CN109735364A - A kind of residual hydrogenation equipment and technique - Google Patents
A kind of residual hydrogenation equipment and technique Download PDFInfo
- Publication number
- CN109735364A CN109735364A CN201910170413.7A CN201910170413A CN109735364A CN 109735364 A CN109735364 A CN 109735364A CN 201910170413 A CN201910170413 A CN 201910170413A CN 109735364 A CN109735364 A CN 109735364A
- Authority
- CN
- China
- Prior art keywords
- membrane filter
- outlet
- communicated
- head tank
- oil
- 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.)
- Pending
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of residual hydrogenation equipment and techniques, including head tank, the discharge port of head tank is communicated with the first pump, the liquid outlet of first pump is communicated with the first membrane filter, the concentrated solution outlet of first membrane filter is parallel with the first concentration liquid pipe and the second concentration liquid pipe, the first concentration liquid pipe is connected to head tank, and the outlet end of the second concentration liquid pipe is communicated with the second membrane filter, and the purified liquor outlet of the second membrane filter is connected to head tank；The purified liquor outlet of first membrane filter is communicated with the Clear liquid tank for storing clear liquid；It further include mixed cell, the inlet of mixed cell is connected to Clear liquid tank, and the liquid outlet of mixed cell is communicated with fixed bed reactors.Hydrogeneous residual oil hydrogen carrying amount is high in the present invention and stay in grade can be obtained stable catalytic hydrogenation effect under the conditions of conventional relatively-stationary liquid phase catalytic hydrogenation, is conducive to improving production efficiency, obtains lower, the up-to-standard hydrogenated products of impurity content.
Description
Technical field
The present invention relates to a kind of residual hydrogenation equipment and techniques, belong to petrochemical industry.
Background technique
In recent years, with the increasingly scarcity of petroleum resources, crude oil heaviness, in poor quality trend are on the rise, are steamed by crude oil
S, N, the O and tenor for evaporating resulting intermediate oil are also increase accordingly.However, the laws and regulations of countries in the world are to each
S, N, O and tenor in kind fuel oil require but increasingly harsher.
Hydrotreating is S, N, the O and metal impurities removed in target oil product, improves the common of midbarrel oil quality
Means.Currently, oil refining hydrogenation technique mainly uses fixed bed hydrogenation technique, when carrying out hydrotreating, need hydrogen injection liquid
In state hydrogen oil plant to be added, realizes that air-fuel mixture, gas mixture are then contacted with catalyst, carry out hydrogenation reaction.Fixed bed adds
Hydrogen consersion unit generally comprises oil-gas mixer and fixed bed reactors, and the mixed effect of oil-gas mixer is directly related to plus hydrogen
Treatment effect, in existing fixed bed hydrogenation consersion unit, oil-gas mixer generally uses film mixer, and there are mixing efficiencies not
The disadvantages of enough high.Moreover, charcoal, metal impurities content are high in residual oil, when carrying out adding hydrogen by fixed bed reactors, impurity is easily heavy
Product causes catalyst poisoning to fail, so that hydrogenation plant is unable to operate normally in catalyst bed.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of residual hydrogenation equipment and technique, with realize residual oil it is efficient,
High quality adds hydrogen.
In order to solve the above-mentioned technical problem, technical scheme is as follows:
A kind of residual hydrogenation equipment, including the head tank for storing residual oil, the discharge port of head tank is communicated with the first pump, and first
The liquid outlet of pump is communicated with the first membrane filter, and the concentrated solution outlet of the first membrane filter is parallel with the first concentration liquid pipe and second
Liquid pipe is concentrated, the first concentration liquid pipe is connected to head tank, and the outlet end of the second concentration liquid pipe is communicated with the second film mistake
The purified liquor outlet of filter, the second membrane filter is connected to head tank；
The purified liquor outlet of first membrane filter is communicated with the Clear liquid tank for storing clear liquid；
It further include the mixed cell for mixing residual oil with hydrogen, the inlet of mixed cell is connected to Clear liquid tank, and mixing is single
The liquid outlet of member is communicated with fixed bed reactors.
In the present invention, under the action of the first pump, residual oil iterative cycles between head tank and the first membrane filter, and
The purified liquor outlet of first membrane filter continuously obtains the purification oil of imurity-removal (containing solid impurity), and purification oil enters clear liquid
Tank storage；It meanwhile as the cycle progresses, can will be first when recycling that solid impurity content increases to a certain extent in residual oil
The partial concentration oil that membrane filter concentrated solution outlet obtains is sent into the second membrane filter, cleans, the purification oil of acquisition is sent
Enter head tank, reduce solid impurity content in head tank, solid impurity content balance in recycle oil is maintained, in the first membrane filter
Purified liquor outlet obtains the stable purification oil of solid impurity content, so that the mixing of subsequent microchannel and catalytic hydrogenation are in same work
It carries out can be obtained ideal catalytic hydrogenation effect under the conditions of condition, so that device can the stable hydrogenated products of output quality.In addition,
The application of mixed cell may make purification oil efficiently to mix with hydrogen, and dissolution or mixing of the hydrogen in purification oil is substantially improved
Effect, obtain hydrogen content it is high containing hydrogen purification oil；Oil containing hydrogen purification after the completion of mixing can be directly entered fixed bed reactors,
Catalytic hydrogenation help to obtain higher production efficiency and impurity removal effect；In addition, after the completion of mixing, without carrying out gas-liquid
Separating treatment, directly progress catalytic hydrogenation treatment, device and process flow are simplified.
Further, first flow control valve is installed in the first concentration liquid pipe, is installed on second concentration tube
There is second flow control valve, enriched oil trend and flow can be controlled as needed.
Further, it is communicated with the second pump between the Clear liquid tank and mixed cell, power is provided, oil pump will be purified and entered
Mixed cell.
Further, the mixed cell includes several micro-channel mixers, and the micro-channel mixer includes ontology, this
Be equipped with feed liquor runner, air inlet runner, mixing runner and multiple mixing chambers in vivo, the feed liquor runner, air inlet runner with mix
The feed end of runner is connected to, and the multiple mixing chamber is connected to mixing runner and is sequentially distributed along mixing runner, in mixing chamber
Equipped with vent diverter, mixing chamber is divided into the sub- cavity of at least two.In this way, by the inlet of mixed cell by hydrogen slag to be added
Oil input feed liquor runner, inputs air inlet runner for hydrogen by the air inlet of mixed cell, imports to hydrogenated residue and hydrogen mixed
Collaborate road, and passes sequentially through each mixing chamber, the setting of vent diverter in mixing chamber, so that single channel is divided into tiny area
Multiple flow passages form turbulent region in the tiny area, hydrogen gas bubbles are constantly broken into more tiny bubble, promote hydrogen preferably
It is dissolved in residual oil, and hydrogen is efficiently mixed with to hydrogenated residue.
Further, first membrane filter is purpose ceramic-film filter or metal film filter, preferably ceramic membrane mistake
Filter, commercially available acquisition.Preferably, filtering partial size is 1-5000nm, preferably 5-2500nm, more preferable 5-1000nm.
Further, second membrane filter is metal film filter or purpose ceramic-film filter, preferably metal film mistake
Filter, commercially available acquisition.Preferably, filtering partial size is 1-5000nm, preferably 5-2500nm, more preferable 5-1000nm.
Further, the quantity of the micro-channel mixer is in parallel or series multiple, in this way, can further be promoted mixed
The processing capacity of unit is closed, production capacity is promoted.Can also modularization setting, convenient accurate control mixed processes.
Further, the mixing chamber is flat, and whole is in one of cardioid, circle, ellipse, the preferably heart
Type；The vent diverter is one of crescent, diamond shape, circle, ellipse, preferably crescent.
Further, the cross section of the mixing runner is circle, internal diameter 0.3-3mm, preferably 0.5-1.5mm.
Further, the cross-sectional area of the mixing runner is gradually increased by feed end to discharge end, it is preferable that mixed flow
The cross-sectional area of the feed end in road is 1.1-2 times of discharge end cross-sectional area, preferably 1.1-1.5 times.In this way, taking into account mixing effect
Fruit and the big factor of pressure drop two, ensure that the pressure drop of good mixed effect and suitable size.
Further, the mixed cell includes several metal film mixers and/or several ceramic membrane mixers, optional
Ground, including multiple metal film mixers and/or multiple ceramic membrane mixers are connected in the form of serial or parallel connection.
Optionally, existing conventional fixed bed reactors can be selected in the fixed bed reactors.
Further, the fixed bed reactors include hollow tower body, and the lower end of tower body is connected to mixed cell, tower body
Upper end and be communicated with outlet tube road, catalyst bed is equipped in tower body.
Optionally, the fixed bed reactors are tubular reactor, fluidized-bed reactor, one in fluidized bed reactor
Kind.
A kind of Residue Hydrotreating Technology is carried out using residual hydrogenation equipment as described above, is included the following steps:
The first pump of starting, opens first flow control valve, so that residual oil circulates between head tank and the first membrane filter,
Purification oil is obtained in the purified liquor outlet of the first membrane filter, which is inputted into Clear liquid tank；
Period, control first flow control valve opening, so that the flow and the first membrane filter purified liquor outlet of the first concentration liquid pipe
The ratio between flow be 25-30:1；
When the solid impurity content of the residual oil in head tank is more than 20g/L, second flow control valve is opened, so that the first film filters
The partial concentration slurry oil that device generates enters the second membrane filter, and the purification oil that the second membrane filter generates is sent into head tank, so that
The solid impurity content of residual oil is reduced to 20g/L or less in slurry oil head tank；
Purification oil in Clear liquid tank is inputted into mixed cell, while being passed through hydrogen to mixed cell and (optionally, being contained according to impurity
Amount controls hydrogen-oil ratio (Nm3/ t) be 200-1000:1), obtain gas mixture；
The gas mixture is passed through fixed bed reactors, under conventional liquid phase hydroprocessing condition, gas mixture and solid
Hydrogenation catalyst contacts in fixed bed reactor, obtains residual hydrogenation product.
Compared with prior art, beneficial effects of the present invention are as follows:
1) in the present invention, the oil purification matter into mixed cell is stablized, hydrogeneous residual oil hydrogen carrying amount (the molten hydrogen of residual oil of acquisition
It measures up to 20-50% or more) height and stay in grade can be obtained stable catalysis and add under relatively-stationary catalytic hydrogenation conditions
Hydrogen effect, is conducive to improving production efficiency, help to obtain that impurity content is lower, up-to-standard (raw material impurity solid content is general
In 2-6g/l, 50ppm or less can be down to after the device of the invention or process) hydrogenated products；
2) during air-fuel mixture, without recycle oil, diluent etc., can utmostly lifting means effective rate of utilization, mention
Production capacity is risen, and reduces energy consumption, cost；
3) air-fuel mixture effect is good, without carrying out gas-liquid separation, further simplifies device and process flow.
Detailed description of the invention
Fig. 1 is a kind of residual hydrogenation equipment of the first embodiment of the invention.
Fig. 2 is the structural schematic diagram of the mixed cell of the first embodiment of the invention.
Specific embodiment
Below with reference to embodiment, the present invention will be described in detail.It should be noted that in the absence of conflict, the present invention
In embodiment and embodiment in feature can be combined with each other.For sake of convenience, hereinafter such as occur "upper", "lower", " left side ",
" right side " printed words only indicate consistent with the upper and lower, left and right direction of attached drawing itself, do not play restriction effect to structure.
As depicted in figs. 1 and 2, a kind of residual hydrogenation equipment, including the head tank 1 for storing residual oil, head tank goes out
Material mouth is communicated with the first pump 2, and the liquid outlet of the first pump is communicated with the first membrane filter 4, the concentrated solution outlet of the first membrane filter
It is parallel with the first concentration liquid pipe 14 and the second concentration liquid pipe 15, the first concentration liquid pipe 14 is connected to head tank, and described second
The outlet end of concentration liquid pipe is communicated with the second membrane filter 5, and the purified liquor outlet of the second membrane filter is connected to head tank；
The purified liquor outlet of first membrane filter is communicated with the Clear liquid tank 3 for storing clear liquid；
It further include the mixed cell 7 for mixing residual oil with hydrogen, the inlet of mixed cell is connected to Clear liquid tank, and mixing is single
The liquid outlet of member is communicated with fixed bed reactors 8.
First flow control valve 10 is installed in the first concentration liquid pipe, second is installed on second concentration tube
Control valve 11.
The second pump 6 is communicated between the Clear liquid tank and mixed cell.Pacify on pipeline between second pump and mixed cell
Equipped with heater 16, the purification oil in pipeline is heated to 350-450 °C, preferably 380-400 °C.
The mixed cell includes several micro-channel mixers, and the micro-channel mixer includes ontology 701, is set in ontology
There are feed liquor runner 702, air inlet runner 703, mixing runner 704 and multiple mixing chambers 705, the feed liquor runner, air inlet runner equal
It is connected to the feed end of mixing runner, the multiple mixing chamber is connected to mixing runner and is sequentially distributed along mixing runner, mixes
Close it is intracavitary be equipped with vent diverter 706, mixing chamber is divided into the sub- cavity of at least two.
The quantity of the micro-channel mixer is the multiple of parallel connection.
The mixing chamber is flat, is integrally in cardioid；The vent diverter is crescent.
The cross section of the mixing runner is circle, internal diameter 0.3-3mm.
The cross-sectional area of the mixing runner is gradually increased by feed end to discharge end, it is preferable that mixes the charging of runner
The cross-sectional area at end is 1.1-2 times of discharge end cross-sectional area.
The fixed bed reactors include hollow tower body, and the lower end of tower body is connected to mixed cell, the upper end of tower body with
It is communicated with outlet tube road, is equipped with catalyst bed 9 in tower body.
A kind of Residue Hydrotreating Technology is carried out using residual hydrogenation equipment as described above, is included the following steps:
The first pump of starting, opens first flow control valve, so that residual oil circulates between head tank and the first membrane filter,
Purification oil is obtained in the purified liquor outlet of the first membrane filter, which is inputted into Clear liquid tank；Wherein, purification well cuts contain admittedly
Measure < 50ppm；
Period, control first flow control valve opening, so that the flow and the first membrane filter purified liquor outlet of the first concentration liquid pipe
The ratio between flow be 27:1；
When the impurity solid content of the residual oil in head tank is more than 20g/L, second flow control valve is opened, so that the first film filters
The partial concentration slurry oil that device generates enters the second membrane filter, and the purification oil that the second membrane filter generates is sent into head tank, so that
The impurity solid content of residual oil is reduced to 20g/L or less in slurry oil head tank；
By the feed pathway of the purification oil input micro-channel mixer in Clear liquid tank, while to the inlet channel of micro-channel mixer
It is passed through hydrogen, obtains gas mixture in the discharge end 407 of mixing runner；
The gas mixture is passed through fixed bed reactors, under conventional liquid phase hydroprocessing condition, gas mixture and solid
Hydrogenation catalyst contacts in fixed bed reactor, carries out deep hydrogenation to impurity such as sulphur nitrogen oxygen, obtains residual hydrogenation product；
Period, control reaction pressure are 5-20MPa, preferably 10-20MPa, more preferably 15-20MPa.
The content that above-described embodiment illustrates should be understood as that these embodiments are only used for being illustrated more clearly that the present invention, without
For limiting the scope of the invention, after the present invention has been read, those skilled in the art are to various equivalent forms of the invention
Modification each fall within the application range as defined in the appended claims.
Claims (10)
1. a kind of residual hydrogenation equipment, including the head tank (1) for storing residual oil, the discharge port of head tank is communicated with the first pump
(2), the liquid outlet of the first pump is communicated with the first membrane filter (4), which is characterized in that the concentrated solution outlet of the first membrane filter is simultaneously
It is associated with the first concentration liquid pipe (14) and the second concentration liquid pipe (15), first concentration liquid pipe (14) is connected to head tank, described
The outlet end of second concentration liquid pipe is communicated with the second membrane filter (5), and the purified liquor outlet of the second membrane filter is connected to head tank；
The purified liquor outlet of first membrane filter is communicated with the Clear liquid tank (3) for storing clear liquid；
It further include the mixed cell (7) for mixing residual oil with hydrogen, the inlet of mixed cell is connected to Clear liquid tank, mixing
The liquid outlet of unit is communicated with fixed bed reactors (8).
2. residual hydrogenation equipment according to claim 1, which is characterized in that be equipped with first in the first concentration liquid pipe
Flow control valve (10) is equipped with second flow control valve (11) on second concentration tube.
3. residual hydrogenation equipment according to claim 1, which is characterized in that be connected between the Clear liquid tank and mixed cell
There are the second pump (6).
4. residual hydrogenation equipment according to claim 1-3, which is characterized in that the mixed cell includes several
Micro-channel mixer, the micro-channel mixer include ontology (701), are equipped with feed liquor runner (702), air inlet runner in ontology
(703), mix runner (704) and multiple mixing chambers (705), the feed liquor runner, air inlet runner with the charging that mixes runner
End connection, the multiple mixing chamber are connected to mixing runner and are sequentially distributed along mixing runner, be equipped in mixing chamber and shunt member
Mixing chamber is divided into the sub- cavity of at least two by part (706).
5. residual hydrogenation equipment according to claim 4, which is characterized in that the quantity of the micro-channel mixer is parallel connection
Or it is concatenated multiple.
6. residual hydrogenation equipment according to claim 4, which is characterized in that the mixing chamber is flat, is integrally in the heart
One of type, circle, ellipse；The vent diverter is one of crescent, diamond shape, circle, ellipse.
7. residual hydrogenation equipment according to claim 4, which is characterized in that the cross-sectional area of the mixing runner is by feeding
Discharge end is held to be gradually increased, it is preferable that the cross-sectional area for mixing the feed end of runner is the 1.1-2 of discharge end cross-sectional area
Times.
8. residual hydrogenation equipment according to claim 1 to 3, which is characterized in that the mixed cell includes several metal films
Mixer and/or several ceramic membrane mixers.
9. -3, the described in any item residual hydrogenation equipments of 5-7 according to claim 1, which is characterized in that the fixed bed reactors
Including hollow tower body, the lower end of tower body is connected to mixed cell, the upper end of tower body and is communicated with outlet tube road, is equipped in tower body
Catalyst bed (9).
10. a kind of Residue Hydrotreating Technology, which is characterized in that using such as the described in any item residual hydrogenation equipments of claim 1-9
It carries out, includes the following steps:
The first pump of starting, opens first flow control valve, so that residual oil circulates between head tank and the first membrane filter,
Purification oil is obtained in the purified liquor outlet of the first membrane filter, which is inputted into Clear liquid tank；
Period, control first flow control valve opening, so that the flow and the first membrane filter purified liquor outlet of the first concentration liquid pipe
The ratio between flow be 25-30:1；
When the solid impurity content of the residual oil in head tank is more than 20g/L, second flow control valve is opened, so that the first film filters
The partial concentration slurry oil that device generates enters the second membrane filter, and the purification oil that the second membrane filter generates is sent into head tank, so that
The solid impurity content of residual oil is reduced to 20g/L or less in slurry oil head tank；
Purification oil in Clear liquid tank is inputted into mixed cell, while being passed through hydrogen to mixed cell, obtains gas mixture；
The gas mixture is passed through fixed bed reactors, under conventional liquid phase hydroprocessing condition, gas mixture and solid
Hydrogenation catalyst contacts in fixed bed reactor, obtains residual hydrogenation product.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910170413.7A CN109735364A (en) | 2019-03-07 | 2019-03-07 | A kind of residual hydrogenation equipment and technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910170413.7A CN109735364A (en) | 2019-03-07 | 2019-03-07 | A kind of residual hydrogenation equipment and technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109735364A true CN109735364A (en) | 2019-05-10 |
Family
ID=66369540
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910170413.7A Pending CN109735364A (en) | 2019-03-07 | 2019-03-07 | A kind of residual hydrogenation equipment and technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109735364A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112403412A (en) * | 2020-09-29 | 2021-02-26 | 合肥通用机械研究院有限公司 | Micro-reactor and reinforced mixing structure for same |
| CN115178191A (en) * | 2022-07-28 | 2022-10-14 | 扬州晨化新材料股份有限公司 | Polyether amine continuous production system and method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06285340A (en) * | 1993-04-07 | 1994-10-11 | Toto Ltd | Multistage separation by membrane and its system |
| US20090062590A1 (en) * | 2007-08-28 | 2009-03-05 | Nadler Kirk C | Process for separating a heavy oil feedstream into improved products |
| CN102448596A (en) * | 2009-05-29 | 2012-05-09 | 康宁股份有限公司 | Flow controlled microfluidic devices |
| CN103278028A (en) * | 2013-06-19 | 2013-09-04 | 长沙水泽加热设备制造有限公司 | Steam jet heater |
| CN108201847A (en) * | 2016-12-20 | 2018-06-26 | 浙江工业大学 | Based on the circular arc baffle plane passive type micro-mixer for strengthening mixing into vortex structure |
| CN210103853U (en) * | 2019-03-07 | 2020-02-21 | 湖南中天元环境工程有限公司 | Residual oil hydrogenation device |
-
2019
- 2019-03-07 CN CN201910170413.7A patent/CN109735364A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06285340A (en) * | 1993-04-07 | 1994-10-11 | Toto Ltd | Multistage separation by membrane and its system |
| US20090062590A1 (en) * | 2007-08-28 | 2009-03-05 | Nadler Kirk C | Process for separating a heavy oil feedstream into improved products |
| CN102448596A (en) * | 2009-05-29 | 2012-05-09 | 康宁股份有限公司 | Flow controlled microfluidic devices |
| CN103278028A (en) * | 2013-06-19 | 2013-09-04 | 长沙水泽加热设备制造有限公司 | Steam jet heater |
| CN108201847A (en) * | 2016-12-20 | 2018-06-26 | 浙江工业大学 | Based on the circular arc baffle plane passive type micro-mixer for strengthening mixing into vortex structure |
| CN210103853U (en) * | 2019-03-07 | 2020-02-21 | 湖南中天元环境工程有限公司 | Residual oil hydrogenation device |
Non-Patent Citations (2)
| Title |
|---|
| 华绍曾，杨学宁等编译: "实用流体阻力手册", 国防工业出版社, pages: 178 * |
| 林世雄: "《石油炼制工程（第三版）》", 31 July 2000, 石油工业出版社, pages: 432 - 434 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112403412A (en) * | 2020-09-29 | 2021-02-26 | 合肥通用机械研究院有限公司 | Micro-reactor and reinforced mixing structure for same |
| CN115178191A (en) * | 2022-07-28 | 2022-10-14 | 扬州晨化新材料股份有限公司 | Polyether amine continuous production system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102320910B (en) | Crude benzene hydrogenation method | |
| CN108264935B (en) | Suspension bed hydrogenation system for treating heavy oil | |
| CN109735364A (en) | A kind of residual hydrogenation equipment and technique | |
| CN101249405A (en) | Air-lift type circular current reactor | |
| CN202336337U (en) | Hydrogenation reaction kettle | |
| CN106076211A (en) | A kind of bubble-liquid two-phase jet reactor and bubble-liquid two-phase jet response system | |
| CN101418229A (en) | Mercaptans removal apparatus for light oil and mercaptans removal method thereof | |
| CN105566112A (en) | Continuous hydrogenation reaction method of organic intermediates and reactor thereof | |
| CN105085338B (en) | The production method and device of DMDS | |
| CN109731532A (en) | A kind of hydrocarbon oil hydrogenation reactor and method for hydrotreating hydrocarbon oil | |
| CN107056670B (en) | A kind of preparation method of two tertiary base peroxide | |
| CN210103853U (en) | Residual oil hydrogenation device | |
| CN101962352A (en) | Method for continuously producing p-menthane hydroperoxide by p-menthane and device thereof | |
| CN210079395U (en) | Residual oil hydrogenation device | |
| CN101508633A (en) | Process and apparatus for preparing methanal with low transformational cycle method | |
| CN209714969U (en) | A kind of hydrocarbon oil hydrogenation device | |
| CN100489064C (en) | Method for refining circulating hydrogen in hydrocracking process | |
| CN202860529U (en) | Reaction device for producing cyclohexene by partial hydrogenation of benzene | |
| CN214694015U (en) | Liquid phase hydrotreating system of distillate oil | |
| CN205556513U (en) | Continuous hydrogenation ware of organic intermediate | |
| CN101851531B (en) | Method for decolouring heavy alkylbenzene rectifying still bottom product | |
| CN109731513A (en) | A kind of residual hydrogenation equipment and method | |
| CN201793511U (en) | Continuous production device for preparing p-menthane hydroperoxide from p-menthane | |
| CN209442929U (en) | A kind of floating bed hydrogenation reaction unit | |
| CN208145922U (en) | A kind of exhaust system of liquid phase hydrogenation reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB03 | Change of inventor or designer information |
Inventor after: Xie Zhicheng Inventor after: Huang Deyou Inventor after: Yuan Nianwu Inventor before: Xie Zhicheng Inventor before: Huang Deyou Inventor before: He Xiaojun Inventor before: Yuan Nianwu |
|
| CB03 | Change of inventor or designer information |