CN105363392A - Internal-loop fluidized bed reactor - Google Patents
Internal-loop fluidized bed reactor Download PDFInfo
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- CN105363392A CN105363392A CN201510856974.4A CN201510856974A CN105363392A CN 105363392 A CN105363392 A CN 105363392A CN 201510856974 A CN201510856974 A CN 201510856974A CN 105363392 A CN105363392 A CN 105363392A
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- 238000005191 phase separation Methods 0.000 claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 30
- 239000000463 material Substances 0.000 claims abstract description 19
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 238000009826 distribution Methods 0.000 claims abstract description 15
- 238000000926 separation method Methods 0.000 claims abstract description 5
- 239000003054 catalyst Substances 0.000 claims description 50
- 239000012071 phase Substances 0.000 claims description 10
- 239000007791 liquid phase Substances 0.000 claims description 7
- 239000002245 particle Substances 0.000 claims description 7
- 238000004140 cleaning Methods 0.000 claims description 5
- 230000000903 blocking effect Effects 0.000 claims description 4
- 239000006228 supernatant Substances 0.000 claims description 4
- 238000000034 method Methods 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 5
- 230000008569 process Effects 0.000 abstract description 2
- 230000003139 buffering effect Effects 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 33
- 239000002994 raw material Substances 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 238000004939 coking Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000011949 solid catalyst Substances 0.000 description 2
- WURBVZBTWMNKQT-UHFFFAOYSA-N 1-(4-chlorophenoxy)-3,3-dimethyl-1-(1,2,4-triazol-1-yl)butan-2-one Chemical compound C1=NC=NN1C(C(=O)C(C)(C)C)OC1=CC=C(Cl)C=C1 WURBVZBTWMNKQT-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
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- 238000009835 boiling Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000009527 percussion Methods 0.000 description 1
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- 238000000197 pyrolysis Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000008247 solid mixture Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention discloses an internal-loop fluidized bed reactor which comprises a housing, wherein the housing comprises a three-phase separation section and a reaction section from top to bottom; the reactor further comprises a three-phase separation part which is arranged in the three-phase separation section; a guide cylinder is arranged in the reaction section; a gas uniform distributing device is arranged below the lower opening of the guide cylinder, at least one material distributor is arranged in the guide cylinder above the gas uniform distributing device, and a plurality of baffle plates are arranged on the outer wall of the upper opening of the guide cylinder; the reactor further comprises a baffle arranged above a guide structure. The reactor further comprises a plurality of gas separation tubes connected with the guide structure. The reactor generates a directional loop inside, so that a process is energy-saving; a fresh material and circulation oil are fed in different regions, so that the loop mode is strengthened; oil-gas mixing and gas-liquid distribution are strengthened, and meanwhile, gas disturbance can effectively avoid generation of a dead zone in the bottom of the reactor, and can play a buffering role so as to reduce the impact effect on a distributing plate.
Description
Technical field
The invention belongs to fluidized bed reactor preparation field, be specifically related to a kind of interior circulation type fluidized bed reactor.
Background technology
Fluidized bed reactor is gas-liquid-solid three-phase fluid bed reactor, is applied to hydrogenation reaction and has lot of advantages: the weight, the inferior raw material that can be applicable to high, the high carbon residue of tenor; Evenly and easily control, pressure reduces and constant reactor temperature; Catalyst can be loaded and unloaded online, keep catalyst performance stabilised, course of reaction serialization can be made; Longer operation cycle and higher conversion ratio etc. can be realized.
Existing industrialization boiling bed hydrogenation technology mainly comprises H-Oil technique and LC-Fining technique, in above-mentioned two kinds of techniques, in fluidized bed reactor, arrange circulation cup to carry out gas-liquid separation, the oil product separated circulates through circulation down-comer and circulating pump.In above-mentioned technique: need to arrange oil circulating pump, when oil circulating pump breaks down, catalyst cannot fluidisation, complex operation, and the stability of a system is poor; The fluidisation of catalyst is squeezed into a large amount of recycle oil to realize by oil circulating pump, and energy consumption is large; In circulation down-comer, hydrogen is little, and liquid second pyrolysis at high temperature can occur and causes coking, and product quality also can reduce.
For above-mentioned the deficiencies in the prior art, the improvement direction at present for fluidized bed reactor mainly comprises: the complexity reducing technique, improves the space availability ratio of reactor, reduces energy consumption and improves the operating flexibility etc. of reactor.Such as Chinese patent literature CN101376092A and CN103769010A respectively disclose a kind of fluidized bed reactor, all eliminate complicated charge level monitor and oil circulating pump, therefore there is the advantages such as structure is simple, processing ease, but above-mentioned patent document all comes with some shortcomings.Such as fluidized bed reactor disclosed in Chinese patent literature CN101376092A, in three phase separator bottom, adjacent arranges a guide frame, guide frame is the annular protrusion structure being arranged at reactor wall, guide frame is trapezoidal or arc along the longitudinal section of reactor axis, due to the setting of guide frame, make below three phase separation parts, to define a reaction contraction section, reduce the space availability ratio of inside reactor, affect the production efficiency of reactor; In addition, the catalyst dirty through feed opening and liquid reaction raw material may the up liquid of catalyzed dose of bed directly with uplink cycle, cannot realize, at whole reactor Inner eycle, affecting reaction effect.Such as fluidized bed reactor disclosed in Chinese patent literature CN103769010A, its housing is made up of direct tube section, changeover portion and expanding reach, there is the problem of manufacturing cost increase, processing difficulties; In addition, the corner area that its inside and outside cylinder and changeover portion inwall are formed easily forms dead band, causes coking, and is unfavorable for Matter Transfer in reactor, causes Inner eycle weak effect, and reaction not exclusively.
Summary of the invention
Therefore, the technical problem to be solved in the present invention is to overcome that fluidized bed reactor of the prior art exists processing difficulties, manufacturing cost is high and there is dead band in reactor, the defect of Inner eycle weak effect, thus a kind of easy processing is provided, directed circulation is stablized, cyclic hardening, minimizing dead band interior circulation type fluidized bed reactor.
For this reason, technical scheme of the present invention is as follows:
Circulation type fluidized bed reactor in a kind of, comprising:
Housing, in straight tube shape, described housing comprises three phase separation section and conversion zone from top to bottom successively, the sidewall of described three phase separation section is provided with liquid flooding mouth, the top of described housing is provided with exhaust outlet, bottom is provided with liquid phase feeding mouth and gas phase charging aperture, described housing is also provided with at least one catalyst and adds pipe and at least one catalyst exit line;
Guide shell, is arranged in described housing, and extends to the bottom of described conversion zone from the bottom of described three phase separation section;
Three phase separation parts, are arranged in described three phase separation section;
Described three phase separation parts comprise guide frame and baffle plate, described guide frame has the conically shaped of radian to connect and compose by a center drum and one, and described center drum is located at the upper end open place of described guide shell and is extended downward certain distance in described guide shell from described upper end open; The upper end of described conically shaped is connected with center drum upper end, the lower end of described conically shaped is that umbrella extends towards the outer side-lower of described guide shell with the outer wall exceeding described guide shell, and the annular region that the inwall of described conically shaped and the outer wall of described guide shell are formed forms the first baffling district of three phase separation section; Space between the outer wall of described conically shaped and the inwall of described housing forms the second baffling district of three phase separation section; Described baffle plate is arranged at certain altitude position above described guide frame, and the space between described baffle plate and described guide frame forms the 3rd baffling district of three phase separation section.
In above-mentioned interior circulation type fluidized bed reactor, the outer wall of the upper end open of described guide shell is provided with several deflection plates corresponding with the lower end inner wall of described conically shaped.
In above-mentioned interior circulation type fluidized bed reactor, described three phase separation parts also comprise some gas separaion pipes, the lower ending opening of described some gas separaion pipes is positioned at the top of the conically shaped of described guide frame, and the upper end open of described some gas separaion pipes is between described case top and described baffle plate.
In above-mentioned interior circulation type fluidized bed reactor, the gross area of the lower ending opening of described some gas separaion pipes is 10% ~ 50% of the cross-sectional area of the annular region be made up of the center drum outer wall of described guide frame and described guide shell outer wall.
In above-mentioned interior circulation type fluidized bed reactor, described liquid flooding mouth tilts upward setting, and itself and the axial angle of housing are 5-45 °.
In above-mentioned interior circulation type fluidized bed reactor, described three phase separation parts also comprise overflow surge tank, described overflow surge tank has liquid outlet and catalyst return port, described overflow surge tank is connected with described housing by described liquid flooding mouth, described overflow surge tank is rotary filter press structure, supernatant liquid after separation is discharged from described liquid outlet, and the catalyst taken out of is returned in described housing by the described catalyst return port of bottom.
In above-mentioned interior circulation type fluidized bed reactor, described overflow surge tank is provided with for rinsing deposited particles in order to avoid the cleaning hose of described catalyst return port blocking.
In above-mentioned interior circulation type fluidized bed reactor, described guide shell and described housing are coaxially arranged, and the diameter of described guide shell is 0.6 ~ 0.8 times of described diameter of the housing.
In above-mentioned interior circulation type fluidized bed reactor, described center drum diameter is 0.65 ~ 0.85 times of draft tube diameter, and the lower ending opening diameter of described conically shaped is 0.75 ~ 0.9 times of diameter of the housing.
In above-mentioned interior circulation type fluidized bed reactor, described baffle plate is beveled structure, and it is 1 ~ 1.2 times of draft tube diameter at the projection diameter of a circle of horizontal section.
In above-mentioned interior circulation type fluidized bed reactor, at least one catalyst described adds the top that pipe is positioned at described annular region, and at least one catalyst described adds the barrel of lower ending opening through described conically shaped of pipe, and at least one catalyst exit line described is located at the bottom of described housing.
In above-mentioned interior circulation type fluidized bed reactor, also comprise the even gas distribution device of the bottom being located at guide shell lower ending opening, described even gas distribution device is connected with described gas-phase feed mouth.
In above-mentioned interior circulation type fluidized bed reactor, described even gas distribution device is gas sparging dish, and the outlet of described gas sparging dish is downward.
In above-mentioned interior circulation type fluidized bed reactor, also comprise at least one the material distributor be arranged in described guide shell, above even gas distribution device.
In above-mentioned interior circulation type fluidized bed reactor, described material distributor is the foraminate circular flat board of distribution, and described circular platen area and the ratio of the cross-sectional area of guide shell are 0.8 ~ 1, and described circular dull and stereotyped percent opening is 0.2 ~ 0.7.
In above-mentioned interior circulation type fluidized bed reactor, the diameter being positioned at the aperture of circular dull and stereotyped central area is less than the diameter of the aperture away from central area.
In above-mentioned interior circulation type fluidized bed reactor, also comprise some recycle oil feed pipes that the tangential direction along place housing circumference is arranged.
In above-mentioned interior circulation type fluidized bed reactor, described some recycle oil feed pipes on the housing setting position lower than the upper end open position of described guide shell.
Technical scheme of the present invention, tool has the following advantages:
1, interior circulation type fluidized bed reactor of the present invention, in reactor, directed circulation is created by guide shell, baffle plate, guide frame, the circulation of material in reactor can be promoted by the density contrast of material in the kinetic energy of entrance material and tedge (i.e. guide shell) and down-comer (ring pipe be namely made up of housing and guide shell) completely jointly, makes whole technique more energy-conservation; Under the interaction of guide frame and guide shell, form the first baffling district, strengthen heat transfer and the mixing of directed circulation flowing in reactor and mass transfer, make reactor temperature even, reduce coking; Guide frame is baffling pattern, the second baffling district between guide frame and the inwall of housing, forms air cavity air guide, makes center flow to surrounding and is diffused as overflow form and, is convenient to the flowing of directed circulation downwards.Space between baffle plate and guide frame forms the 3rd baffling district of three phase separation section.And the setting of deflection plate makes reactor down-comer (ring pipe be namely made up of housing and water conservancy diversion inner core) form multiple flow region, form the blanking of self-loopa spiral, add turbulence.
2, interior circulation type fluidized bed reactor of the present invention, arranges recycle oil feed pipe, makes fresh material, the charging of recycle oil subregion, enhances the pattern of circulating; Arrange even gas distribution device, strengthening air-fuel mixture and gas-liquid distribution, gas disturbance simultaneously effectively can avoid the generation in reactor bottom dead band, and can play cushioning effect, reduces the percussion to distribution grid.
3, interior circulation type fluidized bed reactor of the present invention, inclination overfall and overflow surge tank are set, form eddy flow discharging, by particle deposition to bottom, the catalyst taken out of returns in housing by the described catalyst return port of bottom, and be provided with cleaning hose flushing deposited particles, backflow regulating flow can be set; Bottom catalyst discharge duct arranges backwash arm, can be used as the shut-down displacement line playing recycle oil; Recycle oil tangentially arranges several charging apertures in reactor side, adopts eddy flow feeding manner.
Accompanying drawing explanation
In order to be illustrated more clearly in the specific embodiment of the invention or technical scheme of the prior art, be briefly described to the accompanying drawing used required in detailed description of the invention or description of the prior art below, apparently, accompanying drawing in the following describes is some embodiments of the present invention, for those of ordinary skill in the art, under the prerequisite not paying creative work, other accompanying drawing can also be obtained according to these accompanying drawings.
The axial section structural representation of the fluidized bed reactor that Fig. 1 provides for the specific embodiment of the invention;
Fig. 2 is the profile of Fig. 1 along A-A line;
Fig. 3 is the profile of Fig. 1 along B-B line;
Fig. 4 is the profile of Fig. 1 along C-C line;
Fig. 5 is the profile of Fig. 1 along D-D line;
Wherein, icon is: 1-housing, 2-liquid phase feeding mouth, 3-gas sparging dish, 4-guide shell, 5-material distributor, 6-guide frame, 7-gas separaion pipe, 8-baffle plate, 9-overfall, 10-overflow surge tank, 11-liquid outlet, 12-catalyst return port, 13-exhaust outlet, 14-deflection plate, 15-recycle oil feed pipe, 16-catalyst adds pipe, 17-catalyst exit line.
Detailed description of the invention
Be clearly and completely described technical scheme of the present invention below in conjunction with accompanying drawing, obviously, described embodiment is the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
In describing the invention, it should be noted that, orientation or the position relationship of the instruction such as term " " center ", " on ", D score, "left", "right", " vertically ", " level ", " interior ", " outward " they be based on orientation shown in the drawings or position relationship; be only the present invention for convenience of description and simplified characterization; instead of instruction or imply the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore can not be interpreted as limitation of the present invention.In addition, term " first ", " second ", " the 3rd " only for describing object, and can not be interpreted as instruction or hint relative importance.
In describing the invention, it should be noted that, unless otherwise clearly defined and limited, term " installation ", " being connected ", " connection " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or connect integratedly; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals.For the ordinary skill in the art, concrete condition above-mentioned term concrete meaning in the present invention can be understood.
In addition, if below in the described different embodiment of the present invention involved technical characteristic do not form conflict each other and just can be combined with each other.
The axial section structural representation of the fluidized bed reactor that Fig. 1 provides for present embodiment.As shown in Figure 1, circulation type fluidized bed reactor in a kind of, comprises housing 1, guide shell 4 and three phase separation parts.
Wherein, housing 1, in straight tube shape, described housing comprises three phase separation section and conversion zone from top to bottom successively, the sidewall of described three phase separation section is provided with liquid flooding mouth 9, the top of described housing 1 is provided with exhaust outlet 13, and bottom is provided with liquid phase feeding mouth 2 and gas phase charging aperture, described housing is also provided with at least one catalyst and adds pipe 16 and at least one catalyst exit line 17.
Guide shell 4, is arranged in described housing 1, and extends to the bottom of described conversion zone from the bottom of described three phase separation section; Three phase separation parts, are arranged in described three phase separation section.
By arranging guide shell in housing, make in reactor, to form directed circulation flowing, the circulation of material in reactor can be promoted by the density contrast of material in the kinetic energy of entrance material and tedge (i.e. guide shell) and down-comer (ring pipe be namely made up of housing and guide shell) completely jointly, makes whole technique more energy-conservation.
Described three phase separation parts comprise guide frame 6 and baffle plate 8, described guide frame 6 has the conically shaped of radian to connect and compose by a center drum and one, and described center drum is located at the upper end open place of described guide shell 4 and is extended downward certain distance in described guide shell from described upper end open; The upper end of described conically shaped is connected with center drum upper end, the lower end of described conically shaped is that umbrella extends towards the outer side-lower of described guide shell 4 with the outer wall exceeding described guide shell 4, the annular region that the inwall of described conically shaped and the outer wall of described guide shell 4 are formed forms the first baffling district of three phase separation section, and the space between the outer wall of described conically shaped and the inwall of described housing 1 forms the second baffling district of three phase separation section.Described baffle plate 8 is arranged at certain altitude position above described guide frame 6, and the space between described baffle plate 8 and described guide frame 6 forms the 3rd baffling district of three phase separation section.
The outer wall of the upper end open of described guide shell 6 is provided with several deflection plates corresponding with the lower end inner wall of described conically shaped 14.
In the present embodiment, deflection plate 14 is set to 3, but the present invention does not do concrete restriction for the quantity of deflection plate, can also be set to 2,4,5 etc. in other embodiments, as shown in Figure 5.
In above-mentioned interior circulation type fluidized bed reactor, described three phase separation parts also comprise some gas separaion pipes 7, the lower ending opening of described some gas separaion pipes 7 is positioned at the top of the conically shaped of described guide frame 6, and the upper end open of described some gas separaion pipes 7 is between described housing 1 top and described baffle plate 8.
The gross area of the lower ending opening of described some gas separaion pipes is 10% of the cross-sectional area of the annular region be made up of the center drum outer wall of described guide frame and described guide shell outer wall.
In the present embodiment, gas separaion pipe 7 is set to 4, but the present invention does not do concrete restriction for the quantity of gas separaion pipe, can also be set to 2,6,8 etc. in other embodiments.
Described liquid flooding mouth 9 tilts upward setting, and itself and the axial angle of housing are 30 °.
In above-mentioned interior circulation type fluidized bed reactor, described three phase separation parts also comprise overflow surge tank 10, described overflow surge tank 10 has liquid outlet 11 and catalyst return port 12, described overflow surge tank 10 is connected with described housing 1 by described liquid flooding mouth 9, described overflow surge tank 10 is rotary filter press structure, supernatant liquid after separation is discharged from described liquid outlet 11, and the catalyst taken out of is returned in described housing 1 by the described catalyst return port 12 of bottom.
Described overflow surge tank 10 is provided with for rinsing deposited particles in order to avoid the cleaning hose of described catalyst return port blocking.
In above-mentioned interior circulation type fluidized bed reactor, described guide shell 4 is coaxially arranged with described housing 1, and the diameter of described guide shell 4 is 0.6 times of described housing 1 diameter.In the present invention, " diameter " typically refers to internal diameter.
Described center drum diameter is 0.7 times of guide shell 6 diameter, and the lower ending opening diameter of described conically shaped is 0.8 times of diameter of the housing.
Described baffle plate 8 is beveled structure, and it is 1.2 times of draft tube diameter at the projection diameter of a circle of horizontal section.
A catalyst adds the top that pipe 16 is positioned at described annular region, and catalyst adds the barrel of lower ending opening through described conically shaped of pipe 16, and a catalyst exit line 17 is located at the bottom of described housing 1.
In above-mentioned interior circulation type fluidized bed reactor, also comprise the gas sparging dish 3 of the bottom being located at guide shell 4 lower ending opening, described gas sparging dish 3 is connected with described gas-phase feed mouth; The outlet of described gas sparging dish 3 is downward, as shown in Figure 3.
In above-mentioned interior circulation type fluidized bed reactor, also comprise the material distributor 5 be arranged in described guide shell 4, above gas sparging dish 3.
In the present embodiment, material distributor 5 is set to 1, but the present invention does not do concrete restriction for the quantity of material distributor, can also be set to 2,3 etc. in other embodiments.
Described material distributor 5 is the foraminate circular flat board of distribution, and described circular platen area and the ratio of the cross-sectional area of guide shell are 0.8, and described circular dull and stereotyped percent opening is 0.5.The diameter being positioned at the aperture of circular dull and stereotyped central area is less than the diameter of the aperture away from central area, as shown in Figure 2.
In above-mentioned interior circulation type fluidized bed reactor, also comprise some recycle oil feed pipes 15 that the tangential direction along place housing circumference is arranged.
In the present embodiment, recycle oil feed pipe 15 is set to 3, recycle oil feed pipe on the housing setting position lower than the upper end open position of described guide shell, as shown in Figure 4.But the present invention does not do concrete restriction for the quantity of recycle oil feed pipe, 2,4,5 etc. can also be set in other embodiments.
The liquid phase feed of reaction enters reactor shell 1 by liquid phase feeding mouth 2, the phase feed of reaction enters housing 1 by gas-phase feed mouth, through gas sparging dish 3 be uniformly distributed backward under enter reactor and up liquid phase feed and down-comer (ring pipe namely formed by housing 1 and guide shell 4) and circulate together with the gas-liquid-solid mixture that comes, enter guide shell 4 through material distributor 5.Guide shell 4 and down-comer are reaction zone, and both Catalyst packing total amounts are 50% of reactor dischargeable capacity.When reactor stable operation, catalyst forms circulation in guide shell 4 and down-comer.Gas-liquid mixed raw material in guide shell 4 reacts under the catalysis of solid catalyst.
Around the upper end of guide shell 4, guide frame 6 is set, gas-solid raw material and reacted oil gas are entrained with in the center drum that most of catalyst solid particle enters along separate routes guide frame 6 and the annular space formed with guide shell 4 thereof, the space that the liquid moved upward in annular space and solid are formed along with guide frame 6 and guide shell 4 enters down-comer as the first baffling district, gas directly can enter the gas enrichment region at housing 1 top by gas separaion pipe 7, and is discharged by the exhaust outlet 13 at housing 1 top subsequently.In the center drum of guide frame 6, logistics moves upward and runs into the structure of sudden enlargement, speed reduces, curved baffle 8 is set at reactor upper space simultaneously, forced guiding is shunted, liquid entrainment catalyst and portion gas, and to start baffling along guide frame 6 downward, enter the second baffling district formed by described guide frame 6 and housing 1 inwall and enter down-comer, because liquid velocity is less, major part gas due to buoyancy effusion and in reactor head enrichment, with after discharge reactor through exhaust outlet 13.
In the second baffling district, partially liq can enter overflow surge tank 10 by overfall 9.Because overfall is inclined upwardly, in flooding process part by the catalyst granules taken out of because Action of Gravity Field turns back in reactor, small part catalyst is brought into overflow surge tank 10 in addition, surge tank 10 is rotary filter press structure, through being separated rear catalyst by catalyst return port 12 Returning reactor, and establish cleaning hose to rinse deposited particles, in order to avoid blocking; Supernatant liquor is collected by liquid outlet 11.In order to strengthen the circulation power in down-comer, by the tangential recycle oil charging aperture 15 replenishment cycles oil that housing is arranged.Fresh solid catalyst adds pipe 16 by the catalyst at housing 1 top and adds, and the catalyst of inactivation is discharged by the catalyst exit line 15 bottom housing 1, thus realizes catalyst and change online.
Obviously, above-described embodiment is only for clearly example being described, and the restriction not to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without the need to also giving all embodiments.And thus the apparent change of extending out or variation be still among the protection domain of the invention.
Claims (18)
1. a circulation type fluidized bed reactor in, comprising:
Housing, in straight tube shape, described housing comprises three phase separation section and conversion zone from top to bottom successively, the sidewall of described three phase separation section is provided with liquid flooding mouth, the top of described housing is provided with exhaust outlet, bottom is provided with liquid phase feeding mouth and gas phase charging aperture, described housing is also provided with at least one catalyst and adds pipe and at least one catalyst exit line;
Guide shell, is arranged in described housing, and extends to the bottom of described conversion zone from the bottom of described three phase separation section;
Three phase separation parts, are arranged in described three phase separation section;
It is characterized in that, described three phase separation parts comprise guide frame and baffle plate, described guide frame has the conically shaped of radian to connect and compose by a center drum and one, and described center drum is located at the upper end open place of described guide shell and is extended downward certain distance in described guide shell from described upper end open; The upper end of described conically shaped is connected with center drum upper end, the lower end of described conically shaped is that umbrella extends towards the outer side-lower of described guide shell with the outer wall exceeding described guide shell, and the annular region that the inwall of described conically shaped and the outer wall of described guide shell are formed forms the first baffling district of three phase separation section; Space between the outer wall of described conically shaped and the inwall of described housing forms the second baffling district of three phase separation section; Described baffle plate is arranged at certain altitude position above described guide frame, and the space between described baffle plate and described guide frame forms the 3rd baffling district of three phase separation section.
2. interior circulation type fluidized bed reactor according to claim 1, is characterized in that, the outer wall of the upper end open of described guide shell is provided with several deflection plates corresponding with the lower end inner wall of described conically shaped.
3. interior circulation type fluidized bed reactor according to claim 1, it is characterized in that, described three phase separation parts also comprise some gas separaion pipes, the lower ending opening of described some gas separaion pipes is positioned at the top of the conically shaped of described guide frame, and the upper end open of described some gas separaion pipes is between described case top and described baffle plate.
4. interior circulation type fluidized bed reactor according to claim 3, it is characterized in that, the gross area of the lower ending opening of described some gas separaion pipes is 10% ~ 50% of the cross-sectional area of the annular region be made up of the center drum outer wall of described guide frame and described guide shell outer wall.
5. circulation type fluidized bed reactor according to any one of claim 1-4, is characterized in that, described liquid flooding mouth tilts upward setting, and itself and the axial angle of housing are 5-45 °.
6. circulation type fluidized bed reactor according to any one of claim 1-5, it is characterized in that, described three phase separation parts also comprise overflow surge tank, described overflow surge tank has liquid outlet and catalyst return port, described overflow surge tank is connected with described housing by described liquid flooding mouth, described overflow surge tank is rotary filter press structure, supernatant liquid after separation is discharged from described liquid outlet, and the catalyst taken out of is returned in described housing by the described catalyst return port of bottom.
7. interior circulation type fluidized bed reactor according to claim 6, is characterized in that, described overflow surge tank is provided with for rinsing deposited particles in order to avoid the cleaning hose of described catalyst return port blocking.
8. circulation type fluidized bed reactor according to any one of claim 1-7, is characterized in that, described guide shell and described housing are coaxially arranged, and the diameter of described guide shell is 0.6 ~ 0.8 times of described diameter of the housing.
9. circulation type fluidized bed reactor according to any one of claim 1-8, is characterized in that, described center drum diameter is 0.65 ~ 0.85 times of draft tube diameter, and the lower ending opening diameter of described conically shaped is 0.75 ~ 0.9 times of diameter of the housing.
10. circulation type fluidized bed reactor according to any one of claim 1-9, is characterized in that, described baffle plate is beveled structure, and it is 1 ~ 1.2 times of draft tube diameter at the projection diameter of a circle of horizontal section.
11. according to any one of claim 1-10 in circulation type fluidized bed reactor, it is characterized in that, at least one catalyst described adds the top that pipe is positioned at described annular region, and at least one catalyst described adds the barrel of lower ending opening through described conically shaped of pipe, and at least one catalyst exit line described is located at the bottom of described housing.
12. according to any one of claim 1-11 in circulation type fluidized bed reactor, it is characterized in that, also comprise the even gas distribution device of the bottom being located at guide shell lower ending opening, described even gas distribution device is connected with described gas-phase feed mouth.
13. interior circulation type fluidized bed reactors according to claim 12, it is characterized in that, described even gas distribution device is gas sparging dish, and the outlet of described gas sparging dish is downward.
14. interior circulation type fluidized bed reactors according to claim 13, is characterized in that, also comprise at least one the material distributor be arranged in described guide shell, above even gas distribution device.
15. interior circulation type fluidized bed reactors according to claim 14, it is characterized in that, described material distributor is the foraminate circular flat board of distribution, and described circular platen area and the ratio of the cross-sectional area of guide shell are 0.8 ~ 1, and described circular dull and stereotyped percent opening is 0.2 ~ 0.7.
16. interior circulation type fluidized bed reactors according to claim 15, is characterized in that, the diameter being positioned at the aperture of circular dull and stereotyped central area is less than the diameter of the aperture away from central area.
17. according to any one of claim 1-16 in circulation type fluidized bed reactor, it is characterized in that, also comprise some recycle oil feed pipes that the tangential direction along place housing circumference is arranged.
18. interior circulation type fluidized bed reactors according to claim 17, is characterized in that, described some recycle oil feed pipes on the housing setting position lower than the upper end open position of described guide shell.
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| CN106345375A (en) * | 2016-10-26 | 2017-01-25 | 中国科学院青岛生物能源与过程研究所 | Inner loop reactor with reacting and separating functions |
| CN110559944A (en) * | 2018-06-05 | 2019-12-13 | 中国石油天然气股份有限公司 | gas mixing distributor and fixed bed reactor |
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| CN112427002B (en) * | 2020-11-21 | 2024-06-07 | 贵州锦江生物能源科技有限公司 | Tower-type superfine contact reaction device for biodiesel |
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| CN114749112B (en) * | 2021-01-11 | 2023-04-07 | 中国石油化工股份有限公司 | Fluidized bed reactor |
| CN114353063A (en) * | 2021-11-30 | 2022-04-15 | 西安交通大学 | Liquid chemical looping combustion cogeneration and carbon capture system and process |
| CN115738915A (en) * | 2022-11-02 | 2023-03-07 | 中国石油化工股份有限公司 | Prevent excursion fixed bed reactor |
| CN115738915B (en) * | 2022-11-02 | 2024-07-02 | 中国石油化工股份有限公司 | Bias-flow-preventing fixed bed reactor |
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