CN2547391Y - Loop reactor with up and down double discharge functions - Google Patents
Loop reactor with up and down double discharge functions Download PDFInfo
- Publication number
- CN2547391Y CN2547391Y CN 02232887 CN02232887U CN2547391Y CN 2547391 Y CN2547391 Y CN 2547391Y CN 02232887 CN02232887 CN 02232887 CN 02232887 U CN02232887 U CN 02232887U CN 2547391 Y CN2547391 Y CN 2547391Y
- Authority
- CN
- China
- Prior art keywords
- reactor
- circulation tube
- circulation
- discharge function
- liquid
- 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
Images
Landscapes
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
A new-type loop reactor with up and down double discharge functions belongs to the petroleum process or coal liquification process consersion unit and mainly comprises a loop shell set in the reactor, a ring gas distributor in the reactor and a material feeding pipe tangential to a reactor shell and so on, so that the material flow reacted in the reactor is of a loop shape and discharge can be achieved up and down of the reactor in case of air. The utility model can be applied to the reacting process of air, liquor and solid existing at the same time, in particular to the heavy oil (atmospheric residue, vacuum residue and viscous oil) slurry bed hydrocracking process utilizing a light concentration and high dispersing catalytic agent.
Description
The utility model relates to a kind of novel circulation flow reactor of bidirectional discharge function up and down that has, and belongs to the consersion unit in PETROLEUM PROCESSING or the coal liquefaction craft, and it can be used for gas, liquid and the simultaneous course of reaction of solid three-phase.Be specially adapted to use heavy oil (reduced crude, decompression residuum, the consistency crude oil) hydrocracking process of suspended bed of low concentration, dispersed catalysts.It mainly is by the circulation tube group that is arranged at inside reactor, annular gas distributor and is tangential material feeding tube etc. with reactor shell and constitutes, thereby make the logistics of portion's reaction within it be the circulation shape, and be able under the situation at the two ends up and down of reactor discharge there being gas to exist.
At present, the used reactor of suspension bed hydrogenation process in the world, mostly be the up-flow reactor that goes out on advancing under the material, interim coke discharging mouth has also been added in the bottom of the reactor that has, these reactors are applicable to the process of big (about 3 ~ 10%) of catalyst amount usually, as Canmet technology, or solid particle reaches tens percent coal dust and heavy oil and refines altogether and liquefaction process.Because the existence of a large amount of catalyst or pulverized coal particle, Jiao who generates in the course of reaction can be attached on catalyst or the pulverized coal particle, and discharge outside the reactor with it, even there is part temporarily can not be discharged from, because the existence of a large amount of catalyst and solid particle, they can not be gathered into big coke button mutually yet.But be deposited on the solid particle of reactor bottom, can influence the long-term operation of device, have to sometimes discharge by interim coke discharging mouth.
In the hydrocracking process of suspended bed of heavy oil, heavy oil has burnt the generation when being cracked into lighter hydrocarbons, light oil.But using low concentration (as the amount of metal of catalyst less than 0.5%), dispersed catalysts (metallic salt solution, organo-metallic compound, or their mixture is dispersed in the heavy oil) the heavy oil floating bed hydrocracking process in, even Jiao that reaction generates measures not very big (as 1%), burnt amount has been a large amount of with respect to the amount of catalyst, because the burnt grain that generates is the comparison thickness, if can not in time discharge outside the reactor, in the hot environment in reactor, be deposited on the burnt grain of reactor bottom, will be agglomerated into piece together with the catalyst granules of high dispersive, even reactor bottom is provided with interim coke discharging mouth, also can't discharge reactor, stop up reactor the most at last.For Jiao who generates being discharged outside the reactor, can improve the linear velocity of liquid material in the reactor, so that Jiao is given rise to the outlet on reactor top.And improve the method for liquid linear velocity, adopt the method for circulating pump usually.This circulating pump that utilizes is extracted liquid material out from reactor top, squeeze into reactor lower part then, improves the method for liquid linear velocity, still exists problem.Owing in course of reaction, need hydrogen to be mixed with feedstock oil, and mix to such an extent that the complete reaction effect is good more more by the hydrogen distributor.When from the top of reactor material being squeezed into the bottom with circulating pump, need be with hydrogen and oily the separation, the gas that contains in the material is few more, then the easy more raising pump speed of circulating pump.And feedstock oil mixes fully more with hydrogen, separates just difficultly more with oil at reactor head gas, and this can only bring up to the linear velocity of liquid in the reactor about 3cm/s usually with regard to having limited circulating pump.If want further to improve the flow velocity of liquid by the rotating speed that improves pump, will be owing to the increase of gas content from the material of top suction, generation vapour lock and pump can't be run well.Even under such liquid speed, the material in the reactor also exists density contrast, promptly Jiao who generates in the course of reaction is more at reactor bottom, and is less at the top.And material is discharged from reactor head, after Chen Ji Jiao stagnates a period of time in reactor like this, will form bulk and stops up reactor.Another problem be can't guarantee circulating pump can be under high temperature, high pressure long-term operation continuously, in case circulating pump breaks down, Jiao of generation will deposit to the bottom of reactor rapidly.Usually, the solution of problem has 2 points, and the first makes material discharge from reactor bottom, like this no matter whether Jiao who generates to the bottom sedimentation, can both discharge; It two is to change the material endless form, owing to exist the localized heat release phenomenon in the course of reaction, and should not eliminate with the method for annotating cold hydrogen, the material circulation must keep.Traditional circulation flow reactor is exactly to consider from the endless form that changes material, relies on the effect of circulation tube, rather than circulating pump, improves the linear velocity of liquid in reactor, and then improves the lifting force of liquid to solid particle, and Jiao is given rise to the reactor head outlet.But traditional circulation flow reactor can not thoroughly solve the problem that coke is assembled in the bottom in the heavy oil floating bed hydrocracking process of using the low concentration catalyst.In addition, traditional circulation flow reactor also exists following five shortcomings: one, because it pursues high liquid linear velocity, liquid dispersion is too serious, just entered the fresh feed in the reactor, complete reaction is not just from the discharging opening discharge at top for some, and conversion of raw material is low; Its two because the linear velocity height of liquid, the speed that hydrogen rises is also fast, to account for the ratio (gas holdup just) of liquid lower for hydrogen in the reactor, the hydrogenation weak effect; Its three, the hydrogen that contains in the liquid charging stock between circulation drum outer wall and reactor wall is less, green coke reaction is more serious; Its four, gas-liquid separation zone is arranged at the top of traditional circulation flow reactor, at the intersection of gas-liquid, reactor wall adheres to coke easily when processing heavy oil; Its six because gas-liquid separation zone is arranged at the top of traditional circulation flow reactor, the utilization rate of reactor is lower, can only use 70～80% of reactor volume usually.
The purpose of this utility model provides a kind of circulation flow reactor of bidirectional discharge function up and down that has with regard to being to avoid the deficiencies in the prior art part.It mainly is to have adopted at inside reactor the circulation tube to be set and the method for tangential admission mouth is set at reactor bottom, and utilize gas to produce the inside and outside density contrast of circulation tube, make it both have traditional circulation flow reactor and eliminate the local heat effect of reactor, make material keep the advantage of appropriate back-mixing, reactor temperature homogeneous; Have flow reactor average gas traditionally again and contain rate height, advantage that the reactor utilization rate is high.The mode that it adopts material to discharge simultaneously up and down from reactor can make Jiao get rid of from reactor bottom, has eliminated the shortcoming that traditional circulation flow reactor top gas-liquid separation zone reactor wall adheres to coke again, has also improved the utilization rate of reactor.Simultaneously, improve the distribution of hydrogen, the difficult arrival of the interior hydrogen gas bubbles of circulation flow reactor district is significantly reduced, reduced the green coke of course of reaction.It mainly is reactor shell, built-in circulation tube, annular gas distributor and special-purpose formations such as tangential admission mouth, its major technology characteristics are that circulation tube group is arranged on the inside of reactor along reactor axis, the annular gas distributor then is provided with the bottom with reactor, and placing that the circulation tube is outer to be connected with the gas access, the feed(raw material)inlet then is to form an angle tangentially and with the cross section of reactor to be arranged on the bottom of reactor.
Accompanying drawing 1 is structural representation of the present utility model.
Accompanying drawing 2 is the structural representation in the utility model A-A cross section.
Accompanying drawing 3 is the structural representation in the utility model B-B cross section.
Accompanying drawing 4 is the structural representation in the utility model C-C cross section.
In order to realize better above-mentioned purpose of the present utility model, designer of the present utility model is designed to a list with the circulation tube The cylinder of one upper and lower opening. Then can be by the series connection of single hop or multistage circulation tube for the circulation tube group that is arranged at inside reactor Form, its total height is 30～90% of reactor inner chamber height, the outer diameter of its circulation tube be 20 of reactor wall diameter～80%. Can be formed by one or more feed pipes for the feed(raw material)inlet that is arranged at reactor bottom, and and reactor cross-section Become 0～45 degree angle, and reactor outer wall circumference can become 0～60 angle of spending with the axial line of its feed pipe.
The drawing of accompanying drawing is described as follows:
1---circulation tube group 2---reactor shell 3---circulation tube bracing frame 4---thermocouple
The upper discharge gate 8---feed pipe of 5---gas distributor 6---reactor loam cake 7---
Drainage conduit under the 9---gas inlet pipe 10---
Below in conjunction with drawings and Examples in detail design feature of the present utility model is described in detail:
In actual design with in making, the utility model is achieved in that the circulation tube is housed in the housing of reactor, and this circulation tube is than the diameter of the circulation tube of traditional circulation flow reactor and highly all little.With circulation tube supporting construction the circulation tube is fixed in the reactor.One or more tangential admission mouths are arranged at the bottom at the reactor of thickening, and after the liquid material of process preheating enters reactor from the tangential admission mouth, rise along the rotation of the space between circulation drum outer wall and the reactor wall.The temperature-measuring heat couple sleeve pipe is installed on the position at axle center in the circulation tube, produces eddy current when preventing the material rotational flow.In the bottom of reactor, the hydrogen distributor of dress annular between circulation drum outer wall and reactor wall.The inner member loading port is arranged at the top of reactor, and the diameter of mouth is not less than the external diameter of circulation tube and hydrogen distributor.Gas enters reactor by the hydrogen distributor.Reacted material is discharged by constant flow from the discharge gate of reactor bottom, and this flow is less than the feed rate of liquid material, and the material behind the remaining reaction is discharged from the discharge gate of reactor head.Owing to adopted the mode of two-way discharge about internal diameter and highly less circulation tube and the material, the lower part of reactor is similar to traditional circulation flow reactor, the top of reactor is similar to traditional up-flow reactor, it can allow the interior material of reactor be in appropriate back-mixing state, eliminate the hot-spot in the reactor in the course of reaction, make temperature maintenance homogeneous everywhere in the reactor; It can strengthen the time of contact of liquids and gases; Simultaneously, the solid particle that produces in the course of reaction promptly can be discharged reactor, be unlikely in reactor, to be agglomerated into bulk solid.Because the circulation tube of the circulation tube aspect ratio that adopts tradition circulation flow reactor is little, fresh material is again to enter reactor in the mode that rotation is risen, excessive back-mixing between the material that has reduced fresh feed and reacted, the result is gas and burnt minimizing that reaction generates, conversion ratio improves.
Compared with prior art, utility model has following outstanding characteristics:
(1) Tong up-flow reactor is compared, and reactor is in full back-mixing state at the maintenance material, eliminates aspect the local heat effect in the reactor, is not to adopt the mode of using circulating pump, but adds the circulation tube in reactor, the method for employing circulation.
(2) compare with traditional circulation flow reactor, the height and the internal diameter of the circulation tube of reactor are less, have reduced the degree of material back-mixing, and the hydrogen gas holdup of integral reactor is higher.
(3) compare with circulation flow reactor with traditional up-flow reactor, the utility model has reduced the deposition of solid particles such as catalyst and Jiao at reactor bottom circular arc place in the mode of reactor bottom with tangential admission.Rise because liquid material is rotation, and carry the hydrogen rotation and rise the time of contact that has increased liquid and hydrogen like this.
(4) flow direction of the material of the reactor that utility model provided rises along circulation tube inner rotary usually, along descending in the circulation tube.
(5) reactor use circulation tube provided by the utility model is in order to eliminate the local heat effect of reactor, to make material keep the temperature homogeneous.Reactor will with accelerator activator particle and burnt to the reactor bottom sedimentation, be got rid of by the discharge gate of reactor bottom getting reduction circulation liquid velocity under the situation when work.Because the circulation liquid velocity is less in the reactor, gas time of staying in reactor is longer, and gas holdup is higher in the reactor, and the utilization rate of gas is just higher.
(6) under same reaction conditions, the conversion ratio height of raw material in reactor provided by the utility model.After fresh feed tangentially enters reactor from the outside of circulation tube, outside the circulation tube sideway swivel upwards, the circulation liquid velocity is slower, the material back-mixing is not too serious, from the material that reactor bottom is discharged, the ratio of the fresh material of complete reaction does not reduce, so the conversion ratio height.
(7) difference of hydrogen distribution.Except small part hydrogen injects in the stokehold, improve outside the speed of feedstock oil in boiler tube, most of hydrogen is that the hydrogen distributor by annular enters reactor.That is, the mode that adopts hydrogen and feedstock oil to enter reactor respectively, rather than the mixed feeding of hydrogen G﹠O.Can reduce the possibility of coking on the distributor like this.
(8) the liquid charging of traditional up-flow reactor and traditional circulation flow reactor enters from reactor bottom, discharge from reactor head, the power of discharging is flowing naturally by charging, when running into contingency or device power failure, the liquid that is full of whole reactor can't be discharged, and have green coke to stop up the possibility of reactor.The liquid charging of the reactor that the utility model is related enters from reactor bottom, discharge simultaneously from reactor bottom and top, the power of discharging is by the pressure differential between reactor and the post-processing unit, when running into contingency or device power failure, can the liquid in the reactor all be discharged by pressure differential.
Claims (4)
1. has the circulation flow reactor of bidirectional discharge function up and down, it mainly is by reactor shell (2), built-in circulation tube (1), annular gas distributor (5) and special-purpose tangential admission mouth formations such as (8), it is characterized in that circulation tube group (1) is arranged on the inside of reactor along reactor axis, annular gas distributor (5) then is arranged on the bottom of reactor, and placing the circulation tube outside to be connected with gas access (9), the feed pipe of feed(raw material)inlet (8) then is to form an angle tangentially and with the cross section of reactor to be arranged on the bottom of reactor.
2. according to claim 1 have a up and down circulation flow reactor of bidirectional discharge function, it is characterized in that described circulation tube is the cylinder of a single upper and lower opening.
3. according to claim 1 have a up and down circulation flow reactor of bidirectional discharge function, it is characterized in that the described circulation tube group (1) that is arranged at inside reactor can be to be in series by single hop or multistage circulation tube, its total height is 30～90% of a reactor inner chamber height, and the outer diameter of its circulation tube is 20～80% of a reactor wall diameter.
4. according to claim 1 have a up and down circulation flow reactor of bidirectional discharge function, it is characterized in that the described reactor bottom charging aperture that is arranged at can be made up of one or more feed pipes (8), and becoming 0～45 degree angle with reactor cross-section, reactor outer wall circumference becomes 0～60 angle of spending with the axial line of its feed pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02232887 CN2547391Y (en) | 2002-05-23 | 2002-05-23 | Loop reactor with up and down double discharge functions |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02232887 CN2547391Y (en) | 2002-05-23 | 2002-05-23 | Loop reactor with up and down double discharge functions |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2547391Y true CN2547391Y (en) | 2003-04-30 |
Family
ID=33708163
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02232887 Expired - Lifetime CN2547391Y (en) | 2002-05-23 | 2002-05-23 | Loop reactor with up and down double discharge functions |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2547391Y (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101274245B (en) * | 2007-03-28 | 2010-09-01 | 中国石油大学(北京) | Annular space air-lift gas-solid loop flow reactor |
| CN101481433B (en) * | 2008-01-08 | 2011-04-20 | 李长荣化学工业股份有限公司 | Hydrogenation reaction system for conjugated diolefine polymer |
| CN111097337A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN111744437A (en) * | 2020-06-05 | 2020-10-09 | 洛阳瑞华新能源技术发展有限公司 | Gas-liquid-solid three-phase suspended bed reactor system with liquid circulation and without lower distribution plate |
-
2002
- 2002-05-23 CN CN 02232887 patent/CN2547391Y/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101274245B (en) * | 2007-03-28 | 2010-09-01 | 中国石油大学(北京) | Annular space air-lift gas-solid loop flow reactor |
| CN101481433B (en) * | 2008-01-08 | 2011-04-20 | 李长荣化学工业股份有限公司 | Hydrogenation reaction system for conjugated diolefine polymer |
| CN111097337A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN111097337B (en) * | 2018-10-25 | 2022-04-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN111744437A (en) * | 2020-06-05 | 2020-10-09 | 洛阳瑞华新能源技术发展有限公司 | Gas-liquid-solid three-phase suspended bed reactor system with liquid circulation and without lower distribution plate |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US20190321833A1 (en) | Separation device | |
| WO2020143140A1 (en) | Separation system for slurry bed reactor | |
| CN2547391Y (en) | Loop reactor with up and down double discharge functions | |
| CN113083169B (en) | Fluidized bed hydrogenation reactor and using method thereof | |
| CN201260960Y (en) | Novel reactor | |
| CN101301640B (en) | Cyclone separating device | |
| CN2538416Y (en) | Circulation reactor for hydrocracking process of heavy oil suspension bed | |
| CN2782685Y (en) | Radial reactor for Ficcher-Tropsch Oil | |
| CN206139357U (en) | Tangential entry separates assembly and uses contrajet cyclone of this separation assembly | |
| CN1283349C (en) | Highly effective slurry phase bed reactor | |
| CN104388124A (en) | Entrained flow bed gasifier | |
| CN2548696Y (en) | Loop reactor with lower discharge for suspension hydrocracking process | |
| CN107519826A (en) | A kind of suspended-bed reactor and the method that liquid phase self-loopa is realized using the reactor | |
| CN215610317U (en) | Catalytic reforming oil gas filtering device | |
| CN1657150A (en) | Riser reactor for hydrocarbon fluidized catalytic conversion | |
| CN103769007B (en) | A kind of fluidized bed reactor | |
| CN210826069U (en) | Upper and lower double-heat high-resolution suspension bed reaction device | |
| CN205109603U (en) | Novel fluidized bed reactor | |
| CN2463042Y (en) | Fluidizing, catalyzing and inverting stripper | |
| CN206483444U (en) | A kind of suitable Low Temperature Fischer Tropsch synthesis powder catalyst charge groove | |
| CN208944069U (en) | A kind of Novel suspending bed hydroprocessing reactor | |
| CN206285874U (en) | A kind of double material slurry-bed hydrocracking device of outer circulation type | |
| CN205095762U (en) | Slurry bed reactor | |
| CN113244860B (en) | Fluidized bed hydrogenation reactor and using method thereof | |
| CN219449622U (en) | Elbow reactor for pulverized coal second-level fast pyrolysis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |
Expiration termination date: 20120523 Granted publication date: 20030430 |