CN103769010B - A kind of fluidized bed reactor - Google Patents
A kind of fluidized bed reactor Download PDFInfo
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- CN103769010B CN103769010B CN201210401551.XA CN201210401551A CN103769010B CN 103769010 B CN103769010 B CN 103769010B CN 201210401551 A CN201210401551 A CN 201210401551A CN 103769010 B CN103769010 B CN 103769010B
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Abstract
A kind of fluidized bed reactor, comprise housing and three phase separation parts, housing comprises expanding reach, changeover portion and direct tube section from top to bottom successively, and three phase separation parts are arranged in expanding reach and changeover portion, and the sidewall of expanding reach is provided with liquid outlet, wherein, fluidized bed reactor also comprises interior pipe and gas-liquid distributor, and interior pipe is arranged in housing, and extends to the bottom of expanding reach from the bottom of direct tube section, the lower ending opening of interior pipe is communicated with direct tube section, and the upper end open of interior pipe is communicated with expanding reach; Three phase separation component distribution is in the top periphery of interior pipe; Gas-liquid distributor is arranged in direct tube section, and is positioned at the bottom of pipe.In this fluidized bed reactor, the circulation of material can be promoted by the density contrast of material in zones of different in the kinetic energy of entrance material and reactor completely, makes whole technics comparing energy-conservation; And the utilization ratio of reactor is higher, the generation of the heat scission reaction under non-hydrogen environment can be greatly reduced in heavy-oil hydrogenation cracking 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 kind of reactor has the following advantages: can process high tenor, the weight of high carbon residue, inferior raw material; Temperature of reactor is easily controlled and evenly, pressure drop is low and constant; Can add online and take out catalyst, therefore catalyst performance can keep constant in the whole operation cycle; Higher conversion ratio and longer operation cycle can be reached.
Existing industrialization boiling bed hydrogenation technology comprises H-Oil technique and LC-Fining technique etc., and being provided with circulation cup in the fluidized bed reactor of these two kinds of techniques carries out gas-liquid separation, and isolated oil product circulates through circulation down-comer and circulating pump.Existing boiling bed hydrogenation technique also exists following deficiency: (1) complex operation, need to use complicated charge level monitor and oil circulating pump, the stability of a system is poor, and when oil circulating pump breaks down, catalyst can, because of cannot fluidisation and 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 to realize by oil circulating pump; (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: the complexity reducing technique, improves the space availability ratio of reactor, reduces the operating flexibility etc. of energy consumption and raising reactor.Such as, CN1448212A discloses a kind of fluidized bed reactor, and this fluidized bed reactor eliminates complicated charge level monitor and oil circulating pump, therefore has the features such as structure is simple, 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 easily takes reactor out of, the operational stability of influential system.CN201529519U discloses a kind of fluidized bed reactor of external loop type, catalyst can 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 structure of this external loop reactor is higher to the requirement of material in actual production.
Summary of the invention
The object of the invention is the above-mentioned defect existed 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, the sidewall of described expanding reach is provided with liquid outlet, wherein, described fluidized bed reactor also comprises interior pipe and gas-liquid distributor, described interior pipe is arranged in described housing, and the bottom of described expanding reach is extended to from the bottom of described direct tube section, the lower ending opening of described interior pipe is communicated with described direct tube section, the upper end open of described interior pipe is communicated with described expanding reach, described three phase separation component distribution is in the top periphery of described interior pipe, described gas-liquid distributor is arranged in described direct tube section, and is positioned at the bottom of described pipe.
Preferably, the outlet of described gas-liquid distributor is positioned at more than the lower ending opening of described pipe.
Preferably, the diameter of described interior pipe 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 big uncork hollow round table down, the hollow round table of the bottom of described inner core is positioned at the below of the upper end open of described pipe, 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 pipe, the upper end open diameter of the hollow round table of the bottom of described inner core is greater than the diameter of described interior pipe, 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 big uncork of hollow round table is relative concept with " greatly " in little opening and " little ", the big uncork of hollow round table refers to one end that the opening diameter of hollow round table is larger, and the little opening of hollow round table refers to one end that the opening diameter of hollow round table is less.
More preferably, the upper end open diameter of the diameter of described interior pipe, the upper end open diameter of described inner core and described urceolus increases 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 big uncork hollow round table upward.
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 big uncork hollow round table down.
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 exit line.
In described fluidized bed reactor of the present invention, by arranging interior pipe in the direct tube section of housing, and make gas-liquid distributor be positioned at the bottom of described pipe, the circulation of material in reactor can be promoted by the density contrast of material in the kinetic energy of entrance material and tedge (managing namely) and down-comer (ring pipe be namely made up of interior pipe and direct tube section) completely jointly, thus circulating pump and the charge level monitor of complicated operation can be cancelled, make whole technique more energy-conservation, and operation is simpler.
And, in the running of described fluidized bed reactor of the present invention, be all the state that gas-liquid-solid three-phase coexists in tedge and down-comer, thus can react in tedge and down-comer, thus substantially increase the utilization ratio of reactor; And ensure that tedge and down-comer face nitrogen atmosphere, thus greatly reduce the generation of the heat scission reaction under non-hydrogen environment, thus the coking that produces due to the heat scission reaction of non-hydrogen atmosphere can be avoided.
Other features and advantages of the present invention are described in detail in detailed description of the invention part subsequently.
Accompanying drawing explanation
Accompanying drawing is 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 detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is the structural representation of the fluidized bed reactor according to the preferred embodiment of the present invention;
Fig. 2 is the parameter schematic diagram of the fluidized bed reactor according to 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
Pipe in 4 changeover portion 5 direct tube sections 6
7 gas-liquid distributor 9 catalyst add pipe 10 catalyst exit line
11 charging aperture 12 exhaust outlet 21 inner cores
22 urceolus 31 liquid outlets
Detailed description of the invention
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, detailed description of the invention described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
In the present invention, when not doing contrary explanation, the noun of locality such as " upper and lower " of use typically refers to reference to shown in the drawings upper and lower; " inside and outside " refers to profile inside and outside relative to 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, the sidewall of described expanding reach 3 is provided with liquid outlet 31, wherein, described fluidized bed reactor also comprises interior pipe 6 and gas-liquid distributor 7, described interior pipe 6 is arranged in described housing 1, and the bottom of described expanding reach 3 is extended to from the bottom of described direct tube section 5, the lower ending opening of described interior pipe 6 is communicated with described direct tube section 5, the upper end open of described interior pipe 6 is communicated with described expanding reach 3, described three phase separation parts 2 are distributed in the top periphery of described interior pipe 6, described gas-liquid distributor 7 is arranged in described direct tube section 5, and is positioned at the bottom of described pipe 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 relative to described direct tube section 5, and described expanding reach 3 is straight-tube shape usually 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 namely the diameter of the lower ending opening of described changeover portion 4 is substantially equal with the diameter of described direct tube section 5, and the diameter of the upper end open of described changeover portion 4 is substantially equal 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 its big uncork upward, 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, arrange described interior pipe 6 mainly in order to make reaction mass form outside circulation in reactor, therefore, there is no particular limitation for the size of described interior pipe 6, as long as can realize forming circulation.Under preferable case, the diameter (d of described interior pipe 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 interior pipe 6
4) with the height (h of described direct tube section 5
1) ratio can be 1-1.2:1.The top of described interior pipe 6 and the top of described housing 1 have gap, and the described bottom of interior pipe 6 and the bottom of described direct tube section 5 have 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 usually, and the gas-liquid mixture of question response is by described charging aperture 11 and enter in described fluidized bed reactor through described gas-liquid distributor 7.The top of described housing 1 is also provided with exhaust outlet 12 usually, 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, the outlet of described gas-liquid distributor 7 is preferably placed at more than the lower ending opening of described interior pipe 6.More preferably, the outlet of described gas-liquid distributor 7 is positioned at the top of the lower ending opening of described pipe 6, and also namely the outlet of gas-liquid distributor 7 is positioned at the inside of described pipe 6 completely.In this case, the gas-liquid mixture injected by described gas-liquid distributor 7 all can enter described interior pipe 6(also referred to as tedge), and in this tedge on flowing, thus be conducive to forming circulation between described interior pipe 6 and the endless tube (also referred to as down-comer) be made up of described direct tube section 5 and described interior pipe 6.
Described gas-liquid distributor 7 can for various routine can make gas and the uniform structure of liquid distribution, can be such as 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 carrying out gas-solid-liquid three phase separation by through the reacted material of described interior pipe 6, with the gas that reaction is produced and fluid separation applications out and discharge respectively by exhaust outlet 12 and liquid outlet 31, and the mixture through three phase separation is turned back in described interior pipe 6, to form circulation by down-comer (ring pipe be made up of described interior pipe 6 and described direct tube section 5).In the preferred case, in order to be reduced by the amount of the catalyst that liquid outlet 31 is taken out of, and impel further between described interior pipe 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 big uncork hollow round table down, the hollow round table of the bottom of described inner core 21 is positioned at the below of the upper end open of described pipe 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 pipe 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 interior pipe 6
2), have gap between the lower end of described inner core 21 and described urceolus 22 and the inwall of described housing 1, 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.
When described three phase separation parts 2 have above-mentioned preferred structure, between described inner core 21 and described interior pipe 6, form the first baffling district; Form the second baffling district between described inner core 21 and described urceolus 22, between described urceolus 22 and the inwall of described housing 1, form liquid collection region.In the running of described fluidized bed reactor, through the reacted gas-liquid-solid mixture of described interior pipe 6 in described interior pipe 6 on flowing, enter described first baffling district, because gas-liquid-solid mixture stream runs into the structure of sudden enlargement, this logistics speed upwards reduces, partially liq is then entrained with most of solid and portion gas starts baffling downwards, enters in described down-comer, partially liq is entrained with fraction solid and portion gas covers described interior pipe 21, enter described second baffling district, now the flow velocity of liquid is less, major part gas due to buoyancy effect effusion and in the top enrichment of reactor, and liquid entrainment solid and small portion of 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 is fast much smaller than making solids fluidized critical liquid speed herein, described solid particle can not enter supernatant layer, substantially solid particle is not comprised in the liquid of therefore being discharged by liquid outlet 31.And the logistics entering described first baffling district and described second baffling district is the mixture of gas-liquid-solid three-phase; And the logistics entered 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 is formed, the logistics at all the other positions is all exist with the form of the mixture of gas-liquid-solid three-phase, thus catalytic reaction can both occur.Therefore, when described three phase separation parts 2 have above-mentioned preferred structure, substantially catalyst solid can be avoided to be taken out of by liquid outlet 31, but also the utilization ratio of fluidized bed reactor can be improved further, greatly reduce the generation of the heat scission reaction under non-hydrogen environment simultaneously.
When described three phase separation parts 2 have above-mentioned preferred structure, preferably, described interior pipe 6, described inner core 21 and described urceolus 22 are all coaxially arranged with described housing 1.
Further preferably, the inlet area in described first baffling district and upper end open the area ratio ((d of described interior pipe 6
6 2-d
2 2)/d
2 2) be 0.3-1.5:1; The inlet area in described second baffling district and the ratio ((d of the inlet area in described 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 first baffling district.
When described three phase separation parts 2 have above-mentioned preferred structure, further preferably, the diameter (d of described interior pipe 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, advantageously realize being separated in the mixture of gas-liquid-solid three-phase by described three phase separation parts 2.
When 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.
When described three phase separation parts 2 have above-mentioned preferred structure, the top of described inner core 21 can be straight tube, also can be big uncork hollow round table upward.Under preferable case, the top of described inner core 21 is big uncork hollow round table upward.When the top of described inner core 21 is big uncork hollow round table upward, described inner core 21 is preferably made up of the big uncork hollow round table upward on top and the big uncork hollow round table down of bottom, and the lower ending opening of the hollow round table on top overlaps with the upper end open of the hollow round table of bottom.Further preferably, the position that the lower ending opening of the hollow round table on top overlaps with both upper end open of the hollow round table of bottom is positioned at the below of the upper end open of described pipe 6 and the lower ending opening of described expanding reach 3.
When the top of described inner core 21 is big uncork hollow round table upward, the bus of the hollow round table on the top of described inner core 21 and the angle (γ) of axis 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 (β) of axis can for being greater than 0 ° to 75 °.
When described three phase separation parts 2 have above-mentioned preferred structure, described urceolus 22 can be straight tube structure.When 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.
Even avoid solid particle to take out of from liquid outlet 31 to reduce as far as possible, described urceolus 22 has such preferred structure: the top of described urceolus 22 is straight tube, and bottom is big uncork hollow round table down.
When 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.
When 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 (θ) of axis are for being greater than 0 ° to 75 °.
In described fluidized bed reactor of the present invention, be preferably also provided with the system of online more catalyst changeout, add online to realize solid catalyst and take out function.The system of described more catalyst changeout can select any suitable equipment and method, such as can with reference to equipment disclosed in US4398852 and method.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, catalyst exit line 10 is set in the bottom of described housing 1.In this case, pipe 9 can be added by the catalyst of reactor head and add fresh solid catalyst, and the solid catalyst of inactivation can be discharged by the catalyst exit line 10 of reactor bottom.Described catalyst adds the degree of depth that pipe 9 stretches in described housing 1, and there is no particular limitation, under preferable case, the outlet that described catalyst adds pipe 9 is positioned at the top of the lower ending opening of described expanding reach 3, and the minimum range exporting to the lower ending opening of described expanding reach 3 that described catalyst adds pipe 9 is the height (h of described expanding reach 3
4) 40-95%, be preferably 60-90%.
In one more preferably 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, the sidewall of described expanding reach 3 is provided with liquid outlet 31, wherein, described fluidized bed reactor also comprises interior pipe 6 and gas-liquid distributor 7, described interior pipe 6 is arranged in described housing 1, and the bottom of described expanding reach 3 is extended to from the bottom of described direct tube section 5, the lower ending opening of described interior pipe 6 is communicated with described direct tube section 5, the upper end open of described interior pipe 6 is communicated with described expanding reach 3, described three phase separation parts 2 are distributed in the top periphery of described interior pipe 6, described gas-liquid distributor 7 is arranged in described direct tube section 5, and is positioned at the bottom of described pipe 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 big uncork hollow round table down, and top is big uncork hollow round table upward; The top of described urceolus 22 is straight tube, and bottom is big uncork hollow round table down; The hollow round table of the bottom of described inner core 21 is positioned at the below of the upper end open of described pipe 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 pipe 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 interior pipe 6
2), have gap between the lower end of described inner core 21 and described urceolus 22 and the inwall of described housing 1, 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, enter in interior pipe 6 together with the gas-liquid-solid mixture stream circulated with down-comer (ring pipe be namely made up of with interior pipe 6 direct tube section 5) after the gas-liquid distributor 7 at middle part, and flowing in interior pipe 6 and on flowing to.Interior pipe 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%.When reactor stable operation, catalyst forms circulation at interior pipe 6 and down-comer.Gas-liquid mixed raw material in interior pipe 6 carries out catalytic reaction under the catalysis of solid catalyst, and reacted oil gas is entrained with partially catalyzed agent solid particle and enters three phase separation parts 2 from the upper end open of interior pipe 6 and carry out gas-liquid-solid three-phase separation.First gas-liquid-solid mixture stream enter the first baffling district be made up of inner core 21 and interior pipe 6, because logistics runs into the structure of sudden enlargement, logistics speed upwards reduces, partially liq is entrained with most of solid catalyst and portion gas starts baffling downwards, enters described down-comer through the annulus between inner core 21 and interior pipe 6.Partially liq is entrained with the upper end open that fraction solid catalyst and portion gas cover inner core 21 and enters the second baffling district be made up of inner core 21 and urceolus 22, now the flow velocity of liquid is less, major part gas due to buoyancy effect effusion and in reactor head enrichment, with after discharge reactor through exhaust outlet 12, and liquid entrainment solid catalyst and small portion of gas baffling is downward, enter the annulus between inner core 21 and urceolus 22, major part logistics enters down-comer by the gap between described inner core 21 and the inwall of described housing 1, fraction logistics then enters the liquid collection region be made up of with the inwall of housing 1 urceolus 22 by the gap between described urceolus 22 and the inwall of described housing 1, because liquid is fast much smaller than making solids fluidized critical liquid speed herein, so solid particle can not enter supernatant layer, substantially solid particle is not comprised in the liquid of therefore being discharged by liquid outlet 31.Fresh solid catalyst adds pipe 9 by the catalyst at housing 1 top and adds, and the solid catalyst of inactivation is discharged by the catalyst exit line 10 bottom housing 1, thus realizes catalyst and change online.
As can be seen 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 and reactor of entrance material, energy consumption is lower.And when described three phase separation parts 2 have above-mentioned more preferably structure, the double-deck three phase separation parts of this reactor ensure that the fluidized state of solid catalyst and the effect of three phase separation simultaneously.First, expanding ratio set by the first baffling district is little, liquid speed is also larger in this region, portion gas can be entrained in down-comer again and go, this both ensure that in tedge (namely pipe 6) and down-comer to have gas holdup difference, namely had density contrast in tedge and down-comer, can provide power for circulating of material, what can also ensure circulation down-comer faces nitrogen atmosphere, makes also sufficient catalytic reaction can occur in down-comer.Secondly, the existence in the second baffling district makes the operating flexibility of three phase separation parts greatly increase, and on the one hand, the first baffling district can be separated material completely here and again be separated; On the other hand, also have the effect of buffering here, the material that the flow velocity that the first baffling district can be made to separate is larger cannot impact the supernatant layer in liquid collection region, thus can reduce and even avoid catalyst solid to take reactor out of.
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 is promoted jointly by the kinetic energy of entrance material and tedge (namely pipe 6) and the density contrast of down-comer, reduces energy consumption.Eliminate circulating pump and the charge level monitor of complicated operation, simple to operate.And compared with cancelling other existing fluidized bed reactors of circulating pump equally, under identical energy consumption, this reactor can support higher catalyst concn, improves the utilization ratio of reactor.
(2) three phase separation parts use two separate structure, and export (i.e. exhaust outlet 12 and liquid outlet 31) with reactor expanding reach and reactor content and organically combine, improve the operating flexibility of three phase separation parts, ensure that the separating effect in ebullated bed needed for circulation: greatly reduce catalyst taking-out amount on the one hand simultaneously, portion gas can also be allowed to be recycled to annular space down-comer on the other hand, ensure that the reaction efficiency in down-comer region.
(3) in fluidized bed reactor, except the gas enrichment region of reactor head and liquid collection region, other places in reactor are all the states that gas-liquid-solid three-phase coexists, substantially increase the utilization ratio of reactor, greatly reduce 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 increase the operating flexibility of reactor as regulating measure, can flexible modulation catalyst particle size scope and catalyst concn as required, enhances the adaptability to different catalysts.The particle diameter being 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 used in following examples is the fluidized bed reactor in above-mentioned more preferably embodiment.
Embodiment 1
The concrete size of the fluidized bed reactor used in the present embodiment is as shown in table 1 below.
Solid catalyst selects particle diameter to be the spheric catalyst of 0.2-0.3mm.Catalyst filling amount is 55% of reactor dischargeable capacity.Liquid phase uses virgin kerosene, and volume space velocity is 0.25-3h
-1.Gas phase uses nitrogen, and gas-oil ratio is 20-150.
Carry out detection to the liquid of being discharged by liquid outlet 31 to learn, the drag-out of solid catalyst is 2.1 μ g/g, and the drag-out of visible catalyst is extremely low.
And make discovery from observation, down-comer also has sufficient recyclegas in (the ring pipe region be namely made up of with direct tube section 5 interior pipe 6), 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 |
Embodiment 2
The concrete size of the fluidized bed reactor used in the present embodiment is as shown in table 2 below.
Solid catalyst selects particle diameter to be the spheric catalyst of 0.5-0.6mm.Catalyst filling amount is 45% of reactor dischargeable capacity.Liquid phase uses virgin kerosene, and volume space velocity is 0.25-3h
-1.Gas phase uses nitrogen, and gas-oil ratio is 20-150.
Carry out detection to the liquid of being discharged by liquid outlet 31 to learn, the drag-out of solid catalyst is 1.6 μ g/g, and the drag-out of visible catalyst is extremely low.
And make discovery from observation, down-comer also has sufficient recyclegas in (the ring pipe region be namely made up of with direct tube section 5 interior pipe 6), 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 |
As can be seen from above-described embodiment 1 and 2, in larger catalyst particle size and inlet amount excursion, described fluidized bed reactor of the present invention can support the catalyst of high concentration, and catalyst fluidization is in good condition, and the drag-out of catalyst is lower, industrial demand can be met.
Below the preferred embodiment of the present invention is described in detail by reference to the accompanying drawings; 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 characteristic described in above-mentioned detailed description of the invention, in reconcilable situation, can be combined by any suitable mode.In order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible combination.
In addition, also can be combined between various different embodiment of the present invention, 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 (13)
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), the sidewall of described expanding reach (3) is provided with liquid outlet (31), it is characterized in that, described fluidized bed reactor also comprises interior pipe (6) and gas-liquid distributor (7), described interior pipe (6) is arranged in described housing (1), and the bottom of described expanding reach (3) is extended to from the bottom of described direct tube section (5), the lower ending opening of described interior pipe (6) is communicated with described direct tube section (5), the upper end open of described interior pipe (6) is communicated with described expanding reach (3), described three phase separation parts (2) are distributed in the top periphery of described interior pipe (6), described gas-liquid distributor (7) is arranged in described direct tube section (5), and is positioned at the bottom of described pipe (6),
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 big uncork hollow round table down, the hollow round table of the bottom of described inner core (21) is positioned at the below of the upper end open of described pipe (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 pipe (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 interior pipe (6), between the lower end of described inner core (21) and described urceolus (22) and the inwall of 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).
2. fluidized bed reactor according to claim 1, wherein, the outlet of described gas-liquid distributor (7) is positioned at more than the lower ending opening of described pipe (6).
3. fluidized bed reactor according to claim 1, wherein, the diameter of described interior pipe (6) and the diameter ratio of described direct tube section (5) are 0.55-0.84:1.
4. fluidized bed reactor according to claim 1, wherein, the ratio of the height of described interior pipe (6) and the height of described direct tube section (5) is 1-1.2:1.
5. fluidized bed reactor according to claim 1, wherein, the upper end open diameter of the diameter of described interior pipe (6), the upper end open diameter of described inner core (21) and described urceolus (22) increases successively.
6. fluidized bed reactor according to claim 1, wherein, the lower ending opening diameter of described urceolus (22) is greater than the lower ending opening diameter of described inner core (21).
7. fluidized bed reactor according to claim 1, wherein, the upper end open of described urceolus (22) is positioned at the below of the upper end open of described expanding reach (3).
8. according to the fluidized bed reactor in claim 1 and 5-7 described in any one, wherein, the top of described inner core (21) is big uncork hollow round table upward.
9. fluidized bed reactor according to claim 8, 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 °.
10. according to the fluidized bed reactor in claim 1 and 5-7 described in any one, wherein, the top of described urceolus (22) is straight tube, and bottom is big uncork hollow round table down.
11. fluidized bed reactors according to claim 10, 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).
12. fluidized bed reactors according to claim 10, 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 °.
13. 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 exit line (10).
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| CN105983377B (en) * | 2015-01-30 | 2020-07-28 | 上海睿碳能源科技有限公司 | Air lift type internal circulation slurry bed reactor |
| CN105363392B (en) * | 2015-11-30 | 2017-12-01 | 华电重工股份有限公司 | A kind of interior circulation type fluidized bed reactor |
| FR3058421B1 (en) * | 2016-11-09 | 2020-07-24 | Ifp Energies Now | NEW LIQUID GAS SEPARATION DEVICE FOR EQUIPPING REACTORS WITH THREE-PHASE FLUIDIZED BEDS SUCH AS THOSE USED IN THE OIL PROCESS |
| CN111482146B (en) * | 2020-04-17 | 2022-02-22 | 中国石油化工股份有限公司 | Three-phase separator, three-phase reactor and three-phase reaction method |
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| CN101618305A (en) * | 2008-07-04 | 2010-01-06 | 中国石油化工股份有限公司 | Fluidized bed reactor |
| CN101759294A (en) * | 2009-12-29 | 2010-06-30 | 浙江大学 | Fluidized bed processing device of printing and dyeing waste water |
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| CN201969548U (en) * | 2011-01-24 | 2011-09-14 | 中国石油化工股份有限公司 | Internal circulating-flow slurry bed reactor |
| CN102463077A (en) * | 2010-11-05 | 2012-05-23 | 中国石油化工股份有限公司 | Three-phase boiling bed reactor |
| EP2492006A1 (en) * | 2009-10-21 | 2012-08-29 | China Petroleum & Chemical Corporation | Fluidized-bed reactor and hydrotreating method thereof |
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| CN101618305A (en) * | 2008-07-04 | 2010-01-06 | 中国石油化工股份有限公司 | Fluidized bed reactor |
| EP2492006A1 (en) * | 2009-10-21 | 2012-08-29 | China Petroleum & Chemical Corporation | Fluidized-bed reactor and hydrotreating method thereof |
| CN101759294A (en) * | 2009-12-29 | 2010-06-30 | 浙江大学 | Fluidized bed processing device of printing and dyeing waste water |
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