CN1309164A - Residue hydrogenating and delaying coking combined process - Google Patents
Residue hydrogenating and delaying coking combined process Download PDFInfo
- Publication number
- CN1309164A CN1309164A CN 00100879 CN00100879A CN1309164A CN 1309164 A CN1309164 A CN 1309164A CN 00100879 CN00100879 CN 00100879 CN 00100879 A CN00100879 A CN 00100879A CN 1309164 A CN1309164 A CN 1309164A
- Authority
- CN
- China
- Prior art keywords
- oil
- gas oil
- coker gas
- heavy
- residue
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
A process for combining hydrogenating residue with delaying coking includes such steps as mixing residue, coked gas oil and hydrogen together, hydrogenation reaction in the presence of catalyst, separating the hydrogenated resultant, delay coking of hydrogenated residue individually or along with conventional raw materials for preparing needle coke, separating coked resultant, and returning the coked gas oil back to hydrogenation equipment. Its advantages are high yield of needle coke (up to 41.5 wt.%), low CTE and sulfur content of needle coke, and high yield and quality of light oil.
Description
The invention belongs to the multistage processes with a hydroprocessing technique process and a thermal conversion step processing hydrocarbon ils, more particularly, is a kind of combined technical method with residual hydrocracking and two kinds of processing methodes combinations of delayed coking.
Conventional delayed coking is a kind of mink cell focus to be converted into the heat processing technique of cooking gas, coker gasoline, coker gas oil, coker gas oil and coke through drastic cracking, is the main means that refinery improves yield of light oil and produces refinery coke.Delayed coking less investment, instant effect are particularly suitable for transforming the poor residuum of low value.Generally except that the light ends of 30～50 heavy %, still can obtain the coker gas oil of 20～35 heavy % and the refinery coke of 15～25 heavy %.After coker gasoline, coker gas oil needed hydrofining, quality just can meet the product specification requirement.Coker gas oil is generally directly sneaked in the vacuum gas oil (VGO) as fluid catalytic cracking (FCC) charging with the ratio of 20～30 heavy %, though enlarged the FCC raw material sources like this, but, influence FCC transformation efficiency and quality product because coker gas oil contains impurity such as higher sulphur, nitrogen.
Refinery coke is a kind of black or lead, has the porosu solid of metalluster that main component is a carbene.Delayed coking can only be produced common Jiao under the routine operation condition, but along with to carbonaceous product, particularly the continuous increase of the required ultra-high power graphite electrode demand of Iron And Steel Industry makes the demand of producing the used starting material-needle coke of these products growing.Sulphur content and thermal expansivity (CTE) are to weigh good and bad topmost two quality index of refinery coke, require its sulphur content below 0.7 heavy % for needle coke, and CTE is less than 2.6 * 10
-6/ ℃ (1000 ℃ of carbon rod sample preparation methods, down together).In order on delayed coking unit, to produce needle coke, need stock oil and processing condition are done suitable adjustment.One of characteristics of China's main oils are that sulphur content is low, and therefore, China's oil Jiao's actual measurement sulphur content but is a raw material with Shengli crude vacuum residuum generally all about 0.5 heavy %, and the refinery coke sulphur content that is generated is higher, reaches about 2 heavy %.For the doctor positive middle-eastern crude, the sulphur content of its refinery coke is then higher, generally more than 5% weight.And no matter be doctor negative domestic oil or doctor positive Middle East oil, even under the delayed coking condition of producing needle coke, the refinery coke CTE of production is all 5.0 * 10
-6/ ℃ about.
Hydrotreatment is a kind of effective ways that improve coker gas oil character, and the coker gas oil behind the hydrogenation can be used as fine FCC charging.In order to improve the quality of delayed coking product, people have proposed residual oil is carried out hydrotreatment earlier, and then remove the technological line of delayed coking.By residual hydrocracking, sulphur, nitrogen and metal impurities in the residual oil are removed in a large number, thereby can obtain quality coke chemicals preferably.USP4,235,703 vacuum residuum that proposed with high-sulfur, high metal are raw material, earlier after hydrodemetallation (HDM), hydrogenating desulfurization, mix with other conventional raw material of producing needle coke, carry out coking under the operational condition of producing needle coke, wherein coker gas oil is back to pyrogenic process furnace with recycle ratio (accounting for coking raw material) 0.5～1.5, although the needle coke CTE that this method is produced is very low, its sulphur content is very high.In addition, the residual oil that these patent special requirement are processed derives from the naphthenic base crude of characterization factor K≤11.4, as Saudi Arabia's heavy crude.
Above-mentioned residual hydrocracking also is the important means of residual oil processing upgrading, and is wherein ripe with fixed bed residual hydrogenation technology.Residual hydrocracking reaction is the process of internal diffusion control, and the higher residual oil raw material of viscosity will influence the hydrogenation reaction effect, to the flow state of residual oil in beds be distributed with influence.Therefore, hydrotreatment for the bigger residual oil raw material of viscosity, existing method is normally sneaked into some lighter distillates (from subtracting VGO cut below four lines and light ends oil to the catalytic cracking light cycle oil), to reduce residual hydrocracking raw material oil viscosity, improves the hydrogenation reaction effect.EP 0 462 823 A1 propose from atmospheric gas oil (AGO), vacuum gas oil (VGO), select a kind of in catalytic cracking light cycle oil (LCO) or the heavy cycle oil (HCO) as thinner, dilution vacuum residuum, metal and/or sulphur in can effective elimination residual oil, the thinner that this method adopts mostly is the light ends oil of high value, some can be directly as the blend component of product or product, and VGO is the main raw material of hydrocracking (HC) and catalytic cracking (FCC), and, the scale of hydrocracking is constantly enlarged along with the demand of market to the high-quality intermediate oil constantly increases.Therefore at present there are in various degree hydrocracking and the catalytic cracking contradiction of contending over raw materials.
The objective of the invention is to provide on the basis of existing technology a kind of combined technical method of residue hydrogenating and delaying coking, this method is produced the needle coke impurity in the effective elimination coker gas oil simultaneously with maximum.
Technical scheme of the present invention is:
This combined technical method comprises the following steps:
A, residual oil and coker gas oil enter hydrotreater together, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst;
B, gained hydrogenated residue enter delayed coking unit separately or with other conventional raw material of producing needle coke, carry out heat cracking reaction;
The coker gas oil that C, delayed coking unit obtain all is back to hydrogenation unit.
The used residual oil of the present invention can be long residuum and/or vacuum residuum, also can be long residuum and/or the vacuum residuum that mixes the part lightweight oil, described lightweight oil is one or more the mixture that is selected among heavy catalytic cycle oil, fluid catalytic cracking decant oil and the solvent-deasphalted oils.
The described coker gas oil of steps A accounts for 3～35 heavy % of residual oil.Coker gas oil described in the steps A can be the coker gas oil that obtains among the independent step B, also can be the mixture of the coker gas oil that obtains among the step B and external coker gas oil.
The conventional raw material that described in the step B other produced needle coke is selected from fluid catalytic cracking decant oil, thermal cracking residue, lube oil furfural refining and extracts among oil or the preparing ethylene by steam cracking tar one or more mixture out.
The main purpose of residual hydrogenation process is in the presence of hydrogen, makes the catalyst reaction in residual oil raw material and the hydrogenator, removes sulphur, nitrogen and metal impurities, reduces carbon residue, and the while is some light ends oil of by-product also.
The reaction conditions of hydrotreatment is: 330 ℃～450 ℃ of temperature, hydrogen dividing potential drop 5.0～22.0MPa, volume space velocity 0.1～3.0 hour
-1, hydrogen to oil volume ratio 350～2000Nm
3/ m
3
Hydrotreater comprises at least one reactor and reaction product separation system such as separation column, and reactor both can be a fixed bed, also can be ebullated bed or moving-bed.
The active metal component of hydrogenation catalyst is Ni-W, Ni-W-Co, Ni-Mo, Co-Mo etc., and typical carrier has aluminum oxide, silicon-dioxide and silicon-aluminum mixture, and the most frequently used is aluminum oxide.Owing to contain dissimilar impurity in the residual oil, as S, N, various metal and solid particulate etc., be difficult to the various impurity in a kind of catalyst removal residual oil, therefore the fixed bed Residue Hydrotreating Technology is generally all united the multiple catalyzer with difference in functionality of use, promptly adopt the technology of classification filling, this technology can obviously improve the running period of residual hydrogenation equipment.Usually residual oil hydrocatalyst is divided into three types of hydrogenation protecting agent, hydrodemetallation (HDM) (HDM) catalyzer and hydrogenating desulfurizations (HDS), and its characteristic is listed in table 1.
Table 1
| Catalyst type | The hydrogenation protecting agent | The HDM catalyzer | The HDS catalyzer |
| Shape | Sphere/extrusion | Sphere/extrusion | Extrusion |
| Particle diameter, mm | ??3～10 | ??1.2～6 | ??0.8～1.6 |
| Active phase | ??- | ??Mo/NiMo | ??NiMo/CoMo/NiW |
| The HDM activity | ??- | High | Medium |
| The HDS activity | ??- | Low | Higher |
The oil gas that hydrotreatment generates through fractionation separates is: gas (C
4 -), petroleum naphtha (C
5～180 ℃), diesel oil distillate (180 ℃～350 ℃), (＞538 ℃ in vacuum residuum behind vacuum gas oil (350 ℃～538 ℃) and the hydrogenation, brief note HVR), wherein gas is sneaked in the refinery gas, petroleum naphtha can be used as the charging of reformer, diesel oil distillate is the blend component of good diesel product, comprised the coker gas oil after hydrotreatment in the vacuum gas oil, can directly be used as the stock oil of FCC and hydroeracking unit, the HVR that removes most of metal and sulphur can also can some call in the low sulphur fuel oil as the case may be all as the charging of delayed coking unit.
The typical delays coker comprises a process furnace, two coke drums and a separation column at least, and production technique is divided coking and decoking two portions: coking is the continous way operation, and decoking is a batch operation.The operational condition of producing needle coke has very big difference with common Jiao of production, the operational condition of producing needle coke is: 425 ℃～540 ℃ of furnace outlet temperature, 400 ℃～540 ℃ of coke tower top outlet temperature, coke drum pressure 0.05-0.7MPa, recycle ratio 0.3-1.0.The oil gas that separates the coking generation obtains coking dry gas, coker gasoline, coker gas oil, coker gas oil and needle coke, and wherein coker gas oil all loops back hydrotreater.
Below in conjunction with accompanying drawing method provided by the present invention is given further instruction.
Accompanying drawing illustrates the combined technical method flow process of residue hydrogenating and delaying coking, and the shape and size of equipment and pipeline are not subjected to the restriction of accompanying drawing, but determines as the case may be.
Respectively from pipeline 1,2,3,15 residual oil, external coker gas oil, hydrogen, after the round-robin coker gas oil mixes, enter residual hydrogenation equipment 4, the gas (C4-) that generates, petroleum naphtha (C5～180 ℃), diesel oil (180 ℃-350 ℃), vacuum gas oil (350 ℃-538 ℃) is respectively through pipeline 5,6,7,8 go out device, vacuum residuum behind the hydrogenation (＞538 ℃) enters delayed coking unit 11 through pipeline 9 or with other the conventional raw material of producing needle coke from pipeline 10 separately, the coking dry gas that coking generates, coker gasoline, coker gas oil, needle coke is respectively through pipeline 12,13,14,16 go out device, and coker gas oil all returns residual hydrogenation equipment 4 through pipeline 15.
Combined technical method provided by the invention greatly reduces residual hydrogenation equipment charging viscosity by the coker gas oil freshening, makes the residual hydrogenation reaction carry out easily, and residual hydrocracking device quality product under the situation that reactor volume does not increase improves.Light ends oil sulphur, nitrogen content that distillate that hydrogenation generates and coking generate reduce; And energy greatly preparing hihg-quality needle coke, the yield of needle coke is up to 41.5 heavy % (accounting for coking raw material), and the CTE of needle coke is lower than 2.6 * 10
-6/ ℃, the sulphur content of needle coke is less than 0.7 heavy %.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Testing used raw material is vacuum residuum, and its character is listed in table 2; Catalyst system therefor comprises hydrogenation protecting agent RG-1 (by China Petrochemical Corporation's Chang Ling Catalyst Production), HDM catalyzer RF-220 (being produced by Dutch Aksu chemical company), HDS catalyzer RF-1000 (being produced by Dutch Aksu chemical company), and three kinds of catalyst loading volume ratios of said sequence are 5: 45: 50.
Comparative Examples
This Comparative Examples explanation coker gas oil is not to loop back hydrotreater but directly go out device is circulated to the process furnace of coker as catalytic cracking or hydrocracking raw material situation.
Vacuum residuum and the hydrogen of not mixing any coker gas oil are mixed together, in the presence of catalyzer, enter the hydrotreater reaction, separate hydrogenation reaction product and obtain gas, petroleum naphtha, diesel oil, vacuum gas oil and HVR, wherein HVR carries out delayed coking separately, separates the coking product and obtains coking dry gas, coker gasoline, coker gas oil, coker gas oil and common Jiao.Operational condition, material balance and portioned product character see Table 3 respectively, table 4 and table 5.
From table 3 to table 5 as can be seen, vacuum gas oil (350～538 ℃) yield is 21.8 heavy %, and sulphur, nitrogen, basic nitrogen, carbon residue content are respectively 0.55 heavy %, 0.26 heavy %, 550ppm, 0.35 heavy %; The yield of HVR is 56.5 heavy %, and the sulphur of HVR, nitrogen content are respectively 0.85 heavy %, 0.35 heavy %, and carbon residue is 14.0 heavy %, and nickel content is 18.8ppm, and content of vanadium is 38.4ppm.The total liquid of coking is received and is about 69.3 heavy % (accounting for coking raw material); Because the HVR sulphur content is higher, so coking can only go out to be used to produce common Jiao's green coke, and under the listed operational condition of table 3, the yield of green coke is 23.9 heavy % (accounting for coking raw material), and common Jiao's who is produced by this green coke CTE is 5.65 * 10
-6/ ℃, sulphur content is up to 1.01 heavy %.
Embodiment
Vacuum residuum, 20 heavy % coker gas oils (accounting for vacuum residuum) and hydrogen are mixed together, in the presence of catalyzer, enter the hydrotreater reaction, separate gas, petroleum naphtha, diesel oil, vacuum gas oil and HVR that hydrogenation reaction product obtains generating, wherein HVR carries out delayed coking separately, separate the coking product and obtain coking dry gas, coker gasoline, coker gas oil, coker gas oil and needle coke, wherein coker gas oil is circulated to hydrotreater.Operational condition, material balance and portioned product character see Table 3 respectively, table 4 and table 5.
As can be seen from Table 2, the vacuum residuum feed viscosity of mixing behind the coker gas oil significantly reduces, and 100 ℃ of viscosity are from nearly 1300mm
2/ s reduces to 300mm
2About/s.The poor quality of vacuum residuum and coker gas oil shows that the vacuum residuum sulphur content is 4.1 heavy %, the nearly 290ppm of metal (Ni+V) content; The sulphur content of coker gas oil is 3.1 heavy %, and basic n content is more than 1500ppm.
From table 3 and table 5 as can be seen, vacuum gas oil (350～538 ℃) yield is 40.0 heavy %, and vacuum gas oil quality (sulphur, nitrogen, basic nitrogen, carbon residue) increases substantially than the coker gas oil in the raw material, compares with Comparative Examples, also increases; The yield of HVR is 56.6 heavy %, and the total liquid of coking is received and is about 48 heavy % (accounting for coking raw material), and the yield of green coke is about 43 heavy % (accounting for coking raw material), and the CTE of the needle coke of being produced by this green coke is 2.56 * 10
-6/ ℃, the sulphur content of needle coke only is 0.63 heavy %.
Table 2
| Numbering | Comparative Examples | ?????- | Embodiment |
| Stock oil is formed, umber | |||
| Vacuum residuum | ????100 | ????0 | ????100 |
| Coker gas oil | ????0 | ????100 | ????20 |
| Density (20 ℃) gram per centimeter 3 | ????1.0085 | ????0.9616 | ????1.0007 |
| Viscosity (100 ℃) millimeter 2/ second | ????1281 | ????7.152 | ????305 |
| Carbon residue, heavy % | ????20.5 | ????1.12 | ????17.3 |
| Constituent content, heavy % | |||
| Carbon | ????85.05 | ????85.51 | ????85.13 |
| Hydrogen | ????10.36 | ????10.64 | ????10.41 |
| The H/C atomic ratio | ????1.462 | ????1.493 | ????1.467 |
| Sulphur | ????4.1 | ????3.1 | ????3.9 |
| Nitrogen | ????0.49 | ????0.53 | ????0.50 |
| Basic nitrogen, ppm | ????- | ????1539 | ????- |
| Metal content, ppm | |||
| ??Ni | ????70.6 | ????＜0.1 | ????58.8 |
| ??V | ????217 | ????＜0.1 | ????181 |
| Group composition, heavy % | |||
| Stable hydrocarbon | ????14.3 | ????44.8 | ????19.4 |
| Aromatic hydrocarbons | ????48.5 | ????44.0 | ????47.8 |
| Colloid | ????29.7 | ????11.2 | ????26.5 |
| Bituminous matter (C 7Insolubles) | ????7.5 | ????0 | ????6.3 |
Table 3
| Numbering | Comparative Examples | Embodiment |
| Stock oil is formed, umber | ||
| Vacuum residuum | ????100 | ????100 |
| Coker gas oil | ????0 | ????20 |
| Hydroprocessing condition | ||
| The hydrogen dividing potential drop, MPa | ????15.2 | ????15.2 |
| Temperature, ℃ | ????395 | ????395 |
| Volume space velocity, hour -1 | ????0.25 | ????0.30 |
| Hydrogen to oil volume ratio, Nm 3/m 3 | ????1000 | ????1000 |
| The delayed coking condition | ||
| The furnace outlet temperature, ℃ | ????500 | ????500 |
| Coke drum pressure, MPa | ????0.17 | ????0.3 |
| Recycle ratio | ????0.30 | ????0.58 |
Table 4
| Numbering | Comparative Examples | Embodiment |
| The product of hydrotreatment distributes, heavy % | ||
| Gas | ????3.7 | ????4.2 |
| Petroleum naphtha | ????3.1 | ????3.3 |
| Diesel oil | ????16.8 | ????17.8 |
| Vacuum gas oil | ????21.8 | ????40.0 |
| HVR | ????56.5 | ????56.6 |
| Add up to | ????101.9 | ????121.9 |
| The product of delayed coking distributes, heavy % | ||
| The coking dry gas | ????6.8 | ????9.5 |
| Coker gasoline | ????14.7 | ????16.1 |
| Coker gas oil | ????30.6 | ????23.1 |
| Coker gas oil | ????24.0 | ????7.6 |
| Needle coke | ????23.9 | ????42.9 |
| Add up to | ????100.0 | ????100.0 |
Table 5
| Numbering | Comparative Examples | Embodiment |
| Vacuum gas oil | ||
| Density (20 ℃) gram per centimeter 3 | ????0.9280 | ????0.9172 |
| Viscosity (100 ℃) millimeter 2/ second | ????6.0 | ????5.4 |
| Carbon residue, heavy % | ????0.35 | ????0.30 |
| Ni,ppm | ????＜0.1 | ????＜0.1 |
| V,ppm | ????＜0.1 | ????＜0.1 |
| S, heavy % | ????0.55 | ????0.35 |
| N, heavy % | ????0.26 | ????0.25 |
| Basic nitrogen, ppm | ????550 | ????500 |
| HVR | ||
| Density (20 ℃) gram per centimeter 3 | ????0.9831 | ????0.9716 |
| Viscosity (100 ℃) millimeter 2/ second | ????350 | ????250 |
| Carbon residue, heavy % | ????14.0 | ????11.8 |
| Ni,ppm | ????18.8 | ????12.6 |
| V,ppm | ????38.4 | ????21.6 |
| S, heavy % | ????0.85 | ????0.52 |
| N, heavy % | ????0.35 | ????0.29 |
| Coke | Common Jiao | Needle coke |
| Volatile matter, heavy % (green coke) | ????8.8 | ????8.1 |
| Ash content, heavy % | ????0.1 | ????0.04 |
| True density, gram per centimeter 3 | ????2.008 | ????2.129 |
| Sulphur, heavy % | ????1.01 | ????0.63 |
| ?CTE,×10 -6/ ℃ (1000 ℃ of carbon rod sample preparation methods) | ????5.65 | ????2.56 |
Claims (9)
1, a kind of residue hydrogenating and delaying coking combined technical method comprises:
A, residual oil and coker gas oil enter hydrotreater together, carry out hydrogenation reaction in the presence of hydrogen and hydrogenation catalyst;
B, gained hydrogenated residue enter delayed coking unit separately or with other conventional raw material of producing needle coke, carry out heat cracking reaction;
The coker gas oil that C, delayed coking unit obtain all is back to hydrogenation unit.
2, according to the processing method of claim 1, it is characterized in that the residual oil described in the steps A can be long residuum and/or vacuum residuum, also can be long residuum and/or the vacuum residuum that mixes the part lightweight oil.
3,, it is characterized in that described lightweight oil is one or more the mixture that is selected among heavy catalytic cycle oil, fluid catalytic cracking decant oil and the solvent-deasphalted oils according to the processing method of claim 2.
4,, it is characterized in that the described coker gas oil of steps A accounts for 3～35 heavy % of residual oil according to the processing method of claim 1.
5, according to the processing method of claim 1, it is characterized in that the hydrogenation catalyst described in the steps A, its active metal component is selected from nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum, and carrier is selected from aluminum oxide, silicon-dioxide or amorphous aluminum silicide.
6, according to the processing method of claim 1, it is characterized in that the hydrogenation conditions described in the steps A is: hydrogen dividing potential drop 5.0～22.0 MPas, 330～450 ℃ of temperature of reaction, volume space velocity 0.1～3.0 hour
-1, hydrogen and residual oil volume ratio 350～2000Nm
3/ m
3
7,, it is characterized in that other the conventional raw material of producing needle coke described in the step B is selected from fluid catalytic cracking decant oil, thermal cracking residue, lube oil furfural refining and extracts among oil or the preparing ethylene by steam cracking tar one or more mixture out according to the method for claim 1.
8, according to the method for claim 1, the delayed coking operation condition described in the step B that it is characterized in that is: 425 ℃～540 ℃ of furnace outlet temperature, coke drum pressure 0.05～0.7MPa, recycle ratio 0.3～1.0.
9, according to the method for claim 1, it is characterized in that the coker gas oil described in the steps A can be the coker gas oil that obtains among the independent step B, also can be the mixture of the coker gas oil that obtains among the step B and external coker gas oil.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00100879A CN1098336C (en) | 2000-02-18 | 2000-02-18 | Residue hydrogenating and delaying coking combined process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00100879A CN1098336C (en) | 2000-02-18 | 2000-02-18 | Residue hydrogenating and delaying coking combined process |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1309164A true CN1309164A (en) | 2001-08-22 |
| CN1098336C CN1098336C (en) | 2003-01-08 |
Family
ID=4575717
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN00100879A Expired - Lifetime CN1098336C (en) | 2000-02-18 | 2000-02-18 | Residue hydrogenating and delaying coking combined process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1098336C (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1311058C (en) * | 2005-03-09 | 2007-04-18 | 内蒙古远兴天然碱股份有限公司 | Process for producing fuel oil from coal tar |
| CN103059997A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Combined technique of hydrotreating and delay coking of residual oil |
| CN103102986A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and delayed coking for residual oil |
| CN103305271A (en) * | 2013-06-25 | 2013-09-18 | 中石化南京工程有限公司 | Combined process method of lightening residual oil/ medium and low temperature coal tar |
| CN104364353A (en) * | 2012-03-20 | 2015-02-18 | 沙特阿拉伯石油公司 | Integrated hydroprocessing and steam pyrolysis of crude oil to produce light olefins and coke |
| CN104560155A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Coking method |
| US9452955B2 (en) | 2013-03-14 | 2016-09-27 | Lummus Technology Inc. | Process for producing distillate fuels and anode grade coke from vacuum resid |
| CN104364353B (en) * | 2012-03-20 | 2016-11-30 | 沙特阿拉伯石油公司 | Crude oil is carried out integrated hydrogenation process and steam pyrolysis to produce light olefin and coke |
| CN106367113A (en) * | 2015-07-23 | 2017-02-01 | 中国石化扬子石油化工有限公司 | Residual oil hydrotreating method |
| CN111320167A (en) * | 2018-12-13 | 2020-06-23 | 中国石油化工股份有限公司 | Combined process method for producing high-end graphite carbon material |
| CN112708462A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Combined process for treating heavy oil |
| EP3971266A1 (en) | 2020-09-18 | 2022-03-23 | Indian Oil Corporation Limited | A process for production of needle coke |
| CN114426885A (en) * | 2020-09-25 | 2022-05-03 | 中国石油化工股份有限公司 | Method and apparatus for processing residual oil |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1317358C (en) * | 2004-03-31 | 2007-05-23 | 中国石油化工股份有限公司 | Improved delayed coking method |
| CN1323130C (en) * | 2004-03-31 | 2007-06-27 | 中国石油化工股份有限公司 | Hydro-delayed coking method |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4235703A (en) * | 1979-03-27 | 1980-11-25 | Conoco, Inc. | Method for producing premium coke from residual oil |
| JP2825248B2 (en) * | 1988-12-28 | 1998-11-18 | 株式会社東芝 | Fluid compressor |
| CN1029626C (en) * | 1991-04-01 | 1995-08-30 | 中国石油化工总公司石油化工科学研究院 | Method for manufacturing superhigh viscosity index base oil for lubricating oil |
-
2000
- 2000-02-18 CN CN00100879A patent/CN1098336C/en not_active Expired - Lifetime
Cited By (23)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1311058C (en) * | 2005-03-09 | 2007-04-18 | 内蒙古远兴天然碱股份有限公司 | Process for producing fuel oil from coal tar |
| CN103059997A (en) * | 2011-10-21 | 2013-04-24 | 中国石油化工股份有限公司 | Combined technique of hydrotreating and delay coking of residual oil |
| CN103059997B (en) * | 2011-10-21 | 2014-08-20 | 中国石油化工股份有限公司 | Combined technique of hydrotreating and delay coking of residual oil |
| CN103102986A (en) * | 2011-11-10 | 2013-05-15 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and delayed coking for residual oil |
| CN103102986B (en) * | 2011-11-10 | 2015-05-13 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and delayed coking for residual oil |
| CN104364353B (en) * | 2012-03-20 | 2016-11-30 | 沙特阿拉伯石油公司 | Crude oil is carried out integrated hydrogenation process and steam pyrolysis to produce light olefin and coke |
| CN104364353A (en) * | 2012-03-20 | 2015-02-18 | 沙特阿拉伯石油公司 | Integrated hydroprocessing and steam pyrolysis of crude oil to produce light olefins and coke |
| US9228139B2 (en) | 2012-03-20 | 2016-01-05 | Saudi Arabian Oil Company | Integrated hydroprocessing and steam pyrolysis of crude oil to produce light olefins and coke |
| CN105164233B (en) * | 2013-03-14 | 2017-07-04 | 鲁姆斯科技公司 | Cut oil fuel and the burnt method of anode grade are produced from decompression residuum |
| US9452955B2 (en) | 2013-03-14 | 2016-09-27 | Lummus Technology Inc. | Process for producing distillate fuels and anode grade coke from vacuum resid |
| CN103305271A (en) * | 2013-06-25 | 2013-09-18 | 中石化南京工程有限公司 | Combined process method of lightening residual oil/ medium and low temperature coal tar |
| CN103305271B (en) * | 2013-06-25 | 2015-10-21 | 中石化南京工程有限公司 | The combined technical method of a kind of residual oil/middle coalite tar lighting |
| CN104560155B (en) * | 2013-10-23 | 2016-08-17 | 中国石油化工股份有限公司 | A kind of coking method |
| CN104560155A (en) * | 2013-10-23 | 2015-04-29 | 中国石油化工股份有限公司 | Coking method |
| CN106367113A (en) * | 2015-07-23 | 2017-02-01 | 中国石化扬子石油化工有限公司 | Residual oil hydrotreating method |
| CN111320167A (en) * | 2018-12-13 | 2020-06-23 | 中国石油化工股份有限公司 | Combined process method for producing high-end graphite carbon material |
| CN111320167B (en) * | 2018-12-13 | 2023-09-01 | 中国石油化工股份有限公司 | Combined process method for producing high-end graphite carbon material |
| CN112708462A (en) * | 2019-10-25 | 2021-04-27 | 中国石油化工股份有限公司 | Combined process for treating heavy oil |
| CN112708462B (en) * | 2019-10-25 | 2022-09-23 | 中国石油化工股份有限公司 | Combined process for treating heavy oil |
| EP3971266A1 (en) | 2020-09-18 | 2022-03-23 | Indian Oil Corporation Limited | A process for production of needle coke |
| US11788013B2 (en) | 2020-09-18 | 2023-10-17 | Indian Oil Corporation Limited | Process for production of needle coke |
| CN114426885A (en) * | 2020-09-25 | 2022-05-03 | 中国石油化工股份有限公司 | Method and apparatus for processing residual oil |
| CN114426885B (en) * | 2020-09-25 | 2023-09-05 | 中国石油化工股份有限公司 | Method and device for processing residual oil |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1098336C (en) | 2003-01-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1165601C (en) | Process for hydrogenating residual oil and catalytically cracking heavy oil | |
| CN1098336C (en) | Residue hydrogenating and delaying coking combined process | |
| CN101942332A (en) | Method for hydrotreating heavy hydrocarbon | |
| CN103102986B (en) | Combined process of hydrotreatment and delayed coking for residual oil | |
| CN1119397C (en) | Hydrogenation and catalystic cracking combined process for residual oil | |
| CN1191321C (en) | Process for preparing acicular petroleum coke from S-contained ordinary-pressure residual oil | |
| CN102899082A (en) | Catalyst grading method in coal tar hydrofining process | |
| EP0640678A2 (en) | Process for hydrotreating heavy hydrocarbon oil | |
| CN111378470B (en) | Residual oil hydrodemetallization treatment method | |
| CN111378469B (en) | Residual oil hydrodemetallization method | |
| CN112708462B (en) | Combined process for treating heavy oil | |
| CN111378472B (en) | Method for removing metal impurities in residual oil by hydrogenation | |
| CN115491232B (en) | Method for producing ultralow-sulfur marine fuel oil by low-pressure hydrogenation of heavy inferior residual oil | |
| CN112342059B (en) | Method for blending catalytic cracking slurry oil in delayed coking unit | |
| CN1117071A (en) | Process for the conversion of a residual hydrocarbon oil | |
| CN115895718B (en) | Deoiling asphalt hydrocracking treatment method | |
| CN113930255B (en) | Hydrogenation method for producing chemical raw materials from crude oil | |
| CN113563921B (en) | Method and system for producing low-sulfur petroleum coke | |
| RU2723625C1 (en) | Method for catalytic hydroforming of gas condensate residue | |
| CN109988634B (en) | Residual oil hydrotreating and hydrofining combined process | |
| CN116023995A (en) | Method for producing low-sulfur petroleum coke | |
| CN114426881A (en) | Residual oil hydrogenation method | |
| CN116024005A (en) | Residual oil processing method | |
| CN116024006A (en) | Hydrocracking method of deasphalted oil | |
| CN114437795A (en) | Method and system for processing heavy oil |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |