CN103977747A - State slurry bed reactor, and method using slurry bed reactor for slurry bed reaction - Google Patents
State slurry bed reactor, and method using slurry bed reactor for slurry bed reaction Download PDFInfo
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- CN103977747A CN103977747A CN201310050846.1A CN201310050846A CN103977747A CN 103977747 A CN103977747 A CN 103977747A CN 201310050846 A CN201310050846 A CN 201310050846A CN 103977747 A CN103977747 A CN 103977747A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
- B01J8/224—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement
- B01J8/226—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid the particles being subject to a circulatory movement internally, i.e. the particles rotate within the vessel
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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
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
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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
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
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- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a slurry bed reactor which includes a reactor cylinder body (1), a plurality of drop tubes (28), a plurality of injectors (13) and a gas distributor (27) which are arranged in the reactor cylinder body, and a middle outer circulation device and / or a top outer circulation device; the middle outer circulation device is used for leading out at least a portion of a slurry material in the reactor cylinder body and outer circulation of at least a portion of the slurry material back to the reactor cylinder body, the top outer circulation device is used for leading out at least a portion of a gas material in the reactor cylinder body and outer circulation of at least a portion of a liquid material separated from the gas material back to the reactor cylinder body, wherein the plurality of drop tubes are arranged along the inner wall of the reactor cylinder body (1), the injectors (13) are arranged at different vertical heights in the central area of the reactor cylinder body (1), and the opening direction of the injectors (13) is diagonally upward or rightly upward. By use of the slurry bed reactor, particle suspension, liquid-solid mixing, heat transfer and mass transfer in the slurry bed reactor can be strengthened by outer circulation of slurry. The invention also provides a method for using the slurry bed reactor for slurry bed reaction.
Description
Technical field
The present invention relates to chemical field, relate in particular to for carry out the novel paste state bed reactor of the suspension of enhanced reactor endoparticle, liquid-solid mixing and heat and mass by material outside circulation, the present invention is also specifically related to use this paste state bed reactor to carry out the method for slurry reactor.
Background technology
Along with the minimizing day by day of petroleum resources in world wide, the exploitation of alternative energy source technology comes into one's own gradually.The raw material that contains carbon, hydrogen resource by coal, natural gas, living beings etc. is produced synthesis gas, again by PROCESS FOR TREATMENT synthesis gas such as Water gas shift/WGS and purifications, take this synthesis gas produces hydro carbons as raw material passes through Fischer-Tropsch synthetic technology, by-product oxygenatedchemicals, then adopts ripe Petroleum Processing Technology can produce the products such as fuel with high cleanness and high-quality wax simultaneously.The core of this technology path is Fischer-Tropsch synthetic technology.
Take coal or natural gas comprises two classes through the synthetic catalyst of producing liquid fuel of Fischer-Tropsch as raw material, and a class is ferrum-based catalyst, and another kind of is cobalt-base catalyst.Ferrum-based catalyst less stable, just need to carry out more changing jobs of a catalyst in 70 ~ 100 days, and more catalyst changeout causes the development of this technology to be restricted continually.And cobalt-base catalyst good stability can be avoided frequently more catalyst changeout, so cobalt-base catalyst can be applicable to the synthetic fixed bed reactors of Fischer-Tropsch.But Fischer-Tropsch synthesis is the reaction that a kind of thermal discharge is very large, and fixed bed reactors easily produce focus and coking problem, this makes the amplification ratio of fixed bed Fischer-Tropsch synthesis device more difficult.After this, Fischer-Tropsch synthesis device develops into again recirculating fluidized bed, fixed fluidized bed and slurry state bed.The fluid mapper process of recirculating fluidized bed is difficult to control, the low serious wear of catalyst utilization, and also production capacity is still on the low side.Fixed fluidized bed simple in structure, solved the low and wear problem of catalyst utilization, but it is synthetic to be only applicable to high temperature fischer-tropsch, be not suitable for the heavy ends such as the clean diesel of production high added value and wax.
With traditional gas-solid fluidized bed comparing, the bubbling paste state bed reactor technology that comprises gas-liquid-solid three-phase has advantage in the following areas: (1) reaction heat can effectively shift out, adopt high activated catalyst (being high yield catalyst) still can effectively control reaction temperature, scaling-up is relatively easy like this, is conducive to realize uniserial large industrialized and produces; (2) the approximate isothermal operation of reactor, by selecting suitable catalyst and reaction temperature, the liquid hydrocarbon product such as clean diesel that can main product high added value and heavy wax; (3) running environment of catalyst is improved, and the wearing and tearing of catalyst can decrease.By replacing regularly catalyst, the average catalyst life-span is easy to control.Therefore, paste state bed reactor technology becomes synthetic production of Fischer-Tropsch and take the dominant technology that diesel oil and wax is major product.Except Fischer-Tropsch synthesis technique, paste state bed reactor also has very wide application prospect in other comprises the reaction process of gas-liquid-solid three-phase.
Slurry reactor relates to mass transfer, heat transfer and the reaction between gas-liquid-solid three-phase, the basis that on its micro-scale, the even suspension of particle and liquid-solid even mixing are W-responses.Otherwise paste state bed reactor will produce the react hot issue similar with fixed bed reactors because of particle agglomeration, thereby affect the operation heat endurance of reactor monolith.Given this, the design of paste state bed reactor need meet following 2 basic demands: (1) is in order to keep starching state bed characteristic, catalyst need be prepared into the fine particle with sufficient mechanical strength through specific moulding process, is evenly suspended in liquid slurry guaranteeing.(2) reactor diameter choose need meet unstrpped gas with certain empty tower gas velocity bubbling by slurry state bed bed.Unstrpped gas is crossed young pathbreaker by the gas speed of slurry state bed bed and is caused catalyst granules deposition and reunite, and gas speed is too high will cause serious tail gas mist and particle entrainment.
But than liquid medium, the density of gas medium is limited, the empty tower gas velocity of bubbling slurry state bed also only limits to limited scope, and the kinetic energy that the bubble of so certain gas speed provides is to the suspension of particle and strengthen mass transfer, heat transfer effect is also limited.For the design of slurry bed ft synthetic reactor, how to design that the turbulent flow of strengthening and suitable inner member strengthen that particle in whole reactor suspends, mass transfer, heat transfer and reaction between liquid-solid even mixing and three-phase be still one of its core technology.
Therefore, those skilled in the art still wish to develop a kind of paste state bed reactor, and it has better particle suspension and liquid-solid mixed effect.
Summary of the invention
In order to overcome the above problems, the invention provides a kind of paste state bed reactor and using method thereof with better particle suspension and liquid-solid mixed effect.
Specifically, of the present invention aspect first, a kind of paste state bed reactor is provided, described paste state bed reactor comprises: reactor shell, be arranged on a plurality of down-comers within described reactor shell, a plurality of injectors and gas distributor, middle part external circulating device and/or top external circulating device, described middle part external circulating device is used at least a portion slurry state material in reactor shell to draw and at least a portion outer circulation is returned in reactor shell, described top external circulating device is used at least a portion gaseous state material in reactor shell to draw and at least a portion outer circulation is returned in reactor shell, wherein, described a plurality of down-comer is along the inwall setting of described reactor shell, described injector is arranged on different vertical heights in described cylindrical shell central authorities, the opening direction of described injector towards directly over or oblique upper.
In an embodiment of the invention, described gas distributor and the difference in height approaching most between the injector of this gas distributor are at least 1% of reactor cylinder height, are preferably at least 2.5% of reactor cylinder height.In an embodiment of the invention, described gas distributor and the difference in height approaching most between the injector of this gas distributor are no more than 20% of reactor cylinder height, are preferably and are no more than 10% of reactor cylinder height.
In an embodiment of the invention, approach the injector of described gas distributor most and away from the difference in height between the injector of described gas distributor, be at least 40% of reactor cylinder height, being preferably at least 50% of reactor cylinder height.In an embodiment of the invention, approach the injector of described gas distributor most and away from the difference in height between the injector of described gas distributor, be no more than 90% of reactor cylinder height, being preferably and being no more than 80% of reactor cylinder height.
In an embodiment of the invention, approach most the injector of described gas distributor and between the injector away from described gas distributor, have an injector at least, between described injector in vertical direction with even or inhomogeneous vertical separation setting.
In an embodiment of the invention, described middle part external circulating device comprises liquid-solid separator and circulating pump in reactor shell, preferably also can comprise and be positioned at the external gas-liquid separator of described reactor cylinder; Described top external circulating device comprises and is positioned at the external condenser of reactor cylinder of the present invention, gas-liquid separator and circulating pump.
In an embodiment of the invention, described paste state bed reactor comprises that 2-10 group is arranged on the down-comer of different vertical height, and every group of down-comer extend in identical vertical height, in the mode of horizontal alignment, along reactor shell inwall, arrange; Belong to not corresponding down-comer vertically alignment separately on the same group.
Another aspect of the present invention provides a kind of method that is used for carrying out slurry reactor, described method is used paste state bed reactor of the present invention, said method comprising the steps of: i) gas reaction material is delivered to gas distributor, in space through the gas after gas distributor in reactor shell, beyond down-comer, rises and drives and starch state material and rise thereupon, and react under the effect of starching state material inner catalyst; Ii) the gaseous state material clamp after reaction rises to the top of reactor shell with some slurries, use top external circulating device that the gaseous state material after described reaction is drawn, gas in gaseous state material after described reaction is separated with the slurries of carrying secretly, then within the liquid substance outer circulation in the isolated slurries of at least a portion being returned to reactor shell, preferably send back to through described injector, described injector towards top or oblique upper spray; Iii) alternatively, use middle part external circulating device that at least a portion slurry state material in reactor shell is drawn, liquid substance in described slurry state material is separated with solid matter, and within the isolated liquid substance outer circulation of at least a portion is returned to reactor shell, preferably send back to through described injector, described injector towards top or oblique upper spray; Iv) a part of described slurry state material flows in described down-comer from described down-comer top end opening, in down-comer, flow downward, and flow out from down-comer bottom, then under the drive of gas reaction material, in the space in reactor shell, outside down-comer, rise, and repeat above-mentioned step I) ~ iv).
Another aspect of the present invention, also put forward a kind of method that is used for carrying out slurry reactor, described method is used the paste state bed reactor with the reactor shell of slurries, said method comprising the steps of: i) to the gas distributor conveying gas precursor reactant material in described reactor shell to drive described slurries to rise, and described gas reaction material reacts in slurries; Ii) from reactor shell upper area, the reacted gaseous state material of at least a portion is drawn to reactor shell, gas in described reacted gaseous state material is separated with the slurries of carrying secretly, within the isolated liquid substance outer circulation of at least a portion is returned to reactor shell, preferably by injector, send back to, described injector towards top or oblique upper spray; Iii) alternatively, at least a portion is starched to state material to be led to outside reactor shell from reactor shell, liquid substance in described slurry state material is separated with solid matter, and then within the isolated liquid substance outer circulation of at least a portion is returned to reactor shell, preferably by injector, send back to, described injector towards top or oblique upper spray; Iv) the described slurry state of part material is flowed into from described down-comer upper opening, and flow out from described down-comer bottom opening, enter lower region in reactor shell.
In an embodiment of the invention, in above-mentioned method of carrying out slurry reactor, draw reacted gaseous state material from reactor shell before, described reacted gaseous state material first carries out initial gross separation in reactor shell, makes the slurries wherein carried secretly separated with gaseous matter.
By design of the present invention, the effect that gas distributor in reactor shell makes progress makes to contain reacting gas and liquid state-solid matter rises thereupon, in uphill process, react and form and starch state material, slurry state material is near gas-liquid interface, gaseous matter self continues to rise, enter the region at reactor shell top, after gaseous matter departs from, the density of slurries increases, then from described down-comer top end opening, enter in described down-comer, under self gravitation effect, flow downward, after down-comer bottom opening flows out again under the drive of gas reaction material in reactor shell, in space outside down-comer, rise, thereby form an inner reaction cycle.Simultaneously, middle part external circulating device and/or top external circulating device at least a portion can be starched to state material again and/or gaseous state material is drawn reactor shell, above-mentioned slurry state material and/or gaseous state material are carried out to solution-air, gas-solid, liquid-solid and/or gas-liquid-solid separation, separating obtained available liquid substance is got back in reactor shell by injector outer circulation, and separating obtained available gaseous matter is sent back in reactor shell by gas distributor.The recyclegas that loops back continues to participate in reaction, and the circulating fluid looping back (for example light hydrocarbons of carbon containing 5-carbon 10) continues to get back in reactor shell slurries are played to stirring, suspension effect.By above-mentioned set-up mode, the particle suspension in described paste state bed reactor, liquid-solid mixing and heat transfer and mass transfer have been strengthened.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in more detail:
Fig. 1 is the schematic diagram of the paste state bed reactor of one embodiment of the present invention, within wherein all down-comers are arranged on one deck.
Fig. 2 is the sectional view that shows down-comer 28 set-up modes in Fig. 1.
Fig. 3 is the schematic diagram of the paste state bed reactor of one embodiment of the present invention, comprising three layers of down-comer.
Fig. 4 is the schematic diagram of the injector of Venturi tube structure.
Fig. 5 A and 5B are the schematic diagrames that exit face has the tube-shaped sputtering device of a plurality of small pore-like openings.
Fig. 6 A is a kind of preferred injection situation schematic diagram of tube-shaped sputtering device of the present invention.
Fig. 6 B is that the another kind of tube-shaped sputtering device of the present invention preferably sprays situation schematic diagram.
Fig. 7 is reactor cylinder height L of the present invention and gas-liquid interface height H schematic diagram.
Description of reference numerals
1. reactor shell 2. gas-liquid interface 3. gas-liquid separation spaces
4. condenser 5. gas-liquid separator 6. certain liquid-phase products
7. condensed fluid 8. tail gas 9. recyclegas
10. circulating pump 11. heaters 13,13A, 13B, 13C injector
28,28A, 28B, 28C down-comer 16. liquid-solid separators
17. poor solids content slurry 18. pressure-reducing valve 19. gas-liquid separators
20. tail gas 21. secondary liquid-solid separator 22. product liquids
The outer circulation slurry of 23. circulating pump 24. poor solid contents
The gas reaction material that 25. gas compressors 26. are fresh
27. gas distributor 110 exit face 112 small pore-like openings
101 block pieces
The specific embodiment
" scope " disclosed herein is with the form of lower limit and the upper limit.Can be respectively one or more lower limits, and one or more upper limit.Given range limits by a selected lower limit and a upper limit.Selected lower limit and the upper limit define the border of special scope.All scopes that can limit by this way comprise with capable of being combined, and any lower limit can be combined to form a scope with any upper limit.For example, for special parameter, listed the scope of 60-120 and 80-110, be interpreted as that the scope of 60-110 and 80-120 also expects.In addition, if the minimum zone value 1 and 2 of listing, and if listed maximum magnitude value 3,4 and 5, scope below can all expect: 1-3,1-4,1-5,2-3,2-4 and 2-5.In the present invention, if not special explanation, all embodiments mentioned in this article and preferred embodiment can be combined to form new technical scheme mutually.
In the present invention, if not special explanation, all technical characterictics mentioned in this article and preferred feature can be combined to form new technical scheme mutually.
In the present invention, if not special explanation mentioned in this article can sequentially be carried out in steps, also can carry out at random, but preferably in sequence.For example, described method comprises step (a) and (b), represents that described method can comprise in sequence step (a) and (b), also can comprise in sequence step (b) and (a).For example, describedly mention described method and also can comprise step (c), represent that step (c) can random order join described method, for example, described method can comprise step (a), (b) and (c), also step (a), (c) and (b) be can comprise, step (c), (a) and (b) etc. also can be comprised.
Fig. 1 has shown a specific embodiment of paste state bed reactor of the present invention.As seen from the figure, this reactor comprises two parts, i.e. part beyond part in reactor shell and reactor shell.In reactor shell 1, comprise a plurality of down-comers 28, a plurality of injector 13 (for example 13A, 13B) and gas distributor 27.Described reactor shell 1 can contain slurries, and described slurries can be anyly by solid matter, to be dispersed in the slurry forming in liquid.Outside described reactor shell 1, comprise that can be used to that at least a portion slurry state material in the slurries of gas-liquid interface 2 belows is drawn to also outer circulation from reactor gets back to described reactor shell 1, described injector 13A is got back in outer circulation specifically, the middle part external circulating device of 13B, and can be used at least a portion outer circulation in reacted gaseous state material to get back to described reactor shell 1, described injector 13A is got back in outer circulation specifically, the top external circulating device of 13B.Described reacted gaseous state material can comprise in the gaseous products that obtains after slurry reactor and reaction the not gas raw material of complete reaction, and described gas raw material can comprise the inert gas that participates in the reacting gas of reaction and do not participate in reacting.
Gas reaction material 26 can be controlled or the parts such as manually operated pipeline, valve, control device are delivered to gas distributor 27 by well known to a person skilled in the art by automation, according to concrete technique needs, these parts can also comprise optional pump, pressue device, decompressor, heater, cooling device, checkout gear etc.The gas reaction material 26 of carrying can comprise any gas material that reaction process is required, such as reactant, inert dilution gas, be used for making reaction system inactivation and stop the gas etc. of reaction.These gas materials can mix first mutually, and then send in reactor shell 1, or according to required ratio, carry multiple gases material by many parallel pipelines simultaneously.
Described gas distributor 27 can be arbitrary gas distribution apparatus known in the art, for example, comprise the gas distribution grid of porous, comprises the gas distributor of emitter construction etc.
As shown in Figure 3, above described gas distributor 27, a plurality of down-comers 28 evenly arrange along the inwall of described reactor shell 1.According to the size of reactor and concrete reaction process, can use the down-comer 28 of any amount.In an embodiment of the invention, described reactor comprises 3-20 down-comer, preferably 6-10 down-comer, more preferably 8 down-comers.Optionally, below down-comer, outlet arranges block piece 101, described block piece 101 along continuous straight runs are greater than the cross-sectional area in exit, down-comer below conventionally in the face of the area of the cross section of the face of gas distributor 27, thereby prevent from a longitudinal direction directly entering described center down-comer and affecting wherein homogeneity and the mobile performance of slurries from the ascending air of gas distributor 27.
As shown in Figure 1, for example 13A and 13B of a plurality of injector 13() in mode placed in the middle, be arranged on the interior different height of described reactor shell 1.As shown in Figure 3, for example 13A, 13B and 13C of a plurality of injector 13() in mode placed in the middle, be arranged on the interior different height of described reactor shell 1 equally.In reactor of the present invention, can comprise that 2-10 layer is arranged on the injector 13 of differing heights, every layer comprises 1-10 injector, and the injector in every layer arranges in symmetrical mode.That is to say and work as every layer when only comprising 1 injector, this injector arranges in mode placed in the middle along the longitudinal central axis line of reactor.When comprising over 1 injector, these injectors are set in centrosymmetric mode around the longitudinal central axis line of reactor.The opening direction of described injector make liquid substance from described injector to directly over or oblique upper eject.
In the present invention, also the height of these injectors has been carried out to concrete restriction.In one embodiment, described gas distributor 27 and injector (the injector 13B in Fig. 1 for example that approaches this gas distributor 27 most, injector 13C in Fig. 3) difference in height between is at least reactor cylinder height L(reactor cylinder height L as shown in Figure 7, for the top head bend line of the reactor distance to bottom head bend line) 1%, for example 1%, 1.5%, 2%, 2.5%, 3%, 3.5%, 4%, 4.5% or 5%, be preferably at least 2.5% of reactor cylinder height L; Described gas distributor 27 and the difference in height approaching most between the injector of this gas distributor 27 are no more than 20% of reactor cylinder height L, for example 8%, 9%, 10%, 11%, 12%, 13%, 14%, 15% or 20%, be preferably and be no more than 10% of reactor cylinder height L.
In one embodiment, approach most injector (the injector 13B of Fig. 1 for example of described gas distributor 27, injector 13C in Fig. 3) with the most for example, away from the injector of described gas distributor 27 (the injector 13A in Fig. 1, injector 13A in Fig. 3) difference in height between is at least 40% of reactor cylinder height L, for example 40%, 45%, 50%, 55% or 60%, be preferably at least 50% of reactor cylinder height; Approach most injector (the injector 13B of Fig. 1 for example of described gas distributor 27, injector 13C in Fig. 3) with the most for example, away from the injector of described gas distributor 27 (the injector 13A in Fig. 1, injector 13A in Fig. 3) difference in height between is no more than 90% of reactor cylinder height L, for example 70%, 75%, 80%, 85% or 90%, be preferably and be no more than 80% of reactor cylinder height.
In one embodiment, approach the injector of described gas distributor 27 most and between the injector away from described gas distributor 27, have an injector at least, between described injector in vertical direction with even or inhomogeneous vertical separation setting.
In an embodiment of the invention, when paste state bed reactor of the present invention is during in regular service conditions, the height of the gas-liquid interface 2 of setting from described gas distributor 27 to described serum materials be H(gas-liquid interface height H as shown in Figure 7), described gas distributor 27 and the difference in height that approaches most between the injector 13 of this gas distributor are 2% ~ 20%H, be preferably 5% ~ 10%H, remaining injector is arranged between described gas-liquid interface and the described injector that approaches gas distributor most, preferably with uniform vertical separation setting.
It is 0.001 ~ 0.05W/m that the unit volume of the slurry penetrating from described injector in an embodiment of the invention, is sprayed kinetic energy
3, be preferably 0.002 ~ 0.005W/m
3.The unit volume of the slurry that in an embodiment of the invention, described injector penetrates is sprayed kinetic energy and is at least 0.001W/m
3, 0.002W/m
3, 0.003W/m
3, 0.004W/m
3, 0.005W/m
3or 0.008W/m
3.The unit volume of the slurry that in an embodiment of the invention, described injector penetrates is sprayed kinetic energy and is no more than 0.01W/m
3, 0.02W/m
3, 0.03W/m
3, 0.04W/m
3or 0.05W/m
3.In an embodiment of the invention, the position of described injector in reactor shell is adjustable.
Described injector 15 can be the injector of any kind, and Fig. 4 has shown the schematic diagram that can be used as the venturi-type eductors of injector of the present invention.This venturi-type eductors opening upwards, near bore its opening first dwindles gradually and then expands gradually, the variation of this kind of bore can make all correspondingly to increase by the pressure of the liquid of this Venturi tube and flow velocity, thereby provides stronger motive force for the rising of serum materials.Similarly, Fig. 5 A has shown to have as the top of injector of the present invention the tube-shaped sputtering device of a plurality of small pore-like openings, the opening surface 110 of this injector upwards, opening surface 110 has a plurality of small pore-like openings 112 as shown in Figure 5 B, remaining part is sealed, a plurality of small pore-like openings 112 shown in figure mode with center of circle symmetry on described opening surface 110 arranges, but also can take as required other form setting.The exit direction of the liquid penetrating from described a plurality of small pore-like openings 112 can be perpendicular with described opening surface 110, also can tilt.In a most preferred embodiment, the exit direction of the liquid penetrating from described a plurality of small pore-like openings 112 distributes along the cone that is some bottom surface for summit, the described exit facet of take being positioned at described tube-shaped sputtering device axis, in described exit facet below, as shown in Figure 6A; More preferably, the exit direction of described liquid tilts with identical angle on the side of described cone, makes the direction of the liquid that each small pore-like opening penetrates without the summit of described cone, that is to say, the exit direction of liquid is that vortex makes progress, as shown in Figure 6B.In a most preferred embodiment, described small pore-like opening 112 opening direction separately in the mode inwardly assembled towards oblique upper, with the angle of horizontal plane be 45-90 °, with the angle of vertical direction be 0-45 °.This kind arranges form especially can provide for the decline of serum materials in down-comer stronger motive force equally.
Although the reactor shown in Fig. 1 only comprises one deck down-comer, according to the concrete feature of the aspects such as concrete reactive species, reaction system scale, structure of reactor, also can the more multi-layered down-comer of choice for use.Fig. 3 has specifically shown a kind of reactor that comprises three layers of down-comer.Reactor shown in Fig. 3 comprises three groups of down-comers, and every group comprises 3-20 down-comer, preferably 6-10 down-comer, more preferably 8 down-comers.The down-comer of each group is arranged in same layer, along the inwall of reactor shell 1, vertically extends identical length.That is to say, the down-comer of every one deck is mutually to align in the horizontal direction, and it is horizontally disposed with position as shown in sectional view 2.Not down-comer on the same group vertically alignment separately in vertical direction, makes serum materials can pass through swimmingly each down-comer, near arrival gas distributor 27 tops that decline liquid-vapor interface 2.In the reactor of Fig. 3, also comprise three injectors, the set-up mode of the injector in its set-up mode and above Fig. 1 is basic identical, does not repeat them here.
In described reactor shell 1, holding slurries, for example, for Fischer-Tropsch reaction, described slurries can be that the solid matters such as corresponding catalyst are suspended in the materials such as liquid solvent, product, accessory substance and form.Under paste state bed reactor use state, preferably, the height of the gas-liquid interface 2 of described slurries, higher than the height of described down-comer and injector, is all positioned under described gas-liquid interface 2 the latter.
In the outside of described reactor shell 1, be also provided with middle part external circulating device and/or top external circulating device.Can only have middle part external circulating device, can only have top external circulating device, preferably have top external circulating device, most preferably middle part external circulating device and top external circulating device all have.Described middle part external circulating device comprises liquid-solid separator 16 and the circulating pump 23 being positioned within reactor shell, when if in the middle part of carrying out there is gas in the serum materials of outer circulation, also can comprise gas-liquid separator 19 at middle part external circulating device, optionally also can comprise in addition secondary liquid-solid separator 21 and optional heater 11.Under paste state bed reactor normal operating condition, preferably, described liquid-solid separator 16 is positioned under gas-liquid interface 2, is used for a part of slurries carry out solid-liquid separation and draw, this liquid-solid separator 16 can be the filter of one or more routines, can be also liquid-solid cyclone separator.Preferably, through the poor solids content slurries 17 that filter, by pressure-reducing valve 18, be transported to gas-liquid separator 19, from liquid, aftertreatment technology is directly discharged or sent to isolated gas as tail gas 20, remove gas liquid afterwards and carry out further solid-liquid separation or the separation of liquid-liquid at secondary liquid-solid separator 21, valuable liquid reaction product 22 is shifted out to reaction system, then by remaining liquid, be that the outer circulation slurry 24 of poor solid content is by circulating pump 23, at optional heater 11, be heated to reaction temperature, then send reactor shell 1 back to, particularly send injector 13A back to, 13B, 13C, thereby complete the middle part outer circulation process of slurries.Hereinto in portion's external circulating device, the devices such as described liquid-solid separation device, gas-liquid separator, circulating pump and heater can be any suitable means well known in the art, but one preferred embodiment in, described circulating pump is unshrouded impeller circulating pump preferably, this kind of circulating pump has stronger resistance to abrasion of particles performance, is also conducive to slow down the abrasion of particles of catalyst simultaneously.
Described top external circulating device comprises condenser 4, gas-liquid separator 5, circulating pump 10 and optional heater 11.The product of gaseous state or accessory substance carrying secretly some liquid even solid matter leave described gas-liquid interface 2 and rise to gas-liquid separation space 3, in this space, there is solution-air or gas-solid separation to a certain degree, then come reactor shell 1 outside, in condenser 4, there is condensation, in gas-liquid separator 5, carry out sufficient gas-liquid separation, in gas phase separation thing, nugatory component discharges or delivers to other aftertreatment technology as tail gas 8, after unreacted gas raw material compresses by gas compressor 25 as recyclegas 9, again deliver to gas distributor 27 with after fresh gas reaction material 26 mixes.A part in the liquid component that separation obtains is discharged as certain liquid-phase product 6, and liquid component capable of circulation (being generally the light hydrocarbons of carbon 5-carbon 10) is as outer circulation serum materials process circulating pump 10, at optional heater 11, be heated to required reaction temperature, then send injector 13A, 13B, 13C back to.In the present invention, the heater that the heater that described middle part external circulating device comprises and described top external circulating device comprise can, for same (example as shown in figures 1 and 3), also can comprise respectively a heater (not shown).In an embodiment of the invention, middle part external circulating device and top external circulating device respectively comprise a heater, top outer circulation can keep the arrangement of Fig. 1 and Fig. 3 constant, for middle part outer circulation, need to be after the outer circulation slurries 24 process circulating pumps 23 of poor solid content, before getting back to injector 13, access a heater.
Specifically, outer circulation liquid of the present invention can be the gas-phase product at the in the future autoreactor top oil phase through foam removal, condensation, after being separated, dewatering, also can be from the slurries phase below slurries liquid level, but also can only adopt wherein a kind of to provide outer circulation material for described injector.For example, can only use top external circulating device that outer circulation material is provided, also can only use middle part external circulating device that outer circulation material is provided, preferably only use top external circulating device that outer circulation material is provided.
The paste state bed reactor of the application of the invention, the invention provides a kind of slurry reactor method with improved Matter Transfer and stability, specifically, described method can be carried out according to following steps: first, by gas reaction material 26 for example synthesis gas deliver to gas distributor 27, through gas distributor 27, make this gas reaction material 26 be uniformly distributed or distribute according to ad hoc fashion, after described gas distributor 27, gas reaction material is within reactor shell 1, in space outside down-comer 28, rise, when rising be contained in described cylindrical shell 1 within slurry state material contact, in slurries, under the effect of catalyst, react, in addition, the rising of described gas has also brought rising power to slurries, drive described slurries to rise thereupon, described gas reaction material rises to gas-liquid interface 2 in reaction, carry some slurries risings secretly and leaving described gas-liquid interface 2, from the outlet at reactor shell 1 top, draw, send into top external circulating device, this top external circulating device as described above, by condenser 4 condensations, by gas-liquid separator 5, liquids and gases are separated, using containing for example carbon 12, to the liquid of the heavy hydrocarbon of carbon 30, as certain liquid-phase product 6, discharge, in isolated gas, nugatory part is discharged as tail gas 8, and the unreacted unstrpped gas wherein comprising as recyclegas 9 after gas compressor 25 compression, mix with fresh gas reaction material 26, again be transported to gas distributor 27 and carry out circular response.In gas-liquid separator, isolated reusable edible for example contains carbon 5 to the liquid substance of the light hydrocarbons of carbon 10, for example solvent or liquid product material, after 10 pressurizations of process circulating pump and optional heater 11 heat, be transported to described injector, within spurting into reactor shell 1.
Alternatively, use middle part external circulating device to carry out outer circulation to a part of liquid substance in the serum materials of gas-liquid interface 2 belows in reactor shell 1, preferably when carrying out outer circulation by top external circulating device, carry out middle part outer circulation.Specifically, by the liquid-solid separator 16 in reactor, remove the solid constituent in slurries, by removing solid poor solids content slurries 17 afterwards, by pressure-reducing valve 18, be transported to gas-liquid separator 19, isolated gas is drained as tail gas 20, slurry liquid phase part carries out further liquid-solid lock out operation at secondary liquid-solid separator 21, isolated a part of liquid wherein, for example the synthetic hydrocarbon product obtaining of fischer-tropsch reaction is drawn as product liquid 22, further process the operation of refining, remaining valuable liquid material (such as solvent etc.) through circulating pump 23 pressurizations and optional heater 11, heat, be transported to described injector, towards directly over or within the direction of oblique upper spurts into reactor shell 1, within the jet-action of described injector has further promoted described reactor shell 1, the rising of the serum materials in the space beyond down-comer 28.
On the other hand, under the vapor reaction material rising and injector effect, described serum materials is within reactor shell 1, after rising near gas-liquid interface 2 in space outside down-comer 28, after described reacted gaseous material leaves gas-liquid interface 2, gaseous matter departs from slurries and arrives gas-liquid separation space 3, the density of slurries increases, described serum materials enters described down-comer 28 from the top end opening of described down-comer 28, under the effect of slurries self gravitation, flow downward, at down-comer 28 bottom openings, flow out, now slurries arrive gas distributor 27 tops, again under the drive of gas reaction material within reactor shell, in space outside down-comer, rise.That is to say, the slurries within reactor shell 1 rise outside down-comer 28, within down-comer 28, decline, and form the interior circulation of slurries within reactor shell 1.Simultaneously, in reactor shell, arrange and there is the described injector that height, interval and angle are set, by towards directly over or oblique upper atomizing of liquids material, promoted the rising of slurries in the space between reactor shell inwall and down-comer, accelerated interior circulation.In addition, middle part external circulating device makes at least a portion slurry state material get back in reactor shell by the external outer circulation of reactor cylinder, and the circulating fluid looping back (for example light hydrocarbons of carbon containing 5-carbon 10) continues to get back in reactor shell slurries are played to stirring, suspension effect; Top external circulating device makes at least a portion gaseous state material get back in reactor shell by the external outer circulation of reactor cylinder, the recyclegas looping back continues to participate in reaction, and the circulating fluid looping back (light hydrocarbons of carbon containing 5-carbon 10) continues to get back to reactor shell slurries are played to stirring, suspension effect.By above-mentioned set-up mode, the particle suspension in described paste state bed reactor, liquid-solid mixing and heat transfer and mass transfer have been strengthened.The slurry reactor that can use the method to carry out is selected from the reaction of fischer-tropsch reaction, DCL/Direct coal liquefaction reaction, synthesizing dimethyl ether by synthetic gas and the reaction of synthesis gas synthesizing methanol, is preferably fischer-tropsch reaction.
When using reactor of the present invention to carry out Fischer-Tropsch reaction, described slurry is that catalyst solid is suspended in the slurry forming in hydrocarbon ils, the mist of unstrpped gas CO and hydrogen reacts in described slurry, generates the accessory substances such as hydrocarbon product and a small amount of water, carbon dioxide.In the case, in the cyclic process outside of described middle part external circulating device, remove moisture and the gaseous matter in slurry, by the separated recovery of hydrocarbon product, then send remaining slurries back to injector.And liquid in the external circulating device of top is mainly low boiling volatile component, as C5 ~ C10 light hydrocarbons.In addition, entrainment effect due to reactor head tail gas, under a small amount of reaction temperature and pressure, for the heavy end of liquid also can enter exhaust system, through foam removal, condensation, phase-splitting and after dewatering, finally still have and seldom measure heavy end and enter outer circulation liquid stream thigh (engineering term, a logistics).
Slurry bed ft synthetic reactor is a complete reaction system, by external liquid circulation, is strengthened turbulent flow and is improved that particle suspends and liquid-solid mixed effect is one of effective means.In paste state bed reactor of the present invention, be provided with the down-comer that contributes to circulation in slurry.
The present invention is by arranging down-comer and injector, and serum materials rises outward at down-comer under the effect of injector, in down-comer, declines, and setting up thus inside and outside down-comer is the interior circulation in reactor shell.The present invention will be sprayed and be entered reactor shell by injector after material outside circulation by top external circulating device and middle part external circulating device, by position and the angle of preferred injector, strengthened turbulence effects, strengthened gas-liquid and liquid-solid between stirring, improved that particle suspends and liquid-solid circulation.Preferably, the injection kinetic energy of unit slurry volume only need maintain the required turbulent flow of reaction, otherwise too high injection kinetic energy will cause energy consumption excessive, also can produce to reactor inner member the problems such as mechanical oscillation simultaneously.Outer circulation liquid sprays and enters reactor slurry from the injector according to special angle and set positions, and the injection kinetic energy of unit slurry volume is 0.001 ~ 0.05W/m
3, be preferably 0.002 ~ 0.005W/m
3, for example, can be at least 0.001W/m
3, 0.002W/m
3, 0.003W/m
3, 0.004W/m
3, 0.005W/m
3or 0.008W/m
3, for example can be no more than 0.01W/m again
3, 0.02W/m
3, 0.03W/m
3, 0.04W/m
3or 0.05W/m
3.
Claims (25)
1. a paste state bed reactor, described paste state bed reactor comprises: reactor shell (1), be arranged on a plurality of down-comers (28) within described reactor shell, a plurality of injectors (13) and gas distributor (27), middle part external circulating device and/or top external circulating device, described middle part external circulating device is used at least a portion slurry state material in reactor shell to draw and at least a portion outer circulation is returned in reactor shell, described top external circulating device is used at least a portion gaseous state material in reactor shell being drawn and at least a portion isolated liquid substance outer circulation from described gaseous state material being returned in reactor shell, wherein, described a plurality of down-comer is along the inwall setting of described reactor shell (1), described injector (13) is arranged on different vertical heights at described cylindrical shell (1) middle section, the opening direction of described injector (13) towards directly over or oblique upper.
2. paste state bed reactor as claimed in claim 1, it is characterized in that, described gas distributor (27) and the difference in height approaching most between the injector of this gas distributor (27) are at least 1% of reactor cylinder height, are preferably at least 2.5% of reactor cylinder height.
3. paste state bed reactor as claimed in claim 2, it is characterized in that, described gas distributor (27) and the difference in height approaching most between the injector of this gas distributor (27) are no more than 20% of reactor cylinder height, are preferably and are no more than 10% of reactor cylinder height.
4. the paste state bed reactor as described in any one in claim 1-3, it is characterized in that, approach most the injector of described gas distributor (27) and away from the difference in height between the injector of described gas distributor (27), be at least 40% of reactor cylinder height, being preferably at least 50% of reactor cylinder height.
5. paste state bed reactor as claimed in claim 4, it is characterized in that, approach most the injector of described gas distributor (27) and away from the difference in height between the injector of described gas distributor (27), be no more than 90% of reactor cylinder height, being preferably and being no more than 80% of reactor cylinder height.
6. the paste state bed reactor as described in any one in claim 1-5, it is characterized in that, approach most the injector of described gas distributor (27) and between the injector away from described gas distributor (27), have an injector at least, between described injector in vertical direction with even or inhomogeneous vertical separation setting.
7. the paste state bed reactor as described in any one in claim 1-6, is characterized in that, described middle part external circulating device comprises liquid-solid separator (16) and circulating pump (23).
8. paste state bed reactor as claimed in claim 7, is characterized in that, described middle part external circulating device also comprises gas-liquid separator (19).
9. paste state bed reactor as claimed in claim 8, is characterized in that, described middle part external circulating device also comprises secondary liquid-solid separator (21).
10. paste state bed reactor as claimed in any one of claims 7-9, is characterized in that, described middle part external circulating device also comprises heater.
11. paste state bed reactors as described in any one in claim 7-10, is characterized in that, described liquid-solid separator (16) is positioned at described reactor shell.
12. paste state bed reactors as described in any one in claim 7-11, is characterized in that, described top external circulating device comprises condenser (4), gas-liquid separator (5) and circulating pump (10).
13. paste state bed reactors as claimed in claim 12, is characterized in that, described top external circulating device also comprises heater.
14. paste state bed reactors as described in any one in claim 7-13, is characterized in that, described circulating pump (10,23) is centrifugal pump with open impellerpump.
15. paste state bed reactors as described in any one in claim 1-14, is characterized in that, described injector (13) is venturi-type eductors.
16. paste state bed reactors as described in any one in claim 1-15, it is characterized in that, injector described at least one (13) is the tube-shaped sputtering device that exit face has a plurality of small pore-like openings, described small pore-like opening opening direction separately in the mode inwardly assembled towards oblique upper, with the angle of horizontal plane be 45-90 °.
17. paste state bed reactors as described in any one in claim 1-16, is characterized in that, described paste state bed reactor comprises that 2-10 group is arranged on the down-comer of different vertical height.
18. paste state bed reactors as claimed in claim 17, is characterized in that, every group of down-comer extends in substantially the same vertical height.
19. paste state bed reactors as described in any one in claim 17-18, is characterized in that, every group of down-comer in the mode of substantial horizontal alignment along reactor shell (1) inwall setting.
20. paste state bed reactors as described in any one in claim 17-19, is characterized in that, belong to not corresponding down-comer on the same group substantial alignment vertically separately.
21. 1 kinds of methods that are used for carrying out slurry reactor, described method is used the paste state bed reactor as described in any one in claim 1-20, said method comprising the steps of:
I) gas reaction material is delivered to gas distributor (27), through the gas after gas distributor reactor shell (1) in, rise in down-comer (28) space in addition and drive and starch state material and rise thereupon, and react under the effect of starching state material inner catalyst;
Ii) the gaseous state material clamp after reaction rises to the top of reactor shell with some slurries, use top external circulating device that the gaseous state material after described reaction is drawn, gas in gaseous state material after described reaction is separated with the slurries of carrying secretly, then within the isolated liquid substance outer circulation of at least a portion being returned to reactor shell (1), preferably send back to through described injector, described injector towards top or oblique upper spray;
Iii) alternatively, use middle part external circulating device that at least a portion slurry state material in reactor shell is drawn, liquid substance in described slurry state material is separated with solid matter, and within the isolated liquid substance outer circulation of at least a portion is returned to reactor shell (1), preferably send back to through described injector, described injector towards top or oblique upper spray;
Iv) a part of described slurry state material flows in described down-comer (28) from described down-comer (28) top end opening, in down-comer, flow downward, and flow out from down-comer (28) bottom opening, then under the drive of gas reaction material, in the space in reactor shell, outside down-comer, rise, and repeat above-mentioned step (i)-(iv).
22. 1 kinds of methods that are used for carrying out slurry reactor, described method is used the paste state bed reactor with the reactor shell of slurries, said method comprising the steps of:
I) to gas distributor (27) the conveying gas precursor reactant material in described reactor shell to drive described slurries to rise, and described gas reaction material reacts in slurries;
Ii) from reactor shell upper area, the reacted gaseous state material of at least a portion is drawn to reactor shell, gas in described gaseous state material is separated with the serum materials of carrying secretly, then within the isolated liquid substance outer circulation of at least a portion being returned to reactor shell, preferably by injector (13), send back to, described injector towards top or oblique upper spray;
Iii) alternatively, at least a portion is starched to state material to be led to outside reactor shell from reactor shell, liquid substance in described slurry state material is separated with solid matter, and then within the isolated liquid substance outer circulation of at least a portion is returned to reactor shell, preferably by injector (13), send back to, described injector towards top or oblique upper spray;
Iv) the described slurry state of part material is flowed into from described down-comer upper opening, and flow out from described down-comer bottom, enter lower region in reactor shell.
23. methods as described in any one in claim 21-22, is characterized in that, the unit volume of the slurry penetrating from described injector is sprayed kinetic energy for 0.001W/m at least
3, be preferably at least 0.002W/m
3.
24. methods as described in any one in claim 21-23, is characterized in that, the unit volume of the slurry penetrating from described injector is sprayed kinetic energy and is no more than 0.05W/m
3, be preferably and be no more than 0.005W/m
3.
25. methods as described in any one in claim 21-24, is characterized in that, described slurry reactor is selected from the reaction of fischer-tropsch reaction, DCL/Direct coal liquefaction reaction, synthesizing dimethyl ether by synthetic gas and the reaction of synthesis gas synthesizing methanol, is preferably fischer-tropsch reaction.
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|---|---|---|---|
| CN201310050846.1A CN103977747B (en) | 2013-02-08 | 2013-02-08 | Paste state bed reactor and the method that slurry reactor is carried out with the paste state bed reactor |
| PCT/CN2014/071655 WO2014121720A1 (en) | 2013-02-08 | 2014-01-28 | A slurry-bed reactor and a method for conduction slurry-bed reaction using the slurry-bed reactor |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201310050846.1A CN103977747B (en) | 2013-02-08 | 2013-02-08 | Paste state bed reactor and the method that slurry reactor is carried out with the paste state bed reactor |
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| WO (1) | WO2014121720A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN113061071A (en) * | 2021-03-29 | 2021-07-02 | 上海睿碳能源科技有限公司 | Method and equipment for directly preparing olefin from synthesis gas based on slurry bed reactor |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117487641B (en) * | 2023-11-05 | 2024-04-02 | 枣庄市杰诺生物酶有限公司 | Isoleucine preparation equipment and preparation method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6835756B2 (en) * | 2000-10-13 | 2004-12-28 | Bp Exploration Operating Company Ltd. | Fischer-tropsch synthesis process |
| CN101396647B (en) * | 2007-09-29 | 2011-03-16 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
| CN102441351A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Slurry bed Fischer-Tropsch synthetic reactor |
| CN202376973U (en) * | 2011-12-07 | 2012-08-15 | 新奥科技发展有限公司 | Fluidized bed reactor |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5382748A (en) * | 1992-12-18 | 1995-01-17 | Exxon Research & Engineering Co. | Hydrocarbon synthesis reactor employing vertical downcomer with gas disengaging means |
| US6570047B1 (en) * | 2001-11-06 | 2003-05-27 | Exxonmobil Research And Engineering Company | Slurry hydrocarbon synthesis with external hydroisomerization in downcomer reactor loop |
| GB2410906B (en) * | 2001-12-04 | 2006-07-12 | Sasol Technology | Slurry phase apparatus |
| US8119014B2 (en) * | 2008-12-23 | 2012-02-21 | Exxonmobil Research And Engineering Company | Systems and methods to remove liquid product and fines from a slurry reactor |
-
2013
- 2013-02-08 CN CN201310050846.1A patent/CN103977747B/en not_active Expired - Fee Related
-
2014
- 2014-01-28 WO PCT/CN2014/071655 patent/WO2014121720A1/en active Application Filing
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6835756B2 (en) * | 2000-10-13 | 2004-12-28 | Bp Exploration Operating Company Ltd. | Fischer-tropsch synthesis process |
| CN101396647B (en) * | 2007-09-29 | 2011-03-16 | 中科合成油技术有限公司 | Gas-liquid-solid three-phase suspended bed reactor for f-t synthesis and use thereof |
| CN102441351A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Slurry bed Fischer-Tropsch synthetic reactor |
| CN202376973U (en) * | 2011-12-07 | 2012-08-15 | 新奥科技发展有限公司 | Fluidized bed reactor |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN113061071A (en) * | 2021-03-29 | 2021-07-02 | 上海睿碳能源科技有限公司 | Method and equipment for directly preparing olefin from synthesis gas based on slurry bed reactor |
| CN113061071B (en) * | 2021-03-29 | 2024-02-13 | 上海睿碳能源科技有限公司 | Method and equipment for directly preparing olefin from synthesis gas based on slurry bed reactor |
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| CN103977747B (en) | 2018-01-30 |
| WO2014121720A1 (en) | 2014-08-14 |
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