CN104056580A - Fixed fluidized bed reactor and application thereof - Google Patents
Fixed fluidized bed reactor and application thereof Download PDFInfo
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- CN104056580A CN104056580A CN201310085580.4A CN201310085580A CN104056580A CN 104056580 A CN104056580 A CN 104056580A CN 201310085580 A CN201310085580 A CN 201310085580A CN 104056580 A CN104056580 A CN 104056580A
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Abstract
The invention discloses a fixed fluidized bed reactor and an application thereof. The reactor comprises a top sealing structure and a reactor main body; an outlet pipe (8) and a material feeding pipe (1) are communicated with the reactor; the reactor main body comprises, from up to down, a settling section (I), a first reaction section (II-1), a second reaction section (II-2), and an oil agent initial contact section (III); the cross-sectional area of the lower end of the settling section (I) is equal to the cross-sectional area of the upper end of the first reaction section (II-1); the cross-sectional area of the lower end of the first reaction section (II-1) is equal to the cross-sectional area of the upper end of the second reaction section (II-2); the cross-sectional area of the lower end of the second reaction section (II-2) is equal to the cross-sectional area of the upper end of the oil agent initial contact section (III); the cross-sectional area of the first reaction section (II-1) increases gradually from up to down; and the cross-sectional area of the second reaction section (II-2) decreases gradually from up to down. When used in catalytic cracking of light oil such as naphtha and the like, the fixed fluidized bed reactor provided by the invention has the advantages of stable bed layer linear speed, complete oil agent contact, and the like, and is beneficial to product distribution improvement.
Description
Technical field
The present invention relates to a kind of fixed fluidized-bed reactor and application thereof.
Background technology
Catalytic pyrolysis is, under the condition existing at catalyst, petroleum hydrocarbon is carried out to cracking to produce the technology of low-carbon alkene, due to advantages such as raw material sources are wide, olefin product structure is easily adjusted, energy consumption is low and CO2 emission is few, in recent years, catalytic pyrolysis technology has obtained development faster.Especially for light-end products as naphtha catalytic cracking technology be to optimize to utilize naphtha resource, improve the important technology of refinery's economic benefit, around the process exploitation of this technology, the development of catalyst, or different material oil, screening of catalyst evaluation, all be unable to do without laboratory room small-sized evaluating apparatus.
At present, the experimental provision that is applied to catalytic pyrolysis mainly contains recirculating fluidized bed, fixed fluidized bed and fixed bed, fixed fluidized bed device because it is simple in structure, operating flexibility is good, bed isothermal, heat transfer efficiency advantages of higher be widely used in catalytic pyrolysis experimental study, and fixed fluidized-bed reactor is the nucleus equipment of the type experimental provision.
In prior art, the structure of conventional fixed fluidized-bed reactor as shown in Figure 1.This reactor is made up of the settling section of ring flange, column, cone shape conversion zone from top to bottom.In addition, be provided with the members such as feeding line, thermocouple sheath, reaction oil gas screen pipe at this inside reactor.As seen from Figure 1, feeding line, thermocouple sheath, screen pipe are all fixed on reactor head by ring flange, and its feeding line from top to down inserts in reactor along central axis, and its insertion depth is generally the more than 1/2 of reactor vertical height.The feature such as that although this reactor has is simple in structure, operating flexibility is good, but owing to being subject to the restriction of feeding manner, the actual preheat temperature of feedstock oil often departs from the desired preheat temperature of test, and close to inside reactor temperature, cause excessive thermal cracking that the output of dry gas and coke is increased.In addition, the atomizing effect of feedstock oil is also not ideal enough, and especially, in the time that in feedstock oil, more than 538 DEG C cut content is higher, the coke yield that test obtains is much larger than industrial production data, and the comparativity of test data will be affected.
US 6069012 discloses a kind of improved fixed fluidized-bed reactor, and its structure as shown in Figure 2.It is cylindric that the settling section of this reactor and conversion zone are all, and fixed fluidized-bed reactor can be by regulating feed nozzle height to realize the adjustment to the reaction time.In addition, reactor bottom is set up fluidizing gas nozzle to improve the fluidized state of catalyst.Owing to being subject to the restriction of bed linear speed, this reactor is only suitable for testing under conventional catalytic cracking reaction condition.
In addition, the patented technologies such as CN 2512495Y, CN 201042664Y, CN 202438304U are all on the basis of the conventional fixed fluidized-bed reactor configuration shown in Fig. 1, to have made part to improve, to adapt to different technique.For example, CN 201042664Y adopts similar feed system, adopts tapered reactor simultaneously, and has set up distribution grid, has improved to a certain extent the shortcoming of fluidisation Quality Down under high temperature high linear speed.
And for example, CN 201064712Y discloses a kind of fixed fluidized-bed reactor for experimental study, and its structure as shown in Figure 3.This reactor comprises the initial contact-segment III of settling section I, conversion zone II and finish from top to bottom, this reactor has mainly been done improvement to the configuration of settling section, described settling section is made up of round table-like settling section Ia and columned settling section Ib from top to bottom, can shorten reaction intermediate the coexisting the time of catalyst dilute phase section, effectively shorten the polycondensation reaction between small-numerator olefin.
In sum, the fixed fluidized-bed reactor of prior art is mainly for conventional catalytic cracking and the catalytic pyrolysis of mink cell focus, high owing to thering is reaction temperature as the catalytic cracking reaction of the light-end products such as naphtha, oil ratio is large, oil gas linear speed is high, the features such as fecund gas, and while adopting above-mentioned fixed fluidized-bed reactor to carry out catalytic pyrolysis, at pyroreaction condition lower bed layer inner catalyst skewness, finish contact is insufficient, distribute and can affect final product, thereby the fixed fluidized-bed reactor of prior art be not suitable for as high in the catalytic cracking reaction temperature of the light-end products such as naphtha, oil ratio is large, oil gas linear speed is high, the special reaction requirement such as fecund gas.
Summary of the invention
In order to address the above problem, the invention provides a kind of new fixed fluidized-bed reactor and application thereof.
To achieve these goals, the invention provides a kind of fixed fluidized-bed reactor, described fixed fluidized-bed reactor comprises the top seal structure and the reactor body that are tightly connected removably, the outlet 8 being communicated with this reactor and feed pipe 1, described reactor body comprises from top to bottom: settling section I, the initial contact-segment III of conversion zone II and finish, wherein, described conversion zone II comprises the first conversion zone II-1 and the second conversion zone II-2 from top to bottom, the cross-sectional area of settling section I lower end equates with the cross-sectional area of the first upper end, conversion zone II-1, the cross-sectional area of the first lower end, conversion zone II-1 equates with the cross-sectional area of the second upper end, conversion zone II-2, the cross-sectional area of the second lower end, conversion zone II-2 equates with the cross-sectional area of the initial contact-segment III of finish upper end, and the cross-sectional area of described the first conversion zone II-1 increases from top to bottom gradually, the cross-sectional area of the second conversion zone II-2 dwindles from top to bottom gradually.
The present invention also provides described fixed fluidized-bed reactor for light-end products, the particularly application in naphtha catalytic cracking.
Fixed fluidized-bed reactor provided by the invention is by improving the configuration of conversion zone II, make this reactor in the time of the catalytic cracking being applied to as light-end products such as naphthas, show the features such as bed linear speed is stable, finish contact is abundant, distribute and be conducive to improve product, improve the yield of target product.
Other features and advantages of the present invention are described in detail the detailed description of the invention part subsequently.
Brief description of the drawings
Accompanying drawing is to be used to provide a further understanding of the present invention, and forms a part for description, is used from explanation the present invention, but is not construed as limiting the invention with detailed description of the invention one below.In the accompanying drawings:
Fig. 1 is a kind of structural representation of conventional fixed fluidized-bed reactor;
Fig. 2 is the structural representation of US 6069012 disclosed a kind of fixed fluidized-bed reactors;
Fig. 3 is the structural representation of the disclosed a kind of fixed fluidized-bed reactor of CN 201064712Y;
Fig. 4 is the structural representation of the fixed fluidized-bed reactor of a kind of detailed description of the invention of the present invention.
Description of reference numerals
1-feed pipe; 2-distribution grid; 3-thermocouple temperature measurement pipe; 4-screen pipe; 5-lower flange;
6-sealing gasket; 7-screen pipe seal receptacle; 8-outlet; 9-upper flange plate; 10-bolt;
I-settling section; II-conversion zone (II-1 the first conversion zone, II-2 the second conversion zone);
The initial contact-segment of III-finish;
The round platform angle of α-the first conversion zone II-1;
The round platform angle of β-the second conversion zone II-2.
Detailed description of the invention
Below the specific embodiment of the present invention is elaborated.Should be understood that, detailed description of the invention described herein only, for description and interpretation the present invention, is not limited to the present invention.
In the present invention, in the situation that not doing contrary explanation, reactor head refers to the lower surface at the top in height for reactor direction, preferably refers to the lower surface of upper flange plate 5.The bottom of reactor refers to the initial contact-segment III of the finish rear surface in height for reactor direction.Percent opening refers to distribution grid 2(sieve tray) on the gross area of sieve aperture and the ratio of the area of sieve tray.
Top, bottom refer to top or the bottom in the short transverse of reactor, taking 1/2 place of height for reactor as benchmark, lower than this position be bottom, higher than this position is top.
According to the present invention, as shown in Figure 4, described fixed fluidized-bed reactor comprises the top seal structure and the reactor body that are tightly connected removably, the outlet 8 being communicated with this reactor and feed pipe 1, described reactor body comprises from top to bottom: settling section I, the initial contact-segment III of conversion zone II and finish, wherein, described conversion zone II comprises the first conversion zone II-1 and the second conversion zone II-2 from top to bottom, the cross-sectional area of settling section I lower end equates with the cross-sectional area of the first upper end, conversion zone II-1, the cross-sectional area of the first lower end, conversion zone II-1 equates with the cross-sectional area of the second upper end, conversion zone II-2, the cross-sectional area of the second lower end, conversion zone II-2 equates with the cross-sectional area of the initial contact-segment III of finish upper end, and the cross-sectional area of described the first conversion zone II-1 increases from top to bottom gradually, the cross-sectional area of the second conversion zone II-2 dwindles from top to bottom gradually.
Wherein, described " passing hermetically the top of reactor " refers to: thermocouple temperature measurement pipe 3 enters reactor from the top of reactor, and the tube wall of thermocouple temperature measurement pipe 3 and the sealing of reactor head junction, to prevent that the material in reactor from leaking out reactor from thermocouple temperature measurement pipe 3 and reactor head junction." passing hermetically " stated in following other places all can be with reference to this explanation.
The present invention is by improving the structure of conversion zone II, conversion zone II is designed to form (described conversion zone II comprises the first conversion zone II-1 and the second conversion zone II-2 from top to bottom) by two sections, be along the cross-sectional area of feedstock direction conversion zone II and first expand gradually then diminishing shape, thereby make described fixed bed reactors can be specially adapted to the light-end products particularly catalytic cracking reaction of naphtha of processing taking saturated hydrocarbons as chief component.Be mainly manifested in:
(1) the initial contact-segment of finish expanding contributes to form the catalyst fluidization bed of homogeneous, has reduced because oil gas linear speed is compared with driving catalyst to move upward greatly, in the formation of reactor bottom dilute-phase zone, has improved finish contact condition;
(2) first conversion zone II-1 undergauge design has from bottom to top reduced the ratio of the catalyst that is entrained to settling section, has reduced to a certain extent the generation of settling section reaction oil gas secondary response, has improved the selective of target product;
(3) preferably adopt the design of the truncated conical shape that cross-sectional diameter reduces gradually from bottom to top in the first conversion zone II-1, contribute to shorten the time of staying of reaction oil gas at settling section, improve the productive rate of target product; Overcome oil gas, particularly light-end products (naphtha) raw material is submitted sharply expansion to after entering reactor, the drawbacks such as In Oil-gas Line speed is large and influx the settling section of reactor on the catalyst emulsion zone that causes, and finish is not suitable for time of contact, catalyst sedimentation weak effect;
(4) cone angle of preferably optimizing the initial contact-segment III of finish and conversion zone II can be avoided after light-end products and catalyst haptoreaction, due to the problem of the volume bed linear speed excessively rapid growth that expansion brings rapidly, has maintained the stability of bed linear speed and operation.
(5) preferably the initial contact-segment III of finish and conversion zone II adopt the Integral design of equal angular can optimize the gas-solid fluidization quality of contact-segment III top and junction, conversion zone II bottom, prevent the appearance at this execution angle.
According to the present invention, between settling section I in fixed fluidized-bed reactor of the present invention and conversion zone II, there is dead angle, preferably, the cross-sectional area of settling section I lower end (settling section I bottom) is not less than the cross-sectional area at the first upper end, conversion zone II-1 (the first top, conversion zone II-1), and more preferably the cross-sectional area of settling section I lower end (settling section I bottom) equates with the cross-sectional area at the first upper end, conversion zone II-1 (the first top, conversion zone II-1); The cross-sectional area of the first lower end, conversion zone II-1 (the first bottom, conversion zone II-1) is not less than the cross-sectional area at the second upper end, conversion zone II-2 (the second top, conversion zone II-2), more preferably, the cross-sectional area of the first lower end, conversion zone II-1 (the first bottom, conversion zone II-1) equates with the cross-sectional area at the second upper end, conversion zone II-2 (the second top, conversion zone II-2); The cross-sectional area of the second lower end, conversion zone II-2 (the second bottom, conversion zone II-2) is not less than the cross-sectional area at the initial contact-segment III of finish upper end (the initial contact-segment III of finish top), more preferably, the cross-sectional area of the second lower end, conversion zone II-2 (the second bottom, conversion zone II-2) equates with the cross-sectional area at the initial contact-segment III of finish upper end (the initial contact-segment III of finish top), and catalyst can fluidisation and sedimentation well in fixed fluidized-bed reactor of the present invention thus.
In the present invention, the fixed fluidized-bed reactor that meets aforementioned requirement all can be realized object of the present invention, and for the present invention, preferably described the first conversion zone II-1 and the second conversion zone II-2 are truncated conical shape.
According to the present invention, in order further to strengthen catalyst being uniformly distributed and gas-solid fluidization quality in fixed fluidized-bed reactor of the present invention, under preferable case, the angle α of the first conversion zone II-1 of described truncated conical shape is not less than 15 °, is preferably not less than 26 °.The angle β of the second conversion zone II-2 of described truncated conical shape is no more than 30 °, is preferably no more than 18 °.In order further to reach the height that reduces settling section, control the object of excessive thermal cracking, minimizing coke and dry gas yied simultaneously, preferably, the angle α of described the first conversion zone II-1 is not less than the angle β of described the second conversion zone II-2.
In the present invention, the angle of described round platform refers to the angle between the line parallel with the central axis of round platform and the bus of round platform.
According to the present invention, realize better goal of the invention of the present invention in order to make catalyst being more evenly distributed in fixed fluidized-bed reactor of the present invention, further under preferable case, the height of the first conversion zone II-1 is 1:1-4, more preferably 1:1.5-2.5 with the diameter ratio of the cross section of this conversion zone upper end.The height of the second conversion zone II-2 is 1-3.5:1, more preferably 1.4-2:1 with the diameter ratio of the cross section of this conversion zone upper end.
According to the present invention, installation site to described feed pipe 1 on reactor is without particular/special requirement, goal of the invention of the present invention all can be realized in the various installation sites of prior art, for example can be arranged on fixed fluidized-bed reactor of the present invention top (as can be hermetically through as described in the top of reactor be communicated with reactor body), also can be arranged on the sidewall of described fixed fluidized-bed reactor.For the present invention, under preferable case, as shown in Figure 4, described feed pipe 1 is communicated with the bottom port of the initial contact-segment III of finish.Feed pipe 1 is designed and is being communicated with the bottom port of the initial contact-segment III of finish, adopt the mode of lower charging, oil gas directly enters reactor and contacts with catalyst after preheating, can control more exactly feeding temperature, reduced oil gas heat scission reaction at high temperature simultaneously, the content that has reduced dry gas and coke in product, improves product and distributes.
The present invention to described outlet 8 installation site on reactor without particular/special requirement, goal of the invention of the present invention all can be realized in the various installation sites of prior art, for example, can be arranged on the top (as be communicated with reactor body through the top of reactor body) of fixed fluidized-bed reactor of the present invention, also can be arranged on the sidewall of fixed fluidized-bed reactor of the present invention.For the present invention, in order effectively to suppress the polycondensation of small-numerator olefin under catalytic action, the height of reduction settling section, preferably, the top that described outlet 8 inserts settling section I through top cover flange 9 hermetically, the top that more preferably described outlet 8 vertically inserts settling section I through the top of reactor hermetically.
According to the present invention, preferred described outlet 8 has multiple, and multiple this outlet 8 is uniformly distributed on reactor body.
According to the present invention, preferably in one end that is at least positioned at reactor body of described outlet 8, screen pipe 4 is installed, so by screen pipe 4, catalyst is filtered down, and reaction oil gas continues to discharge outside fixed fluidized-bed reactor by outlet 8.Wherein, the installation of described screen pipe 4 and fixed form can adopt the method for well known to a person skilled in the art to carry out, according to a kind of detailed description of the invention of the present invention, as shown in Figure 4, described screen pipe 4 comprises the polycrystalline substance that is positioned at outlet 8 ends in reactor body and is arranged on the pipe portion structure on the outer circle wall of this section port pipe 8, and the pipe portion structure of part screen pipe 4 is upwards extended along the length direction of outlet 8, and higher than upper flange plate 9(, be exposed to the outside of described reactor body through the top of this reactor), more preferably, the pipe portion structure of the described part screen pipe 4 higher than upper flange plate 9 is sealed and is fixed on the top of reactor by screen pipe seal receptacle 7.In order to be applicable to the operating condition of naphtha catalytic cracking higher temperature, under preferable case, described screen pipe 4 selects that heat resistance is good, long service life, resistance to thermal shocks corundum material good, that be difficult for bursting are made.
According to the present invention, for assaying reaction temperature more exactly, described fixed fluidized-bed reactor also comprises thermocouple temperature measurement pipe 3, the present invention to described thermocouple temperature measurement pipe 3 installation site on reactor without particular/special requirement, goal of the invention of the present invention all can be realized in the various installation sites of prior art, for example, can insert in described conversion zone II through the top of reactor, for measuring the temperature in reactor.For the present invention, for the ease of installing and can monitoring better reaction temperature, described thermocouple temperature measurement pipe 3 vertically inserts in described reactor body through the top of described fixed fluidized-bed reactor hermetically, and extends to the bottom of the second conversion zone II-2 in described reactor body.Under preferable case, described thermocouple temperature measurement pipe 3 inserts in described reactor body along the central axis of described reactor.Insertion depth for described thermocouple temperature measurement pipe 3 in reactor body, for the conventional design of this type of reactor of this area, does not repeat them here.
According to the present invention, in order further to strengthen catalyst being uniformly distributed and fluidized state in fixed fluidized-bed reactor of the present invention, under preferable case, as shown in Figure 4, described fixed fluidized-bed reactor also comprises distribution grid 2, and this distribution grid 2 is fixed on the lower end of described thermocouple temperature measurement pipe 3.So fluidizing agent can by described fluidizing agent distribution grid 2 equably in reactor body with catalyst counter current contacting, thereby greatly strengthened the fluidized state of catalyst in fixed fluidized-bed reactor of the present invention.Further under preferable case, described distribution grid 2 is sieve tray, and perpendicular to the direction of the central axis of described fixed fluidized-bed reactor, perforate on described sieve tray is uniformly distributed, preferred described sieve tray is circular, the bore dia of described sieve tray is 0.3-0.9:1 with the ratio of the internal diameter of the reactor cross-section of its place height, and percent opening is 5-50%, and bore dia is 0.2-3mm.
According to the present invention, as shown in Figure 4, described top seal structure is flangeseal structure, and described flangeseal structure comprises upper flange plate 9 and lower flange 5, and described reactor head is upper flange plate 9.And by upper flange plate 9 and lower flange 5, the top of reactor and reactor body are sealed, and make to react the outlet 8 of rear oil gas for discharging, be all fixed on upper flange plate 9, also insert inside reactor through upper flange plate 9 hermetically for the thermocouple temperature measurement pipe 3 of thermometric.
According to the present invention, it is conventionally known to one of skill in the art adopting the mode of flangeseal, and the form of upper flange plate, lower flange and material all adopt the conventional design of this type of reactor of this area.Be directed to the present invention, adopt the device simple structure of flangeseal mode, and dismounting transformation is convenient.Well known to a person skilled in the art to be, can conventionally adopt the modes such as welding or bolt connection by fixing to upper flange plate 9 and lower flange 5, from making the top seal of reactor body.
According to a kind of detailed description of the invention of the present invention, under preferable case, as shown in Figure 4, for the ease of the structure of described fixed fluidized-bed reactor, described lower flange 5 is arranged on the open-topped perisporium of reactor body, described upper flange plate 9 covers the top at reactor body, and by bolt 10, upper flange plate 9 is connected with lower flange 5 bolts.In addition, under normal circumstances, tightr for what upper flange plate 9 was connected by bolt 10 with lower flange 5, and can play cushioning effect, between upper flange plate 9 and lower flange 5, be also provided with sealing gasket 6.
More preferably, seal better in order to be beneficial to reactor body, described lower flange 5 is integrated with reactor body.
Improvement of the present invention is mainly the structure of conversion zone II, therefore, for the structure (comprising shape (being preferably cylindrical shape), height etc.) of the settling section I of described fixed fluidized-bed reactor, the structure of the initial contact-segment III of finish all can adopt (comprising shape (being preferably inverted cone shape), height etc.) conventional design of this type of reactor of this area.For example, generally speaking, the settling section I of the conventional fixed fluidized-bed reactor of prior art is truncated conical shape or cylindrical shape, same settling section I of the present invention can be truncated conical shape or cylindric, the initial contact-segment III of finish can be truncated conical shape or inverted cone shape, specifically can select as required.
For the present invention, under preferable case, as shown in Figure 4, settling section I of the present invention is cylindric, the blade diameter length ratio of described settling section I is 1:1.5-2.5, more preferably 1:1.8-2.2, and the height of described settling section I is the 31-35% of reactor head apart from the vertical range of reactor bottom.Selection settling section is that cylindrical shape, the initial contact-segment of finish are that the advantage of inverted cone shape is: can shorten the time of staying of reaction intermediate in settling section I, suppress the polycondensation reaction of small-numerator olefin, initial contact-segment oil gas and the accuracy that catalyst mixes rapidly, good contact improves experimental result.
Under preferable case, for the present invention, as shown in Figure 4, the height of described conversion zone II is the 58-62% of reactor head apart from the vertical range of reactor bottom.
Under preferable case, for the present invention, as shown in Figure 4, the initial contact-segment III of described finish is inverted cone-shaped, and the height of the initial contact-segment III of described finish is the 3-11% of reactor head apart from the vertical range of reactor bottom.The present inventor finds, the cone angle that expands the initial contact-segment III of finish and conversion zone II can be avoided after light-end products and catalyst haptoreaction, due to the problem of the volume bed linear speed excessively rapid growth that expansion brings rapidly, maintain the stability of bed linear speed and operation, therefore, preferably, the cone angle of the initial contact-segment III of described finish is 20-45 °, more preferably 32-40 °; The height of described finish starting stage III is 1.21-2.25:1, more preferably 1.37-1.74:1 with the diameter ratio of the cross section of this finish starting stage III upper end.
Wherein, cone angle refers to the angle between two buses in cone axis cross section.
Below with reference to Fig. 4, the course of work of the fixed fluidized-bed reactor to a kind of preferred embodiment of the present invention is described in detail.
As one preferred embodiment, the structure of described fixed fluidized-bed reactor provided by the invention as shown in Figure 4, described fixed fluidized-bed reactor comprises the top seal structure and the reactor body that are tightly connected removably, described reactor body comprises from top to bottom: settling section I, the initial contact-segment III of conversion zone II and finish, described conversion zone II comprises the first conversion zone II-1 and the second conversion zone II-2 from top to bottom, the cross-sectional area of settling section I lower end equates with the cross-sectional area of the first upper end, conversion zone II-1, the cross-sectional area of the first lower end, conversion zone II-1 equates with the cross-sectional area of the second upper end, conversion zone II-2, the cross-sectional area of the second lower end, conversion zone II-2 equates with the cross-sectional area of the initial contact-segment III of finish upper end, and the first conversion zone II-1 and the second conversion zone II-2 are truncated conical shape.The angle α of the first conversion zone II-1 of described truncated conical shape is not less than 15 °, and the angle β of the second conversion zone II-2 of described truncated conical shape is no more than 30 °, and the angle α of described the first conversion zone II-1 is greater than the angle β of described the second conversion zone II-2.Settling section I is cylindrical shape, and the initial contact-segment III of finish is inverted cone shape.
The top seal structure of described reactor is flangeseal structure, and described flangeseal structure comprises upper flange plate 9 and lower flange 5, and described reactor head is upper flange plate 9.Described lower flange 5 is arranged on the open-topped perisporium of reactor body, described upper flange plate 9 covers the top at reactor body, and by bolt 10, upper flange plate 9 is connected with lower flange 5 bolts, and be provided with sealing gasket 6 between upper flange plate 9 and lower flange 5.Described reactor also comprises thermocouple temperature measurement pipe 3, outlet 8 and screen pipe 4, wherein, described thermocouple temperature measurement pipe 3 through the top of described fixed fluidized-bed reactor (hermetically, upper flange plate 9) vertical insertion in (along the direction of central axis) described reactor body, and extend to the bottom of the second conversion zone II-2 in described reactor body.Described fixed fluidized-bed reactor also comprises distribution grid 2, and this distribution grid 2 is fixed on the lower end (perpendicular to the direction of the central axis of described fixed fluidized-bed reactor) of described thermocouple temperature measurement pipe 3.Three tops that outlet 8 vertically inserts settling section I through the top (, upper flange plate 9) of described fixed fluidized-bed reactor hermetically, are communicated with this reactor.The one end that is positioned at reactor body at described outlet 8 is separately installed with three screen pipes 4, three screen pipes 4 comprise respectively the polycrystalline substance that is positioned at outlet 8 ends in reactor body and are arranged on the pipe portion structure on the outer circle wall of this section port pipe 8, and the pipe portion structure of part screen pipe 4 is upwards extended along the length direction of outlet 8, and higher than upper flange plate 9(, be exposed to the outside of described reactor body through the top of this reactor), the pipe portion structure of the described part screen pipe 4 higher than upper flange plate 9 is sealed and is fixed on the top of reactor by screen pipe seal receptacle 7.Feed pipe 1 is communicated with the bottom port of the initial contact-segment III of finish.
Catalyst is through feed pipe 1, under the effect of negative pressure, introduce in this fixed fluidized-bed reactor, fluidizing agent (can be one or more the gaseous mixture that is selected from air, steam, nitrogen or helium) also enters reactor by feed pipe 1, in order to the catalyst in fluidized reactor.Hydrocarbon oil crude material after preheating injects the beds that reaches assigned temperature through feed pipe 1, contact, and carry out catalytic cracking reaction with catalyst under the operating condition of specifying.
In order to improve the flow regime of catalyst, the mixture of fluidizing gas and catalyst is adjusted its flow direction and speed through distribution grid 2, to form uniform catalyst dense-phase bed in conversion zone.In raw material oil gas motion process from bottom to top, through conversion zone II-1, gas line speed further reduces, and fully mixes with catalyst, forms mixed uniformly emulsion zone, to ensure raw material oil gas catalytic cracking reaction required time of contact; Catalyst granules forms back-mixing under the effect of conversion zone II-2, being conducive to gas-solid evenly mixes, partially catalyzed agent is carried secretly to settling section, along with the reduction of fluidizing gas linear speed, wherein most of catalyst granules returns in conversion zone II, and fluidizing gas is discharged through outlet 8 after filter 4 filters, the air-flow of discharge is collected, is measured through subsequent product recovery system.
Reacted catalyst can for example, carry out stripping with stripping medium (steam, nitrogen or helium), and stripping medium and the reaction oil gas proposing that rises are also discharged through outlet 8 after screen pipe 4 filters.Afterwards, the mist of being introduced oxygen, air and being contained oxygen by feed pipe 1 carries out catalyst coke burning regeneration and operates.After catalyst coke burning regeneration finishes, the reaction of above-mentioned steps capable of circulation.
The invention will be described in further detail by the following examples.
Embodiment 1
The present embodiment is used for illustrating fixed fluidized-bed reactor provided by the invention and application thereof.
Prepare fixed fluidized-bed reactor according to the reactor configuration shown in Fig. 4, described conversion zone II comprises the first conversion zone II-1 and the second conversion zone II-2 from top to bottom, the cross-sectional area of settling section I lower end equates with the cross-sectional area of the first upper end, conversion zone II-1, the cross-sectional area of the first lower end, conversion zone II-1 equates with the cross-sectional area of the second upper end, conversion zone II-2, the cross-sectional area of the second lower end, conversion zone II-2 equates with the cross-sectional area of the initial contact-segment III of finish upper end, and the cross-sectional area of described the first conversion zone II-1 increases from top to bottom gradually, the cross-sectional area of the second conversion zone II-2 all dwindles from top to bottom gradually.
Described the first conversion zone II-1 and the second conversion zone II-2 are truncated conical shape, and wherein, the angle α of the first conversion zone II-1 of described truncated conical shape is 26 °; The angle β of the second conversion zone II-2 of described truncated conical shape is 14 °; And the angle α of described the first conversion zone II-1 is greater than the angle β of described the second conversion zone II-2.The height of the first conversion zone II-1 is 1:1.5 with the diameter ratio of the cross section of this conversion zone upper end; The height of the second conversion zone II-2 is 1.7:1 with the diameter ratio of the cross section of this conversion zone upper end.
Described settling section I is cylindrical shape, the blade diameter length ratio of described settling section I is 1:1.8, the initial contact-segment III of described finish is inverted cone shape, the cone angle of the initial contact-segment III of described finish is 40 °, and the height of described finish starting stage III is 1.5:1 with the diameter ratio of the cross section of this finish starting stage III upper end.The height of described settling section I is reactor head apart from 31% of the vertical range of reactor bottom; The height of described conversion zone II is reactor head apart from 58% of the vertical range of reactor bottom; The height of the initial contact-segment III of described finish is reactor head apart from 11% of the vertical range of reactor bottom.
Described feed pipe 1 is communicated with the bottom port of the initial contact-segment III of finish.
Described thermocouple temperature measurement pipe 3 through the top of described fixed fluidized-bed reactor (hermetically, upper flange plate 9) vertical insertion in (along the central axial direction of described reactor) described reactor body, and extend to the bottom of the 3rd conversion zone II-3 in described reactor body; Described fixed fluidized-bed reactor also comprises distribution grid 2, this distribution grid 2 is fixed on the lower end of described thermocouple temperature measurement pipe 3, described distribution grid 2 is circular sieve tray, and perpendicular to the central axis of described fixed fluidized-bed reactor, the diameter of described sieve tray is 0.3:1 with the ratio of the internal diameter of the reactor cross-section of its place height, percent opening is 5%, and bore dia is 0.2mm.
Three tops that outlet 8 vertically inserts settling section I through the top (, upper flange plate 9) of described fixed fluidized-bed reactor hermetically, are communicated with this reactor.The one end that is positioned at reactor body at described outlet 8 is separately installed with three screen pipes 4, three screen pipes 4 comprise respectively the polycrystalline substance that is positioned at outlet 8 ends in reactor body and are arranged on the pipe portion structure on the outer circle wall of this section port pipe 8, and the pipe portion structure of part screen pipe 4 is upwards extended along the length direction of outlet 8, and higher than upper flange plate 9(, be exposed to the outside of described reactor body through the top of this reactor), the pipe portion structure of the described part screen pipe 4 higher than upper flange plate 9 is sealed and is fixed on the top of reactor by screen pipe seal receptacle 7.
Fixed fluidized-bed reactor described in employing the present embodiment, and test with reference to the experimental technique of small fixed flowing bed device (FFB).
Raw material adopts straight-run naphtha, and feedstock property is as shown in table 1; Catalyst adopts catalytic cracking catalyst, and trade names are CEP-1, and catalyst property is as shown in table 2.
Feed naphtha, after preheating, is injected in the above-mentioned fixed fluidized-bed reactor that CEP-1 catalyst is housed by feed pump, makes reactor carry out under the conditions shown in Table 3 catalytic cracking reaction.Gaseous product is analyzed its composition by on-line chromatograph, and product liquid is carried out simulation distil and analyzed by off-line chromatograph, has deposited the catalyst of coke through on-line decoking, passes through CO
2in-line analyzer is measured CO in flue gas
2content, draw coke output, analysis result is as shown in table 3.
Comparative example 1
It is consersion unit that this comparative example adopts the conventional small fixed flowing bed device (FFB) using in laboratory.
Feed naphtha, after preheating, is injected into by feed pump in the described fixed fluidized-bed reactor of the laboratory routine that CEP-1 catalyst is housed, and makes reactor carry out under the conditions shown in Table 3 catalytic cracking reaction.Gaseous product is analyzed its composition by on-line chromatograph, and product liquid is carried out simulation distil and analyzed by off-line chromatograph, has deposited the catalyst of coke through on-line decoking, passes through CO
2in-line analyzer is measured CO in flue gas
2content, draw coke output, analysis result is as shown in table 3.
Table 1
Table 2
Table 3
From the result of upper table 3, under identical operating condition, carry out the catalytic cracking reaction of feed naphtha, the product of embodiment 1 distributes significantly better than comparative example 1, be in particular in: the dry gas of embodiment 1 and the output of coke are starkly lower than comparative example 1, the fall of dry gas is 40.8%, and the fall of coke is 68.2%.The diene yield of embodiment 1 is 32.13%, has improved 8.27 percentage points with respect to comparative example 1, and wherein propylene increases significantly.
Embodiment 2
The present embodiment is used for illustrating fixed fluidized-bed reactor provided by the invention and application thereof.
According to the method for embodiment 1, fixed fluidized-bed reactor described in employing the present embodiment, the straight-run naphtha as shown in table 1 to feedstock property carries out catalytic cracking reaction under the effect of catalyst property catalyst as shown in table 2, and product is analyzed, operating condition and product analysis result are as shown in table 4.
Difference is, each section of dimensional parameters difference of this embodiment fixed fluidized-bed reactor used, fixed fluidized-bed reactor the first conversion zone II-1 and the second conversion zone II-2 that this embodiment adopts are truncated conical shape, wherein, the angle α of the first conversion zone II-1 of described truncated conical shape is 41 °; The angle β of the second conversion zone II-2 of described truncated conical shape is 18 °; And the angle α of described the first conversion zone II-1 is greater than the angle β of described the second conversion zone II-2.The height of the first conversion zone II-1 is 1:2.5 with the diameter ratio of the cross section of this conversion zone upper end; The height of the second conversion zone II-2 is 1.8:1 with the diameter ratio of the cross section of this conversion zone upper end.
Described settling section I is cylindrical shape, the blade diameter length ratio of described settling section I is 1:2.2, the initial contact-segment III of described finish is inverted cone shape, the cone angle of the initial contact-segment III of described finish is 32 °, and the height of described finish starting stage III is 1.86:1 with the diameter ratio of the cross section of this finish starting stage III upper end.The height of described settling section I is reactor head apart from 35% of the vertical range of reactor bottom; The height of conversion zone II is reactor head apart from 62% of the vertical range of reactor bottom; The height of the initial contact-segment III of described finish is reactor head apart from 3% of the vertical range of reactor bottom.
Described feed pipe 1 is communicated with the bottom port of the initial contact-segment III of finish.
Described thermocouple temperature measurement pipe 3 through the top of described fixed fluidized-bed reactor (hermetically, upper flange plate 9) vertical insertion in (along the central axial direction of described reactor) described reactor body, and extend to the bottom of the 3rd conversion zone II-3 in described reactor body; Described fixed fluidized-bed reactor also comprises distribution grid 2, this distribution grid 2 is fixed on the lower end of described thermocouple temperature measurement pipe 3, described distribution grid 2 is circular sieve tray, and perpendicular to the central axis of described fixed fluidized-bed reactor, the bore dia of described sieve tray is 0.9:1 with the ratio of the internal diameter of the reactor cross-section of its place height, percent opening is 50%, and bore dia is 3mm.
Comparative example 2
It is consersion unit that this comparative example adopts the conventional small fixed flowing bed device (FFB) using in laboratory.
Feed naphtha, after preheating, is injected into by feed pump in the described fixed fluidized-bed reactor of the laboratory routine that CEP-1 catalyst is housed, and makes reactor carry out under the conditions shown in Table 3 the catalytic cracking reaction of feed naphtha.Gaseous product is analyzed its composition by on-line chromatograph, and product liquid is carried out simulation distil and analyzed by off-line chromatograph, has deposited the catalyst of coke through on-line decoking, passes through CO
2in-line analyzer is measured CO in flue gas
2content, draw coke output, analysis result is as shown in table 4.
Table 4
From the result of upper table 4, under identical operating condition, carry out the catalytic cracking reaction of feed naphtha, the product of embodiment 2 distributes significantly better than comparative example 2, be in particular in: the dry gas of embodiment 2 and the output of coke are starkly lower than comparative example 2, the fall of dry gas is 41.2%, and the fall of coke is 58.2%.The diene yield of embodiment 2 is 29.13%, has improved 9.54 percentage points with respect to comparative example 2, and wherein propylene increases significantly.
Embodiment 3
The present embodiment is used for illustrating fixed fluidized-bed reactor provided by the invention and application thereof.
According to the method for embodiment 1, fixed fluidized-bed reactor described in employing embodiment 1 carries out catalytic cracking reaction to feedstock property straight-run naphtha as shown in table 1 under the effect of catalyst property catalyst as shown in table 2, difference is, only change cone angle and the ratio of height to diameter of the initial contact-segment III of finish, the cone angle of described finish contact-segment III is 30 °, the ratio of height to diameter of the initial contact-segment III of finish is 1.87:1, and product is analyzed, operating condition and product analysis result are as shown in table 5.
Table 5
From the result of upper table 5, in other conditions all under immovable condition, only regulate the cone angle of the initial contact-segment III of finish, after the cone angle of the initial contact-segment III of finish being carried out preferably and limiting its ratio of height to diameter, embodiment 1 is with respect to embodiment 3, dry gas and coke yield obviously decline, and diene yield has improved 7.31 percentage points.
As can be seen here, adopt and of the present invention the configuration of conversion zone is carried out to improved fixed fluidized-bed reactor, by changing contacting and the raising change heat and mass transport effect that flows and control catalyst and the time of contact of raw material oil gas, catalyst and product, change control feeding temperature by feeding manner, pass through fluidization quality of finish in reactor and catalyst, therefore can be good at improving product distribution.And these advantages are cannot realize in conventional fixed fluidized-bed reactor.
More than describe the preferred embodiment of the present invention in detail; but the present invention is not limited to the detail in above-mentioned embodiment, within the scope of technical conceive of the present invention; can carry out multiple simple variant to technical scheme of the present invention, these simple variant all belong to protection scope of the present invention.
It should be noted that in addition, each concrete technical characterictic described in above-mentioned detailed description of the invention, in reconcilable situation, can combine by any suitable mode, for fear of unnecessary repetition, the present invention is to the explanation no longer separately of various possible combinations.
In addition, between various embodiment of the present invention, also can be combined, as long as it is without prejudice to thought of the present invention, it should be considered as content disclosed in this invention equally.
Claims (19)
1. a fixed fluidized-bed reactor, described fixed fluidized-bed reactor comprises the top seal structure and the reactor body that are tightly connected removably, the outlet (8) being communicated with this reactor and feed pipe (1), described reactor body comprises from top to bottom: settling section (I), conversion zone (II) and the initial contact-segment of finish (III), it is characterized in that, described conversion zone (II) comprises the first conversion zone (II-1) and the second conversion zone (II-2) from top to bottom, the cross-sectional area of settling section (I) lower end equates with the cross-sectional area of the first conversion zone (II-1) upper end, the cross-sectional area of the first conversion zone (II-1) lower end equates with the cross-sectional area of the second conversion zone (II-2) upper end, the cross-sectional area of the second conversion zone (II-2) lower end equates with the cross-sectional area of the initial contact-segment of finish (III) upper end, and the cross-sectional area of described the first conversion zone (II-1) increases from top to bottom gradually, the cross-sectional area of the second conversion zone (II-2) dwindles from top to bottom gradually.
2. fixed fluidized-bed reactor according to claim 1, wherein, described the first conversion zone (II-1) and the second conversion zone (II-2) are truncated conical shape.
3. reactor according to claim 2, wherein, the angle (α) of first conversion zone (II-1) of described truncated conical shape is not less than 15 °, is preferably not less than 26 °.
4. reactor according to claim 2, wherein, the angle (β) of second conversion zone (II-2) of described truncated conical shape is no more than 30 °, is preferably no more than 18 °.
5. according to the reactor described in claim 3 or 4, wherein, the angle (α) of described the first conversion zone (II-1) is not less than the angle (β) of described the second conversion zone (II-2).
6. according to the reactor described in claim 2 or 3, wherein, the height of the first conversion zone (II-1) than for 1:1-4, is preferably 1:1.5-2.5 with the diameter of the cross section of this conversion zone upper end.
7. according to the reactor described in claim 2 or 4, wherein, the height of the second conversion zone (II-2) than for 1-3.5:1, is preferably 1.4-2:1 with the diameter of the cross section of this conversion zone upper end.
8. reactor according to claim 1, wherein, the initial contact-segment of described finish (III) is inverted cone shape, the cone angle of the initial contact-segment of described finish (III) is 20-45 °, is preferably 32-40 °; The diameter of the cross section of the height of described finish starting stage (III) and this finish starting stage (III) upper end, than for 1.21-2.25:1, is preferably 1.37-1.74:1.
9. according to the reactor described in claim 1 or 8, wherein, described feed pipe (1) is communicated with the bottom port of the initial contact-segment of finish (III).
10. according to the reactor described in any one in claim 1-9, wherein, described fixed fluidized-bed reactor also comprises thermocouple temperature measurement pipe (3), described thermocouple temperature measurement pipe (3) vertically inserts in described reactor body through the top of described fixed fluidized-bed reactor hermetically, and extends to the bottom of the second conversion zone (II-2) in described reactor body; Described fixed fluidized-bed reactor also comprises distribution grid (2), and this distribution grid (2) is fixed on the lower end of described thermocouple temperature measurement pipe (3).
11. reactors according to claim 10, wherein, described distribution grid (2) is sieve tray, and perpendicular to the central axis of described fixed fluidized-bed reactor, the diameter of described sieve tray is 0.3-0.9:1 with the ratio of the internal diameter of the reactor cross-section of its place height, percent opening is 5-50%, and bore dia is 0.2-3mm.
12. reactors according to claim 10, wherein, described thermocouple temperature measurement pipe (3) inserts in described reactor body along the central axis of described reactor.
13. reactors according to claim 1, wherein, described outlet (8) inserts the top of settling section (I) hermetically through the top of reactor.
14. reactors according to claim 13, wherein, described outlet (8) has multiple, and multiple this outlet (8) is uniformly distributed.
15. according to the reactor described in claim 1,13 or 14, and wherein, the one end that is at least positioned at reactor body at described outlet (8) is provided with screen pipe (4).
16. reactors according to claim 1, wherein, described top seal structure is flangeseal structure, described flangeseal structure comprises upper flange plate (9) and lower flange (5), and described reactor head is upper flange plate (9).
17. reactors according to claim 16, wherein, described lower flange (5) is arranged on the open-topped perisporium of reactor body, described upper flange plate (9) covers the top at reactor body, and by bolt (10), upper flange plate (9) is connected with lower flange (5) bolt, and be provided with sealing gasket (6) between upper flange plate (9) and lower flange (5).
18. reactors according to claim 17, wherein, described lower flange (5) is integrated with reactor body.
Fixed fluidized-bed reactor in 19. claim 1-18 described in any one, for light-end products, is preferably the application in naphtha catalytic cracking.
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