CN1202212C - Heavy hydrocarbon hydroprocessing method - Google Patents
Heavy hydrocarbon hydroprocessing method Download PDFInfo
- Publication number
- CN1202212C CN1202212C CN 02133138 CN02133138A CN1202212C CN 1202212 C CN1202212 C CN 1202212C CN 02133138 CN02133138 CN 02133138 CN 02133138 A CN02133138 A CN 02133138A CN 1202212 C CN1202212 C CN 1202212C
- Authority
- CN
- China
- Prior art keywords
- oil
- hydrogenation
- present
- residual
- bed layer
- 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.)
- Expired - Lifetime
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention discloses a hydrogenation method for heavy hydrocarbon. Residual oil raw materials respectively pass through a protective agent bed layer, a hydrodematalization catalyst bed layer, a hydrodesulfurization catalyst bed layer and a hydrodenitro-genation (cracking) catalyst bed layer, and deasphalted oil and/or coking wax oil are led behind the protective agent bed layer and before the hydrodesulfurization catallst bed layer. Compared with the prior art, the method of the present invention effectively makes use of the activity of high activated catalysts, such as hydrodesulfurization, hydrodenitrogenation and/or hydrocracking, etc., and various functional catalysts of residual oil hydrogenation processing devices can evenly deactivated. The present invention decreases the operating cost of the hydrogenation catalysts and processes deasphalted oil and coking wax oil, so the deasphalted oil and the coking wax oil can carry out light device processes, such as down hydrogenation of processing stream catalytic cracking or hydrocracking, etc., and the present invention reduces the reconstruction of the hydrogenation processing devices. The method of the present invention is mainly used for the hydrotreatment of the residual oil, deasphalted oil and the coking wax oil.
Description
1, technical field
The present invention relates to the hydrocarbons hydrogenation treatment technology.In particular, relate to a kind of technology of the common hydrotreatment of different heavy hydrocarbon kind of raw materials.
2, background technology
Along with crude oil becomes heavy day by day, becomes bad, more and more heavy, residual oil needs processing treatment.Processing treatment heavy, residual oil will be not lower boiling product with its cracking still, as petroleum naphtha, intermediate oil and vacuum gas oil, but also will improve their hydrogen-carbon ratio, and this just need realize by the method for decarburization or hydrogenation.Wherein decarbonization process comprises coking, solvent deasphalting, heavy oil fluid catalytic cracking etc.; Hydrogenation comprises hydrocracking, hydrofining etc.Hydrogenation method can hydrocracking residual oil, improves the productive rate of liquid product, and can also remove heteroatoms wherein, and quality product is not bad.But hydrogenation method is the catalysis complete processing, has hydrogenation catalyst inactivation problem, and when especially processing poor quality, heavier hydrocarbon feeds, the catalyst deactivation problem is more serious.In order to reduce heavy, poor residuum cost of processing, increase the oil refining enterprise profit.At present, the technology of processing more heavy, poor residuum is still based on decarbonization process, but its poor product quality, need carry out aftertreatment could utilize, wherein deasphalted oil and wax tailings cut especially need to carry out hydrotreatment, could continue to use lighting devices such as catalytic cracking or hydrocracking to process, therefore, each oil refining enterprise all has the hydrotreater of deasphalted oil and wax tailings in addition.
Slag oil cracking rate heavy, the residual hydrocracking technology is lower, and main purpose is to supply raw materials for downstream raw material lighting device such as devices such as catalytic cracking or coking.By hydrotreatment, sulphur, nitrogen, metal impurities content and carbon residue in the poor residuum are obviously reduced, thereby obtain the charging that raw material lighting device in downstream can receive, especially be mainstream technology with residue fixed-bed hydrotreatment-RFCC combination technique in the catalytic cracking unit, therefore heavy at present, residual hydrogenation residua upgrading Technology.US4,713,221 disclose on the residual hydrogenation of routine and catalytic cracking combined basis, and the heavy cycle oil of catalytic cracking (comprising wax catalysis cracking and recycle stock catalytic cracking) is circulated to residual hydrogenation equipment, with carry out hydrogenation after residual oil mixes, enter catalytic cracking unit again.But this technology has only been considered the lighting of the treatable residual oil of residual hydrocracking device, improve profit by the yield that utilizes catalytic cracking turning oil to increase light oil, and do not consider the handling problem of poor residuum more, just do not consider handicraft product utilizations such as decarburization yet.
The more employing fixed-bed reactor of residual hydrocracking technology; the catalyzer of difference in functionality is divided in different reactors or the different bed; general residual oil raw material is earlier by protective material, metal remover, more successively by Hydrobon catalyst, hydrodenitrogenation catalyst and/or hydrocracking catalyst.The catalyst activity difference of difference in functionality, its deactivation rate are also different.Protective material and metal remover activity are lower, and its major function is to remove metal in the residual oil raw material, easy coking component, with and the solid particulate that carries, so these two kinds of catalyst deactivation rate are very fast.And the hydrogenating desulfurization in its downstream, hydrodenitrification and/or hydrocracking catalyst is active higher, and its major function is to remove impurity such as sulphur in the residual oil raw material, nitrogen, and transforms residual oil raw material, so their deactivation rate is lower than protective material and metal remover.The unbalanced inactivation of the above-mentioned all kinds of catalyzer of result, when treating that hydrogenation unit changes agent, hydrogenating desulfurization, hydrodenitrification and hydrocracking still have activity, especially hydrodenitrification and/or hydrocracking, cause the catalyst activity waste, reduced refinery's profit, this point is industrial to be proved.
3, summary of the invention
Purpose of the present invention is exactly the deficiency that remedies above-mentioned Technology, develops a kind of activity that promptly makes full use of hydrogenation catalyst, can handle the heavy distillate of decarbonization process again, and they can be processed on catalytic cracking or hydroeracking unit.
Processing method provided by the invention may further comprise the steps:
A, residual oil raw material and recycle hydrogen are mixed into the heavy-oil hydrogenation treatment unit; successively by protective material bed, Hydrodemetalation catalyst bed, Hydrobon catalyst bed and hydrodenitrification (conversion) beds; (hydrogen make-up can be arranged with deasphalted oil and/or the wax tailings after the protective material bed and before the Hydrobon catalyst bed, introduced; can not have yet) converge common each beds that passes through the downstream successively.The introducing position of deasphalted oil and/or wax tailings is preferably in after the partial hydrogenation catalyst for demetalation bed, as introducing after 50% Hydrodemetalation catalyst bed.
B, reaction finish, and reactant flow is separated, and isolates hydrogen-rich gas and liquid phase hydro carbons.
C, isolated liquid phase hydro carbons further separates in B, continues the difference of lighting device at the downstream, isolates normal slag of petroleum naphtha, intermediate oil and hydrogenation or vacuum gas oil and hydrogenation and subtracts slag etc.Make downstream lighting device such as catalytic cracking, coking, hydrocracking or lube oil hydrogenation device etc. continue processing; Isolated hydrogen-rich gas then carries out washing, purifying, purifies and return the reactive system of hydrogenation unit again.
Compared with prior art, the characteristics of hydrogenation technique of the present invention have: (1) has effectively utilized the activity of high activated catalysts such as hydrogenating desulfurization, hydrodenitrification and/or hydrocracking, make the balanced inactivation of each function catalyzer of residual hydrocracking device, reduce the hydrogenation catalyst running cost.(2) hydrotreatment of residual hydrocracking device maximum capacity deasphalted oil and wax tailings, make it to carry out lighting devices such as downstream catalytic cracking or hydrocracking and handle, reduce reproducing of hydrotreater, for having saved the capital construction cost in the refinery.
4, description of drawings
Fig. 1 is the simple and easy schematic flow sheet of the embodiment of the invention, and Fig. 2 is a comparative example schematic flow sheet of the present invention.
5, embodiment
Specify the present invention program and effect below in conjunction with accompanying drawing.As shown in Figure 1; residual oil raw material 1 mixes with recycle hydrogen 8; enter the reactive system of hydrogenation unit jointly; order is by protective material and partial hydrogenation catalyst for demetalation 2 at least, mixes jointly with deasphalted oil and/or wax tailings 11 and hydrogen make-up 12 and carries out hydroconversion reactions by hydrogenating desulfurization, hydrodenitrification and/or hydrocracking catalyst bed 3 and 4 successively.After reaction finished, resultant of reaction entered separation system 5, is separated into hydrogen-rich gas 7 and liquid phase hydro carbons 6.Hydrogen-rich gas 7 mixes with residual oil raw material 1 after boosting through washing, purifying, purification system 9 and recycle compressor 10, Returning reacting system again, liquid phase hydro carbons 6 is then pressed the difference of downstream lighting device, carry out different fractionation cuttings, generally be that normal slag of gas, petroleum naphtha, intermediate oil and hydrogenation or vacuum gas oil and hydrogenation subtract slag etc. with its fractionation, so that vacuum gas oil fraction is carried out hydrocracking or produced lubricant base, residue oil fraction can carry out catalytic cracking and/or coking.
The prior art scheme as shown in Figure 2, residual oil raw material 1 mixes with recycle hydrogen 8, enters the reactive system of hydrogenation unit jointly, the order carry out hydroconversion reactions by hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification and/or hydrocracking catalyst bed 2,3 and 4.After reaction finished, resultant of reaction entered separation system 5, is separated into hydrogen-rich gas 7 and liquid phase hydro carbons 6.Hydrogen-rich gas 7 mixes with residual oil raw material 1 after boosting through washing, purifying, purification system 9 and recycle compressor 10, Returning reacting system again, liquid phase hydro carbons 6 is then pressed the difference of downstream lighting device, carry out different fractionation cuttings, generally be that normal slag of gas, petroleum naphtha, intermediate oil and hydrogenation or vacuum gas oil and hydrogenation subtract slag etc. with its fractionation, so that vacuum gas oil fraction is carried out hydrocracking or produced lubricant base, residue oil fraction can carry out catalytic cracking and/or coking.
Heavy, residual hydrocracking technology of the present invention can be suitable for any Residue Hydrotreating Technology technology, as fixed bed residual hydrogenation technology, boiling bed residual oil hydrogen addition technology, expanded bed residual hydrogenation technology, moving-bed residual hydrogenation technology., residual hydrogenation technology heavy with at present industrial more ripe fixed bed is example: the heavy residual oil hydrocatalyst of employing is meant the single catalyst or the combination catalyst of functions such as having weight, residuum hydrogenating and metal-eliminating, hydrogenating desulfurization, hydrodenitrification and hydrocracking.These catalyzer generally all are to be carrier with porous refractory inorganic oxides such as aluminum oxide, the oxide compound of group vib and/or VIII family metal such as W, Mo, Co, Ni etc. is an active ingredient, the catalyzer that optionally adds other various auxiliary agents such as P, Si, elements such as F, B, for example CEN, the FZC series of being produced by Fushun new and high-tech development zone weighs, residuum hydrogenating and metal-eliminating catalyst, and ZTN, the ZTS catalyst series produced by first fertilizer plant of Qilu Petrochemical company just belong to this class catalyzer.At present in fixed bed residual hydrogenation technology; it often is the supporting use of multiple catalyzer; protective material, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogenation catalyst are wherein arranged, and the filling order generally is that stock oil is contacted with protective material, hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrification, hydrocracking catalyst successively.Technology with these several catalyst mix fillings is also arranged certainly.Be 5MPa-35MPa in absolute pressure normally, preferably 10MPa-20MPa, temperature are 300 ℃-500 ℃, preferably 350 ℃-450 ℃ operations down.Volume space velocity and hydrogen dividing potential drop are to select according to the characteristic for the treatment of material and the transformation efficiency and the refining depth of requirement during liquid.Volume space velocity is generally at 0.1h during residual oil raw material liquid
-1-5.0h
-1, 0.15h preferably
-1-2h
-1Scope in, volume space velocity is generally at 0.02h when deasphalted oil and/or wax tailings liquid
-1-1.0h
-1, 0.05h preferably
-1-0.5h
-1Scope in.Total hydrogen to oil volume ratio is 100-5000, is preferably 300-3000.The present invention is applicable to normal pressure and vacuum residuum hydrotreatment, is particularly useful for the hydrocracking of heavy hydrocarbon oil.
Embodiment 1-3
Present embodiment with the residue fixed-bed example that is hydrogenated to, carries out the present invention's test on pilot scale residual hydrocracking device.The residue fixed-bed hydrogenation catalyst that uses in the test is heavy, the residuum hydrogenating and metal-eliminating catalyst of being produced by Fushun new and high-tech development zone of CEN, FZC series, by ZTN, ZTS series weight, residual hydrogenation denitrogenation, the desulfurization catalyst of first fertilizer plant of Qilu Petrochemical company production.The order of catalyst loading is hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrogenation catalyst.That hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrogenation catalyst are seated in respectively is one anti-, two anti-and three anti-.The Hydrodemetalation catalyst that uses in this test is CEN-5, CEN-6; Protective material is CEN-2, CEN-4, FZC-16 (over current protection agent); Hydrobon catalyst ZTS-01, ZTS-02, ZTS-03; Hydrodenitrogenation catalyst ZTN-01.Admission space ratio between each catalyzer is:
CEN-2∶FZC-16∶CEN-4∶CEN-5∶CEN-6∶ZTS-01∶ZTS-02∶ZTS-03∶ZTN-01＝1∶1.25∶1.5∶2.62∶7.8∶6.63∶0.69∶0.87∶11(V/V)。
The residual oil raw material oil that this test is used is Middle East residual oil, and the decarbonization process distillate is a wax tailings, and its character sees Table 1.Volume space velocity is 0.22h when stablizing residual oil liquid
-1, test-results sees Table-2.
Table 1 stock oil main character
| Project | Residual oil | Wax tailings |
| Density (20 ℃), g/cm 3 | 1.018 | 0.8866 |
| Cut, ℃ | 538℃ + | 349℃-538℃ |
| Elementary composition | ||
| S，w％ | 4.24 | 0.86 |
| N，w％ | 0.33 | 0.23 |
| Carbon residue, w% | 20.2 | 0.13 |
| Ni+V，μg/g | 120.3 | / |
Table 2 residual hydrocracking result of the present invention
| Embodiment | 1 | 2 | 3 |
| Operational condition | |||
| Reaction pressure, MPa | 16.0 | ||
| Temperature of reaction, ℃ | 385 | ||
| Hydrogen-oil ratio, V/V | 761∶1 | ||
| Volume space velocity during wax tailings liquid, h -1 | 0.03 | 0.06 | 0.1 |
| Product distributes | |||
| 160℃-349℃ | 12.36 | 12.23 | 11.96 |
| 349℃-538℃ | 52.78 | 55.65 | 60.03 |
| 538℃ + | 31.87 | 24.08 | 18.69 |
| 349 ℃-538 ℃ generate oil nature | |||
| Density (20 ℃), g/cm 3 | 0.875 | 0.8866 | 0.8862 |
| S，w％ | 0.10 | 0.09 | 0.09 |
| N，w％ | 0.049 | 0.045 | 0.043 |
| Carbon residue, w% | 0.02 | 0.02 | 0.01 |
| 349℃ +Generate oil nature | |||
| Density (20 ℃), g/cm 3 | 0.9172 | 0.9138 | 0.9011 |
| S，w％ | 0.39 | 0.36 | 0.29 |
| N，w％ | 0.11 | 0.0962 | 0.0867 |
| Carbon residue, w% | 3.47 | 3.16 | 2.89 |
| Ni +V，μg/g | 11.2 | 10.1 | 9.2 |
Comparative example 1
This comparative example with the residue fixed-bed example that is hydrogenated to, carries out traditional Residue Hydrotreating Technology test and is used for comparison on pilot scale residual hydrocracking device.The used same embodiment of catalyzer, stock oil, test conditions in the test, test-results sees Table-3.
Table-3 residual hydrocracking results of the present invention
| Reaction pressure, MPa | 16.0 | |
| Temperature of reaction, ℃ | 385 | |
| Hydrogen-oil ratio, V/V | 761∶1 | |
| Volume space velocity during residual oil liquid, h -1 | 0.22 | |
| Product distributes | ||
| 160℃-349℃ | 17.37 | |
| 349℃-538℃ | 41.10 | |
| 538℃ + | 36.81 | |
| Product property | ||
| Project | 349℃-538℃ | 349℃ + |
| Density (20 ℃), g/cm 3 | 0.8832 | 0.9203 |
| S，w％ | 0.12 | 0.41 |
| N，w％ | 0.0455 | 0.12 |
| Carbon residue, w% | 0.02 | 3.98 |
| Ni+V，μg/g | / | 14.6 |
By table-2 and table-3 as seen,, wax tailings treatment effect of the present invention is good, can satisfy the use of downstream lighting device, in addition, and 349 ℃
+Residual oil character also is better than traditional residual hydrocracking Technology, and 538 ℃
+The transformation efficiency of residual oil also is higher than traditional residual hydrocracking Technology.
Embodiment 4～6 and comparative example 2
Present embodiment and comparative example are used to investigate the balanced inactivation situation of catalyzer, and raw materials used oil, catalyzer and reaction conditions are with embodiment 1～3.Satisfy with hydrogenation long residuum character: S is not more than 0.45w%, N and is not more than 0.15w%, CCR and is not more than 4.0w% and Ni+V to be not more than 15.0 μ g/g be object run.Test-results sees Table-4.
Table-4 test-results
| Embodiment | 4 | 5 | 6 | Comparative example 2 |
| Runtime, h | 4000 | |||
| Volume space velocity during residual oil liquid, h -1 | 0.22 | 0.22 | 0.22 | 0.22 |
| Volume space velocity during wax tailings liquid, h -1 | 0.03 | 0.06 | 0.1 | 0 |
| The pressure of desulfurization catalyst bed falls, MPa | 0.23 | 0.21 | 0.20 | 0.35 |
| The pressure of denitrification catalyst bed falls, MPa | 0.21 | 0.19 | 0.18 | 0.28 |
| The desulfurization catalyst bed temperature, ℃ | 388 | 386 | 385 | 391 |
| The denitrification catalyst bed temperature, ℃ | 394 | 392 | 390 | 399 |
By table-4 as seen, the bed pressure drop of desulfurization of the present invention and denitrification catalyst bed and temperature of reaction are lower than prior art with the prolongation increase amplitude of runtime.The desulfurization catalyst bed pressure drop and the temperature increasing degree that more are apparent that prior art are far longer than the denitrification catalyst bed, present the trend that the desulfurization catalyst deactivation rate is far longer than the denitrification catalyst deactivation rate, finally can cause desulfurization catalyst early than denitrification catalyst inactivation, influence device running period.
Claims (5)
1, a kind of heavy hydrocarbon hydroprocessing process; in the presence of heavy hydrocarbon hydroprocessing condition and hydrogen; residual oil raw material is passed through protective material bed, Hydrodemetalation catalyst bed, Hydrobon catalyst bed, hydrodenitrogenation catalyst bed successively; it is characterized in that behind the protective material bed and the Hydrobon catalyst bed before introduce deasphalted oil and/or wax tailings, volume space velocity is 0.02h during the liquid of deasphalted oil and/or wax tailings
-1-1.0h
-1
2, in accordance with the method for claim 1, it is characterized in that the introducing position of described deasphalted oil and/or wax tailings is after partial hydrogenation catalyst for demetalation bed.
3, according to claim 1 or 2 described methods, it is characterized in that described heavy hydrocarbon hydroprocessing condition is: absolute pressure is 5MPa-35MPa, and temperature is 300 ℃-500 ℃, and volume space velocity is 0.1h during residual oil raw material liquid
-1-5.0h
-1, total hydrogen to oil volume ratio is 100-5000.
Volume space velocity is 0.05h when 4, in accordance with the method for claim 1, it is characterized in that described deasphalted oil and/or wax tailings liquid
-1-0.5h
-1
5, according to claim 1 or 2 described methods, it is characterized in that described heavy hydrocarbon hydroprocessing condition is: absolute pressure is 10MPa-20Mpa, and temperature is 350 ℃-450 ℃, and volume space velocity is 0.15h during residual oil raw material liquid
-1-2h
-1, total hydrogen to oil volume ratio is 300-3000.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02133138 CN1202212C (en) | 2002-10-10 | 2002-10-10 | Heavy hydrocarbon hydroprocessing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02133138 CN1202212C (en) | 2002-10-10 | 2002-10-10 | Heavy hydrocarbon hydroprocessing method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1488719A CN1488719A (en) | 2004-04-14 |
| CN1202212C true CN1202212C (en) | 2005-05-18 |
Family
ID=34145472
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02133138 Expired - Lifetime CN1202212C (en) | 2002-10-10 | 2002-10-10 | Heavy hydrocarbon hydroprocessing method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1202212C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8758565B2 (en) | 2006-01-17 | 2014-06-24 | International Paper Company | Paper substrates containing high surface sizing and low internal sizing and having high dimensional stability |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101191077B (en) * | 2006-11-22 | 2011-09-14 | 中国石油化工股份有限公司 | Hydrogenation deacidification method for acid-containing crude oil |
| CN101987967B (en) * | 2009-07-30 | 2013-11-27 | 中国石油化工股份有限公司 | Hydrotreatment method of deep vacuum distillation wax oil |
| CN102041042B (en) * | 2009-10-22 | 2013-07-31 | 中国石油天然气股份有限公司 | Method for hydrotreating inferior coker gatch |
| CN101967395A (en) * | 2010-10-18 | 2011-02-09 | 李湘平 | Method for producing clean fuel by hydrogenation of mixed oil |
| CN102485843B (en) * | 2010-12-03 | 2013-11-06 | 中国石油天然气股份有限公司 | Method for removing nitride from inferior wax oil |
| CN102816599A (en) * | 2011-06-10 | 2012-12-12 | 中国石油天然气股份有限公司 | Residual oil hydrotreating combined process |
| CN102816592A (en) * | 2011-06-10 | 2012-12-12 | 中国石油天然气股份有限公司 | Method for improving reactivity of residual oil hydrotreater |
| CN102816597A (en) * | 2011-06-10 | 2012-12-12 | 中国石油天然气股份有限公司 | Residual oil hydrotreating process |
| CN102816593A (en) * | 2011-06-10 | 2012-12-12 | 中国石油天然气股份有限公司 | Method for decreasing catalyst carbon deposit of residual oil hydrotreater |
| CN102952579B (en) * | 2011-08-26 | 2015-11-18 | 中国石油天然气股份有限公司 | Improve the inferior heavy oil hydroprocessing technique of catalyst utilization to greatest extent |
| CN105524655B (en) * | 2014-10-24 | 2017-02-15 | 中国石油化工股份有限公司 | Heavy oil hydrodenitrogenation method |
| CN106554812B (en) * | 2015-09-30 | 2019-11-15 | 中国石油化工股份有限公司 | A kind of method that fixed bed residual hydrogenation mixes refining wax tailings |
-
2002
- 2002-10-10 CN CN 02133138 patent/CN1202212C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8758565B2 (en) | 2006-01-17 | 2014-06-24 | International Paper Company | Paper substrates containing high surface sizing and low internal sizing and having high dimensional stability |
| US9309626B2 (en) | 2006-01-17 | 2016-04-12 | International Paper Company | Paper substrates containing high surface sizing and low internal sizing and having high dimensional stability |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1488719A (en) | 2004-04-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP6106354B2 (en) | Process for hydrocracking feedstock containing 200 wtppm to 2 wt% asphaltenes, including a switchable reactor | |
| CA2896247C (en) | Intergration of residue hydrocracking and solvent deasphalting | |
| CN101942332A (en) | Method for hydrotreating heavy hydrocarbon | |
| CN1202212C (en) | Heavy hydrocarbon hydroprocessing method | |
| CN104611047A (en) | Process method for producing lubricating oil base oil through poor-quality raw material | |
| CN108018084B (en) | Heavy oil hydrotreating method for improving catalyst utilization rate | |
| CN108018074B (en) | Heavy oil hydrotreating method for improving catalyst utilization rate | |
| CN101434867B (en) | Suspension bed residual oil hydrogenation-catalytic cracking combined technological process | |
| CN103059974B (en) | Hydrotreatment method for producing food grade solvent naphtha | |
| CN104611014B (en) | Two-stage hydrotreating method of poor-quality raw material | |
| CN110408429B (en) | Method for treating heavy oil by combined process | |
| US6447673B1 (en) | Hydrofining process | |
| CN110408431B (en) | Method for treating inferior oil product by combined process | |
| CN103102981A (en) | Treating method for heavy raw material | |
| CN103131470B (en) | Fixed bed residue oil hydrotreating method | |
| CN1144863C (en) | Heavy hydrocarbon feeding and hydrogenating process | |
| CN1362478A (en) | Heavy hydrocarbon hydroprocessing technique | |
| CN1211467C (en) | Hydrocarbon hydroconversion method | |
| CN113214862A (en) | Heavy oil supercritical/subcritical fluid enhanced hydrogenation method | |
| CN104611052B (en) | Inferior raw material two-stage hydrogenation processing method | |
| CN104611009B (en) | Poor-quality heavy distillate oil hydrotreating method | |
| CN104611055B (en) | A kind of height does raw material two-stage hydrogenation processing method | |
| CN110408428B (en) | Method for treating residual oil by combined process | |
| CN1162520C (en) | Heavy oil and residual oil hydrogenating modification and combination process | |
| CN104611036B (en) | A kind of height does heavy distillate oil hydrotreating method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20050518 |