CN1203157C - Contact chamber for catalytic cracking of oil - Google Patents
Contact chamber for catalytic cracking of oil Download PDFInfo
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- CN1203157C CN1203157C CN 02116286 CN02116286A CN1203157C CN 1203157 C CN1203157 C CN 1203157C CN 02116286 CN02116286 CN 02116286 CN 02116286 A CN02116286 A CN 02116286A CN 1203157 C CN1203157 C CN 1203157C
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Abstract
The present invention relates to a catalytic cracking oil agent contact chamber which comprises a barrel body (10), a sloped partition board (16-7), a vertical partition board (16-4), a gas distributing board (16-10), an air collecting chamber partition board (16-1), a hydrocarbon oil nozzle (16-6) and a sloped tube reaction section (5), wherein the sloped partition board, the vertical partition board and the hydrocarbon oil nozzle are arranged at one side of the central axis of the cylindrical oil agent contact chamber; the sloped partition board fixed to the inner side of the upper edge of the barrel body and the central axis form an included angle gamma of 30 to 60 degrees; the upper edge of the vertical partition board is fixedly connected with the lower edge of the sloped partition board; the sloped partition board and the vertical partition board separate the space above the gas distributing board in the oil agent contact chamber into two zones; and the air collecting chamber partition board vertically fixed to the lower part of the gas distributing board separates the space below the gas distributing board in the oil agent contact chamber into two air collecting chambers corresponding to the positions of the two zones. The hydrocarbon oil nozzle fixedly connected with the barrel body penetrates the vertical partition board, and the included angle alpha formed between the hydrocarbon oil nozzle and the horizontal direction is from 5 to 30 degrees.
Description
Technical field
The invention belongs to catalytic cracking of petroleum hydrocarbon equipment, more particularly, is a kind of finish exposure chamber that is used for the Desending catalytic cracking process.
Background technology
50 for many years, and catalytic cracking occupies critical role always in world refining industry.Therefore, catalytic cracking process is also relative more with catalyst technology research, and development is very fast.From the fluidized-bed reactor to the riser reactor, the reaction times shortens greatly, the also corresponding improvement of product selectivity, and gasoline yield greatly improves, and coke yield descends significantly, and the intermingled dregs ratio example improves rapidly.The catalytic cracking process technology develops to both direction at present, and the one, residual oil catalytic cracking, the 2nd, catalytic cracking fecund gas alkene.Along with the heaviness of stock oil and the raising that quality product is required, riser tube is obvious day by day as the limitation of efficient mink cell focus catalyst cracker:
1) back-mixing of agent oil contact causes colloid in the residual oil, bituminous matter absorption green coke, and carbon residue transforms green coke coefficient height, heavy oil conversion degree of depth deficiency, product selectivity variation.
2) prolongation of the catalyzer back-mixing and the residence time has aggravated secondary reaction and dehydrogenation metal reaction, and the carbon deposit on the catalyzer increases, and reactive behavior descends, and light olefin increases.In addition, the landing of solid particulate causes the alternate contact efficiency of gas-solid poor, same section temperature ununiformity aggravation, and the response intensity difference is bigger.
3) radially-arranged inhomogeneous " ring-nuclear " liquid form that shows as in the riser tube, i.e. limit wall solid concentration height, the center solid concentration is low, has influenced the gas-solid two-phase and has fully contacted.Moreover limit wall gas phase flow velocity is little, easily produces cracking, the transformation efficiency and the selectivity of influence reaction.
4) continually developing of new catalyst, its reactive behavior and selectivity are improved (appearance as molecular sieve catalyst makes activity of such catalysts approximately improve 2 orders of magnitude) day by day, require gas-solid contact efficiency height, time weak point, to slow down catalyst deactivation.
The residual oil catalytic cracking technology mainly comprises charging high-efficient atomizing technology, the pre-lift technique in riser reactor bottom, the terminal gas-solid sharp separation of riser tube technology, reclaimable catalyst multistage steam stripping technique and short contact reaction technology.Real novel residual oil catalytic cracking technology is the short contact reaction technology.Compare with traditional riser tube, the short contact catalytic cracking technology has following characteristics:
1. catalyzer and raw material move along gravity field and under flowing to, and have reduced the solid phase back-mixing, have improved the selectivity of product.
2. catalyzer contacted with the ultrashort time of raw material, improved the primary first-order equation degree of depth, reduced the generation of thermally splitting and coke, can realize the selectivity catalyzed reaction.
3. the outlet particle speed helps sharp separation greater than linear gas velocity.
4. lower coking yield and gas yield have increased turndown ratio, can handle the raw material of broad, also can select different transformation efficiencys and selectivity on request.
Under this background, since the eighties, external famous oil company is as Exxon, Mobli, UOP, Stone ﹠amp; Companies such as Webster have proposed a kind of new residual oil catalytic cracking technology-short contact reactor, and have proposed patented technology separately, as US4411773, and US4514285, US5296131, US5462652, EP663434A1 etc.Compare with riser reactor, short contact reactor gas-solid two-phase and stream are along gravity flowage, the back-mixing degree is little, the gas-solid two-phase residence time distributes very narrow, eliminated the axial landing of reactor limit wall solid particulate, therefore improved the selectivity and the cracking performance of reaction, can develop into the update technology of technologies such as residual oil catalytic cracking, olefin production, be described as " new technology that 21 century replaces riser tube ".The short contact catalyst cracker mainly comprises following cubic surface technology: the high efficiency nozzle atomizing, the agent innage is imitated distribution contact technique, gas-solid quickly separating technology and catalyst regeneration technology, and wherein agent innage effect contact technique and gas-solid quickly separating technology are the bases of short contact reaction.
USP4514285 has proposed a kind of down pipe and dilute phase riser regeneration short contact catalytic-cracking reaction system.Catalyzer removes flue gas at the regeneration degassing vessel after regenerating by dilute phase riser, forms dense-phase bed and improves solid catalyst density.The catalyst recirculation amount is controlled by guiding valve, relies on the self gravitation effect to enter down pipe, and stock oil radially sprays into down pipe by the product distribution endless tube with multitube, realizes that stock oil contacts with catalyzer, carries out further cracking reaction in down pipe.
US4385985 has proposed a kind of down-flow reactor, and regenerated catalyst flows downward by self gravitation after the solid particulate distributions plate distributes, and stock oil and catalyzer also flow to current downflow, thereby realizes the contact of agent oil.Because raw material contacts with the catalyzer following current, and catalyzer is dilute phase mutually, and density is lower, so the oily contact efficiency of agent is relatively poor, and feed stock conversion is lower.
USP5296131 has proposed a kind of circulation type down pipe short contact reactor types, regenerated catalyst forms an annular whereabouts " curtain " by conical-plug valve, stock oil hollow ring under the conical surface radially sprays, carry out cross-flow with stock oil and contact, react at annular down-flow reactor then.The mixing of agent oil has been strengthened in the cross-flow contact, but because catalyzer still is scattered for dilute phase, conversion of raw material is still lower.
For the solid catalyst system of distribution of routine dependence action of gravity, the catalyzer free-falling, when arriving in the agent oil contact area, the catalyzer linear speed is about 8-11m/s, and density of catalyst only is 50kg/m
3, be unfavorable for the catalytic cracking of heavy oil.At this point, USP5449496 has proposed to utilize degassing vessel to change the method for density of catalyst, by promoting gas linear speed and catalyzer length in the control degassing vessel to agent oil zone of action, the linear speed of solid catalyst remains on 2-8m/s when making catalyzer arrive agent oil zone of action, guarantees that density of catalyst is at 80-500kg/m
3, and stock oil sprays into reaction zone with the angle of 20-50 degree.Can make things convenient for the density of control catalyst like this at reaction zone, but gas-solid and flow to contact efficiency and the heat transfer efficiency that current downflow has weakened agent oil.
USP4985136, USP5462652 have introduced ultrashort contact MSCC patent Technology, and catalyzer flows downward with curtain, and " curtain " of catalyzer vertically passed in charging, and reaction product and levels of catalysts realize the gas-solid sharp separation by reaction zone.Catalyzer behind the part stripping does not carry out coke burning regeneration, but turns back to the catalyst mix device with the catalyst mix of holomorphosis, to increase the agent-oil ratio of reaction.Little spatial reaction zone and quick gas solid separation make MSCC technology reduce secondary reaction, have passed through the purpose product selectivity, obtain more lightweight oil.Though the MSCC technology has tentatively solved agent oil contact bottleneck problem, but still there are charging skewness, agent oil contact efficiency difference phenomenon.
USP5662868 has proposed the improved short contact structure of reactor of a kind of riser tube form, and the riser tube reaction times is controlled at 0.6-1.0s, and reaction is after goat's horn formula separator carries out gas solid separation, and the catalyzer after the separation advances stripper and carries out stripping.For preventing oil gas cracking once more in separating pipeline, be provided with chilling in a separator outlet.Though the USP5662868 patented method helps the transformation of riser tube reactive system, do not improve the axial backmixing phenomenon of oil gas and catalyzer.
USP5582712 has also proposed a kind of Desending catalytic cracking reactive system, improves catalyst concn by degassing vessel, and catalyzer relies on gravity to fall voluntarily, to realize the contact reacts of catalyzer and stock oil.Different with other short contact reactive systems, USP5582712 has proposed the two-stage riser renovation process, can reduce the equipment size of regeneration system rapidly so greatly.
USP5997726 has proposed a kind of special down pipe catalyzer and stock oil contact form, regenerated catalyst the storage tank degassing carry dense after, enter down pipe by the regeneration guiding valve.The down pipe entrance structure is one " expanding-contract-expand " form, at down pipe inlet a tapered thing is arranged, further carry when making catalyzer enter down pipe dense, and stock oil expansion section s with the level 10-20 angle cross-flow reaction that contacts with catalyzer that makes progress.Though the contact of agent oil has been strengthened in cross-flow contact, but still there is weakness such as agent oil contact efficiency difference.
Make a general survey of document and patent in the past, the short contact catalytic cracking technology is heavy industrialization not as yet at present, and its reason is mainly and does not resolve following gordian technique: the efficient contact technique of agent oil initial segment.The hot desk study of short contact Catalytic processes down pipe reactor be studies show that low major cause of transformation efficiency of residual oil is that the nozzle region density of catalyst is too low (only for 10kg/m
2), catalyzer fails to be mixed fully and contact with stock oil, and the optimum density of the initial agent oil of heavy oil fluid catalytic cracking contact segment catalyzer is 250～500kg/m
2
Summary of the invention
Main purpose of the present invention is at having defective and the deficiency that short contact catalyst cracker agent oil contact structures exist now, the required density of catalyst of rising agent oil contact segment heavy oil conversion, activator oil contact efficiency, a transformation efficiency of raising heavy oil.
The finish provided by the present invention 16-0 of exposure chamber comprises with lower member: cylindrical shell 10, inclined clapboard 16-7, vertical clapboard 16-4, gas distribution grid 16-10, collection chamber dividing plate 16-1, hydrocarbon ils nozzle 16-6, inclined-tube reaction section 5; Wherein, inclined clapboard, vertical clapboard and hydrocarbon ils nozzle are arranged on a side of the central axis of this cylinder shape finish exposure chamber; Inclined clapboard is fixed on inboard, cylindrical shell upper edge, with the angle γ of central axis be 30～60 °; Fixedly connected with the lower edge of inclined clapboard in the upper edge of vertical clapboard; Inclined clapboard and the vertical clapboard separated by spaces that gas distribution grid in this finish exposure chamber is above is two districts, i.e. district 16-5 He Er district 16-8; Inclined-tube reaction section 5 is arranged on the outside of two district 16-8; And the collection chamber divider upright is fixed on the gas distribution grid below, and with the separated by spaces below the gas distribution grid in the finish exposure chamber be and corresponding two collection chambers in the position in above-mentioned two districts, and each collection chamber is equipped with fluidizing medium ingress pipe 16-3,16-9; The hydrocarbon ils nozzle is fixedlyed connected with cylindrical shell and is passed vertical clapboard, and the angle α of itself and horizontal direction is 5～30 °; The sectional area along the vertical clapboard direction of the catalyst channels between vertical clapboard lower edge and the gas distribution grid 16-10 is 0.2～1A, and A is the cross-sectional area of down pipe reactor 4.
The present invention has following characteristics:
1, by the catalyzer dense-phase bed is set, guaranteed the initial required optimum catalyst density of contact segment of heavy oil fluid catalytic cracking agent oil, overcome the low shortcoming of present down pipe reactor finish exposure chamber territory density of catalyst, improved agent oil contact probability.
2,, and make regenerated catalyst be divided into two stocks not enter this two districts by setting up two separated regions in agent oil initial mixing district.Because entering the catalyzer in a district enters two districts, upwards flows by the passage under the vertical clapboard.The possible stagnant area of two district's inner catalysts has guaranteed that stock oil all contacts with live catalyst, effectively reduces the back-mixing of agent oil initial mixing district catalyzer.
3, the catalyzer in the district constantly flows to two districts by a district in a steady stream, has eliminated inner catalyst mobile dead band, two districts, makes in two districts to enter down pipe by the inclined-tube reaction section smoothly with catalyzer after stock oil contacts and react.Thereby the situation that can prevent the serious coking in initial mixing district of agent oil takes place.
Description of drawings
Fig. 1 is the synoptic diagram of the present invention in catalytic cracking reaction-regeneration system rapidly.
Fig. 2～4th, the structural representation of finish provided by the present invention exposure chamber.
Embodiment
Further specify the structure of finish provided by the present invention exposure chamber below in conjunction with accompanying drawing.
As shown in Figure 1, the finish provided by the invention 16-0 of exposure chamber is arranged between revivifier and the down pipe reactor 4, and its concrete structure as shown in Figure 2.If the diameter of down pipe reactor 4 is d, the diameter D=2～6d of finish exposure chamber then, its height H=3～8d.
As shown in Figure 2, inclined clapboard 16-7 and vertical clapboard 16-4 are set, and aforementioned barriers is divided into two districts with the finish exposure chamber: district 16-5 He Er district 16-8 in inside, finish exposure chamber.The medullary ray that inclined clapboard 16-7 passes the finish exposure chamber is fixed on the inboard, upper end of finish exposure chamber, and the angle γ of the central axis of this inclined clapboard and vertical direction is 30～60 °.Fixedly connected with the lower edge of inclined clapboard in the upper edge of vertical clapboard.Inclined clapboard is 1: 5 with vertical clapboard at the ratio of the height of vertical direction, preferred 1: 4.By vertical clapboard 16-4 the ratio S of cross-sectional area of separated district 16-5 He Er district 16-8
1/ S
2=0.25～1.0.
The top of finish exposure chamber links to each other with catalyst line 6, the diameter d of this catalyst line 6
1=0.5～1.2d (d is the diameter of down pipe reactor 4).The outside at the Er Qu 16-8 of finish exposure chamber is provided with inclined-tube reaction section 5, and this inclined-tube reaction section 5 links to each other with the inlet of down pipe reactor 4.The diameter d of inclined-tube reaction section 5
0=0.8～1.2d, the medullary ray of this inclined-tube reaction section are positioned at the plane that medullary ray constituted of the medullary ray and the 16-0 of finish exposure chamber of down pipe reactor 4, angle β=30～70 of itself and vertical direction °.Between the medullary ray of the 16-0 of finish exposure chamber and the medullary ray of down pipe reactor 4 apart from 1=3～10d.
Gas distribution grid 16-10 is positioned at the below in He Er district, a district.Evenly perforate on the gas distribution grid, percentage of open area is 2～15%, preferred 3～10%; The aperture of described perforate is 10～40mm, preferred 15～30mm.This gas distribution grid can be a level, also can be to recessed sphere or ellipsoid.
Vertical clapboard 16-4 is positioned on the gas distribution grid 16-10, and the space between vertical clapboard lower edge and the gas distribution grid 16-10 is a catalyst channels.This passage is 0.2～1A along the sectional area of vertical clapboard direction, and A is the cross-sectional area of down pipe reactor 4.
The bottom of gas distribution grid 16-10 is a collection chamber, collection chamber dividing plate 16-1 is vertically fixed on the gas distribution grid below, and be and corresponding two collection chambers of district 16-5 He Er district 16-8 with the separated by spaces below the gas distribution grid in the finish exposure chamber: collection chamber one 16-2 and collection chamber two 16-11, and these two districts are corresponding one by one with two districts of gas distribution grid top.Collection chamber one and collection chamber two are equipped with fluidizing medium ingress pipe 16-3 and 16-9.
This finish exposure chamber can be provided with 1～6 hydrocarbon ils nozzle 16-6.If 1 nozzle only is set, then the medullary ray of this nozzle is positioned at the plane that the medullary ray of the medullary ray of down pipe 4 and the 16-0 of finish exposure chamber constitutes, and with this plane in horizontal angle α be 5～30 °.If a plurality of nozzles are set, for example 2～6, then the medullary ray of one of them nozzle is positioned at the plane that the medullary ray of the medullary ray of down pipe 4 and the 16-0 of finish exposure chamber constitutes, and with horizontal angle α in this plane=5～30 °, and the equal intersection point of the medullary ray of the medullary ray by said nozzle and the 16-0 of finish exposure chamber of the medullary ray of all the other nozzles, and be that symmetry axis is along the circumferential direction evenly arranged with above-mentioned sea line.The medullary ray of this sea line and inclined-tube reaction section 5 is at the difference of altitude Δ h=0.5～1d of ingress.
The mode of operation of catalytic cracking of oil provided by the present invention exposure chamber is as follows: as shown in Figure 1, regenerated catalyst removes the gas of being carried secretly in degassing vessel 13, and the catalytic amount in the degassing vessel is as the criterion to keep the catalyzer needed impellent that normally flows downward.The catalyst recirculation amount is by 15 controls of regeneration guiding valve.Regenerated catalyst enters oil solution mixing chamber 16-0 by regeneration guiding valve 15 and by means of the effect of self gravitation.As shown in Figure 2, because the separation of inclined clapboard 16-7 and vertical clapboard 16-4, the catalyzer 30～70% that enters oil solution mixing chamber 16-0 enters a district 16-5, and the rest part catalyzer enters two district 16-8.Control is injected collection chamber one 16-2 and is entered the linear speed of the fluidizing medium in a district through gas distribution grid 16-10 by fluidizing medium ingress pipe 16-3, makes the catalyzer in the district reach the stabilization fluid state, and the bed density of catalyzer is 400～600Kg/m
3, and the passage that can waltz through below the vertical clapboard 16-4 flows into two districts.Meanwhile, control is injected collection chamber two 16-11 and is entered the linear speed of the fluidizing medium in two districts through gas distribution grid 16-10 by fluidizing medium ingress pipe 16-9, and the bed density that makes two district's inner catalysts is 250～500kg/m
2Hydrocarbon oil crude material injects two district's dense-phase bed through nozzle 16-6, contacts with catalyzer, vaporizes rapidly and reacts.The finish mixture enters in the down pipe reactor 4 by inclined-tube reaction section 5 and reacts.Catalyzer in one district constantly flows to two districts by a district in a steady stream, to eliminate inner catalyst mobile dead band, two districts.As shown in Figure 1, reacted finish mixture leaves down pipe 4 and enters in the settling vessel 3, and reaction oil gas separates rapidly under the effect of gas-solid separator 18 with catalyzer, and reaction oil gas is sent into subsequent separation system through pipeline 17, further is separated into various products; And the catalyzer of reaction back carbon deposit falls into settling vessel stripping stage 19, and the stripping medium injects through pipeline 20, with the catalyzer counter current contact, to remove the reaction oil gas that catalyzer is carried secretly.Catalyzer behind the stripping is sent into coke burning regeneration in the revivifier 8 through pipeline 21 to be generated and catalyzer riser tube 1, and the flow of reclaimable catalyst is by guiding valve 2 controls to be generated.Oxygen-containing gas enters revivifier through sparger 7, and regenerated flue gas is discharged through pipeline 9.Catalyzer after the regeneration is delivered in the degassing vessel 13 through pipeline 12, remove the flue gas that catalyzer carries secretly after, return the 16-0 of finish exposure chamber through guiding valve 15 and pipeline 6 and recycle.
Finish provided by the invention exposure chamber does not have special requirement to the catalyzer that is adopted, and any catalyzer in catalytic cracking field that is applicable to all can be used for the present invention.For example, the active ingredient of catalyst system therefor can be selected from: contain or do not contain Y type, HY type or USY type zeolite, β zeolite, the ZSM-5 zeolite of rare earth or in other supersiliceous zeolite with five-membered ring structure one or more.
Finish provided by the invention exposure chamber has no particular limits stock oil character, any hydrocarbon feed of catalytic cracking unit that is applicable to all can be used as raw material, for example, the mixture of long residuum, vacuum residuum, decompressed wax oil, deasphalted oil, wax tailings, hydrogenation tail oil, gasoline fraction, diesel oil distillate and above-mentioned two or more hydrocarbon ils.
The following examples will give further instruction to catalytic cracking of oil provided by the invention exposure chamber, but not thereby limiting the invention.
Embodiment 1
This example explanation: the applicable cases of finish provided by the invention exposure chamber on kitty cracker.
According to the constructional feature of finish provided by the present invention exposure chamber, on catalytic cracking middle-scale device as shown in Figure 1, test.Test raw materials used oil properties and see Table 1, the character of catalyst system therefor sees Table 2, and this catalyzer is by Lanzhou oil-refining chemical company catalyst plant industrial production, and trade names are LV-23.
The structural dimensions of finish exposure chamber is as follows in the used middle-scale device of test: the diameter d=20mm of down pipe reactor, the diameter D=70mm of finish exposure chamber, its height H=100mm.Vertical clapboard is S1: S2=0.4 with the ratio that agent oil exposure chamber is separated into cross-sectional area: two parts of 1.The diameter d of inclined-tube reaction section
0=20mm, angle β=45 of itself and vertical direction °.The gas distribution grid of agent oil exposure chamber is an ellipsoid shape, and the percentage of open area of this gas distribution grid is 8%.The sectional area of the lower edge of vertical clapboard and the catalyst stream circulation passage between the gas distribution grid is 0.3 times of down pipe sectional area.The number of nozzle is 3, angle α=20 of each nozzle and horizontal direction °.
Main testing sequence is as follows: as shown in Figure 1, the regenerated catalyst in the degassing vessel 13 enters oil solution mixing chamber 16-0 by regeneration guiding valve 15 and by means of the effect of self gravitation.As shown in Figure 2, the catalyzer 40% that enters oil solution mixing chamber 16-0 enters a district 16-5, and the rest part catalyzer enters two district 16-8.Beds density in one district is 520Kg/m
3, the beds density in two districts is 380kg/m
2Hydrocarbon oil crude material injects two district's dense-phase bed through three nozzle 16-6, contacts with catalyzer, vaporizes rapidly and reacts.The finish mixture enters in the down pipe reactor 4 by inclined-tube reaction section 5 and reacts.Catalyzer in one district constantly flows to two districts by a district in a steady stream.As shown in Figure 1, reacted finish mixture leaves down pipe 4 and enters in the settling vessel 3, and reaction oil gas separates rapidly under the effect of gas-solid separator 18 with catalyzer, and reaction oil gas is sent into subsequent separation system through pipeline 17, further is separated into various products; And the catalyzer of reaction back carbon deposit falls into settling vessel stripping stage 19, and the stripping medium injects through pipeline 20, with the catalyzer counter current contact, to remove the reaction oil gas that catalyzer is carried secretly.Catalyzer behind the stripping is sent into coke burning regeneration in the revivifier 8 through pipeline 21 to be generated and catalyzer riser tube 1, and the flow of reclaimable catalyst is by guiding valve 2 controls to be generated.Catalyzer after the regeneration is delivered in the degassing vessel 13 through pipeline 12, remove the flue gas that catalyzer carries secretly after, return the 16-0 of finish exposure chamber through guiding valve 15 and pipeline 6 and recycle.
Comparative Examples 1
This Comparative Examples explanation: on the Desending catalytic cracking middle-scale device that does not adopt oil solution mixing chamber of the present invention of routine, adopt stock oil, catalyzer and the reaction conditions resulting test-results identical with embodiment 1.
Main testing sequence is as follows: stock oil is after the process furnace preheating, inject the top of down-flow reactor by the high-efficient atomizing nozzle, contact with high temperature catalyst and react from revivifier, oil gas and catalyzer separate rapidly after by down-flow reactor, oil gas is sent into subsequent separation system through transfer line and is carried out product separation, the long-pending catalyzer that coke is arranged is sent into the revivifier coke burning regeneration after the reaction behind the water vapour stripping, and the catalyzer after the regeneration is delivered to reactor cycles and used.Various products are measured, analyze.
Embodiment 1 and Comparative Examples 1 resulting test-results are listed in table 3.As can be seen from Table 3: after adopting oil solution mixing chamber provided by the invention, light oil yield improves 4 percentage points, and coke yield reduces by 1.6 percentage points.
Table 1
| Stock oil | VGO | VR | VGO+40％VR |
| Density (20 ℃), g/cm 3 | 0.8765 | 0.9553 | 0.9064 |
| Kinematic viscosity (100 ℃), mm 2/s | 4.39 | - | - |
| Condensation point, ℃ | 31 | - | - |
| Molecular weight | 317 | - | - |
| Carbon residue, heavy % | 0.20 | 12.4 | 5.09 |
| Elementary composition, heavy % | |||
| C | 86.44 | 86.55 | 86.50 |
| H | 13.13 | 12.01 | 12.67 |
| Metal content, ppm | |||
| Ni | 0.41 | 26.3 | 10.82 |
| V | 0.76 | 19.3 | 8.20 |
| Boiling range, ℃ | |||
| Initial boiling point | 233 | - | - |
| 5％ | 356 | - | - |
| 10％ | 383 | - | - |
| 30％ | 422 | - | - |
| 50％ | 447 | - | - |
| 70％ | 469 | - | - |
| Characterization factor | 12.13 | 12.21 | 12.19 |
Table 2
| Physical properties | |
| Specific surface area, m 2/g | 92 |
| Pore volume, ml/g | 0.33 |
| Apparent density, g/cm 3 | 0.83 |
| Metal content, ppm | |
| V | 2000 |
| Ni | 2800 |
| Size composition, heavy % | |
| 0～40μm | 11 |
| 40～80μm | 51 |
| ＞80μm | 38 |
| The regenerated catalyst micro-activity | 58 |
Table 3
| Comparative Examples | Embodiment | |
| Temperature of reaction, ℃ | 500 | 500 |
| Reaction pressure (g), kPa | 110 | 110 |
| Raw material preheating temperature, ℃ | 200 | 200 |
| The regenerator temperature, ℃ | 700 | 700 |
| Agent- | 15 | 15 |
| Reaction times, s | 0.68 | 0.50 |
| Product distributes, heavy % | ||
| Dry gas | 3.5 | 2.97 |
| Liquefied gas | 13.26 | 12.27 |
| Gasoline | 41.86 | 41.08 |
| Diesel oil | 24.38 | 30.24 |
| Heavy oil | 8.0 | 6.3 |
| Coke | 8.14 | 6.51 |
| Loss | 0.86 | 0.63 |
Claims (10)
1, a kind of catalytic cracking of oil exposure chamber is characterized in that this finish exposure chamber (16-0) comprises with lower member: cylindrical shell (10), inclined clapboard (16-7), vertical clapboard (16-4), gas distribution grid (16-10), collection chamber dividing plate (16-1), hydrocarbon ils nozzle (16-6), inclined-tube reaction section (5); Wherein, inclined clapboard, vertical clapboard and hydrocarbon ils nozzle are arranged on a side of the central axis of this cylinder shape finish exposure chamber; Inclined clapboard is fixed on inboard, cylindrical shell upper edge, with the angle γ of central axis be 30～60 °; Fixedly connected with the lower edge of inclined clapboard in the upper edge of vertical clapboard; Inclined clapboard and the vertical clapboard separated by spaces that gas distribution grid in this finish exposure chamber is above is two districts, i.e. He Er district, a district (16-5) (16-8); Inclined-tube reaction section (5) is arranged on the outside of two districts (16-8); And the collection chamber divider upright is fixed on the gas distribution grid below, and with the separated by spaces below the gas distribution grid in the finish exposure chamber be and corresponding two collection chambers in the position in above-mentioned two districts, and each collection chamber is equipped with fluidizing medium ingress pipe (16-3,16-9); The hydrocarbon ils nozzle is fixedlyed connected with cylindrical shell and is passed vertical clapboard, and the angle α of itself and horizontal direction is 5～30 °; The sectional area along the vertical clapboard direction of the catalyst channels between vertical clapboard lower edge and the gas distribution grid (16-10) is 0.2～1A, and A is the cross-sectional area of down pipe reactor (4).
2, according to the finish exposure chamber of claim 1, it is characterized in that the diameter D=2～6d of described finish exposure chamber, its height H=3～8d, d is the diameter of down pipe reactor (4).
3,, it is characterized in that described inclined clapboard and vertical clapboard are 1: 5 at the ratio of the height of vertical direction according to the finish exposure chamber of claim 1.
4, according to the finish exposure chamber of claim 1, it is characterized in that described inclined clapboard and the vertical clapboard separated by spaces that gas distribution grid in this finish exposure chamber is above is He Er district, a district (16-5) (16-8), and the ratio S of the cross-sectional area in He Er district, a district
1/ S
2=0.25～1.0.
5,, it is characterized in that the diameter d of described inclined-tube reaction section (5) according to the finish exposure chamber of claim 1
o=0.8～1.2d, d are the diameter of down pipe reactor (4); The medullary ray of this inclined-tube reaction section is positioned at the plane that medullary ray constituted of medullary ray and finish exposure chamber (16-0) of down pipe reactor, and with angle β=30～70 of vertical direction °.
6, according to the finish exposure chamber of claim 1, it is characterized in that between the medullary ray of the medullary ray of described finish exposure chamber (16-0) and down pipe reactor (4) apart from 1=3～10d, d is the diameter of down pipe reactor (4).
7, according to the finish exposure chamber of claim 1, it is characterized in that described gas distribution grid can be a level, also can be to recessed sphere or ellipsoid; And the percentage of open area of gas distribution grid is 2～15%, and the aperture of perforate is 10～40mm.
8, according to the finish exposure chamber of claim 7, the percentage of open area that it is characterized in that described gas distribution grid is 3～10%, and the aperture of perforate is 15～30mm.
9,, it is characterized in that described vertical clapboard (16-4) is positioned on the gas distribution grid (16-10) according to the finish exposure chamber of claim 1.
10,, it is characterized in that described hydrocarbon ils nozzle (16-6) is provided with 1～6 according to the finish exposure chamber of claim 1; When 1 nozzle was set, the medullary ray of this nozzle was positioned at the plane that the medullary ray of the medullary ray of down pipe (4) and finish exposure chamber (16-0) constitutes, and with this plane in horizontal angle α be 5～30 °; When 2～6 nozzles are set, the medullary ray of one of them nozzle is positioned at the plane that the medullary ray of the medullary ray of down pipe (4) and finish exposure chamber (16-0) constitutes, and with horizontal angle α in this plane=5～30 °, and the equal intersection point of the medullary ray of the medullary ray by said nozzle and finish exposure chamber (16-0) of the medullary ray of all the other nozzles, and be that symmetry axis is along the circumferential direction evenly arranged with above-mentioned sea line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02116286 CN1203157C (en) | 2002-03-29 | 2002-03-29 | Contact chamber for catalytic cracking of oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02116286 CN1203157C (en) | 2002-03-29 | 2002-03-29 | Contact chamber for catalytic cracking of oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1448467A CN1448467A (en) | 2003-10-15 |
| CN1203157C true CN1203157C (en) | 2005-05-25 |
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ID=28680675
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02116286 Expired - Fee Related CN1203157C (en) | 2002-03-29 | 2002-03-29 | Contact chamber for catalytic cracking of oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1203157C (en) |
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2002
- 2002-03-29 CN CN 02116286 patent/CN1203157C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| CN1448467A (en) | 2003-10-15 |
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