CN105368488B - Hydro carbons continuous reforming process - Google Patents
Hydro carbons continuous reforming process Download PDFInfo
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- CN105368488B CN105368488B CN201410414872.2A CN201410414872A CN105368488B CN 105368488 B CN105368488 B CN 105368488B CN 201410414872 A CN201410414872 A CN 201410414872A CN 105368488 B CN105368488 B CN 105368488B
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Abstract
The invention discloses a kind of hydro carbons continuous reforming process, it is characterised in that：The technique includes：Two reforming reactor groups and a regenerator are set, wherein, the first reforming reactor group includes two reforming reactors, and the second reforming reactor group only includes a reforming reactor；Wherein, reaction feed is that series connection is carried out relative to the conveying of each reactor in each reforming reactor group；And the circulation conveying between conveying and reactor group and regenerator of the catalyst between each reactor group is progress in parallel, but conveying of the catalyst in the first reforming reactor group is that series connection is carried out.In the present invention, all reactor groups can use fresh high activated catalyst and carry out on demand separately adjustable and change catalyst flow, can give full play to the activity of catalyst, improve the utilization rate of catalyst, improve reforming conversion and product yield.
Description
Technical field
The present invention relates to a kind of hydro carbons continuous reforming process.
Background technology
CONTINUOUS REFORMER is a kind of oil secondary operation technology, the raw material of processing be mainly the straight-run naphtha of low octane rating,
Hydrotreated naphtha etc., using platinum Pt- tin Sn bimetallic catalysts, at a high temperature of 500 DEG C or so, reset molecule, it is different
Structure, increase the yield of aromatic hydrocarbons, improve the technology of octane number.
Moving-burden bed reactor continuous regenerative reforming, abbreviation CONTINUOUS REFORMER.Commercial Application in the world is main at present
Three CONTINUOUS REFORMER patented technology providers are Uop Inc. of the U.S., French Axens and Chinese SEI respectively.Filled in CONTINUOUS REFORMER
Put, catalyst continuously flows successively through three (or four) moving-burden bed reactors of series connection, from the outflow of last reactor
Reclaimable catalyst carbon content is generally 2%-8% (mass fraction), and reclaimable catalyst is transported to regeneration by gravity or gas lift
Regenerated in device.Regenerated catalyst after activity recovery returns to first reactor and reacted again, catalyst shape in system
Into a closed cycle.
By reaction feed and catalyst transport model split, existing industrialized continuous reforming process can be divided into
" following current " and " adverse current " two kinds of patterns.
The reaction mass of " following current " continuous reforming process flows to most end reactor from first reactor successively, in each reactor
In catalyst on reacted.Moving direction of the catalyst between each reactor is consistent with reaction mass, that is, is regenerated
High activated catalyst be introduced into the first reforming reactor by the order of reaction stream, then pass sequentially through the second reforming reaction
Device, tri-reforming device are gradually reduced, from most until most end reforming reactor from first reactor to most end reactor pressure
The catalyst activity that last reactor comes out is relatively low, is sent in regenerator and is regenerated, and the catalyst after regeneration is lifted to the again
One reactor completes the circulation of catalyst.The technical process catalyst of this CONTINUOUS REFORMER is used in series in the reactor,
Catalyst into the first reforming reactor is the catalyst of " fresh " high activity just regenerated, and reactor below
All it is the above reactor relatively low catalyst of used activity.This process is schematically as follows：
The reaction that this catalyst circulation conveying mode makes it easy to carry out is in the reaction for having high activated catalyst above
Carried out in device, and the difficult reaction carried out having below is carried out in the reactor of low activity catalyst, catalyst reactor
The reaction complexity that activated state is carried out with it does not match that.The circulation arrangement of this catalyst is irrational.Such as accompanying drawing 1
It is shown.
The reaction mass of " adverse current " continuous reforming process flows to most end reactor from first reactor successively, and catalyst exists
Moving direction between each reactor is, that is, the order of the high activated catalyst back reaction logistics that regenerated opposite with reaction mass
Rearmost reactor is introduced into, then the direction of back reaction logistics is successively forward until first reactor, then anti-from first
Answer device to be sent in regenerator to be regenerated, the catalyst after regeneration lifts a last reactor and completes following for catalyst again
Ring.This process is schematically as follows：
The technical process of this adverse current CONTINUOUS REFORMER causes reaction of the difficult reaction carried out in high activated catalyst below
Carried out in device, reaction easy to perform is carried out in the reactor of low activity catalyst above.The circulation peace of this catalyst
It is more reasonable that row conveys compared to following current, and the activated state of catalyst reactor matches compared with its reaction carried out complexity.
As shown in Figure 2.
But either " following current " still " adverse current " CONTINUOUS REFORMER, circulation conveying of the catalyst between reactor are all adopted
With the mode of series connection, the catalyst that this mode of movement is only transported to first reactor from regenerator is only what is just regenerated
The high catalyst of " fresh " activity, such as first reforming reactor of " following current " CONTINUOUS REFORMER, " adverse current " CONTINUOUS REFORMER it is last
One reforming reactor, and the catalyst in other reforming reactors is all that above reactor is used containing carbon deposition activity
Decreased catalyst, catalyst convey in the backward, and its activity is lower, active minimum in the reactor that catalyst leaves.
The activity of catalyst can not give full play in all reactors as can be seen here.The mode of this catalyst cascade conveying, passes through
The catalyst internal circulating load of each reactor is all identical, all catalyst in each reactor must circular regeneration simultaneously, each
The catalyst flow of reactor can not on demand be carried out separately adjustable and changed, and can not individually carry out circular regeneration.
The U of CN 203513593, which disclose a kind of regeneration CONTINUOUS REFORMER system, the system side by side, includes catalyst reformer
(relative to regenerator) and charging/effluent exchanger, heating furnace and the reactor being sequentially connected, catalyst reformer are provided with
For adjusting the regulating valve of catalyst circulation rate.Although the system because equipped with the regulating valve can according to response situation and
Catalyst coking situation adjusts catalyst circulation rate, but with regard to being still foregoing " suitable from the point of view of reaction feed and the flow direction of catalyst
The form of stream " continuous reforming process, the foregoing problems of " following current " continuous reforming process are not overcome.
The content of the invention
It is an object of the invention to provide a kind of hydro carbons continuous reforming process, each reactor group is used fresh high living
Property regenerated catalyst, and can be as needed independently adjusted and change the catalyst recycle stream in each group of reactor
Amount, to give full play to the activity of catalyst, improves the utilization rate of catalyst, there is provided the operability of device, improves reforming
Rate and product yield.
To achieve these goals, the present invention provides a kind of hydro carbons continuous reforming process, it is characterised in that：The technique bag
Include：At least two reforming reactor groups and at least one catalyst regenerator are set, wherein at least one reforming reactor group
Reactor quantity is at least two, and the reactor quantity of other reactor groups is at least one；Reaction feed is relative to each heavy
The conveying of each reactor in whole reactor group is that series connection is carried out, i.e., reaction feed passes sequentially through each reforming reactor group
In each reactor and reacted with catalyst therein；And catalyst is between each reactor group and reactor
Circulation conveying between group and regenerator is progress in parallel, but catalyst is between each reactor inside each reactor group
Conveying be series connection carry out.
Preferably, the hydro carbons continuous reforming process, wherein, the technique includes：Two reforming reactor groups and one are set
Individual regenerator (12), wherein two reactors that the first reforming reactor group includes being arranged in series are i.e. positioned at the first of charging front end
Reforming reactor (3) and the second reforming reactor (5) positioned at charging rear end, the second reforming reactor group include a reactor
That is tri-reforming device (7).
Preferably, the hydro carbons continuous reforming process, wherein, the technique also includes setting being located at the first reforming reactor
(3) the one of top anti-top hopper (8), the three anti-top hoppers (9) positioned at tri-reforming device (7) top, regeneration catalyzing
Agent reprocessing and distribution system RCTS (10), reclaimable catalyst reprocessing and distribution system WCTS (11), reclaimable catalyst lifting
Blower fan (13) and regenerated catalyst lifting blower fan (14)；Reaction feed is reformed by the first reforming reactor (3), second successively
Reactor (5) and tri-reforming device (7), the reaction product and reaction feed for leaving tri-reforming device (7) are being reacted
Exchanged heat in charging/product exchanger (1), then arrive follow-up separator again and separated；Regenerated catalyst regeneration catalyzing
Agent lifting blower fan (14) is promoted to RCTS (10) from regenerator (12)；RCTS (10) by 2 tremie pipes respectively with an anti-top
Hopper (8) and three anti-top hoppers (9) are connected, and an anti-top hopper (8) passes through tremie pipe and the first reforming reactor (3) phase
Connection, three anti-top hoppers (9) are connected by tremie pipe and tri-reforming device (7)；With reclaimable catalyst lifting blower fan (13)
The reclaimable catalyst in the second reforming reactor (5) and tri-reforming device (7) is promoted to WCTS (11) respectively；WCTS
(11) it is connected by 1 tremie pipe and regenerator (12).
Preferably, the hydro carbons continuous reforming process, wherein, the first reforming reactor 3 and the second reforming reactor 5 are upper
Lower series connection overlaps, and the first reforming reactor 3 is located at the top of the second reforming reactor 5, the beds of two reactors
Between there are more diplegs to be connected, the catalyst in the first reforming reactor 3 can lean on gravity through dipleg enter second reform it is anti-
Answer device 5.
Preferably, the hydro carbons continuous reforming process, wherein, regenerated catalyst is promoted to RCTS10 from regenerator 12 and carried out
Dust elutriation, reduction and redistribution process, then it is respectively delivered in a manner of parallel side-by-side from RCTS10 by 2 tremie pipes
In first reforming reactor 3 and tri-reforming device 7, the catalyst in the first reforming reactor 3 enters second by gravity again
In reforming reactor 5；It is only from RCTS10 to the conveying capacity of the regenerated catalyst of each reforming reactor group and/or conveying opportunity
It is vertical controllable.
Preferably, the hydro carbons continuous reforming process, wherein, in the second reforming reactor 5 and tri-reforming device 7
Reclaimable catalyst in a manner of parallel side-by-side it is elevated be delivered in WCTS11 mixed, dust elutriation and locking become press through
Journey, regenerator 12 is then transported to by tremie pipe and regenerated；Urged from each reforming reactor group to the to be generated of WCTS11
The lifting conveying capacity of agent and/or conveying opportunity are all individually controllable.
Preferably, the hydro carbons continuous reforming process, wherein, RCTS10 operating pressure is less than the operation pressure of regenerator 12
Power, so as to which regenerated catalyst is lifted to RCTS10 from regenerator 12；The position of RCTS10 bottoms is higher than an anti-top material
The position on the top of 8 and three anti-top hopper 9 of bucket, and RCTS10 operating pressure is higher than the operation of the first reforming reactor 3
Pressure, so that regenerated catalyst can be flowed into all reactors from RCTS10.
Preferably, the hydro carbons continuous reforming process, wherein, the position of WCTS11 bottoms is higher than the position on the top of regenerator 12
Put, it is two pressure areas that WCTS11, which is divided to, and the upper zone before transformation is low-pressure area, and pressure is less than tri-reforming device 7, can
So that reclaimable catalyst is lifted to the low-pressure area from the second reforming reactor 5 and tri-reforming device 7；Under after the transformation
Area of portion is higher-pressure region, and pressure is higher than regenerator 12, and reclaimable catalyst can be flowed into regenerator 12 from the higher-pressure region.
The present invention is existing to overcome by changing circulation conveying mode of the catalyst between multiple moving-burden bed reactor groups
The shortcomings that each catalyst reactor activity can not give full play in industrialized technology, multiple reforming reactor groups in parallel
In catalyst can carry out cyclic regeneration simultaneously.Between reaction and regenerative system, by the way of parallel connection conveys catalyst,
So that the catalyst into each group of reactor is all high activity " fresh " catalyst for just having regenerated；Reclaimable catalyst is from each
Individually regenerative system is arrived in lifting in parallel to reactor group so that can to the catalyst of regenerator lifting conveying capacity from each reactor group
To be adjusted and change as needed, circulation conveying and the regeneration of catalyst can be neatly carried out, so as to optimize reaction
And regeneration condition, all reactors is used fresh high activated catalyst and is carried out on demand separately adjustable and change catalysis
Agent flux, carbon deposit on catalyst is reduced, to give full play to the activity of catalyst, improve the utilization rate of catalyst, extend catalyst
Life-span, reduce the inlet temperature of each reactor, the side reaction for reducing CONTINUOUS REFORMER occurs, and improves reforming conversion and product
Yield, increasing gasoline yield and hydrogen, increase the benefit.Because the reformation of the mainly cycloalkane dehydrogenation carried out in the first reforming reactor
Course of reaction, reaction are easier to carry out, and the amount of coke generated on a catalyst during the course of the reaction is less, and activity reduction is less,
Second reactor recycling can be directly entered, so as to reduce the number of catalyst lifting.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Accompanying drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is existing downflow type hydro carbons continuous reforming process schematic flow sheet
Fig. 2 is existing reverse-flow hydro carbons continuous reforming process schematic flow sheet
Fig. 3 is the hydro carbons continuous reforming process schematic flow sheet according to the present invention
Description of reference numerals
The reaction heating furnace of 101 reaction feeds/product exchanger 102 first
The reaction heating furnace of 103 first reforming reactors (one is anti-) 104 second
The reaction heating furnace of 105 second reforming reactors (two is anti-) 106 the 3rd
The reaction heating furnace of 107 tri-reforming devices (three is anti-) 108 the 4th
The regenerated catalyst lifter of 109 fourth reforming reactors (four is anti-) 110
The 111 4 anti-anticatalyst lifters of top hopper 112 4
The 113 3 anti-anticatalyst lifters of top hopper 114 3
The 115 2 anti-anticatalyst lifters of top hopper 116 2
The 117 1 anti-reclaimable catalyst lifters of top hopper 118
The 119 separation regenerators of hopper 120
The reaction heating furnace of 201 reaction feeds/product exchanger 202 first
The reaction heating furnace of 203 first reforming reactors (one is anti-) 204 second
The reaction heating furnace of 205 second reforming reactors (two is anti-) 206 the 3rd
The reaction heating furnace of 207 tri-reforming devices (three is anti-) 208 the 4th
The regenerated catalyst lifter of 209 fourth reforming reactors (four is anti-) 210
The 211 4 anti-anticatalyst lifters of top hopper 212 4
The 213 3 anti-anticatalyst lifters of top hopper 214 3
The 215 2 anti-anticatalyst lifters of top hopper 216 2
The 217 1 anti-reclaimable catalyst lifters of top hopper 218
The 219 separation regenerators of hopper 220
The reaction heating furnace of 1 reaction feed/product exchanger 2 first
The reaction heating furnace of 3 first reforming reactor 4 second
The reaction heating furnace of 5 second reforming reactor 6 the 3rd
7 tri-reforming device, 8 one anti-top hopper
The 9 three anti-regenerated catalyst of top hopper 10 reprocessing and distribution system (RCTS)
11 reclaimable catalysts are reprocessed and the regenerator of distribution system (WCTS) 12
13 reclaimable catalysts lifting blower fan 14 regenerated catalyst lifting blower fan
Embodiment
The embodiment of the present invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The embodiment stated is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The present invention provides a kind of hydro carbons continuous reforming process, it is characterised in that：The technique includes：At least two reformations are set
Reactor group and at least one catalyst regenerator, the reactor quantity of wherein at least one reforming reactor group is at least two
Individual, the reactor quantity of other reactor groups is at least one；Reaction feed is relative to each in each reforming reactor group
The conveying of reactor is that series connection is carried out, i.e., reaction feed passes sequentially through each reactor in each reforming reactor group simultaneously
Reacted with catalyst therein；And catalyst following between each reactor group and between reactor group and regenerator
Ring conveying is progress in parallel, but conveying of the catalyst between each reactor inside each reactor group is that series connection is carried out
's.
According to the hydro carbons continuous reforming process of the present invention, wherein used various process conditions, including feedstock oil, made
Catalyst, the operating condition of reactor, operating condition of regenerator etc. be all it is well known to those of ordinary skill in the art,
There is no particular limitation to it by the present invention.
For example, described catalyst can contain primary activity component noble metal platinum (Pt) etc., cocatalyst component tin
And the aluminum oxide of rhenium (Re) etc. and acid carrier etc. and other adjuvants, but not limited to this (Sn).The operation of each reactor
Condition can be independently, but be not limited to：0.1~1.5MPa of reaction pressure, preferably 0.2~1.0MPa；(raw material enters reaction temperature
Mouthful temperature) 400~550 DEG C, preferably 480-520 DEG C；Hydrogen-oil ratio (mol ratio) 0.1~10.0, preferably 1.0~5.0；Weight space velocity
For 0.5~5, preferably 1.5~3.Described feedstock oil may be, but not limited to,：Straight-run naphtha, the hydrogenation of low octane rating
Naphtha etc..
According to the hydro carbons continuous reforming process of the present invention, the continuous reforming reactor is those skilled in the art institute
Well known moving-burden bed reactor；Described regenerator is used to make the reclaimable catalyst by reaction inactivation realize cyclic regeneration, wraps
Include by burning, oxychlorination, drying (or roasting), the technique such as reduction make the high reclaimable catalyst activity recovery of carbon content, regenerate
The quantity of device is preferably one, can also set again one it is standby.
According to the continuous reforming process of the present invention, wherein, the technique includes：It is provided with two reforming reactor groups and one
Regenerator 12, wherein two reactors that the first reforming reactor group includes being arranged in series are reformed positioned at the first of charging front end
Reactor 3 and the second reforming reactor 5 positioned at charging rear end, the second reforming reactor group are the triple including a reactor
Whole reactor 7, and the technique is additionally provided with the anti-top hopper 8 positioned at the top of the first reforming reactor 3, triple positioned at
The three anti-top hoppers 9 on the whole top of reactor 7, regenerated catalyst are reprocessed and distribution system RCTS10, reclaimable catalyst are located again
Reason and distribution system WCTS11, reclaimable catalyst lifting blower fan 13 and regenerated catalyst lifting blower fan 14；Reaction feed is successively
By the first reforming reactor 3, the second reforming reactor 5 and tri-reforming device 7, the anti-of tri-reforming device 7 is left
Answer product to be exchanged heat with reaction feed in reaction feed/product exchanger 1, then arrive follow-up separator again and separated；
Regenerated catalyst regenerated catalyst lifting blower fan 14 is promoted to RCTS10 from regenerator 12；RCTS10 passes through 2 tremie pipes point
It is not connected with an anti-8 and three anti-top hopper 9 of top hopper, an anti-top hopper 8 passes through tremie pipe and the first reforming reaction
Device 3 is connected, and three anti-top hoppers 9 are connected by tremie pipe and tri-reforming device 7；Divided with reclaimable catalyst lifting blower fan 13
The reclaimable catalyst in the second reforming reactor 5 and tri-reforming device 7 WCTS11 is not promoted to；WCTS11 passes through 1
Tremie pipe is connected with regenerator 12.
According to the hydro carbons continuous reforming process of the present invention, the regenerated catalyst reprocessing and distribution system RCTS can be right
Regenerated catalyst carries out dust elutriation, reduction and reallocation, is then sent to respectively by tremie pipe in a manner of parallel side-by-side each
It is used for chemical reaction process in individual reforming reactor.
According to the hydro carbons continuous reforming process of the present invention, the reclaimable catalyst reprocessing and distribution system WCTS can be right
Reclaimable catalyst is mixed, dust elutriation and locking transformation, is then delivered to regenerator by tremie pipe and is regenerated.
According to the hydro carbons continuous reforming process of the present invention, those skilled in the art are it is appreciated that reaction feed can be with
First exchanged heat with reaction product, then successively and alternately enter heating furnace and reactor below, reaction product leaves heat exchange
Follow-up separator is arrived after device again to be separated.
According to the hydro carbons continuous reforming process of the present invention, the catalyst after regeneration is lifted to RCTS, Ran Houtong from regenerator
Tremie pipe is crossed to be respectively delivered to be chemically reacted in each reactor by catalyst.Leave the reclaimable catalyst difference of each reactor
Lifting is delivered to WCTS, and being then delivered to regenerator by tremie pipe is regenerated.
Embodiment
The present embodiment combination accompanying drawing 3 illustrates to a kind of embodiment provided by the invention.By carried out
It is prolonged commerical test, wherein described various process conditions allow to have about ± 10% fluctuation.
As shown in Figure 3, successively by the after reaction feed exchanges heat in reaction feed/product exchanger 1 with reaction product
One reaction heating furnace 2, the first reforming reactor 3, the second reaction heating furnace 4, the second reforming reactor 5, the 3rd reaction heating furnace
6th, tri-reforming device 7, it is in reaction feed/product exchanger 1 and anti-after reaction product leaves tri-reforming device 7
Heat exchange should be fed, follow-up separator is then arrived again and is separated.Reactant produces pressure drop, reactor in flow process
The order of operating pressure from high to low is：First reforming reactor 3, the second reforming reactor 5 and tri-reforming device 7.
Regenerator 12 regeneration after catalyst by regenerated catalyst lifted blower fan 14 with nitrogen from regenerator 12 lifted to
RCTS10.Carry out the dust elutriation of catalyst first in RCTS10, then reusable heat hydrogen is to the catalyst after removing dust
Reduced, the nitrogen after removing dust is sent to regenerated catalyst lifting blower fan 14 as regenerated catalyst lifting nitrogen circulation
Use.Catalyst after reduction has respectively entered an anti-8 and three anti-top hopper 9 of top hopper by gravity by 2 tremie pipes,
Then corresponding first reforming reactor 3 and tri-reforming device 7 are respectively enterd by gravity again, into the first reforming reaction
The catalyst of device flows through after beds participate in reformate chemical reaction by gravity by the dipleg between two reactors to enter again
Enter the second reforming reactor 5, catalyst participates in chemical reaction process in each reactor.It is used in reactor group each
The catalyst of the high activity just regenerated.Catalyst flow control device can be set on the tremie pipe or top hopper,
The flow for entering the regenerated catalyst in each reactor is controlled or even dammed to realize.In two groups of reactors, first
The operating pressure highest of reforming reactor, in order that RCTS10 catalyst can enter each group reactor, RCTS pressure is higher than
The one anti-reforming reactor 3 of top hopper 8 and first.
Reclaimable catalyst lifts blower fan 13 with nitrogen respectively from the second reforming reactor 5 and tri-reforming by reclaimable catalyst
Reactor 7, which is lifted, is delivered to WCTS11 top low-pressure area, and the operating pressure of low-pressure area is less than tri-reforming device 7, from every
Catalyst lifting conveying of the individual reactor group to regenerator is all independent, can be changed lifting conveying capacity as needed.
Catalyst is mixed first in WCTS, then carries out the dust elutriation of catalyst again, the nitrogen after dust is removed and send
Used to reclaimable catalyst lifting blower fan 13 as reclaimable catalyst lifting nitrogen circulation, the catalyst after removing dust enters again
Row locking is boosted, and WCTS11 bottom higher-pressure region is then sent through after boosting, and the operating pressure of higher-pressure region is higher than regenerator 12, higher-pressure region
Catalyst regenerator 12 be delivered to by tremie pipe regenerated, the pressure of regenerator 12 is higher than RCTS10, leaves regenerator
Catalyst be promoted to RCTS, so far complete catalyst conveying circulation.
The present embodiment carries out cycloalkanes dehydrogenation, cyclization of paraffins dehydrogenation, different in the hydrogen gas atmosphere using C6~C12 naphthas hydro carbons
Structure and the reaction such as it is hydrocracked, hydrogen/oil ratio 2.2 of reaction raw materials, it is 58/30/12 (wt%) that P/N/A, which is formed, and inlet amount is
600000 tons/year, the time of CONTINUOUS REFORMER is 1 year.Reaction feed (naphtha and hydrogen mixture) reacted charging/product heat exchange
After device 1 exchanges heat, reformed successively by the first reaction heating furnace 2, the first reforming reactor 3, the second reaction heating furnace 4, second anti-
Answer device 5, the 3rd reaction heating furnace 6, tri-reforming device 7, after reaction product leaves tri-reforming device 7, react into
Exchanged heat in material/product exchanger 1 with reaction feed, then arrive follow-up separator again and separated.First reforming reactor
3 inlet pressure 0.56MPa (g), the inlet pressure 0.50MPa (g) of the second reforming reactor 5, the inlet pressure of tri-reforming device 7
0.42MPa (g), reaction weight space velocity is 2.1, and the inlet temperature of each reactor is 517 DEG C.
Used catalyst contains noble metal platinum (Pt) and tin for Research Institute of Petro-Chemical Engineering (RIPP) exploitation
(Sn) and other adjuvants PS-VI continuous reforming catalysts.The catalyst phosphorus content after regenerator 12 regenerates is left to be less than
0.2% (wt), lifted by regenerated catalyst lifting blower fan 14 with nitrogen from regenerator 12 to RCTS10.Carried out first in RCTS
The dust elutriation of catalyst, remove dust after nitrogen be sent to regenerated catalyst lifting blower fan 14 as regenerated catalyst lifted
Nitrogen circulation uses, and reusable heat hydrogen reduces to the catalyst after removing dust in RCTS10 reducing zone, and RCTS is also
The operating pressure in former area is 0.58MPa (g), 0.02MPa (g) higher than the first reforming reactor.Catalyst after reduction leans on gravity
An anti-8 and three anti-top hopper 9 of top hopper is had respectively entered after 2 tremie pipes leave RCTS, is then distinguished again by gravity
Into corresponding first reforming reactor 3 and tri-reforming device 7, the catalyst into the first reforming reactor flows through catalysis
Agent bed enters the second reforming reactor 5 by gravity by the dipleg between two reactors again after participating in reformate chemical reaction,
Catalyst participates in chemical reaction process in each reactor, and used in each reactor group is the high activity just regenerated
Catalyst.
The carbon distribution content for leaving the reclaimable catalyst of each reactor is 2.8%~3.3% (wt).Reclaimable catalyst is by be generated
Catalyst lifts blower fan 13 and is delivered to WCTS11 from the second reforming reactor 5 and the lifting of tri-reforming device 7 respectively with nitrogen
Top low-pressure area, the operating pressure of WCTS11 tops low-pressure area is 0.30MPa, than 7 low 0.05MPa of tri-reforming device,
Independently carried out from each reactor group to the lifting conveying of WCTS15 catalyst, each group reaction can be changed as needed
The catalyst lifting conveying capacity of device, can also carry out individually lifting conveying, Ke Yiling to the reclaimable catalyst in single group reactor
The circulation conveying of catalyst is carried out livingly.Catalyst is mixed first in the low-pressure area of WCTS11 tops, then carried out again
The dust elutriation of catalyst, remove dust after nitrogen be sent to reclaimable catalyst lifting blower fan 13 as reclaimable catalyst lifted
Nitrogen circulation uses, and the catalyst after WCTS11 tops low-pressure area removes dust carries out locking boosting again, then enters back into
The higher-pressure region of WCTS11 bottoms, the operating pressure of higher-pressure region is 0.68MPa (g), and reclaimable catalyst passes through tremie pipe from higher-pressure region
It is delivered to regenerator 12 to be regenerated, the operating pressure of regenerator is 0.65 MPa (g), and the catalyst after regeneration lifts conveying again
To RCTS10, the circulation of catalyst is completed.
Hydro carbons continuous reforming process of the present invention is by the way of the conveying of catalyst parallel circulating so that enters each reactor
The catalyst of group is all " fresh " catalyst just regenerated, and the average carbon deposition quantity of reactor is low, and the effect of catalyst can more obtain
Give full play to.The catalyst higher with the activity just regenerated into the reaction in each reactor group contacts, and reduces bed
About 4~5 DEG C of mean temperature, the side reaction such as it is hydrocracked so as to reduce, and reduces the carbon distribution on catalyst, extends the longevity of catalyst
Life.
Under identical operating mode, operation and reaction condition, hydro carbons continuous reforming process of the present invention and existing work
The CONTINUOUS REFORMER technology of industry is compared to gasoline products yield 0.9% is added, and C5+ liquid yields increase by 0.8%, hydrogen yield increases
Add 2.0%.For the catalytic reforming unit that a set for the treatment of capacity is 1,000,000 tons/year, annual 0.9 ten thousand tons of increasing gasoline yield, increase
Add into 27,000,000 yuan.Annual 700 tons of hydrogen of volume increase, 7,000,000 yuan of increase income.
Because in the present embodiment, the operating mode of continuous reforming process of the present invention and existing industrial continuous reforming process uses
Identical air speed and identical catalyst filling ratio, i.e., the operating mode of continuous reforming process of the present invention do not optimize.It is if excellent
Changed the reaction condition (such as catalyst filling ratio) of continuous reforming process of the present invention, then can reduce catalyst filling amount or
Liquid yield is further improved, is increased the benefit.
Claims (4)
- A kind of 1. hydro carbons continuous reforming process, it is characterised in that：The technique includes：Two reforming reactor groups and one are set again Raw device (12), wherein two reactors that the first reforming reactor group includes being arranged in series are reformed positioned at the first of charging front end Reactor (3) and the second reforming reactor (5) positioned at charging rear end, the second reforming reactor group are the including a reactor Tri-reforming device (7)；The technique also includes setting the anti-top hopper (8) positioned at the first reforming reactor (3) top, position Three anti-top hoppers (9) in tri-reforming device (7) top, regenerated catalyst reprocessing and distribution system RCTS (10), Reclaimable catalyst is reprocessed and distribution system WCTS (11), reclaimable catalyst lifting blower fan (13) and regenerated catalyst lifting wind Machine (14)；Reaction feed passes through the first reforming reactor (3), the second reforming reactor (5) and tri-reforming device successively (7) reaction product for, leaving tri-reforming device (7) exchanges heat with reaction feed in reaction feed/product exchanger (1), Then follow-up separator is arrived again to be separated；Regenerated catalyst lifts blower fan (14) from regenerator (12) with regenerated catalyst It is promoted to RCTS (10)；RCTS (10) by 2 tremie pipes respectively with an anti-top hopper (8) and three anti-top hoppers (9) It is connected, an anti-top hopper (8) is connected by tremie pipe and the first reforming reactor (3), and three anti-top hoppers (9) pass through blanking Guan Yu tri-reformings device (7) is connected；With reclaimable catalyst lifting blower fan (13) respectively by the second reforming reactor (5) and the Reclaimable catalyst in tri-reforming device (7) is promoted to WCTS (11)；WCTS (11) passes through 1 tremie pipe and regenerator (12) It is connected；Reclaimable catalyst in second reforming reactor (5) and tri-reforming device (7) is elevated in a manner of parallel side-by-side Be delivered in WCTS (11) mixed, dust elutriation and locking transformation process, regenerator is then transported to by tremie pipe (12) regenerated；From lifting conveying capacity from each reforming reactor group to WCTS (11) reclaimable catalyst and/or conveying when Machine is all individually controllable；Regenerated catalyst is promoted to the elutriation of RCTS (10) progress dust, reduction from regenerator (12) and divided again With process, then the first reforming reactor (3) is respectively delivered to from RCTS (10) by 2 tremie pipes in a manner of parallel side-by-side In tri-reforming device (7), the catalyst in the first reforming reactor (3) enters the second reforming reactor by gravity again (5) in；It is individually controllable from RCTS (10) to the conveying capacity of the regenerated catalyst of each reforming reactor group and/or conveying opportunity 's.
- 2. hydro carbons continuous reforming process according to claim 1, wherein, the first reforming reactor (3) and the second reforming reactor (5) overlapped for series connection up and down, the first reforming reactor (3) be located at the second reforming reactor (5) top, two reactors There are more diplegs to be connected between beds, the catalyst in the first reforming reactor (3) can lean on gravity to enter through dipleg Enter the second reforming reactor (5).
- 3. according to the hydro carbons continuous reforming process of claim 1 or 2, wherein, RCTS (10) operating pressure is less than regenerator (12) operating pressure, so as to which regenerated catalyst is lifted to RCTS (10) from regenerator (12)；RCTS (10) bottom Position is higher than an anti-top hopper (8) and the position on the top of three anti-top hoppers (9), and RCTS (10) operating pressure is high Operating pressure in the first reforming reactor (3) so that regenerated catalyst can be flowed into from RCTS (10) it is all anti- Answer device.
- 4. according to the hydro carbons continuous reforming process of claim 1 or 2, wherein, the position of WCTS (11) bottom is higher than regenerator (12) position on top, WCTS (11) are divided into two pressure areas, and the upper zone before transformation is low-pressure area, and pressure is less than the 3rd Reforming reactor (7), reclaimable catalyst can be lifted to this from the second reforming reactor (5) and tri-reforming device (7) Low-pressure area；Lower region after transformation is higher-pressure region, and pressure is higher than regenerator (12), and reclaimable catalyst can be from the higher-pressure region It is flowed into regenerator (12).
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4069136A (en) * | 1976-10-26 | 1978-01-17 | Uop Inc. | Countercurrent hydrocarbon conversion with gravity-flowing catalyst particles |
| CN1524928A (en) * | 2003-02-28 | 2004-09-01 | 中国石油化工股份有限公司 | Multi moving bed reactor mixed flow catalytic reforming technology |
| CN1530427A (en) * | 2003-03-11 | 2004-09-22 | Regenerating and reforming method |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4069136A (en) * | 1976-10-26 | 1978-01-17 | Uop Inc. | Countercurrent hydrocarbon conversion with gravity-flowing catalyst particles |
| CN1524928A (en) * | 2003-02-28 | 2004-09-01 | 中国石油化工股份有限公司 | Multi moving bed reactor mixed flow catalytic reforming technology |
| CN1530427A (en) * | 2003-03-11 | 2004-09-22 | Regenerating and reforming method |
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