric pressure, 81.6 wt.%
    EXAMPLE 3 The experiment was carried out according to the technological stage (Fig. 5) e j using the starting material described in Example 1, but with a carbon content according to Ramebottom of 17.1 wt.%. This material is processed under the conditions specified in
    Example 2, except for togo | that solvent deasphalting is carried out as the final stage when using a 2: 1 mass ratio between solvent and petroleum product and at cracking temperatures of 490 and 100 mas, respectively. a vacuum residue with a boiling point above 520 ° C and a Remsbottom carbon content of 17.1% by weight of the blended JO is partially mixed with the resulting separation from 25.3 wt.h. circulation flow to obtain 125.3 May, h mixtures with a carbon content according to Remsbottom, 21.8 wt.%, the mixture is subjected to hydrotreatment under the indicated conditions, and the resulting product (fraction C -, which is characterized by a carbon content of 9.8 wt.%) is separated by atmospheric distillation into a gaseous stream, 18.9 mAh of atmospheric distillate C - 350 ° C and 99.8 mAh of atmospheric residue with a boiling point higher. The atmospheric residue is subjected to vacuum distillation and 28.4 wt. Parts are obtained. vacuum distillate with boil. 350-520 ° C and 71.4 ma.ch. vacuum residue with a temperature of interest above 520 ° C. The vacuum residue is subjected to thermal cracking in the first cracking coil with and the resulting product is separated by atmospheric distillation into a gaseous fraction, atmospheric distillate 350 ° C and atmospheric residue.
    Cs
    The obtained atmospheric residue is mixed with the atmospheric residue obtained by distilling the product obtained at the secondary stage of thermal cracking and this mixture is subjected to vacuum distillation to obtain 14 | 7 May, h. vacuum distillate with m, kip. 350-520 ° C and 60.5 mAh, vacuum residue with a boiling point above 520 ° C. The vacuum residue thus obtained is subjected to solvent deasphalting using the indicated conditions in order to obtain 25.3 May, h. deasphal tizate and 35.3 May, h, asphalt bitumen. Asphalt bitumen is divided into two parts: 21.2 May, which serves as a circulating stream for hydrotreating and the rest is removed. The resulting deasphthalic acid is mixed with a portion of the atmospheric residue remaining after atmospheric distillation of the product obtained during the secondary thermal cracking, and the mixture obtained by TaKitM is subjected to secondary thermal cracking at 500 ° C. The resulting product is separated by atmospheric distillation into a gaseous fraction, atmospheric distillate C - 350 ° C and an atmospheric residue with a boiling point above 350 ° C, which
    falsetis and partly with the atmospheric residue remaining after the atmospheric distillation of the product obtained by the first thermal
    cracking at a temperature of 490 C. The total amount of atmospheric distillates obtained after two stages of thermal cracking is 18.7 wt.h.
    I The total number of distillates (atmospheric and vacuum) K) obtained at 100 May, h, of the starting material, 80.7 wt.h. (including individual streams 78 and 99, 80 and 88), Results
    experience presented in table 3.
    Table3
    Note. At 100 mach., I raw materials (72) 100.2,
    May 25.3, h the product obtained (91) () is recycled (73) to be mixed with the raw material (72) fed to the catalytic hydrotreatment, 25.2 mash, deasphalon 130647912
    The recovered oil products are recycled (90), fed to the second heat treatment. The third atmospheric distillation residue (97) is separated and sent to the second heat treatment (stream 92) and the second vacuum treatment unit (stream 86) is recycled. distillation, Example 4. The experiment was carried out according to the technological scheme (FIG. 3) - 10 using a mixture of hydrocarbons containing asphaltenes as the starting material, and the crude residue obtained as a residue after distillation in a vacuum. cum distillate Having t, heated. oil from the Middle East, Osta- 350-520 ° C, and 86.0 ma.h, vacuum
    ma.ch. the recycle stream obtained according to the described method, resulting in 129 wt.h. mixtures with an RCT of 26.3 wt.%; The mixture was subjected to hydrotreating under the indicated conditions and a product (fraction of RCT of which is equal to 14.1 wt.%) was separated by distillation at atmospheric pressure, resulting in
    this is 14.2 May, h. fractions boiling at 350 ° C in the form of a distillate and 113 parts of mash, residue.
    The residue was separated by vacuum distillation at 27.0 parts by weight. A cotton wool has a temperature in vacuum of more than 520 C, its carbon content according to Remsbottom is 22.4 wt.%.
    The initial product is subjected to catalytic hydroprocessing, which is carried out in two reactors, the first of which is filled with a catalyst based on Ni / Mo / SiO containing 3 parts by weight. nickel and May 9, h. molybdenum at 100 mach. h, silicon dioxides, and the second is filled with a catalyst on CO / MO / AI О, containing 4 ma.ch, cobalt and 12 May, h. molybdenum on
    oetatka. Vacuum residue is subjected to deasphalting in a solvent using the specified conditions, 20 to obtain 66.7 May, h. deasphalting agent
    and 19.3 ma.ch, aphaltic bitumen. one
    Received. deasphalted oil
    (66.7 May, part) are mixed with a part of the oatcat obtained by distillation at atmospheric pressure at the next thermal cracking stage, nocjie of which the mixture is subjected to thermal cracking under the specified conditions. Product ter100 May, h, aluminum dioxides. Catalya-30 bokrakking is then subjected to distillation of such hydroprocessing ashe-P at atmospheric pressure, obtaining
    gaseous fraction, 23.2 wt. distillate C - 350 ° C and the residue. 38.5 mach., The residue obtained as a result of distillation at atmospheric pressure (having a boil point, 350 ° C) is subjected to vacuum distillation to obtain a 17.3 mash. Vacuum distillate with a boil pump, 350-520 C and 21.2 mach., Vacuum residue (having a boiling point higher); The resulting vacuum distillation residue is recycled to the catalytic hydroprocessing stage together
    at a pressure of 175 bar of hydrogen, a volumetric ekoreti measured for both reactors, 1.5 and at a ratio of hydrogen to an initial product of 2000 n / l per 1 kg; average temperature of 425 ° C in the first reactor and in the second reactor.
    Subsequent deafiltration is carried out at 190 ° C and a pressure of 70 bar using n-pentane as a solvent. The mass ratio of the amounts of solvent and oil 3: 1.
    The final thermal cracking treatment was carried out in a reaction cracking coil at 480 ° C, a pressure of 30 bar and a space velocity of 0.1 kg of fresh starting reaction coil for cracking in 1 minute. The ratio of product to 1 liter of the recycling volume in the coil is 2 (the ratio of the weight of the Maes parts to
    about
    to the number of parts by weight of the fresh starting product).
    100 ma.ch. A vacuum distillation pot with t, bale, 520 ° C and above, having a RCT of 22.4 wt.%, is mixed with 29.0
    kumny distillate having t, kip. 350-520 ° C, and 86.0 mach. H, vacuum
    ma.ch. the recycle stream obtained according to the described method, resulting in 129 wt.h. mixtures with an RCT of 26.3 wt.%; The mixture was subjected to hydrotreating under the indicated conditions and a product (fraction of RCT of which is equal to 14.1 wt.%) was separated by distillation at atmospheric pressure, resulting in
    kumny distillate having t, kip. 350-520 ° C, and 86.0 mach. H, vacuum
    this is 14.2 May, h. fractions boiling at 350 ° C in the form of a distillate and 113 parts of mash, residue.
    The residue was separated by vacuum distillation at 27.0 parts by weight. wooetatka The vacuum residue is subjected to deasphalting in a solvent using the indicated conditions, obtaining 66.7 May, h. deasphalting agent
    and 19.3 ma.ch, aphaltic bitumen.
    Received. deasphalted oil
    (66.7 May, part) are mixed with a part of the oatat obtained by distillation under atmospheric pressure at the next thermal cracking stage, nocjie of which the mixture is subjected to thermal cracking under the specified conditions. The thermal cracking product is then distilled with P at atmospheric pressure to obtain
    gaseous fraction, 23.2 wt. distillate C - 350 ° C and the residue. 38.5 mach., The residue obtained as a result of distillation at atmospheric pressure (having a boil point, 350 ° C) is subjected to vacuum distillation to obtain a 17.3 mash. Vacuum distillate with a boil pump, 350-520 C and 21.2 mach., Vacuum residue (having a boiling point higher); The resulting vacuum distillation residue is recycled to the catalytic hydroprocessing stage together
    from 11.5 May, h asphalt bitumen obtained at the stage of deafaltisation in a solvent, 7.8 wt.h. the aphaltic bitumen is removed. The combined yield of the dillets produced by vacuum distillation and distillation under atmospheric pressure (obtained by summing in May parts of streams 24, 26, 37 and 40) is 81.7 May, h . on
    100 ma.Ch. vacuum residue e
    f
    jr.KIP. and above used as a starting product.
    The results of the experiment are presented in table 4.
    13h
    Table 4
    Note, On 100 ma.ch. feedstock (18) 100.0.
    EXAMPLE 5 The experiment was carried out according to the technological scheme (Fig. 4) using the same starting materials as in Example 4, i.e. a vacuum distillate having a boiling point above 520 ° C and an RCT of 14.5% by weight.
    The initial product is subjected to catalytic hydroprocessing carried out in two chambers, the first of which is filled with a catalyst based on Ni / Mo / SiO containing 3 wt.h. nickel and 9 ma.ch. molybdenum at 100 May, h, silica, and the second is filled with a catalyst based on Co / Mo / A Od, containing D au.h, cobalt and 12 au.h. molybdenum per 100 mach. aluminum.
    The catalytic hydroprocessing was carried out at a hydrogen pressure of 75 bar and a space velocity measured for both reactors, 0.2 hours, the ratio of hydrogen to starting product was 1500 nl per kg, and the average temperature was 400 ° C in the first reactor and 375 ° C in the second reactor ,
     Subsequent deasphorization is carried out at 40 bar and pressure using n-butane as the solvent. The mass ratio of the amounts of solvent and oil is .3: 1 /
    15
    20
    25
    0647914
    Thermal cracking is also carried out on two reaction coils: the first coil operates at 460 ° C, a pressure of 20 bar and a space velocity
    5 0.4 kg of fresh raw material per I liter of the reaction coil for cracking in I min, and a second coil at a pressure of 10 bar and a space velocity of 2 kg of fresh feed per liter of the reaction coil for cracking in 1 min. The recirculation ratio in the respective cracking reaction coils (i.e., the number of parts by mass of the residue per number of parts by mass of the fresh starting product) is 2.
    100 ma.ch. a vacuum residue with a boiling point higher than that of an RCT value of 14.5% by weight is mixed with 22.3 parts by weight. said recycle stream, resulting in 122.3 wt.h. a mixture having a RCT value of 20.1 wt.%. The mixture is subjected to catalytic hydroprocessing under the indicated conditions and the product formed is separated (fraction C--, having a RCT value of 9.4 May.%) By distillation, to obtain
     22.4 mach.h fractions C, - 350 C, and 98.0 mach.ch. oetatka. The carbon dioxide formed by distillation under atmospheric pressure is subjected to vacuum distillation, yielding 31.8
    35 ma.ch. vacuum distillate having so-called boiling point. 350-520 C, and 66.2 ma.ch. vacuum residue with so kip. and higher. Vacuum residue is deasphalted in solvent
     using the specified conditions, resulting in 45.9 May, h, deafaltaltiz and 20.3 May, h. aphaltic bitumen.
    45 Deaephaltizate emeshat e oetat-, lump, obtained by distillation at the specified atmofer pressure and the resulting mixture is subjected to the second process of thermal cracking
    50 hectares The product obtained as a result of a second thermal cracking process (carried out at 490 ° C) is separated by distillation at atmospheric pressure for distillate and residue.
    55 A portion of the residue obtained by distillation at atmospheric pressure is used in conjunction with the asphalt-free oil as a feedstock for the second thermal cracking process.
    67, 51 and 69). The results of the experiment are predds. Table 5.
    T a b l and c a
    ten
    f5
    From 4
    C - S
    48
    66
    350 C 49
    67
    6.4 40.7
    and the residue is subjected to vacuum distillation, together with the residue obtained by distillation at atmospheric pressure of the product resulting from thermal cracking at 460 ° C of the asphalt bitumen. From the combined residues obtained by distillation at atmospheric pressure, 13.0 parts by weight are obtained. vacuum distillate with boil. 350-520 C, as well as 30.4 ma.ch. vacuum residue boiling at 52Q ° C and above. 22.3 ma.ch. the vacuum residue thus obtained is used in a recycle stream for catalytic hydroprocessing, and the rest is separated.
    Asphalt bitumen obtained at the indicated stages of the process is subjected to thermal cracking at 460 ° C, followed by distillation of the product formed at the same time at atmospheric pressure. When distilled at atmospheric pressure after two stages of thermal cracking, the yield is 18.3 wt.h. united distillates comrade.
    The total amount of distillates (obtained by distillation both under vacuum and at atmospheric pressure) per 100 mash, the starting product is 30 Comparative data from a known pressure of 85.5 mash. (as a result of the proposed methods, the addition of mass parts of flows 49 is given in Table 6
    Table
    1.9
    A, 5 22.4
    18.3
    350 20
    25
    Note. On May 100 including feedstock (43) 100.0,
    Parts of the products returned to the process are not taken into account in the total quantity of the product obtained per 100 mash. recycled raw materials.
    Thus, the proposed method can effectively handle residues of vacuum distillation of oil.
    权利要求:
    Claims (3)
    [1]
    1. A method for producing hydrocarbon petroleum distillates by hyd67, 51 and 69). The results of the experiment are given in table 5.
    T a b l and c a 5
    ten
    From 4
    C - S
    48
    66
    350 C 49
    67
    6.4 40.7
    1.9
    A, 5 22.4
    18.3
    350 20
    25
     Comparative data of the known and proposed methods are given in table 6,
    Note. On May 100 including feedstock (43) 100.0,
    cleaning of asphalt-containing oil residues in the temperature range of 375–425 s, hydrogen pressure 75–175 bar, flow rate 0.2–55 h, hydrogen – raw material ratio 1000–2000 nl / kg on an aluminobolmdenum catalyst, subsequent atmospheric vacuum distillate hydrotreated product from a half
    the distillates and the residue, which is fed through successive stages of processing, including deasphaltization, carried out by the solvent — n-butane or n-pentane at 110–190 ° C, a pressure of 40–70 bar and a mass ratio of solvent: raw material (2- 3): 1, thermal cracking, conducted at BOC-ZOO C, pressure 10-30 bar and flow rate O, - 2 kg / l coil volume per 1 minute, and atmospheric vacuum distillation of deasphalting and thermal cracking products, which distinguishes - so that, in order to increase the yield of distillate fractions and reduce gaseous For example, as an asphalten-containing oil residue, the residue of vacuum distillation of oil containing 14.5–22.4 wt.% Ramsbottom carbon and having an initial boiling point and 85 wt.% boil-up is used, hydrotreating to reduce the carbon content of Remsbottom in the hydrotreating product by 46.4 I
    I
    06479 8
    56.3% of the initial content, the distillation residue after hydrotreatment is either subjected to deasphalting to produce asphalt bitumen and deasto-5 foltizate, which is subjected to thermal cracking followed by separation of the distillate and residue, or thermal cracking followed by separation of the residue and) 0 supplying it for deasphalting and hydroprocessing, deasphalting and thermal cracking is carried out so that the total yield of the fraction C. is 6.4-10.6 wt.% to the original residues
    15 oil.
    [2]
    2, Method pop.1, characterized by the fact that asphalt bitumen, obtained by deasphalting, is used as a component
    20 feedstock for catalytic hydrotreating or as a feedstock for thermal cracking.
    [3]
    3. Method according to claims, 1 or 2, about t - characterized by the fact that
    The cracking is carried out in two reactors.
    a to
     37 W
    F1L.CH
    99
    ao
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    同族专利:
    公开号 | 公开日
    AU9133382A|1983-06-16|
    NL8105560A|1983-07-01|
    DE3269261D1|1986-03-27|
    ZA829036B|1984-05-30|
    JPS58108295A|1983-06-28|
    ES517987A0|1983-09-01|
    ES8308585A1|1983-09-01|
    AU553542B2|1986-07-17|
    EP0082551A1|1983-06-29|
    EP0082551B1|1986-02-19|
    CA1198388A|1985-12-24|
    MX162957B|1991-07-22|
    AR247915A1|1995-04-28|
    JPH0581636B2|1993-11-15|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    RU2663896C2|2013-02-04|2018-08-13|Ламмус Текнолоджи Инк.|Residue hydrocracking processing|US3549517A|1968-07-23|1970-12-22|Hydrocarbon Research Inc|High conversion level hydrogenation of residuum|
    US3730875A|1971-02-16|1973-05-01|Universal Oil Prod Co|Combination process for black oil conversion|
    US3723297A|1971-10-18|1973-03-27|Universal Oil Prod Co|Conversion of asphaltene-containing charge stocks|
    NL7612960A|1976-11-22|1978-05-24|Shell Int Research|METHOD FOR CONVERTING HYDROCARBONS.|
    JPS5740879B2|1977-06-07|1982-08-31|
    GB2031011B|1978-10-05|1983-01-06|Chiyoda Chem Eng Construct Co|Processing heavy hydrocarbon oils|NL8201233A|1982-03-24|1983-10-17|Shell Int Research|PROCESS FOR THE PREPARATION OF LOW ASPHALTENE HYDROCARBON MIXTURE.|
    CA2117571A1|1993-08-30|1995-03-01|Junichi Kubo|Process for hydrotreating heavy hydrocarbon oil|
    FR2906812A1|2006-10-06|2008-04-11|Inst Francais Du Petrole|Heavy oil feedstock e.g. atmospheric residue, converting method for producing e.g. petrol, involves distilling effluent to separate residue, and recycling part of residue during de-asphalting of feedstock by mixing part with feedstock|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    NL8105560A|NL8105560A|1981-12-10|1981-12-10|PROCESS FOR PREPARING HYDROCARBON OIL DISTILLATES|
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