CN103769009A - Fluidized bed reactor - Google Patents
Fluidized bed reactor Download PDFInfo
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- CN103769009A CN103769009A CN201210400942.XA CN201210400942A CN103769009A CN 103769009 A CN103769009 A CN 103769009A CN 201210400942 A CN201210400942 A CN 201210400942A CN 103769009 A CN103769009 A CN 103769009A
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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 outer pipe and a gas-liquid distributer, wherein the upper end opening and the lower end opening of the outer pipe are respectively communicated with the upper opening and the lower opening on the side wall of the straight tube section, and the gas-liquid distributer is arranged on the bottom of the straight tube section. 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 external loop 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.
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 outer tube and gas-liquid distributor, the upper end open of described outer tube and lower ending opening are communicated with upper shed and under shed on the sidewall of described direct tube section respectively, described gas-liquid distributor is arranged at the bottom of described direct tube section.
Preferably, the outlet of described gas-liquid distributor is positioned at the below of the lower ending opening of described outer tube.
Preferably, the diameter of described outer tube and the diameter ratio of described direct tube section are 0.5-1:1.In the present invention, " diameter " typically refers to internal diameter.
Preferably, the angle of the direction of the upper end open of described outer tube and the axis of described direct tube section is 15-90 °, and the angle of the direction of the lower ending opening of described outer tube and the axis of described direct tube section is 15-90 °.
Preferably, described three phase separation parts are divided into the inner space of described expanding reach and described changeover portion the Disengagement zone, the first baffling district, the second baffling district and the liquid collection region that distribute successively from inside to outside, described Disengagement zone be positioned at described direct tube section directly over, between the bottom of described the first baffling district, described the second baffling district and described liquid collection region and described direct tube section, there is the communicating passage distributing along the sidewall of described housing; The top of described Disengagement zone is communicated with described the first baffling district, and the top in described the first baffling district is communicated with described the second baffling district, and described liquid outlet is positioned at described liquid collection region.
More preferably, described three phase separation parts comprise the inner core distributing successively from inside to outside, middle cylinder and urceolus, the bottom of described inner core and described middle cylinder is large downward opening hollow round table, the upper end open of described urceolus is arranged in the top of the upper end open of described cylinder, and the upper end open of described middle cylinder is positioned at the top of the upper end open of described inner core; The lower ending opening of described urceolus is arranged in the top of the lower ending opening of described cylinder, and the lower ending opening of described middle cylinder is positioned at the top of the lower ending opening of described inner core; Between described inner core, described middle cylinder and the lower end of described urceolus and the inwall of described housing, all have gap, wherein, the inwall of described inner core and the upper end open of described direct tube section form described Disengagement zone; The inwall of described middle cylinder and the outer wall of described inner core form described the first baffling district; The outer wall of the inwall of described urceolus and described middle cylinder forms described the second baffling district; The inwall of described housing and the outer wall of described urceolus form described liquid collection region.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.
Further preferably, the lower ending opening diameter of the diameter of described direct tube section, described inner core, the lower ending opening diameter of described middle cylinder and the lower ending opening diameter of described urceolus increase successively.
Further preferably, the upper end open diameter of described inner core, the upper end open diameter of described middle cylinder and the upper end open diameter of described urceolus increase successively.
Further preferably, described urceolus is straight tube.
Further preferably, the upper end open of described urceolus is positioned at the below of the upper end open of described expanding reach, and the lower ending opening of described urceolus is positioned at the below of the lower ending opening of described expanding reach.
Further preferably, the top of described inner core is large opening up hollow round table.
Still 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 30 °, 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 °.
Further preferably, the top of described middle cylinder is large opening up hollow round table.
Further preferably, the bus of hollow cylinder on the top of described middle cylinder and the angle of axis are for being greater than 0 ° to 45 °, and the bus of hollow cylinder of the bottom of described middle cylinder and the angle of axis are for being greater than 0 ° to 75 °.
Further preferably, the inlet area in described the first baffling district is 0.5-2:1 with the ratio of the upper end open area of described inner core.
Further preferably, the inlet area in described the second baffling district is 0.5-2:1 with the ratio of the inlet area in described the first baffling district.
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, sidepiece by the direct tube section at housing arranges outer tube, and the bottom at the direct tube section of reactor arranges gas-liquid distributor, the circulation of material in reactor and outer tube can be promoted jointly by the density contrast of material in the kinetic energy of entrance material and tedge (being direct tube section) and down-comer (being outer tube) 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 down-comer, be the state that gas-liquid-solid three-phase coexists, thereby still can react in down-comer, thereby greatly improved the utilization ratio of reactor; And guaranteed the nitrogen atmosphere of facing of 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.
Description of reference numerals
1 housing 2 three phase separation parts 3 expanding reach
4 changeover portion 5 direct tube section 6 outer tubes
7 gas-liquid distributor 9 catalyst add pipe 10 catalyst discharge pipes
11 charging aperture 12 exhaust outlet 21 inner cores
2-1 Disengagement zone 2-2 first baffling district 2-3 the second baffling district
2-4 liquid collection region
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 outer tube 6 and gas-liquid distributor 7, the upper end open of described outer tube 6 and lower ending opening are communicated with upper shed and under shed on the sidewall of described direct tube section 5 respectively, described gas-liquid distributor 7 is arranged at the bottom of described direct tube section 5.
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.The diameter of described direct tube section 5 is 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
11) 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
11) ratio be 0.6-2:1, 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 outer tube 6 in order to make reaction mass form outside circulation between described reactor and described outer tube 6 that described outer tube 6 is set, and forms outside circulation as long as can realize.Under preferable case, the diameter (d of described outer tube 6
2) with the diameter (d of described direct tube section 5
1) ratio be 0.5-1:1.
In the preferred case, for the ease of form outside circulation between described reactor and described outer tube 6, the upper end open of described outer tube 6 trends towards downward-sloping, and the lower ending opening of described outer tube 6 trends towards being inclined upwardly.There is no particular limitation for the shape of described outer tube 6, and for example, described outer tube 6 can be semicircular ring shape.In one, more preferably in embodiment, as illustrated in fig. 1 and 2, described outer tube 6 comprises three sections to the shape of described outer tube 6, and from the lower ending opening of outer tube 6 described in the upper end open road of described outer tube 6, is followed successively by tilting section, vertically section and tilting section.
More preferably, the angle (ω) of the axis of the direction of the upper end open of described outer tube 6 and described direct tube section 5 is 15-90 °, and more preferably 30 ° to being less than 75 °, more preferably 40-60 °.
More preferably, the angle (θ) of the axis of the direction of the lower ending opening of described outer tube 6 and described direct tube section 5 is 15-90 °, and more preferably 30 ° to being less than 75 °, more preferably 40-60 °.
In the preferred case, for the ease of form outside circulation between described reactor and described outer tube 6, the outlet of described gas-liquid distributor 7 is positioned at the below of the lower ending opening of described outer tube 6.Here, " outlet of described gas-liquid distributor 7 is positioned at the below of the lower ending opening of described outer tube 6 " refers to that the outlet of described gas-liquid distributor 7 is positioned at the below on the lower edge of the lower ending opening of described outer tube 6.Certainly, the below that the outlet of described gas-liquid distributor 7 is positioned at the lower ending opening of described outer tube 6 is completely more preferably, this is because impact the logistics from described outer tube 6 from the flow velocity logistics meeting faster of described gas-liquid distributor 7, thereby change fast the flow direction from the logistics of outer tube 6, it is moved upward, thereby can advantageously realize circulation.
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, 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.
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 direct tube section 5 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.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 direct tube section 5 and described outer tube 6 and successfully form circulation, as illustrated in fig. 1 and 2, described three phase separation parts 2 are divided into the inner space of described expanding reach 3 and described changeover portion 4 the Disengagement zone 2-1 distributing successively from inside to outside, the first baffling district 2-2, the second baffling district 2-3 and liquid collection region 2-4, described Disengagement zone 2-1 be positioned at described direct tube section 5 directly over, described the first baffling district 2-2, between the bottom of described the second baffling district 2-3 and described liquid collection region 2-4 and described direct tube section 5, there is the communicating passage distributing along the sidewall of described housing 1, the top of described Disengagement zone 2-1 is communicated with described the first baffling district 2-2, and the top of described the first baffling district 2-2 is communicated with described the second baffling district 2-3, and described liquid outlet 31 is positioned at described liquid collection region 2-4.
For the inner space of realizing just described expanding reach 3 and described changeover portion 4 is divided into Disengagement zone 2-1, the first baffling district 2-2, the second baffling district 2-3 and liquid collection region 2-4, the structure of described three phase separation parts 2 is preferably as follows: described three phase separation parts 2 comprise the inner core 21 distributing successively from inside to outside, middle cylinder 22 and urceolus 23, the bottom of described inner core 21 and described middle cylinder 22 is large downward opening hollow round table, the upper end open of described urceolus 23 is arranged in the top of the upper end open of described cylinder 22, the upper end open of described middle cylinder 22 is positioned at the top of the upper end open of described inner core 21, the lower ending opening of described urceolus 23 is arranged in the top of the lower ending opening of described cylinder 22, and the lower ending opening of described middle cylinder 22 is positioned at the top of the lower ending opening of described inner core 21, between described inner core 21, described middle cylinder 22 and the lower end of described urceolus 23 and the inwall of described housing 1, all have gap, wherein, the upper end open of the inwall of described inner core 21 and described direct tube section 5 forms described Disengagement zone 2-1, the inwall of described middle cylinder 22 and the outer wall of described inner core 21 form described the first baffling district 2-2, the outer wall of the inwall of described urceolus 23 and described middle cylinder 22 forms described the second baffling district 2-3, the outer wall of the inwall of described housing 1 and described urceolus 23 forms described liquid collection region 2-4.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, in the running of described fluidized bed reactor, enter described Disengagement zone 2-1 through the reacted gas-liquid-solid mixture of described direct tube section 5, because gas-liquid-solid mixture stream runs into the structure of sudden enlargement, this logistics speed upwards reduces, liquid entrainment most of solid and portion gas, and to start baffling downward, enters described the first baffling district 2-2, then turns back to direct tube section 5 along the communicating passage of the sidewall of described housing 1; Partially liq is being carried the upper end open that fraction solid and portion gas cover middle cylinder 22 secretly and is being entered described the second baffling district 2-3, now the flow velocity of liquid is less, most of gas is overflowed and is enriched in the top of housing 1 under the effect of buoyancy, discharge through exhaust outlet 12 subsequently, for the mixing logistics (liquid entrainment solid and fraction gas) that enters described the second baffling district 2-3, the communicating passage of most of sidewall along described housing 1 turns back to direct tube section 5, and fraction liquid enters described liquid collection region 2-4.In described liquid collection region 2-4, because liquid speed is much smaller than the critical liquid speed of solid fluidisation, described solid particle can not enter supernatant layer, does not substantially comprise solid particle in the liquid of therefore discharging by liquid outlet 31.And the logistics that enters described Disengagement zone 2-1, described the first baffling district 2-1 and described the second baffling district 2-3 is the mixture of gas-liquid-solid three-phase; And the logistics entering in described urceolus 6 by the upper shed on the sidewall of described direct tube section 5 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 2-4 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 core 21, described middle cylinder 22 and described urceolus 23 all coaxially arrange with described housing 1.
Further preferably, the diameter (d of described direct tube section 5
1), the lower ending opening diameter (d of described inner core 21
3), the lower ending opening diameter (d of described middle cylinder 22
4) and the lower ending opening diameter (d of described urceolus 23
10) increase successively.
Further preferably, the upper end open diameter (d of described inner core 21
7), the upper end open diameter (d of described middle cylinder 22
9) and the upper end open diameter of described urceolus 23 increase successively (d
10).
In the time that described three phase separation parts 2 have above-mentioned preferred structure, there is no particular limitation for the shape of described urceolus 23, and for example, described urceolus 23 can be made up of the large downward opening hollow round table of the straight tube on top and bottom.In one embodiment, as illustrated in fig. 1 and 2, described urceolus 23 is straight tube.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, preferably, the upper end open of described urceolus 23 is positioned at the below of the upper end open of described expanding reach 3, and the lower ending opening of described urceolus 23 is positioned at the below of the lower ending opening of described expanding reach 3.Further preferably, the upper end open of described urceolus 23 is positioned at the top of described liquid outlet 31, to guarantee that liquid in described liquid collection region 2-4 can not overflow across described urceolus 23 and enter described the second baffling district 2-3.Height (the h of described urceolus 23
4) with the height (h of described expanding reach 3
3) ratio can be 0.8-1.2:1.
As described liquid outlet 31, it is preferably near the top of described expanding reach 3, and more preferably, the central axis of described liquid outlet 31 accounts for the height (h of described expanding reach 3 to the minimum range of the lower ending opening of described expanding reach 3
3) 60-90%.
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, and 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, the bus of the hollow round table on the top of described inner core 21 and the angle of axis can be for being greater than 0 ° to 30 °.The bus of the hollow round table of the bottom of described inner core 21 and the angle of axis can be for being greater than 0 ° to 75 °.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, the top of described middle cylinder 22 can be straight tube, can be also large opening up hollow round table, and under preferable case, the top of described middle cylinder 22 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, the bus of hollow cylinder and the angle of axis on the top of described middle cylinder 22 can be for being greater than 0 ° to 45 °.The bus of hollow cylinder and the angle of axis of the bottom of described middle cylinder 22 can be for being greater than 0 ° to 75 °.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, preferably, the ratio ((d of described the first inlet area of baffling district 2-2 and the upper end open area of described inner core 21
8 2-d
7 2)/d
7 2) be 0.5-2:1, wherein, d
7for the upper end open diameter of described inner core 21, d
8for the inlet diameter of described the first baffling district 2-2.
In the time that described three phase separation parts 2 have above-mentioned preferred structure, preferably, the ratio ((d of the inlet area of described the second baffling district 2-3 and the inlet area of described the first baffling district 2-2
10 2-d
9 2)/(d
8 2-d
7 2)) be 0.5-2:1, wherein, d
9for the upper end open diameter of described middle cylinder 22, d
10for the inlet diameter of described the second baffling district 2-2.
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, wherein, described fluidized bed reactor also comprises outer tube 6 and gas-liquid distributor 7, the upper end open of described outer tube 6 and lower ending opening are communicated with upper shed and under shed on the sidewall of described direct tube section 5 respectively, described gas-liquid distributor 7 is arranged at the bottom of described direct tube section 5,
Described three phase separation parts 2 comprise the inner core 21 distributing successively from inside to outside, middle cylinder 22 and urceolus 23, the bottom of described inner core 21 and described middle cylinder 22 is large downward opening hollow round table, the top of described inner core 21 and described middle cylinder 22 is large opening up hollow round table, the upper end open of described urceolus 23 is arranged in the top of the upper end open of described cylinder 22, and the upper end open of described middle cylinder 22 is positioned at the top of the upper end open of described inner core 21; The lower ending opening of described urceolus 23 is arranged in the top of the lower ending opening of described cylinder 22, and the lower ending opening of described middle cylinder 22 is positioned at the top of the lower ending opening of described inner core 21; Between described inner core 21, described middle cylinder 22 and the lower end of described urceolus 23 and the inwall of described housing 1, all have gap, wherein, the upper end open of the inwall of described inner core 21 and described direct tube section 5 forms described Disengagement zone 2-1; The inwall of described middle cylinder 22 and the outer wall of described inner core 21 form described the first baffling district 2-2; The outer wall of the inwall of described urceolus 23 and described middle cylinder 22 forms described the second baffling district 2-3; The outer wall of the inwall of described housing 1 and described urceolus 23 forms described liquid collection region 2-4;
Described urceolus 23 is straight tube, the diameter of described direct tube section 5, the lower ending opening diameter of described inner core 21, the lower ending opening diameter of described middle cylinder 22 and the lower ending opening diameter of described urceolus 23 increase successively, and the upper end open diameter of described inner core 21, the upper end open diameter of described middle cylinder 22 and the upper end open diameter of described urceolus 23 increase successively;
On the sidewall of described expanding reach 3, be provided with liquid outlet 31, and described liquid outlet 31 is positioned at the below of the upper end open of described urceolus 23;
The upper end open of described urceolus 23 is positioned at the below of the upper end open of described expanding reach 3, and the lower ending opening of described urceolus 23 is positioned at the below of the lower ending opening 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 11, together with the gas-liquid-solid mixture coming flows, enters in direct tube section 5 and upwards and flows after gas-liquid distributor 7 with outer tube 6 circulations.Direct tube section 5 and outer tube 6 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 at direct tube section 5 and outer tube 6, makes catalyst be covered with whole conversion zone, and therefore the utilization ratio of reactor is higher.Gas-liquid raw material in direct tube section 5 carries out catalytic reaction under the catalysis of solid catalyst, reacted part gas-liquid-solid mixture enters in outer tube 6 and loops back reactor inlet, and part gas-liquid-solid mixture enters three phase separation parts 2 and carries out gas-liquid-solid three-phase separation from the top of direct tube section 5.First gas-liquid-solid mixture enters described Disengagement zone 2-1, because logistics runs into the structure of sudden enlargement, logistics speed upwards reduces, liquid entrainment most of solid and portion gas, and to start baffling downward, enter described the first baffling district 2-2, then turn back to direct tube section 5 along the communicating passage of the sidewall of described housing 1; Partially liq is being carried the upper end open that fraction solid and portion gas cover middle cylinder 22 secretly and is being entered described the second baffling district 2-3, now the flow velocity of liquid is less, most of gas is overflowed and is enriched in the top of housing 1 under the effect of buoyancy, discharge through exhaust outlet 12 subsequently, for the mixing logistics (liquid entrainment solid and fraction gas) that enters described the second baffling district 2-3, the communicating passage of most of sidewall along described housing 1 turns back to direct tube section 5, and fraction liquid enters described liquid collection region 2-4.In described liquid collection region 2-4, because liquid speed is much smaller than the critical liquid speed of 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.Owing to also there being gas to exist in outer tube 6, make, in outer tube 6, sufficient catalytic reaction also to occur, so this reactor has higher utilization ratio.And, in described fluidized bed reactor, in the time that described three phase separation parts 2 have above-mentioned more preferably structure, the operating flexibility of three phase separation has increased greatly, on the one hand, can again separate not separating material completely in described the first baffling district 2-2; On the other hand, described the second baffling district 2-3 has the effect of buffering, the larger material of flow velocity of separating through described the first baffling district 2-2 cannot be impacted the liquid of liquid collection region 2-4, even avoid solid catalyst 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 external loop type fluidized bed reactor, the circulation of material in reactor promoted jointly by the kinetic energy of entrance material and the density contrast of tedge (being direct tube section 5) and down-comer (being outer tube 6), 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), greatly reduce catalyst taking-out amount, improved the operating flexibility of three phase separation parts.
(3) adopt external loop type 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) adopt external loop type fluidized bed reactor, the density contrast of tedge (being direct tube section 5) and down-comer (being outer tube 6) can be used as regulating measure increases the operating flexibility of reactor, 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.
D
5for the top hollow round table of described inner core 21 and the opening diameter of lower hollow round platform overlapping position, d
6for the top hollow round table of described middle cylinder 22 and the opening diameter of lower hollow round platform overlapping position.
Embodiment 1
The concrete size of the fluidized bed reactor using in the present embodiment is as shown in table 1 below.
Table 1
| Code name | Numerical value | Code name | Numerical value |
| d 1/mm | 400 | h 1/mm | 3200 |
| d 2/mm | 350 | h 2/mm | 160 |
| d 3/mm | 410 | h 3/mm | 600 |
| d 4/mm | 480 | h 4/mm | 630 |
| d 5/mm | 220 | α/° | 45 |
| d 6/mm | 400 | β/° | 60 |
| d 7/mm | 350 | γ/° | 20 |
| d 8/mm | 450 | ε/° | 60 |
| d 9/mm | 540 | φ/° | 20 |
| d 10/mm | 620 | ω/° | 60 |
| d 11/mm | 720 | θ/° | 60 |
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 2.0 μ g/g, and the drag-out of visible catalyst is extremely low.
And, make discovery from observation, in outer tube 6, also there is sufficient recyclegas, the fluidized state of solid catalyst is good.
Embodiment 2
The concrete size of the fluidized bed reactor using in the present embodiment is as shown in table 2 below.
Table 2
| Code name | Numerical value | Code name | Numerical value |
| d 1/mm | 300 | h 1/mm | 3600 |
| d 2/mm | 240 | h 2/mm | 87 |
| d 3/mm | 310 | h 3/mm | 500 |
| d 4/mm | 400 | h 4/mm | 520 |
| d 5/mm | 240 | α/° | 60 |
| d 6/mm | 300 | β/° | 45 |
| d 7/mm | 240 | γ/° | 0 |
| d 8/mm | 350 | ε/° | 45 |
| d 9/mm | 440 | φ/° | 15 |
| d 10/mm | 540 | ω/° | 45 |
| d 11/mm | 600 | θ/° | 45 |
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 1.5 μ g/g, and the drag-out of visible catalyst is extremely low.
And, make discovery from observation, in outer tube 6, also there is sufficient recyclegas, the fluidized state of solid catalyst is good.
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 (17)
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 outer tube (6) and gas-liquid distributor (7), the upper end open of described outer tube (6) and lower ending opening are communicated with upper shed and under shed on the sidewall of described direct tube section (5) respectively, described gas-liquid distributor (7) is arranged at the bottom of described direct tube section (5).
2. fluidized bed reactor according to claim 1, wherein, the outlet of described gas-liquid distributor (7) is positioned at the below of the lower ending opening of described outer tube (6).
3. fluidized bed reactor according to claim 1, wherein, the diameter ratio of the diameter of described outer tube (6) and described direct tube section (5) is 0.5-1:1.
4. according to the fluidized bed reactor described in claim 1 or 3, wherein, the angle of the axis of the direction of the upper end open of described outer tube (6) and described direct tube section (5) is 15-90 °, and the angle of the axis of the direction of the lower ending opening of described outer tube (6) and described direct tube section (5) is 15-90 °.
5. fluidized bed reactor according to claim 1, wherein, described three phase separation parts (2) are divided into the inner space of described expanding reach (3) and described changeover portion (4) Disengagement zone (2-1) distributing successively from inside to outside, the first baffling district (2-2), the second baffling district (2-3) and liquid collection region (2-4), described Disengagement zone (2-1) be positioned at described direct tube section (5) directly over, described the first baffling district (2-2), between the bottom of described the second baffling district (2-3) and described liquid collection region (2-4) and described direct tube section (5), there is the communicating passage distributing along the sidewall of described housing (1), the top of described Disengagement zone (2-1) is communicated with described the first baffling district (2-2), and the top in described the first baffling district (2-2) is communicated with described the second baffling district (2-3), and described liquid outlet (31) is positioned at described liquid collection region (2-4).
6. fluidized bed reactor according to claim 5, wherein, described three phase separation parts (2) comprise the inner core (21) distributing successively from inside to outside, middle cylinder (22) and urceolus (23), the bottom of described inner core (21) and described middle cylinder (22) is large downward opening hollow round table, the upper end open of described urceolus (23) is arranged in the top of the upper end open of described cylinder (22), and the upper end open of described middle cylinder (22) is positioned at the top of the upper end open of described inner core (21); The lower ending opening of described urceolus (23) is arranged in the top of the lower ending opening of described cylinder (22), and the lower ending opening of described middle cylinder (22) is positioned at the top of the lower ending opening of described inner core (21); Between described inner core (21), described middle cylinder (22) and the lower end of described urceolus (23) and the inwall of described housing (1), all there is gap, wherein, the upper end open of the inwall of described inner core (21) and described direct tube section (5) forms described Disengagement zone (2-1); The described middle cylinder inwall of (22) and the outer wall of described inner core (21) form described the first baffling district (2-2); The outer wall of the inwall of described urceolus (23) and described middle cylinder (22) forms described the second baffling district (2-3); The outer wall of the inwall of described housing (1) and described urceolus (23) forms described liquid collection region (2-4).
7. fluidized bed reactor according to claim 6, wherein, the lower ending opening diameter of the diameter of described direct tube section (5), described inner core (21), the described middle cylinder lower ending opening diameter of (22) and the lower ending opening diameter of described urceolus (23) increase successively.
8. fluidized bed reactor according to claim 6, wherein, the upper end open diameter of described inner core (21), the described middle cylinder upper end open diameter of (22) and the upper end open diameter of described urceolus (23) increase successively.
9. according to the fluidized bed reactor described in any one in claim 6-8, wherein, described urceolus (23) is straight tube.
10. according to the fluidized bed reactor described in any one in claim 6-8, wherein, the upper end open of described urceolus (23) is positioned at the below of the upper end open of described expanding reach (3), and the lower ending opening of described urceolus (23) is positioned at the below of the lower ending opening of described expanding reach (3).
11. according to the fluidized bed reactor described in any one in claim 6-8, and wherein, the top of described inner core (21) is large opening up hollow round table.
12. fluidized bed reactors according to claim 11, 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 30 °, 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 °.
13. according to the fluidized bed reactor described in any one in claim 6-8, and wherein, the top of described middle cylinder (22) is large opening up hollow round table.
14. fluidized bed reactors according to claim 13, wherein, the bus of hollow cylinder on the top of described middle cylinder (22) and the angle of axis are for being greater than 0 ° to 45 °, and the bus of hollow cylinder of the bottom of described middle cylinder (22) and the angle of axis are for being greater than 0 ° to 75 °.
15. according to the fluidized bed reactor described in any one in claim 5-8, and wherein, the ratio of the upper end open area of the inlet area in described the first baffling district (2-2) and described inner core (22) is 0.5-2:1.
16. according to the fluidized bed reactor described in any one in claim 5-8, and wherein, the ratio of the inlet area in the inlet area in described the second baffling district (2-3) and described the first baffling district (2-2) is 0.5-2:1.
17. 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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