Method of producing light products and fuel oil

专利摘要:
The invention describes a process for producing light products, such as engine and diesel fuels, and fuel oils for conventional use by thermal conversion of heavy metal- and sulfur-rich-crude oil residue. Thermal cracking of the residues is done by mild cracking in several stages, where the residue remaining after separation of the conversion products of the preceding stage is fed to the respective subsequent stage.
公开号:SU1604162A3
申请号:SU874202274
申请日:1987-04-03
公开日:1990-10-30
发明作者:Фрон Вернер；Больман Дитер；Херманн Франке；Циммерманн Вернер；Лиммер Хейнц；Хепфнер Эберхард；Линднер Хорст；Маттей Рейнхард；Мюллер Хеннер；Поппен Ханс；Шюттер Хартмут；Дитрих Детлев
申请人:Феб Петрольхемишес Комбинат Шведт (Инопредприятие)；Тойо Инджиниринг Корпорейшн (Фирма)；Мицуико, Лтд (Фирма)；
IPC主号:

专利说明:

The invention relates to a process for the preparation of light products, such as diesel and carburetor fuels, and common oil. liquid fuel (fuel oil) suitable for use, by thermal conversion of heavy metal and sulfur-containing residues from the distillation of oil.
The purpose of the invention is to improve the quality of the target products at the lower cost of thermal transformation: the heaviest metal and sulfur containing oil distillation residues.
The method is carried out as follows.
The residue of oil distillation obtained by vacuum distillation with the following characteristics:
Density at
15 С, kg / l
Temperature
hardening, with
Conradson test
wt.%
Viscosity at 130 ° C, cSt
1,011
42
18.3
and tc

oa
182
3
Soluble substances in cyclohexanone, wt.%. 8.1
Sulfur, wt.% 3,12
Nitrogen, wt.% 0,86
Nickel, ppm 74
Vanadium, ppm 195 is subjected to thermal cracking by the method of light cracking. In this case, by varying the parameters, you can maximize the conversion.
The results are summarized in table 1.
Experimental data shows that
for existing feedstocks, a conversion of 25 wt.% per 500 ° C can be achieved. A satisfactory result to ensure a conversion degree above 30% cannot be achieved using conventional light cracking. The light products obtained by atmospheric distillation from the products of the conversion make up a relatively small proportion of them. Vacuum distillation is then carried out and does not allow a significant increase in the amount of the distillate, since it is associated with significant costs, which many times can exceed the effect to achieve.
In the course of further experiments, the residue of distillation of crude oil according to the proposed method is subjected to two-stage soft thermal cracking with intermediate removal of conversion products. Get eaten following results:

0.106 0.106
5 6
424 425
400 400
eleven

20 20
60 55 15 15
Q
five
0 5
.--
0
five
0
five
wt.% in the calculation
on ref. product 18 25.5 Total i conversion wt.% (500 ° C) 54.4 58.5 The quality of the residue after the first stage, the content of dry sludge according to the test is hot
filtration, wt.% 0.15 .0.15 The quality of the residue after the second stage is the difference between the dry sludge after accelerated aging and the sludge contained in the hot filtration test, wt.% 0.04 0.02
Sulfur, wt.% 2.99 3.06 Viscosity at
225 C, cSt 42 45 Distillate yield at atmospheric distillation calculated on the initial one,. product wt.% g °
five
6.2 21.5 23.8
6.0 20.6 29.1 55.7
at C:
200
200-350
350-500
Total distillate
The results of this series of experiments show that a significant increase has been achieved in the yield of light products from the distillation residue of such a quality that allows its use as ordinary liquid fuel. When comparing experiments 5 and 6, it is clear that the conversion product at stage I separates as much as possible under moderately mild conditions at stage D5 II, the total conversion increases, in particular, fractions 350-500 s, which are used to produce carburetor fuel by combining thermal and catalytic cracking, including preliminary hydrocatalytic treatment.
In modern installations for burning liquid fuels, residues with viscosity values ranging from 40 to 50 cSt can be used with preheating to.
It is possible to adjust viscosity in outdated plants, etc., by mixing with recycle, which
It was obtained by catalytic cracking subjected to preliminary hydro-. Atalytic treatment of a mixture of the same distillate fraction of two-stage moderate (light) thermal cracking according to test 6 and obtained by distillation from a vacuum distillate oil.
eight
88 12
74
26
4120 1377 15 2.75
356
144
2.45
0.15 0.15
Experience
The rest of the experience 6, wt.% Recirculated, wt.%
The quality of the mixture of boiler fuel, viscosity, cSt, at C: 70 100 225
Sulfur, wt,% Hot filtration test, dry sludge content, wt,% The difference of dry sludge after accelerated aging and contained dry sludge, wt.% Experiments 7 and 8 show that the proposed options for mixtures provide the possibility of obtaining boiler installations that require a viscosity of about 15 cSt as well as achieving higher viscosity requirements, for example, in the case of so-called bunker fuel, and there is no problem of storage stability.
The product, which is introduced into the second thermal stage of cleavage, has average boiling points, i.e. surplus, and only a few percent of its constituents are boiled at temperatures below 500 C. The content of this product (insoluble in hexane) in asphaltenes 5 was 9.9% by weight; in the experiment, approximately 11.1% by weight. Asphaltenes, 0.01, 0.02
04162
-. .
t 10
15
20
25
thirty
35
40
45
50
; ";
adverse effects affect the results of the thermal breakdown. The removal of asphaltenes using a separate unit is costly and the asphaltene product remaining during such extraction cannot be used as a conventional boiler fuel.
Table 2 shows the results of experiments 9-12, indicating the value of processing time at each stage. Test 9 was carried out in accordance with the claims, test 10 with a shorter processing time in the second stage compared to the first stage. In this case, the floor: or, however, as a lower degree of conversion, and unacceptable for the boiler fuel quality residue. Increasing the temperature in the second stage in order to achieve a higher conversion was not possible due to the coking problem in the apparatus.
In Example 11, decomposition in the second stage is carried out at the same processing time as in the first stage. The results show, however, only a relatively small conversion and an insufficient degree of conversion.
In order to achieve an acceptable residue quality, the processing time in test 12 is less than the processing time in test 11.

权利要求:
Claims (1)
[1]
Invention Formula
The method of obtaining light products and fuel oil from gels of metal- and sulfur-containing oil distillation residues by thermal cracking in the first stage, followed by separation of the products obtained and feeding one of the products to the second stage of thermal cracking with the target products, characterized in that in order to increase the quality of the target product, the first stage of thermal cracking is carried out at a temperature of 421- 425 ° C, a pressure of 1 MPa and a time of 20 minutes, the second stage at a temperature of 4004, a pressure of 0.106 - 0.11 MPa or 55-60 min.
Table 1
) -
According to the content of the dry sludge determined by the hot filtration test, the quality of the conversion residues of the distillation Atmospheric distillate is judged.
Temperature,
° С
Pressure, MPa Time, min Total conversion, wt.%
(500 ° С) Quality of residue after the second stage (hot filtration) - dry sludge content, wt.% Difference in dry: sludges after accelerated aging and available, wt.%
hot filtration
Table
420
one
20
420
one
ten
38.2
39.3
33.5
0.63
0.25
0.19
0.21
0.14
0.10

类似技术:

---

公开号 | 公开日 | 专利标题

---

EP0621334B1|1998-11-11|Process for producing a fuel by extraction and hydrotreatment of a hydrocarboneous feed and produced gasoil

---

CA1079215A|1980-06-10|Thermal treatment of used petroleum oils

---

EP0432235B1|1994-09-14|Process for the production of improved octane numbers gasolines

---

FR2725725A1|1996-04-19|PROCESS AND INSTALLATION FOR THE PURIFICATION OF USED OILS

---

SU1604162A3|1990-10-30|Method of producing light products and fuel oil

---

JPH03199290A|1991-08-30|Preparation of low-sulfur and high-sulfur cokes

---

CA1226839A|1987-09-15|Process and facility for making coke suitable formetallurgical purposes

---

US3673077A|1972-06-27|Process for producing electrode binder pitch and carbon black feedstock

---

US3167500A|1965-01-26|Removal of metal comprising contaminants from petroleum oils

---

DE2555812C2|1982-05-19|Method of making pitch

---

US2906693A|1959-09-29|Pretreatment of catalytic cracking feed to remove metals

---

CA1178231A|1984-11-20|Process for obtaining a synthetic crude petroleum

---

US1936210A|1933-11-21|Process of treating cracked petroleum distillates

---

EP0768363B1|1999-12-29|Process for reducing the viscosity of heavy oil residues

---

US2280227A|1942-04-21|Refining of petroleum distillates

---

US4169781A|1979-10-02|Denitrification by furfural-ferric chloride extraction of coker oil

---

US2149351A|1939-03-07|Refining and stabilization of motor fuel

---

US2890963A|1959-06-16|Improving color of lubricating oils and waxes

---

DE102019134472B4|2021-05-27|Process for upgrading waste oil

---

RU2613634C1|2017-03-21|Method for processing oil residues

---

US3352776A|1967-11-14|Process for the preparation of binder oils

---

RU2139911C1|1999-10-20|Petroleum derivative production process

---

US2024117A|1935-12-10|Method of treating and purifying motor fuels

---

RU2237700C1|2004-10-10|Heavy petroleum residue processing method

---

SU1595881A1|1990-09-30|Method of purifying heavy oil residues

同族专利:

---

公开号 | 公开日

---

ES2035827T3|1993-05-01|

---

US4792389A|1988-12-20|

---

DE3782545T2|1993-03-25|

---

EP0249052A3|1989-05-31|

---

EP0249052A2|1987-12-16|

---

HUT50862A|1990-03-28|

---

HU206514B|1992-11-30|

---

DE3782545D1|1992-12-17|

---

GR3006612T3|1993-06-30|

---

KR880000552A|1988-03-26|

---

JPS62290792A|1987-12-17|

---

CS270226B2|1990-06-13|

---

KR910009923B1|1991-12-05|

---

DD249916A1|1987-09-23|

---

DD249916B1|1989-11-22|

---

EP0249052B1|1992-11-11|

---

CS426487A2|1989-10-13|

引用文献:

---

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

---

EA000032B1|1995-10-13|1998-02-26|Аджип Петроли С.П.А.|Process for reducing the viscosity of heavy oil residues|US2100048A|1920-07-31|1937-11-23|Power Patents Co|Process of cracking oil|

---

US1676694A|1926-02-02|1928-07-10|Standard Oil Dev Co|Pyrogenesis of petroleum products|

---

US2166787A|1937-01-15|1939-07-18|Universal Oil Prod Co|Hydrocarbon oil conversion|

---

US2247740A|1937-12-31|1941-07-01|Universal Oil Prod Co|Conversion of hydrocarbon oils|

---

US2363237A|1942-10-09|1944-11-21|Southern Wood Preserving Co|Production of useful materials|

---

US2748061A|1951-08-18|1956-05-29|Shell Dev|Thermal treatment and separation process|

---

US3148136A|1959-09-14|1964-09-08|Texaco Inc|Treatment of hydrocarbons to produce a jet fuel and high octane gasoline|

---

JPS5391908A|1977-01-24|1978-08-12|Chiyoda Chem Eng & Constr Co Ltd|Method of treating heavy oil|

---

JPS5715796B2|1977-03-29|1982-04-01|

---

US4268375A|1979-10-05|1981-05-19|Johnson Axel R|Sequential thermal cracking process|

---

JPS6256917B2|1981-01-16|1987-11-27|Toyo Enjiniaringu Kk|

---

JPS6147194B2|1982-04-09|1986-10-17|Toyo Engineering Corp|

---

JPS6158515B2|1983-02-28|1986-12-11|Fuji Sekyu Kk|

---

JPS61163992A|1985-01-16|1986-07-24|Fuji Standard Res Kk|Continuously producing pitch suitable for use as raw material of carbon fiber|

---

JPH0437873B2|1986-05-26|1992-06-22|Maruzen Sekyu Kagaku Kk|US5316660A|1990-11-15|1994-05-31|Masaya Kuno|Hydrodelayed thermal cracking process|

---

US6632351B1|2000-03-08|2003-10-14|Shell Oil Company|Thermal cracking of crude oil and crude oil fractions containing pitch in an ethylene furnace|

---

EP1999235B1|2006-03-29|2018-09-05|Shell International Research Maatschappij B.V.|Process for producing lower olefins|

---

JP2009531529A|2006-03-29|2009-09-03|シエル・インターナシヨナル・リサーチ・マートスハツペイ・ベー・ヴエー|Improved process for producing lower olefins from heavy hydrocarbon feeds using two vapor / liquid separators|

---

CN104560153B|2013-10-24|2016-05-18|中国石油化工股份有限公司|A kind of method of utilizing ethylene bottom oil and heavy benzol to produce clean fuel oil|

---

US10920158B2|2019-06-14|2021-02-16|Saudi Arabian Oil Company|Supercritical water process to produce bottom free hydrocarbons|

法律状态:

优先权:

---

申请号 | 申请日 | 专利标题

---

DD86291132A|DD249916B1|1986-06-10|1986-06-10|METHOD OF PRODUCING LIGHT PRODUCTS AND CONVENTIONALLY UTILIZABLE HEATING OILS FROM HEAVY METAL AND SULFUR RESOURCES|

---