CN102465020B - Combined hydrofining method - Google Patents
Combined hydrofining method Download PDFInfo
- Publication number
- CN102465020B CN102465020B CN201010539545.1A CN201010539545A CN102465020B CN 102465020 B CN102465020 B CN 102465020B CN 201010539545 A CN201010539545 A CN 201010539545A CN 102465020 B CN102465020 B CN 102465020B
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- unionfining
- oil
- hydrogenation
- reaction
- 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.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a combined hydrofining method, which comprises: mixing reforming prehydrogenation raw oil with hydrogen fully, passing the mixture through a heating furnace, and putting the mixture in a hydrogenation reactor for desulphurization and denitrification reactions; separating the reforming prehydrogenation raw oil and the hydrogen in a separator, with the obtained refined oil able to satisfy the quality requirements of reforming feedstocks; mixing a hydrogen rich gas with the catalytic heavy gasoline hydrogenation raw material directly, passing the mixture through a heating furnace and subjecting the mixture to hydrogenation reaction in a reactor, and mixing the refined oil with catalytic light gasoline so as to obtain gasoline able to satisfy the quality index requirements of clean gasoline vehicles. The method of the invention can meet the demands of producing qualified products simultaneously by two hydrogenation units, and has the advantages of simple process, no need for circulating hydrogen compressor or new hydrogen compressor, low investment and operation cost, good product property, and stable operation, etc.
Description
Technical field
The present invention relates to a kind of Unionfining method, particularly a kind of reformed pre-hydrogenated processing method of combining with catalytic gasoline selective hydrogenation device.
Background technology
Reformed pre-hydrogenated device and catalytic gasoline selective hydrogenation device are put hydrogenation common in oil refining enterprise.Reformed pre-hydrogenated device is mainly for reformer provides qualified charging, and catalytic gasoline selective hydrogenation device is mainly to produce clean motor spirit blend component.Because the purposes difference of two covering devices is larger, therefore oil refining enterprise separately builds two covering devices conventionally at present.But reformed pre-hydrogenated device and catalytic gasoline hydrogenation unit are no matter in technical process, or operational condition is all very similar, the catalyzer using is also essentially identical, if by this two covers hydrogenation unit composition Unionfining device, in plant investment and process cost, all can reduce significantly, and not affect quality product separately.
Constantly soaring along with International Crude Oil, and improving constantly that fuel oil quality is required, cause oil refining enterprise's cost more and more higher, and enterprise faces serious survival pressure.Therefore, how reducing oil refining cost is the problem of current extensive concern.Can consider from the purchasing of raw materials and plant investment and process cost two portions and reduce costs mainly.So, the better method of reduction oil refining cost while reducing plant investment and operational cost.
In existing Unionfining technology main adopt high-tension unit and in, the production method of low pressure hydrogenation unit associating.The mode that for example newly-built ten million ton of Refinery Projects of Sinopec Plant of Tianjin Petrochemical Company branch office adopts diesel oil hydrogenation to combine with kerosene hydrogenation, main purpose is that kerosene hydrogenation device can utilize the unnecessary thermal source of diesel hydrotreating unit, to reach energy-conservation object.Domestic other newly-built Refinery Projects, as petrochemical industry is combined in Fujian, Qingdao great oil refining project has also all designed Unionfining device, have been obtained good effect from the condition of production.But these methods are owing to being the hydrogenation unit that pressure rating is different, so the investment of machinery and process cost obviously do not reduce at present.
CN100448956C discloses a kind of Unionfining technological process.The new hydrogen of the method utilization carries out deep hydrofinishing to poor quality boat coal cut, and the hydrogen-rich gas in effluent is as the hydrogen make-up of H-G hydrocracking; Utilize method for hydrogen cracking to process poor ignition quality fuel, the poor ignition quality fuel in effluent recycles.Adopt this inventive method hydro-refining unit can obtain high quality boat product of coal and hydroeracking unit can obtain clean diesel cut, and can by-product part high-quality boat coal and the petroleum naphtha of Gao Fangqian.Due to technical process be low pressure to high pressure, some necessary equipment not do not reduce, as supercharger etc.So the cost of investment of reduction and running cost amplitude are limited.
CN101412924A discloses a kind of Unionfining technological process, the Unionfining technological process of particularly wax oil hydrogenation processing, diesel oil hydrogenation modification, diesel oil hydrofining.This processing method, taking wax oil and poor ignition quality fuel as raw material, is divided into three reaction zones, although can produce quality products, technical process is comparatively complicated.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of Unionfining method, the inventive method technical process is simpler, without circulating hydrogen compressor and make-up hydrogen compressor, has investment and process cost low, and product property is good, the advantages such as stable operation.
Unionfining technological process of the present invention comprises following content:
(1) reformed pre-hydrogenated stock oil fully mix with hydrogen after through process furnace, enter hydrogenator and react;
(2) reaction effluent of step (1) enters separator and carries out gas-liquid separation, and hydrogen-rich gas directly mixes with catalysis heavy petrol hydrogenating materials is oily, enters reactor carry out hydrogenation reaction through process furnace;
(3) reaction effluent of step (2) carries out gas-liquid separation, and product liquid is mixed to get cleaning cart gasoline products with catalytic light gasoline after air lift.Remaining hydrogen can directly use as the hydrogen make-up of other hydrogenation units, or returns to hydrogen pipe network.
In Unionfining technological process of the present invention, the processing condition of two cover hydrogenation units are close, if volume space velocity is all at 4.0h
-1left and right, working pressure can finely mate.Therefore, composition Unionfining device is very applicable, and all without circulating hydrogen compressor and make-up hydrogen compressor, can significantly reduce cost of investment.
According to Unionfining technological process of the present invention, wherein the hydrogen described in step (1) is the new hydrogen of pipe network.
In Unionfining method of the present invention, technical process can adopt state of the art form, as single hop hydrogenation technique (hydrogenator), single hop serial hydrogenation technique (two hydrogenator series connection) etc.Hydrotreatment operational condition and catalyzer are also close with prior art.As reformed pre-hydrogenated operational condition is: hydrogen dividing potential drop 1.0MPa～6.0MPa, is preferably 1.5MPa～4.0MPa; Temperature of reaction is 220 DEG C～360 DEG C, is preferably 260 DEG C～330 DEG C; Volume space velocity is 1.0h
-1～12.0h
-1, be preferably 2.0h
-1～8.0h
-1; Hydrogen to oil volume ratio is 50～800, is preferably in 100～600.Catalysis heavy petrol hydroprocessing condition is: hydrogen dividing potential drop 1.0MPa～6.0MPa, is preferably 1.0MPa～3.2MPa; Temperature of reaction is 220 DEG C～360 DEG C, is preferably 240 DEG C～330 DEG C; Volume space velocity is 1.0h
-1～8.0h
-1, be preferably 2.0h
-1～6.0h
-1; Hydrogen to oil volume ratio is 50～800, is preferably in 100～600.In hydrofinishing process of the present invention, two cover hydrogenation units organically can be combined, to reach best effect.
In Unionfining method of the present invention, the hydrotreating catalyst of use can be commodity hydrotreating catalyst, as the FH series hydrotreating catalyst of Fushun Petrochemical Research Institute's development and production, also can prepare by art processes.Concerning two cover associating hydrogenation units, use existing conventional Hydrobon catalyst to meet respectively production requirement separately, quality product can meet the demands completely.The catalyzer of recommendation of the present invention is W-Mo-Ni system or Mo-Co series hydrocatalyst.Wherein the composition of W-Mo-Ni series hydrocatalyst comprises: Tungsten oxide 99.999+molybdenum oxide is not less than 25wt%, and nickel oxide is not less than 2wt%, in oxide compound active metal total content for being not less than 27wt%.The composition of Mo-Co series hydrocatalyst comprises: molybdenum oxide is not less than 15wt%, and cobalt oxide is not less than 5wt%, in oxide compound active metal total content for being not less than 20wt%.The implication of described " being not less than " refers to " being more than or equal to ".Support of the catalyst is generally refractory porous oxide, as aluminum oxide, silicon oxide etc., can also contain other adjuvant component.Two covering devices can be selected identical Hydrobon catalyst, also can select different Hydrobon catalysts.
The inventive method is compared with conventional hydrofining technology flow process, and technical process is comparatively simple, can omit make-up hydrogen compressor and circulating hydrogen compressor, and hydrogen utilization ratio is higher.Therefore, no matter investment cost, or tooling cost is all lower.Naphtha fraction and the common hydrogen to oil volume ratio of catalysis heavy naphtha hydrotreatment are lower, and hydrogen consumption is also lower, can cancel circulating hydrogen compressor completely.And the cost of investment of circulating hydrogen compressor accounts for the large percentage of whole plant investment cost, so present method can obviously reduce plant investment cost.By optimization technological process, the inventive method can, under investment and the lower condition of process cost, obtain the technique effect suitable with existing complete processing.
Brief description of the drawings
Fig. 1 is a kind of concrete process flow diagram of Unionfining method of the present invention.
Wherein: the reformed pre-hydrogenated stock oil of 1-, the new hydrogen of 2-pipe network, 3-process furnace, the reformed pre-hydrogenated reactor of 4-, 5-gas-liquid separator, 6-gas stripping column, 7-treated oil, 8-hydrogen-rich gas, 9-catalysis heavy petrol raw material, 10-process furnace, 11-catalysis heavy petrol hydrogenator, 12-gas-liquid separator, 13-gas stripping column, 14-treated oil, 15-reacts remaining hydrogen.
Embodiment
Further illustrate detailed process and the effect of Unionfining method of the present invention below in conjunction with accompanying drawing.
As described in Figure 1, the concrete mode of the one of Unionfining technological process of the present invention comprises following content:
Adopt single hop technical process, after mixing with hydrogen, reformed pre-hydrogenated device stock oil 1 enters process furnace 3, then under the processing condition that relax, contact with hydrogenation catalyst, carry out conventional hydrofining processing, in reactor 4, use catalyzer for W-Mo-Ni system or Mo-Co be Hydrobon catalyst, the composition of catalyzer generally comprises: molybdenum oxide is not less than 15wt%, cobalt oxide is not less than 5wt%, in oxide compound active metal total content for being not less than 20wt%, reactant separates in gas-liquid separator 5, liquid-phase product enters gas stripping column 6, hydrogen-rich gas 8 directly uses as the hydrogen make-up of catalysis heavy petrol hydrogenation unit, at the bottom of gas stripping column 6 towers, oil is qualified reformer charging.Hydrogen-rich gas 8 and catalysis heavy petrol raw material 9 are after mixing, enter process furnace 10, then under the processing condition that relax, contact with hydrogenation catalyst, carry out conventional hydrofining processing, in reactor 11, use the catalyzer can be consistent with the catalyzer that reactor 4 uses, reaction effluent separates in gas-liquid separator 12, liquid-phase product enters gas stripping column 13, react the direct hydrogen make-up as other hydrogenation units of remaining hydrogen 15 or return to the use of hydrogen pipe network, at the bottom of gas stripping column 13 towers, oil obtains clean motor spirit blend component after mixing with catalytic light gasoline.
In the inventive method, after reformed pre-hydrogenated device and the associating of catalysis heavy petrol hydrogenation unit, in technical process, comparatively simple and simplified equipment, has omitted circulating hydrogen compressor and make-up hydrogen compressor, and respective lines.
After the inventive method is processed, product can reach following character: reformed pre-hydrogenated treated oil meets the requirement that sulphur, nitrogen content are less than 0.5 other character of μ g/g and meet reformer charging; After catalysis heavy petrol hydrogenation unit treated oil mixes with catalytic light gasoline, product meets clean vehicle gasoline fuel index request.
In the methods of the invention, described catalysis heavy petrol raw material is that catalytic cracking unit obtains gasoline fraction, the last running obtaining after fractionation again, reformed pre-hydrogenated raw material is the mixing oil of virgin naphtha cut or virgin naphtha cut and part secondary processing petroleum naphtha.The contents such as concrete technology condition can be determined by those skilled in the art according to material elementses such as the character of raw material.
The invention has the advantages that: technical process is simple, easy and simple to handle, invest less, superfluous hydrogen-rich gas and can recycle, reduce tooling cost, quality product can meet quality index requirement completely.For the newly-built hydrogenation unit of oil refining enterprise, can greatly reduce the construction cost of device, thereby reduce cost of investment, and can reduce running cost.The inventive method hydrogen utilization ratio is higher, has reduced to a certain extent tooling cost, has alleviated the problem of hydrogen source anxiety.
The following examples illustrate the present invention further.
The FH-40B Hydrobon catalyst that experiment is used catalyzer to develop for Fushun Petrochemical Research Institute, its physico-chemical property index is in table 1.
Embodiment 1
Adopt the inventive method to process feed naphtha 1 and catalysis heavy naphtha raw material 1, reformed pre-hydrogenated reaction conditions is: hydrogen pressure component 1.9MPa, volume space velocity 4.0h
-1, 278 DEG C of temperature of reaction, hydrogen to oil volume ratio is 150: 1; Catalysis heavy petrol hydrogenation conditions is: hydrogen pressure component 1.6MPa, volume space velocity 3.0h
-1, 260 DEG C of temperature of reaction, hydrogen to oil volume ratio is 300: 1.Stock oil character and product property are listed in table 2.
From table 2, adopt sulphur, nitrogen content that this Technology can meet reformed pre-hydrogenated device product below 0.5 μ g/g, catalysis heavy petrol hydrogenation unit treated oil and catalytic light gasoline meet state's III cleaning cart gasoline quality index requirement after being in harmonious proportion.
Embodiment 2
Adopt the inventive method to process feed naphtha 2 and catalysis heavy naphtha raw material 2, reformed pre-hydrogenated reaction conditions is: hydrogen pressure component 2.0MPa, volume space velocity 4.6h
-1, 281 DEG C of temperature of reaction, hydrogen to oil volume ratio is 160: 1; Catalysis heavy petrol hydrogenation conditions is: hydrogen pressure component 1.7MPa, volume space velocity 3.5h
-1, 280 DEG C of temperature of reaction, hydrogen to oil volume ratio is 280: 1.Stock oil character and product property are listed in table 3.
From table 3, adopt sulphur, nitrogen content that this Technology can meet reformed pre-hydrogenated device product below 0.5 μ g/g, catalysis heavy petrol hydrogenation unit treated oil and catalytic light gasoline meet state's IV cleaning cart gasoline quality index requirement after being in harmonious proportion.
Embodiment 3
Adopt the inventive method to process feed naphtha 3 and catalysis heavy naphtha raw material 3, reformed pre-hydrogenated reaction conditions is: hydrogen pressure component 2.3MPa, volume space velocity 3.8h
-1, 280 DEG C of temperature of reaction, hydrogen to oil volume ratio is 150: 1; Catalysis heavy petrol hydrogenation conditions is: hydrogen pressure component 1.9MPa, volume space velocity 4.0h
-1, 265 DEG C of temperature of reaction, hydrogen to oil volume ratio is 260: 1.Stock oil character and product property are listed in table 4.
From table 4, adopt sulphur, nitrogen content that this Technology can meet reformed pre-hydrogenated device product below 0.5 μ g/g, catalysis heavy petrol hydrogenation unit treated oil and catalytic light gasoline meet state's III cleaning cart gasoline quality index requirement after being in harmonious proportion.
The physico-chemical property index of table 1 catalyzer
| Catalyzer numbering | FH-40B |
| Active metal, wt% | |
| MoO 3 | 17.3 |
| CoO | 7.1 |
| Physical properties | |
| Pore volume, mL/g | ≮0.40 |
| Specific surface area, m 2/g | ≮200 |
| Shape | Trifolium |
Table 2 embodiment 1 stock oil character and test-results
Continued 2 embodiment 1 stock oil character and test-results
Table 3 embodiment 2 stock oil character and test-results
Continued 3 embodiment 2 stock oil character and test-results
Table 4 embodiment 3 stock oil character and test-results
Continued 4 embodiment 3 stock oil character and test-results
Claims (10)
1. a Unionfining method, comprising:
(1) reformed pre-hydrogenated stock oil fully mix with hydrogen after through process furnace, enter hydrogenator and react; Described hydrogen is the new hydrogen of pipe network;
(2) step (1) reaction effluent enters separator and separates, and hydrogen-rich gas directly mixes with catalysis heavy petrol hydrogenating materials, enters hydrogenator react through process furnace;
(3) reaction effluent of step (2) carries out gas-liquid separation, and product liquid is mixed to get cleaning cart gasoline products with catalytic light gasoline after air lift.
2. according to Unionfining method claimed in claim 1, it is characterized in that, the gas that in step (3), gas-liquid separation obtains directly uses as the hydrogen make-up of other hydrogenation units, or returns to after treatment hydrogen pipe network.
3. according to Unionfining method claimed in claim 1, it is characterized in that, the reaction conditions in step (1) is: hydrogen dividing potential drop is 1.0MPa～6.0MPa, and temperature of reaction is 220 DEG C～360 DEG C, and volume space velocity is 1.0h
-1～12.0h
-1, hydrogen to oil volume ratio is 50～800.
4. according to Unionfining method claimed in claim 3, it is characterized in that, the reaction conditions described in step (1) is: hydrogen dividing potential drop is 1.5MPa～4.0MPa, and temperature of reaction is 260 DEG C～330 DEG C, and volume space velocity is 2.0h
-1～8.0h
-1, hydrogen to oil volume ratio is 100～600.
5. according to Unionfining method claimed in claim 1, it is characterized in that, the reaction conditions described in step (2) is: hydrogen dividing potential drop is 1.0MPa～6.0MPa, and temperature of reaction is 220 DEG C～360 DEG C, and volume space velocity is 1.0h
-1～8.0h
-1, hydrogen to oil volume ratio is 50～800.
6. according to Unionfining method claimed in claim 5, it is characterized in that: the reaction conditions described in step (2) is: hydrogen dividing potential drop is 1.0MPa～3.2MPa, temperature of reaction is 240 DEG C～330 DEG C, and volume space velocity is 2.0h
-1～6.0h
-1, hydrogen to oil volume ratio is 100～600.
7. according to Unionfining method claimed in claim 1, it is characterized in that: described reformed pre-hydrogenated stock oil is the mixing oil of virgin naphtha cut or virgin naphtha cut and part secondary processing petroleum naphtha, described catalysis heavy petrol hydrogenating materials is the gasoline fraction that catalytic cracking unit is produced, the last running obtaining after fractionation.
8. according to Unionfining method claimed in claim 1, it is characterized in that, single hop hydrogenation technique or single hop serial hydrogenation technique are taked in described technical process reformed pre-hydrogenated or catalysis heavy petrol hydrogenation.
9. according to Unionfining method claimed in claim 1, it is characterized in that, the Hydrobon catalyst using in the hydrogenator described in step (1) and step (2) is W-Mo-Ni system or Mo-Co series hydrocatalyst.
10. according to Unionfining method claimed in claim 9, it is characterized in that, the composition of described W-Mo-Ni series hydrocatalyst comprises: Tungsten oxide 99.999+molybdenum oxide is not less than 25wt%, and nickel oxide is not less than 2wt%, in oxide compound active metal total content for being not less than 27wt%; Described Mo-Co series hydrocatalyst composition comprises: molybdenum oxide is not less than 15wt%, and cobalt oxide is not less than 5wt%, in oxide compound active metal total content for being not less than 20wt%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010539545.1A CN102465020B (en) | 2010-11-05 | 2010-11-05 | Combined hydrofining method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010539545.1A CN102465020B (en) | 2010-11-05 | 2010-11-05 | Combined hydrofining method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102465020A CN102465020A (en) | 2012-05-23 |
| CN102465020B true CN102465020B (en) | 2014-08-20 |
Family
ID=46069149
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201010539545.1A Active CN102465020B (en) | 2010-11-05 | 2010-11-05 | Combined hydrofining method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102465020B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107619680B (en) * | 2017-10-17 | 2023-08-08 | 正和集团股份有限公司 | System and process for naphtha direct-supply reforming device of diesel hydrogenation device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1260376A (en) * | 1999-03-08 | 2000-07-19 | 中国石化集团洛阳石油化工工程公司 | Converting and combining method for hydrogenation of hydrocarbon |
| CN1335360A (en) * | 2001-09-11 | 2002-02-13 | 中国石油天然气股份有限公司 | Method and catalyst for selective hydrogenation refining of cracked gasoline |
| CN1464034A (en) * | 2002-06-17 | 2003-12-31 | 中国石油化工股份有限公司安庆分公司 | Process for catalyzed gasoline hydrogenation desulfurization |
| CN1912062A (en) * | 2005-08-09 | 2007-02-14 | 中国石油化工股份有限公司 | Hydrogenation method for producing catalytic reforming raw material |
| CN101418234A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Method for producing low-sulfur gasoline from catalytically cracked gasoline |
-
2010
- 2010-11-05 CN CN201010539545.1A patent/CN102465020B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1260376A (en) * | 1999-03-08 | 2000-07-19 | 中国石化集团洛阳石油化工工程公司 | Converting and combining method for hydrogenation of hydrocarbon |
| CN1335360A (en) * | 2001-09-11 | 2002-02-13 | 中国石油天然气股份有限公司 | Method and catalyst for selective hydrogenation refining of cracked gasoline |
| CN1464034A (en) * | 2002-06-17 | 2003-12-31 | 中国石油化工股份有限公司安庆分公司 | Process for catalyzed gasoline hydrogenation desulfurization |
| CN1912062A (en) * | 2005-08-09 | 2007-02-14 | 中国石油化工股份有限公司 | Hydrogenation method for producing catalytic reforming raw material |
| CN101418234A (en) * | 2007-10-26 | 2009-04-29 | 中国石油化工股份有限公司 | Method for producing low-sulfur gasoline from catalytically cracked gasoline |
Non-Patent Citations (3)
| Title |
|---|
| 张文成.新型重整预加氢催化剂的研制.《中国优秀硕士学位论文全文数据库工程科技Ⅰ辑》.2009,第2-5页. |
| 新型重整预加氢催化剂的研制;张文成;《中国优秀硕士学位论文全文数据库工程科技Ⅰ辑》;20091204;第2-5页 * |
| 说明书第7页第20-23行. |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102465020A (en) | 2012-05-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100434496C (en) | Two-way combined process of wax-oil hydrogenation treatment and catalytic cracking | |
| CN103059972B (en) | Combined hydrogenation method of producing chemical materials | |
| CN103013559A (en) | Hydrocracking method for selective increasing of aviation kerosene yield | |
| CN102453535B (en) | Hydrocracking method for reforming material yield increase | |
| CN103059986B (en) | Hydrocracking method for producing chemical materials | |
| CN1952069A (en) | Combined hydrogenation method | |
| CN101747936B (en) | Hydrogenation method for producing high-quality low-sulfur diesel fraction | |
| CN103805247B (en) | A kind of combined technical method processing poor ignition quality fuel | |
| CN103059946B (en) | Low-energy consumption catalytic gasoline hydrodesulfurizationmethod method | |
| CN109777481B (en) | Combined processing method for refinery gas | |
| CN102465016B (en) | Combined hydrogenation process | |
| CN102465011A (en) | Hydrotreatment method of heavy distillate oil | |
| CN100419044C (en) | Production of large-specific-weight aircraft liquid petroleum oil at maximum from coal liquefied oil | |
| CN102465020B (en) | Combined hydrofining method | |
| CN109777501A (en) | A kind of refinery gas combinational processing method | |
| CN106520197B (en) | A kind of method for hydrogen cracking that boat coal is produced by inferior feedstock oil | |
| CN109777488B (en) | Refinery gas combined processing technology | |
| CN102465027A (en) | Hydrotreating method of heavy distillate oil | |
| CN103059958B (en) | Catalytic cracking and catalytic gasoline hydrogenation combined process | |
| CN103059965B (en) | Catalytic gasoline deep hydrodesulfurizationmethod method | |
| CN103059951B (en) | Catalytic cracking and catalytic gasoline hydrogenation combined technological method | |
| CN102465019B (en) | Low-pressure combined hydrogenation technological method | |
| CN109777499A (en) | A kind of refinery gas Combined machining technique | |
| CN109777487A (en) | Refinery gas combinational processing method | |
| CN109988630B (en) | Wax oil hydrogenation method and system |
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 |