CN107674704B - A kind of poor residuum floating bed hydrogenation method for transformation - Google Patents
A kind of poor residuum floating bed hydrogenation method for transformation Download PDFInfo
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- CN107674704B CN107674704B CN201711043502.2A CN201711043502A CN107674704B CN 107674704 B CN107674704 B CN 107674704B CN 201711043502 A CN201711043502 A CN 201711043502A CN 107674704 B CN107674704 B CN 107674704B
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- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/205—Metal content
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses a kind of poor residuum floating bed hydrogenation method for transformation.This method comprises the following steps: 1) hydrogen and the residual oil raw material containing catalyst preheat after mixing, enter Airlift circulating reactor after radial-axial quadratic distribution device, reaction mass axial rotary rising in Airlift circulating reactor is chemically reacted；2) reaction mass through chemically reacting enters high pressure and low pressure separator, completes crude conversion after separation.In the method for the present invention, raw material is after secondary efficient distribution, raw material and hydrogen is set sufficiently efficiently to be mixed into Airlift circulating reactor, gas-liquid mixture prolongs axial rotary rising, keep material and temperature uniform in radial distribution, since material prolongs axial rotary rising, increase material residence time (4 times) in reactor, improve conversion ratio, due to the revolving special designing of reactor, material coking in reactor is greatly reduced, realizes poor residuum Efficient Conversion and reduction coking in suspended-bed reactor.
Description
Technical field
The invention belongs to chemical technology field more particularly to a kind of poor residuum floating bed hydrogenation method for transformation.
Background technique
With crude oil become weight trend aggravation and heavy, the exploitation of super heavy crude and market to oil product, especially
Being continuously increased for various demand for fuel, mink cell focus by be 21 century important energy source；Mink cell focus especially high-sulfur, high pitch
The conversion of matter, high metal and high residual carbonaceous heavy oil will be still that 21 century petroleum refining is closed because it has high economic benefit
The important technology of note.Mink cell focus processing may bring the problems such as such as product quality decline, environmental protection, should be using corresponding
Proassing technique is solved.To the decompression residuum of crude oil with poor quality, because its sulphur, carbon residue and tenor are higher, it is intended to efficiently turn
Change, improve yield of light oil, reduce or prevent reactor coking and solve the problems, such as long-term operation, can only use at present plus hydrogen turns
Change the technical solution of processing or coking processing.As a kind of poor residuum processing technology, floating bed hydrogenation technology, which has, efficiently to be turned
Change feature has its unique excellent in terms of processing poor residuum, residual oil weight-lightening, high conversion, high desulfurization
Gesture.But the floating bed hydrogenation technology developed both at home and abroad at present has respective advantage and insufficient, most of floating bed hydrogenation skill
Art all in the development phase, there are conversion ratios it is low, desulfurization demetalization is low, air speed is low, reactor coking is serious the problems such as, this is directly
Affect technical application and on-stream time.Reactor coking is reduced, conversion ratio is improved, has great significance to petroleum refining industry.
Summary of the invention
It is anti-by using Airlift circulating the object of the present invention is to provide a kind of poor residuum floating bed hydrogenation method for transformation
Device and radial-axial quadratic distribution device are answered, Efficient Conversion of the poor residuum in suspended-bed reactor is realized and reduces coking.
A kind of poor residuum floating bed hydrogenation method for transformation provided by the invention, includes the following steps:
(1) hydrogen and the residual oil raw material containing catalyst preheat after mixing, and enter after radial-axial quadratic distribution device
Airlift circulating reactor, reaction mass axial rotary rising in the Airlift circulating reactor are chemically reacted；
(2) reaction mass through the chemical reaction enters high pressure and low pressure separator, completes crude conversion after separation；
Along the direction that material enters, the radial-axial quadratic distribution device successively includes radial distribution device and axial distribution
Device；The radial distribution device is the distributing barrel that one end is equipped with feed inlet, and the side wall of the distributing barrel is equipped with several radial distributions
Hole；The axial direction distributor is a distribution grid, and the surface of the distribution grid is equipped with several axial distribution holes；
The Airlift circulating reactor includes: shell, and the bottom of the shell has fluid inlet；Guide shell, it is described
Guide shell is vertically arranged in the shell by bracket, makes to form annular space between the shell and guide shell；Blade is more
The group blade is arranged at intervals on its outer wall along the short transverse of the guide shell, and the blade is in the guide shell
The setting of heart line；Helical baffles, the helical baffles set within it on wall around the center line of the guide shell.
In above-mentioned method, in the radial-axial quadratic distribution device, the radial distribution hole can uniformly be divided around a circle
Cloth is on the side wall of the distributing barrel.
The aperture in the radial distribution hole can be 0.1~1.0mm, such as 0.5mm.
The number in the radial distribution hole can be 4~20, such as 8.
The axial direction distribution hole can be evenly distributed on the periphery of the distribution grid around a circle.
The aperture of the axial direction distribution hole can be 0.1~1.0mm, such as 0.5mm.
The number of the axial direction distribution hole can be 8~32, such as 16.
The both ends of the axial direction distribution hole are in horn-like.Further, the horn-like cambered surface and the distribution grid can
In 45 degree of angles.Flare openings play the role of gas-liquid mixed when entering, and play gas-liquid distribution out.
In above-mentioned method, in the Airlift circulating reactor, blade described in every group includes being evenly distributed described
Multiple blades on water conservancy diversion drum outer wall, each blade can be in be obliquely installed upwards relative to the center line of the guide shell.
Each blade and level can be in 60 ° of angles.
The shell can be overlapped with the center line of both guide shells, settable around the bracket in the housing bottom
Multiple fluid inlets.
Above-mentioned method, in step (1), the volume of the volume of the hydrogen and the catalyst and the residual oil raw material it
The ratio of sum can be (800~1400): 1, concretely 1000:1.
The ratio of the catalyst and the poor residuum is determined by the property of the activity of the catalyst, selectivity and residual oil
Fixed, the content of such as catalyst can be 600~100ppm, such as 300ppm.The catalyst can be hydrogenation of residual oil suspended bed work
Conventional use of catalyst in skill, such as Mo catalyst series, Fe catalyst series or Ni catalyst series.
The temperature of the preheating can be 150~220 DEG C, such as 180 DEG C.
The pressure controllable system of the reactor is in 10~18Mpa, such as 12~16Mpa, 12Mpa, 14Mpa or 16Mpa；Temperature
Control is at 400~460 DEG C, and such as 420~460 DEG C, 420 DEG C, 440 DEG C or 460 DEG C；Volume space velocity (volume space velocity=(feed volume
Flow/h)/reactor volume) can be controlled in 0.5~1.5h-1, such as 0.5~1.0h-1、0.5h-1Or 1.0h-1。
Above-mentioned method, in step (2), gas after separation is measured by mass flowmenter, and liquid is in knockout drum bottom
Sampling.
The invention has the following beneficial effects:
The method of the present invention can increase substantially the conversion of poor residuum, and coking yield is low, and gas yield is low, specific as follows:
The present invention uses Airlift circulating reactor and the secondary efficient distributor of radial-axial, and material can be made anti-in circulation
It answers the linear velocity in device improving 1.5~2 times, enhances circulation effect, and make hydrogen and the raw material gas and liquid two phases in reactor
It comes into full contact with, catalyst is preferably dissolved and is dispersed in residual oil in reactor, when the contact of the reaction mass greatly increased
Between and the reaction time, and then improve bottoms conversion.
In the method for the present invention, raw material (residual oil) is mixed into raw material sufficiently efficiently with hydrogen after secondary efficient distribution
Entering Airlift circulating reactor, gas-liquid mixture prolongs axial rotary rising, and keep material and temperature uniform in radial distribution, due to
Material (gas-liquid mixture) prolongs axial rotary rising, increases material residence time (4 times) in reactor, improves conversion
Rate is greatly reduced material coking in reactor, is realized poor residuum and existed due to the revolving special designing of reactor
Efficient Conversion and reduction coking in suspended-bed reactor.
In short, the method for the present invention is that a kind of conversion ratio and air speed are high, material is evenly distributed, and desulfurization metal removal effect is ideal,
And the poor residuum floating bed hydrogenation Efficient Conversion of reactor coking can be reduced and reduce reactor method for coke.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of radial-axial quadratic distribution device in embodiment, wherein A is the vertical view of radial distribution device
Figure, B are the sectional view of radial distribution device；C is the overall structure figure of radial distribution device；D is the top view of axial distributor, and E is
The sectional view of axial distributor, F are the structural schematic diagram of axial distributor；
Fig. 2 is the overall structure diagram of Airlift circulating reactor in embodiment；
Fig. 3 is the structural schematic diagram of guide shell in embodiment；
Fig. 4 is the overlooking structure diagram of guide shell in embodiment；
Fig. 5 is for the structural schematic diagram of the helical baffles in embodiment on guide shell.
Fig. 6 is the structural schematic diagram of radial-axial quadratic distribution device and Airlift circulating reactor in embodiment.
Each digital representation is as follows in Fig. 1-Fig. 6:
I sealing flange, II radial distribution hole, III axial distribution hole, IV link flange, V Airlift circulating reactor, 1 shell
Body, 2 guide shells, 3 blades, 4 helical baffles, 5 brackets, 6 fluid inlets.
Specific embodiment
Experimental method used in following embodiments is conventional method unless otherwise specified.
The materials, reagents and the like used in the following examples is commercially available unless otherwise specified.
Catalyst as used in the following examples is that tetrathio molybdic acid is received, specifically according to a kind of entitled " four sulphur
The preparation method received for molybdic acid ", preparation method disclosed in embodiment 1 is prepared in Patent No. ZL201610115331.9.
As shown in figures 1 to 6, the direction (arrow direction, from the bottom up) entered along material, used in following embodiments
Radial-axial quadratic distribution device includes radial distribution device and axial distributor；In radial distribution device, radial distribution hole II is around one
Circle is evenly distributed on the side wall of distributing barrel；The outer diameter of distributing barrel is 6mm, internal diameter 4mm, is highly 7mm, bottom thickness is
1mm；The aperture in radial distribution hole II is 0.5mm；The number in radial distribution hole II is 8；In axial distributor, axial distribution hole
III is evenly distributed on the periphery of distribution plate surface around a circle；The diameter of distribution grid is 14mm, with a thickness of 2mm；Axial distribution hole
III aperture is 0.5mm；The number of axial distribution hole III is 16；In horn-like, this is horn-like at the both ends of axial distribution hole III
Cambered surface and distribution grid are in 45 degree of angles, and the height at horn-like both ends is 0.5mm.
Use process is as follows material enters in radial distribution device (arrow direction, from lower past from the feed inlet of radial distribution device
On), axial distributor is entered after the radial distribution in radial distribution hole, after the axial distribution of axial distribution hole, is realized efficient
Distribution.
As figures 2-6, Airlift circulating reactor as used in the following examples includes shell 1, guide shell 2, blade
3 and helical baffles 4；Guide shell 2 is vertically arranged in shell 1 by bracket 5, makes to form annular between shell 1 and guide shell 2
Space；Multiple groups blade 3 is set along short transverse interval on 2 outer wall of guide shell, and sets blade 3 around the center line of guide shell 2
It sets；Meanwhile helical baffles 4 are set around its center line in guide shell 2；The bottom of shell 1 has fluid inlet 6.Every group of rotation
Piece 3 includes being evenly distributed multiple blades on 2 outer wall of guide shell, each blade relative to the center line of guide shell 2 be in
On be obliquely installed；In such manner, it is possible to which turbulence state of the strengthening fluid when annular space flows, makes bubble be not easy to collect in a liquid
Poly-, solid is more evenly distributed in a liquid and is not easy to deposit, while increasing the stroke of fluid flowing, i.e., increase fluid (it is gas-solid-
Liquid) residence time in reactor, make fluid radial distribution more evenly.Each blade and level are in 60 ° of angles, are conducive to anti-
The mixed effect of gas-liquid-solid three-phase in device is answered, improves and flows intracorporal gas holdup or solid holdup.In both shell 1 and guide shell 2
Heart line is overlapped, and multiple fluid inlets 6 are arranged around bracket 5 in 1 bottom of shell.
Specification is as follows: reactor diameter=Φ 14mm, high H=56mm, the finned draft tube diameter of inside reactor
=Φ 6mm, reactor effective volume are 46mL.
Use process is as follows: fluid (gas-solid-liquid) is entered in reactor with certain speed through fluid inlet 6, in shell 1
3 spiral of blade in annular space between guide shell 2, and on 2 outer wall of guide shell, fluid cover the top of guide shell 2
Behind portion, fluid enters in guide shell 2, declines in guide shell 2 along 4 spiral of helical baffles, is again introduced into after flowing out guide shell 2
Annular space spiral moves upwards, so that fluid be made to be formed in reactor from circulation；Due to fluid inside and outside guide shell 2 equal edge
Helical flow path flowing, can increase intensity of circulation and residence time of the fluid in reactor, fluid guide shell 2 it is outer from lower and
Upstream cross blade 3 when generate shrink and expansion, can strengthening fluid turbulence, simultaneously as blade 3 and water conservancy diversion outside guide shell 2
Helical baffles 4 in cylinder 2 exist, and tangential flow are provided to flow intracorporal bubble, when blade of the fluid on 2 outer wall of guide shell
When 3 tangential flow at high speed, the fracture between blade 3 is struck, air pocket in fluid is cut by blade 3, is split into more stingy
Bubble, minute bubbles are acted on vulnerable to flow-disturbing, can not quickly be flowed up with object system, to increase stream of the bubble under the object system
The range ability of dynamic time and fluid system, keeps bubble uniform in size in fluid and uniform along reactor radial distribution, flows
Body is uniform in radial distribution, the concentration and uniformity of temperature profile of material, while gas holdup increases；Inside reactor entirety flow velocity adds
Fastly, due to the presence of blade and inside spin baffle plate outside guide shell, the flow resistance of fluid system is increased, makes internal flow shape
State becomes turbulent flow, is conducive to heat transfer, mass transfer and the momentum transmitting of fluid, is not easy the gas contained in fluid or solid from main body
It separates, is conducive to the progress of reaction, reduce the coking in reactor, easy solid is separated from fluid.
The floating bed hydrogenation conversion of embodiment 1, decompression residuum
Using CNOOC Huizhou refinery decompression residuum as raw material (feedstock property is as shown in table 1), in accordance with the following steps to subtracting
Residual oil is pressed to carry out floating bed hydrogenation conversion:
Table 1, feedstock property data
It is pumped with raw material according to 0.5h-1Volume space velocity contain 300ppm catalyst residual oil raw material and hydrogen according to volume
Than to enter preheating furnace after 1:1000 mixing, preheated stove heating enters radial-axial quadratic distribution device to 180 DEG C, is efficiently divided
Enter Airlift circulating reactor after cloth, in Airlift circulating reactor, the residual oil raw material containing catalyst and hydrogen prolong instead
The axial rotary rising of device is answered, poor residuum is chemically reacted in reactor, reactor pressure 12Mpa, and 420 DEG C of temperature, gas
Body and hydrogen come out from reactor head, and the reacted device top-side of product liquid, which exports out, enters height separator, reaction
After sampling analysis, open reactor and check reactor internals and wall coking situation.
Experimental result: conversion ratio 92.3m%, coking yield 2.25m%, gas yield 5.87m%.
The floating bed hydrogenation conversion of embodiment 2, decompression residuum
Using CNOOC Huizhou refinery decompression residuum as raw material (feedstock property is as shown in table 1), in accordance with the following steps to subtracting
Residual oil is pressed to carry out floating bed hydrogenation conversion:
It is pumped with raw material according to 1.0h-1Volume space velocity contain 300ppm catalyst raw material and hydrogen according to volume ratio be 1:
Enter preheating furnace after 1000 mixing, preheated stove heating enters radial-axial quadratic distribution device to 180 DEG C, is efficiently distributed laggard
Enter Airlift circulating reactor, in Airlift circulating reactor, the residual oil raw material containing catalyst and hydrogen prolong reactor axis
It is chemically reacted to rotatably rising, poor residuum in reactor, reactor pressure 14Mpa, 440 DEG C of temperature, gas and hydrogen
Gas comes out from reactor head, and the reacted device top-side of product liquid, which exports out, enters height separator, after reaction
Sampling analysis opens reactor and checks reactor internals and wall coking situation.
Experimental result: conversion ratio 94.25m%, coking yield 2.04m%, gas yield 6.45m%.
The floating bed hydrogenation conversion of embodiment 3, decompression residuum
Using CNOOC Huizhou refinery decompression residuum as raw material (feedstock property is as shown in table 1), in accordance with the following steps to subtracting
Residual oil is pressed to carry out floating bed hydrogenation conversion:
It is pumped with raw material according to 0.5h-1Volume space velocity contain 300ppm catalyst residual oil raw material and hydrogen according to 1:
Enter preheating furnace after 1000 mixing, preheated stove heating enters radial-axial quadratic distribution device to 180 DEG C, is efficiently distributed laggard
Enter Airlift circulating reactor, in Airlift circulating reactor, the residual oil raw material containing catalyst and hydrogen prolong reactor axis
It is chemically reacted to rotatably rising, poor residuum in reactor, reactor pressure 16Mpa, 460 DEG C of temperature, gas and hydrogen
Gas comes out from reactor head, and the reacted device top-side of product liquid, which exports out, enters height separator, after reaction
Sampling analysis opens reactor and checks reactor internals and wall coking situation.
Experimental result: conversion ratio 95.02m%, coking yield 3.15m%, gas yield 7.52m%.
Claims (8)
1. a kind of poor residuum floating bed hydrogenation method for transformation, includes the following steps:
(1) hydrogen and the residual oil raw material containing catalyst preheat after mixing, and gas lift is entered after radial-axial quadratic distribution device
Formula circulation flow reactor, reaction mass axial rotary rising in the Airlift circulating reactor are chemically reacted；
(2) reaction mass through the chemical reaction enters high pressure and low pressure separator, completes crude conversion after separation；
Along the direction that material enters, the radial-axial quadratic distribution device successively includes radial distribution device and axial distributor；
The radial distribution device is the distributing barrel that one end is equipped with feed inlet, and the side wall of the distributing barrel is equipped with several radial distribution holes；
The axial direction distributor is a distribution grid, and the surface of the distribution grid is equipped with several axial distribution holes；
The Airlift circulating reactor includes:
The bottom of shell, the shell has fluid inlet；
Guide shell, the guide shell are vertically arranged in the shell by bracket, make to be formed between the shell and guide shell
Annular space；
Blade, blade described in multiple groups is arranged at intervals on its outer wall along the short transverse of the guide shell, and the blade is around institute
State the center line setting of guide shell；
Helical baffles, the helical baffles set within it on wall around the center line of the guide shell.
2. according to the method described in claim 1, it is characterized by: in the radial-axial quadratic distribution device,
The radial distribution hole is evenly distributed on the side wall of the distributing barrel around a circle；
The aperture in the radial distribution hole is 0.1~1.0mm；
The number in the radial distribution hole is 4~20.
3. method according to claim 1 or 2, it is characterised in that: in the radial-axial quadratic distribution device,
The axial direction distribution hole is evenly distributed on the periphery of the distribution grid around a circle；
The aperture of the axial direction distribution hole is 0.1~1.0mm；
The number of the axial direction distribution hole is 8~32.
4. method according to claim 1 or 2, it is characterised in that: the both ends of the axial direction distribution hole are in horn-like；It is described
Horn-like cambered surface and the distribution grid are in 45 degree of angles.
5. method according to claim 1 or 2, it is characterised in that: in the Airlift circulating reactor, revolved described in every group
Piece includes the multiple blades being evenly distributed on the water conservancy diversion drum outer wall, and each blade is relative in the guide shell
Heart line is in be obliquely installed upwards.
6. according to the method described in claim 5, it is characterized by: in the Airlift circulating reactor, each blade
It is in 60 ° of angles with level.
7. method according to claim 1 or 2, it is characterised in that: in the Airlift circulating reactor, the shell with
The center line of both guide shells is overlapped, and multiple fluid inlets are arranged around the bracket in the housing bottom.
8. method according to claim 1 or 2, it is characterised in that: the pressure of the reactor is controlled in 10~18Mpa；
Temperature is controlled at 400~460 DEG C；Volume space velocity is controlled in 0.5~1.5h-1。
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| CN1233454C (en) * | 2003-09-28 | 2005-12-28 | 上海兖矿能源科技研发有限公司 | Gas distributor in use for reactor in slurry state bed in three phases |
| US20080107575A1 (en) * | 2004-12-08 | 2008-05-08 | Vetter Michael J | Apparatus and process for reacting fluid over catalyst bed |
| CN101249405A (en) * | 2008-04-03 | 2008-08-27 | 中国石化扬子石油化工有限公司 | Air-lift type circular current reactor |
| US8092755B2 (en) * | 2009-04-06 | 2012-01-10 | Lummus Technology Inc. | Devices for injection of gaseous streams into a bed of fluidized solids |
| CN102166501B (en) * | 2011-03-04 | 2013-05-29 | 清华大学 | Airlift-jet multi-stage loop reactor |
| CN204466707U (en) * | 2015-02-13 | 2015-07-15 | 冯红玉 | Ultra-low volume directional electrical centrifugal atomizer |
| CN105694959B (en) * | 2016-02-03 | 2017-08-22 | 浙江大学 | A kind of ejection-type common loop reactor for hydrocracking heavy oil |
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