CN103773446B - A kind of heavy oil cracking reactor and heavy oil cracking process - Google Patents
A kind of heavy oil cracking reactor and heavy oil cracking process Download PDFInfo
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- CN103773446B CN103773446B CN201210397732.XA CN201210397732A CN103773446B CN 103773446 B CN103773446 B CN 103773446B CN 201210397732 A CN201210397732 A CN 201210397732A CN 103773446 B CN103773446 B CN 103773446B
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Abstract
The heavy oil cracking process of a kind of heavy oil cracking reactor and this heavy oil cracking reactor of use, this heavy oil cracking reactor comprises pre lift zone, bed conversion zone, riser tube conversion zone, settling section and stripping stage, wherein, the diameter of pre lift zone and the diameter of riser tube conversion zone are all less than the diameter of bed conversion zone, by being communicated with along the extension diameter section expanding to the direction of bed conversion zone from pre lift zone between pre lift zone with bed conversion zone, by being communicated with along from bed conversion zone to the undergauge section of the direction undergauge of riser tube conversion zone between bed conversion zone with riser tube conversion zone, stripping stage is positioned at the below of settling section, and the top of stripping stage is communicated with settling section, riser tube conversion zone runs through stripping stage and one end is positioned at settling section, the end that riser tube conversion zone is positioned at settling section is provided with gas-solid separating device.Heavy oil cracking reactor according to the present invention can alleviate and even prevents from forming coking in bed conversion zone, and improves the yield of light-end products.
Description
Technical field
The present invention relates to a kind of heavy oil cracking reactor, and use this heavy oil cracking reactor to carry out the method for heavy oil cracking.
Background technology
China is the country of oil-poor rich coal, and crude oil is heaviness, in poor quality increasingly, the heavy component carbon residue in some crude oil and metal content all very high, with traditional working method be difficult to efficiently it is fully utilized.The technique that current process mink cell focus is conventional is delayed coking, reactor is coking tower, High Temperature and Heavy Oil enters reactor, under higher reaction temperatures and the condition in longer reaction times, make heavy oil generation degree of depth thermal conversion reaction, generate cooking gas, coker gasoline, coker gas oil, heavy distillate (wax tailings) and refinery coke.Gas-liquid-solid three-phase is there is when reactor reacts.In this technique, because mink cell focus needs at high temperature to generate lighter oil product through the longer time by thermally splitting, therefore, when raw material carbon residue is very high, green coke amount is very large.In order to address this problem, develop the fluidized coking process that temperature of reaction is higher, the residence time is shorter.Fluidized coking process adopts bed conversion zone, and take coke powder as the thermal barrier of Heavy Oil Thermal, the heavy oil entering reactor is attached on particle with liquid film, decreases the time that heavy oil exists with liquid phase, thus improves the yield of light-end products.
But existing heavy oil cracking reactor can only mix refining part heavy oil, even can not process inferior heavy oil.Therefore, need to develop the heavy oil cracking reactor made new advances.
For this reason, CN202070330U proposes a kind of riser tube conversion zone being conducive to processing inferior heavy oil, reactor is divided into three reactor zones to produce alkene for boundary by this reactor: charging reaction zone, olefine reaction district and deep reaction district, in these three reaction zones, the largest diameter in olefine reaction district is about 2 times of charging reaction zone, and the diameter in deep reaction district is minimum.Reactor can process heavy raw oil by larger proportion, but can't process inferior heavy oil completely.
CN101993723A proposes a kind of method and apparatus of modifying low-quality heavy oil.This invention relies on catalytic cracking unit, arranges heavy oil modification reactor, utilizes carbon deposited catalyst to be generated as the thermal barrier of heavy oil modification.Heavy oil modification device is upper coarse and lower fine structure, and reactor hypomere is riser tube, and top is bed structure.This kind of reactor, when high throughput deep processing inferior heavy oil, easily causes the coking of initial reaction section, affects the steady running of device.
US20110206563A1 proposes a kind of improved loop fluidized-bed reactor being applied to fluid coking, heavy oil reaction zone, reactor top, stripping zone, bottom, and be dense phase fluidized bed operation, stripping zone is provided with the baffle plate improving grain flow voltinism.Stripping zone is in the below of reaction zone, and the oil gas that stripping goes out through bed conversion zone, will add the residence time of product gas, will reduce the yield of product liquid.
Summary of the invention
The object of the invention is the above-mentioned defect existed to overcome existing heavy oil cracking reactor, a kind of new heavy oil cracking reactor is provided.
The invention provides a kind of heavy oil cracking reactor, this heavy oil cracking reactor comprises pre lift zone, bed conversion zone, riser tube conversion zone, settling section and stripping stage, wherein, the diameter of described pre lift zone and the diameter of described riser tube conversion zone are all less than the diameter of described bed conversion zone, by being communicated with along the extension diameter section expanding to the direction of described bed conversion zone from described pre lift zone between described pre lift zone with described bed conversion zone, by being communicated with along the undergauge section from described bed conversion zone to the direction undergauge of described riser tube conversion zone between described bed conversion zone with described riser tube conversion zone, described stripping stage is positioned at the below of described settling section, and the top of described stripping stage is communicated with described settling section, described riser tube conversion zone runs through described stripping stage and one end is positioned at described settling section, the end that described riser tube conversion zone is positioned at described settling section is provided with gas-solid separating device.
Preferably, the diameter ratio of described pre lift zone and described bed conversion zone is 1:1.1-6, is more preferably 1:2-3.
Preferably, the inwall of described extension diameter section and the angle of vertical direction are 10-60 °, are more preferably 10-45 °.
Preferably, the diameter ratio of described riser tube conversion zone and described bed conversion zone is 1:1.5-8, is more preferably 1:2-5.
Preferably, the length-to-diameter ratio of described bed conversion zone is 1-15:1, is more preferably 1-10:1; The length-to-diameter ratio of described riser tube conversion zone is 2-30:1, is more preferably 5-20:1.
Preferably, the inwall of described undergauge section and the angle of described vertical direction are 10-60 °, are more preferably 10-45 °.
Preferably, described riser tube conversion zone, described settling section and described stripping stage are coaxially arranged.
Preferably, the diameter ratio of described riser tube conversion zone and described stripping stage is 1:1.5-8, is more preferably 1:2-5; The diameter ratio of described stripping stage and described settling section is 1:1-2, is more preferably 1:1-1.5.
Preferably, described heavy oil cracking reactor also comprises nozzle, and described nozzle is arranged on the sidewall of described bed conversion zone and/or described extension diameter section.
More preferably, described heavy oil cracking reactor is provided with multilayer nozzle, and at least one deck nozzle is arranged on the sidewall of described extension diameter section.
Further preferably, the number of plies of described nozzle is 2-4, and the nozzle number of every layer is 3-10.
More preferably, described nozzle comprises spray tube and sleeve pipe, flow to along the logistics in described spray tube, described spray tube comprises mixing section successively, transportation section and shower nozzle, the internal diameter of described mixing section is greater than the internal diameter of described transportation section, described transportation section and described shower nozzle are contained in described sleeve pipe, and between the outer wall of the inwall of described sleeve pipe and described transportation section and described shower nozzle, there is gap, described mixing section is provided with steam-in and heavy oil entrance, the sidepiece of described shower nozzle is provided with opening, the top of described shower nozzle is provided with opening, the sidepiece of described sleeve pipe is provided with steam-in, the top of described sleeve pipe is provided with nozzle opening.
Further preferably, described spray tube also comprises undergauge section, and described undergauge section is arranged between described mixing section and described transportation section.
Further preferably, be provided with diverting device in described mixing section, described mixing section is divided into two regions be interconnected by described diverting device.Described diverting device is preferably swirl flow nozzle.For described swirl flow nozzle, the middle part of described swirl flow nozzle is preferably provided with hole, Lavalle, and the sidepiece of described swirl flow nozzle is preferably provided with spiral groove.
Still more preferably, in described mixing section, described diverting device is near one end of described transportation section.
In described spray tube, the internal diameter of described mixing section is preferably 2-20:1 with the ratio of the internal diameter of described transportation section.
For described shower nozzle, flow to along the logistics in described spray tube, described shower nozzle preferably comprises enlarged diameter region and reducing area successively, and the opening of shower nozzle sidepiece is preferably arranged on the sidewall of described enlarged diameter region.
More preferably, flow to along the logistics in described spray tube, the height of described enlarged diameter region accounts for the 30-60% of the total height of described shower nozzle.
More preferably, flow to along the logistics in described spray tube, the top of described sleeve pipe is undergauge section, and the sidewall of described reducing area is parallel with the sidewall at the top of described sleeve pipe.
Present invention also offers the heavy oil cracking process using above-mentioned heavy oil cracking reactor.
In described heavy oil cracking reactor provided by the invention, the diameter of pre lift zone is less than the diameter of bed conversion zone, and therebetween by being communicated with along the extension diameter section expanding to the direction of bed conversion zone from pre lift zone, the contact substance velocity of flow after entering bed conversion zone from pre lift zone is reduced.In this case, inject bed conversion zone heavy oil and can touch relatively many contact substance within the unit time, thus the macrobead that formed because contact substance contacts with more heavy oil can be avoided, and then can alleviate and even prevent from forming coking in bed conversion zone.And, the velocity of flow of contact substance in bed conversion zone is less, velocity of flow in pre lift zone is comparatively large, the contact substance contacted with heavy oil in bed conversion zone can not back-mixing in pre lift zone, thus avoid the coking that back-mixing contact substance causes owing to contacting with a large amount of heavy oil.
And, in described heavy oil cracking reactor provided by the invention, the diameter of riser tube conversion zone is less than the diameter of bed conversion zone, and therebetween by being communicated with along from bed conversion zone to the undergauge section of the direction undergauge of riser tube conversion zone, the oil gas velocity of flow after entering riser tube conversion zone produced by bed conversion zone is increased, thus the residence time of oil gas can be shortened, improve the yield of light-end products.
In addition, in described heavy oil cracking reactor provided by the invention, settling section, stripping stage and riser tube conversion zone etc. are coupled, are conducive to simplified apparatus processing.
Other features and advantages of the present invention are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing is used to provide a further understanding of the present invention, and forms a part for specification sheets, is used from explanation the present invention, but is not construed as limiting the invention with embodiment one below.In the accompanying drawings:
Fig. 1 is the structural representation of heavy oil cracking reactor according to the present invention;
Fig. 2 is the structural representation of a kind of preferred implementation of nozzle in described heavy oil cracking reactor of the present invention;
Fig. 3 is the structural representation of the another kind of preferred implementation of nozzle in described heavy oil cracking reactor of the present invention;
The local structure schematic diagram at the top of the nozzle in Fig. 4 described heavy oil cracking reactor of the present invention.
Description of reference numerals
1 pre lift zone 2 bed conversion zone 3 riser tube conversion zone
4 settling section 5 stripping stage 6 nozzles
7 gas-solid separating device 8 cyclonic separator 9 stripping gas distributor
10 pre-lift gas sparger 11 stripping stage dipleg 12 pre lift zone diplegs
13 oil gas vent pipeline 61 spray tube 62 sleeve pipes
63 diverting device 611 mixing section 612 transportation sections
613 shower nozzle 614 steam-in 615 heavy oil entrances
616 opening 617 opening 618 undergauge sections
619 hole, Lavalle, reducing area 631, enlarged diameter region 620
632 spiral grooves
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.Should be understood that, embodiment described herein, only for instruction and explanation of the present invention, is not limited to the present invention.
In the present invention, when not doing contrary explanation, the noun of locality such as " upper and lower " of use typically refers to reference to shown in the drawings upper and lower; " inside and outside " refers to profile inside and outside relative to each parts itself; " bottom ", " top " and " sidepiece " are all flow to based on the logistics in each parts, wherein, " bottom " refers to the end of the upstream flowed to along the logistics in corresponding component, " top " refers to the end in the downstream flowed to along the logistics in corresponding component, and " sidepiece " refers to the part between top and bottom.
As shown in Figure 1, described heavy oil cracking reactor provided by the invention comprises pre lift zone 1, bed conversion zone 2, riser tube conversion zone 3, settling section 4 and stripping stage 5, wherein, the diameter of described pre lift zone 1 and the diameter of described riser tube conversion zone 3 are all less than the diameter of described bed conversion zone 2, by being communicated with along the extension diameter section expanding to the direction of described bed conversion zone 2 from described pre lift zone 1 between described pre lift zone 1 with described bed conversion zone 2, by being communicated with along the undergauge section from described bed conversion zone 2 to the direction undergauge of described riser tube conversion zone 3 between described bed conversion zone 2 with described riser tube conversion zone 3, described stripping stage 5 is positioned at the below of described settling section 4, and the top of described stripping stage 5 is communicated with described settling section 4, described riser tube conversion zone 3 runs through described stripping stage 5 and one end is positioned at described settling section 4, the end that described riser tube conversion zone 3 is positioned at described settling section 4 is provided with gas-solid separating device 7.
In described heavy oil cracking reactor, the object making the diameter of pre lift zone 1 be less than the diameter of bed conversion zone 2 is that the contact substance velocity of flow after entering bed conversion zone 2 from pre lift zone 1 is reduced.As long as owing to ensureing that the diameter of pre lift zone 1 is less than the diameter of bed conversion zone 2, can realize making contact substance enter the process of bed conversion zone 2 from pre lift zone 1 and slow down, there is no particular limitation for the concrete ratio of diameter therefore.In the preferred case, pre lift zone 1 is 1:1.1-6 with the diameter ratio of bed conversion zone 2, is more preferably 1:2-3.
In described heavy oil cracking reactor, the object making the diameter of riser tube conversion zone 3 be less than the diameter of bed conversion zone 2 is that the oil gas velocity of flow after entering riser tube conversion zone 3 making to be produced by bed conversion zone 2 increases, to shorten the residence time of oil gas.As long as owing to ensureing that the diameter of riser tube conversion zone 3 is less than the diameter of bed conversion zone 2, can realize making oil gas enter in the process of riser tube conversion zone 3 and accelerate, there is no particular limitation for the concrete ratio of diameter therefore.In the preferred case, riser tube conversion zone 3 is 1:1.5-8 with the diameter ratio of bed conversion zone 2, is preferably 1:2-5.In the preferred case, the length-to-diameter ratio of bed conversion zone 2 is 1-15:1, is more preferably 1-10:1; The length-to-diameter ratio of riser tube conversion zone 3 is 2-30:1, is more preferably 5-20:1.
In described heavy oil cracking reactor, extension diameter section (along expanding to the direction of bed conversion zone 2 from pre lift zone 1) is set between pre lift zone 1 and bed conversion zone 2, and the object arranging undergauge section (along from bed conversion zone 2 to the direction undergauge of riser tube conversion zone 3) between bed conversion zone 2 and riser tube conversion zone 3 is that transitional region in order to prevent heavy oil from changing at diameter is assembled, thus cause coking.In the preferred case, the inwall of described extension diameter section and the angle of vertical direction are 10-60 °, are more preferably 10-45 °; The inwall of described undergauge section and the angle of described vertical direction are 10-60 °, are more preferably 10-45 °.
In described heavy oil cracking reactor, riser tube conversion zone 3, settling section 4 and stripping stage 5 are coupled by such mode: inside riser tube conversion zone 3 being arranged on settling section 4 and stripping stage 5, and run through stripping stage 5, also namely run through top and the bottom of stripping stage 5, and the top of stripping stage 5 is communicated with the bottom of settling section 4.By such coupled structure, be conducive to simplified apparatus processing, and save occupation area of equipment.In a preferred embodiment, as shown in Figure 1, riser tube conversion zone 3, settling section 4 and stripping stage 5 are coaxially arranged.Here, described coaxial setting is not that the central axis of requirement riser tube conversion zone 3, settling section 4 and stripping stage 5 overlaps utterly completely, as long as but ensure that the central axis of three substantial deviation does not occur by visual inspection.
In the preferred case, riser tube conversion zone 3 is 1:1.5-8 with the diameter ratio of stripping stage 5, is preferably 1:2-5.
In the preferred case, stripping stage 5 is 1:1-2 with the diameter ratio of settling section 4, is preferably 1:1-1.5.
The internal structure of described stripping stage 5 can be the structure of various routine, such as, can be empty barrel structure, disc-annular shape baffle arrangement or two sections of circulation structures.In the preferred case, the internal structure of described settling section 5 is disc-annular shape baffle arrangement.
Described gas-solid separating device 7 is preferably the fast gas-solid separator that this area routine uses.
As shown in Figure 1, described heavy oil cracking reactor can also comprise cyclonic separator 8.Cyclonic separator 8 is arranged in settling section 4, for further gas solid separation, to isolate the oil gas of the solid particulate being substantially free of contact substance.Can be derived by oil gas vent pipeline 13 by the isolated oil gas of described cyclonic separator 8.In the preferred case, described cyclonic separator 8 is two-stage gas-solid cyclone separator.
As shown in Figure 1, described heavy oil cracking reactor can also comprise stripping gas distributor 9.Described stripping gas distributor 9 is arranged on the position of the bottom near stripping stage 5, for supplying stripping gas to described stripping stage 5, carries out stripping to the contact substance settled down through settling section 4.
As shown in Figure 1, described heavy oil cracking reactor can also comprise stripping stage dipleg 11.Described stripping stage dipleg 11 is arranged on the bottom of stripping stage 5.When being provided with stripping gas distributor 9 in stripping stage 5, described stripping stage dipleg 11 is preferably arranged on the below of stripping gas distributor 9.Described stripping stage dipleg 11 is for regenerating carrying in follow-up revivifier (not shown) through steam stripped contact substance.
As shown in Figure 1, described heavy oil cracking reactor can also comprise pre lift zone dipleg 12 and pre-lift gas sparger 10.Pre lift zone dipleg 12 and pre-lift gas sparger 10 are all arranged on the position of the bottom near pre lift zone 1, and pre lift zone dipleg 12 is arranged on the top of pre-lift gas sparger 10.Described pre lift zone dipleg 12 is for being supplied to the contact substance regenerated through revivifier (not shown) and/or fresh contact substance (namely without the contact substance of heavy oil cracking reaction) in pre lift zone.Described pre-lift gas sparger 10 for supplying pre-lift gas to described pre lift zone 1, so that the contact substance provided by pre lift zone dipleg 12 is risen in bed conversion zone 2.
As shown in Figure 1, described heavy oil cracking reactor can also comprise nozzle 6.Described nozzle 6 can be arranged on the sidewall of bed conversion zone 2 and/or extension diameter section.In the preferred case, described heavy oil cracking reactor is provided with multilayer nozzle 6, and at least one deck nozzle 6 is arranged on the sidewall of described extension diameter section.Further preferably, the sidewall of described extension diameter section arranges one deck nozzle 6, remaining nozzle is arranged on the sidewall of bed conversion zone 2.Under above-mentioned preferable case, the contact substance generation back-mixing contacting heavy oil can be prevented further, and the yield of light-end products can be improved.
When described nozzle 6 is multilayer, the number of plies of described nozzle 6 is preferably 2-4, and the nozzle number of every layer is preferably 3-10, is more preferably 3-8.The sidewall of bed conversion zone 2 arranges nozzle 6, nozzle 6 is preferably arranged on the region near bottom, more preferably, be arranged on the nozzle on the sidewall of bed conversion zone 2 accounts for whole bed conversion zone 2 height 5-45% to the distance of the bottom of bed conversion zone 2, be more preferably 10-40%.The sidewall of described extension diameter section arranges nozzle 6, nozzle 6 is preferably arranged on the middle part of the short transverse of described extension diameter section.
In each nozzle layer, preferably each nozzle described heavy oil cracking reactor radial section be circumferentially equally distributed.
Described nozzle 6 can be the various heavy oil nozzles that this area routine uses.In the preferred case, as shown in Figures 2 and 3, described nozzle 6 comprises spray tube 61 and sleeve pipe 62, flow to along the logistics in described spray tube 61, described spray tube 61 comprises mixing section 611 successively, transportation section 612 and shower nozzle 613, the internal diameter of described mixing section 611 is greater than the internal diameter of described transportation section 612, described transportation section 612 and described shower nozzle 613 are contained in described sleeve pipe 62, and between the inwall of described sleeve pipe 62 and the outer wall of described transportation section 612 and described shower nozzle 613, there is gap, described mixing section 611 is provided with steam-in 614 and heavy oil entrance 615, the sidepiece of described shower nozzle 613 is provided with opening 616, the top of described shower nozzle 613 is provided with opening 617, the sidepiece of described sleeve pipe 62 is provided with steam-in 621, the top of described sleeve pipe 62 is provided with nozzle opening 622.In this case, described nozzle 6 can be stretched into inside reactor and carry out injection heavy oil, thus heavy oil can be avoided to be sprayed onto on the sidewall of reactor; And the steam injected by the steam-in 621 of sleeve pipe 62 sidepiece can be shielded to the heavy oil in the transportation section 612 of spray tube 61 and shower nozzle 613, thus can prevent heavy oil temperature from raising and coking occurs.
And, in described nozzle 6, by the internal diameter making the internal diameter of described mixing section 611 be greater than described transportation section 612, make from the described heavy oil of mixing section 611 and the gas-oil mixture of steam after entering described transportation section 612, pressure and velocity of flow can increase, thus can impel the heavy oil in gas-oil mixture and steam Homogeneous phase mixing.In the preferred case, the internal diameter of described mixing section 611 is 2-20:1 with the ratio of the internal diameter of described transportation section 612, is more preferably 2-10:1.
In described nozzle, for the connection of described mixing section 611 and described transportation section 612, such as, can as shown in Figure 2, directly described mixing section 611 be connected with described transportation section 612.But in this case, there is dead angle with the junction of described transportation section 612 in described mixing section 611, heavy oil can be assembled at this dead angle place.Therefore, in order to avoid the gathering of heavy oil in mixing section 611, preferably, as shown in Figure 3, undergauge section 618 is set between described mixing section 611 and described transportation section 612.The height of described undergauge section 618 (also namely described mixing section 611 top to described transportation section 612 bottom between distance) can be 1:0.1-10 with the ratio of the internal diameter of described mixing section 611, preferably 1:0.5-5.
When being provided with undergauge section 618 between described mixing section 611 and described transportation section 612, the bottom of described sleeve pipe is preferably fixedly connected on the outer wall of described undergauge section 618, described in the mode that is fixedly connected with can be such as welding.
In described nozzle, in order to impel the gas-oil mixture Homogeneous phase mixing of heavy oil and steam, thus improving atomizing effect further, be preferably provided with diverting device 63 in described mixing section 611, described mixing section 611 is divided into two regions be interconnected by described diverting device 63.In the preferred case, described diverting device 63 swirl flow nozzle.More preferably, the middle part of described swirl flow nozzle is provided with hole, Lavalle 631, and the sidepiece of described swirl flow nozzle is provided with spiral groove 632.The middle part of described swirl flow nozzle refers to the part of central axis parallel or overlapping with the central axis (flowing to along the logistics in described spray tube 61) of described spray tube 61 in described swirl flow nozzle.When the middle part of described swirl flow nozzle is provided with hole, Lavalle 631 and the sidepiece of described swirl flow nozzle is provided with spiral groove 632, liquid heavy oil can be formed liquid film by hole, described Lavalle 631 and described spiral groove 632 effectively, liquid film can be torn into fluid column and/or drop by the high velocity vapor injected by steam-in 614, thus makes heavy oil and steam Homogeneous phase mixing.In described swirl flow nozzle, the number of described spiral groove 632 can be 2-6.The size in hole, described Lavalle 631 can be determined by the treatment capacity of heavy oil.Preferably, the minimum-value aperture in hole, described Lavalle 631 is 1:5-100 with the ratio of the internal diameter of described mixing section 611, is more preferably 1:10-50; The maximum diameter of hole in hole, described Lavalle 631 is 1:1.5-10 with the ratio of the internal diameter of described mixing section 611, is more preferably 1:2-5.
Further preferably, in described mixing section 611, described diverting device 63 is near one end of described transportation section 612.More preferably, described diverting device 63 accounts for the 50-80% of the total height (i.e. described mixing section 611 distance from bottom to top) of described mixing section 611 to the distance of the bottom of described mixing section 611.
In described nozzle, described transportation section 612 and shower nozzle 613 are contained in described sleeve pipe 62.The external diameter of described transportation section 612 can be 1:1.1-2 with the ratio of the internal diameter of described sleeve pipe 62, is preferably 1:1.1-1.5.
As in Figure 2-4, for described shower nozzle 613, flow to along the logistics in described spray tube 61, described shower nozzle 613 preferably comprises enlarged diameter region 619 and reducing area 620 successively, and the opening 616 of shower nozzle 613 sidepiece is arranged on the sidewall of described enlarged diameter region 619.In this case, gas-oil mixture from described transportation section 612 first carries out reducing pressure and reduction of speed in described enlarged diameter region 619, carry out pressurizeing and accelerating again in described reducing area 620, the velocity contrast of heavy oil and steam can be improved, thus impel heavy oil and steam Homogeneous phase mixing and atomization.
In order to impel heavy oil uniform atomizing further, the opening 616 of shower nozzle 613 sidepiece is preferably multiple, is more preferably 2-20, more preferably 3-15.When the opening 616 of shower nozzle 613 sidepiece is multiple, the opening 616 of shower nozzle 613 sidepiece is preferably evenly distributed on the surrounding of the sidewall of described enlarged diameter region 619.The height (distance namely along the logistics flow direction in described spray tube 61 from the upstream extremity of described enlarged diameter region 619 to downstream end) of described enlarged diameter region 619 preferably accounts for the 10-80% of the total height (distance the opening 617 namely along the logistics flow direction in described spray tube 61 from the upstream extremity of described shower nozzle 613 to shower nozzle 613 top) of described shower nozzle 613, is more preferably 30-60%.Further, as shown in Figure 4, the sidewall of described enlarged diameter region 619 and the angle β of horizontal direction can be 1-45 °, are preferably 10-45 °.
As shown in Figure 4, flow to along the logistics in described spray tube 61, the top of described sleeve pipe 62 is preferably undergauge section.This undergauge section can improve the speed of the vapour stream injected by steam-in 621, make the gas-oil mixture that this vapour stream is sprayed by the opening 617 at shower nozzle 613 top with higher velocity shock, thus the atomizing effect of heavy oil can be improved further, and improve the mixing uniformity of heavy oil and steam.Still more preferably, the sidewall of described reducing area 620 is parallel with the sidewall at the top of described sleeve pipe 62.The sidewall of the reducing area 620 at the top of described sleeve pipe 62 and the angle α of horizontal direction can be 10-70 °, are preferably 20-70 °, are more preferably 30-60 °.
In one embodiment, as shown in Figure 1, described heavy oil cracking reactor comprises pre lift zone 1, bed conversion zone 2, riser tube conversion zone 3, settling section 4 and stripping stage 5.The bottom of pre lift zone 1 is provided with pre-lift gas sparger 10, sidewall is provided with the pre lift zone dipleg 12 for transporting the contact substance through regeneration from revivifier (not shown).Bed conversion zone 2 is communicated with by extension diameter section (along expanding to the direction of bed conversion zone 2 from pre lift zone 1) with pre lift zone 1.Described heavy oil cracking reactor is provided with the two-layer nozzle 6 for supplying heavy oil altogether, every layer of nozzle is provided with 6 nozzles, and distribute along the even circumferential of the radial section of heavy oil cracking reactor, wherein, one deck nozzle is arranged on the sidewall of described extension diameter section, and another layer of nozzle is arranged on the sidewall of bed conversion zone 2.The top of riser tube conversion zone 3 is provided with fast gas-solid separator 7, makes oil gas and contact substance sharp separation, reduces the further cracking of oil gas.Riser tube conversion zone 3 is communicated with settling section 4 by described fast gas-solid separator 7.Stripping stage 5 is arranged on the below of settling section 4, and riser tube conversion zone 3 is positioned at the inside of settling section 4 and stripping stage 5.The inside of stripping stage 5 is provided with disc-annular shape baffle arrangement.The bottom of stripping stage 5 is provided with stripping gas distributor 9 and for the stripping stage dipleg 11 by being transported to revivifier through steam stripped contact substance.Two-stage gas-solid cyclone separator 8 is provided with in settling section 4.Oil gas after two-stage gas-solid cyclone separator is separated, then enters follow-up oil gas fractionating system through oil gas vent pipeline 13.
Present invention also offers the heavy oil cracking process using described heavy oil cracking reactor of the present invention.The specific implementation process of described heavy oil cracking process can be as follows: the contact substance from revivifier enters bed conversion zone 2 through pre-lift solid/liquid/gas reactions device 1, and the form of contact substance with fluidized-bed in bed conversion zone 2 moves; Mink cell focus enters bed conversion zone 2 by nozzle 6, contacts cracking/cracking reaction occurs with contact substance; In bed conversion zone 2, heavy oit pyrolysis/cracking is oil gas (comprising light-end products and splitting gas), oil gas and contact substance enter riser tube conversion zone 3 and further cracking occur, then the gas-solid separating device 7 through riser tube conversion zone 3 top is separated, settling section 4 is entered after separation, contact substance enters stripping stage 5 through sedimentation and carries out stripping, oil gas and stripping gas are separated through two-stage gas-solid cyclone separator 8 and enter follow-up oil and gas separating system, and the contact substance after stripping enters follow-up revivifier and regenerates.
Below the preferred embodiment of the present invention is described in detail by reference to the accompanying drawings; but; the present invention is not limited to the detail in above-mentioned embodiment; within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each the concrete technical characteristic described in above-mentioned embodiment, in reconcilable situation, can be combined by any suitable mode.In order to avoid unnecessary repetition, the present invention illustrates no longer separately to various possible array mode.
In addition, also can carry out arbitrary combination between various different embodiment of the present invention, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (15)
1. a heavy oil cracking reactor, this heavy oil cracking reactor comprises pre lift zone (1), bed conversion zone (2), riser tube conversion zone (3), settling section (4) and stripping stage (5), it is characterized in that, the diameter of described pre lift zone (1) and the diameter of described riser tube conversion zone (3) are all less than the diameter of described bed conversion zone (2), by being communicated with along the extension diameter section expanding to the direction of described bed conversion zone (2) from described pre lift zone (1) between described pre lift zone (1) with described bed conversion zone (2), by being communicated with along the undergauge section from described bed conversion zone (2) to the direction undergauge of described riser tube conversion zone (3) between described bed conversion zone (2) with described riser tube conversion zone (3), described stripping stage (5) is positioned at the below of described settling section (4), and the top of described stripping stage (5) is communicated with described settling section (4), described riser tube conversion zone (3) runs through described stripping stage (5) and one end is positioned at described settling section (4), the end that described riser tube conversion zone (3) is positioned at described settling section (4) is provided with gas-solid separating device (7),
Described heavy oil cracking reactor also comprises nozzle (6), described nozzle (6) is arranged on the sidewall of described bed conversion zone (2) and/or described extension diameter section, described nozzle (6) comprises spray tube (61) and sleeve pipe (62), flow to along the logistics in described spray tube (61), described spray tube (61) comprises mixing section (611) successively, transportation section (612) and shower nozzle (613), the internal diameter of described mixing section (611) is greater than the internal diameter of described transportation section (612), described transportation section (612) and described shower nozzle (613) are contained in described sleeve pipe (62), and between the outer wall of the inwall of described sleeve pipe (62) and described transportation section (612) and described shower nozzle (613), there is gap, described mixing section (611) is provided with steam-in (614) and heavy oil entrance (615), the sidepiece of described shower nozzle (613) is provided with opening (616), the top of described shower nozzle (613) is provided with opening (617), the sidepiece of described sleeve pipe (62) is provided with steam-in (621), the top of described sleeve pipe (62) is provided with nozzle opening (622),
Flow to along the logistics in described spray tube (61), described shower nozzle (613) comprises enlarged diameter region (619) and reducing area (620) successively, and the opening (616) of shower nozzle (613) sidepiece is arranged on the sidewall of described enlarged diameter region (619).
2. heavy oil cracking reactor according to claim 1, wherein, described pre lift zone (1) is 1:1.1-6 with the diameter ratio of described bed conversion zone (2).
3. heavy oil cracking reactor according to claim 1 and 2, wherein, the inwall of described extension diameter section and the angle of vertical direction are 10-60 °.
4. heavy oil cracking reactor according to claim 1, wherein, described riser tube conversion zone (3) is 1:1.5-8 with the diameter ratio of described bed conversion zone (2).
5. the heavy oil cracking reactor according to claim 1 or 4, wherein, the length-to-diameter ratio of described bed conversion zone (2) is 1-15:1, and the length-to-diameter ratio of described riser tube conversion zone (3) is 2-30:1.
6. the heavy oil cracking reactor according to claim 1 or 4, wherein, the inwall of described undergauge section and the angle of vertical direction are 10-60 °.
7. heavy oil cracking reactor according to claim 1, wherein, described riser tube conversion zone (3), described settling section (4) and described stripping stage (5) are coaxially arranged.
8. the heavy oil cracking reactor according to claim 1 or 7, wherein, described riser tube conversion zone (3) is 1:1.5-8 with the diameter ratio of described stripping stage (5), and described stripping stage (5) is 1:1-2 with the diameter ratio of described settling section (4).
9. heavy oil cracking reactor according to claim 1, wherein, described heavy oil cracking reactor is provided with multilayer nozzle (6), and at least one deck nozzle (6) is arranged on the sidewall of described extension diameter section.
10. heavy oil cracking reactor according to claim 1, wherein, the number of plies of described nozzle (6) is 2-4, and the nozzle number of every layer is 3-10.
11. heavy oil cracking reactors according to claim 1, wherein, described spray tube (61) also comprises undergauge section (618), and described undergauge section (618) is arranged between described mixing section (611) and described transportation section (612).
12. heavy oil cracking reactors according to claim 1, wherein, be provided with diverting device (63) in described mixing section (611), described mixing section (611) is divided into two regions be interconnected by described diverting device (63).
13. heavy oil cracking reactors according to claim 12, wherein, in described mixing section (611), described diverting device (63) is near one end of described transportation section (612).
14. heavy oil cracking reactors according to claim 1, wherein, flow to along the logistics in described spray tube (61), the top of described sleeve pipe (62) is undergauge section, and the sidewall of described reducing area (620) is parallel with the sidewall at the top of described sleeve pipe (62).
The heavy oil cracking process of the heavy oil cracking reactor in 15. use claim 1-14 described in any one.
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|---|---|---|---|---|
| CN86102643A (en) * | 1985-05-13 | 1986-11-12 | 东洋工程株式会社 | The treating processes of heavy oil residue |
| CN1154400A (en) * | 1996-01-11 | 1997-07-16 | 中国石油化工总公司 | Method for catalytic conversion of petroleum hydrocarbon |
| CN101850226A (en) * | 2010-01-21 | 2010-10-06 | 中国石油天然气股份有限公司 | Riser reactor for fluidized catalytic conversion of dense-phase section feeding |
| CN202131286U (en) * | 2011-04-29 | 2012-02-01 | 中国石油化工股份有限公司 | Catalytic cracking and atomizing material feeding spray nozzle |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN86102643A (en) * | 1985-05-13 | 1986-11-12 | 东洋工程株式会社 | The treating processes of heavy oil residue |
| CN1154400A (en) * | 1996-01-11 | 1997-07-16 | 中国石油化工总公司 | Method for catalytic conversion of petroleum hydrocarbon |
| CN101850226A (en) * | 2010-01-21 | 2010-10-06 | 中国石油天然气股份有限公司 | Riser reactor for fluidized catalytic conversion of dense-phase section feeding |
| CN202131286U (en) * | 2011-04-29 | 2012-02-01 | 中国石油化工股份有限公司 | Catalytic cracking and atomizing material feeding spray nozzle |
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