CN205328949U - Continuous reforming unit of hydro carbons - Google Patents
Continuous reforming unit of hydro carbons Download PDFInfo
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- CN205328949U CN205328949U CN201521081842.0U CN201521081842U CN205328949U CN 205328949 U CN205328949 U CN 205328949U CN 201521081842 U CN201521081842 U CN 201521081842U CN 205328949 U CN205328949 U CN 205328949U
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- 238000002407 reforming Methods 0.000 title claims abstract description 122
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 21
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 250
- 238000006243 chemical reaction Methods 0.000 claims abstract description 147
- 239000000463 material Substances 0.000 claims abstract description 5
- 230000008929 regeneration Effects 0.000 claims description 39
- 238000011069 regeneration method Methods 0.000 claims description 39
- 239000003795 chemical substances by application Substances 0.000 claims description 30
- 238000012958 reprocessing Methods 0.000 claims description 24
- 238000010438 heat treatment Methods 0.000 claims description 23
- 230000000694 effects Effects 0.000 abstract description 21
- 230000008859 change Effects 0.000 abstract description 6
- 230000009466 transformation Effects 0.000 abstract description 4
- 239000007795 chemical reaction product Substances 0.000 abstract 1
- 239000000047 product Substances 0.000 abstract 1
- 238000000629 steam reforming Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 24
- 230000008569 process Effects 0.000 description 16
- 239000000428 dust Substances 0.000 description 14
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 10
- 229910052799 carbon Inorganic materials 0.000 description 10
- 230000005484 gravity Effects 0.000 description 7
- 239000000571 coke Substances 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 230000002411 adverse Effects 0.000 description 5
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000005204 segregation Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- 239000002671 adjuvant Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000007363 ring formation reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
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Abstract
The utility model discloses a continuous reforming unit of hydro carbons, the device include four at least reforming reactor and at least one catalyst regenerators, its characterized in that: through reaction material passageway series connection between each reforming reactor, wherein, according to the reaction material of device enters the mouth to reaction product outlet 's direction, four at least reforming reactor divide into first group reaction ware and second group reaction ware, first group reaction ware and second group reaction ware be through catalyst transfer passage parallel connection between with the regenerator, and first group reaction ware is through catalyst transfer passage series connection between with the regenerator. The utility model discloses in, all reactors can both fresh high activity catalyst and are carried out independently adjust and change catalyst flow rate according to needs, activity that can the full play catalyst improves the utilization ratio of catalyst, improve steam reforming transformation rate with the product yield.
Description
Technical field
This utility model relates to hydrocarbon reformation field, is specifically related to a kind of hydro carbons continuous reformer。
Background technology
CONTINUOUS REFORMER is a kind of oil secondary operations technology, the raw material of processing is mainly low-octane straight-run naphtha, hydrotreated naphtha etc., utilize platinum Pt-stannum Sn bimetallic catalyst, under the high temperature of about 500 DEG C, make molecule reset, isomery, increase the yield of aromatic hydrocarbons, improve the technology of octane number。
Moving-burden bed reactor continuous regenerative reforming, is called for short CONTINUOUS REFORMER。At present main three CONTINUOUS REFORMER patented technology providers of commercial Application are American UOP company, France Axens and China SEI respectively in the world。In continuous reformer, catalyst flows successively through three (or four) moving-burden bed reactors of series connection continuously, the reclaimable catalyst carbon content flowed out from last reactor is generally 2%-8% (mass fraction), and reclaimable catalyst is transported to regenerator by gravity or gas lift and regenerates。Regeneration catalyzing agent after activity recovery returns the first reactor and reacts again, and catalyst forms a closed cycle in system。
By catalyst transport model split, existing industrialized continuous reforming process can be divided into " following current " and " adverse current " two ways。
In the catalyst circulation conveying technique of " following current " CONTINUOUS REFORMER, reaction mass flows most end reactor successively from the first reactor, and the catalyst in each reactor reacts。Catalyst moving direction between each reactor is consistent with reaction mass, namely the high activated catalyst regenerated is introduced into the first reactor by the order of reaction logistics, then the second reactor, the 3rd reactor are passed sequentially through until most end reactor, it is gradually reduced from the first reactor to most end reactor pressure, relatively low from most end reactor catalyst activity out, being sent in regenerator and regenerate, the catalyst after regeneration rises to the first reactor again and completes the circulation of catalyst。In the technical process of this CONTINUOUS REFORMER, catalyst is that series connection uses in the reactor, the catalyst entering the first reforming reactor is " fresh " the highly active catalyst just regenerated, and reactor below is all the above reactor catalyst that used activity is relatively low。
In the catalyst circulation conveying technique of " adverse current " CONTINUOUS REFORMER, reaction mass flows most end reactor successively from the first reactor。And the moving direction that catalyst is between each reactor is contrary with reaction mass, the order of the high activated catalyst back reaction logistics namely regenerated is introduced into rearmost reactor, then the direction of back reaction logistics is successively forward until first reactor, delivering to regenerator from the first reactor and regenerate, the catalyst after regeneration rises to last reactor again and completes the circulation of catalyst。The technical process of this adverse current CONTINUOUS REFORMER makes to carry out in the reactor of reaction that difficulty the carries out high activated catalyst below, it is easy to the reaction carried out carries out in the reactor of low activity catalyst above。
But, no matter it is " following current " or " adverse current " continuous reforming process, catalyst circulation conveying between reactor all adopts the mode of series connection, the catalyst that this mode of movement is only transported to first reactor from regenerator is only the catalyst that " fresh " activity just regenerated is high, such as first reforming reactor of " following current " CONTINUOUS REFORMER, last reforming reactor of " adverse current " CONTINUOUS REFORMER。And the catalyst in other reforming reactor is all that above reactor is used containing the active decreased catalyst of carbon distribution, catalyst is more carried backward, and its activity is more low, and the activity in the reactor that catalyst leaves is minimum。The activity of catalyst can not give full play in all reactors as can be seen here。The mode of this catalyst cascade conveying, it is all identical by the catalyst circulating load of each reactor, the necessary circular regeneration simultaneously of catalyst in all reactors, the catalyst flow of each reactor can not carry out independent regulation and change on demand, it is impossible to is individually circulated regeneration。
Utility model content
The purpose of this utility model is to provide a kind of hydro carbons continuous reformer, overcome prior art can not realize reactor use fresh high activated catalyst as required and independent regulation can not be carried out on demand and change the disadvantage of catalyst flow, to give full play to the activity of catalyst, improve the utilization rate of catalyst, improve reforming conversion and yield。
To achieve these goals, this utility model provides a kind of hydro carbons continuous reformer, and this device includes at least four reforming reactor and at least one catalyst regenerator, wherein: connected by reaction mass Tandem between each reforming reactor；Wherein, according to the reaction mass entrance of described device to the direction of reacting product outlet, described at least four reforming reactor is divided into the first group reaction device and the second group reaction device, first group reaction device includes all reforming reactors except last reforming reactor, and the second group reaction device is last reforming reactor described；Described first group reaction device and the second group reaction device are connected in parallel by catalyst transport passage with between regenerator；According to the reaction mass entrance of described device to the direction of reacting product outlet, the catalyst outlet of penultimate reactor and the catalyst inlet of end reactor in described first group reaction device are connected by catalyst transport passage with regenerator, by catalyst transport Tandem between catalyst outlet and the catalyst inlet of initial reactor of end reactor in described first group reaction device, in addition, described first group reaction device passes through catalyst transport Tandem between catalyst outlet and the catalyst inlet of later reactor of previous reactor。
Preferably, this device is set to: from every group reaction device to the conveying capacity of the reclaimable catalyst of described regenerator and/or conveying opportunity be individually controllable, and from described regenerator to the conveying capacity of the regeneration catalyzing agent of every group reaction device and/or conveying opportunity be individually controllable。
Preferably, this device also includes a regeneration catalyzing agent reprocessing and distribution system RCTS and a reclaimable catalyst reprocessing and distribution system WCTS；The catalyst inlet UNICOM of the catalyst outlet UNICOM of the catalyst inlet of RCTS and regenerator, the catalyst outlet of RCTS and every group reaction device；The catalyst inlet UNICOM of the catalyst outlet UNICOM of the catalyst inlet of WCTS and every group reaction device, the catalyst outlet of WCTS and regenerator。
Preferably, the catalyst outlet of every group reaction device is provided by the catalyst inlet of catalyst transport passage and reclaimable catalyst reprocessing and distribution system WCTS that reclaimable catalyst promotes blower fan and connects, reclaimable catalyst reprocessing is connected with the catalyst inlet of regenerator by tremie pipe with the catalyst outlet of distribution system WCTS, and described WCTS is divided into top low-pressure area and higher-pressure region, bottom；The catalyst inlet of every group reaction device is connected with the catalyst outlet of regeneration catalyzing agent reprocessing and distribution system RCTS by catalyst transport passage, and the catalyst outlet of regenerator is provided by the catalyst transport passage of regeneration catalyzing agent lifting blower fan and connects with the catalyst inlet of regeneration catalyzing agent reprocessing and distribution system RCTS。
Preferably, the position of the catalyst outlet of reclaimable catalyst reprocessing and distribution system WCTS is higher than the position of the catalyst inlet of regenerator；The position of the catalyst outlet of regeneration catalyzing agent reprocessing and distribution system RCTS is higher than the position of the catalyst inlet of each group reaction device。
Preferably, the described reaction mass passage of the material front end of each reforming reactor is provided with heating furnace。
Preferably, this device includes four reforming reactors and a regenerator, i.e. the first reforming reactor, the second reforming reactor, tri-reforming device, fourth reforming reactor and regenerator, described first group reaction device includes the first reforming reactor, the second reforming reactor and tri-reforming device, and described second group reaction device is fourth reforming reactor。
Continuous reformer of the present utility model can make catalyst parallel connection and serial connection circulate conveying in combination, making the catalyst entered in the third and fourth two reactors that difficulty reacts is all " fresh " catalyst just regenerated, and the reaction that carries out in the first and second reactors above is relatively easy, catalyzer coke content in tri-reforming device is relatively low, application in the first and second reactors being delivered to above can be promoted by inverse following current series connection, reaction impact is less, adopt the circulating conveyor that this catalyst parallel connection and serial connection of the present utility model combines, make flow process relatively easy, the average coke content of reactor is low, the effect of catalyst more can be not fully exerted。
The reforming reactor that this utility model combines by providing series connection and parallel connection is to change catalyst circulation mode of movement between multiple reforming reactors, thus overcoming the shortcoming that in existing industrialized technology, each catalyst reactor activity can not give full play to。The catalyst making to enter the reactant in latter two reactor all higher with the activity just regenerated contacts, bed mean temperature about 5～10 DEG C can be reduced, such that it is able to reduce the side reactions such as hydrogenation cracking, product yield about 1% can be increased compared with existing industrialized continuous reformer, and the carbon deposit on catalyst can be reduced, extend the life-span of catalyst。The catalyst circulating load entering every group reaction device can be adjusted as required, thus optimizing reaction and regeneration condition, improves catalyst service efficiency。
Other feature and advantage of the present utility model will be described in detail in detailed description of the invention part subsequently。
Accompanying drawing explanation
Accompanying drawing is used to provide novel being further appreciated by of this use, and constitutes a part for description, is used for explaining this utility model, but is not intended that restriction of the present utility model together with detailed description below。In the accompanying drawings:
Fig. 1 is the schematic diagram of a kind of detailed description of the invention of hydro carbons continuous reformer of the present utility model。
Description of reference numerals
1 reaction feed/product exchanger 2 first reaction heating furnace
3 first reforming reactors (one is anti-) 4 second reaction heating furnace
5 second reforming reactors (two is anti-) 6 the 3rd reaction heating furnace
7 tri-reforming devices (three is anti-) 8 the 4th reaction heating furnace
9 fourth reforming reactors (four is anti-) 10 1 anti-top hopper
11 2 anti-top hopper 12 3 anti-top hoppers
13 4 anti-top hoppers 14 1 are counter cushions hopper
15 regeneratoies
16 regeneration catalyzing agent reprocessing and distribution system (RCTS)
17 reclaimable catalyst reprocessing and distribution systems (WCTS)
18 regeneration catalyzing agent promote blower fan 19 reclaimable catalyst and promote blower fan
Detailed description of the invention
Below in conjunction with accompanying drawing, detailed description of the invention of the present utility model is described in detail。It should be appreciated that detailed description of the invention described herein is merely to illustrate and explains this utility model, it is not limited to this utility model。
This utility model provides a kind of hydro carbons continuous reformer, and this device includes at least four reforming reactor and at least one catalyst regenerator, wherein: connected by reaction mass Tandem between each reforming reactor；Wherein, according to the reaction mass entrance of described device to the direction of reacting product outlet, described at least four reforming reactor is divided into the first group reaction device and the second group reaction device, first group reaction device includes all reforming reactors except last reforming reactor, and the second group reaction device is last reforming reactor described；Described first group reaction device and the second group reaction device are connected in parallel by catalyst transport passage with between regenerator；According to the reaction mass entrance of described device to the direction of reacting product outlet, the catalyst outlet of penultimate reactor and the catalyst inlet of end reactor in described first group reaction device are connected by catalyst transport passage with regenerator, by catalyst transport Tandem between catalyst outlet and the catalyst inlet of initial reactor of end reactor in described first group reaction device, in addition, described first group reaction device passes through catalyst transport Tandem between catalyst outlet and the catalyst inlet of later reactor of previous reactor。
According to hydro carbons continuous reformer of the present utility model, described reforming reactor is the moving-burden bed reactor known by those skilled in the art；Moving-burden bed reactor can be 4～6 series connection, it is preferred to 4 series connection；Described regenerator realizes cyclic regeneration for making the reclaimable catalyst through reaction inactivation, including burning, oxychlorination, the technique such as dry (or roasting) device, make the reclaimable catalyst activity recovery that carbon content is high, the quantity of regenerator is preferably one, it is also possible to arrange again one standby。
According to a kind of detailed description of the invention of the present utility model, described hydro carbons continuous reformer can also include a regeneration catalyzing agent reprocessing and distribution system RCTS and a reclaimable catalyst reprocessing and distribution system WCTS；The catalyst inlet UNICOM of the catalyst outlet UNICOM of the catalyst inlet of RCTS and regenerator, the catalyst outlet of RCTS and every group reaction device；The catalyst inlet UNICOM of the catalyst outlet UNICOM of the catalyst inlet of WCTS and every group reaction device, the catalyst outlet of WCTS and regenerator。Described regeneration catalyzing agent reprocessing and distribution system RCTS may be used for regeneration catalyzing agent is carried out dust elutriation, reduction and reallocation, then to be delivered to respectively in each reforming reactor for chemical reaction process by tremie pipe in the way of parallel side-by-side。Described reclaimable catalyst reprocessing and distribution system WCTS may be used for reclaimable catalyst is mixed, dust elutriation and locking transformation, then passes through tremie pipe and is delivered to regenerator and regenerates。By arranging RCTS and WCTS, it is possible to better regeneration catalyzing agent or reclaimable catalyst are carried out conveying and controls and further process。
Described reaction mass passage and catalyst transport passage are well-known to those skilled in the art, and there is no particular limitation to it for this utility model。Such as, reaction mass passage can include feed-line and necessary pumping equipment or the like；Temperature required in order to make reaction mass reach reaction, in the material channel of each reforming reactor front end, heating furnace can be set。Equally, such as, catalyst transport passage can include catalyst transport pipeline, for the reclaimable catalyst that reclaimable catalyst rises to WCTS or regenerator from reforming reactor is promoted blower fan, and for the regeneration catalyzing agent that the catalyst after regeneration rises to RCTS or each reforming reactor from regenerator is promoted blower fan etc.。
According to a kind of detailed description of the invention of the present utility model, this hydro carbons continuous reformer can include four reforming reactors and a regenerator, i.e. first reforming reactor the 3, second reforming reactor 5, tri-reforming device 7, fourth reforming reactor 9 and regenerator 15, described first group reaction device includes first reforming reactor the 3, second reforming reactor 5 and tri-reforming device 7, and described second group reaction device is fourth reforming reactor 9。More specifically, this device can also include reaction feed/product exchanger the 1, first reaction heating furnace the 2, second reaction heating furnace the 4, the 3rd reaction heating furnace the 6, the 4th reaction heating furnace 8, anti-top hopper 10, two anti-top hopper 11, three anti-top hopper 12, four anti-top hopper 13, anti-buffering hopper 14, regeneration catalyzing agent reprocessing and distribution system RCTS16, reclaimable catalyst reprocessing and distribution system WCTS17, reclaimable catalyst promote blower fan 19 and regeneration catalyzing agent promotes blower fan 18。As shown in Figure 1。
According to a kind of detailed description of the invention of the present utility model, described reaction feed/product exchanger the 1, first reaction heating furnace the 2, first reforming reactor the 3, second reaction heating furnace the 4, second reforming reactor the 5, the 3rd reaction heating furnace 6, tri-reforming device the 7, the 4th reaction heating furnace 8 and fourth reforming reactor 9 pass sequentially through reaction mass Tandem and connect, and fourth reforming reactor 9 is connected with reaction feed/product exchanger 1 again by reaction mass passage。Reactor operating pressure order from high to low is: first reforming reactor the 3, second reforming reactor 5, tri-reforming device 7 and fourth reforming reactor 9。Second and fourth reforming reactor 5, the catalyst outlet of 9 is provided by the catalyst transport pipeline of reclaimable catalyst lifting blower fan 19 and is connected with WCTS17, WCTS17 is connected with regenerator 15 by 1 tremie pipe, regenerator 15 pass sequentially through 1 tremie pipe be provided with regeneration catalyzing agent promote blower fan 18 catalyst transport pipeline be connected with RCTS16, RCTS16 respectively and is positioned at the third and fourth reforming reactor 7 by 2 tremie pipes, the three of 9 catalyst inlets are anti-and four anti-top hoppers 12,13 are connected。Tri-reforming device 7 instead cushions hopper 14 and is connected with an anti-top hopper 10 of the first reforming reactor 3 catalyst inlet by one, and the catalyst outlet of the first reforming reactor 3 is connected with the catalyst inlet of the second reactor 5 by two anti-top hoppers 11。
According to another detailed description of the invention of the present utility model, described WCTS17 can be divided into top low-pressure area and higher-pressure region, bottom；The purpose arranging higher-pressure region is when reclaimable catalyst is after low-pressure area processes and enters higher-pressure region, and owing in the pressure ratio regenerator of higher-pressure region, pressure is big, catalyst can automatically flow in regenerator。
Below in conjunction with accompanying drawing 1, the work process of a kind of detailed description of the invention of the present utility model is illustrated。Being long commerical test due to what carry out, wherein said various process conditions allow the fluctuation of about ± 10%。
Embodiment
A kind of detailed description of the invention that this utility model is provided by the present embodiment in conjunction with accompanying drawing 1 illustrates。Being long commerical test due to what carry out, wherein said various process conditions allow the fluctuation of about ± 10%。
As shown in Figure 1, reaction feed sequentially passes through the first reaction heating furnace 2 with after product heat exchange in reaction feed/product exchanger 1, first reforming reactor 3, second reaction heating furnace 4, second reforming reactor 5, 3rd reaction heating furnace 6, tri-reforming device 7, 4th reaction heating furnace 8 and fourth reforming reactor 9, product is left reactor 9 and is then arrived follow-up segregation apparatus in reaction feed/product exchanger 1 with reaction feed heat exchange again and be easily separated, wherein, first, second and tri-reforming device be called the first group reaction device, fourth reforming reactor is called the second group reaction device。Reaction mass produces Pressure Drop in flow process, and reactor operating pressure order from high to low is: first reforming reactor the 3, second reforming reactor 5, tri-reforming device 7 and fourth reforming reactor 9。Catalyst after regenerator 15 regenerates is promoted blower fan 18 nitrogen by regeneration catalyzing agent and rises to RCTS16 from regenerator 15。First carrying out the dust elutriation of catalyst in RCTS16, then the catalyst after removing dust is reduced by reusable heat hydrogen, and the nitrogen after removing dust is delivered to regeneration catalyzing agent and promoted blower fan 18 as regeneration catalyzing agent lifting nitrogen circulation use。The pressure of RCTS16 is higher than the first group reaction device and the second group reaction device, namely three anti-top hoppers 12, tri-reforming device 7, four anti-top hopper 13 and fourth reforming reactor 9, catalyst after reduction respectively enters the top hopper 12 of each group reaction device by gravity by 2 tremie pipes, 13, enter in corresponding reactor 7,9 by gravity again and carry out chemical reaction。The catalyst hydrogen reacting complete from reactor 7 is promoted to one and instead cushions in hopper 14, then is entered in an anti-top hopper 10 by tremie pipe by gravity, reacts subsequently in reactor 3。From reactor 3, react complete catalyst transport to two anti-top hoppers 11, then entered in reactor 5 by tremie pipe by gravity again and react。
Used by each group reaction device is all the highly active catalyst just regenerated。Catalyst flow can be set on described tremie pipe or top hopper and control device, to realize being controlled even damming to the flow of the regeneration catalyzing agent entered in each group reaction device。Promote blower fan 19 nitrogen with reclaimable catalyst and reclaimable catalyst is promoted, from each group reaction device i.e. the second reforming reactor 5 and fourth reforming reactor 9, the top low-pressure area being delivered to WCTS17 respectively, the operation pressure of WCTS17 top low-pressure area is lower than the second reforming reactor 5 and fourth reforming reactor 9, it is all independent for promoting conveying from every group reaction device to the catalyst of WCTS, and it is controlled for promoting conveying capacity, it is possible to change the lifting conveying capacity of reclaimable catalyst as required。In the top low-pressure area of WCTS17, first catalyst is mixed, then the dust elutriation of catalyst is carried out again, nitrogen after removing dust is delivered to reclaimable catalyst and is promoted blower fan 19 as reclaimable catalyst lifting nitrogen circulation use, catalyst after removing dust carries out locking transformation again, catalyst after boosting enters back into the higher-pressure region, bottom of WCTS17, the operation pressure of higher-pressure region is higher than regenerator 15, catalyst after boosting is delivered to regenerator 15 by tremie pipe and regenerates, the pressure of regenerator 15 is higher than RCTS16, the catalyst leaving regenerator is promoted to RCTS, so far the conveying circulation of catalyst is completed。
The present embodiment adopts C6～C12Petroleum hydro carbons carries out the reactions such as cycloalkanes dehydrogenation, cyclization of paraffins dehydrogenation, isomerization and hydrogenation cracking in the hydrogen gas atmosphere。After reaction feed (Petroleum and hydrogen mixture) reacted charging/product exchanger 1 heat exchange, sequentially pass through first reaction heating furnace the 2, first reforming reactor the 3, second reaction heating furnace the 4, second reforming reactor the 5, the 3rd reaction heating furnace 6, tri-reforming device the 7, the 4th reaction heating furnace 8 and fourth reforming reactor 9, after product leaves fourth reforming reactor 9, with reaction feed heat exchange in reaction feed/product exchanger 1, then arrive follow-up segregation apparatus again and be easily separated。First reforming reactor 3 inlet pressure is about 0.56MPa (g), the second reforming reactor 5 inlet pressure is about 0.49MPa (g), tri-reforming device 7 inlet pressure is about 0.42MPa (g), fourth reforming reactor 9 inlet pressure is about 0.35MPa (g)。
The catalyst used is the PS-VI continuous reforming catalyst containing noble metal platinum (Pt) and stannum (Sn) and other adjuvant that Research Institute of Petro-Chemical Engineering (RIPP) develops。Leave the catalyst carbon content after regenerator 15 regeneration and be approximately less than 0.2% (wt), regeneration catalyzing agent promote blower fan 18 nitrogen and rise to RCTS16 from regenerator 15。First carrying out the dust elutriation of catalyst in RCTS16, then with hot hydrogen, the catalyst after removing dust is reduced in RCTS16, the nitrogen after removing dust is delivered to regeneration catalyzing agent and is promoted blower fan 18 as regeneration catalyzing agent lifting nitrogen circulation use。Operation pressure ratio tri-reforming device the operation high 0.01～0.08MPa of pressure, 0.01～0.08MPa lower than regenerator 15 of RCTS。Catalyst after reduction respectively enters reactor top hopper 12 by gravity after 2 tremie pipes leave RCTS, 13, then corresponding reforming reactor 7 is entered by gravity from reactor top hopper again, chemical reaction is carried out in 9, the catalyst reacting complete in reforming reactor 7 is delivered to reforming reactor 3,5 more successively。Used by each group reaction device is all the highly active catalyst just regenerated。
Blower fan 19 is promoted by the reclaimable catalyst nitrogen reforming reactor 5 from each group reaction device respectively with reclaimable catalyst, 9 liftings are delivered to WCTS17 top low-pressure area, the operation low 0.01～0.08MPa of pressure ratio fourth reforming reactor 9 of low-pressure area, lower than all of reactor。Promote conveying from every group reaction device to the catalyst of WCTS all independently to carry out, the catalyst that can change each group reaction device as required promotes conveying capacity, reclaimable catalyst in single group or many group reactions device individually can also be promoted conveying, it is possible to carry out the circulation conveying of catalyst neatly。First carrying out the mixing of catalyst in the low-pressure area of WCTS17 top, then carry out the dust elutriation of catalyst again, the nitrogen after removing dust is delivered to reclaimable catalyst and is promoted blower fan 19 as reclaimable catalyst lifting nitrogen circulation use。Catalyst after removing dust carries out locking transformation again, and the catalyst after boosting enters back into the higher-pressure region, bottom of WCTS17, the high about 0.01～0.08MPa of operation pressure ratio regenerator 15 of higher-pressure region, bottom。The reclaimable catalyst of higher-pressure region is delivered to regenerator 15 by tremie pipe and regenerates, and the operation pressure of regenerator is about 0.65MPa (g), and the catalyst after regeneration promotes and is delivered to RCTS16, completes the circulation of catalyst。
Reaction mass reacts in the reactor and all can make carbon deposit on catalyst surface, leave the coke content on the catalyst of reactor than entering the high of reactor, process for series connection conveying, carbon deposited catalyst to go successively to reactor below, therefore, its coke content also can constantly accumulate, more more high toward the coke content of rear catalyst, activity also constantly reduces, existing CONTINUOUS REFORMER adopts this series connection mode of movement exactly, the circulation of its catalyst makes the reactor lower than upstream of the catalyst activity in downstream reactor, and the activity of catalyst can not give full play to。Mode based on the circulation conveying that the technique employing catalyst connection in series-parallel of this utility model continuous reformer combines, making the catalyst entering every group reaction device is all " fresh " catalyst just regenerated, the average coke content of reactor is low, and the effect of catalyst more can be not fully exerted。The catalyst entering the reaction in every group reaction device all higher with the activity just regenerated contacts, bed mean temperature about 5～10 DEG C can be reduced, such that it is able to reduce the side reactions such as hydrogenation cracking, product yield about 1% can be increased compared with existing industrialized CONTINUOUS REFORMER technology, and the carbon deposit on catalyst can be reduced, extend the life-span of catalyst。
Table 1 lists in the present embodiment respectively according to based on the technique (catalyst connection in series-parallel circulation conveying) of this utility model continuous reformer with carry out the result of the test of three groups of controlled trials of hydro carbons CONTINUOUS REFORMER according to prior art (conveying of catalyst following current series circulation)。
Have the following advantages compared with existing industrialized continuous reforming process based on the technique of this utility model continuous reformer from the results shown in Table 1:
1, the catalyst based on the technique each group reaction device of entrance of this utility model continuous reformer is all the fresh catalyst without carbon deposit just regenerated, activity is the highest, at identical reaction severity conditions (product reaches identical RON value), compared with existing industrialized CONTINUOUS REFORMER, the inlet temperature of four reactors declines 3～5 DEG C。
2, under identical reaction severity conditions, the technique based on this utility model continuous reformer declines than existing industrialized continuous reforming process average reaction temperature so that the average carbon deposit rate on catalyst reduces by 30～40%, C5 +Liquid yield increases by 0.7～1.1%, and 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, adopt the technique based on this utility model continuous reformer compared with adopting existing continuous reforming process, annual increasing gasoline yield 0.7～1.1 ten thousand tons, increase income about 2100～33,000,000 yuan, volume increase hydrogen 720～1700 tons, increases income about 720～17,000,000 yuan。
In above-mentioned comparative example, the air speed identical with the operating mode employing of existing industrial continuous reforming process based on the technique of this utility model continuous reformer and identical catalyst filling ratio, namely the operating mode based on the technique of this utility model continuous reformer does not optimize。If optimize technique based on this utility model continuous reformer reaction condition (as catalyst filling than etc.), then can reduce catalyst filling amount or improve liquid yield further, increasing the benefit。
Table 1
Claims (7)
1. a hydro carbons continuous reformer, this device includes at least four reforming reactor and at least one catalyst regenerator, it is characterised in that:
Connected by reaction mass Tandem between each reforming reactor；Wherein, according to the reaction mass entrance of described device to the direction of reacting product outlet, described at least four reforming reactor is divided into the first group reaction device and the second group reaction device, first group reaction device includes all reforming reactors except last reforming reactor, and the second group reaction device is last reforming reactor described；
Described first group reaction device and the second group reaction device are connected in parallel by catalyst transport passage with between regenerator；
According to the reaction mass entrance of described device to the direction of reacting product outlet, the catalyst outlet of penultimate reactor and the catalyst inlet of end reactor in described first group reaction device are connected by catalyst transport passage with regenerator, by catalyst transport Tandem between catalyst outlet and the catalyst inlet of initial reactor of end reactor in described first group reaction device, in addition, described first group reaction device passes through catalyst transport Tandem between catalyst outlet and the catalyst inlet of later reactor of previous reactor。
2. hydro carbons continuous reformer according to claim 1, it is characterized in that: this device is set to: from every group reaction device to the conveying capacity of the reclaimable catalyst of described regenerator and/or conveying opportunity be individually controllable, and from described regenerator to the conveying capacity of the regeneration catalyzing agent of every group reaction device and/or conveying opportunity be individually controllable。
3. hydro carbons continuous reformer according to claim 1, it is characterised in that: this device also includes a regeneration catalyzing agent reprocessing and distribution system RCTS and a reclaimable catalyst reprocessing and distribution system WCTS；The catalyst inlet UNICOM of the catalyst outlet UNICOM of the catalyst inlet of RCTS and regenerator, the catalyst outlet of RCTS and every group reaction device；The catalyst inlet UNICOM of the catalyst outlet UNICOM of the catalyst inlet of WCTS and every group reaction device, the catalyst outlet of WCTS and regenerator。
4. hydro carbons continuous reformer according to claim 3, it is characterized in that: the catalyst outlet of every group reaction device is provided by the catalyst inlet of catalyst transport passage and reclaimable catalyst reprocessing and distribution system WCTS that reclaimable catalyst promotes blower fan and connects, reclaimable catalyst reprocessing is connected with the catalyst inlet of regenerator by tremie pipe with the catalyst outlet of distribution system WCTS, and described WCTS is divided into top low-pressure area and higher-pressure region, bottom；The catalyst inlet of every group reaction device is connected with the catalyst outlet of regeneration catalyzing agent reprocessing and distribution system RCTS by catalyst transport passage, and the catalyst outlet of regenerator is provided by the catalyst transport passage of regeneration catalyzing agent lifting blower fan and connects with the catalyst inlet of regeneration catalyzing agent reprocessing and distribution system RCTS。
5. hydro carbons continuous reformer according to claim 3, it is characterised in that: the position of the catalyst outlet of reclaimable catalyst reprocessing and distribution system WCTS is higher than the position of the catalyst inlet of regenerator；The position of the catalyst outlet of regeneration catalyzing agent reprocessing and distribution system RCTS is higher than the position of the catalyst inlet of each group reaction device。
6. hydro carbons continuous reformer according to claim 1, it is characterised in that: the described reaction mass passage of the material front end of each reforming reactor is provided with heating furnace。
7. the hydro carbons continuous reformer according to any one in claim 1～6, it is characterized in that: this device includes four reforming reactors 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), described first group reaction device includes the first reforming reactor (3), the second reforming reactor (5) and tri-reforming device (7), and described second group reaction device is fourth reforming reactor (9)。
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