CN103962068B - Paste state bed reactor - Google Patents
Paste state bed reactor Download PDFInfo
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- CN103962068B CN103962068B CN201310039719.1A CN201310039719A CN103962068B CN 103962068 B CN103962068 B CN 103962068B CN 201310039719 A CN201310039719 A CN 201310039719A CN 103962068 B CN103962068 B CN 103962068B
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Abstract
The invention provides a kind of paste state bed reactor, the reactor includes reactor shell (1) and bottom air intake assembly, reaction zone cylinder (6), sedimentation pipe (5) and upper outlet (14), the upper outlet（14）For exporting the gaseous matter in the chamber, the bottom air intake assembly is Venturi, the bottom of reaction zone cylinder described in the communication of the bottom air intake assembly, and the lower flow of the sedimentation pipe (5), which is communicated in the side of the bottom air intake assembly, the reactor enclosure body, allows slurries to sequentially pass through the reaction zone cylinder（6）, sedimentation pipe（5）, bottom air intake assembly, reaction zone cylinder（6）Form a circulation loop.In the described implementation, mixing and the mass-transfer efficiency in the reactor are promoted by the air intake assembly.
Description
Technical field
The invention belongs to chemical industry equipment device field, some embodiments of the application are specifically related to a kind of drum of interior circulation
Bubble three phase slurry bed reactor.
Background technology
Paste state bed reactor is being changed due to simple in construction, easily fabricated and amplification and the low advantage of Operation and Maintenance expense
As being widely used in terms of oxidizing process, F- T synthesis, biofermentation, wastewater treatment in work production.Various paste state bed reactors
Design in document and patent more to be had been reported that.Include riser, down-comer, gas as Chinese patent CN1137769C describes one kind
The slurry bed system synthetic reaction device of body distributor and agitator；Chinese patent CN1233451C describes a kind of gas of continuous operation
The solid three phase slurry bed industrial reactor of liquid；Chinese patent application CN1593740A describe it is a kind of by reducing inner sleeve, Anti-clogging spray nozzle,
The efficient reactor with paddle bed of the compositions such as quadratic distribution plate；Chinese patent CN100443155C describe a kind of separative efficiency it is high,
Slurry bed circulatory flow reactor simple in construction；Chinese patent CN100512941C then announces a kind of slurry bed system with gas interior circulation
Reaction unit；Chinese patent CN101396647B describes a kind of airwater mist cooling suspension bed for F- T synthesis and reacted
Device；Chinese patent CN201052457Y describes a kind of new interior circulation paste state bed reactor, using set of heat exchange tubes into lifting
Pipe, realizes the interior circulation of slurries；Chinese patent CN101417220B and CN101480595B are then respectively by laying multiple-layer horizontal
Grid type damping internal construction member and the tubulation beam with needle type fin, respectively describe a kind of paste state bed reactor of the improvement with tubulation；In
State patent application CN102188938A describes a kind of F- T synthesis slurry bed system of slurries interior circulation by setting one group of circulation cup
Reactor；Chinese patent CN102416307A, which is described, includes the internal-circulation type paste state bed reactor of multiple built-in cylinders；It is international
Application WO1994015160 describes a kind of interior circulation paste state bed reactor for strengthening gas-liquid separation.
Some paste state bed reactors of the prior art mainly using mechanical agitation, gas distributor and redistributor and
The down-comer of circulation flow reactor strengthens mixing and the interphase mass transfer of gas liquid solid.The gas distributor and circulation typically used is anti-
The down-comer in device is answered to be found limited to the effect for strengthening mixing and interphase mass transfer.Moreover, circulation flow reactor etc. utilizes density
It is relatively low that the inner loop mode that is formed of difference is found slurry velocity, so as to cause operating gas velocity too high, to avoid some
In the case of gas-liquid relative velocity is excessive causes unfavorable back-mixing.And mechanical agitation such as axle envelope problem due to being considered as inapplicable
In elevated pressures situation.
Because in some embodiments of paste state bed reactor, gas is dispersed in slurries in the form of bubbles, bubble with
Slurries are basic in uphill process to carry out gas-liquid mass transfer and chemical reaction simultaneously.Its interphase mass transfer efficiency is considered as to course of reaction
Play vital influence（Wang Yu etc., Chemical Reaction Engineering and technique, 23（6）, 499-504,2007）.Meanwhile, operating gas velocity
It is too low, it is recognized as directly limit the space-time yield of reactor.Therefore, how while back-mixing is reduced, slurry bed system is improved
In alternate mixing and dispersion effect, promote mass transport process, improve catalyst utilization, realize efficient reactor with paddle bed
It is crucial.Therefore need to research and develop a kind of paste state bed reactor that disclosure satisfy that the demand.
The present invention develops a kind of novel reactor, and it also belongs to use with the CN201052457Y reactors recorded
The circulation flow reactor of slurries interior circulation, and it is used as reaction zone and guide shell by the use of central cylinder.But the present invention is imitated by venturi
Answer and sedimentation pipe, enhance mixing and mass transport process, improve reaction efficiency.Meanwhile, made using Ground Settlement pipe and low pressure siphon
With promotion slurries interior circulation reduces back-mixing, improves the space-time yield of reactor.
In addition, the guide shell of the reactor described in CN201052457Y is made up of heat exchange coil, easily limited by heat exchange amount
System.The reaction zone cylinder and sedimentation pipe and heat-exchanging tube bundle of the present invention is separated, and increases the operability of reactor.
The content of the invention
The invention provides a kind of novel efficient reactor with paddle bed, some embodiments of the paste state bed reactor are led to
Improvement bottom air intake assembly, reinforcing mixing and mass transport process, or promotion course of reaction, or raising reactor efficiency are crossed, while gram
Take the above-mentioned unfavorable defect of prior art presence.
The first aspect of the invention provide a kind of paste state bed reactor, the reactor include reactor shell 1 with
And be arranged within the reactor shell 1 or on lower component：Bottom air intake assembly, reaction zone cylinder 6, sedimentation pipe 5
With upper outlet 14, it is same in the top of the reaction zone cylinder 6, the upper opening of the sedimentation pipe 5 to reactor enclosure body
Chamber and it is in flow communication, the upper outlet 14 is used to export gaseous matter in the chamber, it is characterised in that under described
Portion's air intake assembly is Venturi, the bottom of reaction zone cylinder described in the communication of the bottom air intake assembly, and
And the lower flow of the sedimentation pipe 5 is communicated to permission slurries in the side of the bottom air intake assembly, the reactor enclosure body
Sequentially pass through the reaction zone cylinder 6, sedimentation pipe 5, bottom air intake assembly, one circulation loop of formation of reaction zone cylinder 6.At this
In one embodiment of invention, the reactor also includes liquid-phase outlet 8, and the liquid-phase outlet 8 is used to export reactor enclosure
Liquid substance in chamber inside body.The bottom air intake assembly includes：The air inlet pipe 15 that is sequentially connected, contraction mouth 21, trunnion 16.
The bottom air intake assembly is connected and is in fluid communication with the sedimentation pipe 5 by the trunnion 16 or contraction mouth 21.
In an embodiment of the invention, the lower end of reaction zone cylinder 6 is provided with cylinder extension mouth 22 and imbibition
Cover 19, the fluid aspirator 19 carries downward extension mouth.Preferably, it is provided between the cylinder extension mouth 22 and fluid aspirator 19 mixed
Close pipe 20.Preferably, the lower end of reaction zone cylinder 6 is additionally provided with distributor 23.
One of the present invention preferred embodiment in, the upper end outlet of the trunnion 16 is located in reaction zone cylinder 6,
It is preferably located in mixing tube 20.
In yet another embodiment of the present invention, the reactor includes one or more sedimentation pipe 5, the sedimentation pipe
5 include：Sedimentation pipe extension mouth 24, tremie pipe 25 and pipette 18, the junction between the tremie pipe 25 and pipette 18 is
Involute shape.It is highly preferred that one or more described sedimentation pipe 5 is set along reactor axial direction around reactor axis
Put.In another preferred embodiment of the present invention, the reactor includes n roots sedimentation pipe 5, and n is 2 to 20 integer, often
The pipette 18 of root sedimentation pipe 5 is connected and is in fluid communication with the trunnion 16 of the air intake assembly, the diameter d of the pipette 18i
Less than trunnion 16 along the cross section perpendicular to the reactor longitudinal axis girth 1/n, the diameter d of preferably described pipette 18iIt is small
In trunnion 16 along the cross section perpendicular to the reactor longitudinal axis girth 1/2n.
In another preferred embodiment of the present invention, the reactor include n roots sedimentation pipe 5, n for 2 to 20 it is whole
Number, the pipette 18 of every sedimentation pipe 5 is connected and is in fluid communication with the trunnion 16 of the air intake assembly.
In another preferred embodiment of the present invention, the sedimentation pipe extension mouth 24 is eccentric funnel shape, thereon
The ratio for holding the diameter of feed liquid port 26 and the radius of reactor shell 1 is 0.1-1, most preferably more preferably 0.5-1,0.6-
1.In another preferred embodiment of the present invention, the lower end outlet 27 of the sedimentation pipe extension mouth 24 is higher than reaction zone cylinder
6 top.
In another preferred embodiment of the present invention, the diameter of the reaction zone cylinder 6 is straight with reactor shell 1
The ratio between footpath is 0.7~0.97, preferably 0.95, and the ratio between the height of reaction zone cylinder 6 and height of whole reactor shell 1 are
0.5~0.9, preferably 0.6.
In another preferred embodiment of the present invention, the reactor also includes heat-exchanging tube bundle 4, the heat-exchanging tube bundle
4 include one or more heat exchanger tube.Preferably, every heat exchanger tube therein is sleeve type structure, by outer tube 28 and inner tube 29
Composition.
In another preferred embodiment of the present invention, the reactor top is additionally provided with dividing plate 12 and one or many
Individual separator 11, the separator 11 is made up of separator 30, downcomer 31 and downcomer bottom plate 32, wherein being led under described
Inwall extension of the pipe 31 along the reactor shell 1, the inwall of the orientating reaction device housing 1 of downcomer bottom plate 32 laterally takes
To.
In another preferred embodiment of the present invention, the reactor also includes slurries, and the top of the sedimentation pipe 5
End is submerged under Starch Level 3.Preferably, in the reactor height of the Starch Level 3 of slurries and reactor shell 1 height
Ratio be 0.5~0.9, preferably 0.7.
The second aspect of the invention provides a kind of recirculation assembly for being used to improve serum recycle in paste state bed reactor,
Characterized in that, the recirculation assembly includes sedimentation pipe and air intake assembly, the air intake assembly includes the air inlet pipe being sequentially connected
15th, contraction mouth 21, trunnion 16, the air intake assembly and sedimentation fluid communication.
In an embodiment of the invention, the sedimentation pipe includes sedimentation pipe extension mouth 24, the blanking being sequentially connected
Pipe 25 and pipette 18.Preferably, the junction of the tremie pipe 25 and pipette 18 is involute shape.
In yet another embodiment of the present invention, the air intake assembly is inhaled with sedimentation pipe by the trunnion 16 with described
Liquid pipe 18 is connected and is in fluid communication.
In another preferred embodiment of the present invention, in addition to reaction zone cylinder 6, the lower end of reaction zone cylinder 6
Cylinder extension mouth 22, mixing tube 20 and fluid aspirator 19 are provided with, the fluid aspirator 19 carries downward extension mouth.
In another preferred embodiment of the present invention, the upper end outlet of the trunnion 16 is located in reaction zone cylinder 6,
It is preferably located in mixing tube 20.
The third aspect of the invention provides a kind of paste state bed reactor, and the reactor includes：
Reactor shell, and
Be arranged within the reactor shell or on lower component：Bottom air intake assembly, reaction zone cylinder, sedimentation
Pipe and upper outlet,
Wherein, the top of the reaction zone cylinder, the sedimentation pipe（5）Top respectively carry opening, described two openings
It is in fluid communication,
Wherein described bottom air intake assembly includes the air inlet pipe, contraction mouth and the trunnion that are sequentially connected, the trunnion with it is described
The lower flow connection of reaction zone cylinder, the bottom air intake assembly is located at the lower section of the reaction zone cylinder,
And the bottom of wherein described sedimentation pipe and the bottom air intake assembly are in the fluid near the trunnion or trunnion
Connection.
Brief description of the drawings
Fig. 1 shows the structure chart of a certain embodiment of paste state bed reactor of the present invention；
Fig. 2 shows the detailed structure view of a certain embodiment of the bottom air intake assembly of paste state bed reactor of the present invention；
Fig. 3 shows the structure chart of a certain embodiment of the sedimentation pipe of paste state bed reactor of the present invention；
Fig. 4 shows the structure chart of a certain embodiment of the sleeve-type heat exchanging pipe of paste state bed reactor of the present invention；
Fig. 5 shows the structure chart of a certain embodiment of the top separator of paste state bed reactor of the present invention.
The reference used in accompanying drawing and specification is as follows：
Reactor shell 1
Bottom air inlet 2
Starch Level 3
Heat-exchanging tube bundle 4
Sedimentation pipe 5
Reaction zone cylinder 6
Filter 7
Liquid-phase outlet 8
Heat exchange tube inlet 9
Heat exchanger tube outlet 10
Separator 11
Dividing plate 12
Demister 13
Top exit 14
Air inlet pipe 15
Trunnion 16
Down-comer 17
Pipette 18
Fluid aspirator 19
Mixing tube 20
Contraction mouth 21
Cylinder extension mouth 22
Distributor 23
Sedimentation pipe extension mouth 24
Tremie pipe 25
Upper end feed liquid port 26
Lower end outlet 27
Outer tube 28
Inner tube 29
Separator 30
Downcomer 31
Downcomer bottom plate 32
Embodiment
Numerical value " scope " disclosed herein is generally in the form of the lower and upper limit of numerical value.For the application certain number
Value, can be respectively one or more lower limits, and one or more upper limits.Given range is by selecting a lower limit and one
What the upper limit was defined.Selected lower and upper limit define the border of special scope.It is all to be defined by this way
Scope include and can be combined, i.e., any lower limit can combine to form a scope with any upper limit.For example, for specific
Parameter lists 60-120 and 80-110 scope, and the scope for being interpreted as 60-110,60-80,110-120 and 80-120 is also pre-
Expect.If in addition, the minimum zone value 1 and 2 listed, and if listing maximum magnitude value 3,4 and 5, then following model
Enclosing all to expect：1-2,1-3,1-4,1-5,2-3,2-4,2-5,3-4 and 4-5.In the present invention, if without special
Illustrate, all embodiments and preferred embodiment mentioned in this article can be mutually combined to form new technical scheme.
In the present invention, if without particularly illustrating, any technical characteristic and preferred feature mentioned in this article can
New technical scheme is formed to be mutually combined in a suitable form.
In the present invention, if without particularly illustrating, the order that any step mentioned in this article can be described is carried out
Or carried out with any other suitable order.For example, methods described includes step (a) and (b), it preferably includes methods described
It may include the step of order is carried out (a) and (b), the step of order is carried out (b) and (a) can also be included.For example, methods described is also
It may include step (c), represent that step (c) preferably can be added to methods described with random order, for example, methods described can include
Step (a), (b) and (c), may also comprise step (a), (c) and (b), can also include step (c), (a) and (b) etc..
Some preferred embodiments of the present invention are discussed below in conjunction with accompanying drawing, but those skilled in the art can
Understand, these embodiments can be carried out various etc. on the premise of the scope limited without departing substantially from claims of the present invention
Replacement, improvement and the combination of effect, are substituted by the above, improved and combined the new technical scheme obtained and be also included in this
Within the protection domain of invention.It should be noted that the device or equipment in accompanying drawing of the present invention are not to be painted according to actual ratio
System, specifically, the length-width ratio of some elongated members is changed, and the diameter of some elongated members, such as sedimentation pipe may
Amplified, in order to clearly observe.
Fig. 1 shows an embodiment of the paste state bed reactor of the present invention.The reactor include housing 1 with
And be arranged in the housing 1 with lower component：In accordance with the order from top to bottom, top exit 14, demister 13, dividing plate 12,
Separator 11, slurries, heat-exchanging tube bundle 4, sedimentation pipe 5, reaction zone cylinder 6 and bottom air intake assembly.
In the reactor shown in Fig. 1, the bottom air intake assembly is Venturi, as shown in Fig. 2 the bottom air inlet
Component is made up of air inlet pipe 15, contraction mouth 21, trunnion 16, fluid aspirator 19 and mixing tube 20.The Venturi is in air inlet pipe
There is larger diameter, the diameter is gradually reduced in contraction mouth 21, and the side of trunnion 16 is in fluid communication with pipette 18 at 15.
Wherein air inlet pipe 15 is extended to beyond reactor shell 1, is connected with outside feed gas source or pump, for importing in the reactor
Gas needed for the reaction of progress.These gases are after air inlet pipe 15 enters, gas flow rate when by contraction mouth 21
Increase, pressure reduction.The trunnion 16 is in fluid communication by the perforate on its side wall and the pipette 18 of the bottom of sedimentation pipe 5.By
There is the pressure differential between the gas and pipette 18 of the pressure reduction passed through from trunnion 16, will be settled by siphonage
Material in pipe 5 is sucked within trunnion 16 by the pipette 18, is delivered up together with the gas by trunnion 16.It is same with this
When, violent broken and immixture occurs under the conditions of high gas flow rate, between gas and slurry, forms gas-paste and mixes
Compound.The trunnion 16 is inserted within the fluid aspirator 19 and mixing tube 20, while also using identical principle by outside sedimentation pipe 5
Slurries bring into mixing tube 20, these slurries beyond sedimentation pipe 5 in mixing tube 20 with the gas from trunnion 16-
Slurry mix is mixed, and the mixture formed is delivered up, and by cylinder extension mouth 22, is uniformly divided by distributor 23
Cloth, subsequently into reaction zone cylinder 6.The reaction zone cylinder can have any appropriate shape and size, and not only limit
In the cylindrical shape shown in accompanying drawing of the present invention.The diameter of the reaction zone cylinder 6 is 0.7 with the diameter proportion of reactor shell 1
~0.97, preferably 0.71,0.73,0.75,0.78,0.80,0.81,0.82,0.83,0.84,0.85,0.86,0.87,
0.88th, 0.89,0.90,0.91,0.92,0.93,0.94,0.95,0.96,0.97, or above-mentioned any two numerical value group
Any number in the scope closed, Starch Level 3 lower section most volume position of such a larger diameter than causing slurry
Within reactor shell 6, for carrying out slurry reactor.The height of reaction zone cylinder 6 is the height of whole reactor shell 1
0.5~0.9, preferably 0.6,0.65,0.7,0.75,0.8,0.85, or above-mentioned any two combinations of values is formed
Scope in any number.
In the present invention, can be that common any in this area is appropriate for gas-solid-liquid equal for the distributor 23
The device of even distribution.In one preferred embodiment, the distributor 23 is to include the distribution grid of a large amount of through holes, this area
Technical staff can select the size and number of through hole in distribution grid according to specific reaction process and structure of reactor, and these lead to
Hole can be distributed in the form such as concentric circles, involute, petal-shaped, star, random pattern on distribution grid.
Can use n root sedimentation pipes in the reactor of the present invention, according to the difference of reactor size, n for 2 to 20 it is whole
Number, these directions of sedimentation pipe 5 along reactor axis are set around reactor center line.In the present invention, axis represents to pass through
The imaginary straight line that the center line of reactor extends vertically.The n roots sedimentation pipe can be around reactor center line with symmetrically
Form is set, and form heterogeneous can also be taken to set.Fig. 3 shows the detailed structure view of sedimentation pipe 5.As shown in figure 3, every
Root sedimentation pipe 5 is made up of sedimentation pipe extension mouth 24, tremie pipe 25 and pipette 18, the diameter d of the pipette 18iLess than trunnion
16 along the section girth perpendicular to reactor y direction 1/n, preferably smaller than trunnion 16 is along vertical perpendicular to reactor
The 1/2n of the section girth of direction of principal axis, the junction between the tremie pipe 25 and pipette 18 is involute shape.It is described
Sedimentation pipe extension mouth 24 be eccentric funnel shape, in other words, the upper end feed liquid port 26 of the sedimentation pipe extension mouth it is transversal
Face is a circle, and the cross section of its lower end outlet 27 is also a circle, in the vertical direction, the two circular centers of circle
It is not overlapping, but one segment distance of skew.The present invention one preferred embodiment in, the upper end feed liquid port 26
The ratio of diameter and the radius of reactor shell 1 is 0.1-1, more preferably more preferably 0.2-1, more preferably 0.3-1,0.4-
1, more preferably 0.5-1, most preferably 0.6-1.The structure of extension mouth 24, which is tried one's best, ensure that most slurries pass through sedimentation pipe
Carry out interior circulation.
Referring again to Fig. 1, the upper end level of the sedimentation pipe 5 is approached with the height of Starch Level 3 of the slurries, and is submerged in slurry
Under liquid level 3, the vertical drop between the upper end of the sedimentation pipe 5 and the Starch Level 3 of the slurries is preferably 0.1-2 meters,
More preferably 0.2-1.5 meters, more preferably 0.3-1.2 meters, more preferably 0.4-1 meters, more preferably 0.5-0.8 meters, most preferably
For 0.6-0.7 meters；And the height of the reaction zone cylinder 6 and the lower end of sedimentation pipe extension mouth 24 of sedimentation pipe 5 are exported residing for 27
Highly approach, and 27 height is exported less than lower end, it is vertical between the upper limb of the reaction zone cylinder 6 and lower end outlet 27
Straight difference in height is preferably 0.1-2 meters, more preferably 0.2-1.5 meters, more preferably 0.3-1.2 meters, more preferably 0.4-1 meters, more
Preferably 0.5-0.8 meters, most preferably 0.6-0.7 meters.Height and reactor shell 1 in the reactor residing for liquid level 3
The ratio of height be 0.5-0.9, more preferably more preferably 0.6-0.8,0.65-0.75, more preferably 0.7, with ensure reaction
Possess enough separated spaces in device top.Those skilled in the art can be according to concrete technology requirement to each part described above
Size, height and difference in height each other are configured.
In order to promote the heat exchange in reactor, multigroup heat-exchanging tube bundle 4 is also provided with wherein.Have according in reactor
The property of the reaction process neither endothermic nor exothermic of body, can be in heat-exchanging tube bundle by cooling fluid or heating fluid, so as to putting
Thermal response system is cooled down or supplies heat to endothermic reaction systems, to cause temperature of reaction system to be maintained at the model of restriction
Enclose.As shown in figure 4, every heat exchanger tube in the heat-exchanging tube bundle 4 is sleeve type structure, it is made up of outer tube 28 and inner tube 29.
In one embodiment, the heat exchanging fluid by heat exchange tube inlet 9 enter heat-exchanging tube bundle 4 in outer tube 28, in outer tube 28
It is interior to be exchanged heat with slurries, inner tube 29 is then flowed into, is flowed out by heat exchanger tube outlet 10.The heat exchanging fluid that the present invention is used can be
Any fluid well known by persons skilled in the art, such as air, nitrogen, inert gas, water, cooling oil, supercritical fluid etc.,
The supercritical fluid is preferably supercritical carbon dioxide.In an embodiment of the invention, carried out in the reactor
Reaction be exothermic reaction, the heat exchanging fluid is the water for eliminating oxygen and salt, and it is to prevent why to remove oxygen
Heat-exchanging tube bundle 4 is aoxidized, it is possible thereby to the effectively extension fixture life-span；Removing salt is to prevent fouling.The heat exchange stream
Gasification occurs after the heat of absorbing reaction system and produces vapor for body, and these vapor are exported by inner tube 29 from heat exchanger tube
10 outflows.
The top of Starch Level 3 is provided with separator 11, dividing plate 12 and demister 13.After being reacted in slurries,
The gas material stream for being mingled with a part of liquid and solid rises to separator 11.The separator 11 by separator 30,
Downcomer 31 and downcomer bottom plate 32 are constituted.The separator 30 can be it is known in the art it is any can be used for into promoting the circulation of qi,
Any separator of liquid, solid three phase separation, preferably cyclone hydraulic separators.Therefrom it is separated off after liquid and solid, gas thing
Matter rises through dividing plate 12 from the separator, then removes wherein remaining foam by demister 13, i.e., a small amount of residual liquid,
Then discharged from reactor head outlet 14.And liquid isolated in separator 30 and solid constituent are then along downcomer
31 flow downward, from downcomer bottom plate 32 returns to slurries.In a preferred embodiment of the present invention, the downcomer 31
Extend along the inwall of the reactor shell 1.In a preferred embodiment of the present invention, reactor of the invention includes
1-20, preferably 1-15, preferably 1-12, preferably 1-10, preferably 3-8, preferably 5-7 separator 11, these points
It is uniformly distributed from device 11 below dividing plate 12 around inwall, their downcomer 31 is all along in the reactor shell 1
Wall is extended downwardly.In a preferred embodiment of the present invention, the lower section of the insertion of outlet 32 Starch Level 3 of the downcomer 31.
The present invention another preferred embodiment in, the inwall of the orientating reaction device housing 1 of downcomer bottom plate 32 laterally takes
To.
In an embodiment of the invention, slurry reactor is carried out in such a way：Unstripped gas is by air inlet pipe 15
Into reactor, increase by gas flow rate when contraction mouth 21, pressure reduction, with forming pressure differential in reactor.When this
When the gas of a little pressure drop reductions is by throat 16, the siphonage formed using inside and outside differential pressure, by the slurry in sedimentation pipe 5
Liquid is sucked in trunnion 16 by pipette 18.
Strong broken and immixture occurs under the conditions of high gas flow rate, between gas and liquid.Gas and slurries
Mixture be delivered up with high speed from trunnion 16 by fluid aspirator 19, while also using identical principle by outside sedimentation pipe 5
Slurries are brought into mixing tube 20, these slurries beyond sedimentation pipe 5 in mixing tube 20 with gas-slurry from trunnion 16
Material mixture is mixed, and the stretched mouth 22 of the material after mixing and distribution grid 23 ascend into reaction zone cylinder 6.
The gas-paste mixed material, by reaction zone cylinder 6, reaches reactor top under bubbling state, is rising
During react, generation liquid or gaseous product.Wherein liquid product is by being arranged at reactor middle part of sliding channel
The filtering of filter 7 carries out separation of solid and liquid, is introduced by liquid-phase outlet 8.Gas-phase product, accessory substance or unreacted gas raw material rise
Depart from slurries, be separated off in separator 11 after the liquid and solid that are wherein mingled with, by demister 13, by exporting 14 rows
Go out.The slurries that separator is separated decline along downcomer 31 on reactor periphery, and Starch Level is returned to through downcomer bottom plate 32
Below.
As described above, the slurry carried secretly by gas of a part after separated device 11 is separated along under downcomer 31
Drop is returned in slurries.In addition, a part of slurry risen to along reaction zone cylinder above slurries upper surface can also be made in gravity
With decline.Because the downcomer 31 is all set on reactor periphery along reactor wall, and sedimentation pipe 5 is also all along anti-
The direction of device axis is answered, is set around reactor center line, and with the specially designed structure of extension mouth 24, therefore these decline
Largely stretched mouth 24 is collected within sedimentation pipe 5 slurries, enters tremie pipe 25 through lower end outlet 27.The institute of trunnion 16 in bottom
Under the siphonage of formation, and the promotion of the inside and outside density contrast of pipe, enter trunnion 16 through pipette 18, form the main interior of slurries
Circulation.A small amount of slurries outside reaction zone cylinder 6 and sedimentation pipe 5, the promotion of the serum density difference inside and outside reaction zone cylinder 6
Under, form slow secondary interior circulation.
Therefore, some embodiments of reactor of the invention compare traditional inner circulation reactor, to bottom air intake assembly
Improved, caused depression formation Venturi effect shunk using trunnion 16, gas-liquid mixed and mass transfer is not only enhanced,
And by siphonage, accelerate the slurry velocity in sedimentation pipe 5, promote serum recycle, to improve reactor efficiency, and reduce
Back-mixing.
Compared with prior art, the beneficial effects of the invention are as follows：
Inlet duct in some embodiments of the present invention enhances the mixing of unstripped gas and slurries using Venturi effect
And mass-transfer efficiency, promote the progress of reaction；The low pressure formed using unstripped gas porch, the siphonic effect of generation accelerates reaction
The dynamic speed of device entoplasm liquid recycle stream, reduces back-mixing, so as to improve reactor space-time yield, lowers capital cost of reactor；
The serum materials that the separator of reactor head is reclaimed not only avoid downcomer slurries to anti-along tube wall blanking
Answer the interference of device interior circulation；Moreover, the discharging opening of the horizontal orientation of particular design avoids rising gas in some embodiments
Lift effect of the body to slurries in tremie pipe.So as to improve top separating effect, it is allowed to higher reactor operating gas velocity, enter
And improve the space availability ratio and space-time yield of reactor.
Improved by above structure, reactor entoplasm liquid recycle stream moves the increase of speed, improves heat transfer efficiency, it is to avoid
Limitation of the exchange capability of heat to production capacity.
Embodiment
With reference to example, the present invention will be further described.In the examples below, with mainly comprising hydrogen and an oxygen
The synthesis gas for changing carbon gas is raw material, synthetic hydrocarbon oil and dimethyl ether (DME) product.It should be noted however that the present invention's is anti-
Device is answered to can be used for carrying out other slurry reactors.
Embodiment 1：
In the present embodiment 1, the use of the mixed gas of hydrogen and carbon monoxide is raw material, is synthesized in paste state bed reactor
Hydrocarbon ils, wherein synthetic hydrocarbon oil are filtered to remove after solid by filter 7 and exported from liquid product as the product of liquid form
8 draw.Specifically, the present embodiment uses paste state bed reactor as shown in Figure 1, and the paste state bed reactor housing inner diameter is 1
Rice, reactor longitudinal direction height is 25 meters, and liquid level is 18 meters in reactor.Reaction zone cylinder is set along reactor axis,
Its internal diameter is 0.92 meter, is highly 15 meters.6 sedimentation pipes are uniformly arranged around reactor axis, internal diameter is 0.028 meter.It is heavy
A diameter of 0.3 meter of the upper end feed liquid port of pipe upper end extension mouth 24, the slurries of the upper end feed liquid port 26 and the slurries drop
Vertical drop between face 3 is 0.6 meter.0.25 meter of throat pipe diameter, 0.02 meter of imbibition pipe diameter.
Reactor pressure is maintained at 2MPa, using the water for removing oxygen and salinity as condensing agent, is passed to heat exchange
Tube bank, so that the temperature of reaction system is maintained at into 220 DEG C.
The gas raw material used is H2The synthesis gas of/CO volume ratio=2 is as reaction raw materials, and synthesis gas is by reactor bottom
Air inlet enters, and superficial gas velocity is 0.371 meter per second.The slurries included in reactor are that cobalt-base catalyst is suspended in atoleine
The solid-weight content formed in solvent is 15% slurries, and the percentage is counted on the basis of the gross weight of slurries, the cobalt-based
Catalyst is the Co/ZrO that the granularity provided by Shanghai Institute for Advanced Study of the Chinese Academy of Sciences is 50 microns2/SiO2Catalyst, is used as solvent
Atoleine for carbon number be about 18~30 hydrocarbon mixture.Details on catalyst pulp can be found in Chang Jie
Deng catalysis journal, 26（10）, 859-868,2005.
CO in the tail gas stream that the GC-14C types gas Chromatographic Determination produced using Shimadzu Corporation is drawn from top exit 14
Content, compared with the CO moles that bottom inlet is fed, it is 59.9% that calculating, which obtains CO conversion ratios, thus with reference to material gas quantity
And reactor volume calculates and obtains the space-time yield of reactor for 68.02 kgs/hr/meter3.In addition, applicant also uses
Reactor described in CN201052457Y, has carried out contrast experiment under identical process conditions, as a result the gas of the reactor
The CO conversion ratios of outlet are 51.53%, and the space-time yield of reactor is 58.51 kgs/hr/meter3.As can be seen here, with this area
Existing reactor is compared, paste state bed reactor of the invention, can be by CO conversion ratios due to strengthening mixing and mass-transfer efficiency
For and reactor space-time yield improve about 16.3% or so.
Embodiment 2：
In the present embodiment 2, the use of the mixed gas of hydrogen and carbon monoxide is raw material, is synthesized in paste state bed reactor
Dimethyl ether.The reactor of reactor design and implementation example 1 is essentially identical, differs only in, because product DME is gaseous form,
Drawn together with tail gas from top exit, therefore, the reactor of embodiment 2 does not need filter 7 and liquid-phase outlet 8.
Pressure in reactor is 4MPa, using the water for removing oxygen and salinity as condensing agent, is passed to heat exchanger tube
Beam, so that the temperature of reaction system is maintained at into 270 DEG C.The unstrpped gas used is H2/ CO volume ratio is 1:1 synthesis
Gas.Catalyst is the bifunctional catalyst that commercial synthesis catalyst for methanol C301 and alumina dehydration catalyst are constituted, and these are urged
Agent is suspended in solvent liquid paraffin liquid, forms the slurries that solid-weight content is 15%, the percentage is with the gross weight of slurries
Counted on the basis of amount, the boiling point of the solvent liquid paraffin is higher than 340 DEG C, and mean molecule quantity is 345, on the catalyst slurry
It is described in detail referring to Guo Junwang etc., chemistry of fuel journal, 26（4）321-325,1998.
Synthesis gas is entered by reactor bottom air inlet, and superficial gas velocity is 0.136m/s.Use Shimadzu Corporation's GC-14C types
CO contents in the tail gas stream that gas Chromatographic Determination is drawn from top exit 14, compared with the CO moles that bottom inlet is fed
Compared with it is 33.64% that calculating, which obtains CO conversion ratios, and the space-time for obtaining reactor is thus calculated with reference to material gas quantity and reactor volume
Yield is 44.07 kgs/hr/meter3.Other applicant also using the reactor described in CN201052457Y under the same conditions
Carry out identical reaction process operation, measure gas vent CO conversion ratios be 31.2%, space-time yield be 40.87 kilograms/it is small
When/rice3.Therefore, compared with the existing reactor of prior art, paste state bed reactor of the invention by CO conversion ratios can be and
The space-time yield of reactor improves about 8% or so.
Claims (24)
1. a kind of paste state bed reactor, the reactor includes reactor shell (1) and is arranged on the reactor shell (1)
Within or on lower component：Bottom air intake assembly, reaction zone cylinder (6), sedimentation pipe (5) and upper outlet (14), it is described
Reaction zone cylinder（6）Top, the sedimentation pipe（5）Upper opening to reactor enclosure body in same chamber and with its fluid
Connection, the upper outlet（14）For exporting the gaseous matter in the chamber, it is characterised in that the bottom air intake assembly is
Venturi, the bottom of reaction zone cylinder described in the communication of the bottom air intake assembly, and the sedimentation pipe
(5) lower flow, which is communicated in the side of the bottom air intake assembly, the reactor enclosure body, allows slurries to sequentially pass through institute
State reaction zone cylinder（6）, sedimentation pipe（5）, bottom air intake assembly, reaction zone cylinder（6）Form a circulation loop；The reaction
The diameter of area's cylinder (6) and the diameter ratio of reactor shell (1) are 0.7~0.97, the height of reaction zone cylinder (6) with it is whole
The ratio between height of reactor shell (1) is 0.5~0.9；
The reactor includes one or more sedimentation pipe (5), and the sedimentation pipe (5) includes：Sedimentation pipe extension mouth (24), blanking
(25) and pipette (18) are managed, the junction between the tremie pipe (25) and pipette (18) is involute shape；It is described heavy
The lower end outlet (27) for dropping enlargement of pipe mouthful (24) is higher than the top of reaction zone cylinder (6).
2. paste state bed reactor as claimed in claim 1, it is characterised in that the reactor also includes liquid-phase outlet（8）, institute
State liquid-phase outlet（8）For exporting the liquid substance in reactor enclosure chamber inside body.
3. paste state bed reactor as claimed in claim 1, it is characterised in that the bottom air intake assembly includes：It is sequentially connected
Air inlet pipe (15), contraction mouth (21), trunnion (16).
4. paste state bed reactor as claimed in claim 3, it is characterised in that the bottom air intake assembly passes through the trunnion
Or contraction mouth (21) is connected and is in fluid communication with the sedimentation pipe (5) (16).
5. paste state bed reactor as claimed in claim 3, it is characterised in that reaction zone cylinder (6) lower end is provided with cylinder
Body extension mouth (22) and fluid aspirator (19), the fluid aspirator (19) carry downward extension mouth.
6. paste state bed reactor as claimed in claim 5, it is characterised in that the cylinder extension mouth (22) and fluid aspirator (19)
Between be provided with mixing tube (20).
7. paste state bed reactor as claimed in claim 6, it is characterised in that the upper end outlet of the trunnion (16) is located at reaction
In area's cylinder (6).
8. paste state bed reactor as claimed in claim 6, it is characterised in that the upper end outlet of the trunnion (16) is located at mixing
Manage in (20).
9. paste state bed reactor as claimed in claim 5, it is characterised in that reaction zone cylinder (6) lower end is additionally provided with
Distributor（23）.
10. paste state bed reactor as claimed in claim 1, it is characterised in that one or more described sedimentation pipe (5) is along anti-
Device axial direction is answered to be set around reactor axis.
11. paste state bed reactor as claimed in claim 10, it is characterised in that the reactor includes n roots sedimentation pipe (5), n
For 2 to 20 integer, the pipette (18) of every sedimentation pipe (5) and the trunnion of the air intake assembly（16）Connect and fluid connects
It is logical, the diameter d of the pipette (18)iThe 1/n of girth less than trunnion (16) along the cross section perpendicular to the reactor longitudinal axis.
12. paste state bed reactor as claimed in claim 10, it is characterised in that the reactor includes n roots sedimentation pipe (5), n
For 2 to 20 integer, the pipette (18) of every sedimentation pipe (5) and the trunnion of the air intake assembly（16）Connect and fluid connects
It is logical, the diameter d of the pipette (18)i1/ of girth less than trunnion (16) along the cross section perpendicular to the reactor longitudinal axis
2n。
13. paste state bed reactor as claimed in claim 10, it is characterised in that the reactor includes n roots sedimentation pipe (5), n
For 2 to 20 integer, the pipette (18) of every sedimentation pipe (5) and the trunnion of the air intake assembly（16）Connect and fluid connects
It is logical.
14. paste state bed reactor as claimed in claim 1, it is characterised in that the sedimentation pipe extension mouth (24) is leaked to be eccentric
The ratio of bucket shape shape, the diameter of its upper end feed liquid port (26) and the radius of reactor shell (1) is 0.1-1.
15. paste state bed reactor as claimed in claim 1, it is characterised in that the sedimentation pipe extension mouth (24) is leaked to be eccentric
The ratio of bucket shape shape, the diameter of its upper end feed liquid port (26) and the radius of reactor shell (1) is 0.5-1.
16. paste state bed reactor as claimed in claim 1, it is characterised in that the sedimentation pipe extension mouth (24) is leaked to be eccentric
The ratio of bucket shape shape, the diameter of its upper end feed liquid port (26) and the radius of reactor shell (1) is 0.6-1.
17. paste state bed reactor as claimed in claim 1, it is characterised in that the diameter of the reaction zone cylinder (6) and reaction
The diameter ratio of device housing (1) is 0.95, and the ratio between the height of reaction zone cylinder (6) and height of whole reactor shell (1) are
0.6。
18. paste state bed reactor as claimed in claim 1, it is characterised in that the reactor also includes heat-exchanging tube bundle (4),
The heat-exchanging tube bundle (4) includes one or more heat exchanger tube.
19. paste state bed reactor as claimed in claim 18, it is characterised in that every heat exchanger tube therein is bushing type knot
Structure, is made up of outer tube (28) and inner tube (29).
20. the paste state bed reactor as described in claim 1 or 19, it is characterised in that the reactor top be additionally provided with every
Plate (12) and one or more separators (11), the separator (11) by separator (30), downcomer (31) and under lead
Pipe outlet (32) composition, wherein inwall extension of the downcomer (31) along the reactor shell (1), the downcomer goes out
The inwall horizontal orientation of mouth (32) orientating reaction device housing (1).
21. the paste state bed reactor as described in claim any one of 1-19, it is characterised in that the reactor also includes slurry
Liquid, and the top of the sedimentation pipe (5) is submerged under Starch Level (3).
22. paste state bed reactor as claimed in claim 20, it is characterised in that the reactor also includes slurries, and described
The top of sedimentation pipe (5) is submerged under Starch Level (3).
23. paste state bed reactor as claimed in claim 21, it is characterised in that the Starch Level (3) of slurries in the reactor
Height and reactor shell (1) height ratio be 0.5~0.9.
24. paste state bed reactor as claimed in claim 21, it is characterised in that the Starch Level (3) of slurries in the reactor
Height and reactor shell (1) height ratio be 0.7.
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| CN201310039719.1A CN103962068B (en) | 2013-01-31 | 2013-01-31 | Paste state bed reactor |
| PCT/CN2014/071622 WO2014117723A1 (en) | 2013-01-31 | 2014-01-28 | Slurry-bed reactor and method of use thereof |
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| CN201310039719.1A CN103962068B (en) | 2013-01-31 | 2013-01-31 | Paste state bed reactor |
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| CN105056845B (en) * | 2015-08-28 | 2017-11-10 | 湖南百利工程科技股份有限公司 | Paste state bed reactor and its application in hydrogen peroxide is produced |
| CN107790073A (en) * | 2017-09-28 | 2018-03-13 | 北京中科诚毅科技发展有限公司 | A kind of reactor novel internal structure and its design method and purposes |
| CN109647289A (en) * | 2019-01-16 | 2019-04-19 | 华陆工程科技有限责任公司 | A kind of iris type vinyl ethers product reactor |
| CN109847659A (en) * | 2019-01-16 | 2019-06-07 | 华陆工程科技有限责任公司 | A kind of guide cylinder type vinyl ethers product reactor |
| WO2022040844A1 (en) * | 2020-08-24 | 2022-03-03 | 中国科学院青岛生物能源与过程研究所 | Method and apparatus for extracting clean liquid from slurry reactor |
| CN114736319B (en) * | 2021-01-07 | 2023-12-26 | 中昊晨光化工研究院有限公司 | Apparatus system and method for purifying polymer from polymeric emulsion |
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| CN101717656A (en) * | 2008-10-09 | 2010-06-02 | 中科合成油技术有限公司 | Grading liquefaction method for solid fuel containing carbon and three-phase suspension bed reactor for same |
| CN102188938A (en) * | 2010-03-17 | 2011-09-21 | 中国石油化工集团公司 | FischerTropsch synthesis slurry bed reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101717656A (en) * | 2008-10-09 | 2010-06-02 | 中科合成油技术有限公司 | Grading liquefaction method for solid fuel containing carbon and three-phase suspension bed reactor for same |
| CN102188938A (en) * | 2010-03-17 | 2011-09-21 | 中国石油化工集团公司 | FischerTropsch synthesis slurry bed reactor |
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