CN1546610A - Down-flow catalytic cracking/ cracking reactor for processing heavy raw oil - Google Patents
Down-flow catalytic cracking/ cracking reactor for processing heavy raw oil Download PDFInfo
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- CN1546610A CN1546610A CNA2003101171930A CN200310117193A CN1546610A CN 1546610 A CN1546610 A CN 1546610A CN A2003101171930 A CNA2003101171930 A CN A2003101171930A CN 200310117193 A CN200310117193 A CN 200310117193A CN 1546610 A CN1546610 A CN 1546610A
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Abstract
The invention discloses a down-flow catalytic cracking/ cracking reactor for processing heavy raw oil, comprising a gas-solid parallel flow descending super short contact catalytic reactor, a steam stripping device, a cascade turbulent fluidized bed form first section regenerator and a lift tube form second section regenerator, wherein the second section regenerator is connected to the main unit of the reactor through a pre-lift tube.
Description
Technical field
The invention belongs to petrochemical complex treatment facility scope, particularly a kind of descending catalytic cracking/cracking reactor of handling heavy raw oil.
Background technology
The present invention relates to a kind of descending catalytic cracking/cracking reactor form of handling heavy raw oil.Catalytic cracking is an essential industry process in the petroleum refining industry.Continue to use and flow to the rapid circulating fluidized bed system in the oil play at present and carry out catalytic cracking reaction.Owing to and flow in the cocycle fluidized-bed gas-solid direction of motion and be contrary gravity field, particle is easy to take place downward landing phenomenon under action of gravity, cause the gas-solid air-teturning mixed phenomenon serious, the diameter of axle is inhomogeneous to pellet density, velocity distribution, and then cause part granules of catalyst overstand in reactor, cause coking and then influence catalytic cracking reaction optionally improving.The proposition of descending catalytic cracking/cracking reactor makes gas-solid become possibility along the gravity field motion, has solved the defective that above-mentioned contrary gravity field motion is brought.Report in the patent US5468369 of the patent US54A9496 of IFP and Exxon-Mobil Corp., various countries are all in the industrialization complete set technology of making great efforts the descending catalytic cracking/cracking reactor of exploitation now; The heaviness of current China's oil resource is particularly outstanding, and the resid feed ratio of China's catalytic cracking in 2000 is near 50%.Therefore developing the novel descending catalytic cracking/cracking reactor that is suitable for China has great importance for the competitive power of increase China Petroleum, the industry development of promotion energy industry.
Tsing-Hua University has carried out a large amount of research for descending bed catalyst cracker, comprising: patent 87205749.6 catalytic cracking feed nozzle devices, shower nozzle adopts tongue type throat structure, the reinforced bump mutually of stock oil bilateral, outlet is flat type, the material scattering angle is big, and has the velocity of discharge height, and sufficient characteristics atomize.Second patent 85100040 composite internals of fluidized bed reactors is the integral body of the member be made up of baffle plate and vertical tube bundle, evenly is staggered in stripper, avoided occurring in the stripper bed space and dead band, guarantees the uniform of bubble.The 3rd patent 00106169.0 is applicable to the catalyst inlet device of gas-solid cocurrent flow descending bed reactor, utilizes the collision of gas high-speed jet to realize catalyzer and the raw material oil gas uniform distribution at inlet device.Simultaneously the structure of inlet device guaranteed beds with the high-density of maintenance 200Kg/m3 before raw material oil gas contact.Highdensity beds can absorb high speed oil gas effusive momentum effectively, has also avoided contacting of oil gas and wall when good contact is provided between the gas-solid.The 4th patent 00105781.2 wall-attached cutting type fast gas-solid separator utilizes the difference of gas-solid phase mass force in the two phase flow and the wall attachment effect of particle motion to realize that catalyzer oil gas rapidly and efficiently separates.The 5th patent 00100823.4 flexible catalytic cracking technology proposes a kind of riser tube-descending bed coupled catalyst cracker form, can utilize the advantage of riser tube to guarantee the transformation efficiency of reaction at leading portion, and utilize the plug flow effect of descending bed effectively to suppress secondary reaction at back segment, be that the gas solid catalytic reaction of purpose product is very favourable with the intermediate product for catalytic cracking, catalytic pyrolysis etc.
Hot lab scale proves that descending catalytic cracking/cracking reactor can improve the selectivity of catalytic cracking of hydrocarbon reaction in the laboratory in Tsing-Hua University: three to five percentage points of the gain in yield of descending catalytic cracking/cracking reactor light liquid phase fuel, the generation of dry gas and coking reduces over half.Tsing-Hua University and the China Petrochemical Corporation industrial Chinese style technical scale experiment in the refinery, Jinan in 2002 shows that descending-bed reactor has been obtained significant effect in the catalytic cracking/cracking process of lightweight oil charging.
Summary of the invention
The objective of the invention is to overcome the deficiencies in the prior art, a kind of descending catalytic cracking/cracking reactor of handling heavy raw oil is provided, and described descending catalytic cracking/cracking reactor is connected to form the ultrashort contact catalysis reactor of gas-solid cocurrent flow descending, stripper and two-stage regeneration device by pre-riser tube.It is characterized in that: be provided with catalyzer at the top of Desending catalytic cracking reactor 1 and enter the mouth 2 with the close turbulence mutually of raw material oil gas; Descending-bed reactor 1 and pre-riser tube 6 are provided with secondary fuel injection mouth 3 and 4; The end of descending-bed reactor 1 main body is provided with fast gas-solid separator 5, and 5 are provided with stripper 7 behind the tripping device; Be provided with ridge member 8 gas distributors 9 in the stripper 7; Regenerated catalyst enters close phase turbulence inlet 2 from pre-riser tube 6 with close phase form; Raw material oil gas and atomizing steam spray into by the multiple fuel injection mouth on the close phase turbulence inlet 2; Granules of catalyst and atomizing oil gas carry out the intensive turbulence in close turbulence mutually inlet 2 mix after, evenly enter descending-bed reactor 1 main body.Stock oil can also inject from the many groups secondary fuel injection mouth 3 and 4 on reactor 1 main body or the pre-riser tube 6; The oil nozzle shower nozzle is made up of atomizing steam mouth pipe, stock oil inlet pipe, mixing section and shower nozzle; The nozzle shower nozzle adopts tongue type throat structure, and stock oil is the bilateral charging, and the bump outlet is flat-section mutually; Every group of oil nozzle divides two-layer evenly distributed along reactor 1 circumference up and down, upper strata oil nozzle 3 oblique injections down and lower floor's oil nozzle 4 sprays obliquely; But the oil inlet quantity independent regulation of two-layer oil nozzle up and down.After catalyzer and gas-oil mixture leave reactor 1, enter wall-attached cutting type fast gas-solid separator 5; Fast separation device 5 entrance guiding baffle plates make granules of catalyst have the trend to the motion of limit wall in the ingress; This rear catalyst and gas-oil mixture rotate in the annular space of fast separation device 5; Because the difference of gas-solid phase mass force and the wall attachment effect of particle motion in the two phase flow, most catalyzer in annular space after the motion through 1/4 circular arc, accumulate in the very near frictional belt of limit wall; This moment, the cutting plate of fast separation device 5 was cut catalyzer and oil gas open; After cutting, gas continues rotatablely moving until leaving fast separation device 5 its annular space from the top of cutting plate.Particle then enters stripper 7.Be provided with ridge member 8 in the stripper 7 and improve Srteam Stripping effect; Ridge member 8 is made up of baffle plate and vertical tube bundle; Baffle plate is the ridge-roof type structure, and longitudinal section is the upside down funnel type, and slit, suction hole and dividing plate also are set on it; The whole member uniform distribution that in stripper 7, is staggered.Behind stripper 7, be provided with one section revivifier 10 of turbulent fluidized bed form and two sections revivifiers 12 of riser tube form; Be provided with regeneration orifice plate 11 and gas distributor 16 and 17 in one section revivifier 10, contact with the high performance counter current of stripped vapor so that catalyzer to be provided; Under the condition of 600～700 ℃ of low temperature and 0.01～0.05 atmospheric low remaining oxygen dividing potential drop, sedimentary coke burning generates carbon monoxide on one section revivifier 10 inner catalyst; CO (carbon monoxide converter) gas is taken away most reaction latent heat, keeps mink cell focus cracked heat balance; The half regenerated catalyst band that comes out from one section revivifier 10 not burning out coke and is entered two sections revivifiers 12; Maintain 680～750 ℃ of higher relatively temperature of reaction simultaneously and be higher than 0.05 atmospheric remaining oxygen dividing potential drop; Under high-temperature oxygen-enriched riser tube pattern, the scorching speed of two sections revivifiers is greatly improved, thereby realizes the highly efficient regeneration of catalyzer; The catalyzer and two that regeneration finishes in two sections revivifiers 12 again flue gas enter jointly slightly revolve 19 and whirlwind 20 carry out gas solid separation; Isolated regenerated catalyst enters regenerated catalyst high-level storage groove 13; Isolated two again flue gas contain remaining oxygen, turn back in one section revivifier 10 by flue between device 14 and realize flue gas usefulness again, prevent the tail combustion of flue gas in pipeline and successor devices; The steam that is injected into pre-riser tube 6 is promoted to close phase turbulence inlet 2 to begin next reaction cycle with the regenerated catalyst in the catalyzer high-level storage groove 13; One section revivifier 10 is provided with external warmer 15 and improves turndown ratio with the heat balance of further adjusting regeneration and reaction process.
The invention has the beneficial effects as follows, compare with existing descending-bed reactor technology, this device has adopted the two-stage regeneration device and the descending-bed reactor coupling of " turbulence fluidised form bed " and " riser tube " tandem form, and the two-stage regeneration device can effectively solve the technical problem that descending-bed reactor is handled heavy raw oil.Contain more coking on the catalyzer of heavy oil upgrading, require coking on the catalyzer by abundant burning keeping its catalytic activity, but the heat that perfect combustion brought can surpass the required heat of system's thermal equilibrium.One section rapids bed regenerative operation is comparing under the demulcent condition, and the carbon monoxide of coke products of combustion is kept the thermal equilibrium of system; Two sections riser regenerator operate under the high temperature high oxygen partial pressures condition burns efficiency of carbon conversion to improve.In addition, adopt the form of riser tube regenerated catalyst can be risen to higher height, can be complementary with the form of descending-bed reactor top charging.
Compare with existing descending-bed reactor technology and also to have following characteristics:
1) catalyzer enters with the close inlet of turbulence mutually and many group secondary fuel injection mouths of raw material oil gas from reactor head.Close phase turbulence inlet utilizes the collision of oil gas high-speed jet to realize catalyzer and the raw material oil gas uniform distribution at inlet device.The structure of simultaneously close phase turbulence inlet guaranteed beds with the high-density of maintenance 200Kg/m3 before raw material oil gas contact.Highdensity beds has absorbed the high momentum of high speed oil gas effusive effectively, has avoided contacting of oil gas and wall when good contact is provided between the gas-solid.
2) be provided with wall-attached cutting type fast gas-solid separator behind the reactor, this device can be in 200 milliseconds implementation efficiency in 90%～97% gas solid separation.This helps the duration of contact of control catalyst and oil gas, reduces secondary reaction, improves the selectivity of target product.
3) stripping process of reacted catalyzer is to finish in the stripper of turbulent fluidized bed form, and the ridge member is set in the stripper, in order to improve catalyzer and stripped vapor contact and the residence time of catalyzer in stripper distributes.
4) flue gas of two sections revivifiers turns back in one section revivifier and to realize that flue gas uses again.Flue gas prevents the tail combustion again with the CO concentration that helps to reduce in the flue gas, also helps simultaneously nitride oxide concentration and raising oxygen utilization efficient.
5) one section revivifier and regenerated catalyst high-level storage groove are provided with external warmer and improve turndown ratio with the heat balance of further adjusting regeneration and reaction process.
Description of drawings:
Fig. 1 is for handling the descending catalytic cracking/cracking reactor structural representation of heavy raw oil.
Embodiment
Figure 1 shows that a kind of descending catalytic cracking/cracking reactor of handling heavy raw oil.This descending catalytic cracking/cracking reactor is connected to form the ultrashort contact catalysis reactor of gas-solid cocurrent flow descending, stripper and two-stage regeneration device by pre-riser tube.Be provided with catalyzer at the top of Desending catalytic cracking reactor 1 and enter the mouth 2 with the close turbulence mutually of raw material oil gas; Descending-bed reactor 1 and pre-riser tube 6 are provided with secondary fuel injection mouth 3 and 4; The end of descending-bed reactor 1 main body is provided with fast gas-solid separator 5, and 5 are provided with stripper 7 behind the tripping device, is provided with ridge member 8 gas distributors 9 in the stripper 7; Regenerated catalyst enters close phase turbulence inlet 2 from pre-riser tube 6 with close phase form; Raw material oil gas and atomizing steam spray into by the multiple fuel injection mouth on the close phase turbulence inlet 2; Granules of catalyst and atomizing oil gas carry out the intensive turbulence in close turbulence mutually inlet 2 mix after, evenly enter descending-bed reactor 1 main body.Stock oil can also inject from the many groups secondary fuel injection mouth 3 and 4 on reactor 1 main body or the pre-riser tube 6; The oil nozzle shower nozzle is made up of atomizing steam mouth pipe, stock oil inlet pipe, mixing section and shower nozzle; The nozzle shower nozzle adopts tongue type throat structure, and stock oil is the bilateral charging, and the bump outlet is flat-section mutually; Every group of oil nozzle divides two-layer evenly distributed along reactor 1 circumference up and down, upper strata oil nozzle 3 oblique injections down and lower floor's oil nozzle 4 sprays obliquely; But the oil inlet quantity independent regulation of two-layer oil nozzle up and down.After catalyzer and gas-oil mixture leave reactor 1, enter wall-attached cutting type fast gas-solid separator 5; Fast separation device 5 entrance guiding baffle plates make granules of catalyst have the trend to the motion of limit wall in the ingress; This rear catalyst and gas-oil mixture rotate in the annular space of fast separation device 5; Because the difference of gas-solid phase mass force and the wall attachment effect of particle motion in the two phase flow, most catalyzer in annular space after the motion through 1/4 circular arc, accumulate in the very near frictional belt of limit wall; This moment, the cutting plate of fast separation device 5 was cut catalyzer and oil gas open; After cutting, gas continues rotatablely moving until leaving fast separation device 5 its annular space from the top of cutting plate.Oil gas product after the separation enters follow-up operation to obtain gas phase and liquid-phase product through whirlwind 18; Reclaimable catalyst after the separation then enters stripper 7.Be provided with ridge member 8 in the stripper 7 and improve Srteam Stripping effect; Ridge member 8 is made up of baffle plate and vertical tube bundle; Baffle plate is the ridge-roof type structure, and longitudinal section is the upside down funnel type, and slit, suction hole and dividing plate also are set on it; The whole member uniform distribution that in stripper 7, is staggered.Behind stripper 7, be provided with one section revivifier 10 of turbulent fluidized bed form and two sections revivifiers 12 of riser tube form; Be provided with regeneration orifice plate 11 and gas distributor 16 and 17 in one section revivifier 10, contact with the high performance counter current of stripped vapor so that catalyzer to be provided; Under the condition of 600～700 ℃ of low temperature and 0.01～0.05 atmospheric low remaining oxygen dividing potential drop, sedimentary coke burning generates carbon monoxide on one section revivifier 10 inner catalyst; CO (carbon monoxide converter) gas is taken away most reaction latent heat, keeps mink cell focus cracked heat balance; The half regenerated catalyst band that comes out from one section revivifier 10 not burning out coke and is entered two sections revivifiers 12; Maintain 680～750 ℃ of higher relatively temperature of reaction simultaneously and be higher than 0.05 atmospheric remaining oxygen dividing potential drop; Under high-temperature oxygen-enriched riser tube pattern, the scorching speed of two sections revivifiers is greatly improved, thereby realizes the highly efficient regeneration of catalyzer; The catalyzer and two that regeneration finishes in two sections revivifiers 12 again flue gas enter jointly slightly revolve 19 and whirlwind 20 carry out gas solid separation; Isolated regenerated catalyst enters regenerated catalyst high-level storage groove 13; Isolated two again flue gas contain remaining oxygen, turn back in one section revivifier 10 by flue between device 14 and realize flue gas usefulness again, prevent the tail combustion of flue gas in pipeline and successor devices; The steam that is injected into pre-riser tube 6 is promoted to close phase turbulence inlet 2 to begin next reaction cycle with the regenerated catalyst in the catalyzer high-level storage groove 13; One section revivifier 10 is provided with external warmer 15 and improves turndown ratio with the heat balance of further adjusting regeneration and reaction process.
Claims (2)
1. descending catalytic cracking/cracking reactor of handling heavy raw oil, described descending catalytic cracking/cracking reactor is connected to form the ultrashort contact catalysis reactor of gas-solid cocurrent flow descending, stripper and two-stage regeneration device by pre-riser tube; It is characterized in that: the close inlet of turbulence mutually (2) that is provided with catalyzer and raw material oil gas at the top of Desending catalytic cracking reactor (1); Descending-bed reactor (1) and pre-riser tube (6) are provided with secondary fuel injection mouth (3) and (4); The end of descending-bed reactor (1) main body is provided with fast gas-solid separator (5), and oil gas product and catalyzer are carried out sharp separation; (5) are provided with stripper (7) behind the tripping device, are provided with ridge member (8) and gas distributor (9) in the stripper (7); Behind stripper (7), be provided with two-stage catalytic agent revivifier; Catalyzer enters close phase turbulence inlet (2) by pre-riser tube (6) with close phase form; Raw material oil gas or atomizing steam spray into by the oil nozzle that close phase turbulence enters the mouth on (2); Granules of catalyst evenly enters descending-bed reactor (1) main body and reacts with atomizing oil gas carries out intensive turbulence mixing in close turbulence mutually enter the mouth (2) after.
2. according to the descending catalytic cracking/cracking reactor of the described processing heavy raw oil of claim 1, it is characterized in that: described two-stage catalytic agent revivifier is made up of with two sections revivifiers (12) tandem of riser tube form one section revivifier (10) of turbulent fluidized bed form; Be provided with regeneration orifice plate (11) and gas distributor (16) and (17) in one section revivifier (10), contact with the high performance counter current of stripped vapor so that catalyzer to be provided; Under the condition of 600～700 ℃ of low temperature and 0.01～0.05 atmospheric low remaining oxygen dividing potential drop, sedimentary coke burning generates carbon monoxide on one section revivifier (10) inner catalyst; CO (carbon monoxide converter) gas is taken away most reaction latent heat, keeps mink cell focus cracked heat balance; The half regenerated catalyst band that comes out from one section revivifier (10) not burning out coke and is entered two sections revivifiers (12); Maintain 680～750 ℃ of higher relatively temperature of reaction simultaneously and be higher than 0.05 atmospheric remaining oxygen dividing potential drop; Under high-temperature oxygen-enriched riser tube pattern, the scorching speed of two sections revivifiers is greatly improved, thereby realizes the highly efficient regeneration of catalyzer; The catalyzer and two that regeneration finishes in two sections revivifiers (12) flue gas again enters slightly jointly and revolves (19) and whirlwind (20) carries out gas solid separation; Isolated regenerated catalyst enters regenerated catalyst high-level storage groove (13); Isolated two again flue gas contain remaining oxygen, turn back to by flue between device (14) and realize flue gas usefulness again in one section revivifier (10), prevent the tail combustion of flue gas in pipeline and successor devices; The steam that is injected into pre-riser tube (6) is promoted to close phase turbulence inlet (2) to begin next reaction cycle with the regenerated catalyst in the catalyzer high-level storage groove (13); One section revivifier (10) is provided with external warmer (15) and improves turndown ratio with the heat balance of further adjusting regeneration and reaction process.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103182328A (en) * | 2011-12-29 | 2013-07-03 | 神华集团有限责任公司 | Regeneration method of coal liquefied oil hydrogenation deactivated catalyst |
| CN104513670A (en) * | 2013-09-29 | 2015-04-15 | 中石化洛阳工程有限公司 | Catalytic cracking method and device |
| CN104974788A (en) * | 2014-04-08 | 2015-10-14 | 中石化洛阳工程有限公司 | Catalytic cracking device and catalytic cracking method |
| CN108753356A (en) * | 2018-06-21 | 2018-11-06 | 清华大学 | A kind of multi-stage countercurrent catalytic cracking/cracking system and method |
-
2003
- 2003-12-05 CN CNA2003101171930A patent/CN1546610A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103182328A (en) * | 2011-12-29 | 2013-07-03 | 神华集团有限责任公司 | Regeneration method of coal liquefied oil hydrogenation deactivated catalyst |
| CN103182328B (en) * | 2011-12-29 | 2015-09-16 | 神华集团有限责任公司 | A kind of renovation process of liquefied coal coil hydrogenation decaying catalyst |
| CN104513670A (en) * | 2013-09-29 | 2015-04-15 | 中石化洛阳工程有限公司 | Catalytic cracking method and device |
| CN104513670B (en) * | 2013-09-29 | 2016-06-08 | 中石化洛阳工程有限公司 | A kind of catalyst cracking method and device |
| CN104974788A (en) * | 2014-04-08 | 2015-10-14 | 中石化洛阳工程有限公司 | Catalytic cracking device and catalytic cracking method |
| CN104974788B (en) * | 2014-04-08 | 2017-02-22 | 中石化洛阳工程有限公司 | Catalytic cracking device and catalytic cracking method |
| CN108753356A (en) * | 2018-06-21 | 2018-11-06 | 清华大学 | A kind of multi-stage countercurrent catalytic cracking/cracking system and method |
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