CN105505441B - A kind of catalytic cracking reaction regeneration method and device - Google Patents
A kind of catalytic cracking reaction regeneration method and device Download PDFInfo
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- CN105505441B CN105505441B CN201610002678.2A CN201610002678A CN105505441B CN 105505441 B CN105505441 B CN 105505441B CN 201610002678 A CN201610002678 A CN 201610002678A CN 105505441 B CN105505441 B CN 105505441B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J38/00—Regeneration or reactivation of catalysts, in general
- B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/10—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst bed
Abstract
A kind of catalytic cracking reaction regeneration method is used for petroleum hydrocarbon raw material catalytic reaction process；It is characterized in that, regenerator itself, which is divided into, burns gas preheating zone, the first renewing zone, the second renewing zone and gas-solid Disengagement zone；It burns gas and directly realizes preheating with regenerative agent mixed heat transfer in regenerator, the NOx that burning process generates is made to reduce；It burns gas while regenerative agent being made to cool down, so that the oil ratio of reactor is increased, improve the product distribution of reaction；Other low temperature catalyst is provided for reactor simultaneously, which can be spent agent or the regenerative agent of cooling, advanced optimize reactor condition, control product distribution.
Description
Technical field
The present invention relates to a kind of chemical field gas-solid catalysis technologies, are catalyzed for petroleum hydrocarbon more particularly to one kind
Reaction regeneration method.
Background technology
Catalytic cracking of petroleum hydrocarbon reaction is the secondary operation technique of crude oil, reacts two by raw material reaction and catalyst regeneration
Reaction process forms.Raw material reaction process generally generates the coke of inlet amount 5.5%~10.0%, these coke are attached to catalysis
Agent surface, blocking catalyst micropore, it is necessary to which cyclic char makes renewing catalyst activity.Catalytic material reacts and catalyst regeneration is anti-
Sport technique segment should be all important.
Raw material reaction determines purpose product, but in terms of plant investment, operation energy consumption, device maintenance cost, catalyst is again
Raw process occupies main status.
Existing than more typical catalyst regeneration techniques includes two-stage regeneration, adverse current two-stage regeneration technology.Especially UOP is public
The adverse current two-stage regeneration technology of department and the exploitation of sinopec Beijing designing institute embodies higher efficiency.Uop Inc. and Ashland are public
Department discloses the two-phase up-flow regeneration reaction regeneration technology of its joint development in US4299687, and CN 97121795.5 is disclosed
A kind of heavy oil fluidized catalyzed conversion eclipsed form two-stage regeneration technology.
Prior art catalyst regeneration process is concerned only with coke combustion reaction.But coke and burn gas haptoreaction process
Middle nitrogen can generate nitrogen oxides (NOx).With the raising of environmental requirement, traditional scheme is controlled using equipment for denitrifying flue gas is built
The discharge of NOx increases investment, energy consumption and operating cost, influences economic benefit.Combustion reaction is directly reduced in burning process
The technology that journey NOx is generated is better approach.
In prior art, catalyst regeneration (burns) in reaction process and burns gas from next 190 DEG C or so of compressor
(generally air) directly participates in catalyst coke and burns reaction.That improves coke burning burns gas temperature, reduces combustion zone
Temperature especially local " high temperature " can effectively reduce NOx generations.
In the catalytic cracking process that regenerative agent cooler is arranged in regenerator, regenerative agent cooler generates in prior art
Low-temp recovery agent, which returns, burns reaction zone, can reduce the temperature for burning reaction, and influence burns reaction speed, also just reduces burning
Burnt reaction efficiency；The internal circulating load for generally requiring to increase regenerative agent makes up renewing zone temperature.But the regenerative agent phosphorus content being recycled back to is very
It is low, and the content of combustion zone coke can be reduced, while also increasing the energy consumption of catalyst circulation conveying.
In catalytic cracking of petroleum hydrocarbon reaction process, catalyst is key problem, but catalysis in reactor in reaction process
The performance of agent and the performance of unreacted procatalyst are different.By taking hydrocarbon compound catalytic cracking reaction as an example, reaction process
Middle catalyst can be such that the performance of catalyst during real reaction gradually becomes because of green coke, alkaline components and metallic pollution, passivation
Difference, in reactor, especially the performance of each site catalysts is different in tubular reactor, the catalytic action efficiency played
It is different.In addition the activity of catalyst, the temperature and temperature of reaction oil ratio or air speed, reaction raw materials and catalyst in reaction process
The reaction conditions such as difference are all an important factor for influencing raw material reaction result, and being varied and controlled for these conditions can all change reaction knot
Fruit.
Catalytic cracking of petroleum hydrocarbon is more than C with carbon number3Component product as the main purpose, C2And small molecule product master below
If the product of thermal cracking.Intensified catalytic cracking reacts, and it is the target that catalytic cracking process is pursued always to reduce heat cracking reaction.
The selection and control of reaction condition are directly related to the selection of reaction conversion ratio and reactor product during catalytic cracking reaction
Property.There are many technology of existing optimization reaction system operation, by taking petroleum hydrocarbon raw material catalytic conversion reaction as an example, dry gas pre-lifting skill
Art is terminated using the mixing temperature control technology of feed change decanting point and injected media, outlet area rapid separation, chilling
Reaction technology etc. all influences obviously, industrially preferably to be applied on reaction result.Catalyst performance in reaction process
It improves and control is also vital.
From last century the seventies, catalytic cracking of petroleum hydrocarbon reaction replaces fluidized-bed reactor with riser reactor.Stone
Hydrocarbon feedstock catalytic cracking reaction is the gas-solid endothermic reaction, and reaction raw materials are usually liquid feed, and liquid material is firstly the need of suction
Thermal evaporation, then gas reactant enters back into catalyst micro channel and carries out catalysis reaction.The heat of gasification of liquid material is by regenerating
Catalyst provides.All there are two processes of liquid-phase vaporization and gas phase reaction using the liquid charging stock catalysis reaction of tubular reactor.
Gasification is in gasification or more since gasification is not moment, is completed at the same time by being realized with catalyst contact heat supply
Or there is certain reaction less.The essential advantage of tubular reactor is that the presence of " gradient ", could realize that raising is anti-in this way
The target of " motive force " (reactant concentration) is answered, reaction efficiency and selectivity are improved.This is the master that fluid bed is replaced by riser
Want one of reason.Petroleum hydrocarbon raw material constitutes complicated, and the raw molecule amount that reactor inlet enters is substantially 300, reactor outlet
Molecular weight product is substantially 100 or smaller, and different location shows different reactant property and anti-in riser reactor
Answer process, it is also desirable to different reaction conditions.Such as more than atomizer, the incipient stage in gas phase reaction area, feedstock oil is completed
The mainly feedstock oil macromolecular cracking reaction carried out after gasification, when this process generally passes through reaction in 1.0~1.5 seconds or so
Between, the gas phase reaction area of riser latter half be then substantially carried out compared with small molecule such as diesel oil, gasoline, liquefied gas composition react again with
And the reactions such as isomerization, hydrogen migration.Therefore often entire gas phase reaction is divided into " cracking reaction area modifies reaction zone " again
Deng.The high temperature of the temperature difference and catalyst in liquid-phase vaporization reaction process between catalyst and raw material can all increase heat cracking reaction, increase
Add C2Following byproduct ratio, influences economic benefit；Cracking in vapour phase reaction zone, the temperature for modifying reaction zone, oil ratio, catalyst
Activity etc. all significantly affects the reaction result of entire reaction zone.
By taking petroleum hydrocarbon raw material catalyzed conversion as an example, result of study both domestic and external already confirms, regenerative agent temperature is high, causes
Reactant oil is relatively low, and the contact temperature difference between regenerative agent and reaction raw materials is big, can all cause dry gas yied high, be produced to liquid yield
Life significantly affects；As the progress of reaction, the activity of catalyst quickly reduce in riser, riser downstream reaction area efficiency drop
It is low, influence reaction effect.Regenerative agent temperature is reduced, it is to urge for many years to improve oil ratio and improve the activity of catalyst in riser
Change the target that cracking unit is pursued always.
There are many technical measures in terms of the regenerative agent and the feedstock oil temperature difference for reducing reaction raw materials liquid-phase vaporization contact zone.Needle
To reduce with feedstock oil first contact temperature problem, it will be most readily appreciated that method be " low temperature catalyst in external warmer to be drawn
Enter riser pre lift zone ".Uop Inc. proposes in patent US5800697 in external warmer the nineties in last century
Low temperature catalyst is sent into the method that riser carries pre lift zone.The patent application of this respect is more, such as US6059958,
US6558530B1, CN01119805.1, CN1664074A, CN101191067A, CN101191072A etc..
US5800697 discloses a kind of catalytic conversion reaction-regeneration method, and cooling catalyst is arranged beside regenerator
Area, the thermal regenerant from dense bed, which enters after exchanging heat from outlet into cooling area to preference temperature through standpipe, guiding valve, to be carried
Riser reactors bottom participates in reaction, to make reaction oil ratio become independent variable.CN101161786A discloses a kind of stone
The method for transformation of petroleum hydrocarbon class, the hot cooler cooling that is regenerated catalyst through participate in feedstock oil contact simultaneously back to reactor bottom
Carry out cracking reaction, reclaimable catalyst be transported to after stripping regenerator carry out coke burning regeneration after recycle or part directly into
Enter the mixer of reactor bottom.
It is that the temperature of feedstock oil is improved that another kind, which reduces feedstock oil and the method for the regenerative agent first contact temperature difference,.
CN101144028A discloses a kind of cracking method for hydrocarbon oil, and hydrocarbon ils is heated with regenerated catalyst in heat exchanger,
Then make the hydrocarbon ils after heat exchange and the regenerated catalyst after heat exchange haptoreaction in the reactor.
In addition, catalyst includes not only the catalyst temperature of the preceding pre lift zone of reaction, liquid phase (original to the influence factor of reaction
Material oil) the gasification zone contact temperature difference and oil ratio, the cracking in vapour phase reaction zone catalyst activity after raw material oil gasification and oil ratio pair
Reaction process also has a major impact.
Control and improvement to catalyst action in each position reaction process in reactor, in addition to liquid-phase vaporization area, also
Should include the improvement to the catalyst in the gas phase reaction area after raw material oil gasification, the control to the catalyst condition of offer.
To sum up, catalyst enter reactor condition and mode to improve raw material reaction effect it is significant, optimization again
Raw and reaction, formation is mutually matched, the complete reaction regeneration decorum is more meaningful；Gas is burnt using high temperature and carries out catalyst again
Raw reaction can improve the discharge index of flue gas.
Invention content
The main purpose of the present invention is to provide a kind of catalytic cracking reaction regeneration methods, are reacted with catalyst again by raw material
Raw two reactive moieties composition, including catalyst regenerator, tubular reactor, reacting-settler etc., reaction regeneration process is by pressing
Once step carries out：
1, reaction raw materials enter in reactor different parts, are contacted with catalyst and by catalyst heating and gasifying, then into
Row reaction；Reaction product and catalyst enter after reactor outlet outflow immediately together is located at first order gas in referred to as settler
Solid separator and second level gas-solid separator realize that catalyst and product gas separation, product gas are flowed out through settler oil gas vent.
2, the catalyst after the reaction of completion raw material enters settler stripping zone and is stripped, and the spent agent after stripping is through to be generated
Inclined tube enters the regenerative response area bottom in the middle part of regenerator, carries out regenerative response with the gas that burns from below, is catalyzed simultaneously
Agent and regenerative response gas and and the flue gas that generates of regenerative response be delivered up together, realize gas in regenerator gas solid separation area
The separation of body and catalyst, gas flow out regenerator from exhanst gas outlet, and catalyst is introduced into the storage of the dense-phase fluidized bed in regenerator
Deposit area, burn gas preheating zone from the area through what regenerative agent delivery pipe was sent to regenerator bottoms, preheating zone with to burn gas straight
Connecing mixing makes to burn gas heating, while itself is cooled；Regenerative agent after cooling is from gas preheating zone is burnt through regenerator sloped tube
Enter reactor below reaction raw materials entrance.Equipped with regenerator catalyst cooler (also referred to as external warmer), catalysts
When cooler, the regenerator dense-phase fluidized bed is arranged in regenerator catalyst cooler and catalysts cooler catalyst inlet
Storage area.
3, first part burn gas regenerator bottoms burn gas preheating zone from gas distributor enter burn gas
Preheating zone directly forms fluidized state contact heat-exchanging, upwards through Perforated plate distributor inflow catalyst after being heated with regenerative agent
Renewing zone；Another is set above or below the orifice plate burnt between gas preheating zone and catalyst regeneration zones and burns gas
(main wind) enters pipe and distributor pipe (claiming the second distributor), and burning gas by pipe introduction partial regeneration enters regenerator；It is excellent
Change, second part burn gas in regenerative agent preheating zone above catalyst material position, burn gas preheating zone and renewing zone it
Between orifice plate below enter regenerator, with preheating zone come high-temperature gas mix, then enter renewing zone through orifice plate, participate in burning
Reaction；It completes the gas-carrying portion catalyst after burning and carries out full gas solid separation in regenerator gas solid separation area, gas is from cigarette
Gas outlet outflow regenerator.
4, the catalyst inventory or material position of gas preheating zone are burnt by the valve control being arranged in regenerative agent delivery pipe.
5, by burning the variation of gas preheating zone catalyst material position or reserve, and change to enter and burn gas preheating zone
Burn gas flow and can adjust gas preheating temperature and regenerative agent cooling temperature.
According to the method for the present invention, it is divided into catalyst regenerator shell and is divided into catalyst regeneration reactive moieties up and down, burns
Burnt gas (generally using air) regenerator section and gas-solid separate section；It is burning between gas preheating zone and catalyst regeneration zones
Setting circulation orifice plate, is arranged dense phase fluidized catalyst storage area between renewing zone and gas-solid Disengagement zone, is used for being regenerative agent
Delivery pipe, external warmer (if any) provide regenerated catalyst；The regenerative agent storage area can be located at catalyst regeneration zones, can also
It is independently arranged outside renewing zone；In the regenerative agent storage area and burns regenerative agent delivery pipe is set between gas preheating zone；When need
To be regenerator setting catalyst cooler (external warmer), be reactor be arranged reaction regeneration agent cooler when, regeneration catalyzing
The catalyst inlet of agent cooler and reaction regeneration agent cooler is also provided in the area.
Reactor body is riser conversion zone, and feedstock oil gasification zone, catalytic cracking are followed successively by feedstock oil inlet port
Reaction zone, catalytic cracking reaction zone downstream be arranged settler, gas-solid separator is arranged inside, the catalyst isolated by gravity to
It is lower to enter stripping section；Spent agent after stripping enters regenerator renewing zone through regeneration standpipe, is preheated with gas is burnt from below
The gas contact of burning in area carries out burning reaction.
According to the method for the present invention, regenerator renewing zone is further separated into the first renewing zone, the second renewing zone；First regeneration
Area is in lower part, and the second renewing zone is on the first renewing zone top；Each section setting circulation orifice plate in first renewing zone and the second renewing zone
(distributor)；The catalyst and gas of first renewing zone are transported to the second renewing zone by orifice plate simultaneously to be continued to burn；Second
Renewing zone coboundary (catalyst material position) extends up to what the diameter in regenerator renewing zone and gas solid separation section was gradually expanded
Bore section；Cone section due to gas flow rate reduce, so that the density of catalyst is increased, become dense-phase fluidized bed, the fluid bed and meanwhile at
For regenerative agent storage area；Setting flue gas gas solid separation area above second renewing zone；In the second renewing zone dense-phase fluidized bed area and burning
Regenerative agent delivery pipe is set between burnt gas preheating zone, and regenerative agent feeding of the regenerative agent after the regenerative agent delivery pipe will be burnt is burnt
Gas preheating zone；Spent agent enters the first renewing zone；It burns gas (general custom claims main wind) and enters through gas distribution tube in part
Gas preheating zone is in direct contact in preheating zone with regenerative agent, is reproduced agent heating, is then entered the first renewing zone through orifice plate；
Regenerative agent itself is cooled while gas is burnt in heating, is burnt the regenerative agent after gas cooling from preheating zone through catalyst
Pipeline (commonly referred to as standpipe) enters reactor bottom (commonly referred to as pre lift zone).
According to the method for the present invention, interior bucket is set in the cone section below regenerator gas solid separation area, by the second renewing zone
It is divided into the inside and outside areas Liang Ge, outskirt becomes regenerative agent recycling, storage area；The flue gas and catalyst of first renewing zone enter the interior bucket after
It is continuous to burn reaction；The interior bucket is designed as the cylinder of iso-cross-section or cross-sectional area gradually increases upwards, gas flow rate continuously decreases
Burn reaction zone；Air shooter and distributor are burnt in setting outside the interior bucket at this time, are supplemented and are burnt to the catalyst storage area
Burnt gas.
According to the method for the present invention, it is bored in section and gas-solid Disengagement zone shell in regenerator and the second renewing zone shell is set, the
One renewing zone is directly connected to the second renewing zone, and delivery pipe is arranged in the second outlet of the regeneration zone, and delivery pipe outlet setting gas-solid just divides
From device, so that renewing zone and regenerator gas solid separation is separated and be split into two independent parts, the catalyst and gas in regenerative response area
Preliminary gas solid separation directly is carried out in outlet of the regeneration zone, gas is in regenerator gas solid separation area again through being located at renewing zone and regeneration
Two-stage rotation between device shell flows out regenerator after isolating catalyst；Catalyst enters between renewing zone and regenerator shell
Catalyst storage area.
According to the method for the present invention, catalyst circulation pipe, control are set between regenerative agent storage area and the first renewing zone
The combustion reaction temperature of first renewing zone spent agent.
According to the method for the present invention, when catalyst regeneration reaction need to take heat when, from regenerative agent storage area draw catalyst into
Enter catalyst cooler, catalyst after cooling is directly entered from catalyst tube burns gas preheating zone.
Concrete scheme according to the present invention, in method of the invention, in reactor stripping section and reactor bottom (pre-lift
Section) or gasification after the intersegmental setting spent agent return duct of cracking reaction, control temperature, oil ratio and the catalyst of inside reactor
Activity.
Concrete scheme according to the present invention, in method of the invention, in the second renewing zone and reactor bottom (pre-lift
Section) or gasification after cracking reaction it is intersegmental setting reaction regeneration agent cooler and cooling after reaction regeneration agent delivery pipe, make drop
Regenerative agent after temperature enters reactor, controls temperature, oil ratio and the catalyst activity of inside reactor.
Specific embodiment according to the present invention, in method of the invention, in regenerator renewing zone in spent agent entrance it
It is arranged with the first orifice plate, regenerator is divided into renewing zone and gas preheating zone；First orifice plate can be porous barrier,
Can be the distribution grid of other forms, one of effect is that the gas of the preheating zone below distribution grid is made (can to carry part to urge
Agent) by first distribution grid even into the first renewing zone on orifice plate；Another effect of first orifice plate is by gas
The regenerative agent of preheating zone and the catalyst of renewing zone separate, and regenerative agent is prevented to be upwardly into renewing zone by air-flow carrying；It can be with
Understand, in the present invention, can suitably adjust installation position or the control gas preheating zone catalyst controlling level of the first distribution grid
To control the catalytic amount for entering the first renewing zone from preheating zone.In addition, in the method for the present invention, it can also be as desired by
Second gas distributor introducing portion burn gas enter the first renewing zone, the gas distributor can above the first orifice plate,
It can also be below the first orifice plate；Preferably, which is arranged below the first orifice plate.
Specific embodiment according to the present invention in method of the invention, in the regenerator renewing zone, enters in spent agent
It is additionally provided with the second orifice plate on mouthful；Second orifice plate can be porous barrier or the distribution grid of other forms；Second hole
The main function of plate be make the first renewing zone gas and catalyst even into the second renewing zone, make the catalysis of the second renewing zone
Effect is burnt in agent active fluidization and mixing, raising；In addition, in the method for the present invention, it can also be as desired by third gas
Distributor introducing portion burns gas and enters the second renewing zone, which can be above the second orifice plate, can also be
Below second orifice plate；Preferably, which is arranged below the second orifice plate.
Preferred embodiment according to the present invention, in method of the invention, to be passed through the gas that burns of regenerator
Total amount is 100% meter, and the amount for burning gas that gas preheating zone is passed directly into from bottom is 35%~70% or so, from second point
It is 30~60% or so that cloth device entered, which burns the amount of gas, and the amount for burning gas entered from third distributor is 0~10%
Left and right；Each section gas can be introduced by gas distributor in regenerator respectively, and specific gas distributor can be selected affiliated
The prior art in field, the present invention repeat no more.
The effect of the present invention：
Gas is burnt after regenerator self-preheating again with the coke gasification reaction on catalyst, forms the low flue gas of NOx content；
It burns gas while regenerative agent being made to cool down, provide low-temp recovery agent for reactor, form low temperature between reactor and regenerator
Regenerant recycle can reduce thermal cracking and especially gasify and the heat cracking reaction in cracking reaction area, can adjust and gasify and react
Thermal balance relationship is easily and flexibly realized to reacting each area's catalyst progress multi_control and can reduce energy consumption.
Generally speaking, catalyst reaction regeneration method of the invention is used for petroleum hydrocarbon raw material catalytic cracking process, regeneration
Process itself realizes that high-temperature gas is burnt, reduces NOx emission to burning gas preheating；Simultaneously low temperature is provided for reactor again
Independent regenerative agent cooling equipment is arranged without providing low-temp recovery agent for reactor in raw agent；Make spent agent or after cooling
Cracking reaction area of the regenerative agent after reaction raw materials gasification is supplemented into reactor, and dual catalyst cycle is formed for reactor, can
According to different location reaction condition need different catalysts condition is provided, realize easily and flexibly to react each area's catalyst into
Row multi_control.
The present invention's can be found in for realizing the reaction regeneration method shown in Fig. 1~Fig. 8.
Description of the drawings
Fig. 1：Reaction-regenerating section schematic diagram in the catalytic cracking reaction technology of the specific implementation mode of the present invention.
Fig. 2：Catalytic cracking reaction-regenerating section schematic diagram of the another way of the present invention.
Fig. 3：Catalytic cracking reaction-regenerating section schematic diagram of the another way of the present invention.
Fig. 4：Catalytic cracking reaction-regenerating section schematic diagram of the another way of the present invention.
Fig. 5：Catalytic cracking reaction-regenerating section schematic diagram of the another way of the present invention.
Fig. 6：Reaction-regenerating section schematic diagram that heat is taken containing regenerator of the present invention.
Fig. 7：The present invention regenerates a kind of structural schematic diagram of embodiment of section distribution grid.
Fig. 8：The present invention regenerates the structural schematic diagram of the another embodiment of section distribution grid.
Explanation is numbered in figure：1 reactor；2 burn gas preheating zone；3 first catalyst regeneration zones；4 second catalyst are again
Raw area；5 regenerator gas solid separation areas；6 settler stripping sections；7 settler dilute-phase zones；8 regenerator catalyst coolers；9 reactions
Regenerative agent cooler；11 regenerative agent inclined tubes；12 regeneration guiding valves, 13 reactor bottom catalyst sections (commonly referred to as pre-lift)；14、
14B reaction raw materials, 14C reactions or extremely cold raw material；15 reaction raw materials reaction zones；16 catalyst mixed zones；17, spent agent returns
Mouthful；18 spent agents reflux tube valve；19 spent agent return ducts；20 burn gas preheating zone shell；22 burn gas preheating zone gas
Body distributor；23 burn flue；24 low-temp recovery agent outlets；25 gas preheating zone catalyst material positions；26 regenerative agents are distributed
Device；27 regenerative agents convey tube valve；28 regenerative agent delivery pipes；29 regenerative agent delivery pipes；30 first catalyst regeneration zones shells；31
First orifice plate (multihole distributor)；31B recirculation holes；The holes 31C cap；32 burning gases distributors, 33 burn flue；34 to be generated urge
Agent inclined tube valve；35 inclined tubes to be generated；36 reclaimable catalyst distributors；37 regenerant recycle tube valves；38 regenerant recycle pipes；
39 regenerant recycle pipes；40 regenerators bore piece housing；41 second orifice plates (multihole distributor)；41B recirculation holes；The holes 41C cap；41D
Regenerative agent storage area grid；42 gas distributors；43 flues；44A, 44B, 44C, 44D regenerative agent outlet；45 regenerative agents store up
Deposit area's catalyst material position；46 second renewing zone shells, the second renewing zones 46B interior bucket；46C bores section；47 outlet of the regeneration zone delivery pipes；
The first separator of 48 gas-solids；49 regenerator dense phase fluidized catalyst storage areas；50 regenerator gas solid separation area shells；51 regenerators
Level-one gas-solid separator；52 regenerator two level gas-solid separators；53 collection chambers；54 burn exhanst gas outlet；60 settler stripping zones
Shell；61 stripping internals；62 stripping vapour distributors；63 stripping steam pipes；64 spent agents export；65 inclined tubes to be generated；70 settler shells
Body；71 settler level-one gas-solid separators；72 settler two level gas-solid separators；73 collection chambers；74 product gas outlets；81 regeneration
Device catalyst cooler catalyst inlet；82 regenerator catalyst cooler catalyst outlets；83 regenerator catalyst coolers
Outlet valve；91 reaction regeneration agent cooler catalyst inlets；92 reaction regeneration agent coolers export；93 reaction regeneration agent cool down
Device outlet valve；94 low temperature reaction regenerant inlets；31B, 41B gas and catalyst rise hole；31C, 41C distribution grid escutcheon；A
Gas is burnt in compression；C catalyst；F flue gases；S steam；G pre-lift media；O reaction raw materials oil；H burns gas preheating zone catalysis
Agent controlling level.
Specific implementation mode
The technical solution that the present invention will be described in detail with reference to the accompanying drawings and embodiments, protection scope of the present invention include still
It is without being limited thereto.The routine techniques of fields can be used in the device structure not referred in detail in the present invention.
It refers to shown in Fig. 1~Fig. 5, the device of the invention for realizing the reaction regeneration method includes being set up in parallel
Reactor and regenerator, wherein：
Regenerator is used to carry out coke burning regeneration to the spent agent for carrying out autoreactor 1, and regenerator is vertical installation, enclosure interior
Be divided into bottom burns (regeneration) gas preheating zone 2, catalyst regeneration zones and flue gas gas solid separation area 5；Catalyst regeneration is distinguished
For the first renewing zone 3 of lower part and the second renewing zone 4 of top；Orifice plate 31 or 41 is arranged in each section, and orifice plate is porous type, hole
The gross area of 31B, 41B are by the gas flow rate 12m/s~40m/s passed through, aperture 50mm~200mm；2 height of preheating zone is 3.0m
~7.0m is designed by gas superficial flow velocity less than 1.2m/s；First scorch region, 3 height 8.0m~15.0m, by gas superficial flow velocity
1.4m/s~2.5m/s is designed, and gas solid separation area 5 is designed by gas superficial flow velocity less than 0.8m/s；Spent agent and
Enter the first renewing zone between one renewing zone and the 31 top 1.0m/s~4.0m/s of orifice plate for preheating section；It is pre- to burn (regeneration) gas
Hot section catalysts material position H is 2.0~6.0m, and preferred H is 2.5m~3.5m；Gas solid separation is carried out using cyclone separator 51,52；Again
The internal circulating load of raw 38 regenerative agent of agent circulation pipe is 0.5~1.5 times of the catalytic amount for entering reactor 1 by regenerator sloped tube 11；
To lightweight material, when reaction-regeneration system need not take heat, spent agent is by spent agent return duct 19 and return port 17 in raw material
Above oil inlet at 2.0m~10.0m Returning reactor 1 mixed zone 16, or returned at 2.0m~7.0m below the raw material oil inlet
Reactor bottom 13 is returned, spent agent back amount is 0.2~1.0 times of the catalytic amount for entering reactor 1 by regenerator sloped tube 11.
To having the reaction raw materials of surplus heat (needing to take heat), setting regenerative agent cooler 9；It takes thermic load by the following method
It determines：500 DEG C~580 DEG C of regenerative agent temperature after cooling；The flow of catalyst is pressed enters reactor 1 by regenerator sloped tube 11
0.2~1.0 times of determination of catalytic amount；Regenerative agent after cooling is by outlet 92 and inlet port 93 above raw material oil inlet
The mixed zone 16 of Returning reactor 1 at 2.0m~10.0m, or the Returning reactor bottom at 2.0m~7.0m below the raw material oil inlet
Portion 13.
When regenerative agent cooler 8 is arranged, regenerative agent after cooling passes through regenerator catalyst cooler catalyst outlet
82 are directly entered and burn gas preheating zone, and catalyst regeneration zones are entered no longer as routine techniques；Regenerative agent cooler is general
Technical staff being capable of complete design.
Settler, settler stripping zone those skilled in the art being capable of complete designs；According to the above parameter, technical staff can be with
Complete the application design of the method for the present invention；The present invention repeats no more.
The reaction regeneration method of the present invention provides the regenerative agent of different condition for reactor；Keep reaction condition more optimized；By
It is reacted in using high-temperature gas, the NOx content in flue gas can be reduced；It is real in regenerator itself by the improvement of regenerator configuration
Gas preheating is now burnt, device design is simplified, that is, reduces investment, also reduce energy consumption；Optimizing raw material reaction simultaneously improves product
Distribution.
Embodiment：
The control of reaction zone catalyst and regenerative agent used in the present embodiment take the device of hot cooling means referring to Fig. 6 institutes
Show.
Certain produces 150 × 10 per year4The catalytic cracking unit of petroleum hydrocarbon of t/a, reaction regeneration are arranged in juxtaposition, and burn gas preheating zone
2 use fluid bed form, the first renewing zone 3 that recirculating fluidized bed form, the second renewing zone 4 is used to be arranged in 3 He of the first renewing zone
The areas regenerator Zhui Duan between gas solid separation area 5, using fluid bed form；Burn gas preheating zone, the first renewing zone, second again
The first orifice plate distribution grid 31 and the second orifice plate distribution grid 41 is respectively set between raw area；Reactor 1 is to promote form of tubes；Setting is anti-
Regenerative agent cooler 9, reaction regeneration agent cooler 9 is answered to generate middle pressure steam, reaction regeneration agent cooler 9 divides using steam is carried
From type formula, steam trap is connected directly between on reaction regeneration agent cooler 9, and diameter is identical as regenerative agent cooler；Reaction
Catalyst after the cooling of regenerative agent cooler enters reactor above feedstock oil, and specific in-position see the table below；Participation is burnt
The gas flow of gas preheating is the 52% of total amount, and that is sent into the first renewing zone burns 48% that gas is total amount, the gas point
Cloth device and delivery pipe are located above the second orifice plate；Second renewing zone is not supplemented burning gas；Reaction mass and embodiment and original
There is the comparative example reaction condition of technology see the table below.
The anti-plant bulk again of the embodiment of the present invention and crude oil technology comparative example see the table below.
Embodiment see the table below with original technology comparative example reactor product forecast of distribution.
Claims (12)
1. a kind of catalytic cracking reaction regeneration method is made of raw material reaction and two reactive moieties of catalyst regeneration, including urges
Agent regenerator, tubular reactor, reacting-settler, reaction regeneration process carry out according to the following steps：
1., reaction raw materials enter reactor in reactor different parts, contacted with catalyst and by catalyst heating and gasifying, then
It is reacted；Reaction product and catalyst enter first be located in referred to as settler immediately after reactor outlet outflow together
Grade gas-solid separator and second level gas-solid separator realize catalyst and product gas separation, and product gas is through settler oil gas vent
Outflow；
2., complete the catalyst after raw material reaction and enter settler stripping zone and stripped, the spent agent after stripping through it is to be generated tiltedly
Pipe enters the regenerative response area bottom in the middle part of regenerator, and regenerative response, letter are carried out with the gas that burns after preheating from below
Title is burnt, while the flue gas that catalyst and regenerative response gas and regenerative response generate is delivered up together, in regenerator gas
Gu Disengagement zone realizes that the separation of gas and catalyst, the catalyst isolated are introduced into the dense phase fluidized catalyst in regenerator
Storage area, that is, regenerator dense phase fluidized catalyst storage area, abbreviation regenerator dense-phase fluidized bed storage area or regenerator storage
Area burns gas preheating zone from the area through what regenerative agent delivery pipe was sent to regenerator bottoms, is burning gas preheating zone and burning
Gas directly mixing makes to burn gas heating, while catalyst itself is cooled；Regenerative agent after cooling is preheated from gas is burnt
Area enters reactor through regenerator sloped tube below reaction raw materials entrance, is contacted with reaction raw materials under the effect of pre-lift medium；If
When having regenerator catalyst cooler i.e. external warmer, catalysts cooler, regenerator catalyst cooler and reaction are urged
The regenerator dense-phase fluidized bed storage area is arranged in agent cooler catalyst inlet；
3., first part burn gas from regenerator bottoms burn gas preheating zone by first gas distributor enter burn gas
Preheating zone directly forms fluidized state contact heat-exchanging with regenerative agent, gas heated after upwards through the first Perforated plate distributor stream
Enter catalyst regeneration zones；Setting burns gas and enters pipe and second gas distributor above or below the first Perforated plate distributor,
Gas, which is burnt, by distributor introduction second part regeneration enters regenerator；Complete the gas-carrying portion catalyst after burning
Full gas solid separation is carried out in regenerator gas solid separation area, gas flows out regenerator from exhanst gas outlet；
4., from regenerator dense phase fluidized catalyst storage area regenerative agent delivery pipe draw regenerative agent feeding burn gas preheating
The catalyst inventory or material position of gas preheating zone are burnt by the valve control being arranged in regenerative agent delivery pipe in area；
5., the variation by burning gas preheating zone catalyst material position or reserve, and change enter burn gas preheating zone
It burns gas flow and adjusts gas preheating temperature and regenerative agent cooling temperature；
It is divided into gas solid separation part up and down in catalyst regenerator shell, catalyst regeneration reactive moieties, burns gas preheating part
Point, wherein it is air to burn gas；Setting circulation orifice plate between gas preheating zone and catalyst regeneration zones is being burnt, in regenerator
Setting dense phase fluidized catalyst storage area in cone section below gas solid separation area is used for as regenerative agent delivery pipe and optional outer
Heat collector provides regenerated catalyst；The regenerative agent storage area is located at catalyst regeneration zones, or is independently arranged outside renewing zone；
It the regenerative agent storage area and burns regenerative agent delivery pipe is set between gas preheating zone；When need for regenerator be arranged catalyst it is cold
But device, that is, external warmer, for reactor be arranged reaction regeneration agent cooler when, regenerated catalyst cooler and reaction regeneration agent drop
The catalyst inlet of warm device is also provided in the area；Reactor body is riser conversion zone, and original is followed successively by feedstock oil inlet port
Expect that oil gasification area, catalytic cracking reaction zone, catalytic cracking reaction zone downstream are that settler is arranged in top, reactor product is arranged inside
Gas-solid separator, the catalyst isolated are downwardly into stripping section by gravity；Spent agent after stripping enters again through regeneration standpipe
Raw device renewing zone contacts with the gas that burns for burning gas preheating zone from below and carries out burning reaction.
2. catalytic cracking reaction regeneration method as described in claim 1, which is characterized in that regenerator renewing zone is further separated into
First renewing zone, the second renewing zone；First renewing zone is in lower part；First renewing zone and the second regeneration section setting circulation orifice plate,
That is the second orifice plate；The catalyst and gas of first renewing zone are transported to the second renewing zone by orifice plate simultaneously to be continued to burn；The
Two renewing zones coboundary, that is, catalyst material position extends up to regenerator renewing zone and the diameter in gas solid separation section is gradually expanded
Cone section；In cone section since gas flow rate continuously decreases, so that the density of catalyst is increased, become dense-phase fluidized bed, the fluid bed
Become regenerative agent storage area simultaneously.
3. catalytic cracking reaction regeneration method as claimed in claim 1 or 2, which is characterized in that in regenerator gas solid separation area
Second regeneration is distinguished into the inside and outside areas Liang Ge by the interior bucket that setting is connect with lower section renewing zone in the cone section of lower section, and outskirt becomes again
Raw agent recycling, storage area；The flue gas and catalyst of first renewing zone, which enter inside the interior bucket, to be continued to burn reaction；The interior bucket designs
For iso-cross-section cylinder or cross-sectional area gradually increase upwards, gas flow rate continuously decreases burns reaction zone；At this time at this
It is arranged outside interior bucket and burns air shooter and third distributor, burns gas to catalyst storage area supplement.
4. catalytic cracking reaction regeneration method as described in claim 1, which is characterized in that bore section and gas solid separation in regenerator
Second renewing zone shell is set in area's shell, and the first renewing zone is directly connected to the second renewing zone, the setting of the second outlet of the regeneration zone
The diminishing cone section of area and delivery pipe, the first separator of delivery pipe outlet setting flue gas gas-solid；The second renewing zone shell makes
Second renewing zone and regenerator gas solid separation area, catalyst storage, which separate, is split into two independent spaces, and regenerative response area urges
Agent and gas directly carry out preliminary gas solid separation in outlet of the regeneration zone, and catalyst enters urging between renewing zone and regenerator shell
Agent storage area.
5. catalytic cracking reaction regeneration method as described in claim 1, which is characterized in that regenerative agent storage area and first again
Catalyst circulation pipe is set between raw area, controls the combustion reaction temperature of the first renewing zone spent agent.
6. catalytic cracking reaction regeneration method as described in claim 1, which is characterized in that when catalyst regeneration reaction needs to take
When hot, draw catalyst from regenerative agent storage area and enter catalyst cooler, catalyst after cooling is directly entered from catalyst tube
Burn gas preheating zone.
7. catalytic cracking reaction regeneration method as claimed in claim 3, which is characterized in that regenerated to second through third distributor
Area's supplement burns gas.
8. catalytic cracking reaction regeneration method as described in claim 1, which is characterized in that in reactor stripping section and reactor
The intersegmental setting spent agent return duct of cracking reaction behind bottom or gasification, controls temperature, oil ratio and the catalysis of inside reactor
Agent activity.
9. catalytic cracking reaction regeneration method as described in claim 1, which is characterized in that be catalyzed in regenerator dense-phase fluidized bed
The reaction after the intersegmental setting reaction regeneration agent cooler of cracking reaction and cooling after agent storage area and reactor bottom or gasification
Regenerative agent delivery pipe, make by regenerative agent cooler cool down after regenerative agent enter reactor, control inside reactor temperature,
Oil ratio and catalyst activity.
10. catalytic cracking reaction regeneration method as claimed in claim 3, which is characterized in that burn gas be passed through regenerator
The total amount of body be 100% meter, be passed directly into from bottom burn gas preheating zone the amount for burning gas be 35%~85%, make to burn
The gas void tower flow velocity of gas preheating zone is in 0.3m/s~1.0m/s；From the second distributor enter burn gas amount be 30~
60%, the amount for burning gas entered from third distributor is 0~10%；Each section gas is introduced again by gas distributor respectively
In raw device.
11. catalytic cracking reaction regeneration method as described in claim 1, which is characterized in that second part burns gas again
Catalyst material position top, the first Perforated plate distributor lower section burnt between gas preheating zone and renewing zone enter in raw agent preheating zone
Regenerator, the high-temperature gas come with preheating zone mix, and then enter renewing zone through the first Perforated plate distributor, and reaction is burnt in participation.
12. catalytic cracking reaction regeneration method as claimed in claim 7, which is characterized in that described to burn gas first again
Enter regenerator below the orifice plate in raw area and the second regeneration section.
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| CN201610002678.2A CN105505441B (en) | 2016-01-06 | 2016-01-06 | A kind of catalytic cracking reaction regeneration method and device |
| PCT/CN2016/111713 WO2017118301A1 (en) | 2016-01-06 | 2016-12-23 | Method and apparatus for catalytic cracking reaction and regeneration |
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| CN201610002678.2A CN105505441B (en) | 2016-01-06 | 2016-01-06 | A kind of catalytic cracking reaction regeneration method and device |
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| CN105505441B (en) * | 2016-01-06 | 2018-08-21 | 石宝珍 | A kind of catalytic cracking reaction regeneration method and device |
| FR3060415B1 (en) * | 2016-12-15 | 2020-06-26 | IFP Energies Nouvelles | CATALYTIC CRACKING PROCESS OF NAPHTA WITH REPARATOR COMPARTMENT IN TURBULENT FLUIDIZED BED |
| CN110237779A (en) * | 2018-05-29 | 2019-09-17 | 青岛京润石化设计研究院有限公司 | A kind of catalyst multi-stage fluidized regeneration method and catalyst regenerator |
| CN108889341A (en) * | 2018-07-12 | 2018-11-27 | 青岛京润石化设计研究院有限公司 | A kind of regenerating catalyst in fluidized bed method |
| CN110950729B (en) * | 2018-09-27 | 2022-06-07 | 中石化洛阳工程有限公司 | Method and equipment for improving selectivity of low-carbon olefin |
| CN111282602A (en) * | 2018-12-10 | 2020-06-16 | 中国石化工程建设有限公司 | Method and system for oxidizing and regenerating catalyst |
| CN113110638B (en) * | 2021-04-20 | 2022-03-11 | 万华化学集团股份有限公司 | Automatic control method for ethylene cracking furnace coke burning, storage medium and electronic equipment |
| CN115637166A (en) * | 2021-07-20 | 2023-01-24 | 青岛京润石化设计研究院有限公司 | Catalytic conversion method and reactor for raw oil and light hydrocarbon |
| CN113600246A (en) * | 2021-08-23 | 2021-11-05 | 中冶赛迪上海工程技术有限公司 | Desulfurization catalyst regeneration method and system |
| WO2023098879A1 (en) * | 2021-12-03 | 2023-06-08 | 中国石油化工股份有限公司 | Fluid catalytic cracking regeneration apparatus, and use thereof |
| WO2023208083A1 (en) * | 2022-04-29 | 2023-11-02 | 中国石油化工股份有限公司 | Catalytic cracking catalyst regeneration method and system using bio-based gas-phase fuel |
| WO2023208079A1 (en) * | 2022-04-29 | 2023-11-02 | 中国石油化工股份有限公司 | Catalytic cracking catalyst regeneration method and system using biochar fuel |
| TW202342173A (en) * | 2022-04-29 | 2023-11-01 | 大陸商中國石油化工科技開發有限公司 | Catalytic cracking catalyst regeneration method and system using bio-based liquid-phase fuel |
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| US7026262B1 (en) * | 2002-09-17 | 2006-04-11 | Uop Llc | Apparatus and process for regenerating catalyst |
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| CN105505441B (en) * | 2016-01-06 | 2018-08-21 | 石宝珍 | A kind of catalytic cracking reaction regeneration method and device |
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| US7026262B1 (en) * | 2002-09-17 | 2006-04-11 | Uop Llc | Apparatus and process for regenerating catalyst |
| CN101554598A (en) * | 2007-12-21 | 2009-10-14 | Bp北美公司 | System and method of regenerating catalyst in a fluidized catalytic cracking unit |
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| CN105505441A (en) | 2016-04-20 |
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