CN106905996A - A kind of hydro carbons continuous reforming process - Google Patents
A kind of hydro carbons continuous reforming process Download PDFInfo
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- CN106905996A CN106905996A CN201510974974.4A CN201510974974A CN106905996A CN 106905996 A CN106905996 A CN 106905996A CN 201510974974 A CN201510974974 A CN 201510974974A CN 106905996 A CN106905996 A CN 106905996A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
- C10G35/10—Catalytic reforming with moving catalysts
- C10G35/12—Catalytic reforming with moving catalysts according to the "moving-bed" method
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of hydro carbons continuous reforming process, the technique includes：At least four reforming reactors and at least one catalyst regenerator are set, wherein, last reforming reactor is referred to as second group of reactor, reactor in addition to last reforming reactor is referred to as first group of reactor, reaction feed is carried out relative to the conveying series connection of each reforming reactor, catalyst is that parallel connection is carried out with the circulation conveying between regenerator in first group of reactor and second group of reactor, and catalyst is carried out in first group of reactor with the inverse following current of conveying series connection between regenerator.In the present invention, every group of reactor can be carried out separately adjustable using fresh high activated catalyst and on demand 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 hydrocarbon reformation field, and in particular 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, make molecule occur reset, it is different
Structure, increases the yield of aromatic hydrocarbons, improves 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 respectively Uop Inc. of the U.S., France Axens and China SEI.In continuous reformer
In, 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
Device is regenerated.Regenerated catalyst after activity recovery returns to first reactor and is reacted again, and catalyst is formed in system
One closed cycle.
By catalyst transport model split, existing industrialized continuous reforming process can be divided into " following current " and " inverse
Stream " two ways.
In the catalyst circulation conveying technique of " following current " CONTINUOUS REFORMER, reaction mass flows to most end successively from first reactor
Reactor, is reacted on the catalyst in each reactor.Moving direction of the catalyst between each reactor be and reactant
Material is consistent, that is, the high activated catalyst for regenerating is introduced into first reactor by the order of reaction stream, then passes sequentially through
Second reactor, the 3rd reactor are gradually reduced from first reactor until most end reactor to most end reactor pressure, from most
Last reactor catalyst activity out is relatively low, is sent in regenerator and is regenerated, and the catalyst after regeneration is lifted to again
One reactor completes the circulation of catalyst.In the technical process of this CONTINUOUS REFORMER, catalyst is used in series in the reactor
, the catalyst into the first reforming reactor is the catalyst that just regenerated " fresh " high activity, and reactor below
All it is the above reactor relatively low catalyst of used activity.
In the catalyst circulation conveying technique of " adverse current " CONTINUOUS REFORMER, reaction mass flows to most end successively from first reactor
Reactor.And moving direction of the catalyst between each reactor is highly active catalytic opposite with reaction mass, that is, regenerating
The order of agent back reaction logistics is introduced into rearmost reactor, and then the direction of back reaction logistics is successively forward until first
Reactor, then be sent in regenerator from first reactor and regenerated, the catalyst after regeneration lifts last reaction again
Device completes the circulation of catalyst.The technical process of this adverse current CONTINUOUS REFORMER causes that high activity of the difficult reaction for carrying out below is urged
Carried out in the reactor of agent, reaction easy to perform is carried out in the reactor of low activity catalyst above.
But, either " following current " or " adverse current " continuous reforming process, circulation conveying of the catalyst between reactor
All by the way of series connection, the catalyst that this mode of movement is only transported to first reactor from regenerator is only just regeneration
" fresh " activity crossed catalyst high, such as first reforming reactor of " following current " CONTINUOUS REFORMER, " adverse current " CONTINUOUS REFORMER
Last reforming reactor.And the catalyst in other reforming reactors to be all that above reactor is used contain carbon distribution
The decreased catalyst of activity, catalyst is conveyed in the backward, and its activity is lower, and the activity in the reactor that catalyst leaves is most
It is low.The activity of catalyst can not give full play in all reactors as can be seen here.The mode of this catalyst cascade conveying, leads to
The catalyst internal circulating load for crossing each reactor is all identical, the catalyst in all reactors must simultaneously circular regeneration, each
The catalyst flow of reactor can not on demand be carried out separately adjustable and changed, it is impossible to individually be circulated regeneration.
The content of the invention
It is an object of the invention to provide a kind of hydro carbons continuous reforming process, overcome prior art can not realize reactor according to
Need to use fresh high activated catalyst and can not on demand carry out disadvantage that is separately adjustable and changing catalyst flow, with abundant
The activity of catalyst is played, the utilization rate of catalyst is improved, reforming conversion and yield is improved.
To achieve these goals, the present invention provides a kind of hydro carbons continuous reforming process, and the technique includes：Set at least four
The individual reforming reactor being parallel to each other and at least one catalyst regenerator；Wherein：Reaction feed is relative to each reforming reaction
The conveying series connection of device is carried out, i.e., reaction feed passes sequentially through each reforming reactor and carried out instead with catalyst therein
Should；Wherein, flowed to according to reaction feed, at least three reforming reactor is divided into first group of reactor and second group of reaction
Device, first group of reactor includes all reforming reactors in addition to last reforming reactor, and second group of reactor is institute
State last reforming reactor；Catalyst is in first group of reactor and second group of reactor with the circulation conveying between regenerator
Parallel connection is carried out, i.e., the reacted reclaimable catalyst in every group reactor is carried out continuously in being all individually delivered to regenerator
Regeneration, and the regenerated catalyst after regenerating is transported in every group of reactor by parallel connection and is reused for reaction；Catalyst is at first group
Reactor is carried out with the inverse following current of conveying series connection between regenerator, i.e., flowed to according to reaction feed, by first group of reactor
In penultimate reactor in reclaimable catalyst be delivered in regenerator and carry out cyclic regeneration, and the regeneration after regenerating is urged
Reacted in the end reactor that agent is transported in first group of reactor, and catalyst is first inverse by the end reactor
Stream is delivered in the initial reactor in first group of reactor and is reacted, then defeated by the initial reactor successively following current again
Deliver to and reacted in the penultimate reactor.
Preferably, the technique also includes：Independently control the conveying from every group of reactor to the reclaimable catalyst of regenerator
Amount and/or conveying opportunity, and independently control conveying capacity from from regenerator to every group of regenerated catalyst of reactor and/or defeated
Send opportunity.
Preferably, the technique also includes：Reclaimable catalyst reprocessing and distribution system WCTS are set, in every group of reactor
Reclaimable catalyst is elevated in the way of parallel side-by-side to be delivered to the WCTS, is mixed in WCTS, dust elutriation and locking
Transformation process, is then transferred to be regenerated in regenerator；And regenerated catalyst reprocessing and distribution system RCTS are set,
Regenerated catalyst is promoted to the RCTS from regenerator carries out dust elutriation, reduction and redistribution process, then with parallel side-by-side
Mode from RCTS be respectively delivered in each group reactor be used for chemical reaction process.
Preferably, the technique includes that set four reforming reactors being parallel to each other and a regenerator, i.e., first reforms
Reactor, the second reforming reactor, tri-reforming device, fourth reforming reactor and regenerator, and the technique also includes
Regenerated catalyst reprocessing and distribution system RCTS, reclaimable catalyst reprocessing and distribution system WCTS, reclaimable catalyst are set
Lifting blower fan and regenerated catalyst lifting blower fan；First, second, and third reforming reactor is first group of reactor, institute
Fourth reforming reactor is stated for second group of reactor；Reaction feed sequentially pass through the first reforming reactor, the second reforming reactor,
Tri-reforming device and fourth reforming reactor；Regenerated catalyst regenerated catalyst lifting blower fan is promoted to from regenerator
RCTS；RCTS is connected with the third and fourth reforming reactor respectively；Blower fan is lifted by second and quadruple with reclaimable catalyst
Reclaimable catalyst in whole reactor is promoted to WCTS respectively；WCTS is connected by 1 tremie pipe with regenerator；Catalyst exists
The first reforming reactor is flowed to by tri-reforming device in first group of reactor, then is flowed to by the first reforming reactor
Two reforming reactors.
Preferably, regenerated catalyst is promoted to RCTS from regenerator carries out dust elutriation, reduction and redistribution process, so
It is respectively delivered to by tremie pipe in each group reactor for chemical reaction process from RCTS in the way of parallel side-by-side afterwards；From
RCTS is individually controllable to the conveying capacity and/or conveying opportunity of every group of regenerated catalyst of reactor.
Preferably, second and fourth reforming reactor in reclaimable catalyst elevated in the way of parallel side-by-side be delivered to
WCTS, is mixed, dust elutriation and locking transformation process in WCTS, and being then delivered to regenerator by tremie pipe is carried out again
It is raw；It is individually controllable from every group of reactor to the lifting conveying capacity of the reclaimable catalyst of WCTS and/or conveying opportunity.
Preferably, the operating pressure of RCTS is less than the operating pressure of regenerator, such that it is able to catalyst is carried from regenerator
It is raised to RCTS；The position of RCTS bottoms is higher than the position on each group reactor top simultaneously, and the operating pressure of RCTS is triple higher than the
The operating pressure of whole reactor and fourth reforming reactor so that catalyst can be flowed into every group of reactor from RCTS.
Preferably, the position of WCTS bottoms higher than regenerator top position, WCTS be divided to be two pressure areas, transformation it
Preceding upper zone be low-pressure area, pressure be less than the second reforming reactor and fourth reforming reactor, can by reclaimable catalyst from
The low-pressure area is arrived in second reforming reactor and the lifting of fourth reforming reactor；Lower region after transformation is higher-pressure region, pressure
Higher than regenerator, reclaimable catalyst can be flowed into regenerator from the higher-pressure region.
The circulation conveying mode that continuous reforming process of the invention is combined using catalyst parallel connection and serial connection so that enter
Catalyst in the reactor that the third and fourth two difficulties are reacted all is " fresh " catalyst for just regenerating, and above
The reaction carried out in first and second reactors is relatively easy, and the catalyzer coke content in tri-reforming device is relatively low,
Applied in the first and second reactors for being delivered to above by inverse following current lifting, it is smaller on reaction influence, using it is of the invention this
The circulation conveying mode that catalyst parallel connection and serial connection is combined is planted, flow is relatively easy, and the average coke content of reactor is low, catalyst
Effect can more be not fully exerted.
The present invention overcome by changing circulation conveying mode of the catalyst between multiple reforming reactors it is existing
The shortcoming that each catalyst reactor activity can not give full play in industrialized technology.Into anti-in most latter two reactor
The catalyst for answering thing all higher with the activity for just regenerating is contacted, and can reduce about 5~10 DEG C of bed mean temperature, such that it is able to
Reduction such as is hydrocracked at the side reaction, and product yield about 1% can be increased compared with existing industrialized CONTINUOUS REFORMER technology, and
The carbon deposit on catalyst can be reduced, extends the life-span of catalyst.Catalyst internal circulating load into every group of reactor can be according to need
It is adjusted, so as to optimize reaction and regeneration condition, improves catalyst service efficiency.
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 to constitute the part of specification, with following tool
Body implementation method is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is a kind of schematic flow sheet of specific embodiment of hydro carbons continuous reforming process of the present invention.
Description of reference numerals
The reaction heating furnace of 1 reaction feed/product exchanger 2 first
The reaction heating furnace of 3 first reforming reactors (is anti-) 4 second
The reaction heating furnace of 5 second reforming reactors (two is anti-) 6 the 3rd
The reaction heating furnace of 7 tri-reforming devices (three is anti-) 8 the 4th
The anti-top hopper of 9 fourth reforming reactors (four is anti-) 10 1
The 11 2 anti-anti- top hoppers of top hopper 12 3
13 4 anti-top hoppers 14 1 instead buffer hopper
15 regenerators
16 regenerated catalysts are reprocessed and distribution system (RCTS)
17 reclaimable catalysts are reprocessed and distribution system (WCTS)
18 regenerated catalysts lifting blower fan 19 reclaimable catalyst lifting blower fan
Specific embodiment
Specific embodiment of the invention is described in detail below in conjunction with accompanying drawing.It should be appreciated that this place is retouched
The specific 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, and the technique includes：At least four reformations being parallel to each other are set
Reactor and at least one catalyst regenerator；Wherein：Reaction feed relative to the conveying of each reforming reactor be connect into
Capable, i.e., reaction feed passes sequentially through each reforming reactor and is reacted with catalyst therein；Wherein, according to react into
Stream by least three reforming reactor to being divided into first group of reactor and second group of reactor, first group of reactor bag
The all reforming reactors in addition to last reforming reactor are included, second group of reactor is described last reforming reaction
Device；Catalyst is that parallel connection is carried out with the circulation conveying between regenerator in first group of reactor and second group of reactor, i.e., often
Reacted reclaimable catalyst in group reactor carries out cyclic regeneration in being all individually delivered to regenerator, and after regenerating again
Raw catalyst is transported in every group of reactor by parallel connection and is reused for reaction；Catalyst is in first group of reactor between regenerator
The inverse following current of conveying series connection (i.e. first adverse current conveying again following current conveying catalyst) carry out, i.e., flowed to according to reaction feed, will
The reclaimable catalyst in penultimate reactor in first group of reactor carries out cyclic regeneration in being delivered to regenerator, and again
Reacted in the end reactor that regenerated catalyst after life is transported in first group of reactor, and catalyst is by the end
End reaction device is first countercurrently delivered in the initial reactor in first group of reactor and is reacted, then again by the initial action
Device is reacted during following current is delivered to the penultimate reactor successively.
Hydro carbons continuous reforming process of the invention, the various process conditions employed in it, 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 for the present invention.
For example, described catalyst can contain primary activity component noble metal platinum (Pt) etc., cocatalyst component tin
(Sn) and rhenium (Re) etc. and acid carrier aluminum oxide etc. and other adjuvants, but not limited to this.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
It is 0.5~5, preferably 1.5~3.Described feedstock oil may be, but not limited to,：The straight-run naphtha of low octane rating, hydrogenation stone
Cerebrol etc..
Hydro carbons continuous reforming process of the invention, described reforming reactor is that those skilled in the art institute is ripe
The moving-burden bed reactor known；Moving-burden bed reactor can be 4~6 series connection, preferably 4 series connection；Described regenerator is used for
Make to realize cyclic regeneration by the reclaimable catalyst of reaction inactivation, including by burning, oxychlorination, the technique such as drying (or roasting)
The quantity of the reclaimable catalyst activity recovery that carbon content is high, regenerator is preferably one, it is also possible to set again one it is standby.
A kind of specific embodiment of the invention, the hydro carbons continuous reforming process includes that setting four mutually puts down
Capable reforming reactor and a regenerator, i.e. the first reforming reactor 3, the second reforming reactor 5, tri-reforming device 7,
Fourth reforming reactor 9 and regenerator 15, and the technique also includes that setting regenerated catalyst reprocesses and distribution system
RCTS16, reclaimable catalyst reprocessing and distribution system WCTS17, reclaimable catalyst lifting blower fan 19 and regenerated catalyst are carried
Rise blower fan 18；First, second, and third reforming reactor is first group of reactor, and the fourth reforming reactor is second
Group reactor；Reaction feed sequentially passes through the first reforming reactor 3, the second reforming reactor 5, tri-reforming device 7 and
Four reforming reactors 9；Regenerated catalyst regenerated catalyst lifting blower fan 18 is promoted to RCTS16 from regenerator 15；RCTS16 points
It is not connected with the third and fourth reforming reactor 7 and 9；Blower fan 19 is lifted with reclaimable catalyst to react second and fourth reforming
Reclaimable catalyst in device 5 and 9 is promoted to WCTS17 respectively；WCTS17 is connected by 1 tremie pipe with regenerator 15；Catalysis
Agent flows to the first reforming reactor 3 in first group of reactor by tri-reforming device 7, then by the first reforming reactor
3 flow to the second reforming reactor 5.
Hydro carbons continuous reforming process of the invention, the regenerated catalyst reprocessing and distribution system RCTS 16 can
To carry out dust elutriation, reduction and reallocation to regenerated catalyst, then sent respectively by tremie pipe in the way of parallel side-by-side
It is used for chemical reaction process in each group reforming reactor.
Hydro carbons continuous reforming process of the invention, the reclaimable catalyst reprocessing and distribution system WCTS 17 can
Mixed with to reclaimable catalyst, dust elutriation and locking transformation, regenerator is then delivered to by tremie pipe and is regenerated.
Hydro carbons continuous reforming process of the invention, those skilled in the art are it is appreciated that reaction feed can be with
First exchanged heat with product, then successively and alternately entered heating furnace and reactor below, product is left heat exchange
Follow-up separator is arrived after device again to be separated.
Hydro carbons continuous reforming process of the invention, catalyst after regeneration is lifted to RCTS16 from regenerator, then
Catalyst is respectively delivered to by tremie pipe chemically reacted in each group reactor.Leave the catalysis to be generated of each group reactor
Agent is lifted be delivered to WCTS17 respectively, and being then delivered to regenerator by tremie pipe is regenerated.
The present invention will be further illustrated by embodiment below, but the present invention is not therefore subject to any restriction.
Embodiment
A kind of specific embodiment that 1 couple of present invention of the present embodiment combination accompanying drawing is provided is illustrated.By carried out
It is prolonged commerical test, wherein described various process conditions allow about ± 10% fluctuation.
As shown in figure 1, reaction feed sequentially passes through the in reaction feed/product exchanger 1 with after product heat exchange
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, the 4th reaction heating furnace 8 and fourth reforming reactor 9, product leave reactor 9 in reaction
Exchange heat and then arrive follow-up separator again with reaction feed in charging/product exchanger 1 and separated, wherein, first, second
It is referred to as first group of reactor with tri-reforming device, fourth reforming reactor is referred to as second group of reactor.Reaction mass is in stream
Pressure drop is produced during dynamic, reactor operating pressure order from high to low is：First reforming reactor 3, second is reformed anti-
Answer device 5, tri-reforming device 7 and fourth reforming reactor 9.Catalyst after the regeneration of regenerator 15 is carried by regenerated catalyst
Blower fan 18 is risen to be lifted to RCTS16 from regenerator 15 with nitrogen.Carry out the dust elutriation of catalyst first in RCTS16, then
Reusable heat hydrogen is reduced to removing the catalyst after dust, is removed the nitrogen after dust and is sent to regenerated catalyst lifting wind
Machine 18 is used as regenerated catalyst lifting nitrogen circulation.The pressure of RCTS16 is higher than first group of reactor and second group of reaction
The anti-top hopper 12, tri-reforming device 7 of device, i.e., three, four anti-top hoppers 13 and fourth reforming reactor 9, after reduction
Catalyst respectively enters the top hopper 12 of each group reactor by 2 tremie pipes by gravity, and 13, then enter accordingly by gravity
Reactor 7, is chemically reacted in 9.The catalyst hydrogen for finishing is reacted from reactor 7 and is promoted to an anti-buffering hopper 14
In, then entered in an anti-top hopper 10 by tremie pipe by gravity, subsequently into being reacted in reactor 3.From reactor 3
In catalyst transport to the two anti-top hoppers 11 that middle reaction is finished, then entered in reactor 5 by tremie pipe by gravity again
Reacted.
In each group reactor it is used be all the high activity for just regenerating catalyst.Can be on the tremie pipe or top
Catalyst flow control device is set on hopper, to realize controlling the flow for entering the regenerated catalyst in each group reactor
System is even dammed.It is respectively the second reformation from each group reactor by reclaimable catalyst to lift the nitrogen of blower fan 19 with reclaimable catalyst
Reactor 5 and fourth reforming reactor 9 lift the top low-pressure area for being delivered to WCTS17, the operation pressure of WCTS17 tops low-pressure area
Power is less than the second reforming reactor 5 and fourth reforming reactor 9, is all from every group of reactor to the lifting conveying of the catalyst of WCTS
Independent, and it is controllable to lift conveying capacity, can as needed change the lifting conveying capacity of reclaimable catalyst.In WCTS17
Top low-pressure area in, catalyst is mixed first, the dust elutriation of catalyst is then carried out again, after removing dust
Nitrogen is sent to reclaimable catalyst lifting blower fan 19 and is used as reclaimable catalyst lifting nitrogen circulation, removes the catalysis after dust
Agent carries out locking transformation again, and the catalyst after boosting enters back into the bottom higher-pressure region of WCTS17, and the operating pressure of higher-pressure region is higher than
Regenerator 15, the catalyst after boosting is delivered to regenerator 15 and is regenerated by tremie pipe, and the pressure of regenerator 15 is higher than
RCTS16, the catalyst for leaving regenerator is promoted to RCTS, so far completes the conveying circulation of catalyst.
The present embodiment uses C6~C12Naphtha hydro carbons carries out cycloalkanes dehydrogenation, cyclization of paraffins dehydrogenation, different in the hydrogen gas atmosphere
Structure and the reaction such as it is hydrocracked.Reaction feed (naphtha and hydrogen mixture) reacted charging/product exchanger 1 exchanges heat
Afterwards, the first reaction heating furnace 2, the first reforming reactor 3, the second reaction heating furnace 4, the second reforming reactor 5, are sequentially passed through
Three reaction heating furnaces 6, tri-reforming device 7, the 4th reaction heating furnace 8 and fourth reforming reactor 9, product leave
After four reforming reactors 9, exchanged heat with reaction feed in reaction feed/product exchanger 1, follow-up separator is then arrived again
Separated.The inlet pressure of first reforming reactor 3 is about 0.56MPa (g), the inlet pressure of the second reforming reactor 5 and is about
0.49MPa (g), the inlet pressure of tri-reforming device 7 are about 0.42MPa (g), the inlet pressure of fourth reforming reactor 9 and are about
0.35MPa(g)。
The catalyst for being used 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.Leave the catalyst carbon content after regenerator 15 regenerates substantially small
In 0.2% (wt), lifted to RCTS16 from regenerator 15 with nitrogen by regenerated catalyst lifting blower fan 18.In RCTS16 first
The dust elutriation of catalyst is carried out, then the catalyst after removing dust is reduced with hot hydrogen in RCTS16, removed
Nitrogen after dust is sent to regenerated catalyst lifting blower fan 18 and is used as regenerated catalyst lifting nitrogen circulation.The behaviour of RCTS
Make pressure ratio tri-reforming device operating pressure 0.01~0.08MPa high, than the low 0.01~0.08MPa of regenerator 15.Reduction
Catalyst afterwards respectively enters reactor top hopper 12,13 after leaving RCTS through 2 tremie pipes by gravity, and gravity is then leaned on again
Enter corresponding reforming reactor 7 from reactor top hopper, chemically reacted in 9, reaction is finished in reforming reactor 7
Catalyst is delivered to reforming reactor 3,5 successively again.In each group reactor it is used be all the high activity for just regenerating catalysis
Agent.
Blower fan 19 is lifted by reclaimable catalyst nitrogen respectively from the reforming reaction in each group reactor with reclaimable catalyst
The lifting of device 5,9 is delivered to WCTS17 tops low-pressure area, the operating pressure of low-pressure area than fourth reforming reactor 9 low 0.01~
0.08MPa, less than all of reactor.All independently carried out from every group of reactor to the lifting conveying of the catalyst of WCTS, can
Conveying capacity is lifted with the catalyst for changing each group reactor as needed, it is also possible to which to be generated in single group or multigroup reactor is urged
Agent carries out individually lifting conveying, can neatly carry out the circulation conveying of catalyst.In the low-pressure area of WCTS17 tops first
The mixing of catalyst is carried out, the dust elutriation of catalyst is then carried out again, removed the nitrogen after dust and be sent to reclaimable catalyst
Lifting blower fan 19 is used as reclaimable catalyst lifting nitrogen circulation.Remove the catalyst after dust carries out locking transformation again,
Catalyst after boosting enters back into the bottom higher-pressure region of WCTS17, and the operating pressure of bottom higher-pressure region is higher than regenerator 15 by about 0.01
~0.08MPa.The reclaimable catalyst of higher-pressure region is delivered to regenerator 15 and is regenerated by tremie pipe, the operating pressure of regenerator
About 0.65MPa (g), the catalyst after regeneration is lifted be delivered to RCTS16 again, completes the circulation of catalyst.
Reaction mass is reacted in the reactor can all make carbon deposit on catalyst surface, leave on the catalyst of reactor
Coke content than entering the high of reactor, for the process of series connection conveying, carbon deposited catalyst will go successively to reactor below,
Therefore, its coke content can also be accumulated constantly, and the coke content of catalyst is higher in the backward, and activity is also constantly reduced, existing company
Continuous reformation is exactly that, using this series connection mode of movement, its catalyst is circulated and causes the catalyst activity in downstream reactor less than upper
The reactor of trip, the activity of catalyst can not give full play to.Continuous reforming process of the invention is mutually tied using catalyst connection in series-parallel
The mode of the circulation conveying of conjunction so that be all " fresh " catalyst for just regenerating, reaction into every group of catalyst of reactor
The average coke content of device is low, and the effect of catalyst can more be not fully exerted.All regenerated with firm into the reaction in every group of reactor
The catalyst contact active higher crossed, can reduce about 5~10 DEG C of bed mean temperature, be hydrocracked such that it is able to reduce
Side reaction, can increase product yield about 1%, and can reduce on catalyst compared with existing industrialized CONTINUOUS REFORMER technology
Carbon deposit, extend catalyst life-span.
Table 1 is listed in the present embodiment respectively according to (catalyst connection in series-parallel circulation conveying) of the invention and according to prior art
(conveying of catalyst following current series circulation) carries out three groups of result of the tests of check experiment of hydro carbons CONTINUOUS REFORMER.
Continuous reforming process of the present invention and existing industrialized CONTINUOUS REFORMER work from the results shown in Table 1
Skill is compared and had the following advantages：
1st, continuous reforming process of the present invention into the catalyst of each group reactor was just regenerated without carbon deposit
Fresh catalyst, active highest reacts severity conditions (product reaches identical RON values) in identical, and existing
Industrialized CONTINUOUS REFORMER is compared, and four inlet temperatures of reactor decline 3~5 DEG C.
2nd, under identical reaction severity conditions, continuous reforming process of the present invention is than existing industrialized company
Continuous reforming process average reaction temperature declines so that 30~40%, the C of average carbon deposit rate reduction on catalyst5 +Liquid yield increases
Plus 0.7~1.1%, hydrogen yield increases by 2.1~4.7%.
For the catalytic reforming unit that a set for the treatment of capacity is 1,000,000 tons/year, using CONTINUOUS REFORMER work of the present invention
Compared with using existing continuous reforming process, annual increasing gasoline yield 0.7~1.1 ten thousand ton increase income about 2100~33,000,000 to skill
Unit, increases production 720~1700 tons of hydrogen, increases about 720~17,000,000 yuan of income.
In above-mentioned comparative example, continuous reforming process of the present invention is used with the operating mode of existing industrial continuous reforming process
Identical air speed and identical catalyst filling ratio, i.e., the operating mode of continuous reforming process of the present invention do not optimize.If excellent
Changed the reaction condition (such as catalyst filling than) of continuous reforming process of the present invention, then can reduce catalyst filling amount or
Liquid yield is further improved, is increased the benefit.
Table 1
Claims (8)
1. a kind of hydro carbons continuous reforming process, the technique includes：At least four reforming reactors that are parallel to each other and at least are set
One catalyst regenerator；It is characterized in that：
Reaction feed is carried out relative to the conveying series connection of each reforming reactor, i.e., reaction feed passes sequentially through each reformation
Reactor is simultaneously reacted with catalyst therein；Wherein, flowed to according to reaction feed, by least three reforming reactor
It is divided into first group of reactor and second group of reactor, first group of reactor includes owning in addition to last reforming reactor
Reforming reactor, second group of reactor is described last reforming reactor；
Catalyst is that parallel connection is carried out with the circulation conveying between regenerator in first group of reactor and second group of reactor, i.e., often
Reacted reclaimable catalyst in group reactor carries out cyclic regeneration in being all individually delivered to regenerator, and after regenerating again
Raw catalyst is transported in every group of reactor by parallel connection and is reused for reaction；
Catalyst is carried out in first group of reactor with the inverse following current of conveying series connection between regenerator, i.e., according to reaction feed stream
To the reclaimable catalyst in the penultimate reactor in first group of reactor is delivered in regenerator to be carried out continuously again
It is raw, and reacted in the end reactor that the regenerated catalyst after regenerating is transported in first group of reactor, and catalyst
First countercurrently it is delivered in the initial reactor in first group of reactor by the end reactor and is reacted, then again by described
Initial reactor is reacted during following current is delivered to the penultimate reactor successively.
2. hydro carbons continuous reforming process according to claim 1, the technique also includes：Independently control from every group of reactor to again
The conveying capacity of the reclaimable catalyst of raw device and/or conveying opportunity, and independently control from regenerator to every group of reactor again
The conveying capacity of raw catalyst and/or conveying opportunity.
3., according to the hydro carbons continuous reforming process of claim 1 or 2, the technique also includes：Set reclaimable catalyst reprocessing and
Distribution system WCTS, reclaimable catalyst in every group of reactor is elevated in the way of parallel side-by-side to be delivered to the WCTS,
Mixed in WCTS, dust elutriation and locking transformation process, be then transferred to be regenerated in regenerator；And set again
Raw catalyst reprocessing and distribution system RCTS, regenerated catalyst is promoted to the RCTS from regenerator carries out dust elutriation, also
Former and redistribution process, is then respectively delivered in each group reactor for chemically reacting in the way of parallel side-by-side from RCTS
Process.
4. hydro carbons continuous reforming process according to claim 1, the technique includes, sets four reforming reactors being parallel to each other
With a regenerator, i.e. the first reforming reactor (3), the second reforming reactor (5), tri-reforming device (7), fourth reforming
Reactor (9) and regenerator (15), and the technique also include set regenerated catalyst reprocessing and distribution system RCTS (16),
Reclaimable catalyst is reprocessed and distribution system WCTS (17), reclaimable catalyst lift blower fan (19) and regenerated catalyst lifting wind
Machine (18)；First, second, and third reforming reactor is first group of reactor, and the fourth reforming reactor is second group
Reactor；Reaction feed sequentially passes through the first reforming reactor (3), the second reforming reactor (5), tri-reforming device (7)
With fourth reforming reactor (9)；Regenerated catalyst regenerated catalyst lifts blower fan (18) and is promoted to RCTS from regenerator (15)
(16)；RCTS (16) is connected with the third and fourth reforming reactor (7 and 9) respectively；Blower fan (19) is lifted with reclaimable catalyst
Reclaimable catalyst in second and fourth reforming reactor (5 and 9) is promoted to WCTS (17) respectively；WCTS (17) is by 1
Tremie pipe is connected with regenerator (15)；Catalyst flows in first group of reactor by tri-reforming device (7)
One reforming reactor (3), then the second reforming reactor (5) is flowed to by the first reforming reactor (3).
5. hydro carbons continuous reforming process according to claim 4, wherein, regenerated catalyst is promoted to RCTS from regenerator (15)
(16) dust elutriation, reduction and redistribution process are carried out, is then divided by tremie pipe from RCTS (16) in the way of parallel side-by-side
It is not transported in each group reactor for chemical reaction process；From RCTS (16) to every group of conveying of the regenerated catalyst of reactor
Amount and/or conveying opportunity are individually controllable.
6. hydro carbons continuous reforming process according to claim 4, wherein, second and fourth reforming reactor (5 and 9) in it is to be generated
Catalyst is elevated in the way of parallel side-by-side to be delivered to WCTS (17), is mixed in the WCTS (17), dust elutriation and closed
Lock transformation process, is then delivered to regenerator (15) and is regenerated by tremie pipe；From every group of reactor treating to WCTS (17)
The lifting conveying capacity of raw catalyst and/or conveying opportunity are individually controllable.
7. hydro carbons continuous reforming process according to claim 4, wherein, the operating pressure of RCTS (16) is less than regenerator (15)
Operating pressure, such that it is able to catalyst is lifted to RCTS (16) from regenerator；The position of RCTS (16) bottom is higher than each simultaneously
The position on group reactor top, the operating pressure of RCTS (16) is higher than tri-reforming device (7) and fourth reforming reactor (9)
Operating pressure so that catalyst can be flowed into every group of reactor from RCTS (16).
8. hydro carbons continuous reforming process according to claim 4, wherein, the position of WCTS (17) bottom is higher than on regenerator (15)
The position in portion, WCTS (17) is divided into two pressure areas, and the upper zone before transformation is low-pressure area, and pressure is reformed anti-less than second
Device (5) and fourth reforming reactor (9) are answered, reclaimable catalyst can be reacted from the second reforming reactor (5) and fourth reforming
The low-pressure area is arrived in device (9) lifting；Lower region after transformation is higher-pressure region, and pressure is higher than regenerator (15), reclaimable catalyst
Regenerator (15) can be flowed into from the higher-pressure region.
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| CN110699111A (en) * | 2018-07-09 | 2020-01-17 | 中国石油化工股份有限公司 | Countercurrent continuous reforming method |
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| US20040178119A1 (en) * | 2003-03-11 | 2004-09-16 | Eric Sanchez | Process of regenerative reforming |
| CN204111691U (en) * | 2014-08-21 | 2015-01-21 | 中国石化工程建设有限公司 | Hydro carbons continuous reformer (two) |
| CN204111693U (en) * | 2014-08-21 | 2015-01-21 | 中国石化工程建设有限公司 | Hydro carbons continuous reformer (five) |
| CN204111688U (en) * | 2014-08-21 | 2015-01-21 | 中国石化工程建设有限公司 | Hydro carbons continuous reformer (four) |
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| US20040178119A1 (en) * | 2003-03-11 | 2004-09-16 | Eric Sanchez | Process of regenerative reforming |
| CN204111691U (en) * | 2014-08-21 | 2015-01-21 | 中国石化工程建设有限公司 | Hydro carbons continuous reformer (two) |
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| CN110699111B (en) * | 2018-07-09 | 2021-12-17 | 中国石油化工股份有限公司 | Countercurrent continuous reforming method |
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