CN205774340U - A kind of catalytic cracking reaction regenerating unit - Google Patents
A kind of catalytic cracking reaction regenerating unit Download PDFInfo
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- CN205774340U CN205774340U CN201620005002.4U CN201620005002U CN205774340U CN 205774340 U CN205774340 U CN 205774340U CN 201620005002 U CN201620005002 U CN 201620005002U CN 205774340 U CN205774340 U CN 205774340U
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Abstract
A kind of catalytic cracking reaction regenerating unit, for petroleum hydrocarbon raw material catalytic reaction process；It is characterized in that, regenerator itself is divided into and burns gas preheating zone, the first renewing zone, the second renewing zone and gas-solid Disengagement zone；Burning gas directly to preheat with the realization of regenerative agent mixed heat transfer in regenerator, the NOx making burning process generate reduces；Burn gas makes regenerative agent cool down simultaneously, makes the oil ratio of reactor increase, and improves the product slates of reaction；Thering is provided other low temperature catalyst for reactor, this low temperature catalyst can be the regenerative agent of spent agent or cooling simultaneously, optimizes reactor condition further, controls product slates.
Description
Technical field
The present invention relates to a kind of chemical field gas-solid catalysis technology, particularly relate to a kind of for petroleum hydrocarbon catalysis
Reaction regeneration device.
Background technology
Catalytic cracking of petroleum hydrocarbon reaction is the secondary operations technique of crude oil, by raw material reaction and catalyst regenerative response two
Course of reaction forms.Raw material reaction process generally generates the coke of inlet amount 5.5% ~ 10.0%, and these coke are attached to catalyst
Surface, blocking catalyst micropore, it is necessary to cyclic char makes renewing catalyst activity.Catalytic material reaction and catalyst regenerative response
It it is all important sport technique segment.
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.
Include two-stage regeneration than more typical catalyst regeneration techniques, countercurrently two-stage regeneration technology.Especially UOP is public
The adverse current two-stage regeneration technology of department and the exploitation of middle petrochemical industry Beijing designing institute embodies higher efficiency.Uop Inc. and Ashland are public
Department discloses its two-phase up-flow regeneration reaction regeneration technology developed jointly in US4299687, and CN 97121795.5 discloses
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).Along with the raising of environmental requirement, traditional scheme uses builds equipment for denitrifying flue gas control
The discharge of NOx, increases investment, energy consumption and operating cost, affects economic benefit.Combustion reaction is directly reduced in burning process
The technology that journey NOx generates is more preferable approach.
In prior art, catalyst regeneration (burning) course of reaction in from compressor come about 190 DEG C burn gas
(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 generate.
In regenerator arranges the catalytic cracking process of regenerative agent cooler, in prior art, regenerative agent cooler produces
Low-temp recovery agent returns burns reaction zone, can reduce the temperature burning reaction, and impact is burnt response speed, the most just reduced burning
Burnt reaction efficiency；The circulating load generally requiring increasing regenerative agent makes up renewing zone temperature.But the regenerative agent phosphorus content looped back is very
Low, the content of combustion zone coke can be reduced again, too increase the energy consumption of catalyst circulation conveying simultaneously.
In catalytic cracking of petroleum hydrocarbon course of reaction, catalyst is key problem, but catalysis in reactor in course of reaction
The performance of agent and the performance of unreacted procatalyst are different.As a example by hydrocarbon compound catalytic cracking reaction, course of reaction
Middle catalyst can make the performance of catalyst during real reaction gradually become because of green coke, alkaline components and metallic pollution, passivation
Difference, in reactor, especially in tubular reactor, the performance of each site catalysts is different, and the catalytic action efficiency played is also
Different.The additionally activity of catalyst, reaction oil ratio or the temperature of air speed, reaction raw materials and catalyst and temperature in course of reaction
The reaction conditions such as difference are all the key factors affecting raw material reaction result, and being varied and controlled of these conditions all can change reaction knot
Really.
Catalytic cracking of petroleum hydrocarbon is more than C with carbon number3Component be main purpose product, C2And following little molecule product master
If the product of thermal cracking.Intensified catalytic cracking reacts, and reducing heat cracking reaction is the target that catalytic cracking process is pursued always.
During catalytic cracking reaction, the selection of reaction condition and control are directly connected to the selection of reaction conversion ratio and reactor product
Property.The technology of existing optimization response system operation is a lot, as a example by petroleum hydrocarbon raw material catalytic conversion reaction, and dry gas pre-lifting skill
The mixing temperature of art, employing feed change decanting point and injected media controls technology, outlet area rapid separation, chilling termination
Reaction technologies etc. all on reaction result impact substantially, are the most preferably applied.Catalyst performance in course of reaction
Improve and control also it is critical that.
From the seventies in last century, catalytic cracking of petroleum hydrocarbon reaction riser reactor replaces fluidized-bed reactor.Stone
Hydrocarbon feedstock catalytic cracking reaction is the gas-solid endothermic reaction, and reaction raw materials is 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 catalytic reaction.The heat of gasification of liquid material is by regenerating
Catalyst provides.All there are two processes of the gentle phase reaction of liquid-phase vaporization in the liquid charging stock catalytic reaction using tubular reactor.
Gasification realizes by contacting heat supply with catalyst, due to gasify not moment, complete, in gasification or many simultaneously
Or there is certain reaction less.The essential advantage of tubular reactor is that the existence of " gradient ", so could realize improving instead
Answer the target of " motive force " (reactant concentration), improve reaction efficiency and selectivity.This is the master being replaced fluid bed by riser
Want one of reason.Petroleum hydrocarbon raw material constitute complexity, reactor inlet enter raw molecule amount substantially 300, reactor outlet
Molecular weight product is substantially 100 or less, and in riser reactor, diverse location presents different reactant character with anti-
Answer process, it is also desirable to different reaction conditions.As more than atomizer, the incipient stage of gas phase reaction zone, raw oil completes
The mainly raw oil macromole cracking reaction carried out after gasification, this process is typically through the reaction of about 1.0 ~ 1.5 seconds
Between, the gas phase reaction zone of riser latter half is then substantially carried out less molecule such as diesel oil, gasoline, liquefied gas composition react again with
And the reaction such as isomerization, hydrogen migration.The most whole gas phase reaction zone is divided into " cracking reaction district modifies reaction zone "
Deng.In liquid-phase vaporization course of reaction, the high temperature of the temperature difference between catalyst and raw material and catalyst all can increase heat cracking reaction, increases
Add C2Following side-product ratio, affects economic benefit；Cracking in vapour phase reaction zone, the temperature of modification reaction zone, oil ratio, catalyst
The reaction result of whole reaction zone is all caused appreciable impact by activity etc..
As a example by petroleum hydrocarbon raw material catalyzed conversion, result of study both domestic and external already confirms, regenerative agent temperature is high, causes
Reactant oil ratio is relatively low, between regenerative agent with reaction raw materials to contact the temperature difference big, dry gas yied all can be caused high, liquid yield is produced
Raw appreciable impact；Along with the carrying out of reaction in riser, the activity of catalyst quickly reduces, and riser downstream reaction district efficiency drops
Low, affect reaction effect.Reducing regenerative agent temperature, the activity improving oil ratio and raising riser inner catalyst is to urge for many years
Change the target that cracking unit is pursued always.
Many technical measures are had in terms of the regenerative agent reducing reaction raw materials liquid-phase vaporization contact area and the raw oil temperature difference.Pin
To reduce with raw oil first contact temperature problem, it will be most readily appreciated that way be " low temperature catalyst in external warmer to be drawn
Enter riser pre lift zone ".Uop Inc. proposes in external warmer the nineties in last century in patent US5800697
Low temperature catalyst sends 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-renovation process, arranges cooling catalyst on regenerator side
District, the thermal regenerant from dense bed enters cooling area heat exchange from outlet and enters carry through standpipe, guiding valve to preference temperature
Reaction is participated in, so that reaction oil ratio becomes independent variable bottom riser reactors.CN101161786A discloses a kind of stone
The method for transformation of petroleum hydrocarbon class, the cooler cooling that is regenerated catalyst through of heat returns to reactor bottom participation raw oil contact also
Carrying out cracking reaction, reclaimable catalyst is transported to regenerator after stripping to carry out coke burning regeneration Posterior circle use or partly directly enters
Enter the blender of reactor bottom.
The another kind of way reducing raw oil and the regenerative agent first contact temperature difference is that the temperature of raw oil is improved.
CN101144028A discloses a kind of cracking method for hydrocarbon oil, hydrocarbon ils and regenerated catalyst is heated in heat exchanger, then makes to change
Hydrocarbon ils after heat and the regenerated catalyst haptoreaction in the reactor after heat exchange.
It addition, catalyst that the influence factor of reaction not only includes reacting the catalyst temperature of front pre lift zone, liquid phase is (former
Material oil) the gasification zone contact temperature difference and oil ratio, the cracking in vapour phase reaction zone catalyst activity mediating recipe oil comparison after raw oil gasification
Course of reaction also has a major impact.
To the control of catalyst action in each position course of reaction in reactor and improvement, in addition to liquid-phase vaporization district, also
The improvement of the catalyst of the gas phase reaction zone after raw oil is gasified, the control to the catalyst condition provided should be included.
To sum up, condition and the mode of catalyst entrance reactor are significant to improving raw material reaction effect, optimize again
Life and reaction, formation is mutually matched, the complete reaction regeneration decorum is more meaningful；Use high temperature to burn gas and carry out catalyst again
Raw reaction can improve the discharge index of flue gas.
Summary of the invention
Present invention is primarily targeted at a kind of catalytic cracking reaction regenerating unit of offer, by raw material reaction and catalyst again
Raw two reactive moieties composition, including catalyst regenerator, tubular reactor, reacting-settler etc., reaction regeneration process is by pressing
Once step is carried out:
1, reaction raw materials enters at reactor different parts, contacts with catalyst and by catalyst heating and gasifying, then enters
Row reaction；Product enters immediately after reactor outlet flows out together with catalyst and is located at referred to as first order gas in settler
Solid separator and second level gas-solid separator, it is achieved catalyst and product edema caused by disorder of QI from, product gas flows out through settler oil gas vent.
2, completing the entrance of the catalyst after raw material reaction settler stripping zone to strip, the spent agent after stripping is through to be generated
Inclined tube enters bottom the regenerative response district 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 with and the flue gas that produces of regenerative response together be delivered up, realize gas in regenerator gas solid separation district
Body and the separation of catalyst, gas flows out regenerator from exhanst gas outlet, the dense-phase fluidized bed storage that catalyst is introduced in regenerator
Deposit district, burn gas preheating zone from this district through what regenerator bottoms delivered to by regenerative agent conveying pipe, in preheating zone with to burn gas straight
Connecing mixing to make to burn gas heating, self is cooled simultaneously；Regenerative agent after cooling is from burning gas preheating zone through regenerator sloped tube
Reactor is entered below reaction raw materials entrance.It is provided with regenerator catalyst cooler (also referred to as external warmer), catalysts
During cooler, regenerator catalyst cooler and catalysts cooler catalyst inlet arrange this regenerator dense-phase fluidized bed
Storage area.
3, Part I burn gas regenerator bottoms burn gas preheating zone from gas distributor enter burn gas
Preheating zone, directly forms fluidized state contact heat-exchanging with regenerative agent, is heated on backward through Perforated plate distributor inflow catalyst
Renewing zone；Another is set above or below the orifice plate burnt between gas preheating zone and catalyst regeneration zones and burns gas
(main air) enters pipe and distributor pipe (claiming the second distributor), introduces partial regeneration by this pipe and burns gas entrance regenerator；Excellent
Change, Part II burn gas above inner catalyst material position, regenerative agent preheating zone, burn gas preheating zone and renewing zone it
Between orifice plate below enter regenerator, with preheating zone come high-temperature gas mix, then through orifice plate entrance renewing zone, participate in burning
Reaction；Completing the gas-carrying portion catalyst after burning and carry out full gas solid separation in regenerator gas solid separation district, gas is from cigarette
Regenerator is flowed out in gas outlet.
4, catalyst inventory or the material position of gas preheating zone is burnt by the regenerative agent upper Valve controlling arranged of conveying pipe.
5, by burning catalyst material position, gas preheating zone or the change of reserve, and gas preheating zone is burnt in change entrance
Burn gas flow and can regulate gas preheating temperature and regenerative agent chilling temperature.
According to assembly of the invention, it is divided in catalyst regenerator housing and is divided into catalyst regenerative response part, burning up and down
Burnt gas (generally using air) regenerator section and gas-solid separate section；Burning between gas preheating zone and catalyst regeneration zones
Circulation orifice plate is set, dense phase fluidized catalyst storage area is set between renewing zone and gas-solid Disengagement zone, be used for as regenerative agent
Conveying pipe, external warmer (if any) provide regenerated catalyst；This regenerative agent storage area can be located at catalyst regeneration zones, it is also possible to
It is independently arranged outside renewing zone；Regenerative agent conveying pipe is set between gas preheating zone in this regenerative agent storage area and burning；When needing
Regenerator to be arranges catalyst cooler (external warmer), time reaction regeneration agent cooler is set for reactor, regeneration catalyzing
The catalyst inlet of agent cooler and reaction regeneration agent cooler is also provided in this district.
Reactor body is riser conversion zone, is followed successively by raw oil gasification zone, catalytic cracking on raw oil inlet port
Reaction zone, downstream, catalytic cracking reaction zone arranges settler, arranges gas-solid separator in it, isolated catalyst by gravity to
Lower entrance stripping section；Spent agent after stripping enters regenerator renewing zone through regeneration standpipe, preheats with burning gas from below
The gas contact of burning in district carries out burning reaction.
According to assembly of the invention, regenerator renewing zone is further separated into the first renewing zone, the second renewing zone；First regeneration
District is in bottom, and the second renewing zone is on the first top, renewing zone；The each interval in first renewing zone and the second renewing zone arranges circulation orifice plate
(distributor)；The catalyst of the first renewing zone and gas are transported to the second renewing zone through orifice plate simultaneously to be continued to burn；Second
Coboundary, renewing zone (catalyst material position) extends up to what the regenerator renewing zone diameter interval with gas solid separation gradually expanded
Cone section；Reducing due to gas flow rate in cone section, make the density of catalyst increase, become dense-phase fluidized bed, this fluid bed becomes simultaneously
For regenerative agent storage area；Second renewing zone is provided above flue gas gas solid separation district；In the second dense-phase fluidized bed district, renewing zone and burning
Arranging regenerative agent conveying pipe between burnt gas preheating zone, regenerative agent regenerative agent after this regenerative agent conveying pipe will burn is sent into and is burnt
Gas preheating zone；Spent agent enters the first renewing zone；Part is burnt gas (general custom claims main air) and is entered through gas distribution tube
Gas preheating zone, directly contacts with regenerative agent in preheating zone, is reproduced agent heating, then enters the first renewing zone through orifice plate；
Regenerative agent self is cooled while gas is burnt in heating, is burnt the regenerative agent after gas cools down from preheating zone through catalyst
Pipeline (commonly referred to as standpipe) enters reactor bottom (commonly referred to as pre lift zone).
According to assembly of the invention, in the cone section below regenerator gas solid separation district, interior bucket is set, by the second renewing zone
Being divided into inside and outside Liang Ge district, outskirt becomes regenerative agent recovery, storage area；The flue gas of the first renewing zone and catalyst enter this interior bucket and continue
Continue and burn reaction；This interior bucket is designed as the cylinder of iso-cross-section or cross-sectional area is upwards gradually increased, gas flow rate is gradually lowered
Burn reaction zone；Now arrange outside this interior bucket and burn air shooter and distributor, supplement to this catalyst storage district and burn
Burnt gas.
According to assembly of the invention, the second renewing zone housing is set in regenerator cone section and gas-solid Disengagement zone housing, the
One renewing zone directly connects with the second renewing zone, and the second renewing zone exports and arranges conveying pipe, and conveying pipe outlet arranges and divides at the beginning of gas-solid
From device, make renewing zone and regenerator gas solid separation separate and be split into two independent parts, the catalyst in regenerative response district and gas
Directly in renewing zone, outlet carries out preliminary gas solid separation, gas in regenerator gas solid separation district again through being located at renewing zone and regeneration
Two-stage rotation between device housing flows out regenerator after isolating catalyst；Catalyst enters between renewing zone and regenerator housing
Catalyst storage district.
According to assembly of the invention, catalyst circulation pipe is set between regenerative agent storage area and the first renewing zone, controls
The combustion reaction temperature of the first renewing zone spent agent.
According to assembly of the invention, when catalyst regenerative response needs to take heat, draw catalyst from regenerative agent storage area and enter
Entering catalyst cooler, the catalyst after cooling is directly entered from catalyst tube and burns gas preheating zone.
According to the concrete scheme of the present invention, in assembly of the invention, in reactor stripping section and reactor bottom (pre-lift
Section) or gasification after the intersegmental spent agent return duct that arranges of cracking reaction, control the temperature of inside reactor, oil ratio and catalyst
Activity.
According to the concrete scheme of the present invention, in assembly of the invention, in the second renewing zone and reactor bottom (pre-lift
Section) or gasification after cracking reaction intersegmental arrange reaction regeneration agent cooler and cooling after reaction regeneration agent conveying pipe, make fall
Regenerative agent after temperature enters reactor, controls the temperature of inside reactor, oil ratio and catalyst activity.
According to specific embodiments of the present invention, in assembly 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；Described first orifice plate can be porous barrier, also
Can be to be the distribution grid of other forms, one of its effect is to make the gas of preheating zone below distribution grid (portability part is urged
Agent) by this 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 prevent regenerative agent from being carried by air-flow and are upwardly into renewing zone；Permissible
Understand, in the present invention, can suitably adjust position being set or controlling gas preheating zone catalyst controlling level of the first distribution grid
To control to enter the catalytic amount of the first renewing zone from preheating zone.Additionally, in the method for the present invention, it is also possible to as desired by
Second gas distributor introducing portion is burnt gas and is entered the first renewing zone, this gas distributor can above the first orifice plate,
Can also be below the first orifice plate；Preferably, this distributor is arranged below the first orifice plate.
According to specific embodiments of the present invention, in assembly of the invention, in described regenerator renewing zone, enter in spent agent
It is additionally provided with on KouSecond orifice plate；Described second orifice plate can be porous barrier, or the distribution grid of other forms；Second hole
The Main Function of plate is to make the gas of the first renewing zone and catalyst even into the second renewing zone, makes the catalysis of the second renewing zone
Agent active fluidization and mixing, improve and burn effect；Additionally, in the method for the present invention, it is also possible to as desired by the 3rd gas
Distributor introducing portion is burnt gas and is entered the second renewing zone, and this gas distributor can be above the second orifice plate, it is also possible to
Below second orifice plate；Preferably, this distributor is arranged below the second orifice plate.
According to the preferred embodiment of the present invention, in assembly of the invention, to be passed through the gas that burns of regenerator
Total amount is 100% meter, and the amount burning gas being passed directly into gas preheating zone from bottom is 35%～about 70%, from the second distribution
The amount burning gas that device enters is about 30 ~ 60%, and the amount burning gas entered from the 3rd distributor is about 0 ~ 10%；Respectively
Portion gas can be introduced in regenerator by gas distributor respectively, and concrete gas distributor can select showing of art
Technology, the present invention is had to repeat no more.
The effect of the present invention
Burn gas after regenerator self-preheating again with the coke gasification reaction on catalyst, form the low flue gas of NOx content；
Burn gas makes regenerative agent cool down simultaneously, provides low-temp recovery agent for reactor, forms low temperature between reactor and regenerator
Regenerant recycle, can reduce thermal cracking and especially gasify and the heat cracking reaction in cracking reaction district, can adjust and gasify and react
Thermal balance relation, realizes carrying out reaction each district catalyst multi_control and reducing energy consumption easily and flexibly.
Generally speaking, the catalyst reaction regenerating unit of the present invention is used for petroleum hydrocarbon raw material catalytic cracking process, regeneration
Process self is to burning gas preheating, it is achieved high-temperature gas burns, and reduces NOx emission；There is provided low temperature again for reactor simultaneously
Raw agent, it is not necessary to provide low-temp recovery agent that independent regenerative agent cooling device is set for reactor；After making spent agent or cooling
Regenerative agent cracking reaction district after reaction raw materials gasifies supplements and enters reactor, forms dual catalyst circulation for reactor, can
According to diverse location reaction condition need different catalysts condition is provided, it is achieved enter reacting each district catalyst easily and flexibly
Row multi_control.
Being used for of the present invention realizes described reaction regeneration device and can be found in shown in Fig. 1 ~ Fig. 8.
Accompanying drawing explanation
Reaction-regenerating section schematic diagram in the catalytic cracking reaction technology of one detailed description of the invention of Fig. 1: the present invention.
The catalytic cracking reaction of the another way of Fig. 2: the present invention-regenerating section schematic diagram.
The catalytic cracking reaction of the another way of Fig. 3: the present invention-regenerating section schematic diagram.
The catalytic cracking reaction of the another way of Fig. 4: the present invention-regenerating section schematic diagram.
The catalytic cracking reaction of the another way of Fig. 5: the present invention-regenerating section schematic diagram.
Reaction-regenerating section the schematic diagram taking heat containing regenerator of Fig. 6: the present invention.
Fig. 7: the present invention regenerates the structural representation of a kind of embodiment of interval distribution grid.
Fig. 8: the present invention regenerates the structural representation of the another embodiment of interval distribution grid.
Numbering explanation in figure: 1 reactor；2 burn gas preheating zone；3 first catalyst regeneration zones；4 second catalyst are again
Raw district；5 regenerator gas solid separation districts；6 settler stripping sections；7 settler dilute-phase zones；8 regenerator catalyst cooler；9 reactions
Regenerative agent cooler；11 regenerative agent inclined tubes；12 regeneration guiding valves, 13 reactor bottom catalyst section (commonly referred to as pre-lift)；14、
14B reaction raw materials, 14C reaction or the coldest raw material；15 reaction raw materials reaction zones；16 catalyst mixed zones；17, spent agent returns
Mouthful；18 spent agent return duct valves；19 spent agent return ducts；20 burn gas preheating zone housing；22 burn gas preheating zone gas
Body distributor；23 burn gas tube；24 low-temp recovery agent outlets；25 catalyst material position, gas preheating zone；26 regenerative agent distributions
Device；27 regenerative agent conveying tube valves；28 regenerative agent conveying pipes；29 regenerative agent conveying pipes；30 first catalyst regeneration zones housings；31
First orifice plate (multihole distributor);31B opening；31C hole cap；32 burning gases distributors, 33 burn gas tube；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 regenerator cone piece housings；41 second orifice plates (multihole distributor)；41B opening；41C hole cap；41D
Regenerative agent storage area grid；42 gas distributors；43 gas tubes；44A, 44B, 44C, 44D regenerative agent outlet；45 regenerative agent storages
Deposit catalyst material position, district；46 second renewing zone housings, bucket in 46B the second renewing zone；46C bores section；47 renewing zone outlet conduit；
48 gas-solids just separator；49 regenerator dense phase fluidized catalyst storage areas；50 regenerator gas solid separation district housings；51 regeneratoies
One-level gas-solid separator；52 regenerator two grades gas-solid separators；53 collection chambers；54 burn exhanst gas outlet；60 settler stripping zones
Housing；61 stripping internals；62 stripping vapour distributors；63 stripping steam pipes；64 spent agent outlets；65 inclined tubes to be generated；70 settler shells
Body；71 settler one-level gas-solid separators；72 settler two grades gas-solid separators；73 collection chambers；74 product gas outlet；81 regeneration
Device catalyst cooler catalyst inlet；82 regenerator catalyst cooler catalyst outlets；83 regenerator catalyst cooler
Outlet valve；91 reaction regeneration agent cooler catalyst inlets；92 reaction regeneration agent cooler outlets；93 reaction regeneration agent coolings
Device outlet valve；94 low temperature reaction regenerant inlet；31B, 41B gas and catalyst rise hole；31C, 41C distribution grid escutcheon；
Gas is burnt in A compression；C catalyst；F flue gas；S steam；G pre-lift medium；O reaction raw materials oil；H burns gas preheating zone catalysis
Agent controlling level.
Detailed description of the invention
Describing technical scheme in detail below in conjunction with drawings and Examples, protection scope of the present invention includes still
It is not limited to this.The device structure mentioned the most in detail in the present invention, all can use the routine techniques of art.
Refer to shown in Fig. 1 ~ Fig. 5, the present invention for realizing the reaction that described reaction regeneration device includes being set up in parallel
Device and regenerator, wherein:
Regenerator is for carrying out coke burning regeneration to the spent agent 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 district 5；Catalyst regeneration zones is divided
The first renewing zone 3 and the second renewing zone 4 of top for bottom；Each interval arranges orifice plate 31 or 41, and orifice plate is porous type, hole
The gross area of 31B, 41B is by the gas flow rate 12m/s ~ 40m/s, aperture 50mm ~ 200mm passed through；Preheating zone 2 height be 3.0m ~
7.0m, is designed less than 1.2m/s by gas superficial flow velocity；First scorch region 3 height 8.0m ~ 15.0m, by gas superficial flow velocity
1.4m/s ~ 2.5m/s designs, and gas solid separation district 5 is designed less than 0.8m/s by gas superficial flow velocity；Spent agent and the first renewing zone
And enter the first renewing zone between 1.0m/s ~ 4.0m/s above the orifice plate 31 that preheating is interval；Burn the catalysis of (regeneration) gas preheating zone
Agent material position H is 2.0 ~ 6.0m, and preferred H is 2.5m ~ 3.5m；Cyclone separator 51,52 is used to carry out gas solid separation；Regenerant recycle pipe
The circulating load of 38 regenerative agents is 0.5 ~ 1.5 times of the catalytic amount being entered reactor 1 by regenerator sloped tube 11；To lightweight material,
When reaction-regeneration system need not take heat, spent agent passes through spent agent return duct 19 and return port 17 above raw oil import
The mixed zone 16 of Returning reactor 1 at 2.0m ~ 10.0m, or below raw oil import at 2.0m ~ 7.0m bottom Returning reactor
13, spent agent back amount is 0.2 ~ 1.0 times of the catalytic amount being entered reactor 1 by regenerator sloped tube 11.
To there being the reaction raw materials of surplus heat (needs take heat), regenerative agent cooler 9 is set；It takes thermic load by the following method
Determine: the regenerative agent temperature after cooling 500 DEG C ~ 580 DEG C；The flow of catalyst enters reactor 1 by by regenerator sloped tube 11
0.2 ~ 1.0 times of catalytic amount determines；Regenerative agent after cooling passes through outlet 92 and inlet port 93 above raw oil import
The mixed zone 16 of Returning reactor 1 at 2.0m ~ 10.0m, or below raw oil import at 2.0m ~ 7.0m bottom Returning reactor
13。
When arranging regenerative agent cooler 8, the regenerative agent after cooling passes through regenerator catalyst cooler catalyst outlet
82 are directly entered and burn gas preheating zone, no longer enter catalyst regeneration zones as routine techniques；Regenerative agent cooler is general
Technical staff can complete design.
Settler, settler stripping zone those skilled in the art can complete design；According to above parameter, technical staff is permissible
Complete the Application Design of the inventive method；The present invention repeats no more.
The reaction regeneration device of the present invention provides the regenerative agent of different condition for reactor；Reaction condition is made more to optimize；By
In using high-temperature gas reaction, the NOx content in flue gas can be reduced；Real at regenerator self by the improvement of regenerator configuration
Now burn gas preheating, simplify device design, i.e. reduce investment, also reduce energy consumption；Optimizing materials reaction, improves product simultaneously
Distribution.
Embodiment:
It is shown in Figure 3 that reaction zone catalyst control used in the present embodiment and regenerative agent take apparatus for cooling.
Certain produces 150 × 10 per year4The catalytic cracking unit of petroleum hydrocarbon of t/a, reaction regeneration is arranged in juxtaposition, and burns gas preheating zone
2 use fluid bed form, and the first renewing zone 3 uses recirculating fluidized bed form, the second renewing zone 4 to be arranged on the first renewing zone 3 He
Regenerator Zhui Duan district between gas solid separation district 5, uses fluid bed form；Burn gas preheating zone, the first renewing zone is seen, second
The first orifice plate distribution grid 31 and the second orifice plate distribution grid 41 it is respectively provided with between renewing zone；Reactor 1 is riser form；Arrange
Reaction regeneration agent cooler 9, reaction regeneration agent cooler 9 produces middle pressure steam, and reaction regeneration agent cooler 9 uses and carries steam
Separator type, steam trap is connected directly between on reaction regeneration agent cooler 9, and diameter is identical with regenerative agent cooler；Instead
Answering the catalyst after the cooling of regenerative agent cooler to enter reactor above raw oil, concrete in-position see table；Participate in burning
Gas flow is total amount the 52% of burnt gas preheating, that sends into the first renewing zone burns 48% that gas is total amount, and this gas divides
Cloth device and conveying pipe are located at below the second orifice plate；Second renewing zone is not supplemented with burning gas；Reaction mass and embodiment are with former
The comparative example reaction condition having technology see table.
The embodiment of the present invention see table with the anti-plant bulk again of crude oil technology comparative example.
Embodiment see table with original technology comparative example reactor product forecast of distribution.
Claims (9)
1. a catalytic cracking reaction regenerating unit, is regenerated two reactive moieties by raw material reaction and catalyst and forms, including urging
Agent regenerator, tubular reactor, reacting-settler etc., it is characterised in that:
1., be divided into gas solid separation part, catalyst regenerative response part in catalyst regenerator housing up and down, to burn gas pre-
Hot part；Burn and the first gas distributor is set below gas preheating zone；Burn gas preheating zone and catalyst regeneration zones it
Between circulation orifice plate is set, be the first orifice plate, orifice plate is disposed underneath or over the second gas distributor；In regenerator gas solid separation district
In the cone section of lower section, dense phase fluidized catalyst storage area is set, when needs arrange catalyst cooler for regenerator, is used for
Regenerated catalyst is provided for regenerative agent conveying pipe, catalyst cooler；This regenerative agent storage area can be located at catalyst regeneration zones,
Can also be independently arranged outside renewing zone；Regenerative agent conveying is set between gas preheating zone in this regenerative agent storage area and burning
Pipe；When needs arrange catalyst cooler for regenerator, arrange reaction regeneration agent cooler for reactor, regenerated catalyst is cold
But the catalyst inlet of device and reaction regeneration agent cooler is also provided in this district；
2., reactor body be riser conversion zone, be followed successively by raw oil gasification zone, catalytic cracking on raw oil inlet port
Reaction zone, below catalytic cracking reaction zone and in catalytic cracking reaction zone, different parts arranges many places reaction raw materials import；Urge
Change cracking reaction district be provided above settler, reactor product gas-solid separator is set in it, isolated catalyst by gravity to
Lower entrance stripping section；Regeneration standpipe is set between stripping section and regenerator.
2. catalytic cracking reaction regenerating unit as claimed in claim 1, it is characterised in that regenerator renewing zone is further separated into
First renewing zone, the second renewing zone；First renewing zone is in bottom；First renewing zone and the second regeneration interval arrange circulation orifice plate,
It it is the second orifice plate；Second coboundary, renewing zone extend up to the interval diameter of regenerator renewing zone and regenerator gas solid separation by
The cone section that flaring is big；Forming dense-phase fluidized bed between bucket and cone section in second renewing zone, this fluid bed becomes regenerative agent storage simultaneously
Deposit district.
3. catalytic cracking reaction regenerating unit as claimed in claim 1 or 2, it is characterised in that in regenerator gas solid separation district
Arranging the interior bucket being connected with renewing zone, lower section in the cone section of lower section, the second renewing zone is divided into inside and outside Liang Ge district, outskirt becomes again
Raw agent recovery, storage area；The flue gas of the first renewing zone and catalyst enter and continue to burn reaction inside this interior bucket；This interior bucket designs
Upwards be gradually increased for cylinder or the cross-sectional area of iso-cross-section, gas flow rate is gradually lowered burns reaction zone；Now at this
Arrange outside interior bucket and burn air shooter and the 3rd distributor, supplement to this catalyst storage district and burn gas.
4. catalytic cracking reaction regenerating unit as claimed in claim 1, it is characterised in that below regenerator gas solid separation district
Cone section and gas-solid Disengagement zone housing in the second renewing zone housing is set, the first renewing zone directly connects with the second renewing zone,
Two renewing zone outlet setting area diminishing cone sections and conveying pipe, conveying pipe outlet arranges flue gas gas-solid just separator；Should
Second renewing zone housing makes the second renewing zone and regenerator gas solid separation district, catalyst storage separate and is split into two independent skies
Between, directly in renewing zone, outlet carries out preliminary gas solid separation for the catalyst in regenerative response district and gas, and catalyst enters renewing zone
And between regenerator housing catalyst storage district.
5. catalytic cracking reaction regenerating unit as claimed in claim 1, it is characterised in that store at dense phase fluidized catalyst
Catalyst circulation pipe is set between district and the first renewing zone, controls the combustion reaction temperature of the first renewing zone spent agent.
6. catalytic cracking reaction regenerating unit as claimed in claim 1, it is characterised in that when catalyst regenerative response needs to take
During heat, catalyst cooler is set, with catalyst transport with to burn gas pre-after the cooling of this catalyst cooler by regenerator
Hot-zone connects.
7. catalytic cracking reaction regenerating unit as claimed in claim 2, it is characterised in that in the first renewing zone and the second regeneration
Below interval orifice plate, gas distributor is set.
8. catalytic cracking reaction regenerating unit as claimed in claim 1, it is characterised in that at stripping section and reactor bottom or
The intersegmental spent agent return duct that arranges of cracking reaction after gasification, controls the temperature of inside reactor, oil ratio and catalyst activity.
9. catalytic cracking reaction regenerating unit as claimed in claim 1, it is characterised in that store at close item fluid catalyst
Cracking reaction after district and reactor bottom or gasification is intersegmental arranges the reaction regeneration agent after reaction regeneration agent cooler and cooling
Conveying pipe, makes the regenerative agent after regenerative agent cooler is lowered the temperature enter reactor, controls the temperature of inside reactor, oil ratio
And catalyst activity.
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| CN201620005002.4U CN205774340U (en) | 2016-01-06 | 2016-01-06 | A kind of catalytic cracking reaction regenerating unit |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201620005002.4U CN205774340U (en) | 2016-01-06 | 2016-01-06 | A kind of catalytic cracking reaction regenerating unit |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110194967A (en) * | 2018-05-29 | 2019-09-03 | 青岛京润石化设计研究院有限公司 | A kind of catalysis reaction regeneration method of producing more propylene |
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2016
- 2016-01-06 CN CN201620005002.4U patent/CN205774340U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110194967A (en) * | 2018-05-29 | 2019-09-03 | 青岛京润石化设计研究院有限公司 | A kind of catalysis reaction regeneration method of producing more propylene |
| WO2019228131A1 (en) * | 2018-05-29 | 2019-12-05 | 青岛京润石化设计研究院有限公司 | Catalytic reaction regeneration method for increasing yield of propylene |
| CN110194967B (en) * | 2018-05-29 | 2021-07-23 | 青岛京润石化设计研究院有限公司 | Catalytic reaction regeneration method for producing more propylene |
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