CN1853768A - Improved petroleum hydrocarbon catalytic cracking reactor - Google Patents
Improved petroleum hydrocarbon catalytic cracking reactor Download PDFInfo
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- CN1853768A CN1853768A CN 200510068166 CN200510068166A CN1853768A CN 1853768 A CN1853768 A CN 1853768A CN 200510068166 CN200510068166 CN 200510068166 CN 200510068166 A CN200510068166 A CN 200510068166A CN 1853768 A CN1853768 A CN 1853768A
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Abstract
An improved catalytic cracking reactor for petroleum hydrocarbon is composed of a raw material feeding nozzle and a lift-tube reactor. The included angle between the axis of said nozzle and the axis of said reactor is greater than 90 deg but less than or equal to 180 deg, resulting in high atomizing level of raw hydrocarbon.
Description
Technical field
The invention belongs to the catalyst cracker of petroleum hydrocarbon under the situation that does not have hydrogen, more particularly, is a kind of improved petroleum hydrocarbon catalytic conversion reactor.
Background technology
In catalytic cracking process, the big molecule petroleum hydrocarbon of heavy is little molecule petroleum hydrocarbon by cracking.Generally, the hydrocarbon raw material after the preheating is injected in one or more reaction zones through atomizing, contacts and be vaporized into oil gas with the fluidized catalyst particle flux therein, and the oil gas molecule under the effect of catalyst cracking reaction takes place subsequently.In the course of reaction, coke has covered the acid centre on the catalyst at the catalyst particle surface deposition gradually as one of product, catalyst is lost activity gradually, contain burning-off coke in Pd/carbon catalyst enters the renewing zone after stripping oil gas the high-temperature oxygen-enriched environment, recover active, be circulated back to reaction zone then, again carry out haptoreaction with hydrocarbon raw material, product enters subsequent separation system and forms product or partial reflux to reaction zone.
Discover that the way of contact of hydrocarbon feed and fluidized catalyst particle flux is very big to the product distribution influence of catalytic cracking reaction in the riser reaction zone.Along with the change day by day of catalytically cracked material is heavy, byproduct such as coke and dry gas productive rate increases gradually in the product.The instantaneous even contact of hydrocarbon feed and fluidized catalyst particle flux can reduce thermal response in theory, reduced the productive rate of coke and dry gas.The instantaneous even contact of hydrocarbon raw material and fluidized catalyst particle flux requires on the riser cross-section of feed entrance point, and the hydrocarbon raw material whole catalyst particle streams on the cross section therewith carries out instantaneous contact.But accomplishing the whole catalyst contacts on the instantaneous cross section therewith, is impossible in actual applications.The existence of non-instantaneous even contact has influenced the distribution of product to a certain extent, for example the productive rate of dry gas and coke.
The abundant atomizing of hydrocarbon feed can improve the effect that contacts between hydrocarbon feed and catalyst particle.The even contact degree of hydrocarbon feed and catalyst particle stream depends in part on the drop size of hydrocarbon feed.When enough hour of charging drop (usually less than 100 microns), just can think approx that hydrocarbon feed has just fully been atomized before the contact catalyst particle.Fully atomizing can increase the total surface area of charging drop, thereby increases the probability that the hydro carbons drop contacts with catalyst particle, promotes feed liquid to enter in the duct of catalyst pellets sub-surface simultaneously and carries out catalytic cracking reaction.US 3,547, and 805 disclosed by the mixing of steam and hydrocarbon raw material, thus the method that hydrocarbon raw material is atomized.US 3,152, and 065 describes feed nozzle is made up of the sleeve pipe of the different design of a Gent, and steam is by the interior pipe of sleeve pipe by the outer tube of sleeve pipe for hydrocarbon raw material, and two media mixes at the end of sleeve pipe and collides and atomize.Similar US4,523,987, US5,622,677, US4,578,183 and method or equipment such as US 5,318,691, adopt undergauge or venturi effect, vortex effect, vapour-liquid two-phase to mix the atomizing that promotes hydrocarbon feed usually.This requires the hydro carbons drop to have higher speed when leaving nozzle, usually between 30m/s-120m/s, and need realize by increasing feed pressure at a high speed, generally, the pump that this need add or other equipment provide, thereby have increased the energy consumption and the maintenance cost of catalytic cracking unit.And, just reaching fully before contact catalyst, atomizing also exists shortcoming, promptly the liquid-drop diameter owing to hydrocarbon feed diminishes, himself kinetic energy also reduces thereupon, thereby reduced the penetration power of hydrocarbon feed on riser cross-section, can not touch all catalyst particles that flow on this cross section fully.
The movement velocity of raising catalyst particle stream also can be improved the effect that contacts between hydrocarbon feed drop and the catalyst particle stream.Common equipment or method be by use pre-lifting medium accelerator activator in riser on the speed that flows, impel catalyst particle stream to quicken gradually, near the even flow effect of piston flow, hydrocarbon feed can be injected on the catalyst particle equably; Simultaneously pre-lift technique makes it when the contact hydrocarbon feed by improving the upwards flow velocity of catalyst particle, keep high momentum with bump not by atomizing fully, hydrocarbon feed drop that diameter is bigger.US4,479,870 have disclosed method or the equipment that the using gases medium promotes catalyst in advance.Yet the movement velocity of catalyst particle must be limited within the scope of catalytic cracking special process needs, because the movement velocity of catalyst particle also has influence on the time of staying of hydrocarbon raw material in riser reactor; Simultaneously, in actual applications, landing, the air-teturning mixed phenomenon of catalyst particle in riser reactor also makes catalyst particle stream be difficult to reach the perfect condition that piston flow flows.
The direction that sprays into of hydrocarbon feed also has a significant impact solid-liquid contact effect.US4,717,467 have disclosed the method and apparatus that non-radial direction sprays into hydrocarbon feed.US5554341, US5173175, US3654140 and US5139748 have disclosed method or the equipment that radially sprays into hydrocarbon feed, and series of spray nozzles is disposed on the circumferential plane of riser tube wall, and they point to the radial center of riser simultaneously.Such technology or equipment make hydrocarbon feed drop formation curtain on the one hand, strengthen the effect that contacts between hydrocarbon feed drop and catalyst particle stream; Can not make the bigger hydrocarbon feed drop of atomizing fully, diameter at riser radial center place bump on the other hand yet, reach the effect of atomizing fully to impel it to be split into the littler drop of diameter.
The angle of feed nozzle also is to influence hydrocarbon feed to contact one of influence factor of effect with catalyst particle stream.Common technology or equipment are to make nozzle point to the flow direction of catalyst particle stream at a certain angle, i.e. the direction that makes progress of directed in orthogonal at a certain angle in catalytic cracking riser device usually.US6,613,290 point out hydrocarbon raw material spray into angle should with axially vertically upward direction be 40 °～65 °, surpass 65 ° and may cause hydrocarbon raw material to be sprayed onto on the riser inwall.Hydrocarbon feed this sprays into mode or the equipment that the angle directed in orthogonal makes progress can promote that on the one hand oil gas forms the short time of staying; Can prevent landing, the back-mixing of catalyst particle on the other hand, thereby prevent cracking reaction.Yet the flow direction that sprays into direction and fluidized catalyst particle flux of hydrocarbon raw material is identical or become low-angle that disadvantageous aspect is also arranged.The speed that sprays into of hydrocarbon raw material is generally between 30m/s-120m/s, with 30m/s is example (the vertical direction component is between the 13-23m/s), and catalyst linear speed before the hydrocarbon feed nozzle in the riser pipe is generally about 10-12m/s, maximum is no more than 15m/s, and the speed difference between the two causes the long time of catalyst and hydrocarbon feed parallel motion just can contact and carries out the heat transmission.US5,139,748 have disclosed the hydrocarbon raw material horizontal direction or have been 25 ° of method or equipment that spray into riser with horizontal direction.US6,042,717 and US6,627,161 have disclosed hydrocarbon raw material by special equipment, and promptly some little atomizer levels spray into the method for riser.The level of hydrocarbon feed sprays into direction and will avoid hydrocarbon feed to be directly injected on the riser inwall as far as possible.US5,139,748 are provided with particular component at riser axle center place, make hydrocarbon raw material clash into this parts, thereby prevent that hydrocarbon feed is directly injected on the riser inwall.US6,042,717 and US6,627,161 have adopted the special construction small nozzle to spray into velocity level's durection component to reduce hydrocarbon feed, thereby prevent that hydrocarbon feed is directly injected on the riser inwall.
In sum, though those skilled in the art are carrying out unremitting research and exploration at aspects such as feeding manner, atomizing effect, structure of reactor, can realize preferably that up to now the technical scheme of the instantaneous even contact of catalytic cracking of oil do not appear in the newspapers so far as yet.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of improved petroleum hydrocarbon catalytic cracking reactor, in order to improve contacting effect, obtaining even more ideal product and distribute and product property of petroleum hydrocarbon raw material and catalyst.
Improved petroleum hydrocarbon catalytic cracking reactor provided by the present invention comprises feed nozzle and the riser reactor of fixedlying connected and being connected with feed nozzle; Wherein, described feed nozzle is arranged on the feed zone of hole enlargement of riser reactor, and the central axis of the central axis of feed nozzle and riser reactor 90 °＜α of the formed angle of direction≤180 ° vertically upward.
Compared with prior art, beneficial effect of the present invention is mainly reflected in following aspect: the present invention uses the pre-medium that promotes that catalyst is carried out preaceleration at the pre lift zone of riser, and catalyst particle stream is upwards flowed vertically.At the feed zone of riser reactor, plurality of nozzles is arranged symmetrically on the riser tube wall of hole enlargement in the form of a ring, and these nozzles are 90 °～180 ° angle sensing riser central shaft to flow mobile axial direction vertically upward with catalyst particle.Hydrocarbon feed sprays into riser with previously described angle after atomizing in advance through nozzle, this moment the hydrocarbon feed droplet on the direction of motion, have vertically downward component and the component of horizontal movement, and catalyst particle stream has component motion vertically upward, catalyst particle stream clashes at place, riser axle center with the hydrocarbon feed drop, thereby impels the hydrocarbon feed drop further to split into the littler drop of diameter.Simultaneously, hydrocarbon feed drop and catalyst particle head-on collision back make hydrocarbon feed drop division and gasification rapidly by momentum-exchange and exchange heat, and all catalyst particles of this cross-section contact with hydrocarbon feed in the riser thereby impel.Because the head-on collision effect between hydrocarbon feed droplet and catalyst particle makes the hydrocarbon feed droplet split into the littler drop of diameter, increased hydrocarbon feed total surface area, quickened the exchange heat process, make the instantaneous possibility that is gasificated as of hydrocarbon feed drop.In front under the comprehensive function of a plurality of steps of Miao Shuing, hydrocarbon feed is gasified by instantaneous height and mixes with catalyst particle, thereby realize the instantaneous even contact of hydrocarbon feed and catalyst particle, shortened catalyst and mixed needed finish length of mixing with hydrocarbon feed.
Hydrocarbon feed is very big to the influence that the catalytic cracking reaction product distributes with the instantaneous even contact degree that catalyst mixes contact mutually.Under the perfect condition, the hydrocarbon feed drop should be in all catalyst particle even contact of passing through on instantaneous and the riser feed entrance point cross section.Under conventional catalyst cracked charge mode, the hydrocarbon feed drop moves upward along riser is parallel with catalyst particle, and speed difference between the two causes the two to contact and needs the regular hour, so instantaneous even contact is impossible.The existence of non-homogeneous contact has influenced the character of catalytic cracking reaction product, the especially productive rate of byproduct such as coke and dry gas.
Description of drawings
Fig. 1 is the structural representation of improved riser reactor provided by the present invention.
Fig. 2 is the structural representation of riser reactor feed zone of the present invention.
Fig. 3 is the schematic diagram of riser reactor feed zone of the present invention.
Fig. 4 is the top cross-sectional view of riser reactor feed zone of the present invention.
Fig. 5 is the side cutaway view of riser reactor feed zone of the present invention.
The specific embodiment
Further specify improved petroleum hydrocarbon catalytic cracking reactor provided by the present invention below in conjunction with accompanying drawing, but therefore the present invention is not subjected to any restriction.
As shown in Figure 1, catalyst after the regeneration is circulated back to the pre lift zone 8 of riser reactor 3 bottoms through regeneration standpipe 11, the pre-medium 10 that promotes sprays into riser pre lift zone 8 by distributor 9, drive catalyst particle and quicken to move upward, make catalyst enter the feed zone 12 that is positioned at the pre lift zone downstream by pre lift zone.The present invention does not have special restriction for the setting of feed zone, can determine the position of feed zone and the relative length of feed zone according to the concrete condition of FCC apparatus.Generally speaking, feed zone is positioned at the bottom of riser reactor, for example, feed zone can be positioned at the 5-50% place (lower end with riser is a starting point) of riser effective length, be preferably placed at the 6-40% place of riser effective length, further be preferably placed at the 7-35% place of riser effective length.The length of feed zone generally accounts for the 5-30% of riser effective length, preferred 5-25%, further preferred 6-22%.
In riser reactor provided by the present invention, the diameter of described feed zone is 1.1-3 with the ratio of the average diameter of the non-feed zone of riser reactor: 1, and preferred 1.2-2.5: 1, further preferred 1.2-2: 1.On FCC riser reactor of the present invention, also can implement sectional feeding, for example, 2-6 above-mentioned feed zone can be set, 2-4 feed zone preferably is set.In concrete application process, can also different feed zones be set according to the character of petroleum hydrocarbon raw material, for example, the feed zone that has adopts the hole enlargement design, and the not hole enlargement of feed zone that has is as long as can guarantee to obtain comparatively desirable finish contact effect.As shown in Figure 1, catalyst particle enters the feed zone 12 of hole enlargement from the lower end, and deceleration moves upward, and leaves and quickens again behind this feed zone to move upward.A series of feed nozzles 7 are arranged on the feed zone in the form of a ring symmetrically.
As shown in Figure 1, hydrocarbon raw material 5 and atomizing steam 6 pressurized backs are by being injected in the riser feed zone from series of spray nozzles 7.Hydrocarbon raw material mixes mutually with fluidisation attitude catalyst particle after by high atomisation and carries out heat exchange and gasify, and the oil gas of generation continues to move upward.Oil gas is in the process that moves upward along riser 3, and under the effect by catalyst, the big molecule in the oil gas is cracked into little molecule oil product, and simultaneously coke produces and gradually at the catalyst particle surface deposition.Oil gas and catalyst motion enter reactor 14 and carry out further catalytic cracking reaction therein from distributor 18 behind riser 3 tops.In reactor 14, oil gas and catalyst particle are by the centrifugation of primary cyclone 20 and secondary cyclone 21, and oil gas enters into collection chamber 22 and enters into follow-up piece-rate system by oil transfer line 23; Catalyst particle is got back to the stripper 16 of reactor 14 bottoms from cyclone dip-leg 19 under the centrifugation of a series of cyclone separators.Stripped vapor 4 enters into stripper from the distribution grid 15 of stripper 16 bottoms, and the oil-containing catalyst particle contact by chevron shaped baffle plate 17 upwards flows and flows downward together strips the entrained oil gas of catalyst particle.Enter in the regenerative system from regeneration standpipe 25 through steam stripped catalyst particle, finish once circulation.
As shown in Figure 2, the central axis of feed nozzle and the central axis of riser reactor be 90 °＜β of the formed angle of direction≤180 ° vertically upward, preferred 110 °＜β≤180 °, further preferred 130 °＜β＜155 °.The present invention is not particularly limited for the position that specifically is provided with of feed nozzle on feed zone, feed nozzle both can be arranged on the reducing position of feed zone as shown in Figure 1, also can be arranged on the isometrical sidewall of feed zone, as long as can access desirable finish contact effect.It is emphasized that, on the riser reactor each layer feed nozzle all needs to be provided with symmetrically, the central axis of each feed nozzle and the central axis of the riser reactor formed angle of direction vertically upward preferably equate, so that the central axis of each feed nozzle is intersected on the central axis of riser reactor.
Pre-lift technique makes catalyst realize fluidized particles stream mode, the final type of flow that forms approximate piston flow by the acceleration to catalyst particle.The type of flow of catalyst particle stream between hydrocarbon feed drop and catalyst particle to contact influential effect very big.On the one hand, the approximate piston flow type of flow of catalyst can make the hydrocarbon feed drop clash into catalyst particle equably; On the other hand, have bigger momentum thereby the employing of pre-lift technique makes catalyst particle have higher linear speed, catalyst particle is divided the hydro carbons drop when clash into the hydrocarbon feed drop becomes the littler drop of diameter.The present invention is unqualified to pre-lifting medium, and steam is a kind of well pre-medium that promotes.In implementation of the present invention, as shown in Figure 2, regenerated catalyst is entered the bottom of riser pre lift zone 8 by regeneration standpipe 11, the motion linear speed that the catalyst particle of this moment makes progress is zero or negative value, the pre-medium 10 that promotes is sprayed in the riser pre lift zone 8 by pre-lifting dielectric distribution device 9, drives catalyst particle and quickens gradually to move upward.
The pre-atomization technique of nozzle can make hydrocarbon feed be atomized to be the smaller drop of diameter.At first be that bump by gas-liquid two-phase under the high pressure makes the liquid phase division become the drop of less diameter.As shown in Figure 5, hydrocarbon feed is entered into the hybrid chamber 38 of nozzle by pipeline 37; Gas phase media (being generally steam) by pipeline 36 high velocity jet in the hybrid chamber 38 of nozzle; The energy that gas phase media brought splits into less drop with the liquid phase hydrocarbon feed, and this moment, the gas-liquid two-phase height mixed, and became the mixture with high momentum.Simultaneously, the rapid undergauge of hybrid chamber 38 and narrow and small jet expansion 31 make nozzle form the venturi effect, have very big momentum when making gas-fluid two-phase mixture leave nozzle, further impel the division of liquid phase drop.
Being provided with of nozzle has decisive influence to the effect that contacts between hydrocarbon feed and catalyst particle stream.In implementation of the present invention, shown in the β angle of Fig. 2, hydrocarbon feed sprays into the direction of riser and the flow direction of catalyst particle stream is than wide-angle.This wide-angle sensing mode of nozzle makes hydrocarbon feed spray into riser through the pre-atomizing back of nozzle with previously described angle, make the hydrocarbon feed droplet have movement velocity component vertically downward, and catalyst particle stream have component motion vertically upward.In implementation of the present invention, the linear speed that the hydrocarbon feed drop has vertically downward is about 13～30m/s, and the linear speed 0～23m/s of level.Like this, the relative motion linear speed between catalyst particle and hydro carbons drop is between 13～45m/s, and catalyst particle and hydrocarbon feed drop can be at instantaneous mutual bumps.Thereby catalyst particle stream impels the hydrocarbon feed droplet further to split into the littler drop of diameter with the hydrocarbon feed droplet in the head-on collision of place, riser axle center.Simultaneously, pass through exchange heat at hydrocarbon feed droplet and catalyst particle head-on collision back, all catalyst particles of this cross-section contact with hydrocarbon feed in the riser thereby the rapid gasification of hydrocarbon feed droplet makes.Because the collision effect between hydrocarbon feed droplet and catalyst particle makes the hydrocarbon feed droplet split into the littler drop of diameter, thus increased hydrocarbon feed total surface area, quickened the exchange heat process, make the instantaneous atomizing of hydrocarbon feed become possibility.
In implementation of the present invention, as shown in Figure 4, some feed nozzles are symmetrically distributed on the tube wall at riser feed zone reducing position, and it points to all aims at the B point of riser central axis.The symmetrical distribution of feed nozzle and aim at the horizontal component that any mode of riser central axis can cancel out each other or reduce the hydrocarbon feed drop on the one hand avoids hydrocarbon feed to be ejected on the riser tube wall.Can also not make simultaneously and clash the hydrocarbon feed drop mutually in the head-on collision of riser central axis, utilize momentum hydrocarbon feed drop division the becoming littler drop of diameter with catalyst particle.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Embodiment 1
Present embodiment explanation: adopt the present invention can make catalyst particle and the instantaneous even contact of hydrocarbon raw material, distribute thereby improve product.
On catalytic cracking middle-scale device as shown in Figure 1, test.Main test procedure is as follows: promote steam in advance and inject from the bottom of riser reactor, raw material A (its character is as shown in table 1) is through the feed zone of feed nozzle injecting lift pipe reactor.The central axis of feed nozzle and the formed angle of the central axis of riser reactor are 125 °.Feedstock oil with regeneration after catalyst MLC-500 (its character is as shown in table 2) contact, react, the oil gas of generation and reacted catalyst upwards enter settler; Separating reaction oil gas and reacted catalyst, reaction oil gas is sent into subsequent separation system, further is separated into various products; And reacted catalyst is sent into the regenerator coke burning regeneration behind stripping; Catalyst after the regeneration returns riser reactor and recycles.
Comparative Examples 1
For implementation result of the present invention is described, in Comparative Examples 1, adopt feedstock oil identical and catalyst and identical reaction condition to compare test with embodiment 1.The angle of the central axis of the hydrocarbon oil feed nozzle that this contrast test adopted and the central axis of riser reactor is 45 °, and not hole enlargement of feed zone.Main operating condition and result of the test see Table 3.As can be seen from Table 3, behind employing the present invention, the productive rate of light naphthar, liquefied gas is greatly improved than Comparative Examples 1, has increased by 2.5 heavy % and 1.7 heavy % respectively, and heavy oil has reduced by 2.0 heavy %.
Embodiment 2
Present embodiment explanation: adopt the present invention can make catalyst particle and the instantaneous even contact of hydrocarbon raw material, distribute thereby improve product.
Test on the catalytic cracking middle-scale device of the riser of employing feed zone hole enlargement as shown in Figure 1.Main test procedure is as follows: promote the pre lift zone injection of steam from the riser reactor bottom in advance, raw material A (its character is as shown in table 1) is through feed nozzle injecting feeding section.The central axis of feed nozzle and the formed angle of the central axis of riser reactor are 155 °.Catalyst MLC-500 (its character is as shown in table 2) after feedstock oil and the regeneration contacts, reacts, and the oil gas of generation and the reacted catalyst riser reactor of upwards flowing through enters settler; Separating reaction oil gas and reacted catalyst, reaction oil gas is sent into subsequent separation system, further is separated into various products; And reacted catalyst is sent into the regenerator coke burning regeneration behind stripping; Catalyst after the regeneration returns riser reactor and recycles.
Comparative Examples 2
Adopt US6,613,290 described methods, and utilize petroleum hydrocarbon raw material described in the embodiment 1 and catalyst to test resulting result.Main operating condition and product distribution situation are referring to table 4.As can be seen from Table 4, the productivity ratio US6 of light naphthar of the present invention and liquefied gas, 613,290 described methods are greatly improved, and have increased by 5.3 heavy % and 1.0 heavy % respectively, and heavy oil has reduced by 4.1 heavy %.Therefore, the economic benefit that the present invention brought will be very significant.
Table 1
| The feedstock oil title | A |
| Density, g/cm 3 | 0.8764 |
| Kinematic viscosity, mm 2/s 80℃ | 20.39 |
| 100℃ | 12.06 |
| Condensation point, ℃ | ＞50 |
| Element is formed, heavy % | |
| C | 86.70 |
| H | 13.48 |
| S | 0.13 |
| N | 0.13 |
| Group composition, heavy % | |
| Saturated hydrocarbons | 75.0 |
| Aromatic hydrocarbons | 19.8 |
| Colloid | 5.2 |
| Asphalitine | ＜0.1 |
| Boiling range, ℃ | |
| Initial boiling point | 246 |
| 5％ | 402 |
| 10％ | 430 |
| 30％ | 482 |
| 50％ | 519 |
| 70％ | 573(75.2％) |
| Distillation yield (350 ℃), % | 1.5 |
| Distillation yield (500 ℃), % | 39.4 |
| Liquid temperature＞400 ℃, % | 61.6(538℃) |
Table 2
| Catalyst | MLC-500* |
| Chemical composition, heavy % | |
| Al 2O 3 | 44.7 |
| Fe 2O 3 | 0.38 |
| Physical property | |
| Specific area, m2/g | 203 |
| Pore volume, cm 3/g | 2.14 |
| Apparent density, g/cm 3 | 0.7921 |
| Size consist, % | |
| 0～40 micron | 8.5 |
| 0～80 micron | 66.3 |
| 0～110 micron | 87.2 |
| 0～150 micron | 95.9 |
* MLC-500 is trade names, by Sinopec Shandong catalyst plant industrial production, MA=60.
Table 3
| Comparative Examples 1 | Embodiment 1 | |
| The angle of nozzle centre axis and riser central axis | 45° | 125° |
| Reaction temperature, ℃ | 510 | 510 |
| Reaction time, second | 4 | 4 |
| Oil ratio | 6 | 6 |
| Reaction pressure, kPa | 180 | 180 |
| Material balance, heavy % | ||
| Dry gas | 3.2 | 3.6 |
| Liquefied gas | 12.5 | 14.2 |
| Light naphthar | 30.3 | 32.8 |
| Heavy naphtha | 10.8 | 9.7 |
| Diesel oil | 17.2 | 16.3 |
| Heavy oil | 19.7 | 17.7 |
| Coke | 6.3 | 5.7 |
| Conversion ratio, heavy % | 63.1 | 66.0 |
Table 4
| Comparative Examples 2 | Embodiment 2 | |
| The angle of nozzle centre axis and riser central axis | / | 155° |
| Reaction temperature, ℃ | 520 | 520 |
| Reaction time, second | 5 | 5 |
| Oil ratio | 6 | 6 |
| Reaction pressure, kPa | 200 | 200 |
| Material balance, heavy % | ||
| Dry gas | 3.6 | 3.9 |
| Liquefied gas | 13.1 | 14.1 |
| Light naphthar | 29.3 | 34.6 |
| Heavy naphtha | 11.8 | 9.5 |
| Diesel oil | 16.6 | 15.7 |
| Heavy oil | 18.8 | 14.7 |
| Coke | 6.8 | 7.5 |
| Conversion ratio, heavy % | 64.6 | 69.6 |
Claims (13)
1, a kind of improved petroleum hydrocarbon catalytic cracking reactor comprises feed nozzle and the riser reactor of fixedlying connected and being connected with feed nozzle; Wherein, described feed nozzle is arranged on the feed zone of hole enlargement of riser reactor, and the central axis of the central axis of feed nozzle and riser reactor 90 °＜α of the formed angle of direction≤180 ° vertically upward.
2, according to the reactor of claim 1, it is characterized in that the lower end with riser reactor is a starting point, described feed zone is positioned at the 5-50% place of riser effective length, and the length of feed zone accounts for the 5-30% of riser effective length.
3, according to the reactor of claim 2, it is characterized in that the lower end with riser reactor is a starting point, described feed zone is positioned at the 6-40% place of riser effective length, and the length of feed zone accounts for the 5-25% of riser effective length.
4, according to the reactor of claim 3, it is characterized in that the lower end with riser reactor is a starting point, described feed zone is positioned at the 7-35% place of riser effective length, and the length of feed zone accounts for the 6-22% of riser effective length.
5, according to the reactor of claim 1, the diameter that it is characterized in that described feed zone is 1.1-3 with the ratio of the average diameter of the non-feed zone of riser reactor: 1.
6, according to the reactor of claim 5, the diameter that it is characterized in that described feed zone is 1.2-2.5 with the ratio of the average diameter of the non-feed zone of riser reactor: 1.
7, according to the reactor of claim 6, the diameter that it is characterized in that described feed zone is 1.2-2 with the ratio of the average diameter of the non-feed zone of riser reactor: 1.
8,, when it is characterized in that implementing sectional feeding on the described riser reactor, 2-6 feed zone is set, and each feed zone is provided with corresponding feed nozzle according to the reactor of claim 1.
9, according to the reactor of claim 1, the central axis that it is characterized in that the central axis of described feed nozzle and riser reactor is 90 °＜β of the formed angle of direction≤180 ° vertically upward.
10, according to the reactor of claim 9, the central axis that it is characterized in that the central axis of described feed nozzle and riser reactor is 110 °＜β of the formed angle of direction≤180 ° vertically upward.
11, according to the reactor of claim 10, the central axis that it is characterized in that the central axis of described feed nozzle and riser reactor is 130 °＜β of the formed angle of direction＜155 ° vertically upward.
12,, it is characterized in that described feed nozzle is arranged on the reducing position of feed zone, or be arranged on the isometrical sidewall of feed zone according to the reactor of claim 1.
13, according to the reactor of claim 1, it is characterized in that each layer feed nozzle on the described riser reactor is provided with symmetrically, the central axis of each feed nozzle and the central axis of the riser reactor formed angle of direction vertically upward equate that the central axis of each feed nozzle is intersected on the central axis of riser reactor.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108587676A (en) * | 2018-06-20 | 2018-09-28 | 南京博酝化工科技有限公司 | A kind of device of catalytic cracking of crude oil |
| CN111097337A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN111686658A (en) * | 2020-05-09 | 2020-09-22 | 陈躬 | Device for preparing sewage/wastewater coagulant, sewage/wastewater coagulant and preparation method thereof |
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| US5562818A (en) * | 1993-07-16 | 1996-10-08 | Uop | FCC feed injection with non-quiescent mixing |
| CN1091393C (en) * | 1999-08-23 | 2002-09-25 | 中国石化集团洛阳石油化工工程公司 | Catalytic cracking riser reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108587676A (en) * | 2018-06-20 | 2018-09-28 | 南京博酝化工科技有限公司 | A kind of device of catalytic cracking of crude oil |
| CN111097337A (en) * | 2018-10-25 | 2020-05-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN111097337B (en) * | 2018-10-25 | 2022-04-05 | 中国石油化工股份有限公司 | Zoned fluidized bed reaction-regeneration device and process for preparing aromatic hydrocarbon through methanol conversion |
| CN111686658A (en) * | 2020-05-09 | 2020-09-22 | 陈躬 | Device for preparing sewage/wastewater coagulant, sewage/wastewater coagulant and preparation method thereof |
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