前苏联专利SU1565348A3 Method of obtaining hydrocarbon petroleum distillates

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权利要求

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同族专利

引用文献

法律状态

优先权

专利摘要:
Distillates are produced from asphaltenes-containing hydrocarbon mixtures by a process comprising subjecting the hydrocarbon mixtures to solvent deasphalting, and subjecting the resulting asphaltic bitumen fraction to a combination of a catalytic hydrotreatment and thermal cracking.
公开号:SU1565348A3
申请号:SU823522501
申请日:1982-12-14
公开日:1990-05-15
发明作者:Хендрик Ван Донген Роберт；Хартман Июрриан Сторк Виллем
申请人:Шелл Интернэшнл Рисерч Маатсхаппий Бв (Фирма)；
IPC主号:

专利说明:

The invention relates to methods for producing petroleum distillates from. heavy asphalt-containing oil residues and can be used in the refining industry.
The purpose of the invention is to increase the output of the GS fraction - 350 ° C,
The method is illustrated by the flow diagrams shown in Figures 1-6.
According to FIG. 1, the method is carried out in a device comprising the zone below in FIGS. 4-6 in more detail.
faltisation (YES) 1, hydrotreating zone 15 described, respectively, these three techno
25
thirty
(GO) 2 and the thermal cracking zone (TK) 3, respectively. The asphalt-containing hydrocarbon mixture 4 is de-asphalted, and the product is separated into asphalt oil 5 and asphalt bitumen 6. Flow 6 is subjected to GO and the hydrotreated product is divided into one or more distillate fractions 7 and the residual fraction 8. Streams 8 and 5 are subjected to thermal cracked and cracked product is divided into one or more distillate fractions 9 and the residual fraction 10. Apart from this technological scheme, in which stream 10 is not subjected to any further processing, part of stream 10 You can use as a feed component for GO.
In accordance with FIG. 2, the method is carried out in a device comprising zone YES 1, zone TK 3 and zone GO 4, respectively, the Asphaltene-containing hydrocarbon mixture 11 and the residual fraction 12 are deasphalted, and the product is separated into deasphalted oil 13 and asphalt bitumen 14 Stream 13 is subjected to thermal cracking, and the cracked product is divided into one or more distillate fractions 15 and the residual fraction 16. Streams 14 and 16 are subjected to GO and the hydrotreated product is divided into one or more distillate fractions 17 and atochnuyu fraction 12
According to FIG. 3, the method is carried out in a device comprising a zone YES 1, a zone TK 3 and a zone GO 2, respectively. Asphalt-containing hydrocarbon
40
45
50
logic for the production of hydrocarbon petroleum distillates from asphalt-containing petroleum residues. According to FIG. 4, the method is carried out in a device comprising successively the zone DA 25, the zone GO, consisting of the catalytic hydroprocessing unit 26, the atmospheric distillation unit 27 and the vacuum distillation unit 28, and the TC zone, consisting of the thermal cracking unit 29, the second the atmospheric distillation unit 30, the second thermal cracking unit 31, the third atmospheric distillation unit 32, and the second vacuum distillation unit 33. The asphaltene-containing hydrocarbon mixture 34 is separated by deasphalting with a solvent for deasphalted oil 35 and asph alto bitumen 36. Asphalt bitumen 36 is mixed with vacuum residue 37 and the mixture 38 is subjected, together with hydrogen 39, to catalytic hydrotreating. The hydrotreated product 40 is separated by atmospheric distillation into a gas fraction 41, atmospheric distillate 42 and atmospheric residue 43. Atmospheric residue 43 is separated by vacuum distillation into vacuum distillate 44 and vacuum residue 45. Vacuum residue 45 is subjected to thermal cracking and the cracked product 46 is separated by atmospheric distillation into a gas fraction 47, atmospheric distillate 48 and atmospheric residue 49. Deasphalted oil 35 is mixed with atmospheric residue 50 and the mixture 51 is subjected to by thermal cracking. Subjected to the cracking of a prological scheme for the production of hydrocarbon oil distillates from asphaltene-containing oil residues. According to FIG. 4, the method is carried out in a device comprising successively the zone DA 25, the zone GO, consisting of the catalytic hydroprocessing unit 26, the atmospheric distillation unit 27 and the vacuum distillation unit 28, and the TC zone, consisting of the thermal cracking unit 29, the second the atmospheric distillation unit 30, the second thermal cracking unit 31, the third atmospheric distillation unit 32, and the second vacuum distillation unit 33. The asphaltene-containing hydrocarbon mixture 34 is separated by deasphalting with a solvent for deasphalted oil 35 and asph alto bitumen 36. Asphalt bitumen 36 is mixed with vacuum residue 37 and the mixture 38 is subjected, together with hydrogen 39, to catalytic hydrotreating. The hydrotreated product 40 is separated by atmospheric distillation into a gas fraction 41, atmospheric distillate 42 and atmospheric residue 43. Atmospheric residue 43 is separated by vacuum distillation into vacuum distillate 44 and vacuum residue 45. Vacuum residue 45 is subjected to thermal cracking and the cracked product 46 is separated by atmospheric distillation into a gas fraction 47, atmospheric distillate 48 and atmospheric residue 49. Deasphalted oil 35 is mixed with atmospheric residue 50 and the mixture 51 is subjected to by thermal cracking. The cracked prod mixture 18 is subjected to deasphalting, 55 duct 52 is separated using the atmosphere, the product is divided into deasphalted oil 19 and asphalt bitumen 20. Streams 19 and 20 are subjected to TC,
distillation to gas fraction 53, atmospheric distillate 54 and atmospheric residue 55. Atmospheric residue
and the cracked product, is divided into one or more distillate fractions 21 and the residual fraction 22. Stream 22 is subjected to TH, and the hydrotitrated product is divided into one or more distillate fractions 23 and the residual fraction 24. Stream 24 used either as a component of the raw material for YES, or as a component of the raw material for TC, or as a component of the raw material for both DA and TK.
Below in figure 4-6 in more detail
These three techno0 are described respectively.
five
0
,
40
45
50
logic for the production of hydrocarbon petroleum distillates from asphalt-containing petroleum residues. According to FIG. 4, the method is carried out in a device comprising successively the zone DA 25, the zone GO, consisting of the catalytic hydroprocessing unit 26, the atmospheric distillation unit 27 and the vacuum distillation unit 28, and the TC zone, consisting of the thermal cracking unit 29, the second the atmospheric distillation unit 30, the second thermal cracking unit 31, the third atmospheric distillation unit 32, and the second vacuum distillation unit 33. The asphaltene-containing hydrocarbon mixture 34 is separated by deasphalting with a solvent for deasphalted oil 35 and asph alto bitumen 36. Asphalt bitumen 36 is mixed with vacuum residue 37 and the mixture 38 is subjected, together with hydrogen 39, to catalytic hydrotreating. The hydrotreated product 40 is separated by atmospheric distillation into a gas fraction 41, atmospheric distillate 42 and atmospheric residue 43. Atmospheric residue 43 is separated by vacuum distillation into vacuum distillate 44 and vacuum residue 45. Vacuum residue 45 is subjected to thermal cracking and the cracked product 46 is separated by atmospheric distillation into a gas fraction 47, atmospheric distillate 48 and atmospheric residue 49. Deasphalted oil 35 is mixed with atmospheric residue 50 and the mixture 51 is subjected to by thermal cracking. Cracked product 55 is divided by atmospheric distillation into a gas fraction 53, an atmospheric distillate 54, and an atmospheric residue 55. The atmospheric residue
55 is divided into two parts 50 and 56. Part 56 is mixed with atmospheric residue 49 and the mixture 57 is separated by vacuum distillation to a vacuum distillate 58 and vacuum residue 59, the remainder 59 is divided into two parts 37 and 60. Gas fractions 47 and 53 are combined to give a mixture of 61, and atmospheric distillates 48 and 54 are combined to form a mixture of 62.
Referring to FIG. 5, the method is carried out in a device comprising successively an DA 63 zone, a TC zone consisting of a thermal cracking unit 64, an atmospheric distillation unit 65 and a vacuum distillation unit 66, and a GO zone consisting of a catalytic hydrotreating unit 67, the second of the atmospheric distillation unit 68 and the second vacuum distillation unit 69. Asphaltenso
The hydrocarbon mixture holding 70 is mixed with a vacuum residue 71 and the mixture 72 is separated by solvent deasphalting onto deasphalted oil 73 and asphalt bitumen 74. The deasphalted oil 73 is mixed with the atmospheric residue 75 and the mixture 76 is thermally cracked. The cracked product 77 is divided by atmospheric distillation into a gas fraction 78, an atmospheric distillate 79 and an atmospheric residue 80. The atmospheric residue 80 is divided into two streams 75 and 81. The stream 81 is subjected to vacuum distillation to obtain a distillate 82 and vacuum residue 83. Asphalt 74 is divided into two parts 84 and 85. Part 84 is mixed with vacuum residue 83 and the mixture 86 is subjected, together with hydrogen, to catalytic hydrotreating, the Hydropurified product 87 is divided by atmospheric distillation into a gas fraction 88, atmospheric istill 89 m and an atmospheric residue 90. AT- atmo- spheric residue 90 is separated by vacuum distillation into a vacuum distillate and a vacuum residue 91 January 7.
According to FIG. 6, the method is carried out in a device comprising, in series, the DA 92 zone, the TC zone, consisting of a thermal cracking unit 93, an atmospheric distillation unit 94, a second thermal cracking unit 95, a second atmospheric distillation unit 96, and a vacuum unit distillation 97, and the GO zone, consisting of a node katalit0
0
five
about
hydrofining 98, the third bond of atmospheric distillation 95 and the SECOND vacuum peg unit 11) 0. Ac-Falten containing fertile mixture 101 is mixed with vacuum residue 102 and mixture 103 is separated by deasphalting with solvent for deasphalted oil 104 and asphalt bitumen 105. Deasphalyed oil 104 is mixed with atmospheric residue 10 and the mixture 107 is converted by thermal cracking for the product 108 which, with the help of atmospheric distillation, is divided into the gas fraction 109, the atmospheric distillate 110 and the atmospheric residue 111. The atmospheric residue 111 is divided into two parts 106 and M2, Asphalt bitumen 105 using the term The cracking process is converted into product 113, which is separated by atmospheric distillation into the lazup fraction 114, the atmospheric distillate 115 and the atmospheric residue 116. The gas fractions 109 and 114 are combined to form a mixture 117, and the atmospheric distillates 110 and 115 are combined with In order to obtain a mixture of 118, Atmospheric residues 112 to 116 are combined and the mixture 119 is divided by vacuum distillation into a vacuum distillate 120 and a vacuum residue 121, Vacuum residue 121 is divided into two parts 122 and 123. Part 123 of the vacuum residue is put together hydrogen 124 rolled Hydro-refining, Hydro-Purified Product 125, is separated by atmospheric distillation into a gas fraction 126, atmospheric distillate 127, and atmospheric residue 128. Atmospheric residue 128 is separated by vacuum distillation into a vacuum distillate 129 and vacuum residue 102.
0

Three asphalt-containing hydrocarbon mixtures obtained in the form of residues of vacuum distillation of bottom residues of oil obtained by atmospheric distillation of Middle Eastern crude oils are the initial mixtures. All three vacuum residues are boiled at a temperature above 520 ° C, they have the value of Remsbottok (CT), respectively, 21.0; 18.1 and 14.8 wt.%. The process is carried out in accordance with the technological schemes given in Figures 4-6.
In all technological schemes, the catalytic hydrotreating unit contains two reactors, the first of which is filled with Ni / V / SiO - a catalyst containing 0.5 weight, h, nickel and 2.0 parts by weight. Vanadium per 100 weight parts. silica, and the second of which is filled with Co (Mo), - a catalyst containing 4 weight.h. cobalt and 12 wt.h. molybdenum per 100 weight.h. alumina. Catalytic hydrotreating is carried out at a hydrogen pressure of 150 bar and a ratio between HЈ and raw materials of 1000 nl / kg.
In all technological schemes, the DA is carried out at a pressure of 40 bar, using n-butane as the solvent. In all technological schemes, the TC is carried out in one two cracking coils at a pressure of 20 bar and a flow rate of 0.4 kg of fresh raw material per liter of cracking coil volume per minute.
The remaining conditions for conducting GO, DA and TC are given in Table. 1. Example 1 (FIG. 4), 100 weight parts, 520 ° C 4 vacuum residue 34 with a PCT of 21.0 wt.% Divided into streams in the following amounts: 56.0 May, h. deasphalted oil 35, 44.0 weight.h. asphalt bitumen 36, of which receive 72.6 weight.h of a mixture of 38, with a PKT 37.5 wt.%, and product 40, the fraction of which has a PKT of 12.5 wt.%. 14.8 parts by weight Cs - 350 C of atmospheric distillate 42; 52.3 wt.h, 350DC + atmospheric residue 43} 22.5 wt.h. 350-520 ° C vacuum distillate 44, 29.8 weight, h, 520tfC vacuum residue 45; 24.2 weight.h; Cg - 350 ° C atmospheric distillate 62; 57.6 parts by weight 350 ° C atmospheric residue 57J 18.0 weight.h. 350-520 ° С vacuum distillate 58} 39.6 weight, h. 520 ° C vacuum residue 59; 28.6 parts by weight, parts 37 and
11.0 weight, h parts 60,
A consolidated balance of the process is given in table. 2,
PRI mme R 2. Out of 100 weight.h. 520 ° vacuum residue 70 with CT
18.1 mas,%, receive streams in the following amounts: 130.2 wt.h. mixtures 72; 72.9 weight, h, deasphalted oil 73, 57.3 parts by weight asphalt bitumen 74 23.8 weight-.h. SAT - 350 ° C of atmospheric distillate 78;
five
0
five
0
five
0
five
0
five
45.1weight.h. 350CC atmospheric residue 81 17.4 weight.h. 350-520 ° С vacuum distillate 82J 27.7 weight.h, 520 ° С vacuum residue 83J
44.3 weight. 84, 13.0 weight.h. 85, 72.0 wt.h, a mixture of 86, having a PCT of 36.6 wt.%, Product 87, of which the CCP has a PKT of 12.1 wt.%,
14.4 weight. Cg - 350 ° C atmospheric distillate 89; 52 weight.h, atmospheric residue 90; 22.2 weight, h. 350-520 ° C vacuum distillate 91 and
30.2 weight.h. vacuum residue 71,
A consolidated balance of the process is given in table. 2
PRI me R 3. Out of 100 weight.h. 520 ° C vacuum residue 101, having a CT, 14.8 wt.%, Receive flows in the following amounts: 126.4 weight.h. mixtures 103J 77.1 wt.h, deasphalted oil 104; 49.3 parts by weight asphalt bitumen 105J 35.1 weight.h. SAT - 350 ° C of atmospheric distillate 118;
85.5 weight.h. 350 ° С (atmospheric residue 119, 26.0 parts by weight 350-520 С vacuum distillate 120; 59.5 parts by weight vacuum residue 121 J
8.7 weight hours parts 122 50.8 weight.h. part 123, having a PCT of 42.2 wt.%, product 125, the Cd fraction of which has a PCT of 15.9 wt.%, 7.5 wt.h. C - 350 ° C of atmospheric distillate 127 {40.2 weight hours. 350 ° C atmospheric residue 128; 13.8 parts by weight 350-520 ° C vacuum distillate 129 and 26.4 parts by weight. 520 ° C vacuum residue 102, Summary balance of the process is given in table. 2
Thus, in the proposed method, the yield of the C5 fraction - 350 ° C is 38.2-42.6% by weight per 100% by weight,% of the initial charge of the raw material compared to 37.1% by weight in the known method.
four

权利要求:
Claims (3)
[1]
1. A method of producing hydrocarbon oil distillates from asphaltente-containing oil residues having a boiling start of 450 ° C and 85% by volume of boiling above 520 ° C, including de-asphalting with n-butane at a weight ratio of (2-3); 1 , pressure 40 bar, temperature 120-125CC, hydrotreatment on an alumino-cobalt-molybdenum catalyst at a temperature of 395410 ° C, pressure 150 bar, a space velocity of 0.2-0.3 h and a hydrogen: raw material ratio 1000 N-g / kg, thermal cracking at a pressure of 20 bar, temperature 480-495ES, volumetric velocity 0.4 kg / l coil volume / min with obtaining 8.9-9.5 wt.% ha C $, atmospheric and atmospheric vacuum distillations with the release of CJ gas, C5 fractions of 350, 350-520 C, and fractions above 520 ° C, characterized in that, in order to increase the output of the GS fraction of 350 ° C, the initial oil residue deasphalted with a solvent to obtain deasphaltized acid and asphalt; deasphalted oil is used as a raw material for thermal cracking, and asphalt is used as a raw material for hydrotreating or thermal cracking; in the case of asphalt being fed to hydrotreating, the fraction above 520 ° С after atmospheric vacuum distillation of the hydrated product cleaning ICs
five
0
used as a component of raw material for thermal cracking or deasphalting, in the latter case the fraction above 520 ° C obtained after vacuum distillation of the thermal asphalt deasphalted petroleum product is used as a component of the raw material of hydrorefine, and when applying asphalt to the thermal cracking fraction above 520 ° C, the vacuum distillation of the thermal cracking material is used the raw material for hydrotreating, and the fraction above 520 ° С, obtained after vacuum distillation of hydrotreating products, as a component of the raw deasphaltiation.
[2]
2, The method according to claim 1, about tl to h and y - y and u and heme, that thermal cracking is carried out separately on two installations
with the supply of various raw materials to them,
[3]
3. The method according to claim 1, about tl and h ay - y and so, the remainder of the atmospheric distillation of the product of thermal cracking is recycled to thermal cracking.
According to the general technological scheme,
picture
Detailed technological scheme
picture
GO
The volumetric rate determined for both reactors, The average temperature in the first reactor, ° C
Average temperature in the second reactor, C
YES
The weight ratio between solvent and oil Temperature, ° С
TC
Number of cracking units Temperature in the first cracking unit, С
Temperature in the second cracking unit, С
Recycling rate in the second cracking unit (wt.% Of May4% of fresh raw material)
The reported cracking temperatures of PL h M. oena at the outlet of the cracking coils
Table 1
14
2 5
3 6
4 (0
2
480
490
L l .1
Table 2
2
18
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98
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i2
t i
U
Llj
aimepitz
f
17. (,
1 / and
nineteen
L vll
91
but
T
and
28 6L 8L
og
L, i

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法律状态:

优先权:

申请号 | 申请日 | 专利标题

NL8105660A|NL8105660A|1981-12-16|1981-12-16|PROCESS FOR PREPARING HYDROCARBON OIL DISTILLATES|

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