CN1498950A - Method and device for adjusting and controlling coupling between cracking heavy oil and transnaturing gasoline in high efficiency - Google Patents
Method and device for adjusting and controlling coupling between cracking heavy oil and transnaturing gasoline in high efficiency Download PDFInfo
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Abstract
An efficient coupled control process and equipment for cracking heavy oil and modifying gasoline is disclosed. The catalytic cracking equipment for heavy oil has two raiser reactors for increasing the output rate of light oil. An auxiliary fluidized reactor is connected to the regenerator for using the regenerated high-temp catalyst to modify the catalytically cracked gasoline fraction in order to decrease olefin content and maintain octane number. The used catalyst to be regenerated is filled back to the first raiser reactor of original catalytic cracking equipment.
Description
Technical field
The present invention relates to the catalytic conversion process of petroleum hydrocarbon, be meant that especially the heavy oil deep catalytic cracking transforms the coupling control technique that reduces the catalytic conversion process of olefin(e) centent with the catalytic gasoline upgrading, belongs to the petrochemical technology field.
Background technology
Because the alkene chemical property is active, NO in volatilization back and the atmosphere
xMix,, atmosphere is caused severe contamination through the poisonous photo-chemical smog of solar ultraviolet irradiation formation based on ozone.In addition, when olefin(e) centent is high in the gasoline, can cause that electronic fuel injection engine nozzle, feed valve carbon deposit are serious, cause controlled deviation, cause fuel oil consumption to increase.Therefore, in recent years along with the increasingly stringent of environmental protection standard, the U.S., Japan and European various countries have issued new gasoline standard in succession, olefin content in gasoline has been proposed new requirement, and China has also formulated corresponding standard in December, 1999, requires olefin content in gasoline ≯ 35 (v) %, simultaneously, require octane value (organon) ≮ 90, aromaticity content ≯ 40 (v) %, sulphur content ≯ 800ppm.At present, catalytically cracked gasoline accounts for the amount of gasoline product up to 85%, and the volume fraction of alkene is 45%-60% in the catalytically cracked gasoline, far above the gasoline standard of new prescription.At this problem, petroleum refining industry has taked some required measure, but the effect of these measures is limited, 10-12 volume percentage point of the maximum decline of content of olefin in gasoline, and octane value also reduces sometimes to some extent, can not satisfy the requirement of new gasoline standard.
For this reason, proposed on conventional catalytic cracking unit, to set up auxiliary fluidizing reactor to come catalytically cracked gasoline is carried out upgrading, comprise patent: " method and the device of easy catalytic cracking sasoline modifincation and olefine reducing " (application number: 02116786.9), " reducing the method and system of catalytic cracking gasoline olefine content " (application number: 02123817.0), " method for modifying of heavily reducing olefinic hydrocarbon and increasing octane rating for catalytically cracked gasoline and device " (application number: 02123655.0), " reduce catalytic cracking gasoline olefine content and keep the method and system of octane value " (application number: 02123494.9), " method for modifying of gasoline catalyzing and olefine reducing boosting of octane rating and device " (application number: 02123658.9), " reducing the method and the device of catalytic cracking gasoline olefine content " (application number: 02116787.7), these reduce the Technology of catalytic cracking gasoline olefine content owing to adopted auxiliary fluidizing reactor, from technological process is that high-temperature catalytic cracked regenerated catalyst mixes with normal temperature Liquid Phase by Catalytic gasoline and contacts, carry out hydrogen transference, aromizing, isomerization and the reaction of cracked upgrading, therefore this process has coke and reacted gas (most of be liquefied gas) and produces, thereby causes the yield of gasoline of oil refining enterprise and yield of light oil to have loss about 1.5%.Simultaneously, owing to there is the gasoline of 5-15wt% to change into liquefied gas, for the bad oil refining enterprise in liquefied gas market, this result is difficult to accept especially.
The loss that the measure of any catalytically cracked gasoline reduction olefin(e) centent all can bring yield of light oil and liquid yield, this is the science certainty of falling olefin hydrocarbon.That is to say, should reduce the olefin(e) centent of catalytically cracked gasoline, not loss again, this is impossible in theory.Therefore, attention is turned on the heavy oil catalytic cracking process, proposed the heavy oil deep catalytic cracking and transformed, improve yield of light oil and liquid yield, thereby remedy the loss that clean gasoline production brings.
Multianalysis in order to improve yield of light oil, reduce gas and coke yield, improve product distribution and quality product and center on new industrial research and the exploitation that riser reactor carries out, the atomization technique that comprises heavy oil feed (nozzle), riser tube bottom catalyzer promotes new technology in advance, the gas-solid quickly separating technology of riser tube end, spent agent high-efficiency multi-section steam stripping technique, finish mixing zone temperature control technology, riser tube reaction terminating technology, the sectional feeding technology, and still in the Millisecond catalytic cracking new technology in development research stage, downstriker riser tube technology etc., the new approaches of the two-stage riser fluid catalytic cracking that proposes with reference to people such as Zhang Jianfang and the effective realization heavy oil deep catalytic cracking of formation transform the novel technique that improves yield of light oil and liquid yield, comprise patent: " being used for two sections tandem riser reactors of catalytic cracking " (ZL99213769.1), " catalytic cracking process with two-segment lift pipe " (application number: 00134054.9) proposed a kind of multi-effective heavy oil catalytic cracking and gasoline fraction upgrading that has three reactors and fallen the alkene new technology, to satisfy petroleum refining industry, improve the great urgent need that yield of light oil and clean gasoline are produced to the mink cell focus deep processing.The starting point of this technology at first is that the riser reactor of existing industrial catalyticing cracking device is transformed; On revivifier, set up second riser reactor then and come recycle stock and reprocessed oil slurry are carried out further cracking reaction, improve total depth of conversion, thereby improve yield of light oil and liquid yield; At last, revivifier is connected with an auxiliary fluidizing reactor, utilizes the high-temperature regenerated catalyst that attracts from revivifier that the catalytically cracked gasoline cut is carried out the catalytic reforming reaction, to reach the purpose that reduces olefin(e) centent and keep octane value.The reacted reclaimable catalyst of catalytic gasoline upgrading is got back to former catalytic cracking unit revivifier through behind the independent stripping system and sedimenting system sedimentation and stripping.
Catalytically cracked gasoline falls olefin hydrocarbon owing to adopted auxiliary fluidizing reactor in this technology, from technological process is that high-temperature catalytic cracked regenerated catalyst mixes with normal temperature Liquid Phase by Catalytic gasoline and contacts, carry out hydrogen transference, aromizing, isomerization and the reaction of cracked upgrading, the catalyzer of conventional catalytic cracking unit has just been used in this reaction, heat, revivifier even settling vessel, stripping stage and separation column etc. are to the operation of conventional catalytic cracking unit, the product distributions of the cracking reaction of main riser reactor and former catalytic cracking unit etc. are influence not.On the other hand, in auxiliary fluidization reactor catalysis gasoline upgrading process here, since catalyzer only with the gasoline fraction contact reacts, so the coking yield of this process is very low, generally below 1.5wt%, therefore, the level of deactivation of catalyzer is very low, the relevant micro-activity that experiment showed, has only reduced 3-4 unit.So, catalyst temperature after the catalytic gasoline fluidizing reactor upgrading process is lower, but micro-activity is higher, just returned the revivifier of former catalytic cracking unit behind the catalyst stripping, and the catalyzer of this low temperature high activity can be used directly and catalytic reaction process fully again.For this reason, the coupling regulation and control novel method and the device of the reaction of a kind of heavy oil catalytic cracking reaction and its gasoline fraction olefine reducing modification have been proposed, promptly the revivifier at existing industrial catalyticing cracking device is connected with an auxiliary fluidizing reactor, the high-temperature regenerated catalyst that utilization attracts from revivifier comes the catalytically cracked gasoline cut is carried out the catalytic reforming reaction, to reach the purpose that reduces olefin(e) centent and keep octane value.The reacted reclaimable catalyst of catalytic gasoline upgrading is through behind the independent stripping system and sedimenting system sedimentation and stripping, a part is got back to former catalytic cracking unit revivifier, another part is injected into the middle and upper part of heavy oil fluid catalytic cracking master riser reactor, reduce the temperature of reaction in decanting point downstream, heavy oil catalytic cracking reaction is effectively controlled.
Summary of the invention
Main purpose of the present invention is to provide the method and apparatus of a kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulation and control, to satisfy petroleum refining industry to the mink cell focus deep processing, improves the demand that yield of light oil and clean gasoline are produced.
The objective of the invention is to be achieved through the following technical solutions:
A kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulate and control method comprise the steps: at least
Step 1: will send into first riser reactor bottom of heavy oil catalytically cracking equipment without the initial heavy oil feedstock of refining, and carry out catalytic cracking reaction; Reaction oil gas is in this reactor middle and upper part and the catalyst mix of injecting from auxiliary fluidized catalytic reforming reactor, and main reaction oil gas separates at this reactor outlet with catalyzer; Catalyzer enters regeneration system rapidly, and main reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 2: recycle stock and reprocessed oil slurry are sent into second riser reactor bottom, proceed catalytic cracking reaction, reaction oil gas and catalyzer enter regeneration system rapidly at this reactor outlet separating catalyst, and reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 3: the catalytically cracked gasoline cut is sent into auxiliary fluidized catalytic reforming reactor, carry out the gasoline upgrading reaction, a upgrading rear catalyst part is returned former revivifier, another part is recycled into first riser reactor of heavy oil catalytically cracking equipment, and upgrading oil gas enters fractionating system and carries out each fraction separation.
A kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulate and control method also comprise the steps: at least
Step 1: with the regenerated catalyst of heavy oil catalytically cracking equipment, from a part of reclaimable catalyst of gasoline upgrading reactor with have neither part nor lot in catalyst for reaction and introduce simultaneously in the catalyst mix jar and mix, this blended catalyzer is under the rheomorphism of the air of introducing from the mixing tank bottom, burn reaction, send the revivifier of catalytic cracking unit then back to;
Step 2: will send into first riser reactor bottom without the initial heavy oil feedstock of refining, after catalyst mix from the catalyst mix jar, carry out catalytic cracking reaction, main reaction oil gas separates at this reactor outlet with catalyzer, catalyzer enters the catalyst mix jar after returning revivifier, and main reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 3: recycle stock and reprocessed oil slurry are sent into second riser reactor bottom, proceed catalytic cracking reaction; Reaction oil gas separates at this reactor outlet with catalyzer, and catalyzer enters the catalyst mix jar after returning revivifier, and reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 4: the catalytically cracked gasoline cut is sent into auxiliary fluidized catalytic reforming reactor, carry out the gasoline upgrading reaction, a upgrading rear catalyst part is returned former revivifier, and another part is injected into the catalyst mix jar, and upgrading oil gas enters fractionating system and carries out each fraction separation.
In first kind of scheme, the reaction conditions in first riser reactor is:
Temperature of reaction: 450-520 ℃;
Heavy oil feedstock preheating temperature: 160-250 ℃;
Catalyzer oil plant weight ratio: 7-12;
Reaction times: 0.5-2.0s, preferred value is 0.8-1.2s;
Catalyst activity: 50-65;
Reaction pressure: 0.1-0.4Mpa.
In first kind of scheme, the reaction conditions in first riser reactor is:
Temperature of reaction: 450-520 ℃;
Heavy oil feedstock preheating temperature: 160-250 ℃;
Catalyzer oil plant weight ratio: 5-10;
Reaction times: 0.5-2.0s, preferred value is 0.8-1.2s;
Catalyst activity: 50-65;
Reaction pressure: 0.1-0.4Mpa.
Reaction conditions in second riser reactor is:
Temperature of reaction: 450-520 ℃;
Heavy oil feedstock preheating temperature: 250-350 ℃;
Catalyzer oil plant weight ratio: 5-10;
Reaction times: 0.5-2.0s, preferred value is 0.8-1.2s;
Catalyst activity: 50-65;
Reaction pressure: 0.1-0.4Mpa.
In the step 4, enter revivifier or the catalyst mix jar of the catalyzer of auxiliary fluidized catalytic reforming reactor from catalytic cracking unit.
The catalytically cracked gasoline cut comprises the full cut of raw gasline or raw gasline lighting end (＜80-110 ℃) or raw gasline last running (＞60-80 ℃) at least.
Catalyzer is conventional catalytic cracking catalyst, comprises amorphous silicon aluminium catalyzer or molecular sieve catalyst at least.
Upgrading oil gas with enter the main fractionating tower of former catalytic cracking unit after the oil gas of main riser reactor mixes and be separated into rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil; Perhaps entering independent fractionating system separates.
The device of a kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulation and control comprises a heavy oil catalytically cracking equipment at least, and this device connects a fractionation plant; It is characterized in that: heavy oil catalytically cracking equipment comprises two riser reactors at least, is used to finish the catalytic cracking reaction of heavy oil feedstock; Wherein, the middle and upper part of first riser reactor is provided with the catalyzer decanting point, and this decanting point connects auxiliary fluidized catalytic reforming reactor by inclined tube, is used for upgrading catalytically cracked gasoline cut; This reforming reactor is connected with the revivifier of catalytic cracking unit.
The device of a kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulation and control also comprises a heavy oil catalytically cracking equipment at least, and this device connects a fractionation plant; It is characterized in that: heavy oil catalytically cracking equipment comprises two riser reactors at least, is used to finish the catalytic cracking reaction of heavy oil feedstock; Wherein, first riser reactor is connected with a catalyst mix jar; The catalytic cracking unit revivifier is provided with an auxiliary fluidized catalytic reforming reactor, is used for upgrading catalytically cracked gasoline cut; This reforming reactor links to each other with mixing tank respectively with revivifier.
The raw material nozzles of first riser reactor improves 0-10 rice than the raw material nozzles of existing riser reactor, and this first riser reactor internal diameter is 0.6-1.0 times of existing riser reactor internal diameter.
The position of the first riser reactor catalyzer decanting point is located at the 1/3-3/4 place of its raw material to the reactor virtual height, and preferred value is the 1/2-2/3 place of its bottom to the reactor virtual height.
The diameter of the vertical section that the first riser reactor catalyzer decanting point is above is 1.0-2.0 times of existing riser reactor diameter.
Second riser reactor is inserted in the settling vessel of catalytic cracking unit, and in its outlet the efficient gas-solid separating device identical or different with first riser reactor is installed.
Auxiliary fluidized catalytic reforming reactor is that riser reactor or riser tube add turbulent bed reactor or turbulent bed reactor or fast bed reactor.
When using riser reactor, the upgrading reaction conditions is:
Temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, reaction times: 1.0-10.0s, reaction pressure: 0.1-0.4Mpa;
When using riser tube to add the turbulent bed reactor, the upgrading reaction conditions is:
Temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, promote the reaction times of pipeline section: 1.0-10.0s, fluidized-bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa;
When using the turbulent bed reactor, the upgrading reaction conditions is:
Temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-300 ℃, catalyst activity: 50-65, turbulent bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa;
When using the fast bed reactor, the upgrading reaction conditions is:
Temperature of reaction is 350-500 ℃, and the gasoline stocks preheating temperature is 40-300 ℃, and catalyst activity is 50-65, and the bed linear speed is 0.6-2.5m/s, and the reaction times is 0.1-10.0 minute, and reaction pressure is 0.1-0.4Mpa.
Auxiliary fluidized catalytic reforming reactor is provided with independently sedimenting system and stripping system, is respectively applied for the sedimentation and the stripping of catalyzer.
Fractionation plant is the fractionation plant of catalytic cracking unit or independent fractionation plant.
Fractionation plant comprises conventional condenser system and B-grade condensation system at least, and this B-grade condensation system is used for obtaining the full cut of raw gasline or raw gasline lighting end or raw gasline last running.
By above technical scheme, the advantage of Technology of the present invention is that the deep catalytic cracking of utilizing two riser reactors to carry out heavy oil transforms, improve yield of light oil and liquid yield, utilize the 3rd fluidizing reactor that catalytically cracked gasoline is carried out upgrading and fall alkene, produce clean gasoline, simultaneously, the solid cryogenic media that catalytic cracking activity is arranged that utilizes the 3rd fluidizing reactor is again implemented control to the cracking reaction of heavy oil catalytically cracking equipment first riser reactor and is optimized, cracking reaction stops effect improved, and yield of light oil improves.Device is changed minimum, and flow process is simple, is easy to realize.Both reduce the olefin(e) centent of catalytic gasoline, deepened the heavy oil fluid catalytic cracking depth of conversion again, improved yield of light oil and liquid yield, thereby remedied the loss that clean gasoline production brings.The present invention can improve 2-3 percentage point with the heavy oil catalytic cracking process yield of light oil, and catalytic cracking gasoline olefine content is reduced to 25, and (v) below the %, octane value remains unchanged or slightly improves, and when satisfying environmental requirement, obtains high yield of light oil.
Description of drawings
Fig. 1 is the improved fractionating system process flow sheet of existing heavy oil fluid catalytic cracking;
Fig. 2 is the technical process first embodiment synoptic diagram of the present invention;
Fig. 3 is the technical process second embodiment synoptic diagram of the present invention;
Fig. 4 is technical process the 3rd an embodiment synoptic diagram of the present invention;
Fig. 5 is technical process the 4th an embodiment synoptic diagram of the present invention;
Fig. 6 is technical process the 5th an embodiment synoptic diagram of the present invention;
Fig. 7 is technical process the 6th an embodiment synoptic diagram of the present invention;
Fig. 8 is technical process the 7th an embodiment synoptic diagram of the present invention;
Fig. 9 is technical process the 8th an embodiment synoptic diagram of the present invention;
Figure 10 is technical process the 9th an embodiment synoptic diagram of the present invention;
Figure 11 is technical process the tenth an embodiment synoptic diagram of the present invention;
Figure 12 is technical process the 11 an embodiment synoptic diagram of the present invention;
Figure 13 is technical process the 12 an embodiment synoptic diagram of the present invention;
Figure 14 is technical process the 13 an embodiment synoptic diagram of the present invention;
Figure 15 is technical process the 14 an embodiment synoptic diagram of the present invention;
Figure 16 is technical process the 15 an embodiment synoptic diagram of the present invention;
Figure 17 is technical process the 16 an embodiment synoptic diagram of the present invention.
Embodiment
Describe the present invention in detail below in conjunction with the drawings and specific embodiments:
The present invention is that two reactors of a kind of usefulness carry out the conversion of heavy oil deep catalytic cracking and optimal control and carry out the coupling control technique that the catalytic gasoline upgrading reduces the catalyzed conversion of alkene with a reactor, at first be that the riser reactor (i.e. first riser reactor) of existing industrial catalyticing cracking device is transformed, comprise that just processing is without the initial heavy oil fluid catalytic cracking raw material of refining, raw material nozzles improves 0-10 rice, and the riser reactor internal diameter is reduced into 0.6-1.0 times of existing riser reactor internal diameter; On revivifier, set up second riser reactor again, come recycle stock and reprocessed oil slurry are carried out cracking reaction at higher catalyst activity with under than short reaction times condition, improve total depth of conversion, thereby improve yield of light oil and liquid yield.Second riser reactor is inserted in the settling vessel of former catalytic cracking unit and in its outlet efficient gas-solid separating device identical with first riser reactor or other form is installed; Then, revivifier is connected with an auxiliary fluidizing reactor, utilizes the high-temperature regenerated catalyst that attracts from revivifier that the catalytically cracked gasoline cut is carried out the catalytic reforming reaction, to reach the purpose that reduces olefin(e) centent and keep octane value.The reacted reclaimable catalyst of catalytic gasoline upgrading is through behind the independent stripping system and sedimenting system sedimentation and stripping, a part is got back to former catalytic cracking unit revivifier, another part is injected into the middle and upper part of heavy oil fluid catalytic cracking first riser reactor, reduce the temperature of reaction in decanting point downstream, heavy oil catalytic cracking reaction is effectively controlled, reduce the transformation efficiency of first riser reactor, thereby guarantee particularly diesel yield of higher yield of light oil.The injection phase of high reactivity low temperature catalyst can be optimized, the all right optimization design of fluidization form that decanting point is above, can also introduce in the catalyst mix jar, simultaneously high-temperature regenerated catalyst is introduced from former revivifier, also former catalytic cracking unit normal need metathetical being had neither part nor lot in catalyst for reaction introduces, three bursts of catalyst stream are under the fluidisation of the fluidization air that the catalyst mix pot bottom is introduced, mix on one side, burn reaction on one side, mixing the catalyzer of back temperature reduction introduces in first riser reactor, coming that with lower finish mixing temperature and higher agent-oil ratio heavy oil is carried out catalytic cracking transforms, reaching higher light oil yield, and can reduce the yield of dry gas significantly.The auxiliary fluidization catalytic reforming reactor of newly establishing can be the reactor of riser tube form, also can be the reactor that riser tube adds turbulent bed form, fast bed form or turbulent bed form, and the fluidizing reactor of any form all have independent stripping system and sedimenting system.In a word, this coupling control technique is exactly under the little situation of device change amount, realize reacting between the high temperature, short time of first riser reactor, be controlled at the higher diesel yield of acquisition under the not high situation of transformation efficiency, second riser reactor carries out cracking reaction to relatively large recycle stock and reprocessed oil slurry at higher catalyst activity with under than short reaction times condition, improve total depth of conversion, thereby improve yield of light oil and liquid yield, the 3rd fluidizing reactor carries out the upgrading reduction olefin(e) centent of catalytically cracked gasoline.The operational condition of these three reactors all can be regulated arbitrarily, that is to say that each reactor can adopt oneself suitable operational condition, is beneficial to the generation of desired response in this riser reactor, is independent of each other mutually.
The catalytically cracked gasoline cut of institute's upgrading can be the full cut of raw gasline, raw gasline lighting end (＜80-110 ℃) or raw gasline last running (＞60-80 ℃), and these cuts are set up the B-grade condensation system in existing fractionator overhead and obtained.The separation process of upgrading oil gas can adopt mixture length, promptly in the settling vessel of former catalytic cracking unit, mix the laggard main fractionating tower of going into, carry out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil then with catalytic cracking main reaction oil gas; Also can adopt independent separation process.
Fractionator overhead B-grade condensation system sets up through changing design on the conventional condensation cooling system of existing fractionation cat head.When upgrading is carried out in raw gasline lighting end or raw gasline last running, can operate by B-grade condensation, when the full cut of raw gasline is carried out upgrading, condensation cooling operation routinely.If upgrading is carried out in last running to the catalytic cracking raw gasline, so corresponding raw gasline lighting end can directly mix with gasoline fraction, also can carry out upgrading after (as etherificate, isomery aromizing etc.) mix with gasoline fraction again.The visible Fig. 1 of this part flow process is summarized as follows: by the top of separation column 1 oil gas 2 (comprising raw gasline and rich gas) that comes out, 3 condensations are cooled to suitable temp (if upgrading is carried out in last running to the catalytic cracking raw gasline, this temperature are 50-60 ℃ through condenser; If upgrading is carried out in lighting end to the catalytic cracking raw gasline, this temperature is 62-80 ℃) after enter separating tank 4 and carry out the separation of profit gas, condensed water 5 detaches separating tank 4 by condensate pump 6.The product liquid that condensation is got off is raw gasline last running 7, extracts out from separating tank 4 through last running petrol-feed pump 8, and a part refluxes 9 as the top of separation column 1, and another part 10 further is cooled to 40 ℃ through supercooler 11.
If to the full fraction upgrading of raw gasline, at this moment valve 23,30 and 31 is opened, valve 24 is closed, and raw gasline last running 10 and raw gasline lighting end 21 are mixed into gets certain appropriate amount 25 behind the full cut 22 of raw gasline and enter the catalytic reforming reactor and carry out upgrading, and rest part 26 enters absorbing-stabilizing system; If to raw gasline last running upgrading, at this moment valve 23,24 and 30 all open, valve 31 is closed, the raw gasline last running 27 of getting certain appropriate amount by flow control directly enters the catalytic reforming reactor and carries out upgrading, rest part 28 enters absorbing-stabilizing system after being mixed into the full cut 22 of raw gasline with raw gasline lighting end 21, at this moment petroleum naphtha 21 can directly with after raw gasline last running 28 mixes enter absorbing-stabilizing system, also can carry out earlier as the petroleum naphtha etherificate, behind the upgrading of aspects such as isomery aromizing, enter absorbing-stabilizing system again with after raw gasline last running 28 mixes.If upgrading is carried out in the raw gasline lighting end, at this moment valve 23,29 and 30 is all opened, valve 24 and 31 is closed, the raw gasline lighting end 32 of getting certain appropriate amount by flow control directly enters the catalytic reforming reactor and carries out upgrading, and rest part and raw gasline last running 28 enter absorbing-stabilizing system after being mixed into the full cut 22 of raw gasline.
Embodiment 1:
The visible Fig. 2 of flow process of the present invention, be summarized as follows: the initial heavy oil feedstock 33 without refining that contains atomizing steam enters through transforming (raw material nozzles raising 0-10 rice, the 0.6-1.0 that the riser reactor internal diameter is reduced into existing riser reactor internal diameter is doubly) the bottom of first riser reactor 34, with the temperature that is promoted by water vapour 36 from revivifier 35 is that 650-750 ℃ high-temperature regenerated catalyst 37 contacts, gasification, mix and reaction, and it is upwards mobile along first riser reactor, mixing herein and temperature of reaction are 450-520 ℃, initial heavy oil feedstock preheating temperature without refining is 160-250 ℃, catalyzer oil plant weight ratio is 7-12, catalyst activity is 50-65, and reaction pressure is 0.1-0.4Mpa.When catalyzer and reaction oil gas rise to the height of riser reactor useful length of 1/3-3/4 (preferred value is 1/2-2/3) (counting) from the heavy oil feedstock feed nozzle, just be equivalent to experience 0.5-2.0s, preferably after the reaction times of 0.8-1.2s, in the riser reactor middle and upper part and from the temperature after the catalytic gasoline upgrading process of inclined tube 38 is 350-480 ℃, micro-activity is that the low temperature high activity catalyst of 50-62 mixes, the temperature of mixed catalyzer and reaction oil gas descends, difference according to upgrading rear catalyst injection rate, to the riser reactor outlet, temperature of reaction is reduced to 450-520 ℃, make the first riser reactor operational depth little, particularly the catalytic diesel oil yield is higher for light oil yield.To the outlet of this riser reactor, revolve 40 separately by efficient fast gas-solid separator 39 and settling vessel top with main reaction oil gas 41 and catalyzer, catalyzer enters stripping stage 43 through settling vessel 42, enters revivifier 35 through behind the stripping.Main reaction oil gas 41 and the reaction oil gas of second riser reactor mix in settling vessel 42 laggardly goes into main fractionating tower 1 bottom and carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil.Contain the recycle stock of atomizing steam and the bottom that reprocessed oil slurry 44 enters second riser reactor 45, with the temperature that is promoted by water vapour 46 from revivifier 35 is that 650-750 ℃ high-temperature regenerated catalyst 47 contacts, gasification, mix and reaction, and it is upwards mobile along second riser reactor, controlling this riser reactor outlet temperature of reaction is 450-520 ℃, the heavy oil feedstock preheating temperature is 250-350 ℃, catalyzer oil plant weight ratio is 5-10, reaction times is 0.5-2.0s, preferred value is 0.8-1.2s, catalyst activity is 50-65, reaction pressure is 0.1-0.4Mpa, relatively large recycle stock and reprocessed oil slurry are carried out catalytic cracking, improve yield of light oil.To this riser reactor outlet, revolve 40 reaction oil gas 49 and catalyzer by efficient fast gas-solid separator 48 and settling vessel top and separate second riser reactor, catalyzer enters stripping stage 43 through settling vessel 42, enters revivifier 35 through behind the stripping.The reaction oil gas 49 of second riser reactor and main reaction oil gas 41 mix in settling vessel 42 laggardly goes into main fractionating tower 1 bottom and carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil.
The catalytically cracked gasoline cut 50 that contains atomizing steam (is that full cut 25 of catalytic cracking raw gasline among Fig. 1 or raw gasline last running (＞60-80 ℃) 27 or raw gasline lighting end (＜80-110 ℃) 32 enter subsidiary riser catalytic reforming reactor 51 from the bottom, with the high-temperature regenerated catalyst that promotes by water vapour 53 of drawing by an inclined tube 52 of setting up on the existing catalytic cracking unit revivifier 35 be 350-500 ℃ in temperature of reaction, the gasoline stocks preheating temperature is 40-200 ℃, catalyzer oil plant weight ratio is 2-20, catalyst activity is 55-65, reaction times is 1.0-10.0s, reaction pressure is to contact under the 0.1-0.4MPa, gasification, mix and reaction, oil gas, water vapour passes through subsidiary riser catalytic reforming reactor 51 with catalyzer, to this reactor outlet, upgrading oil gas and catalyzer subsidiary riser catalytic reforming reactor 51 with settling vessel 54 in revolve by efficient fast gas-solid separator 55 and settling vessel top and to open in 56 minutes, catalyzer enters stripping stage 57, return former revivifier 35 through a part behind water vapour 58 strippings through inclined tube 59, another part is recycled into the height place (counting from the heavy oil feedstock feed nozzle) of riser reactor useful length of the first riser reactor 1/3-3/4 (preferred value is 1/2-2/3) of existing heavy oil catalytically cracking equipment through inclined tube 38.The catalytic amount that is recycled into first riser reactor of existing heavy oil catalytically cracking equipment through inclined tube 38 is the 40-100% of subsidiary riser catalytic reforming reactor catalyst internal circulating load.After upgrading oil gas 60 leaves settling vessel 54, the main oil gas piping of incorporating former catalytic cracking unit into mixes laggardly to go into the main fractionating tower bottom and carry out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil with the reaction oil gas of first and second riser reactors.
Embodiment 2:
The present invention also comprises flow process shown in Figure 3 for the mode that the catalyzer of the low temperature high activity that is come out by subsidiary riser catalytic reforming reactor is recycled into former catalytic cracking unit first riser reactor, be summarized as follows: the initial heavy oil feedstock 33 without refining that contains atomizing steam enters through transforming (raw material nozzles raising 0-10 rice, the 0.6-1.0 that the riser reactor internal diameter is reduced into existing riser reactor internal diameter is doubly) the bottom of first riser reactor 34, with the temperature that is promoted by water vapour 36 from revivifier 35 is that 650-750 ℃ high-temperature regenerated catalyst 37 contacts, gasification, mix and reaction, and it is upwards mobile along first riser reactor, mixing herein and temperature of reaction are 520-600 ℃, initial heavy oil feedstock preheating temperature without refining is 160-250 ℃, catalyzer oil plant weight ratio is 7-12, catalyst activity is 50-65, and reaction pressure is 0.1-0.4Mpa.The 1/3-3/4 (preferred value is 1/2-2/3) that rises to the riser reactor virtual height when catalyzer and reaction oil gas (is counted from the heavy oil feedstock feed nozzle) when locating, just be equivalent to experience 0.5-2.0s, preferably after the reaction times of 0.8-1.2s, in the riser reactor middle and upper part and from the temperature after the catalytic gasoline upgrading process of inclined tube 38 is 350-480 ℃, micro-activity is that the low temperature high activity catalyst of 50-62 mixes, the temperature of mixed catalyzer and reaction oil gas descends, according to the difference of upgrading rear catalyst injection rate, temperature decline degree difference.At this riser tube vertical section 341 more than inlet, the diameter of riser reactor can add 1.0-2.0 times of greatly existing riser reactor diameter, thereby increase the residence time and the back-mixing degree of catalyzer in this section riser reactor, the olefin(e) centent that this helps improving the depth of conversion of heavy oil fluid catalytic cracking and reduces catalytic gasoline.In the riser reactor outlet, temperature of reaction can be controlled between 450-500 ℃, makes the first riser reactor operational depth little, and particularly the catalytic diesel oil yield is higher for light oil yield.To the outlet of this riser reactor, revolve 40 separately by efficient fast gas-solid separator 39 and settling vessel top with main reaction oil gas 41 and catalyzer, catalyzer enters stripping stage 43 through settling vessel 42, enters revivifier 35 through behind the stripping.Main reaction oil gas 41 and the reaction oil gas of second riser reactor mix in settling vessel 42 laggardly goes into main fractionating tower 1 bottom and carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil.Contain the recycle stock of atomizing steam and the bottom that reprocessed oil slurry 44 enters second riser reactor 45, with the temperature that is promoted by water vapour 46 from revivifier 35 is that 650-750 ℃ high-temperature regenerated catalyst 47 contacts, gasification, mix and reaction, and it is upwards mobile along second riser reactor, controlling this riser reactor outlet temperature of reaction is 450-520 ℃, the heavy oil feedstock preheating temperature is 250-350 ℃, catalyzer oil plant weight ratio is 5-10, reaction times is 0.5-2.0s, preferred value is 0.8-1.2s, catalyst activity is 50-65, reaction pressure is 0.1-0.4Mpa, relatively large recycle stock and reprocessed oil slurry are carried out catalytic cracking, improve yield of light oil.To this riser reactor outlet, revolve 40 reaction oil gas 49 and catalyzer by efficient fast gas-solid separator 48 and settling vessel top and separate second riser reactor, catalyzer enters stripping stage 43 through settling vessel 42, enters revivifier 35 through behind the stripping.The reaction oil gas 49 of second riser reactor and main reaction oil gas 41 mix in settling vessel 42 laggardly goes into main fractionating tower 1 bottom and carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil.
Embodiment 3:
The present invention also comprises flow process shown in Figure 4 for the mode that the catalyzer of the low temperature high activity that is come out by subsidiary riser catalytic reforming reactor is recycled into existing catalytic cracking unit first riser reactor, be summarized as follows: existing catalytic cracking unit revivifier 35 is connected with a catalyst mix jar 61, regenerated catalyst is guided to the bottom of catalyst mix jar 61 with an inclined tube 62 of drawing the high-temperature regenerated catalyst logistics of setting up on the revivifier 35, also existing catalytic cracking unit normal need metathetical is had neither part nor lot in catalyst for reaction 63 simultaneously and introduce catalyst mix jar 61, high reactivity behind the catalytic gasoline upgrading of a part by the catalytic gasoline upgrading assisted reaction system that sets up, (this part is the 20-100% of total amount to the reclaimable catalyst of low temperature, another part turns back in the former revivifier 35 through inclined tube 59) also introduce in this catalyst mix jar 61 through inclined tube 64, three bursts of catalyst stream are under the fluidisation of the fluidization air 65 of catalyst mix jar 61 bottoms introducing, mix on one side, burn reaction on one side, the fluidizing medium of carrying little amount of catalyst secretly returns in the former catalytic cracking unit revivifier 35 through pipeline 66.The catalyzer that mixed temperature reduces enters through transforming (raw material nozzles raising 0-10 rice through inclined tube 67, the 0.6-1.0 that the riser reactor internal diameter is reduced into existing riser reactor internal diameter is doubly) the bottom of first riser reactor 34, upwards promote by pre-lifting steam 36, contact with the initial heavy oil feedstock 33 that contains atomizing steam without refining, gasification, mix and reaction, and it is upwards mobile along first riser reactor, controlling this riser reactor outlet temperature of reaction is 450-520 ℃, the heavy oil feedstock preheating temperature is 160-250 ℃, catalyzer oil plant weight ratio is 5-10, reaction times is 0.5-2.0s, preferred value is 0.8-1.2s, catalyst activity is 50-65, reaction pressure is 0.1-0.4Mpa, makes the first riser reactor operational depth little, and particularly the catalytic diesel oil yield is higher for light oil yield.To the outlet of this riser reactor, revolve 40 separately by efficient fast gas-solid separator 39 and settling vessel top with main reaction oil gas 41 and catalyzer, catalyzer enters stripping stage 43 through settling vessel 42, enters revivifier 35 through behind the stripping.Main reaction oil gas 41 and the reaction oil gas of second riser reactor mix in settling vessel 42 laggardly goes into main fractionating tower 1 bottom and carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil.Contain the recycle stock of atomizing steam and the bottom that reprocessed oil slurry 44 enters second riser reactor 45 together, with the temperature that is promoted by water vapour 46 from revivifier 35 is that 650-750 ℃ high-temperature regenerated catalyst 47 contacts, gasification, mix and reaction, and it is upwards mobile along second riser reactor, controlling this riser reactor outlet temperature of reaction is 450-520 ℃, the heavy oil feedstock preheating temperature is 250-350 ℃, catalyzer oil plant weight ratio is 5-10, reaction times is 0.5-2.0s, preferred value is 0.8-1.2s, catalyst activity is 50-65, reaction pressure is 0.1-0.4Mpa, relatively large recycle stock and reprocessed oil slurry are carried out catalytic cracking, improve yield of light oil.To this riser reactor outlet, revolve 40 reaction oil gas 49 and catalyzer by efficient fast gas-solid separator 48 and settling vessel top and separate second riser reactor, catalyzer enters stripping stage 43 through settling vessel 42, enters revivifier 35 through behind the stripping.The reaction oil gas 49 of second riser reactor and main reaction oil gas 41 mix in settling vessel 42 laggardly goes into main fractionating tower 1 bottom and carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil.
The catalytically cracked gasoline cut 50 that contains atomizing steam (is that full cut 25 of catalytic cracking raw gasline among Fig. 1 or raw gasline last running (＞60-80 ℃) 27 or raw gasline lighting end (＜80-110 ℃) 32 enter subsidiary riser catalytic reforming reactor 51 from the bottom, with the high-temperature regenerated catalyst that promotes by water vapour 53 of drawing by an inclined tube 52 of setting up on the existing catalytic cracking unit revivifier 35 be 350-500 ℃ in temperature of reaction, the gasoline stocks preheating temperature is 40-200 ℃, catalyzer oil plant weight ratio is 2-20, catalyst activity is 55-65, reaction times is 1.0-10.0s, reaction pressure is to contact under the 0.1-0.4MPa, gasification, mix and reaction, oil gas, water vapour passes through subsidiary riser catalytic reforming reactor 51 with catalyzer, to this reactor outlet, upgrading oil gas and catalyzer subsidiary riser catalytic reforming reactor 51 with settling vessel 64 in revolve by efficient fast gas-solid separator 55 and settling vessel top and to open in 56 minutes, catalyzer enters stripping stage 57, return former revivifier 35 through a part behind water vapour 58 strippings through inclined tube 59, another part is got back to catalyst mix jar 61 through inclined tube 64.After upgrading oil gas 60 leaves settling vessel 54, the main oil gas piping of incorporating former catalytic cracking unit into mixes laggardly to go into the main fractionating tower bottom and carry out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil with the reaction oil gas of first and second riser reactors.
Embodiment 4:
The present invention also comprises flow process shown in Figure 5 for the mode that the catalyzer by the low temperature high activity that is come out by subsidiary riser catalytic reforming reactor shown in Figure 4 is recycled into former catalytic cracking unit, be at other under all constant situations, the regenerated catalyst that enters subsidiary riser catalytic reforming reactor 51 from the bottom is from catalyst mix jar 61.
The present invention falls the auxiliary fluidizing reactor that alkene uses for the catalytic gasoline upgrading and also comprises following several form:
Embodiment 5:
Auxiliary fluidized catalytic reforming reactor is that riser tube adds the turbulent bed reactor among Fig. 2, can obtain the invention flow process of Fig. 6 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, and gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, promote the reaction times of pipeline section: 1.0-10.0s, fluidized-bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 6:
Auxiliary fluidized catalytic reforming reactor is that riser tube adds the turbulent bed reactor among Fig. 3, can obtain the invention flow process of Fig. 7 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, and gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, promote the reaction times of pipeline section: 1.0-10.0s, fluidized-bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 7:
Auxiliary fluidized catalytic reforming reactor is that riser tube adds the turbulent bed reactor among Fig. 4, can obtain the invention flow process of Fig. 8 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, and gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, promote the reaction times of pipeline section: 1.0-10.0s, fluidized-bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 8:
Auxiliary fluidized catalytic reforming reactor is that riser tube adds the turbulent bed reactor among Fig. 5, can obtain the invention flow process of Fig. 9 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, and gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, promote the reaction times of pipeline section: 1.0-10.0s, fluidized-bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 9:
Auxiliary fluidized catalytic reforming reactor is the turbulent bed reactor among Fig. 2, can obtain the invention flow process of Figure 10 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-300 ℃, catalyst activity: 50-65, turbulent bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 10:
Auxiliary fluidized catalytic reforming reactor is the turbulent bed reactor among Fig. 3, can obtain the invention flow process of Figure 11 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-300 ℃, catalyst activity: 50-65, turbulent bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 11:
Auxiliary fluidized catalytic reforming reactor is the turbulent bed reactor among Fig. 4, can obtain the invention flow process of Figure 12 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-300 ℃, catalyst activity: 50-65, turbulent bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 12:
Auxiliary fluidized catalytic reforming reactor is the turbulent bed reactor among Fig. 5, can obtain the invention flow process of Figure 13 thus, wherein, the upgrading reaction conditions is: temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-300 ℃, catalyst activity: 50-65, turbulent bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa.
Embodiment 13:
Auxiliary fluidized catalytic reforming reactor is the fast bed reactor among Fig. 2, can obtain the invention flow process of Figure 14 thus, wherein, the upgrading reaction conditions is: temperature of reaction is 350-500 ℃, the gasoline stocks preheating temperature is 40-300 ℃, and catalyst activity is 50-65, and the bed linear speed is 0.6-2.5m/s, reaction times is 0.1-10.0 minute, and reaction pressure is 0.1-0.4Mpa.
Embodiment 14:
Auxiliary fluidized catalytic reforming reactor is the fast bed reactor among Fig. 3, can obtain the invention flow process of Figure 15 thus, wherein, the upgrading reaction conditions is: temperature of reaction is 350-500 ℃, the gasoline stocks preheating temperature is 40-300 ℃, and catalyst activity is 50-65, and the bed linear speed is 0.6-2.5m/s, reaction times is 0.1-10.0 minute, and reaction pressure is 0.1-0.4Mpa.
Embodiment 15:
Auxiliary fluidized catalytic reforming reactor is the fast bed reactor among Fig. 4, can obtain the invention flow process of Figure 16 thus, wherein, the upgrading reaction conditions is: temperature of reaction is 350-500 ℃, the gasoline stocks preheating temperature is 40-300 ℃, and catalyst activity is 50-65, and the bed linear speed is 0.6-2.5m/s, reaction times is 0.1-10.0 minute, and reaction pressure is 0.1-0.4Mpa.
Embodiment 16:
Auxiliary fluidized catalytic reforming reactor is the fast bed reactor among Fig. 5, can obtain the invention flow process of Figure 17 thus, wherein, the upgrading reaction conditions is: temperature of reaction is 350-500 ℃, the gasoline stocks preheating temperature is 40-300 ℃, and catalyst activity is 50-65, and the bed linear speed is 0.6-2.5m/s, reaction times is 0.1-10.0 minute, and reaction pressure is 0.1-0.4Mpa.
It should be noted last that, above embodiment is only unrestricted in order to technical scheme of the present invention to be described, although the present invention is had been described in detail with reference to preferred embodiment, those of ordinary skill in the art is to be understood that, can make amendment or be equal to replacement technical scheme of the present invention, and not breaking away from the spirit and scope of technical solution of the present invention, it all should be encompassed in the middle of the claim scope of the present invention.
Claims (20)
1, the method for a kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulation and control is characterized in that: comprise the steps: at least
Step 1: will send into first riser reactor bottom of heavy oil catalytically cracking equipment without the initial heavy oil feedstock of refining, and carry out catalytic cracking reaction; Reaction oil gas is in this reactor middle and upper part and the catalyst mix of injecting from auxiliary fluidized catalytic reforming reactor, and main reaction oil gas separates at this reactor outlet with catalyzer; Catalyzer enters regeneration system rapidly, and main reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 2: recycle stock and reprocessed oil slurry are sent into second riser reactor bottom, proceed catalytic cracking reaction, reaction oil gas and catalyzer enter regeneration system rapidly at this reactor outlet separating catalyst, and reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 3: the catalytically cracked gasoline cut is sent into auxiliary fluidized catalytic reforming reactor, carry out the gasoline upgrading reaction, a upgrading rear catalyst part is returned former revivifier, another part is recycled into first riser reactor of heavy oil catalytically cracking equipment, and upgrading oil gas enters fractionating system and carries out each fraction separation.
2, the method for a kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulation and control is characterized in that: comprise the steps: at least
Step 1: with the regenerated catalyst of heavy oil catalytically cracking equipment, from a part of reclaimable catalyst of gasoline upgrading reactor with have neither part nor lot in catalyst for reaction and introduce simultaneously in the catalyst mix jar and mix, this blended catalyzer is under the rheomorphism of the air of introducing from the mixing tank bottom, burn reaction, send the revivifier of catalytic cracking unit then back to;
Step 2: will send into first riser reactor bottom without the initial heavy oil feedstock of refining, after catalyst mix from the catalyst mix jar, carry out catalytic cracking reaction, main reaction oil gas separates at this reactor outlet with catalyzer, catalyzer enters the catalyst mix jar after returning revivifier, and main reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 3: recycle stock and reprocessed oil slurry are sent into second riser reactor bottom, proceed catalytic cracking reaction; Reaction oil gas separates at this reactor outlet with catalyzer, and catalyzer enters the catalyst mix jar after returning revivifier, and reaction oil gas carries out separating of rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock and slurry oil;
Step 4: the catalytically cracked gasoline cut is sent into auxiliary fluidized catalytic reforming reactor, carry out the gasoline upgrading reaction, a upgrading rear catalyst part is returned former revivifier, and another part is injected into the catalyst mix jar, and upgrading oil gas enters fractionating system and carries out each fraction separation.
3, the method for high-efficiency heavy oil cracking according to claim 1 and gasoline upgrading coupling regulation and control is characterized in that:
Reaction conditions in first riser reactor is:
Temperature of reaction: 450-520 ℃;
Heavy oil feedstock preheating temperature: 160-250 ℃;
Catalyzer oil plant weight ratio: 7-12;
Reaction times: 0.5-2.0s, preferred value is 0.8-1.2s;
Catalyst activity: 50-65;
Reaction pressure: 0.1-0.4Mpa.
4, the method for high-efficiency heavy oil cracking according to claim 2 and gasoline upgrading coupling regulation and control is characterized in that:
Reaction conditions in first riser reactor is:
Temperature of reaction: 450-520 ℃;
Heavy oil feedstock preheating temperature: 160-250 ℃;
Catalyzer oil plant weight ratio: 5-10;
Reaction times: 0.5-2.0s, preferred value is 0.8-1.2s;
Catalyst activity: 50-65;
Reaction pressure: 0.1-0.4Mpa.
5, the method for high-efficiency heavy oil cracking according to claim 1 and 2 and gasoline upgrading coupling regulation and control is characterized in that:
Reaction conditions in second riser reactor is:
Temperature of reaction: 450-520 ℃;
Heavy oil feedstock preheating temperature: 250-350 ℃;
Catalyzer oil plant weight ratio: 5-10;
Reaction times: 0.5-2.0s, preferred value is 0.8-1.2s;
Catalyst activity: 50-65;
Reaction pressure: 0.1-0.4Mpa.
6, the method for high-efficiency heavy oil cracking according to claim 2 and gasoline upgrading coupling regulation and control, it is characterized in that: in the described step 4, enter revivifier or the catalyst mix jar of the catalyzer of auxiliary fluidized catalytic reforming reactor from catalytic cracking unit.
7, the method for high-efficiency heavy oil cracking according to claim 1 and 2 and gasoline upgrading coupling regulation and control, it is characterized in that: described catalytically cracked gasoline cut comprises the full cut of raw gasline or raw gasline lighting end (＜80-110 ℃) or raw gasline last running (＞60-80 ℃) at least.
8, the method for high-efficiency heavy oil cracking according to claim 1 and 2 and gasoline upgrading coupling regulation and control, it is characterized in that: described catalyzer is conventional catalytic cracking catalyst, comprises amorphous silicon aluminium catalyzer or molecular sieve catalyst at least.
9, the method for high-efficiency heavy oil cracking according to claim 1 and 2 and gasoline upgrading coupling regulation and control is characterized in that: upgrading oil gas is separated into rich gas, raw gasline lighting end, raw gasline last running, diesel oil, recycle stock, slurry oil with entering the main fractionating tower of former catalytic cracking unit after the oil gas of main riser reactor mixes; Perhaps entering independent fractionating system separates.
10, the device of a kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulation and control comprises a heavy oil catalytically cracking equipment at least, and this device connects a fractionation plant; It is characterized in that: heavy oil catalytically cracking equipment comprises two riser reactors at least, is used to finish the catalytic cracking reaction of heavy oil feedstock; Wherein, the middle and upper part of first riser reactor is provided with the catalyzer decanting point, and this decanting point connects auxiliary fluidized catalytic reforming reactor by inclined tube, is used for upgrading catalytically cracked gasoline cut; This reforming reactor is connected with the revivifier of catalytic cracking unit.
11, the device of a kind of high-efficiency heavy oil cracking and gasoline upgrading coupling regulation and control comprises a heavy oil catalytically cracking equipment at least, and this device connects a fractionation plant; It is characterized in that: heavy oil catalytically cracking equipment comprises two riser reactors at least, is used to finish the catalytic cracking reaction of heavy oil feedstock; Wherein, first riser reactor is connected with a catalyst mix jar; The catalytic cracking unit revivifier is provided with an auxiliary fluidized catalytic reforming reactor, is used for upgrading catalytically cracked gasoline cut; This reforming reactor links to each other with mixing tank respectively with revivifier.
12, according to the device of claim 10 or 11 described high-efficiency heavy oil crackings and gasoline upgrading coupling regulation and control, it is characterized in that: the raw material nozzles of described first riser reactor improves 0-10 rice than the raw material nozzles of existing riser reactor, and this first riser reactor internal diameter is 0.6-1.0 times of existing riser reactor internal diameter.
13, the device of high-efficiency heavy oil cracking according to claim 10 and gasoline upgrading coupling regulation and control, it is characterized in that: the position of the first riser reactor catalyzer decanting point is located at the 1/3-3/4 place of its raw material nozzles to the reactor virtual height, and preferred value is the 1/2-2/3 place of its bottom to the reactor virtual height.
14, according to the device of claim 10 or 13 described high-efficiency heavy oil crackings and gasoline upgrading coupling regulation and control, it is characterized in that: the diameter of the vertical section that the first riser reactor catalyzer decanting point is above for the 1.0-2.0 of existing riser reactor diameter doubly.
15, according to the device of claim 10 or 11 described high-efficiency heavy oil crackings and gasoline upgrading coupling regulation and control, it is characterized in that: described second riser reactor is inserted in the settling vessel of catalytic cracking unit, and in its outlet the efficient gas-solid separating device identical or different with first riser reactor is installed.
16, according to the device of claim 10 or 11 described high-efficiency heavy oil crackings and gasoline upgrading coupling regulation and control, it is characterized in that: described auxiliary fluidized catalytic reforming reactor is that riser reactor or riser tube add turbulent bed reactor or turbulent bed reactor or fast bed reactor.
17, the device of high-efficiency heavy oil cracking according to claim 16 and gasoline upgrading coupling regulation and control is characterized in that:
When using riser reactor, the upgrading reaction conditions is:
Temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, reaction times: 1.0-10.0s, reaction pressure: 0.1-0.4Mpa;
When using riser tube to add the turbulent bed reactor, the upgrading reaction conditions is:
Temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-200 ℃, catalyzer oil plant weight ratio: 2-20, catalyst activity: 55-65, promote the reaction times of pipeline section: 1.0-10.0s, fluidized-bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa;
When using the turbulent bed reactor, the upgrading reaction conditions is:
Temperature of reaction: 350-500 ℃, gasoline stocks preheating temperature: 40-300 ℃, catalyst activity: 50-65, turbulent bed weight space velocity: 1-1000/ hour, reaction pressure: 0.1-0.4Mpa;
When using the fast bed reactor, the upgrading reaction conditions is:
Temperature of reaction is 350-500 ℃, and the gasoline stocks preheating temperature is 40-300 ℃, and catalyst activity is 50-65, and the bed linear speed is 0.6-2.5m/s, and the reaction times is 0.1-10.0 minute, and reaction pressure is 0.1-0.4Mpa.
18, according to the device of claim 10 or 11 described high-efficiency heavy oil crackings and gasoline upgrading coupling regulation and control, it is characterized in that: described auxiliary fluidized catalytic reforming reactor is provided with independently sedimenting system and stripping system, is respectively applied for the sedimentation and the stripping of catalyzer.
19, according to the device of claim 10 or 11 described high-efficiency heavy oil crackings and gasoline upgrading coupling regulation and control, it is characterized in that: described fractionation plant is the fractionation plant of catalytic cracking unit or independent fractionation plant.
20, according to the device of claim 10 or 11 described high-efficiency heavy oil crackings and gasoline upgrading coupling regulation and control, it is characterized in that: described fractionation plant comprises conventional condenser system and B-grade condensation system at least, and this B-grade condensation system is used for obtaining the full cut of raw gasline or raw gasline lighting end or raw gasline last running.
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|---|---|---|---|
| CN 02149316 CN1233801C (en) | 2002-11-07 | 2002-11-07 | Method and device for adjusting and controlling coupling between cracking heavy oil and transnaturing gasoline in high efficiency |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02149316 CN1233801C (en) | 2002-11-07 | 2002-11-07 | Method and device for adjusting and controlling coupling between cracking heavy oil and transnaturing gasoline in high efficiency |
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| CN1498950A true CN1498950A (en) | 2004-05-26 |
| CN1233801C CN1233801C (en) | 2005-12-28 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101992046B (en) * | 2009-08-31 | 2013-03-06 | 中国石油化工股份有限公司 | Parallel combined riser circular reaction-regeneration device |
| CN111218297A (en) * | 2018-11-23 | 2020-06-02 | 中国石油天然气股份有限公司 | Combined method for catalytic cracking and etherification |
| CN115404095A (en) * | 2022-09-16 | 2022-11-29 | 北京拓川科研设备股份有限公司 | Multifunctional full-automatic catalytic cracking device |
-
2002
- 2002-11-07 CN CN 02149316 patent/CN1233801C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101992046B (en) * | 2009-08-31 | 2013-03-06 | 中国石油化工股份有限公司 | Parallel combined riser circular reaction-regeneration device |
| CN111218297A (en) * | 2018-11-23 | 2020-06-02 | 中国石油天然气股份有限公司 | Combined method for catalytic cracking and etherification |
| CN111218297B (en) * | 2018-11-23 | 2021-09-28 | 中国石油天然气股份有限公司 | Combined method for catalytic cracking and etherification |
| CN115404095A (en) * | 2022-09-16 | 2022-11-29 | 北京拓川科研设备股份有限公司 | Multifunctional full-automatic catalytic cracking device |
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| CN1233801C (en) | 2005-12-28 |
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