CN205095762U - Slurry bed reactor - Google Patents
Slurry bed reactor Download PDFInfo
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- CN205095762U CN205095762U CN201520848831.4U CN201520848831U CN205095762U CN 205095762 U CN205095762 U CN 205095762U CN 201520848831 U CN201520848831 U CN 201520848831U CN 205095762 U CN205095762 U CN 205095762U
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Abstract
The utility model relates to a petrochemical equipment field discloses a slurry bed reactor, include: reactor casing (1), the lower part of this reactor casing is provided with unloads agent mouthful (12), air inlet (11) and raw oil entry (14), and the upper portion of this reactor casing is provided with gas outlet (9), adds agent mouthful (13) and result oil export (10), the inner space of reactor casing (1) constitutes reactor chamber (8), and the upper portion in this reactor chamber is provided with hydrocyclone (2), reaction material in the reactor chamber gets into from hydrocyclone entry (4) hydrocyclone separates in (2). The utility model provides a novel slurry bed reactor can effectively maintain the content of reactor's catalyst, improves the agent oil ratio to improve reaction efficiency.
Description
Technical field
The utility model relates to a kind of petrochemical equipment, particularly, relates to a kind of paste state bed reactor.
Background technology
Along with heaviness and the in poor quality of crude quality, the processing mode such as catalytic cracking and fixed bed hydrogenation to metal and the higher residual oil disposal ability of carbon residue not enough.Other heavy oil product is as moisture containing solid feature in coal tar wet goods also has, and traditional fixed bed hydrogenation mode is also difficult to direct process.Therefore, slurry bed system hydrogenation mode is the industrial development direction of following processing heavy oil product.
Paste state bed reactor is the consersion unit of the gas-liquid-solid three-phase contact that petrochemical industry is commonly used.Liquid phase is continuous phase, and gas phase and solid phase are decentralized photo.Paste state bed reactor has bed to have a narrow range of temperature, move that the thermal efficiency is high, back-mixing degree is high and can load and unload the advantages such as catalyst online.
At the initial stage of paste state bed reactor development, main development application slurry bed system bubbling reactor.Slurry bed circulatory flow reactor is the paste state bed reactor form developed on slurry bed system bubbling reactor basis.The use gas that slurry bed circulatory flow reactor has is as lifting power, and the mode of some use pumped slurry is as lifting power.
The feature of usual paste state bed reactor be after catalyst mixes with feedstock oil together with enter reactor, after reaction certain hour, oil, agent another flow out from reactor.This operator scheme makes the catalyst content in reactor be in reduced levels.
CN1458234A discloses a kind of oil residual oil processing method and equipment, and adopt the ebullated bed process residual oils of multistage difference in functionality in a reactor, its catalyst substrates is aluminium oxide, and active component is molybdenum and nickel, and catalyst particle size is between 50-400 μm.After catalyst particle size reduces, carrying velocity decreases, and in order to maintain ebullated bed operator scheme, the liquid phase linear speed in bed must decline, otherwise catalyst is taken out of, affects downstream process.
CN102309949A discloses a kind of floating bed hydrogenation reactor with high-pressure separator and method, and use disc type oil catcher that reactor is divided into upper and lower two parts, the latter half is floating bed hydrogenation reaction zone, and the first half is for stablize Disengagement zone.The slurries reacted, in the stable Disengagement zone on top, add the flux oil being rich in aromatic hydrocarbons, avoid coking.The prior art is the combination of conventional bubble slurry bed and high-pressure separator, but can not solve the problem of catalyst device Inner eycle, and the time of staying of catalyst in reactor is shorter.
From analyzing above, it is the subject matter restricting slurry bed system working (machining) efficiency that the concentration of paste state bed reactor inner catalyst maintains with being efficiently separated.
Utility model content
The purpose of this utility model is the above-mentioned defect overcoming prior art, provides a kind of content that effectively can maintain the catalyst in reactor, improving agent oil ratio, thus improves the novel pulpous bed bioreactor of reaction efficiency.
To achieve these goals, the utility model provides a kind of paste state bed reactor, and this reactor comprises:
Reactor shell, the bottom of this reactor shell is provided with unloads agent mouth, air inlet and feedstock oil entrance, and the top of this reactor shell is provided with gas outlet, adds agent mouth and product oil outlet;
The inner space of described reactor shell forms reactor inner chamber, the top of this reactor inner chamber is provided with cyclone hydraulic separators, reaction mass in described reactor inner chamber enters described cyclone hydraulic separators from spin liquid separator entrance and is separated, separating obtained rich solid content component is back to described reactor inner chamber from the underflow pipe of described cyclone hydraulic separators bottom, separating obtained poor solid content component leads to reactor from described product oil outlet, and separating obtained gas phase leads to described cyclone hydraulic separators from gaseous phase outlet.
Preferably, described cyclone hydraulic separators is one-level or at least two-stage, being separated the described poor solid content component obtained in the cyclone hydraulic separators of the previous stage in the described cyclone hydraulic separators of at least two-stage enters in adjacent rear stage cyclone hydraulic separators, be separated the described rich solid content component that obtains to be back to described reactor inner chamber from underflow pipe, and be separated the described poor solid content component obtained in afterbody cyclone hydraulic separators and draw reactor from described product oil outlet.
Preferably, the bottom of described reactor inner chamber is also provided with the sleeve making reaction mass carry out Inner eycle in described reactor inner chamber, and the bottom of described sleeve is less than described sleeve diameter by internal diameter and the conduit stretching into described sleeve inner is communicated with the air inlet of described reactor shell.
Preferably, described sleeve is one or at least two, is provided with gas distributor between the described conduit of the described lower cartridge of at least two and described air inlet.
Preferably, the length of described sleeve is 1/4 to 3/4 of the length of described reactor shell.
Preferably, the diameter of described sleeve is 1/100 to 3/4 of the diameter of described reactor shell.
Preferably, the underflow pipe of described sleeve and described cyclone hydraulic separators bottom is set to interlaced.
Preferably, the length of described underflow pipe is 1/5 to 9/10 of described length sleeve.
Preferably, the length stretching into described sleeve inner of described conduit is 1/1000 to 1/10 of described length sleeve.
Preferably, the height of described spin liquid separator entrance is higher than the overhead height of described sleeve, and both differences in height are 1/200 to 1/2 of the length of described reactor shell.
Preferably, the height of described gaseous phase outlet is higher than the height of described spin liquid separator entrance, and both differences in height are 1/50 to 1/4 of the length of described reactor shell.
The novel pulpous bed bioreactor that the utility model provides effectively can maintain the content of the catalyst in reactor, improving agent oil ratio, thus improves reaction efficiency.
Under preferable case, the combination of the cyclone hydraulic separators that the utility model uses and sleeve, gas is entered in sleeve, rich solid content component in cyclone hydraulic separators enters reactor inner chamber downwards by underflow pipe, utilizes the flowing of the lift of gas in sleeve and the outer liquid of sleeve, and the density contrast inside and outside sleeve, form efficient device Inner eycle, improve liquid speed, avoid the sedimentation of catalyst, the transmission effect of heat and material also can improve.
The utility model arranges cyclone hydraulic separators in paste state bed reactor inside, utilizes slurries to rotate the centrifugal force produced and can form two kinds of different slurries of catalyst content in separator.The slurries (rich solid content component) that catalyst content is higher return reaction bed.The slurries outflow reactor of catalyst content lower (poor solid content component), maintains liquid phase turnover balance.Meanwhile, owing to have employed cyclone hydraulic separators, in bed, catalyst content can significantly promote, and is that general slurry bed system is beyond one's reach.
Other features and advantages of the utility model are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide further understanding of the present utility model, and forms a part for description, is used from explanation the utility model, but does not form restriction of the present utility model with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the structural representation of the paste state bed reactor of a kind of preferred detailed description of the invention of the present utility model.
Description of reference numerals
1, reactor shell 2, cyclone hydraulic separators
3, sleeve 4, spin liquid separator entrance
5, gaseous phase outlet 6, underflow pipe
7, gas distributor 8, reactor inner chamber
9, gas outlet 10, product oil outlet
11, air inlet 12, unload agent mouth
13, agent mouth 14, feedstock oil entrance is added
Detailed description of the invention
Below detailed description of the invention of the present utility model is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
The utility model provides a kind of paste state bed reactor, and this reactor comprises:
Reactor shell 1, the bottom of this reactor shell is provided with unloads agent mouth 12, air inlet 11 and feedstock oil entrance 14, and the top of this reactor shell is provided with gas outlet 9, adds agent mouth 13 and product oil outlet 10;
The inner space of described reactor shell 1 forms reactor inner chamber 8, the top of this reactor inner chamber is provided with cyclone hydraulic separators 2, reaction mass in described reactor inner chamber enters described cyclone hydraulic separators 2 from spin liquid separator entrance 4 and is separated, separating obtained rich solid content component is back to described reactor inner chamber 8 from the underflow pipe 6 of described cyclone hydraulic separators 2 bottom, separating obtained poor solid content component leads to reactor from described product oil outlet 10, and separating obtained gas phase leads to described cyclone hydraulic separators 2 from gaseous phase outlet 5.
In the above-mentioned paste state bed reactor that the utility model provides, gas enters the slurries of reactor inner chamber from air inlet, cause slurries to carry out relative motion in reactor inner chamber thus be conducive to react carrying out.And, slurries containing gas, solid, liquid three-phase enter described cyclone hydraulic separators from spin liquid separator entrance and are separated, relatively light gas phase leads to described cyclone hydraulic separators from gaseous phase outlet, and the more rich solid content component of solid content is back to described reactor inner chamber from the underflow pipe of described cyclone hydraulic separators bottom and recycles, and the less poor solid content component of solid content leads to reactor from described product oil outlet to carry out further Separation of Solid and Liquid or other operating unit.
The above-mentioned novel pulpous bed bioreactor that the utility model provides effectively can maintain the content of the catalyst in reactor, improving agent oil ratio, thus improves reaction efficiency.
Preferably, described cyclone hydraulic separators 2 is one-level or at least two-stage, being separated the described poor solid content component obtained in the cyclone hydraulic separators 2 of the previous stage in the described cyclone hydraulic separators 2 of at least two-stage enters in adjacent rear stage cyclone hydraulic separators 2, be separated the described rich solid content component that obtains to be back to described reactor inner chamber 8 from underflow pipe 6, and be separated the described poor solid content component obtained in afterbody cyclone hydraulic separators 2 and draw reactors from described product oil outlet 10.
Preferably, the bottom of described reactor inner chamber 8 is also provided with the sleeve 3 making reaction mass carry out Inner eycle in described reactor inner chamber 8, and the bottom of described sleeve 3 is less than described sleeve diameter by internal diameter and the conduit stretching into described sleeve inner is communicated with the air inlet 11 of described reactor shell 1.In the utility model, by arranging described sleeve, and gas enters in described sleeve from air inlet, make the Gas content in the slurries in sleeve obviously high than the Gas content in the slurries outside sleeve, thus the slurries in promotion sleeve move upward, and the slurries outside sleeve move downward relatively, so in reactor inner chamber, form Inner eycle, facilitate reacting to each other between gas in slurries, solid, liquid three-phase, thus can reaction efficiency be improved.
In the utility model, require that the internal diameter guiding the internal diameter of the described conduit of gas to be less than described sleeve is to make the slurries in described reactor inner chamber can enter described sleeve from the bottom of described sleeve.Therefore, those skilled in the art can determine the ratio of the internal diameter of described conduit and described sleeve accordingly.
Preferably, described sleeve 3 is one or at least two, is provided with gas distributor 7 between the described conduit of described sleeve 3 bottom of at least two and described air inlet 11.The setting of described gas distributor is in order to the gas entered in described reactor inner chamber can be made to distribute more equably, gas is evenly distributed to each built-in sleeve bottom through gas distributor, hydrogen is dispersed into minute bubbles by gas distributor herein, bubble in each sleeve all moves up, and makes the Gas content in sleeve be greater than Gas content outside sleeve.By means of the difference of fluid density inside and outside sleeve, in certain vertical distance range, form pressure reduction, this pressure reduction promotes sleeve outer fluid and flows downward, and upwards flows, so form Inner eycle at sleeve inner fluid.Liquid phase flow rate in reactor inner chamber be greater than catalyst granules take speed out of time, liquid, solid two-phase are just together at reactor Inner eycle.
Preferably, the length of described sleeve 3 is 1/4 to 3/4 of the length of described reactor shell 1.
Preferably, the diameter of described sleeve 3 is 1/100 to 3/4 of the diameter of described reactor shell 1.At this place, described diameter is also internal diameter.
Preferably, described sleeve 3 is set to interlaced with the underflow pipe 6 of described cyclone hydraulic separators bottom.Described interlaced refer to described cyclone hydraulic separators bottom underflow pipe and described sleeve not on the same line, this setting is that the rich solid content component in order to avoid drawing from the underflow pipe of described cyclone hydraulic separators bottom directly enters in sleeve with flowing, thus disturbs the inside and outside Inner eycle formed of sleeve.
Preferably, the length of described underflow pipe 6 is 1/5 to 9/10 of the length of described sleeve 3.
Preferably, the length stretching into described sleeve inner of described conduit is 1/1000 to 1/10 of the length of described sleeve 3.
Preferably, the height of described spin liquid separator entrance 4 is higher than the overhead height of described sleeve 3, and both differences in height are 1/200 to 1/2 of the length of described reactor shell 1.More preferably, both differences in height are 1/20 to 1/4 of the length of described reactor shell 1.
Preferably, the height of described gaseous phase outlet 5 is higher than the height of described spin liquid separator entrance 4, and both differences in height are 1/50 to 1/4 of the length of described reactor shell 1.
In the utility model, described spin liquid separator entrance is preferably tubaeform, in reactor liquid level place or liquid level slightly below, thus the slurries in reactor inner chamber can be entered in described cyclone hydraulic separators by described spin liquid separator entrance.
On the top of described reactor inner chamber, gas phase is collected more than liquid level, and leads to outside described reactor from gas outlet.
Under preferable case, slurries containing gas, solid, liquid three-phase tangentially enter from spin liquid separator entrance, flow rate between 0.2-5m/s, preferably between 0.3-3.0m/s, in cyclone hydraulic separators, form rotary motion, rely on centrifugal force by gas, liquid, solid three phase separation.The slurries (rich solid phase components) carrying most of solid catalyst move downward, reenter in reactor inner chamber, the slurries (poor solid phase components) carrying a small amount of catalyst enter next stage cyclone hydraulic separators from the top of cyclone hydraulic separators, or flow out described reactor inner chamber from product oil outlet.The gaseous phase outlet of each cyclone hydraulic separators all communicates with the upper gaseous phase section of reactor inner chamber.
Preferably, in the utility model, catalyst enters reactor inner chamber from the agent mouth that adds on the top of reactor shell, flows out to outside described reactor inner chamber from unloading agent mouth.Regular job is added or discharged amount according to parameter determination catalyst such as conversion ratio, bed pressure reduction, coke yields.
Preferably, the particle size of the catalyst used in the utility model can coordinate design and the operation of cyclone hydraulic separators, and catalyst shape is prioritizing selection with spherical, also can be other shape.Catalyst size is between 0.05-1.5mm, preferably in the 0.1-1.0 mm, preferred between 0.1-0.8mm further.
According to the first preferred detailed description of the invention of the present utility model, paste state bed reactor described in the utility model has the structure shown in Fig. 1.Particularly, this reactor comprises:
Reactor shell 1, the bottom of this reactor shell is provided with unloads agent mouth 12, air inlet 11 and feedstock oil entrance 14, and the top of this reactor shell is provided with gas outlet 9, adds agent mouth 13 and product oil outlet 10;
The inner space of described reactor shell 1 forms reactor inner chamber 8, the top of this reactor inner chamber is provided with cyclone hydraulic separators 2, reaction mass in described reactor inner chamber enters described cyclone hydraulic separators 2 from spin liquid separator entrance 4 and is separated, separating obtained rich solid content component is back to described reactor inner chamber 8 from the underflow pipe 6 of described cyclone hydraulic separators 2 bottom, separating obtained poor solid content component leads to reactor from described product oil outlet 10, and separating obtained gas phase leads to described cyclone hydraulic separators 2 from gaseous phase outlet 5.The bottom of this reactor inner chamber 8 is also provided with the sleeve 3 making reaction mass carry out Inner eycle in described reactor inner chamber 8, and the bottom of described sleeve 3 is less than described sleeve diameter by internal diameter and the conduit stretching into described sleeve inner is communicated with the air inlet 11 of described reactor shell 1.Further, described sleeve 3 is 3, and described cyclone hydraulic separators 2 is set to two-stage, is provided with gas distributor 7 between the described conduit of 3 lower cartridge and described air inlet 11.
According to the first preferred detailed description of the invention above-mentioned, catalyst and feedstock oil respectively from described reactor shell 1 add agent mouth 13 and feedstock oil entrance 14 enters described reactor inner chamber 8, and hydrogen is successively by air inlet 11, gas distributor 7 and conduit are incorporated in 3 sleeves 3 in Fig. 1 respectively, be full of in sleeve containing gas, Gu, the slurries of liquid three-phase, the gas introduced makes slurries (reaction mass) Gas content in sleeve increase, thus move upward, and relatively, slurries outside sleeve move downward along described sleeve outer wall, formation Inner eycle like this, simultaneously, gas in reactor inner chamber 8, Gu, liquid three-phase slurries enter the cyclone hydraulic separators 2 of the first order from spin liquid separator entrance 4 and are separated, the gas phase of gained leads to outside described cyclone hydraulic separators 2 by gaseous phase outlet 5, separating obtained rich solid content component is back to described reactor inner chamber 8 from the underflow pipe 6 of described cyclone hydraulic separators 2 bottom, separating obtained poor solid content component is introduced in the second level and is separated, the gas phase of gained leads to outside described cyclone hydraulic separators 2 by gaseous phase outlet 5, separating obtained rich solid content component is back to described reactor inner chamber 8 from the underflow pipe 6 of cyclone hydraulic separators 2 bottom of the second level, separating obtained poor solid content component leads to reactor from described product oil outlet 10.The gas phase introduced from described gaseous phase outlet 5 is led to reactor by gas outlet 9.The catalyst reacted leads to reactor from unloading agent mouth 12.
According to the preferred detailed description of the invention of the second of the present utility model, paste state bed reactor described in the utility model comprises:
Reactor shell 1, the bottom of this reactor shell is provided with unloads agent mouth 12, air inlet 11 and feedstock oil entrance 14, and the top of this reactor shell is provided with gas outlet 9, adds agent mouth 13 and product oil outlet 10;
The inner space of described reactor shell 1 forms reactor inner chamber 8, the top of this reactor inner chamber is provided with cyclone hydraulic separators 2, reaction mass in described reactor inner chamber enters described cyclone hydraulic separators 2 from spin liquid separator entrance 4 and is separated, separating obtained rich solid content component is back to described reactor inner chamber 8 from the underflow pipe 6 of described cyclone hydraulic separators 2 bottom, separating obtained poor solid content component leads to reactor from described product oil outlet 10, and separating obtained gas phase leads to described cyclone hydraulic separators 2 from gaseous phase outlet 5.
According to the preferred detailed description of the invention of above-mentioned the second, catalyst and feedstock oil respectively from described reactor shell 1 add agent mouth 13 and feedstock oil entrance 14 enters described reactor inner chamber 8, and hydrogen is incorporated in described reactor inner chamber 8 by air inlet 11 and conduit successively, the gas introduced makes slurries (reaction mass) Gas content in reactor inner chamber increase, thus formation relative motion, simultaneously, gas in reactor inner chamber 8, Gu, liquid three-phase slurries enter cyclone hydraulic separators 2 from spin liquid separator entrance 4 and are separated, the gas phase of gained leads to outside described cyclone hydraulic separators 2 by gaseous phase outlet 5, separating obtained rich solid content component is back to described reactor inner chamber 8 from the underflow pipe 6 of described cyclone hydraulic separators 2 bottom, separating obtained poor solid content component leads to reactor from described product oil outlet 10.The gas phase introduced from described gaseous phase outlet 5 is led to reactor by gas outlet 9.The catalyst reacted leads to reactor from unloading agent mouth 12.
The utility model does not limit reaction condition when adopting it to react, the paste state bed reactor that the operating condition that those skilled in the art can adopt use paste state bed reactor conventional in this area to carry out reacting uses the utility model to provide.
Further describe the utility model by the following examples.
In the utility model, when not doing contrary explanation, the gas of use and the volumetric quantities of liquid are the numerical value of 25 DEG C and 1 normal atmosphere pressures.
In following examples, the mink cell focus of use is decompression residuum, and the character of this decompression residuum is as shown in table 1.
Table 1
Embodiment 1
The feedstock oil entrance of mink cell focus through reactor is imported in reactor, by hydrogen from air inlet in the sleeve that gas distributor imports reactor.Catalyst joins in reactor from adding agent mouth, and catalyst is Fe-Ni-Co-Mo-W complexing agent, and catalyst particle diameter after shaping is 0.6mm.
The present embodiment uses single sleeve.The internal diameter of sleeve is 1/2 of reactor shell internal diameter, and the length of sleeve is 5/8 of reactor cylinder body length.The conduit length extend in sleeve guiding hydrogen is 1/20 of the length of sleeve.
Gas carry slurries from sleeve to upper flowing, flow downward in reactor inner chamber after going out sleeve, circulate.
Reacted slurries enter in cyclone hydraulic separators through spin liquid separator entrance.A cyclone hydraulic separators is set in the present embodiment.The difference in height at the top of spin liquid separator entrance and sleeve is 1/10 of the length of sleeve.
After the slurries carrying catalyst are separated in cyclone hydraulic separators, the slurries that catalyst content is higher loop back in reactor inner chamber by underflow pipe, continue to participate in reaction.The slurries that catalyst content is lower are led to outside reactor by product oil outlet.A small amount of gas in cyclone hydraulic separators is entered in reactor inner chamber by the gaseous phase outlet of cyclone hydraulic separators.Gas in reactor goes out reactor by gas outlet.Collect the product oil obtained, calculate the conversion situation of mink cell focus.
The process conditions of the present embodiment are: operating temperature 450 DEG C, and in charging, the part by weight of fresh catalyst and heavy oil is 1:1000, and the volume ratio of hydrogen and heavy oil is 800:1, and air speed is 0.5h
-1.
Through actual measurement, the reactor bed temperature difference is less than 3 DEG C.
According to the method for the present embodiment, after stable operation, when the heavy oil gross weight dropped into is 100kg, the C1-C4 alkane obtained is 10.91kg, and gasoline is 16.91kg, and diesel oil is 25.53kg, and wax oil is 26.75kg, and tailings is 19.92kg.
Comparative example 1
Process according to the process conditions of embodiment 1, unlike, taken down by the cyclone hydraulic separators in reactor, other reaction condition is arranged consistent with embodiment 1 with reactor.
According to the method for this comparative example, after stable operation, when the heavy oil gross weight dropped into is 100kg, the C1-C4 alkane obtained is 9.80kg, and gasoline is 12.59kg, and diesel oil is 22.01kg, and wax oil is 27.62kg, and tailings is 27.98kg.
Visible according to the data of embodiment 1 and comparative example 1, when identical fresh catalyst adds, the heavier feeds in mink cell focus can transform by the utility model effectively, and can improve the yield of liquid hydrocarbon.
And the novel pulpous bed bioreactor that the utility model provides effectively can maintain the content of the catalyst in reactor, improving agent oil ratio, thus improve reaction efficiency.
And, the combination of the cyclone hydraulic separators that the utility model uses and sleeve, gas is entered in sleeve, rich solid content component in cyclone hydraulic separators enters reactor inner chamber downwards by underflow pipe, utilizes the flowing of the lift of gas in sleeve and the outer liquid of sleeve, and the density contrast inside and outside sleeve, form efficient device Inner eycle, improve liquid speed, avoid the sedimentation of catalyst, the transmission effect of heat and material also can improve.
More than describe preferred embodiment of the present utility model in detail; but; the utility model is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present utility model; can carry out multiple simple variant to the technical solution of the utility model, these simple variant all belong to protection domain of the present utility model.
It should be noted that in addition, each concrete technical characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode, in order to avoid unnecessary repetition, the utility model illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present utility model, as long as it is without prejudice to thought of the present utility model, it should be considered as content disclosed in the utility model equally.
Claims (11)
1. a paste state bed reactor, is characterized in that, this reactor comprises:
Reactor shell (1), the bottom of this reactor shell is provided with unloads agent mouth (12), air inlet (11) and feedstock oil entrance (14), and the top of this reactor shell is provided with gas outlet (9), adds agent mouth (13) and product oil outlet (10);
The inner space of described reactor shell (1) forms reactor inner chamber (8), the top of this reactor inner chamber is provided with cyclone hydraulic separators (2), reaction mass in described reactor inner chamber enters described cyclone hydraulic separators (2) from spin liquid separator entrance (4) and is separated, separating obtained rich solid content component is back to described reactor inner chamber (8) from the underflow pipe (6) of described cyclone hydraulic separators (2) bottom, separating obtained poor solid content component exports (10) from described product oil and leads to reactor, separating obtained gas phase leads to described cyclone hydraulic separators (2) from gaseous phase outlet (5).
2. reactor according to claim 1, it is characterized in that, described cyclone hydraulic separators (2) is one-level or at least two-stage, being separated the described poor solid content component obtained in the cyclone hydraulic separators (2) of the previous stage in the described cyclone hydraulic separators (2) of at least two-stage enters in adjacent rear stage cyclone hydraulic separators (2), being separated the described rich solid content component obtained is back to described reactor inner chamber (8) from underflow pipe (6), and the described poor solid content component that in afterbody cyclone hydraulic separators (2), separation obtains exports (10) extraction reactor from described product oil.
3. reactor according to claim 1 and 2, it is characterized in that, the bottom of described reactor inner chamber (8) is also provided with the sleeve (3) making reaction mass carry out Inner eycle in described reactor inner chamber (8), and the bottom of described sleeve (3) is less than described sleeve diameter by internal diameter and the air inlet (11) of the conduit and described reactor shell (1) that stretch into described sleeve inner is communicated with.
4. reactor according to claim 3, it is characterized in that, described sleeve (3) is one or at least two, is provided with gas distributor (7) between the described conduit of described sleeve (3) bottom of at least two and described air inlet (11).
5. reactor according to claim 3, is characterized in that, the length of described sleeve (3) is 1/4 to 3/4 of the length of described reactor shell (1).
6. reactor according to claim 3, is characterized in that, the diameter of described sleeve (3) is 1/100 to 3/4 of the diameter of described reactor shell (1).
7. reactor according to claim 3, is characterized in that, described sleeve (3) is set to interlaced with the underflow pipe (6) of described cyclone hydraulic separators bottom.
8. reactor according to claim 3, is characterized in that, the length of described underflow pipe (6) is 1/5 to 9/10 of the length of described sleeve (3).
9. reactor according to claim 3, is characterized in that, the length stretching into described sleeve inner of described conduit is 1/1000 to 1/10 of the length of described sleeve (3).
10. reactor according to claim 3, it is characterized in that, the height of described spin liquid separator entrance (4) is higher than the overhead height of described sleeve (3), and both differences in height are 1/200 to 1/2 of the length of described reactor shell (1).
11. reactors according to claim 1, it is characterized in that, the height of described gaseous phase outlet (5) is higher than the height of described spin liquid separator entrance (4), and both differences in height are 1/50 to 1/4 of the length of described reactor shell (1).
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| CN201520848831.4U CN205095762U (en) | 2015-10-29 | 2015-10-29 | Slurry bed reactor |
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| CN201520848831.4U CN205095762U (en) | 2015-10-29 | 2015-10-29 | Slurry bed reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107983270A (en) * | 2016-10-27 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of moving-burden bed reactor, solid acid alkylating reaction system and solid acid alkylating reaction method |
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2015
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107983270A (en) * | 2016-10-27 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of moving-burden bed reactor, solid acid alkylating reaction system and solid acid alkylating reaction method |
| CN107983270B (en) * | 2016-10-27 | 2021-01-08 | 中国石油化工股份有限公司 | Moving bed reactor, solid acid alkylation reaction system and solid acid alkylation reaction method |
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