CN103769010A - Fluidized bed reactor - Google Patents
Fluidized bed reactor Download PDFInfo
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- CN103769010A CN103769010A CN201210401551.XA CN201210401551A CN103769010A CN 103769010 A CN103769010 A CN 103769010A CN 201210401551 A CN201210401551 A CN 201210401551A CN 103769010 A CN103769010 A CN 103769010A
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Abstract
The present invention relates to a fluidized bed reactor, which comprises a housing and a three-phase separation part, wherein the housing sequentially comprises an enlargement section, a transition section and a straight tube section from top to bottom, the three-phase separation part is arranged inside the enlargement section and the transition section, and the side wall of the enlargement section is provided with a liquid discharge port. The fluidized bed reactor further comprises an inner pipe and a gas-liquid distributer, wherein the inner pipe is arranged inside the housing and extends from the lower portion of the straight tube section to the lower portion of the enlargement section, the lower end opening of the inner pipe is communicated with the straight tube section, the upper end opening of the inner pipe is communicated with the enlargement section, the three-phase separation part is distributed around the upper portion of the inner pipe, and the gas-liquid distributer is arranged in the straight tube section and is positioned on the bottom of the inner pipe. According to the fluidized bed reactor, material circulation can be driven completely through the kinetic energy of the material on the inlet and the density difference of the materials in different areas in the reactor, such that the whole process has the characteristic of energy saving; and the reactor utilization efficiency is high, such that the generation of the thermal cracking reaction in the absence of the hydrogen can be substantially reduced during the heavy oil hydrocracking process.
Description
Technical field
The present invention relates to a kind of fluidized bed reactor, particularly, relate to a kind of interior circulation type fluidized bed reactor.
Background technology
Boiling bed hydrogenation reactor is gas-liquid-solid three-phase fluid bed reactor, and this class reactor has following advantage: weight, the inferior raw material that can process high tenor, high carbon residue; Temperature of reactor is control and even easily, and pressure drop is low and constant; Can add online and take out catalyst, therefore catalyst performance can keep constant in the whole operation cycle; Can reach higher conversion ratio and longer operation cycle.
Existing industrialization boiling bed hydrogenation technology comprises H-Oil technique and LC-Fining technique etc., is provided with circulation cup and carries out gas-liquid separation in the fluidized bed reactor of these two kinds of techniques, and isolated oil product circulates through circulation down-comer and circulating pump.Existing boiling bed hydrogenation technique exists following deficiency: (1) complex operation, need to use complicated charge level monitor and oil circulating pump, the stability of a system is poor, when oil circulating pump breaks down catalyst can because of cannot fluidisation to reactor bottom sedimentation, cause device to be forced to stop work; (2) catalyst in reactor reserve is lower, and space reactor utilization rate is low; (3) energy consumption is large, and the fluidisation of solid catalyst is squeezed into a large amount of recycle oil by oil circulating pump and realized; (4) in circulation down-comer, hydrogen is little, is non-hydrogen environment, and liquid second pyrolysis reaction coking at high temperature can occur and reduces product quality.
At present, the improvement direction of fluidized bed reactor mainly comprises: reduce the complexity of technique, improve the space availability ratio of reactor, reduce the operating flexibility of energy consumption and raising reactor etc.For example, CN1448212A discloses a kind of fluidized bed reactor, and this fluidized bed reactor has been cancelled complicated charge level monitor and oil circulating pump, therefore has the features such as simple in structure, processing ease.But because this reactor uses the solid catalyst that particle diameter is 0.1-0.2mm, therefore operating flexibility is less, and catalyst is easily taken reactor out of, affects the operational stability of system.CN201529519U discloses a kind of fluidized bed reactor of external loop type, catalyst is fluidisation better, but this reactor circulates in down-comer in running does not almost have hydrogen, at high temperature can there is second pyrolysis reaction coking and reduce product quality in liquid; And the requirement to material in actual production of the structure of this external loop reactor is higher.
Summary of the invention
The object of the invention is the above-mentioned defect existing in order to overcome existing fluidized bed reactor, a kind of new fluidized bed reactor is provided.
The invention provides a kind of fluidized bed reactor, this fluidized bed reactor comprises housing and three phase separation parts, described housing comprises expanding reach from top to bottom successively, changeover portion and direct tube section, described three phase separation parts are arranged in described expanding reach and described changeover portion, on the sidewall of described expanding reach, be provided with liquid outlet, wherein, described fluidized bed reactor also comprises inner tube and gas-liquid distributor, described inner tube is arranged in described housing, and extend to the bottom of described expanding reach from the bottom of described direct tube section, the lower ending opening of described inner tube is communicated with described direct tube section, the upper end open of described inner tube is communicated with described expanding reach, described three phase separation component distribution is around the top of described inner tube, described gas-liquid distributor is arranged in described direct tube section, and is positioned at the bottom of described inner tube.
Preferably, more than the outlet of described gas-liquid distributor is positioned at the lower ending opening of described inner tube.
Preferably, the diameter of described inner tube and the diameter ratio of described direct tube section are 0.55-0.84:1.In the present invention, " diameter " typically refers to internal diameter.
Preferably, described three phase separation parts comprise inner core and urceolus from inside to outside successively, the bottom of described inner core is large downward opening hollow round table, the hollow round table of the bottom of described inner core is positioned at the below of the upper end open of described inner tube, the upper end open of described urceolus is positioned at the top of the upper end open of described inner core, the upper end open of described inner core is positioned at the top of the upper end open of described inner tube, the upper end open diameter of the hollow round table of the bottom of described inner core is greater than the diameter of described inner tube, between the lower end of described inner core and described urceolus and the inwall of described housing, there is gap, the lower ending opening of described urceolus is positioned at the below of described liquid outlet, the upper end open of described urceolus is positioned at the top of described liquid outlet.In the present invention, the large opening of hollow round table is relative concept with " greatly " in little opening with " little ", the large opening of hollow round table refers to larger one end of opening diameter of hollow round table, and the little opening of hollow round table refers to less one end of opening diameter of hollow round table.
More preferably, the upper end open diameter of the diameter of described inner tube, described inner core and the upper end open diameter of described urceolus increase successively.
More preferably, the lower ending opening diameter of described urceolus is greater than the lower ending opening diameter of described inner core.
More preferably, the upper end open of described urceolus is positioned at the below of the upper end open of described expanding reach.
Preferably, the top of described inner core is large opening up hollow round table.
More preferably, the bus of the hollow round table on the top of described inner core and the angle of axis are for being greater than 0 ° to 45 °, and the bus of the hollow round table of the bottom of described inner core and the angle of axis are for being greater than 0 ° to 75 °.
Preferably, the top of described urceolus is straight tube, and bottom is large downward opening hollow round table.
More preferably, the upper end open of the hollow round table of the bottom of described urceolus is positioned at the top of the upper end open of the hollow round table of the bottom of described inner core, and is positioned at the below of the upper end open of described inner core; The lower ending opening of the hollow round table of the bottom of described urceolus is positioned at the top of the lower ending opening of the hollow round table of the bottom of described inner core.
More preferably, the bus of the hollow round table of the bottom of described urceolus and the angle of axis are for being greater than 0 ° to 75 °.
Preferably, the top of described housing is provided with catalyst and adds pipe, and the bottom of described housing is provided with catalyst discharge pipe.
In described fluidized bed reactor of the present invention, by inner tube being set in the direct tube section of housing, and make gas-liquid distributor be positioned at the bottom of described inner tube, the circulation of material in reactor can be promoted jointly by the density contrast of material in the kinetic energy of entrance material and tedge (being inner tube) and down-comer (ring pipe being made up of inner tube and direct tube section) completely, thereby can cancel circulating pump and the charge level monitor of complicated operation, make whole technique more energy-conservation, and operation is simpler.
And, in the running of described fluidized bed reactor of the present invention, in tedge and down-comer, be all the state that gas-liquid-solid three-phase coexists, thereby can react in tedge and down-comer, thereby greatly improved the utilization ratio of reactor; And guaranteed the nitrogen atmosphere of facing of tedge and down-comer, thereby greatly reduced the generation of the heat scission reaction under non-hydrogen environment, thus can avoid the coking producing due to the heat scission reaction of non-hydrogen atmosphere.
Other features and advantages of the present invention are described in detail the specific embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is to be used to provide a further understanding of the present invention, and forms a part for description, is used from explanation the present invention, but is not construed as limiting the invention with the specific embodiment one below.In the accompanying drawings:
Fig. 1 is according to the structural representation of the fluidized bed reactor of the preferred embodiment of the present invention;
Fig. 2 is the parameter schematic diagram according to the fluidized bed reactor of the preferred embodiment of the present invention;
Fig. 3 is the structural representation of a kind of embodiment of gas-liquid distributor.
Description of reference numerals
1 housing 2 three phase separation parts 3 expanding reach
4 changeover portion 5 direct tube section 6 inner tubes
7 gas-liquid distributor 9 catalyst add pipe 10 catalyst discharge pipes
11 charging aperture 12 exhaust outlet 21 inner cores
22 urceolus 31 liquid outlets
The specific embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is elaborated.Should be understood that, the specific embodiment described herein only, for description and interpretation the present invention, is not limited to the present invention.
In the present invention, in the situation that not doing contrary explanation, the noun of locality of use typically refers to reference to shown in the drawings upper and lower as " upper and lower "; " inside and outside " refers to inside and outside with respect to the profile of each parts itself.
As illustrated in fig. 1 and 2, fluidized bed reactor according to the present invention comprises housing 1 and three phase separation parts 2, described housing 1 comprises expanding reach 3 from top to bottom successively, changeover portion 4 and direct tube section 5, described three phase separation parts 2 are arranged in described expanding reach 3 and described changeover portion 4, on the sidewall of described expanding reach 3, be provided with liquid outlet 31, wherein, described fluidized bed reactor also comprises inner tube 6 and gas-liquid distributor 7, described inner tube 6 is arranged in described housing 1, and extend to the bottom of described expanding reach 3 from the bottom of described direct tube section 5, the lower ending opening of described inner tube 6 is communicated with described direct tube section 5, the upper end open of described inner tube 6 is communicated with described expanding reach 3, described three phase separation parts 2 are distributed in around the top of described inner tube 6, described gas-liquid distributor 7 is arranged in described direct tube section 5, and is positioned at the bottom of described inner tube 6.
In the present invention, described housing 1 can be the housing of conventional fluidized bed reactor.In described housing 1, described expanding reach 3 refers to the section that diameter is larger with respect to described direct tube section 5, and described expanding reach 3 is straight-tube shape conventionally substantially.Diameter (the d of described direct tube section 5
1) be less than described expanding reach 3.As described changeover portion 4, its lower ending opening overlaps with the upper end open of described direct tube section 5, its upper end open overlaps with the lower ending opening of described expanding reach 3, also the diameter that is the lower ending opening of described changeover portion 4 equates substantially with the diameter of described direct tube section 5, and the diameter of the upper end open of described changeover portion 4 equates substantially with the diameter of described expanding reach 3.
There is no particular limitation for the size of described housing, can determine according to needs of production.In the preferred case, the diameter (d of described expanding reach 3
9) be the diameter (d of described direct tube section 5
1) 1.2-2 doubly, be preferably 1.4-1.8 doubly; Height sum (the h of described expanding reach 3 and described changeover portion 4
2+ h
3) with the diameter (d of described expanding reach 3
9) ratio be 0.5-3:1, be preferably 0.8-1.5:1.Described changeover portion 4 is hollow round table shape, and it is opening up greatly, and the angle (α) of its bus and axis can be 30-75 °, is preferably 45-60 °.Height (the h of described direct tube section 5
1) and diameter (d
1) ratio can be 4-16:1, be preferably 6-12:1.
In the present invention, it is mainly that therefore, there is no particular limitation for the size of described inner tube 6 in order to make reaction mass form outside circulation in reactor that described inner tube 6 is set, and forms circulation as long as can realize.Under preferable case, the diameter (d of described inner tube 6
2) with the diameter (d of described direct tube section 5
1) ratio be 0.55-0.84:1.Height (the h of described inner tube 6
4) with the height (h of described direct tube section 5
1) ratio can be 1-1.2:1.The top of the top of described inner tube 6 and described housing 1 has gap, and the bottom of the bottom of described inner tube 6 and described direct tube section 5 has gap.
In the present invention, as illustrated in fig. 1 and 2, the bottom of described housing 1 is also provided with charging aperture 11 conventionally, and the gas-liquid mixture of question response enters in described fluidized bed reactor by described charging aperture 11 the described gas-liquid distributor 7 of process.The top of described housing 1 is also provided with exhaust outlet 12 conventionally, for discharging reactor through the isolated gas of described three-phase distributed elements 2.Described exhaust outlet 12 is preferably arranged on the center at the top of described housing 1.
In the present invention, as illustrated in fig. 1 and 2, in order to increase the stability of reactor, more than the outlet of described gas-liquid distributor 7 is preferably placed at the lower ending opening of described inner tube 6.More preferably, the outlet of described gas-liquid distributor 7 is positioned at the top of the lower ending opening of described inner tube 6, is also the inside that the outlet of gas-liquid distributor 7 is positioned at described inner tube 6 completely.In this case, the gas-liquid mixture injecting by described gas-liquid distributor 7 can all enter described inner tube 6(also referred to as tedge), and in this tedge on flow, thereby between the endless tube (also referred to as down-comer) that is conducive to form in described inner tube 6 with by described direct tube section 5 and described inner tube 6, form circulation.
Described gas-liquid distributor 7 can for various routines can make gas and the uniform structure of liquid distribution, can be for example bubble cap structure.Particularly, as shown in Figure 3, the opening of described gas-liquid distributor 7 is arranged on middle part.
In described fluidized bed reactor of the present invention, described three phase separation parts 2 are mainly used for the reacted material of described process inner tube 6 to carry out gas-solid-liquid three phase separation, out and respectively discharge by exhaust outlet 12 and liquid outlet 31 with gas and fluid separation applications that reaction is produced, and the mixture through three phase separation is turned back in described inner tube 6, to form circulation by down-comer (ring pipe being made up of described inner tube 6 and described direct tube section 5).In the preferred case, in order to reduce the amount of the catalyst of taking out of by liquid outlet 31, and further impel between described inner tube 6 and described down-comer and successfully form circulation, as illustrated in fig. 1 and 2, described three phase separation parts 2 comprise inner core 21 and urceolus 22 from inside to outside successively, the bottom of described inner core 21 is large downward opening hollow round table, the hollow round table of the bottom of described inner core 21 is positioned at the below of the upper end open of described inner tube 6, the upper end open of described urceolus 22 is positioned at the top of the upper end open of described inner core 21, the upper end open of described inner core 21 is positioned at the top of the upper end open of described inner tube 6, upper end open diameter (the d of the hollow round table of the bottom of described inner core 21
4) be greater than the diameter (d of described inner tube 6
2), between the lower end of described inner core 21 and described urceolus 22 and the inwall of described housing 1, thering is gap, the lower ending opening of described urceolus 22 is positioned at the below of described liquid outlet 31, and the upper end open of described urceolus 22 is positioned at the top of described liquid outlet 31.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, between described inner core 21 and described inner tube 6, form the first baffling district; Between described inner core 21 and described urceolus 22, form the second baffling district, between described urceolus 22 and the inwall of described housing 1, form liquid collection region.In the running of described fluidized bed reactor, through described inner tube 6 reacted gas-liquid-solid mixture described inner tube 6 interior on flow, enter described the first baffling district, because gas-liquid-solid mixture stream runs into the structure of sudden enlargement, this logistics speed upwards reduces, partially liq is being carried most of solid and portion gas secretly, and to start baffling downward, enters in described down-comer, partially liq is carrying fraction solid secretly and portion gas covers described inner tube 21, enter described the second baffling district, now the flow velocity of liquid is less, most of gas is due to the effect effusion of buoyancy and in the enrichment of the top of reactor, and liquid entrainment solid and fraction gas baffling is downward, this logistics major part turns back in described down-comer by the gap between described inner core 21 and the inwall of described housing 1, fraction enters described liquid collection region, because liquid speed is herein much smaller than the critical liquid speed that makes solid fluidisation, described solid particle can not enter supernatant layer, in the liquid of therefore discharging by liquid outlet 31, substantially do not comprise solid particle.And the logistics that enters described the first baffling district and described the second baffling district is the mixture of gas-liquid-solid three-phase; And the logistics entering in described down-comer is also the mixture of gas-liquid-solid three-phase, therefore, in whole described fluidized bed reactor, except the gas enrichment region that the top of described liquid collection region and described housing 1 forms, the logistics at all the other positions is all to exist with the form of the mixture of gas-liquid-solid three-phase, thereby catalytic reaction can both occur.Therefore, in the time that described three phase separation parts 2 have above-mentioned preferred structure, substantially can avoid catalyst solid to take out of by liquid outlet 31, but also can further improve the utilization ratio of fluidized bed reactor, greatly reduce the generation of the heat scission reaction under non-hydrogen environment simultaneously.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, preferably, described inner tube 6, described inner core 21 and described urceolus 22 all coaxially arrange with described housing 1.
Further preferably, the ratio ((d of the inlet area in described the first baffling district and the upper end open area of described inner tube 6
6 2-d
2 2)/d
2 2) be 0.3-1.5:1; The ratio ((d of the inlet area in described the second baffling district and the inlet area in described the second baffling district
8 2-d
7 2)/(d
6 2-d
2 2)) be 0.5-2:1.Wherein, d
6for the inlet diameter in described the first baffling district.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, further preferably, the diameter (d of described inner tube 6
2), the upper end open diameter (d of described inner core 21
7) and the upper end open diameter (d of described urceolus 22
8) increase successively the lower ending opening diameter (d of described urceolus 22
5) be greater than the lower ending opening diameter (d of described inner core 21
3).In this case, the mixture that is more conducive to gas-liquid-solid three-phase is realized and being separated by described three phase separation parts 2.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, further preferably, the upper end open of described urceolus 22 is positioned at the below of the upper end open of described expanding reach 3.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, the top of described inner core 21 can be straight tube, can be also large opening up hollow round table.Under preferable case, the top of described inner core 21 is large opening up hollow round table.In the time that the top of described inner core 21 is large opening up hollow round table, described inner core 21 is preferably made up of the large opening up hollow round table on top and the large downward opening hollow round table of bottom, and the upper end open of the lower ending opening of the hollow round table on top and the hollow round table of bottom overlaps.Further preferably, the two position overlapping of the upper end open of the lower ending opening of the hollow round table on top and the hollow round table of bottom is positioned at the below of the upper end open of described inner tube 6 and the lower ending opening of described expanding reach 3.
In the time that the top of described inner core 21 is large opening up hollow round table, the bus of the hollow round table on the top of described inner core 21 and the angle of axis (γ) are for being greater than 0 ° to 45 °.The bus of the hollow round table of the bottom of described inner core 21 and the angle of axis (β) can be for being greater than 0 ° to 75 °.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, described urceolus 22 can be straight tube structure.In the time that described urceolus 22 is straight tube structure, the lower ending opening of described urceolus 22 is preferably placed at the below of the lower ending opening of described expanding reach 3, and is positioned at the top of the lower ending opening of described inner core 21.
In order to reduce and even to avoid solid particle to take out of from liquid outlet 31 as far as possible, described urceolus 22 has such preferred structure: the top of described urceolus 22 is straight tube, and bottom is large downward opening hollow round table.
In the time that described urceolus 22 has above-mentioned preferred structure, further preferably, the upper end open of the hollow round table of the bottom of described urceolus 22 is positioned at the top of the upper end open of the hollow round table of the bottom of described inner core 21, and is positioned at the below of the upper end open of described inner core 21; The lower ending opening of the hollow round table of the bottom of described urceolus 22 is positioned at the top of the lower ending opening of the hollow round table of the bottom of described inner core 21.Still more preferably, the upper end open of the hollow round table of the bottom of described urceolus 22 and lower ending opening are all positioned at the top of the upper end open of the hollow round table of the bottom of described inner core 21, and are all positioned at the below of the upper end open of described inner core 21.
In the time that described urceolus 22 has above-mentioned preferred structure, further preferably, the bus of the hollow round table of the bottom of described urceolus 22 and the angle of axis (θ) are for being greater than 0 ° to 75 °.
In described fluidized bed reactor of the present invention, be preferably also provided with the online more system of catalyst changeout, add online and take out function to realize solid catalyst.The system of described more catalyst changeout can be selected any suitable equipment and method, for example can be with reference to disclosed equipment and method in US4398852.In one embodiment, in order to realize online more catalyst changeout, catalyst can be set at the top of described housing 1 and add pipe 9, in the bottom of described housing 1, catalyst discharge pipe 10 is set.In this case, can add pipe 9 to add fresh solid catalyst by the catalyst of reactor head, and can discharge by the catalyst discharge pipe 10 of reactor bottom the solid catalyst of inactivation.Described catalyst adds pipe 9 to stretch into the degree of depth in described housing 1, and there is no particular limitation, under preferable case, described catalyst adds pipe 9 outlet to be positioned at the top of the lower ending opening of described expanding reach 3, and described catalyst to add the minimum range of the lower ending opening that exports to described expanding reach 3 of pipe 9 be the height (h of described expanding reach 3
4) 40-95%, be preferably 60-90%.
In one more preferably in embodiment, as illustrated in fig. 1 and 2, described fluidized bed reactor comprises: housing 1 and three phase separation parts 2, described housing 1 comprises expanding reach 3 from top to bottom successively, changeover portion 4 and direct tube section 5, described three phase separation parts 2 are arranged in described expanding reach 3 and described changeover portion 4, on the sidewall of described expanding reach 3, be provided with liquid outlet 31, wherein, described fluidized bed reactor also comprises inner tube 6 and gas-liquid distributor 7, described inner tube 6 is arranged in described housing 1, and extend to the bottom of described expanding reach 3 from the bottom of described direct tube section 5, the lower ending opening of described inner tube 6 is communicated with described direct tube section 5, the upper end open of described inner tube 6 is communicated with described expanding reach 3, described three phase separation parts 2 are distributed in around the top of described inner tube 6, described gas-liquid distributor 7 is arranged in described direct tube section 5, and is positioned at the bottom of described inner tube 6,
Described three phase separation parts 2 comprise inner core 21 and urceolus 22 from inside to outside successively, and the bottom of described inner core 21 is large downward opening hollow round table, and top is large opening up hollow round table; The top of described urceolus 22 is straight tube, and bottom is large downward opening hollow round table; The hollow round table of the bottom of described inner core 21 is positioned at the below of the upper end open of described inner tube 6, the upper end open of described urceolus 22 is positioned at the top of the upper end open of described inner core 21, the upper end open of described inner core 21 is positioned at the top of the upper end open of described inner tube 6, the upper end open diameter (d of the hollow round table of the bottom of described inner core 21
4) be greater than the diameter (d of described inner tube 6
2), between the lower end of described inner core 21 and described urceolus 22 and the inwall of described housing 1, thering is gap, the lower ending opening of described urceolus 22 is positioned at the below of described liquid outlet 31; The upper end open of described urceolus 22 is positioned at the top of described liquid outlet 31, and is positioned at the below of the upper end open of described expanding reach 3.
For above-mentioned preferred fluidized bed reactor, its running can comprise:
The gas-liquid mixed raw material of question response enters reactor by charging aperture 1, together with the gas-liquid-solid mixture stream coming with down-comer (by direct tube section 5 and ring pipe that inner tube 6 forms) circulation after the gas-liquid distributor 7 at middle part, enter in inner tube 6, and mobile inner tube 6 in and on flowing to.Inner tube 6 and down-comer are reaction zone, and both Catalyst packing total amounts are at least 20% of reactor dischargeable capacity, are generally 40%-70%, and preferable range is 50%-60%.In the time of reactor stable operation, catalyst forms circulation in inner tube 6 and down-comer.Gas-liquid mixed raw material in inner tube 6 carries out catalytic reaction under the catalysis of solid catalyst, and reacted oil gas is being carried partially catalyzed agent solid particle secretly and entered three phase separation parts 2 from the upper end open of inner tube 6 and carry out gas-liquid-solid three-phase separation.First gas-liquid-solid mixture stream enter the first baffling district being made up of inner core 21 and inner tube 6, because logistics runs into the structure of sudden enlargement, logistics speed upwards reduces, partially liq is being carried most of solid catalyst and portion gas secretly, and to start baffling downward, and the annulus between inner core 21 and inner tube 6 enters described down-comer.Partially liq is being carried the upper end open that fraction solid catalyst and portion gas cover inner core 21 secretly and is being entered the second baffling district being made up of inner core 21 and urceolus 22, now the flow velocity of liquid is less, most of gas is because the effect of buoyancy is overflowed and in reactor head enrichment, with after discharge reactor through exhaust outlet 12, and liquid entrainment solid catalyst and fraction gas baffling is downward, enter the annulus between inner core 21 and urceolus 22, most of logistics enters down-comer by the gap between described inner core 21 and the inwall of described housing 1, fraction logistics enters by the gap between described urceolus 22 and the inwall of described housing 1 liquid collection region being made up of urceolus 22 and the inwall of housing 1, because liquid speed is herein much smaller than the critical liquid speed that makes solid fluidisation, so solid particle can not enter supernatant layer, in the liquid of therefore discharging by liquid outlet 31, substantially do not comprise solid particle.Fresh solid catalyst adds pipe 9 to add by the catalyst at housing 1 top, and the solid catalyst of inactivation is discharged by the catalyst discharge pipe 10 of housing 1 bottom, changes online thereby realize catalyst.
Can find out from architectural feature and the running of described fluidized bed reactor of the present invention, inner circulation fluidized at reactor under the promotion of solid catalyst density contrast in the kinetic energy of entrance material and reactor, energy consumption is lower.And in the time that described three phase separation parts 2 have above-mentioned more preferably structure, the double-deck three phase separation parts of this reactor have guaranteed the fluidized state of solid catalyst and the effect of three phase separation simultaneously.First, because the hole enlargement ratio that the first baffling district is set is little, liquid speed is also larger in this region, portion gas can be entrained in down-comer and go again, it is poor that this had both guaranteed to have gas holdup in tedge (being inner tube 6) and down-comer, in tedge and down-comer, has density contrast, can provide power for circulating of material, can also guarantee the to circulate nitrogen atmosphere of facing of down-comer, makes also can occur in down-comer sufficient catalytic reaction.Secondly, the existence in the second baffling district increases the operating flexibility of three phase separation parts greatly, on the one hand, the first baffling district can not separated to material completely here and again separates; On the other hand, also have the effect of buffering here, the larger material of flow velocity that can make first fold stream district separate cannot impact the supernatant layer in liquid collection region, even avoids catalyst solid to take reactor out of thereby can reduce.
As can be seen here, the described fluidized bed reactor of above-mentioned preferred embodiment has the following advantages:
(1) adopt in circulation type fluidized bed reactor, the circulation of material in reactor promoted jointly by the kinetic energy of entrance material and tedge (being inner tube 6) and the density contrast of down-comer, reduced energy consumption.Cancel circulating pump and the charge level monitor of complicated operation, simple to operate.And, compare with other existing fluidized bed reactors of same cancellation circulating pump, under identical energy consumption, this reactor can be supported higher catalyst concn, has improved the utilization ratio of reactor.
(2) three phase separation parts use two separate structure, and organically combine with reactor expanding reach and reactor content outlet (being exhaust outlet 12 and liquid outlet 31), improve the operating flexibility of three phase separation parts, guaranteed the required separating effect of circulation in ebullated bed: greatly reduce on the one hand catalyst taking-out amount simultaneously, can also allow on the other hand portion gas be recycled to annular space down-comer, guarantee the reaction efficiency in down-comer region.
(3) in fluidized bed reactor, except the gas enrichment region and liquid collection region of reactor head, other places in reactor are all the states that gas-liquid-solid three-phase coexists, greatly improve the utilization ratio of reactor, greatly reduced the generation of the heat scission reaction under non-hydrogen environment simultaneously.
(4) in fluidized bed reactor, the density contrast of tedge and down-comer can be used as regulating measure increases the operating flexibility of reactor, and flexible modulation catalyst particle size scope and catalyst concn as required, has strengthened the adaptability to different catalysts.The particle diameter that is applicable to the catalyst granules of described fluidized bed reactor of the present invention can be 0.1-1mm, is preferably 0.2-0.6mm.
The invention will be further described by the following examples.
The fluidized bed reactor using in following examples is the fluidized bed reactor in above-mentioned more preferably embodiment.
The concrete size of the fluidized bed reactor using in the present embodiment is as shown in table 1 below.
It is the spheric catalyst of 0.2-0.3mm that solid catalyst is selected particle diameter.Catalyst filling amount is 55% of reactor dischargeable capacity.Liquid phase is used virgin kerosene, and volume space velocity is 0.25-3h
-1.Gas phase is used nitrogen, and gas-oil ratio is 20-150.
The liquid of discharging by liquid outlet 31 is detected and learnt, the drag-out of solid catalyst is 2.1 μ g/g, and the drag-out of visible catalyst is extremely low.
And, making discovery from observation, down-comer also has sufficient recyclegas in (the ring pipe region being made up of inner tube 6 and direct tube section 5), and the fluidized state of solid catalyst is good.
Table 1
| Code name | Numerical value | Code name | Numerical value |
| d 1/mm | 400 | h 1/mm | 3200 |
| d 2/mm | 320 | h 2/mm | 160 |
| d 3/mm | 520 | h 3/mm | 600 |
| d 4/mm | 380 | h 4/mm | 3360 |
| d 5/mm | 660 | h 5/mm | 550 |
| d 6/mm | 440 | α/° | 45 |
| d 7/mm | 540 | β/° | 45 |
| d 8/mm | 620 | γ/° | 6 |
| d 9/mm | 720 | θ/° | 33 |
The concrete size of the fluidized bed reactor using in the present embodiment is as shown in table 2 below.
It is the spheric catalyst of 0.5-0.6mm that solid catalyst is selected particle diameter.Catalyst filling amount is 45% of reactor dischargeable capacity.Liquid phase is used virgin kerosene, and volume space velocity is 0.25-3h
-1.Gas phase is used nitrogen, and gas-oil ratio is 20-150.
The liquid of discharging by liquid outlet 31 is detected and learnt, the drag-out of solid catalyst is 1.6 μ g/g, and the drag-out of visible catalyst is extremely low.
And, making discovery from observation, down-comer also has sufficient recyclegas in (the ring pipe region being made up of inner tube 6 and direct tube section 5), and the fluidized state of solid catalyst is good.
Table 2
| Code name | Numerical value | Code name | Numerical value |
| d 1/mm | 300 | h 1/mm | 3600 |
| d 2/mm | 220 | h 2/mm | 87 |
| d 3/mm | 300 | h 3/mm | 500 |
| d 4/mm | 300 | h 4/mm | 3700 |
| d 5/mm | 540 | h 5/mm | 480 |
| d 6/mm | 340 | α/° | 60 |
| d 7/mm | 440 | β/° | 0 |
| d 8/mm | 540 | γ/° | 20 |
| d 9/mm | 600 | θ/° | 0 |
Can be found out by above-described embodiment 1 and 2, in larger catalyst particle size and inlet amount excursion, described fluidized bed reactor of the present invention can be supported the catalyst of high concentration, and catalyst fluidization is in good condition, and the drag-out of catalyst is lower, can meet industrial demand.
Below describe by reference to the accompanying drawings the preferred embodiment of the present invention in detail; but; the present invention is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition each the concrete technical characterictic described in the above-mentioned specific embodiment, in reconcilable situation, can combine by any suitable mode.For fear of unnecessary repetition, the present invention is to the explanation no longer separately of various possible combinations.
In addition, between various embodiment of the present invention, also can be combined, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (14)
1. a fluidized bed reactor, this fluidized bed reactor comprises housing (1) and three phase separation parts (2), described housing (1) comprises expanding reach (3) from top to bottom successively, changeover portion (4) and direct tube section (5), described three phase separation parts (2) are arranged in described expanding reach (3) and described changeover portion (4), on the sidewall of described expanding reach (3), be provided with liquid outlet (31), it is characterized in that, described fluidized bed reactor also comprises inner tube (6) and gas-liquid distributor (7), described inner tube (6) is arranged in described housing (1), and extend to the bottom of described expanding reach (3) from the bottom of described direct tube section (5), the lower ending opening of described inner tube (6) is communicated with described direct tube section (5), the upper end open of described inner tube (6) is communicated with described expanding reach (3), described three phase separation parts (2) are distributed in around the top of described inner tube (6), described gas-liquid distributor (7) is arranged in described direct tube section (5), and is positioned at the bottom of described inner tube (6).
2. fluidized bed reactor according to claim 1, wherein, more than the outlet of described gas-liquid distributor (7) is positioned at the lower ending opening of described inner tube (6).
3. fluidized bed reactor according to claim 1, wherein, the diameter ratio of the diameter of described inner tube (6) and described direct tube section (5) is 0.55-0.84:1.
4. fluidized bed reactor according to claim 1, wherein, the ratio of the height of the height of described inner tube (6) and described direct tube section (5) is 1-1.2:1.
5. fluidized bed reactor according to claim 1, wherein, described three phase separation parts (2) comprise inner core (21) and urceolus (22) from inside to outside successively, the bottom of described inner core (21) is large downward opening hollow round table, the hollow round table of the bottom of described inner core (21) is positioned at the below of the upper end open of described inner tube (6), the upper end open of described urceolus (22) is positioned at the top of the upper end open of described inner core (21), the upper end open of described inner core (21) is positioned at the top of the upper end open of described inner tube (6), the upper end open diameter of the hollow round table of the bottom of described inner core (21) is greater than the diameter of described inner tube (6), between the inwall of the lower end of described inner core (21) and described urceolus (22) and described housing (1), there is gap, the lower ending opening of described urceolus (22) is positioned at the below of described liquid outlet (31), the upper end open of described urceolus (22) is positioned at the top of described liquid outlet (31).
6. fluidized bed reactor according to claim 5, wherein, the upper end open diameter of the diameter of described inner tube (6), described inner core (21) and the upper end open diameter of described urceolus (22) increase successively.
7. fluidized bed reactor according to claim 5, wherein, the lower ending opening diameter of described urceolus (22) is greater than the lower ending opening diameter of described inner core (21).
8. fluidized bed reactor according to claim 5, wherein, the upper end open of described urceolus (22) is positioned at the below of the upper end open of described expanding reach (3).
9. according to the fluidized bed reactor described in any one in claim 1 and 5-8, wherein, the top of described inner core (21) is large opening up hollow round table.
10. fluidized bed reactor according to claim 9, wherein, the bus of hollow round table on the top of described inner core (21) and the angle of axis are for being greater than 0 ° to 45 °, and the bus of hollow round table of the bottom of described inner core (21) and the angle of axis are for being greater than 0 ° to 75 °.
11. according to the fluidized bed reactor described in any one in claim 1 and 5-8, and wherein, the top of described urceolus (22) is straight tube, and bottom is large downward opening hollow round table.
12. fluidized bed reactors according to claim 11, wherein, the upper end open of the hollow round table of the bottom of described urceolus (22) is positioned at the top of the upper end open of the hollow round table of the bottom of described inner core (21), and is positioned at the below of the upper end open of described inner core (21); The lower ending opening of the hollow round table of the bottom of described urceolus (22) is positioned at the top of the lower ending opening of the hollow round table of the bottom of described inner core (21).
13. fluidized bed reactors according to claim 11, wherein, the bus of hollow round table of the bottom of described urceolus (22) and the angle of axis are for being greater than 0 ° to 75 °.
14. fluidized bed reactors according to claim 1, wherein, the top of described housing (1) is provided with catalyst and adds pipe (9), and the bottom of described housing (1) is provided with catalyst discharge pipe (10).
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| CN105983377A (en) * | 2015-01-30 | 2016-10-05 | 中国科学院上海高等研究院 | Airlift internal loop slurry-bed reactor |
| CN110139918A (en) * | 2016-11-09 | 2019-08-16 | Ifp 新能源公司 | It will be used for the new equipment for being used for gas-liquid separation of such as three-phase fluid bed reactor of those used in the H-oil technique |
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