CN205313468U - Continuous reforming unit of hydro carbons - Google Patents
Continuous reforming unit of hydro carbons Download PDFInfo
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- CN205313468U CN205313468U CN201521082853.0U CN201521082853U CN205313468U CN 205313468 U CN205313468 U CN 205313468U CN 201521082853 U CN201521082853 U CN 201521082853U CN 205313468 U CN205313468 U CN 205313468U
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- 238000002407 reforming Methods 0.000 title claims abstract description 128
- 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 190
- 238000006243 chemical reaction Methods 0.000 claims abstract description 141
- 239000000463 material Substances 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 27
- 238000012958 reprocessing Methods 0.000 claims description 24
- 239000004215 Carbon black (E152) Substances 0.000 claims description 19
- 230000008569 process Effects 0.000 claims description 16
- 230000000694 effects Effects 0.000 abstract description 19
- 230000008929 regeneration Effects 0.000 abstract description 11
- 238000011069 regeneration method Methods 0.000 abstract description 11
- 230000008859 change Effects 0.000 abstract description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 24
- 238000010438 heat treatment Methods 0.000 description 20
- 239000000428 dust Substances 0.000 description 14
- 239000000047 product Substances 0.000 description 14
- 229910052757 nitrogen Inorganic materials 0.000 description 12
- 238000005516 engineering process Methods 0.000 description 8
- 230000005484 gravity Effects 0.000 description 7
- 239000001257 hydrogen Substances 0.000 description 7
- 229910052739 hydrogen Inorganic materials 0.000 description 7
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- 239000000571 coke Substances 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 230000002411 adverse Effects 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 239000003610 charcoal Substances 0.000 description 5
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000004517 catalytic hydrocracking Methods 0.000 description 3
- 125000004122 cyclic group Chemical group 0.000 description 3
- 230000009257 reactivity Effects 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 230000009466 transformation Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 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
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying 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
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001105 regulatory 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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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a continuous reforming unit of hydro carbons, the device include at least three reforming reactor and at least one catalyst regeneration ware, its characterized in that: through reaction material passageway series connection between each reforming reactor, reforming reactor divide into two sets ofly, first group and second group reaction ware parallel connection between with the regenerator, first group reaction ware series connection between with the regenerator. The utility model discloses in, every group reaction ware can both fresh high activity catalyst and is carried out independently adjust and change the catalyst flow according to needs, and activity that can the full play catalyst improves the utilization ratio of catalyst, improves reformation conversion rate and product yield.
Description
Technical field
The utility model relates to hydrocarbon reformation field, is specifically related to a kind of hydrocarbon class continuous reformer.
Background technology
CONTINUOUS REFORMER is a kind of oil secondary processing technology, the raw material of processing is mainly the virgin naphtha of low octane rating, hydrotreated naphtha etc., utilize platinum Pt-tin Sn bimetallic catalyst, under the high temperature of about 500 DEG C, molecule is reset, different structure, increase the output of aromatic hydrocarbons, it is to increase the technology of gasoline octane rating.
Moving-burden bed reactor continuous regenerative reforming, is called for short CONTINUOUS REFORMER. At present main three CONTINUOUS REFORMER patented technology providers of industrial application are American UOP company, France Axens and China SEI respectively in the world. In continuous reformer, catalyzer flows through three (or four) moving-burden bed reactors of series connection continuously successively, the reclaimable catalyst carbon content flowed out from last reactor is generally 2%-8% (massfraction), and reclaimable catalyst is transported to revivifier by gravity or gas lift and regenerates. Regenerated catalyst after activity recovery returns the first reactor and reacts again, and catalyzer forms a closed cycle in system.
By catalyst transport model split, the continuous reforming process of existing industrialization can be divided into " following current " and " adverse current " two kinds of modes.
In the catalyst recirculation delivery technology of " following current " CONTINUOUS REFORMER, reaction mass flows to most end reactor successively from the first reactor, and the catalyzer in each reactor reacts. The travel direction of catalyzer between each reactor is consistent with reaction mass, namely regenerated high activated catalyst is introduced into the first reactor by the order of reaction logistics, then successively by the 2nd reactor, the 3rd reactor until most end reactor, decline gradually from the first reactor to most end reactor pressure, lower from most end reactor catalyst activity out, being sent in revivifier and regenerate, the catalyzer after regeneration rises to the circulation that the first reactor completes catalyzer again. In the technological process of this kind of CONTINUOUS REFORMER, catalyzer is that series connection uses in the reactor, the catalyzer entering the first reforming reactor is the catalyzer of just regenerated " fresh " high reactivity, and reactor below is all the active relatively low catalyzer that reactor had been used above.
In the catalyst recirculation delivery technology of " adverse current " CONTINUOUS REFORMER, reaction mass flows to most end reactor successively from the first reactor. And the travel direction of catalyzer between each reactor is contrary with reaction mass, the order of namely regenerated high activated catalyst reversed reaction logistics is introduced into reactor the most below, then the direction of reversed reaction logistics is successively forward until first reactor, delivering to revivifier from the first reactor and regenerate, the catalyzer after regeneration rises to the circulation that last reactor completes catalyzer again. The technological process of this kind of adverse current CONTINUOUS REFORMER makes to carry out in the reactor of high activated catalyst below of reaction that difficulty carries out, it is easy to carry out in the reactor of the low activity catalyst of the reaction carried out above.
But, no matter it is " following current " or " adverse current " continuous reforming process, the circulation conveying of catalyzer between reactor all adopts the mode of series connection, the catalyzer that this kind of mode of movement is only transported to first reactor from revivifier is only the active high catalyzer of just regenerated " fresh ", such as first reforming reactor of " following current " CONTINUOUS REFORMER, last reforming reactor of " adverse current " CONTINUOUS REFORMER. And the catalyzer in other reforming reactor is all the catalyzer reduced containing long-pending carbon activity that reactor used above, catalyzer is more carried backward, and its activity is more low, active minimum in the reactor that catalyzer leaves. The activity of catalyzer can not give full play in all reactors as can be seen here. The mode of this kind of catalyzer series connection conveying, it is all identical by the catalyst recirculation amount of each reactor, the necessary cyclic regeneration simultaneously of catalyzer in all reactors, the catalyst flow of each reactor can not carry out independent adjustment and change on demand, cannot carry out separately cyclic regeneration.
Practical novel content
The purpose of this utility model is to provide a kind of hydrocarbon class continuous reformer, overcome the disadvantage that prior art can not realize reactor and use fresh high activated catalyst as required and can not carry out independently regulating and changing catalyst flow on demand, to give full play to the activity of catalyzer, improve the utilization ratio of catalyzer, it is to increase reforming conversion and receipts rate.
In order to realize above-mentioned purpose, the utility model provides a kind of hydrocarbon class continuous reformer, and this device comprises at least three reforming reactors 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 three reforming reactors are divided into the first group reaction device and the 2nd group reaction device, first group reaction device comprises all reforming reactors except last reforming reactor, and the 2nd group reaction device is last reforming reactor described; Described first group reaction device and the 2nd group reaction device are connected in parallel by catalyst transport passage with between revivifier; According to the reaction mass entrance of described device to the direction of reacting product outlet, by catalyst transport Tandem between the catalyst outlet of a rear reforming reactor and the catalyst inlet of a front reforming reactor in described first group reaction device, the catalyst outlet of initial reactor and the catalyst inlet of end reactor in described first group reaction device pass through catalyst transport expanding channels with revivifier.
Preferably, this device is set to: be opportunity independent controlled from every group reaction device to the operational throughput of the reclaimable catalyst of described revivifier and/or conveying, and from described revivifier to the operational throughput of the regenerated catalyst of every group reaction device and/or conveying opportunity be independent controlled.
Preferably, this device also comprises a regenerated catalyst reprocessing and a distribution system RCTS and reclaimable catalyst reprocessing and distribution system WCTS; The catalyst inlet of RCTS and the catalyst outlet UNICOM of revivifier, the catalyst outlet of RCTS and the catalyst inlet UNICOM of every group reaction device; The catalyst inlet of WCTS and the catalyst outlet UNICOM of every group reaction device, the catalyst outlet of WCTS and the catalyst inlet UNICOM of revivifier.
Preferably, the catalyst transport passage that the catalyst outlet of every group reaction device promotes blower fan by being provided with reclaimable catalyst is connected with the catalyst inlet of reclaimable catalyst reprocessing with distribution system WCTS, reclaimable catalyst reprocessing is connected with the catalyst inlet of revivifier by tremie pipe with the catalyst outlet of distribution system WCTS, and described WCTS is divided into low pressure area, top and high pressure area, bottom; The catalyst inlet of every group reaction device is connected with the catalyst outlet of regenerated catalyst reprocessing with distribution system RCTS by catalyst transport passage, and the catalyst transport passage that the catalyst outlet of revivifier promotes blower fan by being provided with regenerated catalyst is connected with the catalyst inlet of regenerated catalyst reprocessing with 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 revivifier; The position of the catalyst outlet of regenerated catalyst 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 process furnace.
Preferably, this device comprises four reforming reactors and a revivifier, namely the first reforming reactor, the 2nd reforming reactor, tri-reforming device, the 4th reforming reactor and revivifier, described first group reaction device comprises the first reforming reactor, the 2nd reforming reactor and tri-reforming device, and described 2nd group reaction device is the 4th reforming reactor.
Continuous reformer of the present utility model can make catalyzer parallel connection and serial connection circulate in combination conveying, making to enter the third and fourth two difficulties, to carry out the catalyzer in the reactor reacted be all just regenerated " fresh " catalyzer, and the reaction carried 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 counter flow series, reaction impact is less, adopt the circulating conveyor that this kind of catalyzer parallel connection and serial connection of the present utility model combines, make flow process relatively simple, the average coke content of reactor is low, the effect of catalyzer more can be not fully exerted.
The reforming reactor that the utility model combines by providing series and parallel connections is to change the circulation mode of movement of catalyzer between multiple reforming reactor, thus overcomes the shortcoming that in the technology of existing industrialization, each catalyst reactor activity can not give full play to. The catalyzer making to enter the reactant in latter two reactor all higher with just regenerated activity contacts, bed medial temperature about 5～10 DEG C can be reduced, such that it is able to reduce the side reactions such as hydrocracking, product yield about 1% can be increased compared with the continuous reformer of existing industrialization, and the long-pending charcoal on catalyzer can be reduced, the life-span of extending catalyst. The catalyst recirculation amount entering every group reaction device can regulate as required, thus optimizes reaction and regeneration condition, it is to increase catalyzer service efficiency.
Other feature and advantage of the present utility model are described in detail in embodiment part subsequently.
Accompanying drawing explanation
Accompanying drawing be used to provide to this use novel it is further understood that and form the part of specification sheets, be used from explanation the utility model with embodiment one below, but do not form restriction of the present utility model. In the accompanying drawings:
Fig. 1 is the schematic diagram of a kind of embodiment of hydrocarbon class continuous reformer of the present utility model.
Description of reference numerals
1 reaction feed/product interchanger 2 first reaction heating furnace
3 first reforming reactors (one is anti-) 4 the 2nd reaction heating furnace
5 the 2nd reforming reactor (two is anti-) 6 the 3rd reaction heating furnaces
7 tri-reforming devices (three is anti-) 8 the 4th reaction heating furnace
9 the 4th reforming reactor (four is anti-) 10 1 anti-top hoppers
11 2 anti-top hopper 12 3 anti-top hoppers
13 4 anti-top hoppers 14 1 are counter cushions hopper
15 2 instead cushion hopper 16 revivifier
17 regenerated catalyst reprocessing and distribution system (RCTS)
18 reclaimable catalyst reprocessing and distribution system (WCTS)
19 regenerated catalysts promote blower fan 20 reclaimable catalyst and promote blower fan
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in detail. Should be understood that, embodiment described herein, only for instruction and explanation of the utility model, is not limited to the utility model.
The utility model provides a kind of hydrocarbon class continuous reformer, and this device comprises at least three reforming reactors and at least one catalyst regenerator, is 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 three reforming reactors are divided into the first group reaction device and the 2nd group reaction device, first group reaction device comprises all reforming reactors except last reforming reactor, and the 2nd group reaction device is last reforming reactor described; Described first group reaction device and the 2nd group reaction device are connected in parallel by catalyst transport passage with between revivifier; According to the reaction mass entrance of described device to the direction of reacting product outlet, by catalyst transport Tandem between the catalyst outlet of a rear reforming reactor and the catalyst inlet of a front reforming reactor in described first group reaction device, the catalyst outlet of initial reactor and the catalyst inlet of end reactor in described first group reaction device pass through catalyst transport expanding channels with revivifier.
According to hydrocarbon class 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 3～6 series connection, it is preferable to 3～4 series connection; For making, the reclaimable catalyst through reacting inactivation realizes cyclic regeneration to described revivifier, comprise burn, oxychlorination, the technique such as drying (or roasting) device, the reclaimable catalyst activity recovery making carbon content high, the quantity of revivifier preferably one, it is also possible to arrange one more for subsequent use.
According to a kind of embodiment of the present utility model, described hydrocarbon class continuous reformer can also comprise a regenerated catalyst reprocessing and a distribution system RCTS and reclaimable catalyst reprocessing and distribution system WCTS; The catalyst inlet of RCTS and the catalyst outlet UNICOM of revivifier, the catalyst outlet of RCTS and the catalyst inlet UNICOM of every group reaction device; The catalyst inlet of WCTS and the catalyst outlet UNICOM of every group reaction device, the catalyst outlet of WCTS and the catalyst inlet UNICOM of revivifier.Described regenerated catalyst reprocessing and distribution system RCTS may be used for regenerated catalyst is carried out dust elutriation, reduction and reallocation, then to be delivered to respectively in each group of 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 being mixed by reclaimable catalyst, dust elutriation and locking transformation, are then delivered to revivifier by tremie pipe and regenerate. By arranging RCTS and WCTS, it is possible to better regenerated catalyst or reclaimable catalyst to be carried out pipage control 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 the utility model. Such as, reaction mass passage can comprise line of pipes and necessary pumping equipment or analogue; Temperature required in order to make reaction mass reach reaction, the material channel of each reforming reactor front end can arrange process furnace. Equally, such as, catalyst transport passage can comprise catalyst transport pipeline, for reclaimable catalyst is promoted blower fan from the reclaimable catalyst often organizing reforming reactor and rising to WCTS or revivifier, and for the regenerated catalyst that the catalyzer after regeneration rises to RCTS or each group reforming reactor from revivifier is promoted blower fan etc.
According to a kind of embodiment of the present utility model, this hydrocarbon class continuous reformer can comprise four reforming reactors and a revivifier, i.e. the first reforming reactor 3, the 2nd reforming reactor 5, tri-reforming device 7, the 4th reforming reactor 9 and revivifier 16, described first group reaction device comprises the first reforming reactor 3, the 2nd reforming reactor 5 and tri-reforming device 7, and described 2nd group reaction device is the 4th reforming reactor 9. More specifically, this device can also comprise reaction feed/product interchanger 1, first reaction heating furnace 2, the 2nd reaction heating furnace 4, the 3rd reaction heating furnace 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, two anti-buffering hopper 15, regenerated catalyst reprocessing and distribution system RCTS17, reclaimable catalyst reprocessing and distribution system WCTS18, reclaimable catalyst lifting blower fan 20 and regenerated catalyst lifting blower fan 19. As shown in Figure 1.
According to a kind of embodiment of the present utility model, described reaction feed/product interchanger 1, first reaction heating furnace 2, first reforming reactor 3, the 2nd reaction heating furnace 4, the 2nd reforming reactor 5, the 3rd reaction heating furnace 6, tri-reforming device 7, the 4th reaction heating furnace 8 and the 4th reforming reactor 9 are connected by reaction mass Tandem successively, and the 4th reforming reactor 9 is connected with reaction feed/product interchanger 1 again by reaction mass passage. Reactor operating pressure by high to Low order is: the first reforming reactor 3, the 2nd reforming reactor 5, tri-reforming device 7 and the 4th reforming reactor 9. First and the 4th reforming reactor 3, the catalyst transport pipeline that the catalyst outlet of 9 promotes blower fan 20 by being provided with reclaimable catalyst is connected with WCTS18, WCTS18 is connected with revivifier 16 by 1 tremie pipe, revivifier 16 is connected with RCTS17 with the catalyst transport pipeline being provided with regenerated catalyst lifting blower fan 19 by 1 tremie pipe successively, RCTS17 respectively and is positioned at the third and fourth reforming reactor 7 by 1 tremie pipe, the three of 9 catalyst inlets anti-top anti-with four hopper 12,13 is connected.Tri-reforming device 7 instead cushions hopper 15 by two and is connected with two anti-top hoppers 11 of the 2nd reforming reactor 5 catalyst inlet, and the 2nd reforming reactor 5 is connected with an anti-top hopper 10 of the first reforming reactor catalyst inlet by an anti-buffering hopper 14.
According to another embodiment of the present utility model, described WCTS18 can be divided into low pressure area, top and high pressure area, bottom; The object arranging high pressure area is when reclaimable catalyst is after low pressure area processes and enters high pressure area, and owing to pressure in the pressure ratio revivifier of high pressure area is big, catalyzer can flow in revivifier automatically.
Below in conjunction with accompanying drawing 1, the working process of a kind of embodiment of the present utility model is described. Being long-time commerical test due to what carry out, wherein said various process conditionss allow the fluctuation of approximately ± 10%.
As shown in Figure 1, reaction feed in reaction feed/product interchanger 1 with reaction product heat exchange after successively through the first reaction heating furnace 2, first reforming reactor 3, 2nd reaction heating furnace 4, 2nd reforming reactor 5, 3rd reaction heating furnace 6, tri-reforming device 7, 4th reaction heating furnace 8 and the 4th reforming reactor 9, reaction product is left reactor 9 and is separated with reaction feed heat exchange and then to follow-up tripping device in reaction feed/product interchanger 1, wherein, first, 2nd and tri-reforming device be called the first group reaction device, 4th reforming reactor is called the 2nd group reaction device. reaction mass produces pressure in flow process and falls, and reactor operating pressure by high to Low order is: the first reforming reactor 3, the 2nd reforming reactor 5, tri-reforming device 7 and the 4th reforming reactor 9. catalyzer after revivifier 16 regenerates promotes blower fan 19 nitrogen by regenerated catalyst and rises to RCTS17 from revivifier 16. first carrying out the dust elutriation of catalyzer in RCTS17, then the catalyzer after removing dust is reduced by reusable heat hydrogen, and the nitrogen after removing dust is delivered to regenerated catalyst and promoted blower fan 19 as regenerated catalyst lifting nitrogen circulation use. the pressure of RCTS17 is higher than the first group reaction device and the 2nd group reaction device, i.e. three anti-top hoppers 12, tri-reforming device 7, four anti-top hopper 13 and the 4th reforming reactor 9, catalyzer after reduction enters the top hopper 12 of each group reaction device respectively by gravity by 2 tremie pipes, 13, enter in corresponding reactor 7,9 by gravity again and carry out chemical reaction. the catalyzer reacting complete from reactor 7 instead cushions in hopper 15 by rising to two with hydrogen, then is entered in two anti-top hoppers 11 by tremie pipe by gravity, then enters in reactor 5 and reacts. the catalyzer hydrogen reacting complete from reactor 5 rises to one and instead cushions in hopper 14, then is entered in an anti-top hopper 10 by tremie pipe by gravity, then enters in reactor 3 and reacts.
Used in each group reaction device is all the catalyzer of just regenerated high reactivity. Catalyst flow amount control device can be set on described tremie pipe or top hopper, control even to dam to realize the flow to the regenerated catalyst entered in each group reaction device. Promote blower fan 20 nitrogen with reclaimable catalyst and reclaimable catalyst is promoted, from each group reaction device i.e. the first reforming reactor 3 and the 4th reforming reactor 9, the low pressure area, top being delivered to WCTS18 respectively, the working pressure of low pressure area, WCTS18 top is lower than the first reforming reactor 3 and the 4th reforming reactor 9, it is all independent for promoting conveying from every group reaction device to the catalyzer of WCTS, and it is controlled for promoting operational throughput, it is possible to change the lifting operational throughput of reclaimable catalyst as required.In the low pressure area, top of WCTS18, first catalyzer is mixed, and then carry out the dust elutriation of catalyzer, nitrogen after removing dust is delivered to reclaimable catalyst and is promoted blower fan 20 as reclaimable catalyst lifting nitrogen circulation use, catalyzer after removing dust carries out locking transformation again, catalyzer after boosting enters the high pressure area, bottom of WCTS18 again, the working pressure of high pressure area is higher than revivifier 16, catalyzer after boosting is delivered to revivifier 16 by tremie pipe and regenerates, the pressure of revivifier 16 is higher than RCTS17, the catalyzer leaving revivifier is promoted to RCTS, so far the delivery cycle of catalyzer is completed.
The present embodiment adopts C6～C12Petroleum naphtha hydrocarbon class carries out the reactions such as cycloalkanes dehydrogenation, cyclization of paraffins dehydrogenation, isomerization and hydrocracking in the hydrogen gas atmosphere. Reaction feed (petroleum naphtha and hydrogen mixture) is after reaction feed/product interchanger 1 heat exchange, successively through the first reaction heating furnace 2, first reforming reactor 3, the 2nd reaction heating furnace 4, the 2nd reforming reactor 5, the 3rd reaction heating furnace 6, tri-reforming device 7, the 4th reaction heating furnace 8 and the 4th reforming reactor 9, after reaction product leaves the 4th reforming reactor 9, with reaction feed heat exchange in reaction feed/product interchanger 1, and then it is separated to follow-up tripping device. First reforming reactor 3 inlet pressure is about 0.56MPa (g), the 2nd reforming reactor 5 inlet pressure is about 0.49MPa (g), tri-reforming device 7 inlet pressure is about 0.42MPa (g), the 4th reforming reactor 9 inlet pressure is about 0.35MPa (g).
The PS-VI continuous reforming catalyst containing noble metal platinum (Pt) and tin (Sn) and other auxiliarys that the catalyzer used is developed for Research Institute of Petro-Chemical Engineering (RIPP). Leave the catalyzer carbon content after revivifier 16 regeneration and substantially it is less than 0.2% (wt), promote blower fan 19 nitrogen by regenerated catalyst and rise to RCTS17 from revivifier 16. First the dust elutriation of catalyzer is carried out in RCTS17, then being reduced by the catalyzer after removing dust with hot hydrogen in RCTS17, the nitrogen after removing dust is delivered to regenerated catalyst and is promoted blower fan 19 as regenerated catalyst lifting nitrogen circulation use. The working pressure of RCTS 0.01～0.08MPa higher than tri-reforming device working pressure, 0.01～0.08MPa lower than revivifier 16. Catalyzer after reduction enters reactor top hopper 12 respectively by gravity after 2 tremie pipes leave RCTS, 13, and then enter corresponding reforming reactor 7 by gravity from reactor top hopper, chemical reaction is carried out in 9, the catalyzer reacting complete in reforming reactor 7 is delivered to reforming reactor 5,3 more successively. Used in each group reaction device is all the catalyzer of just regenerated high reactivity.
Blower fan 20 is promoted by reclaimable catalyst nitrogen respectively from the reforming reactor 3 each group reaction device with reclaimable catalyst, 9 liftings are delivered to low pressure area, WCTS18 top, the working pressure of low pressure area than the 4th low 0.01～0.08MPa of reforming reactor 9, lower than all reactors. Promote conveying from every group reaction device to the catalyzer of WCTS all independently to carry out, the catalyzer that can change each group reaction device as required promotes operational throughput, reclaimable catalyst in single group or many group reactions device can also be promoted separately conveying, it is possible to carry out the circulation conveying of catalyzer flexibly. First carrying out the mixing of catalyzer in low pressure area, WCTS18 top, and then carry out the dust elutriation of catalyzer, the nitrogen after removing dust is delivered to reclaimable catalyst and is promoted blower fan 20 as reclaimable catalyst lifting nitrogen circulation use.Catalyzer after removing dust carries out locking transformation again, and the catalyzer after boosting enters the high pressure area, bottom of WCTS18 again, the working pressure of high pressure area, bottom about 0.01～0.08MPa higher than revivifier 16. The reclaimable catalyst of high pressure area is delivered to revivifier 16 by tremie pipe and regenerates, and the working pressure of revivifier is about 0.65MPa (g), and the catalyzer after regeneration promotes and is delivered to RCTS17, completes the circulation of catalyzer.
Reaction mass carries out reacting in the reactor all can make long-pending charcoal on catalyst surface, leave the coke content on the catalyzer of reactor than entering the high of reactor, for the process of series connection conveying, carbon deposited catalyst to be continued the reactor entered below, therefore, its coke content also can constantly accumulate, more coke content toward rear catalyst is more high, activity also constantly reduces, existing CONTINUOUS REFORMER adopts this kind of series connection mode of movement exactly, its catalyst recirculation makes the catalyst activity in downstream reactor lower than the reactor of upstream, and the activity of catalyzer can not give full play to. Based on the mode of the circulation conveying that the technique employing catalyzer series-parallel connection of continuous reformer of the present utility model combines, the catalyzer entering every group reaction device is made to be all just regenerated " fresh " catalyzer, the average coke content of reactor is low, and the effect of catalyzer more can be not fully exerted. The catalyzer entering the reactant in latter two reactor all higher with just regenerated activity contacts, bed medial temperature about 5～10 DEG C can be reduced, such that it is able to reduce the side reactions such as hydrocracking, product yield about 1% can be increased compared with the CONTINUOUS REFORMER technology of existing industrialization, and the long-pending charcoal on catalyzer can be reduced, the life-span of extending catalyst. The catalyst recirculation amount entering every group reaction device can regulate as required, thus optimizes reaction and regeneration condition, it is to increase catalyzer service efficiency.
Table 1 list in the present embodiment respectively according to the utility model (catalyzer series-parallel connection circulation conveying) and conventionally (conveying of catalyzer following current series circulation) carry out the test-results of three groups of controlled trials of hydrocarbon class CONTINUOUS REFORMER.
Technique based on continuous reformer described in the utility model has the following advantages compared with the technique of the continuous reformer based on existing industrialization from the results shown in Table 1:
1, the catalyzer entering the 3rd, the 4th reforming reactor based on the technique of continuous reformer described in the utility model is all just regenerated not containing the live catalyst of long-pending charcoal, activity is the highest, in identical reaction severity condition (reaction product reach identical RON value), compared with the CONTINUOUS REFORMER of existing industrialization, the temperature in decline 3～5 DEG C of each reactor.
2, when identical reaction severity, the technique based on continuous reformer described in the utility model declines than the continuous reforming process average reaction temperature of existing industrialization so that the average long-pending charcoal rate on catalyzer 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, based on continuous reformer described in the utility model technique with adopt existing continuous reformer technique compared with, annual increasing gasoline yield 0.7～1.1 ten thousand tons, increase income about 2100～3,300 ten thousand yuan, volume increase hydrogen 720～1700 tons, increases income about 720～1,700 ten thousand yuan.
In above-mentioned comparative example, adopting identical air speed and identical catalyst filling ratio based on the technique of continuous reformer described in the utility model and the operating mode of existing industrial continuous reforming process, namely operating mode based on the technique of continuous reformer described in the utility model is not optimized. If optimizing the reaction conditions (such as catalyst filling ratio etc.) of the technique based on continuous reformer described in the utility model, then can reduce catalyst filling amount or improve liquid yield further, it is to increase benefit.
Table 1
Claims (7)
1. a hydrocarbon class continuous reformer, this device comprises at least three reforming reactors 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 three reforming reactors are divided into the first group reaction device and the 2nd group reaction device, first group reaction device comprises all reforming reactors except last reforming reactor, and the 2nd group reaction device is last reforming reactor described;
Described first group reaction device and the 2nd group reaction device are connected in parallel by catalyst transport passage with between revivifier;
According to the reaction mass entrance of described device to the direction of reacting product outlet, by catalyst transport Tandem between the catalyst outlet of a rear reforming reactor and the catalyst inlet of a front reforming reactor in described first group reaction device, the catalyst outlet of initial reactor and the catalyst inlet of end reactor in described first group reaction device pass through catalyst transport expanding channels with revivifier.
2. hydrocarbon class continuous reformer according to claim 1, it is characterized in that: this device is set to: be opportunity independent controlled from every group reaction device to the operational throughput of the reclaimable catalyst of described revivifier and/or conveying, and from described revivifier to the operational throughput of the regenerated catalyst of every group reaction device and/or conveying opportunity be independent controlled.
3. hydrocarbon class continuous reformer according to claim 1, it is characterised in that: this device also comprises a regenerated catalyst reprocessing and a distribution system RCTS and reclaimable catalyst reprocessing and distribution system WCTS; The catalyst inlet of RCTS and the catalyst outlet UNICOM of revivifier, the catalyst outlet of RCTS and the catalyst inlet UNICOM of every group reaction device; The catalyst inlet of WCTS and the catalyst outlet UNICOM of every group reaction device, the catalyst outlet of WCTS and the catalyst inlet UNICOM of revivifier.
4. hydrocarbon class continuous reformer according to claim 3, it is characterized in that: the catalyst transport passage that the catalyst outlet of every group reaction device promotes blower fan by being provided with reclaimable catalyst is connected with the catalyst inlet of reclaimable catalyst reprocessing with distribution system WCTS, reclaimable catalyst reprocessing is connected with the catalyst inlet of revivifier by tremie pipe with the catalyst outlet of distribution system WCTS, and described WCTS is divided into low pressure area, top and high pressure area, bottom; The catalyst inlet of every group reaction device is connected with the catalyst outlet of regenerated catalyst reprocessing with distribution system RCTS by catalyst transport passage, and the catalyst transport passage that the catalyst outlet of revivifier promotes blower fan by being provided with regenerated catalyst is connected with the catalyst inlet of regenerated catalyst reprocessing with distribution system RCTS.
5. hydrocarbon class 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 revivifier;The position of the catalyst outlet of regenerated catalyst reprocessing and distribution system RCTS is higher than the position of the catalyst inlet of each group reaction device.
6. hydrocarbon class 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 process furnace.
7. according to hydrocarbon class continuous reformer described in any one in claim 1～6, it is characterized in that: this device comprises four reforming reactors and a revivifier, i.e. the first reforming reactor (3), the 2nd reforming reactor (5), tri-reforming device (7), the 4th reforming reactor (9) and revivifier (16), described first group reaction device comprises the first reforming reactor (3), the 2nd reforming reactor (5) and tri-reforming device (7), and described 2nd group reaction device is the 4th reforming reactor (9).
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114286853A (en) * | 2019-08-26 | 2022-04-05 | 环球油品有限责任公司 | Device for catalytic reforming of hydrocarbons with flow distributor and method for reforming of hydrocarbons |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114286853A (en) * | 2019-08-26 | 2022-04-05 | 环球油品有限责任公司 | Device for catalytic reforming of hydrocarbons with flow distributor and method for reforming of hydrocarbons |
| CN114286853B (en) * | 2019-08-26 | 2024-05-31 | 环球油品有限责任公司 | Apparatus for catalytically reforming hydrocarbons with flow distributor and method for reforming hydrocarbons |
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