CN104877707B - The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization - Google Patents
The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization Download PDFInfo
- Publication number
- CN104877707B CN104877707B CN201510229702.1A CN201510229702A CN104877707B CN 104877707 B CN104877707 B CN 104877707B CN 201510229702 A CN201510229702 A CN 201510229702A CN 104877707 B CN104877707 B CN 104877707B
- Authority
- CN
- China
- Prior art keywords
- hydrogen
- temperature
- way
- reactor
- heating
- 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
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/14—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with moving solid particles
- C10G45/16—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing with moving solid particles suspended in the oil, e.g. slurries
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
- C10G47/26—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles suspended in the oil, e.g. slurries
Abstract
The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization, the method for hydrotreating comprise the following steps：Hydrogen first at heat exchanger with high-temperature high-pressure separator exit gas be hot high score gas converting heat to 300 420 DEG C, be then divided into two-way heating：330 420 DEG C are heated into raw materials furnace and heating form mixing logistics after being mixed all the way with raw material, enter the high-temperature hydrogen that hydrogen heating furnace is heated to 450 580 DEG C all the way, high-temperature hydrogen after the mixing logistics mixing of raw materials furnace and heating outlet all the way with entering one-level hydrogenation reactor, the logistics with the outlet of one-level hydrogenation reactor is mixed into secondary hydrogenation reactor all the way, enter the high-temperature high-pressure separator from bottom all the way, if reactor is three-level or more, sequentially enter.Methods described is easy to operate and is easy to Automated condtrol.The heat form and coal addition position of hydrogen solve the problems, such as that first-stage reactor inlet temperature is unstable, second reactor hydrogen dividing potential drop is inadequate, polycondensation reaction occurs for asphaltene in separator.
Description
Technical field
The present invention relates to slurry bed hydroprocessing series methods of a kind of Multiple Optimization and application thereof, belong to petrochemical industry and coalification
Work field.
Background technology
In recent years, as the continuous reduction being continuously increased with conventional crude reserves of oil extraction amount, crude oil in poor quality become
Gesture is increasingly severe, and crude oil directly distills the centre that the secondary operation such as obtained intermediate oil and coking, catalytic cracking obtain
The S of cut, N content also accordingly increase, at the same time, market to light oil be continuously increased and people's environmental consciousness it is continuous
Enhancing, environmentally friendly laws and regulations require stricter to engine exhaust emission, and various standard of fuel require S, N content also more
It is harsh.How the higher midbarrel of the impurity contents such as sulphur, nitrogen to be processed into and disclosure satisfy that the product of environmental requirement is each refinery
The major issue faced.
Under this actual environment, heavy-oil hydrogenation technology, direct coal liquefaction technology and coal mixing technology are increasingly taken seriously,
Heavy-oil hydrogenation technology not only can effectively utilize petroleum resources, and can improve the economic benefit of oil-processing enterprises.At present
Processing of heavy oil mainly has the techniques such as delayed coking, RFCC and residual hydrogenation.The product liquid of delayed coking unit
It is of poor quality, coke yield is high.Requirement of the RFCC to raw material is higher, can not handle the residual oil of poor quality.Residual hydrogenation can
With handle high-sulfur, high carbon residue, high metal poor residuum, while improve the quality of liquid yield and product liquid.It is residue fixed-bed
Be hydrogenated with and higher required to the content of beary metal in residual oil, residual oil slurry bed hydroprocessing can effectively remove sulphur in residual oil, nitrogen and
Heavy metal.
China is a country rich in coal and poor in oil, in tackling current contradiction between oil supply and demand and implementing energy-saving and emission-reduction policy,
It is the important selection for ensureing energy security to make full use of coal resources.Using coal liquefaction technology and oily coal mixing technology, coal is refined
The important method that light oil is solution China's energy dilemmas is converted into poor residuum.These technologies belong to HTHP
Hydrogenation technique, to ensure device long-period stable operation, it is necessary to a kind of method of hydrotreating of function admirable, to ensure reactor length week
Phase is in stable state, and reduces the coking phenomenon of high-temperature separator.
At present, hydrogenation mode enters raw materials furnace and heating after typically hydrogen is mixed with raw material and heated, and is passed directly into one-level
Hydrogenation reactor, hydrogen is not passed through additionally to second reactor or third-stage reactor and high-temperature high-pressure separator.This mode
Process is simple, cost is low, but the temperature of first-stage reactor is not easy to adjust, and excessively causes temperature of reactor liter in exothermic heat of reaction
Height requires supplementation with largely cold hydrogen or cold oil when exceeding warning temperature, and the too low cold hydrogen or cold oil of temperature can be destroyed in reactor
Reaction system.In addition, with the carry out two level of reaction or the hydrogen dividing potential drop deficiency of third-stage reactor, conversion ratio is reduced, set more
The more thoroughly purpose that stage reactor carries out reaction is just unable to reach.And the operation temperature of high-temperature high-pressure separator exists
More than 400 DEG C, because polycondensation reaction can occur at such high temperatures for the asphaltene generated in the reactor, in turn result in coking.
The content of the invention
, will the invention provides a kind of slurry bed system method of hydrotreating of Multiple Optimization based on problems of the prior art
Hydrogen, which is divided into after two parts heat respectively, to be remixed, adjust appropriate mixed proportion according to hydrogenation reactor inlet temperature requirements so that
Hydrogenation reactor inlet temperature is stable.Additionally provide the purposes of the method for hydrotreating.
Technical scheme：
The slurry bed hydroprocessing series methods of a kind of Multiple Optimization, it is characterised in that the described method comprises the following steps：Hydrogen
It is divided into two-way heating, 330-420 DEG C is heated into raw materials furnace and heating after being mixed all the way with raw material, all the way into hydrogen heating furnace
450-580 DEG C is heated to, then the logistics and all or part of the hydrogen furnace outlet of the raw materials furnace and heating outlet
Enter hydrogenation reactor after hydrogen mixing.
The hydrogen may include hydrogen make-up and circulating hydrogen, and the circulating hydrogen is obtained by hot high score gas purification, institute
State after hydrogen make-up mixes with circulating hydrogen preferably first at heat exchanger with being further divided into two-way point after hot high score gas converting heat
Do not heat, the temperature of the hydrogen after the heat exchange is 300-420 DEG C.
The preferable hydrogenation reactor is first-stage reactor, the hydrogen of the hydrogen furnace outlet all the way with the original
Enter one-level hydrogenation reactor after the logistics mixing of material furnace outlet, all the way into high-temperature high-pressure separator.
The preferable hydrogenation reactor is multistage reactor, the hydrogen of the hydrogen furnace outlet all the way with the original
Enter one-level hydrogenation reactor after the logistics mixing of material furnace outlet, all the way into high-temperature high-pressure separator, in addition at least
All the way, the stage reactor is entered after often being mixed respectively with the logistics of wherein one-level higher order reaction device entrance all the way.
It is preferably 2 that the hydrogen of the hydrogen furnace outlet, which enters first-stage reactor and the ratio of second reactor,:1-20:
1。
The further preferred hydrogenation reactor is third-stage reactor, and the hydrogen of the hydrogen furnace outlet enters three
Stage reactor is the 1/10-1/2 into second reactor.
The ratio for branching to the hydrogen heating furnace and the hydrogen of the raw materials furnace and heating is preferably 1-30：1.
The hydrogen of the preferable hydrogen furnace outlet enters the high-temperature high-pressure separator, and hydrogen inlet from bottom
It is located at below the liquid level of the separator.
The slurry bed system hydrocracking unit of a kind of Multiple Optimization, it is characterised in that Hydrogen Line is divided into two-way and is respectively communicated with hydrogen
The entrance of gas heating furnace and raw materials furnace and heating, the raw materials furnace and heating include the entrance of connection feedstock transportation pipeline, the hydrogen
Heating furnace output channel comprises at least all the way, and it connects entering for hydrogenation reactor after converging with the output channel of raw materials furnace and heating
Mouthful.
Preferably also include heat exchanger, pass through the hot high score gas pipeline of high-temperature high-pressure separator respectively in the heat exchanger
With with Hydrogen Line.
The connection high-temperature high-pressure separator all the way of the preferable hydrogen heating furnace output channel.
When the hydrogenation reactor is multistage reactor, if the hydrogen heating furnace output channel also includes main line, its
Higher order reaction device is connected again after converging respectively with the inlet duct of each higher order reaction device.
The slurry bed hydroprocessing series methods of Multiple Optimization described above and the purposes of device, it is characterised in that for heavy oil plus
Hydrogen technique, direct coal liquefaction process or oily coal calendering process, the heavy oil include crude oil, residual oil, catalytic slurry, de-oiled asphalt,
The one or more of coal tar；The coal includes the one or more in lignite, bituminous coal, dross coal, the ratio of oil and coal
Scope is 97:3-40:60.
The design method of slurry bed hydroprocessing series methods and device also including above-mentioned Multiple Optimization.
The technique effect of the present invention：
Hydrogen is divided into two parts heating by this method first, and small part is heated to being less than reactor inlet after mixing with raw material
Temperature, it is most of to be individually heated above reactor inlet temperature in hydrogen heating furnace, then by high-temperature hydrogen and raw material and hydrogen
The mixture of gas mixes before hydrogenation reactor entrance, is adjusted by the addition of manual or automatic control and regulation high-temperature hydrogen mixed
Temperature is closed so as to control the temperature stabilization of hydrogenation reactor entrance.This method of hydrotreating, which solves, is directly added into cold hydrogen into reactor
The problem of Deng temperature of reaction system or uneven reactant is caused when adjusting temperature, and the solids content that is particularly suitable for use in is higher, adopts
The oily hydrogenation technique of uniform inferior heavy (slag), direct coal liquefaction process or oily coal, which are not easy, with existing temperature control method temperature is kneaded work
Skill, the control to hydrogenation reactor particularly first-stage reactor inlet temperature can be achieved, prevent that reactor temperature is elevated same
Shi Buhui damages to the system in reactor.
This method makes full use of the hot high score gas that high-temperature high-pressure separator exports, and one side temperature is up to 350-470 DEG C
Hot high score gas and hydrogen make-up and circulating hydrogen heat exchange hydrogen source is preheated before heating respectively, save the energy.The opposing party
Circulating hydrogen is made after the hot purified purification of high score gas in face, for hydrogen source, recycles.
If hydrogenation reactor is two level or more, accordingly increase from the hydrogenation position of the hydrogen of hydrogen furnace outlet.
Hydrogenation position includes：First-stage reactor entrance, second reactor entrance, high-temperature high-pressure separator entrance；Three-level or higher level are anti-
Answer device entrance.Solve unstable first-stage reactor inlet temperature and two level (or three-level) reactor, HTHP point simultaneously
The problem of inadequate from hydrogen dividing potential drop in device.
The ratio of two parts hydrogen heated respectively determines according to first-stage reactor inlet temperature.
Hydrogen inlet into high-temperature high-pressure separator is located at below the liquid level of separator, maintains hydrogen partial pressure and one-level anti-
Answer hydrogen partial pressure in device suitable.
The design method design hydrogen is divided into the mode remixed after two parts heating and controls feeding temperature, is additionally arranged one
Hydrogen heating furnace individually heats to hydrogen, at higher temperature relative to just can be heated to the less energy of raw material heating needs and time
Degree.Small part hydrogen mixes the uniformity coefficient of increase raw material and hydrogen with raw material.The two reaches suitable temperature after being thoroughly mixed
Enter back into reactor so that the temperature in reactor ensures the stabilization and reactant of reactor temperature without being adjusted again
System it is uniform.In addition, the high-temperature hydrogen individually heated can be respectively to two level or third-stage reactor and high-temperature high-pressure separator
It is additionally provided hydrogen, increases hydrogen dividing potential drop, so as to solves multistage reactor simultaneously because hydrogen dividing potential drop is not enough reacted insufficient and asked
Topic and separator because temperature is high, hydrogen dividing potential drop is low cause asphaltene that polycondensation reaction, coking occurs the problem of.
Brief description of the drawings
Fig. 1 is the hydrogenation general flow chart of the embodiment of the present invention.
Drawing reference numeral：
1- hydrogen gas separated by high pressure separator heat exchangers；2- hydrogen heating furnaces；3- raw materials furnace and heatings；4- first-stage reactors；5- second order reactions
Device；6- high-temperature high-pressure separators；7- hydrogen make-ups；8- circulating hydrogens；9- raw materials；The hot high score gases of 10-.
Embodiment
For the particular content of the present invention is expanded on further, Fig. 1 will be combined and specific embodiment describes in detail.
Reactor in the present embodiment is two-stage, is kneaded for oily coal, and specific hydrogenation flow is as follows：
The i.e. hot gas separated by high pressure separator of the exit gas of high-temperature high-pressure separator 6 with 470 DEG C after hydrogen make-up 7 mixes with circulating hydrogen 8
Body 10 exchanges heat at hydrogen gas separated by high pressure separator heat exchanger 1 and is warming up to 425 DEG C of hydrogen, is to follow after the hot high score gas 10 after heat exchange is refined
Ring hydrogen 8.Then 20% hydrogen and mass ratio after exchanging heat are 60:Enter raw material after 40 mixing of coal charging 9 to heat
Stove 3 is warming up to 365 DEG C of mixing logistics, and 80% hydrogen enters the high-temperature hydrogen that hydrogen heating furnace 2 is warming up to 535 DEG C.Then
A part of high-temperature hydrogen enters the entrance of first-stage reactor 4 in being mixed with the mixing logistics from the raw materials furnace and heating 3, the two
Amount is controlled such that feeding temperature remains 385 DEG C by automatic control system；A part of high-temperature hydrogen is in second reactor 5
Entrance is mixed into first-stage reactor outlet streams, and hydrogen charging is the 1/15 of the charging of first-stage reactor hydrogen；A part of high-temperature hydrogen
Enter high-temperature high-pressure separator 6, hydrogen dividing potential drop 12.0MPa from bottom.
The present embodiment during the course of the reaction, mix the amount of logistics and high-temperature hydrogen according to the real time temperature in reactor by from
Control system is allocated, and ensure that the uniform of the stabilization of temperature and reactant in first-stage reactor 4, while the He of second reactor 5
Hydrogen dividing potential drop also keeps stable in high-temperature high-pressure separator 6, and coking phenomenon does not occur.
Conclusion：
From above-described embodiment as can be seen that the slurry bed hydroprocessing series methods of the Multiple Optimization using the present invention, operation letter
Just, and it is easy to Automated condtrol.The heat form and coal addition position of hydrogen solve first-stage reactor inlet temperature not well
It is stable, the hydrogen dividing potential drop of second reactor is inadequate, in high-temperature high-pressure separator asphaltene polycondensation reaction generation.Enhance and improve
The stability of plant running, the time between overhauls(TBO) of device is improved, add light oil yield, it is significant.
The preferable embodiment of the present invention is the foregoing is only, but protection scope of the present invention is not limited thereto,
Any one skilled in the art the invention discloses technical scope in, the change of reactor series can be readily occurred in
Change or the replacement of hydrogen source, should all be included within the scope of the present invention.Therefore, protection scope of the present invention should be with power
The protection domain of sharp claim is defined.
Claims (10)
1. the slurry bed hydroprocessing series methods of a kind of Multiple Optimization, it is characterised in that the described method comprises the following steps：Hydrogen point
Heated for two-way, raw materials furnace and heating entered after being mixed all the way with raw material and is heated to 330-420 DEG C less than reactor inlet temperature,
Enter 450-580 DEG C that hydrogen heating furnace is heated above reactor inlet temperature all the way, then the raw materials furnace and heating outlet
Logistics mixed with all or part of hydrogen of the hydrogen furnace outlet after enter hydrogenation reactor, by manual or automatic
The addition for controlling to adjust high-temperature hydrogen adjusts mixing temperature so as to control the temperature of hydrogenation reactor entrance.
2. according to the method for claim 1, it is characterised in that the hydrogen includes hydrogen make-up and circulating hydrogen, described to follow
Ring hydrogen is obtained by hot high score gas purification, the hydrogen make-up mixed with circulating hydrogen after first at heat exchanger with hot high score
It is further divided into two-way after gas converting heat to heat respectively, the temperature of the hydrogen after the heat exchange is 300-420 DEG C.
3. according to the method for claim 1, it is characterised in that the hydrogenation reactor is first-stage reactor, and the hydrogen adds
The hydrogen of hot stove outlet enters one-level hydrogenation reactor after being mixed all the way with the logistics of raw materials furnace and heating outlet, enters all the way
High-temperature high-pressure separator.
4. according to the method for claim 1, it is characterised in that the hydrogenation reactor is multistage reactor, and the hydrogen adds
The hydrogen of hot stove outlet enters one-level hydrogenation reactor after being mixed all the way with the logistics of raw materials furnace and heating outlet, enters all the way
High-temperature high-pressure separator, in addition at least all the way, per after being mixed respectively with the logistics of wherein one-level higher order reaction device entrance all the way
Into the stage reactor.
5. the slurry bed system hydrocracking unit of a kind of Multiple Optimization, it is characterised in that Hydrogen Line is divided into two-way and is respectively communicated with hydrogen
The entrance of heating furnace and raw materials furnace and heating, the raw materials furnace and heating include the entrance of connection feedstock transportation pipeline, and the hydrogen adds
Hot stove output channel comprises at least all the way, and it connects the entrance of hydrogenation reactor after converging with the output channel of raw materials furnace and heating；
Raw materials furnace and heating is heated to 330-420 DEG C less than reactor inlet temperature, and hydrogen heating furnace is heated above reactor inlet
450-580 DEG C of temperature, then the logistics of the raw materials furnace and heating outlet and the hydrogen all the way of the hydrogen furnace outlet mix
Enter hydrogenation reactor after conjunction, mixing temperature is adjusted so as to control by the addition of manual or automatic control and regulation high-temperature hydrogen
The temperature of hydrogenation reactor entrance.
6. device according to claim 5, it is characterised in that also including heat exchanger, pass through high temperature respectively in the heat exchanger
Hot the high score gas pipeline and Hydrogen Line of high-pressure separator.
7. the device according to claim 5 or 6, it is characterised in that the connection all the way of the hydrogen heating furnace output channel is high
Warm high-pressure separator.
8. the device according to claim 5 or 6, it is characterised in that the hydrogenation reactor is multistage reactor, the hydrogen
If gas heating furnace output channel also includes main line, it connects advanced anti-again after converging respectively with the inlet duct of each higher order reaction device
Answer device.
A kind of 9. purposes of the slurry bed hydroprocessing series methods of any described Multiple Optimizations of claim 1-4, it is characterised in that
For heavy oil hydrogenation process, direct coal liquefaction process or oily coal calendering process, the heavy oil includes heavy crude, residual oil, catalysis
Slurry oil, de-oiled asphalt, the one or more of coal tar；The coal includes a kind of or more in lignite, bituminous coal, dross coal
Kind, the proportion of oil and the mass ratio of coal is 97 in the oily coal calendering process:3-40:60.
10. a kind of slurry bed hydroprocessing Series Design method of Multiple Optimization, it is characterised in that design hydrogen is divided into two-way heating：One
Road enters raw materials furnace and heating and is heated to 330-420 DEG C less than reactor inlet temperature after being mixed with raw material, all the way into hydrogen
Heating furnace is heated above 450-580 DEG C of reactor inlet temperature, then the logistics of raw materials furnace and heating outlet with it is described
Enter hydrogenation reactor after all or part of hydrogen mixing of hydrogen furnace outlet, pass through manual or automatic control and regulation high temperature
The addition of hydrogen adjusts mixing temperature so as to control the temperature of hydrogenation reactor entrance.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510229702.1A CN104877707B (en) | 2015-05-07 | 2015-05-07 | The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization |
| PCT/CN2015/094219 WO2016176976A1 (en) | 2015-05-07 | 2015-11-10 | Multi-optimised hydrogenation series method, and design method therefor and use thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510229702.1A CN104877707B (en) | 2015-05-07 | 2015-05-07 | The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104877707A CN104877707A (en) | 2015-09-02 |
| CN104877707B true CN104877707B (en) | 2017-12-15 |
Family
ID=53945388
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510229702.1A Active CN104877707B (en) | 2015-05-07 | 2015-05-07 | The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN104877707B (en) |
| WO (1) | WO2016176976A1 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104877707B (en) * | 2015-05-07 | 2017-12-15 | 北京中科诚毅科技发展有限公司 | The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization |
| CN110724557A (en) * | 2018-07-17 | 2020-01-24 | 中石化广州工程有限公司 | Method for reducing differential pressure of circulating hydrogen system of hydrogenation device |
| CN115090220B (en) * | 2022-07-31 | 2023-04-11 | 中国石油化工股份有限公司 | Down-flow type mixed bubble flow hydrogenation reactor |
| CN116592277B (en) * | 2023-07-19 | 2023-09-08 | 欧科能源技术(天津)有限公司 | Hydrogen energy utilization gas blending device |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861532A (en) * | 2014-03-03 | 2014-06-18 | 北京旭荣工程设计有限公司 | Homogeneous three-phase reactor for jet aeration |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4048054A (en) * | 1976-07-23 | 1977-09-13 | Exxon Research And Engineering Company | Liquefaction of coal |
| DE3022158C2 (en) * | 1980-06-13 | 1989-11-02 | Bergwerksverband Gmbh, 4300 Essen | Process for hydrogenating coal liquefaction |
| DE3141380A1 (en) * | 1981-10-17 | 1983-05-05 | GfK Gesellschaft für Kohleverflüssigung mbH, 6600 Saarbrücken | METHOD FOR HYDROGENATING COAL |
| CN101168685B (en) * | 2006-10-26 | 2010-11-03 | 中国石油天然气股份有限公司 | Device and technique for increasing circulation hydrogen concentration of high-pressure hydrogenation reactor |
| CN104277879B (en) * | 2013-07-05 | 2016-08-24 | 任相坤 | A kind of two-stage slurry bed system hydrogenation technique of middle coalite tar |
| CN103421542B (en) * | 2013-08-08 | 2015-03-11 | 华南理工大学 | Diesel hydrogenation process |
| CN104017601B (en) * | 2014-06-19 | 2016-11-09 | 北京中科诚毅科技发展有限公司 | A kind of residual oil slurry bed system method for hydrogen cracking and device |
| CN104877707B (en) * | 2015-05-07 | 2017-12-15 | 北京中科诚毅科技发展有限公司 | The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization |
-
2015
- 2015-05-07 CN CN201510229702.1A patent/CN104877707B/en active Active
- 2015-11-10 WO PCT/CN2015/094219 patent/WO2016176976A1/en active Application Filing
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861532A (en) * | 2014-03-03 | 2014-06-18 | 北京旭荣工程设计有限公司 | Homogeneous three-phase reactor for jet aeration |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2016176976A1 (en) | 2016-11-10 |
| CN104877707A (en) | 2015-09-02 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104946306B (en) | A kind of full fraction of coal tar floating bed hydrocracking and fixed bed hydrogenation modification combined method | |
| CN104877707B (en) | The hydrogenation series methods and its design method and purposes of a kind of Multiple Optimization | |
| CN104611019B (en) | A kind of low energy consumption method for hydrogen cracking producing high-quality jet fuel | |
| CN104673371B (en) | A kind of method for improving delayed coking liquid product yield | |
| CN203602562U (en) | Coal tar hydrogenation system | |
| CN104388116A (en) | High-efficiency heavy inferior oil conversion process | |
| US20210023547A1 (en) | Method and equipment for circulating cooled regenerated catalyst | |
| CN104673372B (en) | A kind of method improving delayed coking product slates | |
| CN100473712C (en) | Technical flow of hydrogenation of gasoline through catalytic cracking full distillate | |
| CN204058379U (en) | A kind of catalytic diesel oil hydro-upgrading unit heat exchange optimization system inferior | |
| CN105441128B (en) | The temperature control method and its design method and purposes of a kind of hydrogenation technique | |
| US9574141B2 (en) | Wet start-up method for hydrogenation unit, energy-saving hydrogenation process and hydrogenation apparatus | |
| CN103421542B (en) | Diesel hydrogenation process | |
| CN104560182B (en) | A kind of method that the workflow of gasoline and diesel hydrogenation refining plant and its application and gasoline and diesel hydrogenation refine | |
| CN115537231B (en) | Method for realizing oil reduction and oil increase by changing material flow direction | |
| CN101250435B (en) | Hydrocarbons hydrogenation conversion method | |
| CN103361112B (en) | Device for blending catalytic slurry oil in delayed coking technology and method thereof | |
| CN104531211B (en) | A kind of coal tar hydrogenating produces technique and the process matched therewith system of fuel or industrial oil | |
| CN106497601A (en) | A kind of two sections of complete alternation method of hydrotreating | |
| CN104164253A (en) | Heavy oil processing method | |
| CN106244193A (en) | High-wax oil processing means and processing method | |
| CN105399098A (en) | Calcium carbide preparation device and method | |
| CN101250434B (en) | Hydrocarbons hydrogenation conversion method | |
| CN215712822U (en) | Processing system for producing low-sulfur aviation kerosene by normal-pressure heat combined liquid-phase circulation | |
| CN103525448B (en) | System and process for preparing light distillate oil from coal |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |