CN1082392C - Fast swirl gas-solid separator - Google Patents
Fast swirl gas-solid separator Download PDFInfo
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- CN1082392C CN1082392C CN96103420A CN96103420A CN1082392C CN 1082392 C CN1082392 C CN 1082392C CN 96103420 A CN96103420 A CN 96103420A CN 96103420 A CN96103420 A CN 96103420A CN 1082392 C CN1082392 C CN 1082392C
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Abstract
The present invention relates to a fast swirl gas-solid separator in a fluidization reacting system of a lift pipe for fast separating a catalyst and oil gas after reaction, improving gas-solid two-phase separating efficiency and reducing oil gas over cracking after the reaction. The fast swirl gas-solid separator is formed by a circle of 6 to12 circular arc baffle plates of which the curve radius is 0.8 to1.2 of an inside diameter of the lift pipe. The upper end of the fast swirl gas-solid separator is closed and the lower end is opened. The lower end and the upper port of the lift pipe are mutually connected. The fast swirl gas-solid separator is provided with 6 to12 tangential spraying ports sloping downward 10 degrees to 35 degrees. The fast swirl gas-solid separator is mainly applied to catalysts and gas fast separation or gas-solid fast separation at the outlets of lift pipe reactors in an oil refinery and a chemical plant.
Description
The present invention relates to realize the device of the gas-solid sharp separation of riser tube fluidized reaction system catalyst and oil gas.
In the riser tube exit of refinery fluid catalytic cracking reactive system, fast gas-solid separator all is housed to realize the sharp separation of catalyzer and oil gas, stop unnecessary overreaction.This tripping device has two big classes at present, the first kind is that inertia divides device soon, it is to rely on the oil gas that contains a large amount of granules of catalyst sharply to change the gas-solid two-phase inertia difference that is produced when flowing to realize gas solid separation, the typical fast packing of inertia is equipped with structures such as inverted L shape, T type, Multiblade, their characteristics are that pressure drop is very little, generally have only the hundreds of handkerchief, but the solid particulate efficient that flash liberation is come out from gas is lower, has only about 70～80%.The oil gas that separates behind most of catalyzer rises at a slow speed in the bigger settling vessel of diameter, approximately in the cyclonic separator through just being entered settling vessel top in 20 seconds, the catalyzer of carrying secretly is further separated, and catalyzer enters settling vessel bottom bed along cyclone dip-leg.The catalyzer that the front and back secondary separation is come out is all being carried a certain amount of oil gas secretly, needs have water vapor to blow and put forward in the bed of settling vessel bottom, and oil gas rises to the inlet of settling vessel top cyclonic separator again through the time more than 30 seconds.Like this, the mean residence time of reacted oil gas in settling vessel may reach 20～30 seconds, and oil gas back-mixing rate is up to 50%, be easy to take place the elevated temperature heat cracking, yield of light oil is reduced, and can cause serious coking in the settling vessel, influence the device long-term operation.
Second class is a centrifugal separator, and the strong centrifugal force field boundary that it relies on gas-solid two-phase mixture to rotate formation is rapidly realized the gas-solid sharp separation.Representative instance is the one group of simple cyclonic separator of outlet direct connection (be called for short and slightly revolve) at riser reactor, and its gas solid separation efficient can be up to more than 98%, and pressure drop is bigger, about thousands of handkerchiefs.The oil gas that separates most of catalyzer is discharged from slightly revolving riser, enter settler space, rise with slower speed, through just being entered more than 10 seconds in the cyclonic separator on settling vessel top, oil gas further separates the catalyzer of carrying secretly by this cyclonic separator.Thick spin material leg is to discharge catalyzer under positive pressure differential, when so a large amount of catalyzer drops to settling vessel bottom bed stripping stage, not only the catalyst particles intergranular has been carried part oil gas secretly, flow downward, also has a part of oil gas that under positive pressure differential, from dipleg, sprays downwards, these oil gas mix with stripping gas, and then rise at a slow speed along settling vessel and to enter in the cyclonic separator on settling vessel top.Make reaction back oil gas mean residence time in settling vessel at high temperature still have excessive thermally splitting phenomenon like this, influence the safe handling of yield of light oil and device still up to 10～20 seconds.
For improving the efficient that first kind inertia-type divides device catalyzer and oil gas sharp separation soon, U.S. Pat 4,495, ejection type quickly separating method and device have been developed in 063 (1985), its gas-solid flash liberation efficient reaches 80～90%, and the gas backmixing rate is reduced to about 20%, but pressure drop is up to thousands of Pa, turndown ratio is less, and industrial application has certain difficulty.U.S. Pat 4,364,905 (nineteen eighty-twos), US 5,294,331 (1994), US 5,364,515 (1994), US 5,393,414 (nineteen ninety-fives) improved again the fast branch of ejection type, mainly were in order further to shorten the mean residence time of oil gas in settling vessel.But ejection type divides separating effect very not high soon, and turndown ratio is little, and shortcomings such as pressure drop height are unresolved good.
For further improving centrifugal fast minute device of second class, U.S. Pat 4,502,947 (nineteen ninety-fives), US 4,579,716 (1986), US 4,624, enclosed direct connection cyclone separation system has been developed in 772 (1986) etc., will slightly revolve riser directly to link to each other with settling vessel top cyclone inlet, has shortened the residence time of oil gas in settling vessel greatly, make the gas backmixing rate further drop to 6%, but the poor-performing of its compressive resistance fluctuation is wanted SC when going into operation, U.S. Pat 5 subsequently, 158,669 (1992), US 5,314,611 (1994) and European patent EP 0593827A1, Chinese patent CN92112441 (1992) etc. have directly installed a stripper in the portion of screwing off slightly again, change the rough sledding of part reaction back oil gas downward ejection from the dipleg that slightly revolves, further shortened the mean residence time of reaction back oil gas in settling vessel, oil gas back-mixing rate is further dropped to below 2% again.
Japan special permission clear 61-25413 of communique (B2) (1986) and U.S. Pat 4,482, the garden arc bend pipe that several downward-sloping certain angles have then been adopted at the riser tube end in 451 (1984) is as the gas-solid quick disconnector, and adds a seal bootr outside to realize drawing fast of oil gas.And in U.S. Pat 5, in 314,611 (1994), also with the arm-type fast branch of a kind of eddy flow with seal bootr, can realize that the efficient stripping fast and the oil gas of catalyzer draws fast, but this patent does not specify the concrete structure of arm-type fast minute device of this eddy flow.
Do not find riser tube fluidized reaction of the present invention system fast swirl gas-solid separator in the prior art.
The object of the invention provides a kind of fast swirl gas-solid separator that is used for the riser tube fluidized reactor, the sharp separation that is used for post catalyst reaction and oil gas, improve gas-solid two-phase separation efficiency, reduce the oil gas transition cracking of reaction back, eliminate coking phenomenon in the settling vessel.
Fast swirl gas-solid separator of the present invention is installed in the outlet of riser reactor, one section internal diameter is arranged at the bottom that it is characterized in that it is the garden pipe of 1～1.2 times of riser tube internal diameter, garden pipe end opening is connected with riser tube is suitable for reading, the top is the oblique top lid of sealing, and a circle garden curved baffle is housed between sealing oblique top lid and garden pipe.
The circular arc baffle plate has 6～12, and radius-of-curvature is (0.8～1.2) D
1, D
1Be the internal diameter of riser tube, the garden curved baffle constitutes 6～12 downward-sloping tangential ejiction openings of 10 °～35 °, and total area of efflux of tangential ejiction opening is long-pending 0.6～1.2 times in riser tube effective cross section; The corresponding garden arc angle β of garden curved baffle
1=A
1/ B
1, A
1Be 360 °～540 °, B
1Be 6～12.
Elaborate technical scheme of the present invention below in conjunction with accompanying drawing.
Fig. 1 uses synoptic diagram for fast swirl gas-solid separator of the present invention in the riser tube fluidized reactor.Catalyzer and gas-oil mixture upwards enter fast swirl gas-solid separator 2 from riser tube 1, through a plurality of tangential ejiction opening 3 around the fast swirl gas-solid separator, tangentially spray with certain speed, in stripping cover 4, form the rotational flow of gas-solid mixture, most catalyzer in the mixture are thrown to stripping cover 4 under effect of centrifugal force inwall place falls, and finishes reacted oil gas and realizes efficient sharp separation.
Fig. 2 is the structural representation of fast swirl gas-solid separator of the present invention.It has one section garden pipe 24, the inside diameter D of garden pipe 24
0Be the riser tube inside diameter D
11～1.2 times.The end opening 21 of garden pipe 24 is uncovered, is welded on the upper end outlet of riser tube 1.The top of fast swirl gas-solid separator 2 is oblique top lids 23, seals.Be welded with 6～12 garden curved baffles 22 between oblique top lid 23 and garden pipe 24, the radius-of-curvature of garden curved baffle is (0.8～1.2) D
1, height is H
1The corresponding garden arc angle of every garden curved baffle 22 is β
1Oblique top lid 23 downward inclination angles are α, and the α angle generally can be between 10 °～35 °.β
1Be generally β
1=(2～3) π/n, n is general desirable 6～12, the inside diameter D of looking riser tube 1
1And decide.H
10.6～1.2 times of the net sectional area of determining to make the area of efflux of total tangential ejiction opening 3 be about riser tube 1 between.The gaseous mixture that contains a large amount of catalyzer enters the end opening 21 of fast swirl gas-solid separator 2 from riser tube 1, from 6～12 tangential ejiction openings 3 ejections, forms rotational flow again.
The present invention is mainly used in the interior riser reactor outlet catalyzer of the various fluidized catalytic cracking units of refinery and the sharp separation of gas, also can be applicable to the gas-solid sharp separation that other has the fluidization chemical reaction system of riser reactor.
Fast swirl gas-solid separator of the present invention can be realized efficient gas solid separation fast, make and finish reacted gas and finish high efficiency the separation with catalyzer, separation efficiency reaches more than 99.5%, thereby avoided the overreaction unfriendly that causes owing to catalyzer and the excessive Long contact time of reaction product, avoid the coking phenomenon in settling vessel, improved the productive rate of purpose product simultaneously again.
Fig. 1 uses synoptic diagram for fast swirl gas-solid separator of the present invention in riser reactor.Riser tube 1, fast swirl gas-solid separator 2, tangential ejiction opening 3, stripping cover 4, reverse guide device 5, gas diversion tube 6, cyclonic separator 7, vapor pipe 8, interior collection chamber 9, outlet pipe 11, cyclone dip-leg 12, plate washer 13, one-level stripping stage 14, stripping gas 15, one-level stripping distribution pipe 16, flutter valve 17, secondary stripping stage 18.
Fig. 2 is the structural representation of fast swirl gas-solid separator of the present invention.Tangential ejiction opening 3, garden pipe end opening 21, garden curved baffle 22, oblique top lid 23, garden pipe 24.
When being different angle of declination α, separates by table one the efficient table.
Table 2 is that the following separation efficiency of linear gas velocity in the different riser tubes (α=20 °) is shown.
Further narrate fast swirl gas-solid separator of the present invention below by embodiment, should think, technical solution of the present invention is not limited by following examples should.
Embodiment 1
At internal diameter is that fast swirl gas-solid separator of the present invention is equipped with in the exit of the riser tube of 60mm.The garden pipeline section internal diameter of fast swirl gas-solid separator is 68mm, and oblique top lid angle of declination α is 0～30 °, adopts 6 garden curved baffles to constitute 6 tangential ejiction openings of gas, ejiction opening height H
1Be 53mm, the total area of efflux of ejiction opening is 0.75 times of riser tube net sectional area.With the meta particle diameter is that catalytic cracking (FCC) equilibrium catalyst of 64 μ m is made solid powder, makes cold test with air.Following experimental result (see Table 1 and table 2) is arranged.
From table 1 and table 2 result as can be seen, fast swirl gas-solid separator of the present invention and U.S. Pat 4,482, the separation efficiency of the 451 arm-type fast branches of spiral that propose is suitable, and compare with the latter, fast swirl gas-solid separator of the present invention has more that pressure drop is little, turndown ratio is big, advantage of simple structure.
Table 1
| Angle of declination α ° | 0 10 20 30 |
| Linear gas velocity in the riser tube, m/s | 17.4 17.4 17.4 17.4 |
| Fast device pressure drop, the Pa of dividing | 860 1100 1220 1250 |
| Separation efficiency, % | 98.3 98.83 99.64 99.77 |
Table 2
| Linear gas velocity in the riser tube, m/s | 7.56 11.63 15.55 17.44 21.42 |
| Fast device pressure drop, the Pa of dividing | 220 500 1230 880 2050 |
| Separation efficiency, % | 99.54 99.63 99.57 99.74 99.58 |
Claims (2)
1. fast swirl gas-solid separator that is used for the riser tube fluidized reactor, fast swirl gas-solid separator is installed in the riser tube outlet of riser reactor, it is characterized in that the fast swirl gas-solid separator upper end closed, the lower end is uncovered, one section internal diameter is arranged at the bottom is the garden pipe of 1～1.2 times of riser tube internal diameter, garden pipe end opening is connected with riser tube is suitable for reading, the top is the oblique top lid of sealing, one circle garden curved baffle is housed between sealing oblique top lid and garden pipe, adjacent two garden curved baffles are formed a tangential ejiction opening, and tangential ejiction opening is downward-sloping.
2. fast swirl gas-solid separator according to claim 1 is characterized in that said garden curved baffle has 6～12, and radius-of-curvature is (0.8～1.2) D
1, D
1Be the internal diameter of riser tube, said garden curved baffle constitutes 6～12 downward-sloping tangential ejiction openings of 10 °～35 °, and the general export area of tangential ejiction opening is long-pending 0.6～1.2 times in riser tube effective cross section, the corresponding garden arc angle β of said garden curved baffle
1=A
1/ B
1, A
1Be 360 °～540 °, B
1Be 6～12.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96103420A CN1082392C (en) | 1996-03-22 | 1996-03-22 | Fast swirl gas-solid separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96103420A CN1082392C (en) | 1996-03-22 | 1996-03-22 | Fast swirl gas-solid separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1168301A CN1168301A (en) | 1997-12-24 |
| CN1082392C true CN1082392C (en) | 2002-04-10 |
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ID=5118063
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96103420A Expired - Lifetime CN1082392C (en) | 1996-03-22 | 1996-03-22 | Fast swirl gas-solid separator |
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| CN (1) | CN1082392C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102559238B (en) * | 2010-12-30 | 2015-01-07 | 中国石油天然气集团公司 | Reaction and regeneration device of quick-contact cyclone |
| CN103509589B (en) * | 2012-06-26 | 2015-07-29 | 中国石油化工股份有限公司 | A kind of Light hydrocarbon oil catalytic conversion method |
| CN103275756B (en) * | 2013-06-07 | 2016-01-06 | 上海华畅环保设备发展有限公司 | The two-stage eddy flow series connection idetified separation method and device of product in suspension bed hydrogenation process |
| CN105482847B (en) * | 2015-12-18 | 2016-12-21 | 中国石油大学(华东) | A kind of it is used in catalytic cracking regenerator the device carrying out pre-stripping and quickly being sloughed by the oil gas of catalyst surface |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4482451A (en) * | 1982-09-16 | 1984-11-13 | Uop Inc. | Process for the separation of particulate solids from vapors using a discharge having a helical twist |
-
1996
- 1996-03-22 CN CN96103420A patent/CN1082392C/en not_active Expired - Lifetime
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4482451A (en) * | 1982-09-16 | 1984-11-13 | Uop Inc. | Process for the separation of particulate solids from vapors using a discharge having a helical twist |
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| Publication number | Publication date |
|---|---|
| CN1168301A (en) | 1997-12-24 |
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