CN100424154C - Catalytic cracking desulfur method of faulty gasoline and device thereof - Google Patents
Catalytic cracking desulfur method of faulty gasoline and device thereof Download PDFInfo
- Publication number
- CN100424154C CN100424154C CNB2006100484081A CN200610048408A CN100424154C CN 100424154 C CN100424154 C CN 100424154C CN B2006100484081 A CNB2006100484081 A CN B2006100484081A CN 200610048408 A CN200610048408 A CN 200610048408A CN 100424154 C CN100424154 C CN 100424154C
- Authority
- CN
- China
- Prior art keywords
- gasoline
- catalyst
- reactor
- bed reactor
- settling vessel
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention discloses a catalytic cracking desulfurization method of low-grade gasoline in the field of petroleum processing technology and its equipment. It is characterized by that the invented gasoline upgrading reactor adopts gasoline fast bed reactor with cylindrical structure, a portion of spent catalyst can be passed through spent catalyst coveying pipeline with flow control valve and fed into catalyst mixer, and is mixed together with regenerated catalyst coming from regenerator under the action of aqueous vapor, then fed into gasoline fast bed reactor and is contacted with low-grade gasoline feed so as to make reaction to greatly reduce sulfur content of low-grade gasoline.
Description
Technical field
The invention belongs to the refining of petroleum field, relate to a kind of catalytic cracking desulfur method of faulty gasoline and device.
Background technology
In order to control the pollutant emission of vehicle exhaust, strict restriction has been made to the olefin(e) centent and the sulphur content of motor spirit by the main developed country in the world.World fuel standard II, III and IV class motor spirit standard-required sulphur content are respectively less than 200 μ g/g, 30 μ g/g and 10 μ g/g, and olefin(e) centent is respectively less than 20v%, 10v% and 10v% (v% represents percent by volume); Europe III, Europe IV motor spirit emission standard require content of sulfur in gasoline respectively less than 150 μ g/g and 50 μ g/g, and olefin(e) centent is less than 18v%.The 80w% of China's motor spirit is from catalytic cracking process (w% represents weight percentage), olefin(e) centent and sulphur content are all higher, therefore reducing inferior patrol, particularly reduce the olefin(e) centent and the sulphur content of catalytically cracked gasoline, is the key that realizes the motor spirit quality upgrading.
The existing at present effective ways that reduce content of olefin in gasoline, but gasoline desulfur remains a difficult problem.The sulphur content of utilizing catalytic cracking unit to reduce in the gasoline mainly contains following several method: (1) reduces the gasoline cut point, and as the final boiling point of gasoline is reduced to 200 ℃ from 220 ℃, content of sulfur in gasoline approximately can reduce 35w%.(2) catalytic cracking original position desulfurization promptly adds a certain proportion of desulfurization catalyst or auxiliary agent in FCC (fluid catalytic cracking) Primary Catalysts.This method gasoline desulfur rate is on the low side, generally below 30w%.The catalytic cracking sulfur-reducing auxiliary agent that " oil Refining Technologies and engineering " 2005 the 6th phases the 31st～33 page of " industrial application of catalytically cracked gasoline sulfur prodegradant LDS-S1 " literary composition introduced, employing accounts for the promoter addition of catalyst inventory 10w%, can make content of sulfur in gasoline decline 23.47w%.(3) adopt catalytic cracking and desulfurizing technology and method.The catalysis conversion method and the device thereof of the disclosed a kind of modifying inferior patrol of Chinese patent CN1401740A, employing is provided with the double-reactor catalytic cracking process and the device of two riser reactors (heavy oil riser reactor and gasoline rising pipe reactor), and two riser reactors all can processed different stock oil separately under the optimized reaction conditions separately.Wherein in the gasoline rising pipe reactor, inferior patrol is carried out upgrading, make full use of the favourable condition of high reactivity state catalyzer, for the desirable secondary reaction of gasoline provides independently upgrading space and reaction times fully, avoided influencing each other of gasoline upgrading and heavy oil cracking.With respect to the inferior patrol before the upgrading, the olefin(e) centent of gasoline rising pipe reformulated gasoline that reactor produces can reduce by 15～50 white branches of volume.But because the gasoline upgrading reactor adopts riser reactor, agent-oil ratio is on the low side, the reaction times is shorter, and the content of sulfur in gasoline decline scope is limited, the sulphur content 5～30w% that only descends.
U.S. Pat 6,287, related LOCC technology among the 522B1, utilize a kind of double lift pipe catalytic cracking device, will by major part from the lighter hydrocarbons riser reactor without steam stripped reclaimable catalyst and deliver on a small quantity the bottom of heavy oil riser reactor by a catalyst transport from the mixing reclaimable catalyst of forming without steam stripped reclaimable catalyst of heavy oil riser reactor, mix with the high-temperature regenerated catalyst from revivifier, mixed catalyzer is up and heavy oil riser reactor charging contact reacts in the heavy oil riser reactor.This technology is utilized the higher active and lower temperature of the reclaimable catalyst of lighter hydrocarbons riser reactor, reduced the temperature of the catalyzer that contacts with the charging of heavy oil riser reactor, can reduce the heat cracking reaction of heavy oil riser reactor and promote catalytic cracking reaction, improve product and distribute.But because this method self-circulation catalyzer do not deliver to the lighter hydrocarbons riser reactor, make the agent-oil ratio of lighter hydrocarbons riser reactor less, the reaction times is shorter, thereby the gasoline desulfur effect is relatively poor.
Disclosed a kind of method and the device thereof that reduces gasoline olefin of Chinese patent CN1401741A, it is a kind of double lift pipe catalytic cracking device (being provided with heavy oil riser reactor and gasoline rising pipe reactor) that utilizes the catalyzer self-circulation, to deliver to the bottom of gasoline rising pipe reactor from half reclaimable catalyst of gasoline rising pipe reactor with from the mixed catalyst that the regenerated catalyst of revivifier is formed by part, with gasoline rising pipe reactor feed contact reacts.Because the gasoline upgrading reactor adopts riser reactor, so agent-oil ratio is on the low side, the reaction times is shorter.With respect to the inferior patrol before the upgrading, the olefin(e) centent of gasoline rising pipe reformulated gasoline that reactor produces can reduce by 15～50 volume percentage points, but the content of sulfur in gasoline decline scope is limited, the sulphur content 10～30w% that only descends.
Summary of the invention
Technical problem to be solved by this invention is: agent-oil ratio is on the low side, the reaction times is shorter because of gasoline upgrading reactor employing riser reactor makes for existing double lift pipe catalytic cracking technology and device, causes the limited problem of reformulated gasoline sulphur content fall.
For addressing the above problem, the technical solution used in the present invention is: a kind of catalytic cracking desulfur method of faulty gasoline is characterized in that being made up of following process:
A. enter the bottom of heavy oil riser reactor from a part of regenerated catalyst of revivifier, contacting the back with the charging of heavy oil riser reactor reacts along the heavy oil riser reactor is up, after reaction finishes, reactant flow enters first settling vessel by the top exit of heavy oil riser reactor and carries out catalyzer and gas-oil separation, isolated heavy oil riser reactor reaction oil gas enters fractionating system and carries out fractionation, isolated reclaimable catalyst enters behind stripping and carries out coke burning regeneration in the revivifier, a regenerated catalyst part is returned the heavy oil riser reactor, and another part enters the catalyst mix device;
B. in second inclined tube to be generated from gasoline fast bed reactor, at a part of reclaimable catalyst of the second settling vessel stripping stage behind stripping, through the reclaimable catalyst transfer lime, under the adjusting of flowrate control valve set on the reclaimable catalyst transfer lime, enter the catalyst mix device, with regenerated catalyst from process A, up and the mixing at the effect lower edge catalyst mix device of the water vapor that feeds by the steam distributor of being located in the catalyst mix device, enter the bottom of gasoline fast bed reactor through pipe connecting, contact the back along up reaction of gasoline fast bed reactor with the inferior patrol charging, after reaction finishes, reactant flow enters second settling vessel by the top of gasoline fast bed reactor through conduit and carries out catalyzer and gas-oil separation, isolated gasoline fast bed reactor reaction oil gas enters fractionating system and carries out fractionation, obtain the reformulated gasoline product, the isolated reclaimable catalyst of second settling vessel enters second to be generated inclined tube by second regeneration standpipe at the second settling vessel stripping stage behind stripping, reclaimable catalyst part in second inclined tube to be generated enters the catalyst mix device through the reclaimable catalyst transfer lime, and another part enters and carries out coke burning regeneration in the revivifier;
The above-mentioned weight rate that enters the reclaimable catalyst of catalyst mix device through the reclaimable catalyst transfer lime is 5～80w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage, the temperature of reaction of gasoline fast bed reactor is 400～550 ℃, reaction times is that (s is second to 3～10s, down together), agent-oil ratio is 10～50, and the reaction absolute pressure is 0.15～0.40MPa.
Be used to realize the inferior patrol catalytic cracking and desulfurizing device of above-mentioned catalytic cracking desulfur method of faulty gasoline, be provided with the heavy oil riser reactor, first settling vessel, revivifier, the gasoline upgrading reactor, second settling vessel, the top exit of heavy oil riser reactor is connected with first settling vessel, the bottom is provided with heavy oil riser reactor feed entrance, the bottom is connected with revivifier by first regenerator sloped tube and the first regeneration standpipe, the below of first settling vessel is provided with the first settling vessel stripping stage, the below of the first settling vessel stripping stage is provided with first regeneration standpipe, first regeneration standpipe is connected with revivifier, the below of second settling vessel is provided with the second settling vessel stripping stage, the below of the second settling vessel stripping stage is provided with second regeneration standpipe and second inclined tube to be generated, the second settling vessel stripping stage is connected with revivifier, inferior patrol catalytic cracking and desulfurizing device also is provided with the second regeneration standpipe, second regenerator sloped tube and catalyst mix device, be provided with the reclaimable catalyst transfer lime between second inclined tube to be generated and the catalyst mix device, the reclaimable catalyst transfer lime is provided with flowrate control valve, it is characterized in that: the gasoline upgrading reactor is columnar structured gasoline fast bed reactor, gasoline fast bed reactor is provided with cylindrical drum, the top and the bottom of cylindrical drum are respectively equipped with conical section, be provided with conduit between the conical section at top and second settling vessel, the conical section of bottom is provided with the inferior patrol feed entrance, the exit end of conduit is provided with quick disconnector, described catalyst mix device is columnar structured, be located at the below of gasoline fast bed reactor, the catalyst mix device is provided with cylindrical drum, the top of cylindrical drum is provided with conical section, the bottom is provided with end socket, the bottom of catalyst mix device is provided with steam distributor, be provided with pipe connecting between the conical section of the conical section at catalyst mix device cylindrical drum top and gasoline fast bed reactor cylinder shape cylindrical shell bottom, described reclaimable catalyst transfer lime is connected on the cylindrical drum of catalyst mix device, the described second regeneration standpipe and second regenerator sloped tube are between revivifier and catalyst mix device, and second regenerator sloped tube is connected on the cylindrical drum of catalyst mix device.
Adopt the present invention, have following beneficial effect: the present invention improves existing double lift pipe catalytic cracking technology and device, and its gasoline upgrading reactor does not adopt riser reactor but adopts columnar structured gasoline fast bed reactor.Gasoline fast bed reactor is a circulating fluid bed reactor, solid (catalyzer) the internal circulating load G in the operating process in the reactor
SAt 15～50kg/m
3Scope in, gas speed (total speed of all oil gas and water vapor by beds) is in the scope of 1.0～3.0m/s.Because being gasoline and operational condition, the charging of gasoline fast bed reactor relaxes, so the carbon content of its reclaimable catalyst is lower, the activity is higher.A part of reclaimable catalyst of gasoline fast bed reactor is circulated to gasoline fast bed reactor again, the reclaimable catalyst carbon content that has made full use of gasoline fast bed reactor in the double-reactor catalytic cracking unit of the present invention is lower, and (carbon content is generally 0.05～0.40w%), the characteristics of active higher (micro-activity is generally 53～65), makes it mix the reaction of participation gasoline fast bed reactor afterwards with regenerated catalyst from revivifier in the catalyst mix device.Above-mentioned reclaimable catalyst all from gasoline fast bed reactor and at second settling vessel stripping stage process stripping, has improved the overall activity of the mixed catalyst that participates in gasoline fast bed reactor reaction.The reclaimable catalyst transfer lime is provided with flowrate control valve, the flow that enters in the catalyst mix device be can regulate, and reclaimable catalyst and the blending ratio of regenerated catalyst and the temperature of mixed catalyst regulated from gasoline fast bed reactor and the steam stripped reclaimable catalyst of process.Reclaimable catalyst in the catalyst mix device and regenerated catalyst can thorough mixing under the effect of water vapor, catalyzer after mixing enters gasoline fast bed reactor again and the reactor feed of gasoline fast bed---inferior patrol fully contacts and reacts, thereby can improve reaction effect.
Since a part of reclaimable catalyst of gasoline fast bed reactor be circulated to gasoline fast bed reactor again after regenerated catalyst from revivifier mixes, and the blending ratio of described reclaimable catalyst and regenerated catalyst and the temperature of mixed catalyst can be regulated, can improve the catalyst recirculation amount in the gasoline fast bed reactor, thereby improve the agent-oil ratio (agent-oil ratio is 10～50) of gasoline fast bed reactor.Gasoline fast bed reactor can control the relatively long reaction times (3～10s), catalyzer can fully be reacted with all kinds of sulfide (comprising thiophene-type sulfide) in the gasoline, sulfide be converted into hydrogen sulfide and remove.Thereby the present invention can reduce the sulphur content of gasoline fast bed reformulated gasoline that reactor produces effectively, and product distribution and quality product are improved.
Adopt catalytic cracking desulfur method of the present invention and device, can overcome the deficiencies in the prior art, when guaranteeing that gasoline fast bed reactor produces the reformulated gasoline olefin(e) centent and declines to a great extent, make its sulphur content that significantly decline also be arranged.Compare with the inferior patrol charging, the desulfurization degree of gasoline fast bed reformulated gasoline that reactor produces of the present invention can reach 50～80w%, and olefin(e) centent reduces by 20～50 volume percentage points, and octane value improves 0.3～2.0 unit, and the full device product distributes good.For oil refining enterprise of the moderate inferior patrol charging (sulphur content＜300 μ g/g) of some processing sulphur content, but utilize the present invention's direct production sulphur content to be lower than the motor spirit fuel that meets Europe III emission request that 150 μ g/g, olefin(e) centent are lower than 18v%.Thereby the present invention can perform well in producing clean gasoline fuel.The desulfurization degree of above-mentioned gasoline fast bed reformulated gasoline that reactor produces is meant that inferior patrol feed sulphur content (μ g/g) deducts the ratio (representing with weight percentage) that gasoline fast bed reactor produces reformulated gasoline sulphur content (μ g/g) gained difference and inferior patrol feed sulphur content (μ g/g).
In a word, the present invention has characteristics such as easy and simple to handle, that regulation and control are flexible, operate steadily, effect is remarkable.
The present invention is further detailed explanation below in conjunction with accompanying drawing, embodiment and embodiment.Accompanying drawing, embodiment and embodiment do not limit the scope of protection of present invention.
Description of drawings
Fig. 1 is the structure and layout synoptic diagram of inferior patrol catalytic cracking and desulfurizing device of the present invention.
Embodiment
Referring to inferior patrol catalytic cracking and desulfurizing device of the present invention shown in Figure 1.This device is provided with heavy oil riser reactor 12, first settling vessel 11, revivifier 14, gasoline upgrading reactor, second settling vessel 8 for the double-reactor catalytic cracking unit.The top exit of heavy oil riser reactor 12 is connected with first settling vessel 11, and the bottom is provided with heavy oil riser reactor feed entrance 17, and the bottom is connected with revivifier 14 by first regenerator sloped tube 18 and the first regeneration standpipe 16.The below that the below of first settling vessel 11 is provided with the first settling vessel stripping stage, 13, the first settling vessel stripping stages 13 is provided with first regeneration standpipe, 15, the first regeneration standpipes 15 and is connected with revivifier 14.The below that the below of second settling vessel 8 is provided with the second settling vessel stripping stage, 7, the second settling vessel stripping stages 7 is provided with second regeneration standpipe 6 and second inclined tube 5 to be generated, and the second settling vessel stripping stage 7 is connected with revivifier 14.
Referring to Fig. 1, above-mentioned gasoline upgrading reactor is columnar structured gasoline fast bed reactor 4.Gasoline fast bed reactor 4 is provided with cylindrical drum, and the top and the bottom of cylindrical drum are respectively equipped with conical section.Be provided with conduit 24 (conduit 24 is communicated with gasoline fast bed reactor 4 with second settling vessel 8) between the conical section at top and second settling vessel 8, the conical section of bottom is provided with inferior patrol feed entrance 2.Conduit 24 is made up of one section vertical pipeline section and one section horizontal pipeline section, and its exit end is provided with quick disconnector, and the situation that quick disconnector is set with the exit end of riser reactor is identical, is used for the sharp separation of reaction oil gas and catalyzer.The cylindrical drum of gasoline fast bed reactor 4 and the conical section of cylindrical drum top and bottom are hardware, general equal liner insulating and wearing-resistant lining.The internal diameter of gasoline fast bed reactor 4 (interior diameter that refers to cylindrical drum) is generally Φ 40～3000mm, and length (conical section that comprises cylindrical drum top and bottom) is generally 3000～15000mm.
Below gasoline fast bed reactor 4, be provided with columnar structured catalyst mix device 1.Catalyst mix device 1 is provided with cylindrical drum, and the top of cylindrical drum is provided with conical section, and the bottom is provided with end socket.The bottom of catalyst mix device 1 is provided with steam distributor 22.The cylindrical drum of catalyst mix device 1 is the main part of catalyst mix device 1; The conical section at this cylindrical drum and cylindrical drum top, the end socket of bottom are hardware, general equal liner insulating and wearing-resistant lining.Catalyst mix device 1 interior set steam distributor 22 is the steam distribution ring among Fig. 1, and its structure is identical with the employed steam distribution ring of existing catalytic cracking unit with effect; Steam distribution ring and catalyst mix device 1 coaxial arrangement.Steam distributor 22 can also adopt the steam distributor of existing employed other structure of catalytic cracking unit.Be provided with pipe connecting 23 between the conical section of the conical section at catalyst mix device 1 cylindrical drum top and gasoline fast bed reactor 4 cylindrical drums bottom, pipe connecting 23 is connected catalyst mix device 1 with gasoline fast bed reactor 4.Above-mentioned respectively to read the awl section mainly be ligation, and help the flowing of catalyzer, eliminate flow dead, do not have concrete scantlings of the structure to require (gasoline fast bed reactor 4 cylindrical drum tops and conduit 24 continuous conical section identical therewith).The internal diameter of catalyst mix device 1 (interior diameter that refers to cylindrical drum) is generally Φ 100～4000mm, and length (comprising the conical section at cylindrical drum top and the end socket of bottom) is generally 800～8000mm.
Between second inclined tube 5 to be generated and catalyst mix device 1, be provided with reclaimable catalyst transfer lime 3, with the two connection.Reclaimable catalyst transfer lime 3 is provided with flowrate control valve 21, and flowrate control valve 21 can adopt various flowrate control valves commonly used (as adopting guiding valve), to regulate the reclaimable catalyst flow in the reclaimable catalyst transfer lime 3.One end of reclaimable catalyst transfer lime 3 is connected on the tube wall of second inclined tube 5 to be generated (link position does not have strict demand), and the other end is connected on the cylindrical drum of catalyst mix device 1.
Device shown in Figure 1 is provided with the second regeneration standpipe 19, second regenerator sloped tube 20, and its structure and size are conventional.The second regeneration standpipe 19 and second regenerator sloped tube 20 are between revivifier 14 and catalyst mix device 1, with two the two connections.Wherein second regenerator sloped tube 20 is connected on the cylindrical drum of catalyst mix device 1.
The position of two interfaces that reclaimable catalyst transfer lime 3, second regenerator sloped tube 20 link to each other with catalyst mix device 1 cylindrical drum, if guarantee to enter in the catalyst mix device 1 from gasoline fast bed reactor 4 through steam stripped reclaimable catalyst and the bottom that catalyst mix device 1 in, after the stirring of the water vapor that feeds by steam distributor 22 and castering action lower edge catalyst mix device 1 a up segment distance, realization well blend, enters gasoline fast bed reactor 4 from the regenerated catalyst of revivifier 14 again.Generally speaking, two interfaces linking to each other with catalyst mix device 1 cylindrical drum of reclaimable catalyst transfer lime 3, second regenerator sloped tube 20 is centered close on the horizontal plane.
It is circular metal tube that above-mentioned reclaimable catalyst transfer lime 3 and pipe connecting 23, conduit 24 generally all adopt cross section, common liner insulating and wearing-resistant lining, and internal diameter generally is Φ 10～2000mm.Wherein conduit 24 should be a undergauge with respect to gasoline fast bed reactor 4, and reactant gas speed can be improved rapidly, to help separating reclaimable catalyst and reaction oil gas effectively at second settling vessel 8.In addition, several are set on reclaimable catalyst transfer lime 3 usually carry airduct (figure slightly), in operating process, feed and carry wind (medium is generally water vapor) to carry catalyzer.Carrying airduct generally is the direction setting that edge and the mobile direction of catalyzer are 45 degree angles.Identical in the use of carrying the setting of airduct and carrying wind and the close phase transfer lime of existing catalytic cracking unit catalyzer, the genus mature technology.
Adopt the present invention's inferior patrol catalytic cracking and desulfurizing shown in Figure 1 device to carry out the method for inferior patrol catalytic cracking and desulfurizing, form by following process:
A. enter the bottom of heavy oil riser reactor 12 from a part of regenerated catalyst of revivifier 14 through the first regeneration standpipe 16 and first regenerator sloped tube 18, contact afterwards along heavy oil riser reactor 12 up reactions with the heavy oil riser reactor charging 171 that enters by heavy oil riser reactor feed entrance 17.After reaction finished, reactant flow entered first settling vessel 11 by the top exit of heavy oil riser reactor 12 and carries out catalyzer and gas-oil separation; Isolated heavy oil riser reactor reaction oil gas 10 enters fractionating system and carries out fractionation obtaining product, and isolated reclaimable catalyst enters by first regeneration standpipe 15 behind the water vapor stripping at the first settling vessel stripping stage 13 and carries out coke burning regeneration in the revivifier 14.Regenerated catalyst part in the revivifier 14 after the regeneration is returned heavy oil riser reactor 12, and another part enters catalyst mix device 1 through the second regeneration standpipe 19 and second regenerator sloped tube 20;
B. in second inclined tube to be generated 5 from gasoline fast bed reactor 4, at a part of reclaimable catalyst of the second settling vessel stripping stage 7 behind the water vapor stripping, enter columnar structured catalyst mix device 1 through reclaimable catalyst transfer lime 3, under the adjusting of flowrate control valve set on the reclaimable catalyst transfer lime 3 21, with regenerated catalyst from process A, stirring and castering action lower edge catalyst mix device 1 at the water vapor that is fed by the steam distributor of being located in the catalyst mix device 1 22 are up, realize well blend.Catalyzer after mixing enters the bottom of columnar structured gasoline fast bed reactor 4 by the top of catalyst mix device 1 through pipe connecting 23 again, contacts the back along gasoline fast bed reactor 4 up reactions with the inferior patrol charging 201 that is entered by inferior patrol feed entrance 2.After reaction finished, reactant flow entered second settling vessel 8 by the top of gasoline fast bed reactor 4 through conduit 24 and carries out catalyzer and gas-oil separation; Isolated gasoline fast bed reactor reaction oil gas 9 enters fractionating system and carries out fractionation, obtains the reformulated gasoline product that sulphur content reduces.Second settling vessel, 8 isolated reclaimable catalysts enter second to be generated inclined tube 5 by second regeneration standpipe 6 at the second settling vessel stripping stage 7 behind the water vapor stripping; Reclaimable catalyst part in second inclined tube 5 to be generated enters catalyst mix device 1 through reclaimable catalyst transfer lime 3, and another part enters and carries out coke burning regeneration in the revivifier 14.
In above operating process, the operational condition of the second settling vessel stripping stage 7 is conventional; The stripping medium is a water vapor, and the stripping temperature is generally 480～520 ℃.Temperature from the reclaimable catalyst behind the second settling vessel stripping stage, 7 strippings of gasoline fast bed reactor 4 is generally 470～520 ℃ (being to enter catalyst mix device 1 by reclaimable catalyst transfer lime 3 under this temperature basically), carbon content is generally 0.05～0.40w%, and micro-activity is generally 53～65.
Reclaimable catalyst from gasoline fast bed reactor 4 and heavy oil riser reactor 12 carries out coke burning regeneration under conventional catalytic cracking catalyst regeneration condition in revivifier 14, regeneration temperature generally is controlled at 650～750 ℃ (regeneration temperature of revivifier 14 inner catalysts is meant dense-phase catalyst bed temperature), the carbon content of regenerated catalyst is generally 0.02～0.20w%, and micro-activity is generally 55～70.Regenerated catalyst after the regeneration returns heavy oil riser reactor 12 respectively and gasoline fast bed reactor 4 participates in reaction, realizes recycling of catalyzer.The regeneration temperature from the temperature of the regenerated catalyst of revivifier 14 and revivifier 14 inner catalysts that enters catalyst mix device 1 through second regeneration standpipe 19 and second regenerator sloped tube 20 is basic identical.
The above-mentioned weight rate that enters the reclaimable catalyst of catalyst mix device 1 through reclaimable catalyst transfer lime 3 is generally 5～80w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage 7.In the operating process, the conveying airduct that is provided with on reclaimable catalyst transfer lime 3 feeds carries wind (medium is generally water vapor), to carry this part reclaimable catalyst.
In catalyst mix device 1, the temperature of the mixed catalyst that above-mentioned regenerated catalyst and reclaimable catalyst are formed is generally 600～690 ℃.The temperature of the water vapor that is fed by steam distributor 22 is generally 150～250 ℃, and weight rate is generally 0.2～2w% of mixed catalyst weight internal circulating load.The temperature of above-mentioned mixed catalyst, be meant through second regeneration standpipe 19 and second regenerator sloped tube 20 and enter the regenerated catalyst of catalyst mix device 1 and enter the reclaimable catalyst of catalyst mix device 1, the temperature of the mixed catalyst after the water vapor that is fed by steam distributor 22 stirs, mixes through reclaimable catalyst transfer lime 3.Because the flow of the water vapor that steam distributor 22 feeds is very little, the flow of the water vapor that the conveying airduct that is provided with on reclaimable catalyst transfer lime 3 feeds also very little (flow of the water vapor that feeds less than steam distributor 22) is so these two strands of water vapors are little to the mixed catalyst Temperature Influence.
In the aforesaid operations process, gasoline fast bed reactor 4 uses identical catalyzer with heavy oil riser reactor 12; Catalyzer adopts existing various catalytic cracking catalysts (for example CC-20D, MLC-500, LRC-99 etc.) commonly used, can select for use routinely.
The present invention, the condition that heavy oil riser reactor charging 171 is reacted in heavy oil riser reactor 12 is conventional catalytic cracking condition.The principal reaction condition of heavy oil riser reactor 12 is as follows usually: temperature of reaction is generally 450～550 ℃, and the reaction times is generally 0.5～5s, and agent-oil ratio is generally 3～10, and the reaction absolute pressure is generally 0.15～0.40MPa.Wherein, the temperature of reaction of heavy oil riser reactor 12 is meant the oil gas vent temperature of heavy oil riser reactor, and agent-oil ratio is meant in the unit time by the recycling catalyst of heavy oil riser reactor and the weight ratio of heavy oil riser reactor charging.Heavy oil riser reactor charging 171 comprises long residuum, vacuum residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle stock, slurry oil, crude oil, shale oil, synthetic oil, coal tar.The operation and the control process of those skilled in the art's counterweight oil riser reactor 12 are clearly, can select operational condition for use according to the concrete operations situation.In addition, the stripping condition of the first settling vessel stripping stage 13 also is conventional; The stripping medium is a water vapor, and the stripping temperature is generally 480～520 ℃.
The present invention, the reaction conditions of gasoline fast bed reactor 4 is generally as follows: temperature of reaction is 400～550 ℃, and the reaction times is 3～10s, and agent-oil ratio is 10～50, and the reaction absolute pressure is 0.15～0.40MPa.Gasoline fast bed reactor 4 best reaction conditionss are: temperature of reaction is that 450～520 ℃, reaction times are that 4.0～8.0s, agent-oil ratio are 15～40, the reaction absolute pressure is 0.15～0.20MPa.Wherein, the temperature of reaction of gasoline fast bed reactor 4 is meant the oil gas vent temperature of gasoline fast bed reactor, be the temperature of the interface that links to each other with conduit 24 of the conical section at gasoline fast bed reactor 4 cylindrical drum tops among Fig. 1, agent-oil ratio is meant in the unit time by the recycling catalyst of gasoline fast bed reactor and the weight ratio of inferior patrol charging.
Gasoline fast bed reactor of the present invention 4 mainly carries out desulfurization, falls alkene the gasoline that double-reactor catalytic cracking unit heavy oil riser reactor 12 of the present invention itself is produced, but also can handle external or the high-sulfur that other device is produced, the inferior patrol of high olefin content.Said inferior patrol charging 201 comprises catalytically cracked gasoline, catalytic cracking heavy petrol, thermo-cracking and pressure gasoline and heavy petrol, coker gasoline and inferior patrols such as coking heavy petrol, cracking ethylene preparation gasoline; The sulphur content of inferior patrol is generally 100～2000 μ g/g, and olefin(e) centent is generally 30～70v%.
By above explanation as can be known, the heavy oil riser reactor of double-reactor catalytic cracking unit of the present invention and gasoline fast bed reactor use settling vessel separately respectively, and a shared revivifier, use identical catalyzer in the operating process.
Gasoline fast bed reactor 4 of the present invention is a circulating fluid bed reactor, and its bed density is by increasing solid cycle quantity G
SKeep.In the operating process, solid (catalyzer) the internal circulating load G in the reactor
SAt 15～50kg/m
3Scope in, gas speed (total speed of all oil gas and water vapor by beds) is in the scope of 1.0～3.0m/s.The reaction conditions of gasoline fast bed reactor 4 of the present invention is under the condition that satisfies above-mentioned solid cycle quantity and gas speed and propose.
Comparative Examples and embodiment
Comparative Examples 1
On common double lift pipe catalytic cracking testing apparatus, test.Different with the present invention's device shown in Figure 1 is that the gasoline rising pipe reactor of this double lift pipe catalytic cracking testing apparatus is a conventional structure, and device is not provided with catalyst mix device and reclaimable catalyst transfer lime; Apparatus structure is referring to Chinese patent CN1401740A.Heavy oil riser reactor processing northern Suzhou mixing heavy oil, treatment capacity is 30kg/d (kg/day); The inferior patrol charging of the gasoline rising pipe reactor gasoline (self-produced gasoline 1) that the oil riser reactor is produced of attaching most importance to, treatment capacity is 15kg/d.The test catalyst system therefor is a CC-20D industry poiser, and the equilibrium catalyst micro-activity is 62, and carbon content is 0.08w%; The regeneration temperature of revivifier is 690 ℃.The stripping medium of the first settling vessel stripping stage and the second settling vessel stripping stage is water vapor, and the stripping temperature is 500 ℃.The main character of the inferior patrol charging of charging of heavy oil riser reactor and gasoline rising pipe reactor is listed in table 1, the main operational condition of heavy oil riser reactor and gasoline rising pipe reactor is listed in table 2, and the product of gasoline rising pipe reactor distributes and the main character of reformulated gasoline is listed in table 3.In table 2 Comparative Examples 1 (and in table 4 Comparative Examples 2 and table 6 Comparative Examples 3), the temperature of reaction of gasoline rising pipe reactor is meant the oil gas vent temperature of gasoline rising pipe reactor, and the agent-oil ratio of gasoline rising pipe reactor is meant in the unit time weight ratio by the inferior patrol charging of the recycling catalyst of gasoline rising pipe reactor and gasoline rising pipe reactor.In the table 3 (and table 5 and table 7), the white branch of volume that desulfurization degree, octane value increase numerical value and olefin(e) centent reduction all is to calculate with respect to the inferior patrol charging of gasoline rising pipe reactor or gasoline fast bed reactor.
Embodiment 1
Testing on the double-reactor catalytic cracking and desulfurizing testing apparatus of the present invention as shown in Figure 1.The internal diameter of gasoline fast bed reactor is Φ 60mm, and length is 4200mm.The internal diameter of catalyst mix device is Φ 100mm, and length is 800mm.It is circular metal tube that the reclaimable catalyst transfer lime adopts cross section, and liner insulating and wearing-resistant lining, internal diameter are Φ 12mm.Medium through carrying airduct to feed the conveying wind in the reclaimable catalyst transfer lime is a water vapor, and the temperature of water vapor is 200 ℃.The temperature of the water vapor that is fed by steam distributor in the catalyst mix device also is 200 ℃.Heavy oil riser reactor processing northern Suzhou mixing heavy oil, treatment capacity is 30kg/d; The inferior patrol charging of the gasoline fast bed reactor gasoline (self-produced gasoline 1) that the oil riser reactor is produced of attaching most importance to, treatment capacity is 15kg/d.The test catalyst system therefor is a CC-20D industry poiser, and the equilibrium catalyst micro-activity is 63, and carbon content is 0.08w%.The weight rate that enters the reclaimable catalyst of catalyst mix device through the reclaimable catalyst transfer lime is the 5w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage.The main character of the inferior patrol charging of charging of heavy oil riser reactor and gasoline fast bed reactor is listed in table 1, the main operational condition of heavy oil riser reactor and gasoline fast bed reactor is listed in table 2, and the product of gasoline fast bed reactor distributes and the main character of reformulated gasoline is listed in table 3.
Among the embodiment 1 other unaccounted main operational condition all with Comparative Examples 1 in identical.
Embodiment 2～embodiment 5
On the used testing apparatus of embodiment 1, test.The main operational condition of heavy oil riser reactor and gasoline fast bed reactor is listed in table 2, and the product of gasoline fast bed reactor distributes and the main character of reformulated gasoline is listed in table 3.The charging that used testing apparatus, heavy oil riser reactor and gasoline fast bed reactor processed among embodiment 2～embodiment 5 and treatment capacity, test catalyst system therefor and other unaccounted main operational condition all with embodiment 1 in identical.
By table 2 as seen, among embodiment 2～embodiment 5, the weight rate that enters the reclaimable catalyst of catalyst mix device through the reclaimable catalyst transfer lime is respectively 20w%, 40w%, 60w% and the 80w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage.
Comparative Examples 2
On the used testing apparatus of Comparative Examples 1, test.Heavy oil riser reactor processing northern Suzhou mixing heavy oil, treatment capacity is 30kg/d; The inferior patrol charging of the gasoline rising pipe reactor gasoline (self-produced gasoline 2) that the oil riser reactor is produced of attaching most importance to, treatment capacity is 15kg/d.The test catalyst system therefor is a LRC-99 industry poiser, and the equilibrium catalyst micro-activity is 63, and carbon content is 0.09w%.The main character of the inferior patrol charging of charging of heavy oil riser reactor and gasoline rising pipe reactor is listed in table 1, the main operational condition of heavy oil riser reactor and gasoline rising pipe reactor is listed in table 4, and the product of gasoline rising pipe reactor distributes and the main character of reformulated gasoline is listed in table 5.
In the Comparative Examples 2 other unaccounted main operational condition all with Comparative Examples 1 in identical.
Embodiment 6
On the used testing apparatus of embodiment 1, test.Heavy oil riser reactor processing northern Suzhou mixing heavy oil, treatment capacity is 30kg/d; The inferior patrol charging of the gasoline fast bed reactor gasoline (self-produced gasoline 2) that the oil riser reactor is produced of attaching most importance to, treatment capacity is 15kg/d.The test catalyst system therefor is a LRC-99 industry poiser, and the equilibrium catalyst micro-activity is 62, and carbon content is 0.09w%.The weight rate that enters the reclaimable catalyst of catalyst mix device through the reclaimable catalyst transfer lime is the 5w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage.The main character of the inferior patrol charging of charging of heavy oil riser reactor and gasoline fast bed reactor is listed in table 1, the main operational condition of heavy oil riser reactor and gasoline fast bed reactor is listed in table 4, and the product of gasoline fast bed reactor distributes and the main character of reformulated gasoline is listed in table 5.
Among the embodiment 6 other unaccounted main operational condition all with Comparative Examples 2 in identical.
Embodiment 7～embodiment 10
On the used testing apparatus of embodiment 1, test.The main operational condition of heavy oil riser reactor and gasoline fast bed reactor is listed in table 4, and the product of gasoline fast bed reactor distributes and the main character of reformulated gasoline is listed in table 5.The charging that used testing apparatus, heavy oil riser reactor and gasoline fast bed reactor processed among embodiment 7～embodiment 10 and treatment capacity, test catalyst system therefor and other unaccounted main operational condition all with embodiment 6 in identical.
By table 4 as seen, among embodiment 7～embodiment 10, the weight rate that enters the reclaimable catalyst of catalyst mix device through the reclaimable catalyst transfer lime is respectively 20w%, 40w%, 60w% and the 80w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage.
Comparative Examples 3
On the used testing apparatus of Comparative Examples 1, test.Heavy oil riser reactor processing northern Suzhou mixing heavy oil, treatment capacity is 30kg/d; The inferior patrol charging of gasoline rising pipe reactor is outer gasoline feed, and treatment capacity is 15kg/d.The test catalyst system therefor is a CC-20D industry poiser, and the equilibrium catalyst micro-activity is 63, and carbon content is 0.08w%.The main character of the inferior patrol charging of charging of heavy oil riser reactor and gasoline rising pipe reactor is listed in table 1, the main operational condition of heavy oil riser reactor and gasoline rising pipe reactor is listed in table 6, and the product of gasoline rising pipe reactor distributes and the main character of reformulated gasoline is listed in table 7.
In the Comparative Examples 3 other unaccounted main operational condition all with Comparative Examples 1 in identical.
Embodiment 11
On the used testing apparatus of embodiment 1, test.Heavy oil riser reactor processing northern Suzhou mixing heavy oil, treatment capacity is 30kg/d; The inferior patrol charging of gasoline fast bed reactor is outer gasoline feed, and treatment capacity is 15kg/d.The test catalyst system therefor is a CC-20D industry poiser, and the equilibrium catalyst micro-activity is 63, and carbon content is 0.08w%.The weight rate that enters the reclaimable catalyst of catalyst mix device through the reclaimable catalyst transfer lime is the 5w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage.The main character of the inferior patrol charging of charging of heavy oil riser reactor and gasoline fast bed reactor is listed in table 1, the main operational condition of heavy oil riser reactor and gasoline fast bed reactor is listed in table 6, and the product of gasoline fast bed reactor distributes and the main character of reformulated gasoline is listed in table 7.
Among the embodiment 11 other unaccounted main operational condition all with Comparative Examples 3 in identical.
Embodiment 12～embodiment 15
On the used testing apparatus of embodiment 1, test.The main operational condition of heavy oil riser reactor and gasoline fast bed reactor is listed in table 6, and the product of gasoline fast bed reactor distributes and the main character of reformulated gasoline is listed in table 7.The charging that used testing apparatus, heavy oil riser reactor and gasoline fast bed reactor processed among embodiment 12～embodiment 15 and treatment capacity, test catalyst system therefor and other unaccounted main operational condition all with embodiment 11 in identical.
By table 6 as seen, among embodiment 12～embodiment 15, the weight rate that enters the reclaimable catalyst of catalyst mix device through the reclaimable catalyst transfer lime is respectively 20w%, 40w%, 60w% and the 80w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage.
The main character of the various chargings of table 1
The main operational condition of table 2 reactor (Comparative Examples 1, embodiment 1～5)
The main character of distribution of table 3 product and reformulated gasoline
(Comparative Examples 1: gasoline rising pipe reactor; Embodiment 1～5: gasoline fast bed reactor)
| Project | Comparative Examples 1 | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 |
| Product distribution/w% | ||||||
| Dry gas | 0.9 | 1.28 | 1.51 | 1.67 | 1.85 | 2.56 |
| Liquefied gas | 5.4 | 12.64 | 13.25 | 15.47 | 17.80 | 21.35 |
| Gasoline | 88.9 | 78.81 | 76.34 | 72.57 | 69.74 | 64.68 |
| Diesel oil | 3.5 | 5.47 | 6.68 | 7.11 | 7.26 | 7.77 |
| Coke | 1.1 | 1.60 | 2.02 | 2.98 | 3.15 | 3.44 |
| Loss | 0.2 | 0.2 | 0.2 | 0.2 | 0.2 | 0.2 |
| Add up to | 100 | 100 | 100 | 100 | 100 | 100 |
| The reformulated gasoline main character | ||||||
| Sulphur content/μ gg 1 | 495 | 311 | 278 | 216 | 185 | 156 |
| Octane value (RON) | 91.1 | 91.2 | 91.3 | 91.5 | 91.8 | 92.3 |
| Olefin(e) centent/v% | 20.6 | 18.2 | 11.5 | 9.6 | 8.1 | 6.3 |
| Desulfurization degree/w% | 20.8 | 50.2 | 55.5 | 65.4 | 70.4 | 75.0 |
| Octane value increases | 0.4 | 0.5 | 0.6 | 0.8 | 1.1 | 1.6 |
| The volume percentage point that olefin(e) centent reduces | 25.0 | 27.4 | 34.1 | 36.0 | 37.5 | 39.3 |
The main operational condition of table 4 reactor (Comparative Examples 2, embodiment 6～10)
The main character of distribution of table 5 product and reformulated gasoline
(Comparative Examples 2: gasoline rising pipe reactor; Embodiment 6～10: gasoline fast bed reactor)
| Project | Comparative Examples 2 | Embodiment 6 | Embodiment 7 | Embodiment 8 | Embodiment 9 | Embodiment 10 |
| Product distribution/w% | ||||||
| Dry gas | 0.8 | 1.31 | 1.58 | 1.71 | 1.84 | 2.53 |
| Liquefied gas | 5.2 | 12.57 | 13.11 | 15.54 | 17.78 | 21.18 |
| Gasoline | 89.4 | 78.87 | 76.57 | 72.33 | 69.70 | 64.95 |
| Diesel oil | 3.4 | 5.38 | 6.42 | 7.21 | 7.30 | 7.67 |
| Coke | 1.0 | 1.67 | 2.12 | 3.01 | 3.18 | 3.47 |
| Loss | 0.2 | 0.2 | 0.2 | 0.2 | 0.2 | 0.2 |
| Add up to | 100 | 100 | 100 | 100 | 100 | 100 |
| The reformulated gasoline main character | ||||||
| Sulphur content/μ gg 1 | 511 | 316 | 286 | 222 | 189 | 167 |
| Octane value (RON) | 90.7 | 90.9 | 91.1 | 91.3 | 91.5 | 91.8 |
| Olefin(e) centent/v% | 21.2 | 18.6 | 11.3 | 9.8 | 8.4 | 6.7 |
| Desulfurization degree/w% | 19.9 | 50.5 | 55.2 | 65.2 | 70.4 | 73.8 |
| Octane value increases | 0.4 | 0.6 | 0.8 | 1.0 | 1.2 | 1.5 |
| The volume percentage point that olefin(e) centent reduces | 25.2 | 27.8 | 35.1 | 36.6 | 38.0 | 39.7 |
The main operational condition of table 6 reactor (Comparative Examples 3, embodiment 11～15)
The main character of distribution of table 7 product and reformulated gasoline
(Comparative Examples 3: gasoline rising pipe reactor; Embodiment 11～15: gasoline fast bed reactor)
| Project | Comparative Examples 3 | Embodiment 11 | Embodiment 12 | Embodiment 13 | Embodiment 14 | Embodiment 15 |
| Product distribution/w% | ||||||
| Dry gas | 1.0 | 1.26 | 1.49 | 1.68 | 1.87 | 2.29 |
| Liquefied gas | 6.4 | 15.57 | 18.11 | 20.41 | 22.46 | 25.18 |
| Gasoline | 86.7 | 75.82 | 71.87 | 68.34 | 65.69 | 61.82 |
| Diesel oil | 4.5 | 5.68 | 6.42 | 7.21 | 7.30 | 7.67 |
| Coke | 1.2 | 1.47 | 1.91 | 2.16 | 2.48 | 2.84 |
| Loss | 0.2 | 0.2 | 0.2 | 0.2 | 0.2 | 0.2 |
| Add up to | 100 | 100 | 100 | 100 | 100 | 100 |
| The reformulated gasoline main character | ||||||
| Sulphur content/μ gg 1 | 765 | 496 | 436 | 325 | 289 | 238 |
| Octane value (RON) | 89.6 | 89.8 | 89.9 | 90.2 | 90.3 | 90.5 |
| Olefin(e) centent/v% | 22.4 | 17.7 | 13.3 | 9.6 | 8.4 | 7.3 |
| Desulfurization degree/w% | 23.5 | 50.4 | 56.4 | 67.5 | 71.1 | 76.2 |
| Octane value increases | 0.5 | 0.7 | 0.8 | 1.1 | 1.2 | 1.4 |
| The volume percentage point that olefin(e) centent reduces | 34.5 | 39.2 | 43.6 | 47.3 | 48.5 | 49.6 |
Claims (3)
1. catalytic cracking desulfur method of faulty gasoline is characterized in that being made up of following process:
A. enter the bottom of heavy oil riser reactor (12) from a part of regenerated catalyst of revivifier (14), contact the back along up reaction of heavy oil riser reactor (12) with heavy oil riser reactor charging (171), after reaction finishes, reactant flow enters first settling vessel (11) by the top exit of heavy oil riser reactor (12) and carries out catalyzer and gas-oil separation, isolated heavy oil riser reactor reaction oil gas (10) enters fractionating system and carries out fractionation, isolated reclaimable catalyst enters behind stripping in the revivifier (14) and carries out coke burning regeneration, a regenerated catalyst part is returned heavy oil riser reactor (12), and another part enters catalyst mix device (1);
B. in second inclined tube to be generated (5) from gasoline fast bed reactor (4), at a part of reclaimable catalyst of the second settling vessel stripping stage (7) behind stripping, through reclaimable catalyst transfer lime (3), on reclaimable catalyst transfer lime (3), enter catalyst mix device (1) under the adjusting of set flowrate control valve (21), with regenerated catalyst from process A, up and the mixing at the effect lower edge catalyst mix device (1) of the water vapor that feeds by the steam distributor of being located in the catalyst mix device (1) (22), enter the bottom of gasoline fast bed reactor (4) through pipe connecting (23), contact the back along up reaction of gasoline fast bed reactor (4) with inferior patrol charging (201), after reaction finishes, reactant flow enters second settling vessel (8) by the top of gasoline fast bed reactor (4) through conduit (24) and carries out catalyzer and gas-oil separation, isolated gasoline fast bed reactor reaction oil gas (9) enters fractionating system and carries out fractionation, obtain the reformulated gasoline product, the isolated reclaimable catalyst of second settling vessel (8) enters second to be generated inclined tube (5) by second regeneration standpipe (6) at the second settling vessel stripping stage (7) behind stripping, reclaimable catalyst part in second inclined tube to be generated (5) enters catalyst mix device (1) through reclaimable catalyst transfer lime (3), and another part enters in the revivifier (14) and carries out coke burning regeneration;
The above-mentioned weight rate that enters the reclaimable catalyst of catalyst mix device (1) through reclaimable catalyst transfer lime (3) is 5～80w% of the reclaimable catalyst weight internal circulating load behind the stripping in the second settling vessel stripping stage (7), the temperature of reaction of gasoline fast bed reactor (4) is 400～550 ℃, reaction times is 3～10s, agent-oil ratio is 10～50, the reaction absolute pressure is 0.15～0.40MPa, described gasoline fast bed reactor (4) is columnar structured, internal diameter is Ф 40～3000mm, length is 3000～15000mm, catalyst mix device (1) is columnar structured, internal diameter is Ф 100～4000mm, and length is 800～8000mm.
2. catalytic cracking desulfur method of faulty gasoline according to claim 1, it is characterized in that: the temperature of reaction of gasoline fast bed reactor (4) is 450～520 ℃, reaction times is 4.0～8.0s, and agent-oil ratio is 15～40, and the reaction absolute pressure is 0.15～0.20MPa.
3. inferior patrol catalytic cracking and desulfurizing device that is used to realize the described catalytic cracking desulfur method of faulty gasoline of claim 1, be provided with heavy oil riser reactor (12), first settling vessel (11), revivifier (14), the gasoline upgrading reactor, second settling vessel (8), the top exit of heavy oil riser reactor (12) is connected with first settling vessel (11), the bottom is provided with heavy oil riser reactor feed entrance (17), the bottom is connected with revivifier (14) by first regenerator sloped tube (18) and the first regeneration standpipe (16), the below of first settling vessel (11) is provided with the first settling vessel stripping stage (13), the below of the first settling vessel stripping stage (13) is provided with first regeneration standpipe (15), first regeneration standpipe (15) is connected with revivifier (14), the below of second settling vessel (8) is provided with the second settling vessel stripping stage (7), the below of the second settling vessel stripping stage (7) is provided with second regeneration standpipe (6) and second inclined tube to be generated (5), the second settling vessel stripping stage (7) is connected with revivifier (14), inferior patrol catalytic cracking and desulfurizing device also is provided with the second regeneration standpipe (19), second regenerator sloped tube (20) and catalyst mix device (1), be provided with reclaimable catalyst transfer lime (3) between second inclined tube to be generated (5) and the catalyst mix device (1), reclaimable catalyst transfer lime (3) is provided with flowrate control valve (21), it is characterized in that: the gasoline upgrading reactor is columnar structured gasoline fast bed reactor (4), gasoline fast bed reactor (4) is provided with cylindrical drum, the top and the bottom of cylindrical drum are respectively equipped with conical section, be provided with conduit (24) between the conical section at top and second settling vessel (8), the conical section of bottom is provided with inferior patrol feed entrance (2), the exit end of conduit (24) is provided with quick disconnector, described catalyst mix device (1) is columnar structured, be located at the below of gasoline fast bed reactor (4), catalyst mix device (1) is provided with cylindrical drum, the top of cylindrical drum is provided with conical section, the bottom is provided with end socket, the bottom of catalyst mix device (1) is provided with steam distributor (22), be provided with pipe connecting (23) between the conical section of the conical section at catalyst mix device (1) cylindrical drum top and gasoline fast bed reactor (4) cylindrical drum bottom, described reclaimable catalyst transfer lime (3) is connected on the cylindrical drum of catalyst mix device (1), described second regeneration standpipe (19) and second regenerator sloped tube (20) are positioned between revivifier (14) and the catalyst mix device (1), and second regenerator sloped tube (20) is connected on the cylindrical drum of catalyst mix device (1);
The internal diameter of described gasoline fast bed reactor (4) is Ф 40～3000mm, and length is 3000～15000mm, and the internal diameter of catalyst mix device (1) is Ф 100～4000mm, and length is 800～8000mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100484081A CN100424154C (en) | 2006-07-17 | 2006-07-17 | Catalytic cracking desulfur method of faulty gasoline and device thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100484081A CN100424154C (en) | 2006-07-17 | 2006-07-17 | Catalytic cracking desulfur method of faulty gasoline and device thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1903989A CN1903989A (en) | 2007-01-31 |
| CN100424154C true CN100424154C (en) | 2008-10-08 |
Family
ID=37673357
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100484081A Active CN100424154C (en) | 2006-07-17 | 2006-07-17 | Catalytic cracking desulfur method of faulty gasoline and device thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100424154C (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101104815B (en) * | 2007-07-13 | 2010-12-15 | 中国石油化工集团公司 | Upgrading method and device for gasoline |
| CN101921611B (en) | 2009-06-12 | 2013-07-31 | 中国石油天然气股份有限公司 | Catalytic cracking method and system for reducing sulphur content of petrol |
| CN101575534B (en) * | 2009-06-16 | 2012-09-26 | 中国石油化工集团公司 | Device and method for reducing the temperature of catalytic cracking regenerated catalyst |
| CN107661736A (en) * | 2017-11-09 | 2018-02-06 | 江苏新海石化有限公司 | A kind of double lifting catalytic cracking units and its method for modifying high silicon gasoline inferior |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6129833A (en) * | 1997-06-13 | 2000-10-10 | Tricat Industries, Inc. | Catalytic cracking with reduced emission of sulfur oxides |
| CN1721055A (en) * | 2005-05-23 | 2006-01-18 | 中国石油化工集团公司 | Double-riser catalytic cracking device for lowering sulfur content in catalytically cracked gasoline |
-
2006
- 2006-07-17 CN CNB2006100484081A patent/CN100424154C/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6129833A (en) * | 1997-06-13 | 2000-10-10 | Tricat Industries, Inc. | Catalytic cracking with reduced emission of sulfur oxides |
| CN1721055A (en) * | 2005-05-23 | 2006-01-18 | 中国石油化工集团公司 | Double-riser catalytic cracking device for lowering sulfur content in catalytically cracked gasoline |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1903989A (en) | 2007-01-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100338185C (en) | Catalytic cracking method and apparatus | |
| CN101161786B (en) | Conversion method for petroleum hydrocarbons | |
| CN101591562B (en) | Fluid catalytic cracking method and device thereof | |
| CN101575534B (en) | Device and method for reducing the temperature of catalytic cracking regenerated catalyst | |
| CN101104815B (en) | Upgrading method and device for gasoline | |
| CN101665710B (en) | Method and device for catalytic conversion of light Hydrocarbon | |
| CN101665712B (en) | Method and device for fluidized catalytic conversion | |
| CN201161998Y (en) | Petroleum hydrocarbon raw materials catalytic conversion reaction-regeneration apparatus | |
| CN100424154C (en) | Catalytic cracking desulfur method of faulty gasoline and device thereof | |
| CN1298812C (en) | Double lift pipe catalytic cracking method and device for modifying inferior patrol | |
| CN102212390B (en) | Double riser catalytic cracking method and device | |
| CN102268291B (en) | Catalytic cracking technology and device for reducing olefins in gasoline | |
| CN102233253A (en) | Riser catalysis device for processing heavy oil and application thereof | |
| CN101665713B (en) | Method and device for circulating cold regenerated catalyst | |
| CN102199447B (en) | Catalytic conversion method for producing high cetane value light diesel fuel and low olefine gasoline | |
| CN201016112Y (en) | Double-lifted pipe catalytic cracking device | |
| CN102311767B (en) | Gasoline olefin reducing catalytic cracking method and device | |
| CN102839014A (en) | Reactor and method for reinforcing heavy oil conversion and reducing gasoline olefin | |
| CN102268290B (en) | Catalytic cracking method and device | |
| CN1171977C (en) | Method and device for reducing olefine in gasoline | |
| CN102453540B (en) | Catalytic conversion method for increasing high octane number gasoline yield | |
| CN102212389A (en) | Catalytic cracking method and device | |
| CN101993723A (en) | Method and device for modifying low-quality heavy oil | |
| CN1200083C (en) | Catalytic cracking combined process | |
| CN101705110A (en) | Method for enhancing propylene production by catalyzing and splitting coking waxy oil and modifying coker naphtha |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C56 | Change in the name or address of the patentee | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Patentee after: China Petrochemical Group Corp. Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Co-patentee before: Luoyang Petrochemical Engineering Co., China Petrochemical Group Patentee before: China Petrochemical Group Corp. |
|
| ASS | Succession or assignment of patent right |
Owner name: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORAT Free format text: FORMER OWNER: SINOPEC GROUP Effective date: 20130326 Free format text: FORMER OWNER: SINOPEC LUOYANG PETROCHEMICAL ENGINEERING CORPORATION Effective date: 20130326 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 100029 CHAOYANG, BEIJING TO: 471003 LUOYANG, HENAN PROVINCE |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20130326 Address after: 471003 Zhongzhou West Road, Henan, China, No. 27, No. Patentee after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100029 Beijing City, Chaoyang District Hui Street No. 6 Patentee before: China Petrochemical Group Corp. Patentee before: Luoyang Petrochemical Engineering Corporation /SINOPEC |