CN206014775U - A kind of fluidized catalytic cracker - Google Patents

Abstract

The utility model provides a kind of fluidized catalytic cracker, is related to technical field of petrochemical industry.The fluidized catalytic cracker includes the first tubular reactor, gas-solid separator, the second tubular reactor, settler, baffling tubular type regenerator, turbulent bed regenerator, catalyst delivery line and catalyst cooling line.Fluidized catalytic cracker of the present utility model, two sections of tubular reactors of setting, and shorten the reaction segment length of tubular reactor, and then shorten finish time of contact, it is to avoid secondary response；The problem that baffling tubular type regenerator coke is difficult to ignition is avoided using the high temperature catalyst of the close phase section in turbulent bed regenerator bottom, and makes up to higher coke burning degree, while NO in regenerated flue gas can be reduced_XContent.

Description

A kind of fluidized catalytic cracker

Technical field

The utility model is related to technical field of petrochemical industry, more particularly to a kind of fluidized catalytic cracker.

Background technology

At present, the conventional fluid catalytic cracking unit generally existing used by petroleum chemical industry lacking for following several respects Point：First, the regenerator combined with fast bed using turbulent bed regenerator or turbulent bed, coke burning degree are less.By lively again Mechanics is limited, and regeneration temperature is higher, causes the regenerated catalyst temperature for participating in reaction higher (typically at 700 DEG C or so)；Due to The thermally equilibrated restriction of device, makes the oil ratio of heavy oil riser relatively small, and typically total oil ratio is 5～8 (total agent of riser The ratio of the weight flow summation of oil stock charging more each than the weight internal circulating load for catalyst in riser and riser) so that single The number of active center touched by the heavy oil feed of position weight is less, and this inhibits catalytic cracking reaction to a great extent.With When, in riser, the Contact Temperature of finish is higher, promotes heat cracking reaction to a certain extent.Second, riser reactor The time that length longer (generally more than 30 meters), finish are contacted is longer (typically at 4 seconds or so), and this is improving feedstock conversion The secondary response of cracking product is also exacerbated simultaneously；Show as the yield of cracked gas (including dry gas and liquefied gas) and coke compared with Height, vapour, diesel oil distillate yield relatively low；The inferior quality of catalytic diesel oil is also made, vehicle fuel blending component is not suitable as.The Three, using single conventional riser reactor, lack the measure modified by gasoline catalyzing, content of olefin in gasoline is high, quality compared with Low.4th, device itself lacks reduces NO in regenerated flue gas_XThe technical measures of content, cause NO in regenerated flue gas_XContent compared with High；And reduce NO in flue gas_XThe method of content mostly is using reduction catalytic cracking flue gas NO_XThe auxiliary agent of content or gas cleaning dress Put and equipment, relatively costly.For many years, domestic and international research institution is being overcome existing for above-mentioned conventional fluid catalytic cracking unit Substantial amounts of research work has been done in terms of shortcoming：

1st, two riser reactors are adopted, and one of them oil riser reactor of attaching most importance to, another are lighter hydrocarbons riser Reactor.The technology is disadvantageous in that：First, lighter hydrocarbons reclaimable catalyst is mixed with regenerated catalyst, to a certain extent Reduce the activity of the catalyst that reaction is participated in heavy oil riser reactor, unfavorable shadow is brought to product slates and product property Ring.Second, the internal circulating load of lighter hydrocarbons reclaimable catalyst is limited, is restricted the increase rate of heavy oil reaction oil ratio.3rd, adopt With traditional riser catalytic cracking reactor, nozzle set location is relatively low, the finish time of contact of heavy oil riser reactor Can only actually be controlled to 2～4 seconds, be shorter than 2 seconds reaction time be difficult to realize.As finish time of contact is longer, cause weight The property of the product slates and catalytic diesel oil of oil riser reactor is relatively poor.4th, the upgrading processes experience of catalytic gasoline The fractionation operation of heavy oil riser reactor reaction oil gas, the again condensation of gasoline and gasification produce substantial amounts of low temperature Heat, energy consumption are higher.

2nd, one regenerated catalyst cooler, regenerated catalyst cooler bottom are set in the lower section of conventional turbulent bed regenerator Portion arranges main air distributor.The technology is disadvantageous in that：First, the barrel diameter of regenerated catalyst cooler is less, because This is accomplished by limiting the main air quantity of the cooling being passed through by cooling main air distributor.Otherwise, a large amount of regenerated catalyst coolers Regenerated catalyst after interior cooling is flowed upwardly in regenerator by main for heated cooling wind entrainment, through annular space, and formation is urged Agent interior circulation, affects device normal operating.It is restricted due to cooling down main air quantity, thus can affects to high-temperature regenerated catalyst Cooling effect.Second, traditional riser catalytic cracking reactor is used, heavy oil reaction is difficult to realize shorter finish and connects The tactile time.

3rd, at the top of reacting-settler arrange a catalyst hooper and by pipeline be arranged above reacting-settler Catalyst tank is connected, and catalyst tank is connected with the close phase section of regenerator and reacting-settler by different pipelines.The technology It is disadvantageous in that：First, reclaimable catalyst is mixed with regenerated catalyst, reduces the catalysis for participating in reaction to a certain extent The activity of agent, brings adverse effect to product slates and product property.Second, the activity of heavy oil reclaimable catalyst is very low, to ginseng Very big with the activity influence of the catalyst of heavy oil reaction, heavy oil reaction can only be partially participated in, so that heavy oil reactant is oily The increase rate of ratio is restricted.3rd, the space of finish contact area is relatively large, and the finish time of contact of heavy oil reaction is still It is not controlled effectively completely, still suffers from a certain degree of secondary response.4th, lack the measure modified by gasoline catalyzing, Content of olefin in gasoline is high.

Utility model content

The purpose of this utility model is to provide a kind of fluidized catalytic cracker, to solve oil present in prior art The limited extent and gasoline catalyzing modification energy consumption that agent time of contact is longer to cause that secondary response is more, improve oil ratio is higher etc. Problem.

To achieve these goals, the utility model is employed the following technical solutions：

A kind of fluidized catalytic cracker that the utility model is provided, including the first tubular reactor, gas-solid separator, the Two tubular reactors, settler, baffling tubular type regenerator, turbulent bed regenerator, catalyst delivery line and catalyst cooling tube Road；First tubular reactor, the gas-solid separator, second tubular reactor and the settler are successively from lower past On be coaxially arranged in series, and the outlet of the first tubular type reactor top is connected with the gas-solid separator top dilute phase section, The oil gas vent of the gas-solid separator top dilute phase section is connected with the oil gas entrance of the second tubular reactor bottom, described The outlet of the second tubular type reactor top and the settler inner space；The baffling tubular type regenerator and the turbulent bed are again Raw device is coaxially arranged in series from the bottom up, and the outlet on the baffling tubular type regenerator top is dilute with the turbulent bed regenerator top Phase section is connected；The close phase section in the gas-solid separator bottom, the close phase section in the turbulent bed regenerator bottom pass through the catalyst Transfer pipeline is connected with the bottom of the baffling tubular type regenerator；The close phase section in the settler bottom is by the catalyst transport Pipeline is connected with the close phase section in the gas-solid separator bottom；The close phase section in the turbulent bed regenerator bottom is defeated by the catalyst Pipeline is sent to connect with the first tubular type reactor bottom；The close phase section in the turbulent bed regenerator bottom is cold by the catalyst But pipeline is connected with the second tubular type reactor lower part.

Further, the baffling tubular type regenerator includes the first tedge, sedimentation pipe and the second tedge；The sedimentation pipe For the pipeline section of upper end closure, second tedge includes casing section, changeover portion and outlet section from the bottom up, the changeover portion and Outlet section is located at the turbulent bed internal regenerator, and described sleeve pipe section is identical with the close phase section diameter of the turbulent bed regenerator and phase Connection, described sleeve pipe section are socketed the sedimentation pipe, and the sedimentation pipe is socketed first tedge, enable catalyst from described The outlet on the first tedge top flows into the inner chamber of the sedimentation pipe, then flows into described second by the outlet of the sedimentation pipe lower end The inner chamber of tedge, finally flows into the turbulent bed regenerator from the second tedge top export.The skill of the technical scheme Art effect is：Using the double backed arrangement form of the first tedge, sedimentation pipe and the second tedge, sufficient ensureing that regenerator has On the premise of enough reserves, the setting height(from bottom) of whole regenerator is reduced.

Further, the length of the first tubular type reactor reaction section is 5 meters～15 meters, and second tubular reactor is anti- The length for answering section is 5 meters～10 meters.The technical scheme has technical effect that：Length due to the first tubular type reactor reaction section Only 5 meters～15 meters, the length of the second tubular type reactor reaction section is only 5 meters～10 meters.When being carried out with the first tubular reactor When heavy oil catalytic cracking reaction, the second tubular reactor carry out gasoline catalyzing modification reaction, it is possible to achieve shorter finish contact Time (0.3 second～1.2 seconds), so as to effectively suppress secondary response, make the product point of RFCC and gasoline catalyzing modification The property of cloth and catalytic diesel oil significantly improves.

Further, also include that distributor pipe of cardinal wind and main wind inlet tube, the distributor pipe of cardinal wind are arranged at described first and rise Bottom of the tube and the turbulent bed regenerator bottoms；The main wind inlet tube is arranged on the described second side wall for rising bottom of the tube. The technical scheme has technical effect that：Distributor pipe of cardinal wind can be passed through to the first tedge simultaneously by main wind inlet tube to the Input air in two tedges, by rationally being divided with the air quantity of two strands of main wind of the second tedge to being passed through the first tedge Match somebody with somebody, in the first tedge, carry out oxygen deprivation regeneration, in the second tedge, carry out oxygen enrichment regeneration, due to containing in the second tedge Catalyst, can take away the heat of reaction of carbon monoxide generation in time, can avoid in the second tedge as carbon monoxide fires On the premise of burning causes equipment temperature runaway, in the first tedge to flue gas in NO_XReduced, to reduce NO in regenerated flue gas_X Content.

Further, the quantity of the main wind inlet tube is even number, and the circumference along second tedge is uniformly and symmetrically distributed. The technical scheme has technical effect that：The main wind inlet tube being uniformly and symmetrically distributed, makes the main wind in the second tedge of entrance equal Even distribution, is fully contacted with catalyst, ensures that catalyst regeneration effect.

Further, also include multilayer heavy oil feed nozzle, heavy oil feed nozzle described in multilayer is arranged at first tubular type On the side wall of reactor, the axially spaced-apart along first tubular reactor is distributed.The technical scheme has technical effect that：Weight Although oily feed nozzle belongs to existing conventional techniques equipment, but the heavy oil feed nozzle of Spaced distribution, it is adaptable to need oil Agent time of contact different plurality of raw materials oil, improve the applicability of fluidized catalytic cracker.

Further, the catalyst cooling line includes one-level regenerated catalyst cooler and the cooling of secondary regenerator catalyst Device；The close phase section in the turbulent bed regenerator bottom passes sequentially through the one-level regenerated catalyst cooler and the secondary regenerator is urged Agent cooler is connected with the second tubular type reactor lower part.The technical scheme has technical effect that：Regenerated using two-stage Catalyst cooler had both met the requirement of the catalyst temperature to entering the second tubular reactor, turn avoid generation low in a large number Warm, so that reduce energy consumption.

Further, also include low-temp recovery catalyst tank；The secondary regenerator catalyst cooler passes through the low temperature again Raw catalyst tank is connected with the second tubular type reactor lower part, and the spatial altitude of the low-temp recovery catalyst tank is located at institute State on gas-solid separator.The technical scheme has technical effect that：Low-temp recovery catalyst tank is located at secondary regenerator catalyst Between the lower entrances of cooler and the second tubular reactor, play a part of buffering and stabilization fluid, it is to avoid the second tubular type is anti- Answer.

Further, fluidized catalytic cracker also includes that air delivery pipe, the top of the low-temp recovery catalyst tank lead to Cross the air delivery pipe to connect with the close phase section in the turbulent bed regenerator bottom.The technical scheme has technical effect that：By Need to introduce in the catalyst cooling line of conveying regenerated catalyst compressed air as power, this partial air is imported rapid Assisted Regeneration process in dynamic bed regenerator, improves the utilization ratio of air.

The beneficial effects of the utility model are：

First, shorten the length of tubular reactor, it is possible to achieve shorter finish time of contact, so as to effectively suppress secondary counter Should, make the property of the product slates and catalytic diesel oil of RFCC and gasoline catalyzing modification significantly improve.

2nd, tubular type regenerator and turbulent bed regenerator series combination, and the close phase section in turbulent bed regenerator bottom is by described Catalyst delivery line is connected with the bottom of the baffling tubular type regenerator, reclaimable catalyst with from turbulent bed regenerator temperature Higher circular regeneration catalyst mixing, it is ensured that tubular type regenerator has higher inlet temperature, makes the tubular type regenerator can be with Higher coke burning degree is reached, so that the comprehensive coke burning degree of two regenerators of whole catalytic cracking unit and conventional turbulent bed Regeneration techniques is compared and is improved, and creates condition for greatly improving oil ratio.

The 3rd, two tubular reactors connected with gas-solid separator are set, and the first tubular type reactor reaction oil gas is through gas-solid It is directly entered in the second tubular reactor to contact with the regenerated catalyst after cooling after separating and carries out gasoline catalyzing modification reaction, keeps away Exempt from gasoline condensation and gasification again, reduce energy consumption.

Description of the drawings

In order to be illustrated more clearly that the technical scheme of the utility model specific embodiment, below will be to specific embodiment Needed for description, accompanying drawing to be used is briefly described.It should be evident that drawings in the following description are of the present utility model Some embodiments, for those of ordinary skill in the art, on the premise of not paying creative work, can be with basis These accompanying drawings obtain other accompanying drawings.

The structural representation of the fluidized catalytic cracker that Fig. 1 is provided for the utility model.

Reference：

The first tubular reactors of 1-；2- gas-solid separators；

The second tubular reactors of 3-；4- settlers；

5- baffling tubular type regenerators；The first tedges of 51-；

52- sedimentation pipes；The second tedges of 53-；

6- turbulent bed regenerators；The main wind inlet tubes of 7-；

8- distributor pipe of cardinal wind；9- heavy oil feed nozzles；

10- one-level regenerated catalyst coolers；11- secondary regenerator catalyst coolers；

12- low-temp recovery catalyst tanks；13- cyclone separators；

14- reacts collection chamber；15- flue gas collection chambers；

16- pipelines；17- distribution of steam pipes；

18- inertia separators；19- air delivery pipes.

Specific embodiment

The technical solution of the utility model is clearly and completely described below in conjunction with accompanying drawing, it is clear that described Embodiment is a part of embodiment of the utility model, rather than whole embodiments.Embodiment in based on the utility model, this The every other embodiment obtained under the premise of creative work is not made by field those of ordinary skill, belongs to this practicality Novel protected scope.

In description of the present utility model, it should be noted that term " " center ", " on ", D score, "left", "right", " perpendicular Directly ", the orientation of instruction such as " level ", " interior ", " outward " or position relationship are based on orientation shown in the drawings or position relationship, are only For the ease of describe the utility model and simplify description, rather than indicate or hint indication device or element must have specific Orientation, with specific azimuth configuration and operation, therefore it is not intended that to restriction of the present utility model.Additionally, term " the One ", " second ", " the 3rd " are only used for describing purpose, and it is not intended that indicating or hint relative importance.

In description of the present utility model, it should be noted that unless otherwise clearly defined and limited, term " peace Dress ", " being connected ", " connection " should be interpreted broadly, for example, it may be fixedly connected, or be detachably connected, or integratedly Connection；Can be mechanically connected, or electrically connect；Can be joined directly together, it is also possible to be indirectly connected to by intermediary, It can be the connection of two element internals.For the ordinary skill in the art, above-mentioned art can be understood with concrete condition Concrete meaning of the language in the utility model.

A kind of fluidized catalytic cracker is present embodiments provided, wherein：The fluid catalytic that Fig. 1 is provided for the utility model The structural representation of cracking unit.As shown in figure 1, the primary structure of fluidized catalytic cracker include the first tubular reactor 1, Gas-solid separator 2, the second tubular reactor 3, settler 4, baffling tubular type regenerator 5, turbulent bed regenerator 6, catalyst transport Pipeline and catalyst cooling line.

Specifically, the first tubular reactor 1, gas-solid separator 2, the second tubular reactor 3 and settler 4 are successively from lower past On be coaxially arranged in series, and the outlet on 1 top of the first tubular reactor is connected with 2 top dilute phase section of gas-solid separator, gas-solid point Oil gas vent from 2 top dilute phase section of device is connected with the oil gas entrance of 3 bottom of the second tubular reactor, the second tubular reactor 3 The outlet on top and 4 inner space of settler.In addition, baffling tubular type regenerator 5 and turbulent bed regenerator 6 are coaxial from the bottom up going here and there Connection is arranged, and the outlet on 5 top of baffling tubular type regenerator is connected with 6 top dilute phase section of turbulent bed regenerator.Meanwhile, gas-solid separator The close phase section in 2 bottoms, the close phase section in 6 bottom of turbulent bed regenerator are connected by the bottom of catalyst conduit and baffling tubular type regenerator 5 Logical；The close phase section in 4 bottom of settler is connected with the close phase section in 2 bottom of gas-solid separator by catalyst conduit；Under turbulent bed regenerator 6 The close phase section in portion is connected with 1 bottom of the first tubular reactor by catalyst conduit；The close phase section in 6 bottom of turbulent bed regenerator is by urging Agent pipeline is connected with 3 bottom of the second tubular reactor.

The existing fluidized catalytic cracker generally existing of petroleum chemical industry the shortcoming of following several respects：

First, in reactor, finish time of contact is longer, and secondary response is more；2nd, oil ratio is less, and increase rate is limited； 3rd, gasoline catalyzing modification energy consumption is higher.

The fluidized catalytic cracker of the present embodiment, preferably can solve the above problems：Two sections of tubular reactors are set, And shorten the reaction segment length of tubular reactor, and then shorten finish time of contact, it is to avoid secondary response；Regenerated using turbulent bed The high temperature catalyst of the close phase section in device bottom avoids the problem that baffling tubular type regenerator coke is difficult to ignition, and makes up to higher Coke burning degree.It is specifically described as follows：

Due to 6 series combination of baffling tubular type regenerator 5 and turbulent bed regenerator, and the close phase section in 6 bottom of turbulent bed regenerator Connected with the bottom of baffling tubular type regenerator 5 by catalyst delivery line, reclaimable catalyst is warm with from turbulent bed regenerator 6 The higher circular regeneration catalyst mixing of degree, it is ensured that baffling tubular type regenerator 5 has higher inlet temperature, makes baffling tubular type Regenerator 5 can reach higher coke burning degree, so that the synthesis of two regenerators of whole fluidized catalytic cracker is burnt Intensity is improved compared with conventional turbulent bed regeneration techniques the (difference of turbulent bed regenerator 6 and tubular type regenerator：One be In the range of 580～700 DEG C, the coke burning degree of turbulent bed regenerator 6 is much smaller than tubular type regenerator, and two is turbulent bed regenerator 6 Catalyst inventory is larger, thermal capacitance is also larger, not there are problems that coke is difficult to ignition.The catalyst inventory of tubular type regenerator is less, Thermal capacitance is also less, and when catalyst inlet temperature is relatively low, coke is difficult to ignition and allows to ignition, and coke burning degree is relatively low), so as to For greatly improve oil ratio create condition (from the point of view of catalytic cracking unit thermal balance relation, by change pressure balance make to urge The increase of agent internal circulating load can directly reduce the temperature of regenerator catalyst bed, in the case where regeneration is constant, burn strong Degree will decline to a great extent.This is to limit the principal element that oil ratio is greatly improved).While the reaction oil gas of the first tubular reactor 1 Be directly entered after gas solid separation the second tubular reactor 3 with through supercooling regenerated catalyst at a lower temperature (430～ 460 DEG C) contact, under this temperature conditions, heavy oil and diesel component in reaction oil gas substantially do not react, so as to keep away Exempt from gasoline condensation and again gasification, make the energy consumption of gasoline catalyzing upgrading processes realize on the premise of decreasing to be catalyzed vapour The independent modification of oil.

It should be noted that being provided with cyclone separator 13, reaction collection chamber 14 in settler 4.Cyclone separator 13 is wrapped Include a thick cyclone separator and one to four primary cyclones.Second tubular reactor, 3 upper end outlet passes through sealed tube Road 16 is connected with the entrance of thick cyclone separator, and the outlet of primary cyclone is by closed conduct 16 and reaction collection chamber 14 It is connected.And the top that collection chamber 14 is located at settler 4 is reacted, it is connected with fractionating column by reaction oil gas pipeline.Separately, turbulent bed is again The dilute phase section of raw device 6 is provided with one to six primary cyclones and one to six secondary cyclones.Wherein, one cyclonic The entrance of separator is communicated with the dilute phase section of turbulent bed regenerator 6, the outlet of primary cyclone by closed conduct 16 with The entrance of secondary cyclone is connected, and the outlet of secondary cyclone is pushed up with turbulent bed regenerator 6 by closed conduct 16 The entrance of the flue gas collection chamber 15 in portion is connected, and the outlet of flue gas collection chamber 15 is by flue gas pipeline and smoke energy recovering system phase Even.

In the alternative of the present embodiment, further, as shown in figure 1, baffling tubular type regenerator 5 includes the first rising Pipe 51, sedimentation pipe 52 and the second tedge 53.Specifically, pipeline section of the sedimentation pipe 52 for upper end closure, the second tedge 53 is under Up include that casing section, changeover portion and outlet section, changeover portion and outlet section are located inside turbulent bed regenerator 6, casing section with rapid The close phase section diameter of dynamic bed regenerator 6 is identical and is connected, and casing section is socketed sedimentation pipe 52, and sedimentation pipe 52 is socketed the first tedge 6, enable catalyst to flow into the inner chamber of sedimentation pipe 52, then going out by 52 lower end of sedimentation pipe from the outlet on 6 top of the first tedge Mouth flows into the inner chamber of the second tedge 53, finally flows into turbulent bed regenerator 6 from 53 top export of the second tedge.In this enforcement In example, using the double backed arrangement form of the first tedge 51, sedimentation pipe 52 and the second tedge 53, sufficient ensureing that regenerator has On the premise of enough reserves, setting height(from bottom) and the space of whole regenerator is reduced.

In the alternative of the present embodiment, further, as shown in figure 1, the length of 1 conversion zone of the first tubular reactor For 5 meters～15 meters, the length of 3 conversion zone of the second tubular reactor is 5 meters～10 meters.In the present embodiment, due to being provided with two Level tubular reactor, therefore the reaction length of tubular reactor can design shorter, the length of 1 conversion zone of the first tubular reactor is only For 5 meters～15 meters, the length of 3 conversion zone of the second tubular reactor is 5 meters～10 meters.When with the first tubular reactor 1 carry out weight Oily catalytic cracking reaction, when the second tubular reactor 3 carries out gasoline catalyzing modification reaction, it is possible to achieve when shorter finish is contacted Between (0.3 second～1.2 seconds), so as to effectively suppress secondary response, make RFCC and gasoline catalyzing modification product slates And the property of catalytic diesel oil significantly improves, the maximization of yield of gasoline is realized.In actual production, in order to improve production Efficiency, the total length of the first tubular reactor 1 is 7 meters～18 meters, and the internal diameter of 1 conversion zone of the first tubular reactor is 400 millimeters ～2500 millimeters, the total length of the second tubular reactor 3 is 7 meters～13 meters, and the internal diameter of 3 conversion zone of the second tubular reactor is 400 millimeters～2500 millimeters.

In the alternative of the present embodiment, as shown in figure 1, further, fluidized catalytic cracker also includes main wind Distributor pipe 8 and main wind inlet tube 7, distributor pipe of cardinal wind 8 are respectively arranged at 6 bottom of 51 bottom of the first tedge and turbulent bed regenerator Portion；Main wind inlet tube 7 is arranged on the side wall of 53 bottom of the second tedge.In the present embodiment, distributor pipe of cardinal wind 8 can be passed through To the first tedge 51 simultaneously by main wind inlet tube 7 to input air in the second tedge 53, by being passed through the first rising The air quantity of two strands of main wind of pipe 51 and the second tedge 53 carries out reasonable distribution, in the first tedge 51 carries out oxygen deprivation regeneration, Oxygen enrichment regeneration is carried out in the second tedge 53, due to containing catalyst in the second tedge 53, carbon monoxide can be taken away in time The heat that reaction is produced, can on the premise of avoiding causing equipment temperature runaway due to CO burning in the second tedge 53, In the first tedge 51 to flue gas in NO_XReduced, to reduce NO in regenerated flue gas_XContent.

In the alternative of the present embodiment, as shown in figure 1, further, the quantity of main wind inlet tube 7 is set to idol Number, the circumference along the second tedge 53 are uniformly and symmetrically distributed.In the present embodiment, the main wind inlet tube 7 being uniformly and symmetrically distributed, makes The main wind entered in the second tedge 53 is uniformly distributed, and is fully contacted with catalyst, ensures that catalyst regeneration effect.

In the alternative of the present embodiment, as shown in figure 1, further, fluidized catalytic cracker also includes multilayer The heavy oil feed nozzle 9 being arranged on 1 side wall of the first tubular reactor, axle of the heavy oil feed nozzle 9 along the first tubular reactor 1 To interval setting.In the present embodiment, although heavy oil feed nozzle 9 belongs to existing conventional techniques equipment, Spaced is distributed Heavy oil feed nozzle 9, it is adaptable to need finish time of contact different plurality of raw materials oil, improve fluidized catalytic cracker Applicability.

In the alternative of the present embodiment, as shown in figure 1, further, catalyst cooling line includes that one-level regenerates Catalyst cooler 10 and secondary regenerator catalyst cooler 11.Specifically, the close phase section in 6 bottom of turbulent bed regenerator is passed sequentially through One-level regenerated catalyst cooler 10 is connected with the bottom of the second tubular reactor 3 with secondary regenerator catalyst cooler 11.? In the present embodiment, the catalyst temperature to entering the second tubular reactor 3 had both been met using two-stage regenerated catalyst cooler Requirement, turn avoid a large amount of Low Temperature Thermals of generation, so as to reduce energy consumption.

In the alternative of the present embodiment, as shown in figure 1, further, fluidized catalytic cracker also includes low temperature Regenerated catalyst tank 12.Secondary regenerator catalyst cooler 11 is by low-temp recovery catalyst tank 12 and the second tubular reactor 3 Bottom connects, and the spatial altitude of low-temp recovery catalyst tank 12 is located on gas-solid separator 2.In the present embodiment, low temperature Regenerated catalyst tank 12 is located between secondary regenerator catalyst cooler 11 and the lower entrances of the second tubular reactor 3, is played Buffering and the effect of stabilization fluid, it is to avoid occur reaction fluctuation in the second tubular reactor 3 and affect the effect of gasoline upgrading.

In the alternative of the present embodiment, as shown in figure 1, further, fluidized catalytic cracker also includes air Delivery pipe 19.The two ends of air delivery pipe 19 top respectively with low-temp recovery catalyst tank 12,6 bottom of turbulent bed regenerator are close Phase section is connected.Using compressed air as the power for conveying catalyst in catalyst cooling line, compressed air is in low-temp recovery Assisted Regeneration process in turbulent bed regenerator 6 is entered by air delivery pipe 19 again in catalyst tank 12, the profit of air is improve Use efficiency.

Finally it should be noted that：Various embodiments above is only in order to illustrating the technical solution of the utility model, rather than which is limited System；Although being described in detail to the utility model with reference to foregoing embodiments, one of ordinary skill in the art should Understand：Which still can be modified to the technical scheme described in foregoing embodiments, or to which part or whole Technical characteristic carries out equivalent；And these modifications or replacement, do not make the essence of appropriate technical solution depart from this practicality new The scope of each embodiment technical scheme of type.

Claims (10)

1. a kind of fluidized catalytic cracker, it is characterised in that including the first tubular reactor, gas-solid separator, the second tubular type Reactor, settler, baffling tubular type regenerator, turbulent bed regenerator, catalyst delivery line and catalyst cooling line；

First tubular reactor, the gas-solid separator, second tubular reactor and the settler are successively under Up it is coaxially disposed, and the outlet of the first tubular type reactor top is connected with the gas-solid separator top dilute phase section, institute The oil gas vent for stating gas-solid separator top dilute phase section is connected with the oil gas entrance of the second tubular reactor bottom, and described The outlet on two tubular reactor tops and the settler inner space；

The baffling tubular type regenerator and the turbulent bed regenerator are coaxially disposed from the bottom up, the baffling tubular type regenerator top The outlet at end is connected with the turbulent bed regenerator top dilute phase section；

The close phase section in the gas-solid separator bottom, the close phase section in the turbulent bed regenerator bottom pass through the catalyst transport Road is connected with the bottom of the baffling tubular type regenerator；The close phase section in the settler bottom by the catalyst delivery line with The close phase section connection in the gas-solid separator bottom；The close phase section in the turbulent bed regenerator bottom passes through the catalyst delivery line Connect with the first tubular type reactor bottom；The close phase section in the turbulent bed regenerator bottom passes through the catalyst cooling line Connect with the second tubular type reactor lower part.

2. fluidized catalytic cracker according to claim 1, it is characterised in that the baffling tubular type regenerator includes One tedge, sedimentation pipe and the second tedge；The sedimentation pipe is the pipeline section of upper end closure, and second tedge is from the bottom up Including casing section, changeover portion and outlet section, the changeover portion and outlet section are located at the turbulent bed internal regenerator, described sleeve pipe Section is identical with the close phase section diameter of the turbulent bed regenerator and is connected, and described sleeve pipe section is socketed the sedimentation pipe, the sedimentation Pipe is socketed first tedge, catalyst is flowed in the sedimentation pipe from the outlet on the first tedge top Chamber, then the inner chamber of second tedge is flowed into by the outlet of the sedimentation pipe lower end, finally from the second tedge top Outlet flows into the turbulent bed regenerator.

3. fluidized catalytic cracker according to claim 1, it is characterised in that the first tubular type reactor reaction section Length be 5 meters～15 meters, the length of the second tubular type reactor reaction section is 5 meters～10 meters.

4. fluidized catalytic cracker according to claim 2, it is characterised in that also include distributor pipe of cardinal wind, the master Wind distributor pipe is respectively arranged at described first and rises bottom of the tube and the turbulent bed regenerator bottoms.

5. fluidized catalytic cracker according to claim 4, it is characterised in that also include main wind inlet tube, the master Wind inlet tube is arranged on the described second side wall for rising bottom of the tube.

6. fluidized catalytic cracker according to claim 5, it is characterised in that the quantity of the main wind inlet tube is even Number, the circumference along second tedge are uniformly and symmetrically distributed.

7. fluidized catalytic cracker according to claim 1, it is characterised in that also include multilayer heavy oil feed nozzle, Heavy oil feed nozzle described in multilayer is arranged on the side wall of first tubular reactor, along the axle of first tubular reactor To being spaced apart.

8. the fluidized catalytic cracker according to any one of claim 2～7, it is characterised in that the catalyst cooling Pipeline includes one-level regenerated catalyst cooler and secondary regenerator catalyst cooler；

The close phase section in the turbulent bed regenerator bottom passes sequentially through the one-level regenerated catalyst cooler and the secondary regenerator Catalyst cooler is connected with the second tubular type reactor lower part；And the one-level regenerated catalyst cooler space height position On the secondary regenerator catalyst cooler.

9. fluidized catalytic cracker according to claim 8, it is characterised in that also include low-temp recovery catalyst tank；

The secondary regenerator catalyst cooler is by the low-temp recovery catalyst tank and the second tubular type reactor lower part Connection, and the spatial altitude of the low-temp recovery catalyst tank is on the gas-solid separator.

10. fluidized catalytic cracker according to claim 9, it is characterised in that also include air delivery pipe is described low The top of warm regenerated catalyst tank is connected with the close phase section in the turbulent bed regenerator bottom by the air delivery pipe.