CN117946736A - Device and process for reforming hydrocarbons in moving bed - Google Patents
Device and process for reforming hydrocarbons in moving bed Download PDFInfo
- Publication number
- CN117946736A CN117946736A CN202211292058.9A CN202211292058A CN117946736A CN 117946736 A CN117946736 A CN 117946736A CN 202211292058 A CN202211292058 A CN 202211292058A CN 117946736 A CN117946736 A CN 117946736A
- Authority
- CN
- China
- Prior art keywords
- reactor
- catalyst
- nth
- regenerator
- enters
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000002407 reforming Methods 0.000 title claims abstract description 58
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 48
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 36
- 230000008569 process Effects 0.000 title claims abstract description 31
- 239000003054 catalyst Substances 0.000 claims abstract description 151
- 238000006243 chemical reaction Methods 0.000 claims abstract description 100
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 38
- 238000007599 discharging Methods 0.000 claims abstract description 30
- 239000000463 material Substances 0.000 claims abstract description 28
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 23
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 23
- 238000010438 heat treatment Methods 0.000 claims description 37
- 239000000047 product Substances 0.000 claims description 32
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 31
- 239000001257 hydrogen Substances 0.000 claims description 31
- 229910052739 hydrogen Inorganic materials 0.000 claims description 31
- 238000006722 reduction reaction Methods 0.000 claims description 19
- 230000009467 reduction Effects 0.000 claims description 15
- 238000011069 regeneration method Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 14
- 230000008929 regeneration Effects 0.000 claims description 13
- 239000011949 solid catalyst Substances 0.000 claims description 13
- 230000008021 deposition Effects 0.000 claims description 12
- 239000002994 raw material Substances 0.000 claims description 12
- 238000007789 sealing Methods 0.000 claims description 12
- 239000007795 chemical reaction product Substances 0.000 claims description 9
- 239000007789 gas Substances 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 238000005194 fractionation Methods 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 claims description 2
- 239000000376 reactant Substances 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 22
- 239000007788 liquid Substances 0.000 abstract description 7
- 230000000052 comparative effect Effects 0.000 description 13
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 10
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 10
- 239000003921 oil Substances 0.000 description 8
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 150000001335 aliphatic alkanes Chemical class 0.000 description 6
- 238000006356 dehydrogenation reaction Methods 0.000 description 6
- 238000001833 catalytic reforming Methods 0.000 description 5
- 238000004517 catalytic hydrocracking Methods 0.000 description 4
- 239000007809 chemical reaction catalyst Substances 0.000 description 4
- 238000006317 isomerization reaction Methods 0.000 description 4
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 4
- 239000012188 paraffin wax Substances 0.000 description 4
- 238000012958 reprocessing Methods 0.000 description 4
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000002671 adjuvant Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 229910000510 noble metal Inorganic materials 0.000 description 3
- 229910052697 platinum Inorganic materials 0.000 description 3
- 238000006057 reforming reaction Methods 0.000 description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000036632 reaction speed Effects 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- 101100123718 Neurospora crassa (strain ATCC 24698 / 74-OR23-1A / CBS 708.71 / DSM 1257 / FGSC 987) pda-1 gene Proteins 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004566 building material Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000007327 hydrogenolysis reaction Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 239000005061 synthetic rubber Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- 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
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention belongs to the field of hydrocarbon reforming, and relates to a device and a process for reforming hydrocarbon by a moving bed. The device comprises a plurality of reactors and regenerators; the reaction materials sequentially flow through the first reactor and the second reactor to the z-th reactor, and the reactors are sequentially connected in series through reaction material channels; the catalyst is circulated between the regenerator and the reactor: the catalyst discharging pipeline of the regenerator is connected with the nth reactor and then is connected with the z-th reactor, then is sequentially connected with other reactors except the nth reactor in a forward and reverse mode, and finally is connected with the first reactor; the first reactor is provided with a catalyst discharging pipeline at the lower part of the first reactor, and is connected with a catalyst feeding pipeline of the regenerator. The invention reduces the total carbon deposit amount of the catalyst and improves the utilization efficiency of the catalyst, the reforming conversion rate and the liquid yield by flexibly adjusting the conveying path of the regenerated high-activity catalyst.
Description
Technical Field
The invention belongs to the field of hydrocarbon reforming, and particularly relates to a device and a process for reforming hydrocarbons in a moving bed.
Background
Reforming is an important basic process in the field of oil refining chemical industry, and is a key technology for oil refining transformation. It is a process for converting naphthene and alkane in naphtha into aromatic hydrocarbon and by-producing hydrogen under the conditions of a certain temperature, pressure and presence of hydrogen and catalyst. Reforming is a major source of aromatics, high octane gasoline, and hydrogen. Aromatic hydrocarbons in the reformed oil are mainly benzene, toluene and xylene, are important basic organic chemical raw materials, and are widely used in the fields of synthetic fibers, synthetic resins, synthetic rubber, medicines, pesticides, building materials, coatings and the like, and about 87% of the xylene and 38% of the benzene in the world are derived from catalytic reforming; the catalytic reforming generated oil is used as a high-quality clean gasoline blending component, accounts for about 30% of the whole-plant gasoline blending, has the characteristics of liquid yield up to 82-89% (v), octane number more than 100, olefin content generally lower than 1% and no sulfur basically, and is the largest source of the high-octane number blending component in a gasoline pool; the hydrogen consumption of the refinery is large and is 1.5-3% of the crude oil processing amount, and more than 50% of the hydrogen consumption of the refinery is provided by the reformer.
Reforming includes reforming reactions, product separation, and catalyst regeneration processes. There are three main types depending on the catalyst regeneration mode: semi-regenerative reforming, cyclic regenerative reforming, and continuous reforming. The semi-regenerative reforming adopts a fixed bed reactor, carbon deposit on the catalyst in the reactor is increased along with the increase of the reaction time, the activity is reduced, and the device is stopped until a certain time is needed to regenerate the catalyst. Compared with the other two types of processes, the reaction severity is low, the reaction pressure and the hydrogen-oil ratio are high, and the octane number of the product is low. The cyclic regeneration reforming adopts a fixed bed reactor, but one reactor is arranged more than the half regeneration reforming, and one reactor is switched out in turn to regenerate the catalyst in the operation process. Compared with the semi-regeneration process, the method has longer operation period and high reaction severity. The continuous reforming adopts a moving bed reactor, and a catalyst circulation and continuous regeneration system is arranged. The catalyst moves circularly between the reactor and the regenerator, and the carbon deposition catalyst is regenerated in the regenerator and then conveyed back to the reactor, so that the catalyst activity can be fully maintained.
The reforming reaction has more types, and the reactions which are beneficial to improving the octane number and the aromatic hydrocarbon yield mainly comprise naphthene dehydrogenation, alkane dehydrocyclization and isomerization reactions; the side reactions mainly comprise hydrogenolysis and hydrocracking reactions of saturated hydrocarbon. The ease of these reactions varies greatly, with naphthene dehydrogenation being the most readily occurring reaction and the average reaction rate being 30 times that of the alkane dehydrocyclization reaction. The reforming reaction is a strong endothermic reaction, the material reaction causes a temperature drop, and in order to maintain the desired reaction temperature, it is usually carried out in 4 stages, the material being heated to the desired reaction temperature in a heating furnace before each reactor. The reaction materials flow from one reaction to four reactions in turn, the front reactor mainly carries out the reactions with high reaction speed such as naphthene dehydrogenation and the like, and the rear reactor mainly carries out the reactions with low reaction speed such as paraffin dehydrocyclization and the like. In the traditional reforming technology, the regenerated catalyst with high activity firstly enters a reaction, and sequentially passes through four reactors. Namely, the reaction which is easiest to be carried out in the first reaction, but the catalyst in the reactor is regenerated catalyst with highest activity; the reaction which is most difficult to be carried out in the four reactions occurs, but the catalyst in the reactor has high carbon content and relatively worst activity, and the reaction difficulty is not matched with the activity of the catalyst.
The CN105349180A adopts a mode of independently regulating and changing the flow rate of the catalyst according to the requirement to regenerate the high-activity catalyst of each group of reactors, thereby achieving the purposes of fully playing the activity of the catalyst, improving the utilization rate of the catalyst and improving the reforming conversion rate and the product yield. However, the reforming process requires the provision of spent catalyst reprocessing and distribution system WCTS and regenerated catalyst reprocessing and distribution system RCTS, which increases capital and floor space.
Aiming at the problem that the activity state of the catalyst in each reactor is not matched with the reaction difficulty of the catalyst in the traditional reforming reactor, the patent number ZL98117972.X filed in 1998 by Yuan Zhongxun et al is a countercurrent moving bed continuous reforming process patent with the name of < countercurrent moving bed catalytic conversion process of a plurality of reactors >, the flow direction of the catalyst among the reactors is changed, so that the catalyst and the reaction materials flow reversely among the reactors, namely, the reaction materials flow from one reverse to four reverse, the circulation and conveying direction of the regenerated fresh catalyst flows from four reverse to one reverse, the carbon content of the catalyst is gradually increased from four reverse to one reverse, and the activity is gradually reduced. The circulation of the catalyst makes the reaction difficult to carry out utilize a catalyst with higher activity, and the reaction easy to carry out utilizes a catalyst with relatively low activity, so that the problem that the activity state of the catalyst is not matched with the difficulty of the reaction is solved, the reaction condition is optimized, and the product yield is improved.
According to the industrial device carbon deposition research, the catalyst circulation method has the advantages that the proportion of the four-reaction-catalyst carbon deposition to the total carbon deposition is higher than that of the traditional continuous reforming, the four-reaction-catalyst activity is high, the reaction with raw materials is severe, the alkane conversion rate is improved, and meanwhile, the four-reaction-catalyst carbon deposition is increased.
Disclosure of Invention
The invention aims at solving the problems in the prior art and provides a device and a process for reforming hydrocarbons in a moving bed, which enable the activity state of a catalyst to be better matched with the reaction carried out in each reactor, thereby improving the alkane conversion rate and reducing the carbon deposit of the catalyst.
In order to achieve the above object, a first aspect of the present invention provides an apparatus for reforming hydrocarbons in a moving bed, the apparatus comprising a plurality of reactors and regenerators, wherein n is 1 < z, and z is not less than 3; wherein:
The reaction materials sequentially flow through the first reactor and the second reactor to the z-th reactor, and the reactors are sequentially connected in series through reaction material channels; the catalyst moves between the regenerator and the reactor: the catalyst discharging pipeline of the regenerator is connected with the nth reactor and then is connected with the z-th reactor, then is sequentially connected with other reactors except the nth reactor in a forward and reverse mode, and finally is connected with the first reactor; the first reactor is provided with a catalyst discharging pipeline at the lower part of the first reactor, and is connected with a catalyst feeding pipeline of the regenerator.
In a second aspect, the present invention provides a process for moving bed hydrocarbon reforming, the process being carried out using an apparatus for moving bed hydrocarbon reforming, comprising the steps of:
(1) The mixed material of hydrocarbon raw material and hydrogen-containing gas sequentially enters a plurality of reactors, and contacts with a solid catalyst in the reactors;
(2) The catalyst regenerated by the regenerator is firstly conveyed to an nth reactor, then enters a z-th reactor, sequentially enters reactors except the nth reactor in a forward and reverse direction, and finally enters a first reactor;
(3) The carbon deposition catalyst at the bottom of the first reactor is conveyed to a regenerator for regeneration.
According to the invention, the conveying path of the regenerated high-activity catalyst is flexibly adjusted, so that the catalyst activity state in each reactor is matched with the reaction carried out in the reactor, the total carbon deposit amount of the catalyst is reduced, the utilization efficiency of the catalyst is improved, and the reforming conversion rate and the liquid yield are improved.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The foregoing and other objects, features and advantages of the invention will be apparent from the following more particular descriptions of exemplary embodiments of the invention as illustrated in the accompanying drawings wherein like reference numbers generally represent like parts throughout the exemplary embodiments of the invention.
FIG. 1 shows a schematic diagram of an apparatus for moving bed hydrocarbon reforming in one embodiment of the invention.
Figure 2 shows a schematic diagram of an apparatus for moving bed hydrocarbon reforming in another embodiment of the invention.
Description of the reference numerals
E-reaction feed/product heat exchanger, F-first heating device, F-second heating device, F-third heating device, F-fourth heating device, R-first reactor, R-second reactor, R-third reactor, R-fourth reactor, H-regenerator, da-first buffer tank, da-second buffer tank, da-third buffer tank, da-fourth buffer tank, db-first upper hopper, db-second upper hopper, db-third upper hopper, db-fourth upper hopper, dc-first lower hopper, dc-second lower hopper, dc-third lower hopper, dc-fourth lower hopper, de-reduction tank, df-separation hopper, dg-metering tank, dh-sealing tank, T-first riser, T-second riser, T-third riser, T-fourth riser, T-regenerator riser, G-first lock pressure pipe, G-second lock pressure pipe, G-third lock pressure pipe, G-fourth lock pressure pipe.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the preferred embodiments of the present invention are described below, it should be understood that the present invention may be embodied in various forms and should not be limited to the embodiments set forth herein.
In order to achieve the above object, a first aspect of the present invention provides an apparatus for reforming hydrocarbons in a moving bed, the apparatus comprising a plurality of reactors R 1……Rn……Rz and a regenerator H, wherein n is 1 < z, and z is not less than 3; wherein:
The reaction materials sequentially flow through the first reactor R 1 and the second reactor R 2 to the z-th reactor R z, and the reactors are sequentially connected in series through reaction material channels; the catalyst is circulated between the regenerator and the reactor: the regenerator H is provided with a regenerator catalyst discharging pipeline and a regenerator catalyst feeding pipeline, wherein the regenerator catalyst discharging pipeline is connected with an nth reactor R n and then is connected with a z-th reactor R z, then is sequentially connected with other reactors except an nth reactor R n in a forward and reverse direction, and finally is connected with a first reactor R 1; the first reactor R 1 is provided with a first reactor lower catalyst discharge line, which is connected to the regenerator catalyst feed line.
In the invention, at least three reactors and one regenerator are arranged in series. The mixed material of hydrocarbon raw material and hydrogen-containing gas is subjected to heat exchange through a reaction feeding/product heat exchanger E 1, sequentially passes through a first heating device F 1 and then enters a first reactor R 1, and contacts with a solid catalyst in the reactor; the reaction products sequentially pass through subsequent heating equipment, enter corresponding reactors, contact with solid catalysts in the reactors until the reaction products leave the last reactor, exchange heat with the reaction feed in a reaction feed/product heat exchanger E 1, and then enter a subsequent re-contact and fractionation system.
The catalyst adopts flexible and variable flow sequence between the regenerator H and a plurality of reactors connected in series, the regenerated fresh catalyst is firstly conveyed to any front reactor except the last reactor, then enters the last reactor, and is sequentially and reversely conveyed to other reactors from the last reactor from back to front. The carbon deposited catalyst after passing through all the reactors is conveyed back to the regenerator from the first reactor, and the circulation process of the catalyst between the reactors is completed.
The present invention saves investment by at least 10% and land by at least 20% without the need for an independent control system for each reactor and regenerator, without the need for spent catalyst reprocessing and distribution system WCTS, and with regenerated catalyst reprocessing and distribution system RCTS.
According to the present invention, preferably, the apparatus further comprises a reaction feed/product heat exchanger E 1, and a heating device corresponding to each reactor, wherein a reaction feed line is connected to the reaction feed/product heat exchanger E 1 and then sequentially connected to the first heating device F 1 and the first reactor R 1 … …, the n-th heating device F n and the n-th reactor R n … …, the z-th heating device F z and the z-th reactor R z;
The z-th reactor R z is provided with a z-th reactor product discharge line and a z-th reactor lower catalyst discharge line, and the z-th reactor product discharge line is connected with the reaction feed/product heat exchanger E 1 and then is connected with a subsequent system.
According to the invention, preferably, the upper part of each reactor is provided with a buffer tank corresponding to the reactor, and the lower part of each reactor is sequentially provided with a lower hopper and a lifter corresponding to the buffer tank;
The upper part of the nth reactor R n is also provided with a reduction tank De 1 and an nth pressure locking pipe G n, and the nth pressure locking pipe G n is arranged between the reduction tank De 1 and the buffer tank;
The upper parts of the reactors except the nth reactor R n are also provided with corresponding locking pipes and upper hoppers, and the locking pipes are respectively arranged between the corresponding upper hoppers and the buffer tanks;
the upper part of the regenerator (H) is provided with a separation hopper (Df 1) and a metering tank (Dg 1), and the lower part of the regenerator (H) is provided with a sealing tank (Dh 1) and a regenerator lifter (T H);
The regenerator catalyst discharging pipeline is sequentially connected with a sealing tank Dh 1, a regenerator lifter T H, an nth buffer tank Da n, an nth pressure locking pipe G n, a reduction tank De 1 and an nth reactor R n, the nth reactor R n is provided with an nth reactor lower catalyst discharging pipeline, the nth reactor lower catalyst discharging pipeline is sequentially connected with an nth lower hopper Dc n, an nth lifter T n, a z buffer tank Da z, a z pressure locking pipe G z, a z upper hopper De Z and a z reactor R z, and the lower catalyst discharging pipeline of the z reactor is sequentially connected with the z lower hopper Dc z, the z lifter T z and then sequentially and reversely connected with buffer tanks, pressure locking pipes, upper hoppers and reactors corresponding to other reactors except the nth reactor R n;
The lower catalyst discharging pipeline of the first reactor is sequentially connected with a first lower hopper Dc 1, a first lifter T 1, a separation hopper Df 1 and a metering tank Dg 1, and the metering tank Dg 1 is connected with a regenerator H through a regenerator catalyst feeding pipeline;
the corresponding locking pressure pipe of each reactor is independently a light pipe or a locking pressure system with a special structure.
In the invention, the reduction tank De 1 is arranged above the reactor R n into which the fresh catalyst enters, hydrogen is introduced, and the reduction reaction of the catalyst metal center is carried out at 400-480 ℃ to realize the recovery of the catalyst performance. The locking tube G can adopt a light pipe or a locking system with a special structure. The catalyst overcomes the reverse differential pressure flow of 20-300kPa through the pressure locking pipe. The reactor is lifted to the upper part of the last reactor R Z through a corresponding lifter T n to correspond to a z-th buffer tank Da Z, the reactor is directly fed into a corresponding reactor R Z from a z-th buffer tank Da Z, and a pressure locking pipe and an upper hopper can be optionally arranged.
According to the invention, preferably, the apparatus comprises four reactors, namely a first reactor R 1, a second reactor R 2, a third reactor R 3 and a fourth reactor R 4, and the regenerator catalyst take-off line is connected first to the second reactor R 2 or the third reactor R 3.
In one embodiment of the invention, the discharging pipeline of the regenerator is connected with the third reactor R 3, and the regenerated fresh catalyst is conveyed to the third reactor, further enters the fourth reactor, is conveyed to the second reactor, and finally enters the first reactor. The spent catalyst is transported from the first reactor to the regenerator, completing the whole catalyst moving bed cycle. In this way, the carbon deposit amount of the four-reaction catalyst is reduced, the catalyst activity state is better matched with the reaction carried out in each reactor, and the alkane conversion rate is improved.
In another aspect, the present invention provides a process for moving bed hydrocarbon reforming, which is carried out using the apparatus for moving bed hydrocarbon reforming, comprising the steps of:
(1) The mixed material of hydrocarbon raw material and hydrogen-containing gas sequentially enters a plurality of reactors R 1……Rn……Rz, and contacts with a solid catalyst in the reactors;
(2) The catalyst regenerated by the regenerator H is firstly conveyed to an nth reactor R n, then enters a z-th reactor R z, sequentially enters reactors except an nth reactor R n in a forward and reverse direction, and finally enters a first reactor R 1;
(3) The carbon deposition catalyst at the bottom of the first reactor R 1 is conveyed to a regenerator H for catalyst regeneration.
According to the invention, preferably, after the heat exchange of the mixed material of the hydrocarbon raw material and the hydrogen-containing gas by the reaction feeding/product heat exchanger E 1, the mixed material is heated by the first heating device F 1, enters the first reactor R 1, contacts with the solid catalyst in the reactor, the reaction product sequentially enters the corresponding reactor by the subsequent heating device, contacts with the solid catalyst in each reactor, and the reaction product of the z-th reactor R z enters the reaction feeding/product heat exchanger E 1 to exchange heat with the mixed material of the hydrocarbon raw material and the hydrogen-containing gas, and then enters the subsequent re-contact and fractionation system.
According to the invention, preferably, the catalyst regenerated by the regenerator H enters a sealing tank Dh 1, is lifted to an nth buffer tank Da n by a regenerator lifter T H, enters a reduction tank De 1 by an nth pressure locking pipe G n, and then enters an nth reactor R n to be contacted with the reaction material of the nth reactor;
The catalyst after contact enters an nth lower hopper Dc n, is lifted to a zth buffer tank Da z through an nth lifter T n, enters a zth upper hopper Db z through a zth locking pressure pipe Gz, then enters a zth reactor R z, is contacted with a z-th reactor reaction material, then enters a zth lower hopper Dc z, is lifted to a zth-1 buffer tank Da z-1 of a zth-1 reactor R z-1 through the zth lifter T z, enters a zth-1 reactor R z-1 through a zth locking pressure pipe G z-1 and a zth-1 upper hopper Db z-1, sequentially forwards, finally enters a 1 st buffer tank Da 1 of a first reactor R 1 except for the nth reactor R n, and enters the 1 st reactor R 1 through the 1 st locking pressure pipe G 1 and the 1 st upper hopper Db 1; when z-1=n, the z-th riser T z lifts the catalyst to the z-2 buffer tank Da z-2 of the z-2 reactor R z-2;
The carbon deposition catalyst at the bottom of the first reactor R 1 enters a first lower hopper Dc 1, is lifted to a separation hopper Df 1 by a first lower lifter T 1, and enters a regenerator H by a metering tank Dg 1 for catalyst regeneration.
According to the invention, the device pressure relationship is preferably as follows:
PDh1＞PH,PDh1＞PTH＞PDan,PDe1＞PDan,PDe1＞PRn,PDcn＞PRn,PTn＞
PDaZ＞PRZ,PDcZ＞PRZ,PTZ＞PDaZ-1,PDbZ-1＞PRZ-1,PDbZ-1＞PDaZ-1,PDcZ-1＞PRZ,PTX＞PDa1,PDb1＞PR1,PDb1＞PDa1,PDc1＞PR1,PT1＞PDf1＞PDg1＞PH; Wherein, when n=2, X is 3; when n > 2, X is 2.
According to the invention, preferably, the first reactor lifter is lifted by nitrogen, and the rest reactor lifters and the regenerator lifters are lifted by hydrogen; all the upper hoppers of the reactors are filled with hydrogen, and the lower hopper Dc 1, the sealing tank Dh 1 and the separating hopper Df 1 of the first reactor are filled with nitrogen; the reduction pot De 1 introduces hydrogen gas, and the reduction reaction of the catalyst metal center is performed at 400-480 ℃.
According to the invention, preferably, the heating devices corresponding to the reactors are independently heated by heating furnaces or electric heaters, and the outlet temperatures of the heating devices are independently 500-550 ℃, preferably 520-545 ℃; the corresponding pressure locking pipes of each reactor independently enable the catalyst to be conveyed to overcome 20-200kPa counter-pressure difference.
The following is further illustrated by the examples:
Example 1
This example was performed using an apparatus as shown in fig. 1, which includes a reaction feed/product heat exchanger E 1, a first reactor R 1, a second reactor R 2, a third reactor R 3, a fourth reactor R 4, a regenerator H, a first heating device F 1, a second heating device F 2, a third heating device F 3, and a fourth heating device F 4; the upper part of the first reactor R 1 is provided with a first buffer tank Da 1, a first pressure locking pipe G 1 and a first upper hopper Db 1, and the lower part is provided with a first lower hopper Dc 1 and a first lifter T 1; the upper part of the second reactor R 2 is provided with a second buffer tank Da 2, a second pressure locking pipe G 2 and a second upper hopper Db 2, and the lower part is provided with a second lower hopper Dc 2 and a second lifter T 2; the upper part of the third reactor R 3 is provided with a third buffer tank Da 3, a third pressure locking pipe G 3 and a reduction tank De 1, and the lower part is provided with a third lower hopper Dc 3 and a third lifter T 3; the upper part of the fourth reactor R 4 is provided with a fourth buffer tank Da 4, and the lower part is provided with a fourth lower hopper Dc 4 and a third lifter T 4; the upper part of the regenerator (H) is provided with a separation hopper (Df 1) and a metering tank (Dg 1), and the lower part of the regenerator (H) is provided with a sealing tank (Dh 1) and a regenerator lifter (T H);
The reaction material/product heat exchanger E 1 is provided with a reaction material feeding pipeline and a reaction material discharging pipeline, the reaction material discharging pipeline is sequentially connected with a first heating device F 1, a first reactor R 1, a second heating device F 2, a second reactor R 2, a third heating device F 3, a third reactor R 3, a fourth heating device F 4 and a fourth reactor R 4, the fourth reactor R 4 is provided with a fourth reactor product discharging pipeline and a fourth reactor lower discharging pipeline, and the fourth reactor product discharging pipeline is connected with the reaction feeding/product heat exchanger E 4;
The regenerator H is provided with a regenerator catalyst discharging pipeline and a regenerator catalyst feeding pipeline, the regenerator catalyst discharging pipeline is sequentially connected with a sealing tank Dh 1, a regenerator lifter T H, a 3 rd buffer tank Da 3, a third locking pressure pipe G 3, a reduction tank De 1 and a third reactor R 3, the third reactor R 3 is provided with a third reactor lower discharging pipeline, the third reactor lower discharging pipeline is sequentially connected with a third lower hopper Dc 3, a third lifter T 3, a fourth buffer tank Da 4 and a fourth reactor R 4, and the fourth reactor lower discharging pipeline sequentially passes through a fourth lower hopper Dc 4, a fourth lifter T 4, a second buffer tank Da 2, a second locking pressure pipe G 2, a second upper hopper Db 2, a second reactor R 2, a second lower hopper Dc 2, a second lifter T 2, a first buffer tank Db 2, a first locking pressure pipe Db 438 and a first reactor R 1; the lower discharging pipeline of the first reactor is sequentially connected with a first lower hopper Dc 1, a first lifter T 1, a separation hopper Df 1 and a metering tank Dg 1, and the metering tank Dg 1 is connected with a regenerator H through a regenerator feeding pipeline.
The process of moving bed hydrocarbon reforming is as follows:
The flow of the reaction mass was as follows: the mixed material of hydrocarbon raw material and hydrogen-containing gas is subjected to heat exchange through a reaction feeding/product heat exchanger E 1, sequentially passes through a first heating device F 1 and then enters a first reactor R 1, and contacts with a solid catalyst in the reactor; the reaction product enters a second heating device F 2 and then enters a second reactor R 2, and contacts with a solid catalyst in the reactor; the reaction product enters a third heating device F 3 and then enters a third reactor R 3, and contacts with a solid catalyst in the reactor; the reaction product enters a fourth heating device F 4 and then enters a fourth reactor R 4, and contacts with a solid catalyst in the reactor; after leaving the fourth reactor, it is subjected to heat exchange with the reaction feed in a reaction feed/product heat exchanger E 1 and then to a subsequent separation unit for separation.
The regenerated catalyst flows as follows: the regenerated catalyst enters a sealing tank Dh 1 from H, is lifted to a third buffer hopper Da 3 by a regenerator lifter TH, enters a reduction tank De 1 by a third pressure locking pipe G 3, further enters a third reactor R 3, contacts with reaction feed in R 3, and enters a third lower hopper Dc 3; is lifted to a fourth buffer hopper Da 4 by a third lifter T 3, enters a fourth reactor R 4, contacts with reaction feed in R 4 and enters a fourth lower hopper Dc 4; lifting to a second buffer hopper Da 2 through a fourth lifter T 4, entering a second upper hopper Db 2 through a second pressure locking pipe G 2, then entering a second reactor R 2, contacting with reaction feed in R 2, and then entering a second lower hopper Dc 2; is lifted to a first buffer hopper Da 1 through a second lifter T 2, enters a first upper hopper Db 1 through a first locking pressure pipe G 1, then enters a first reactor R 1, contacts with reaction feed in R 1, and enters a first lower hopper Dc 1; is lifted to a separation hopper Df 1 by a first lifter T 1, enters a regenerator H by a metering tank Dg 1, and is regenerated in the regenerator H.
The plant pressure relationship is as follows ：PDh1＞PH,PDh1＞PTH＞PDa3,PDe1＞PDa3,PDe1＞PR3,PDc3＞PR3,PT3＞PDa4＞PR4,PDc4＞PR4,PT4＞PDa2,PDb2＞PR2,PDb2＞PDa2,PDc2＞PR2,PT2＞PDa1,PDb1＞PR1,PDb1＞PDa1,PDc1＞PR1,PT1＞PDf1＞PDg1＞PH.
Specifically, the following operating pressures (units MPaG) are respectively: r 1 -first reactor 0.485-0.495, R 2 -second reactor 0.435-0.445, R 3 -third reactor 0.395-0.405, R 4 -fourth reactor 0.345-0.355, H-regenerator 0.407-0.42, da 1 -first buffer tank 0.385-0.395, da 2 -second buffer tank 0.292-0.305, da 3 -third buffer tank 0.377-0.39, da 4 -fourth buffer tank 0.35-0.36, db 1 -first upper hopper 0.49-0.5, db 2 -second upper hopper 0.45-0.46, dc 1 -first lower hopper 0.475-0.485, dc 2 -second lower hopper 0.425-0.435, dc 3 -third lower hopper 0.385-0.35, dc 35-fourth buffer tank 0.35-0.35, db 1 -first upper hopper 0.49-0.45, dc 1 -first lower hopper 0.45-0.45, dc 2 -fourth buffer tank 0.45-35, dc 3 -third buffer tank 0.435, dc 35-fourth buffer tank 0.35-35-0.45, db-fourth buffer tank 0.45-0.45, db 2 -fourth buffer tank 0.45-35-Db.
In this example, the naphtha hydrocarbon is used for the reactions such as naphthene dehydrogenation, paraffin cyclodehydrogenation, isomerization and hydrocracking in a hydrogen atmosphere, and the naphtha may be derived from low-octane straight-run naphtha or hydrogenated naphtha. The hydrogen/oil ratio of the reaction raw material was 2.8, the P/N/A composition was 49.48/37.15/11.46 (wt%), and the feed amount was 260 ten thousand tons/year. The catalyst used was a PS-VI continuous reforming catalyst developed by the institute of petrochemical science (RIPP) and containing the noble metals platinum (Pt) and tin (Sn) and other adjuvants. The carbon deposition of the spent catalyst leaving the first reactor is between 2.8% and 5.8% (wt). And a catalyst regenerator H is arranged, and after the catalyst is regenerated by the H, the carbon content of the catalyst is less than or equal to 0.2% (wt).
Example 2
This example uses the same apparatus and process as example 1.
In this example, the naphtha hydrocarbon is used for the reactions such as naphthene dehydrogenation, paraffin cyclodehydrogenation, isomerization and hydrocracking in a hydrogen atmosphere, and the naphtha may be derived from low-octane straight-run naphtha or hydrogenated naphtha. The hydrogen/oil ratio of the reaction raw material was 2.4, the P/N/A composition was 45.92/45.67/8.41 (wt%), and the feed amount was 260 ten thousand tons/year. The catalyst used was a PS-VI continuous reforming catalyst developed by the institute of petrochemical science (RIPP) and containing the noble metals platinum (Pt) and tin (Sn) and other adjuvants. And a catalyst regenerator H is arranged, and after the catalyst is regenerated by the H, the carbon content of the catalyst is less than or equal to 0.2% (wt).
Example 3
This example was carried out using the apparatus shown in FIG. 2, and differs from example 1 in that the regenerator exit line was first connected to the second reactor R 2.
The process of moving bed hydrocarbon reforming is as follows:
the flow of the reaction mass was identical to that of example 1.
The regenerated catalyst flows as follows: the regenerated catalyst enters a sealing tank Dh 1 from H, is lifted to a second buffer hopper Da 2 by a regenerator lifter TH, enters a reduction tank De 1 by a second pressure locking pipe G 2, further enters a second reactor R 2, contacts with reaction feed in R 2, and enters a second lower hopper Dc 2; is lifted to a fourth buffer hopper Da 4 by a second lifter T 2, enters a fourth reactor R 4, contacts with reaction feed in R 4 and enters a fourth lower hopper Dc 4; is lifted to a third buffer hopper Da 3 through a fourth lifter T 4, enters a third upper hopper Db 3 through a third locking pressure pipe G 3, then enters a third reactor R 3, contacts with reaction feed in R 3, and enters a third lower hopper Dc 3; is lifted to a first buffer hopper Da 1 through a third lifter T 3, enters a first upper hopper Db 1 through a first locking pressure pipe G 1, then enters a first reactor R 1, contacts with reaction feed in R 1, and enters a first lower hopper Dc 1; is lifted to a separation hopper Df 1 by a first lifter T 1, enters a regenerator H by a metering tank Dg 1, and is regenerated in the regenerator H.
The plant pressure relationship is as follows ：PDh1＞PH,PDh1＞PTH＞PDa2,PDe1＞PDa2,PDe1＞PR2,PDc2＞PR2,PT2＞PDa4＞PR4,PDc4＞PR4,PT4＞PDa3,PDb3＞PR3,PDb3＞PDa3,PDc3＞PR3,PT3＞PDa1,PDb1＞PR1,PDb1＞PDa1,PDc1＞PR1,PT1＞PDf1＞PDg1＞PH.
Specifically, the following operating pressures (units MPaG) are respectively: r 1 -first reactor 0.485-0.495, R 2 -second reactor 0.435-0.445, R 3 -third reactor 0.395-0.405, R 4 -fourth reactor 0.345-0.355, H-regenerator 0.407-0.423, da 1 -first buffer tank 0.332-0.345, da 2 -second buffer tank 0.374-0.387, da 3 -third buffer tank 0.295-0.305, da 4 -fourth buffer tank 0.37-0.385, db 1 -first upper hopper 0.49-0.5, db 3 -third upper hopper 0.4-0.41, dc 1 -first lower hopper 0.475-0.485, dc 2 -second lower hopper 0.425-0.435, dc 3 -third lower hopper 0.385-0.35, dc 335-fourth buffer tank 0.37-0.435, db 1 -first upper hopper 0.49-0.45, db 3 -third upper hopper 0.35-0.45, dc 3 -third lower hopper 0.45-35, dc 335-fourth buffer tank 0.45-35, db 1 -first upper hopper 0.45-0.45, dc 3 -third buffer tank 0.45-45-0.45.
In this example, the naphtha hydrocarbon is used for the reactions such as naphthene dehydrogenation, paraffin cyclodehydrogenation, isomerization and hydrocracking in a hydrogen atmosphere, and the naphtha may be derived from low-octane straight-run naphtha or hydrogenated naphtha. The hydrogen/oil ratio of the reaction raw material was 2.3, the P/N/A composition was 45.92/45.67/8.41 (wt%), and the feed amount was 260 ten thousand tons/year. The catalyst used was a PS-VI continuous reforming catalyst developed by the institute of petrochemical science (RIPP) and containing the noble metals platinum (Pt) and tin (Sn) and other adjuvants. The carbon deposition of the spent catalyst leaving the first reactor is between 2.8% and 5.8% (wt). A catalyst regenerator H is arranged, and after the catalyst is regenerated by the H, the carbon content of the catalyst is less than or equal to 0.1% (wt).
Comparative example 1
The hydrocarbon feedstock treated in this comparative example was subjected to the same conventional continuous reforming catalyst circulation sequence as in example 1, except that the catalyst was lifted to the first reactor in the direction of catalyst movement after regeneration, then lifted from the first lifter to the second reactor, then lifted to the fourth reactor in sequence, and then lifted to the regenerator by the fourth lifter, thereby completing the catalyst circulation.
Comparative example 2
The hydrocarbon feedstock treated in this comparative example was identical to example 2 and the flow of the reaction mass was identical to example 2.
The difference from example 2 is that the regenerated catalyst flows as follows: the circulation and conveying direction of the regenerated fresh catalyst sequentially flows from four reverse directions to one reverse direction, and finally the regenerated fresh catalyst is lifted to a regenerator H for catalyst regeneration.
Comparative example 3
The hydrocarbon feedstock treated in this comparative example was subjected to the same conventional continuous reforming catalyst circulation sequence as in example 3, except that the catalyst was moved in the direction of the regenerated catalyst to the first reactor, then to the second reactor from the first lifter, then to the fourth reactor, and then to the regenerator from the fourth lifter, thereby completing the catalyst circulation.
Comparative example 4
The hydrocarbon feedstock treated in this comparative example was identical to example 1 and the flow of the reaction mass was identical to example 1.
The difference from example 1 is that the regenerated catalyst flows as follows: the regenerated fresh catalyst flows to the first reverse in the circulating conveying direction, then enters the fourth reverse, then flows to the third reverse and the second reverse in sequence, and finally is lifted to the regenerator H from the second reverse for catalyst regeneration.
The effect comparison of example 1 with comparative example 1 is shown in table 1:
TABLE 1
As can be seen from table 1, the hydrocarbon continuous reforming process of the present invention compares with conventional continuous reforming techniques under the same conditions, operations and reaction conditions: the yield of C5+ liquid is increased by 0.6 percent, the yield of pure hydrogen is increased by 0.18 percent, the yield of aromatic hydrocarbon is increased by 1.51 percent, for a set of catalytic reforming device with the treatment capacity of 260 ten thousand tons/year, the yield of aromatic hydrocarbon is increased by 3.9 ten thousand tons each year, the yield of hydrogen is increased by 4680 tons, and the income of products is increased by 2.75 hundred million yuan each year. Under the same working conditions, operation and reaction conditions, the hydrocarbon continuous reforming process disclosed by the invention is compared with the technology of comparative example 4: the yield of C5+ liquid is increased by 0.5 percent, the yield of pure hydrogen is increased by 0.15 percent, and the yield of aromatic hydrocarbon is increased by 1.01 percent. The income of the product is increased by 1.79 hundred million yuan each year.
The effect comparison of example 2 with comparative example 2 is shown in table 2:
TABLE 2
As can be seen from table 2, the hydrocarbon continuous reforming process of the present invention compares with the comparative example 2 continuous reforming technique under the same conditions, operations and reactions: the recovery of C5+ liquid is increased by 0.2 percent, the yield of pure hydrogen is increased by 0.02 percent, the yield of aromatic hydrocarbon is increased by 1.5 percent, and for a set of catalytic reforming device with the treatment capacity of 260 ten thousand tons/year, 3.9 ten thousand tons of aromatic hydrocarbon is increased each year, and the product income is increased by 2.78 hundred million yuan each year.
The effect comparison of example 3 with comparative example 3 is shown in table 3:
TABLE 3 Table 3
/>
As can be seen from table 3, the hydrocarbon continuous reforming process of the present invention compares with conventional continuous reforming techniques under the same conditions, operations and reaction conditions: the yield of C5+ liquid is increased by 1.5%, the yield of pure hydrogen is increased by 0.2%, the yield of aromatic hydrocarbon is increased by 2.32%, for a set of catalytic reforming device with the treatment capacity of 260 ten thousand tons/year, 6 ten thousand tons of aromatic hydrocarbon is increased each year, the yield of hydrogen is increased by 5200 tons, and the income of products is increased by 2.84 hundred million yuan each year.
The foregoing description of embodiments of the invention has been presented for purposes of illustration and description, and is not intended to be exhaustive or limited to the embodiments disclosed. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the various embodiments described.
Claims (10)
1. A device for reforming hydrocarbon in a moving bed is characterized by comprising a plurality of reactors (R 1……Rn……Rz) and a regenerator (H), wherein n is more than 1 and less than z, and z is more than or equal to 3; wherein:
The reaction materials sequentially flow through the first reactor (R 1) and the second reactor (R 2) to the z-th reactor (R z), and the reactors are sequentially connected in series through reaction material channels;
The catalyst is circulated between the regenerator and the reactor: the catalyst discharging pipeline of the regenerator (H) is connected with the nth reactor (R n) and then is connected with the z-th reactor (R z), then is sequentially connected with other reactors except the nth reactor (R n) in a forward and reverse mode, and finally is connected with the first reactor (R 1); the first reactor (R 1) is provided with a lower catalyst discharge line of the first reactor, which is connected with a feed line of the regenerator catalyst (H).
2. The apparatus for reforming hydrocarbons with moving bed according to claim 1, wherein the apparatus further comprises a reaction feed/product heat exchanger (E 1), and a heating device corresponding to each reactor, wherein a reaction feed line is connected to the reaction feed/product heat exchanger (E 1) and then sequentially connected to a first heating device (F 1) and a first reactor (R 1) … … nth heating device (F n) and an nth reactor (R n) … … nth heating device (F z) and a z-th reactor (R z);
The z-th reactor (R z) is provided with a z-th reactor product discharge line and a z-th reactor lower catalyst discharge line, and the z-th reactor product discharge line is connected with the reaction feed/product heat exchanger (E 1) and then connected with a subsequent system.
3. The apparatus for reforming hydrocarbons in a moving bed according to claim 1, wherein the upper part of each reactor is provided with a buffer tank corresponding to the reactor, and the lower part of each reactor is provided with a lower hopper and a lifter corresponding to the lower hopper in turn;
The upper part of the nth reactor (R n) is also provided with a reduction tank (De 1) and an nth pressure locking pipe (G n), and the nth pressure locking pipe (G n) is arranged between the reduction tank (De 1) and the buffer tank;
The upper parts of the reactors except the nth reactor (R n) are also provided with corresponding locking pipes and upper hoppers, and the locking pipes are arranged between the corresponding upper hoppers and the buffer tanks;
the upper part of the regenerator (H) is provided with a separation hopper (Df 1) and a metering tank (Dg 1), and the lower part of the regenerator (H) is provided with a sealing tank (Dh 1) and a regenerator lifter (T H);
The catalyst discharging pipeline of the regenerator is sequentially connected with a sealing tank (Dh 1), a regenerator lifter (T H), an nth buffer tank (Da n), an nth pressure locking pipe (G n), a reduction tank (De 1) and an nth reactor (R n), the nth reactor (R n) is provided with a lower catalyst discharging pipeline of the nth reactor, the lower catalyst discharging pipeline of the nth reactor is sequentially connected with a lower hopper (Dc n), an nth lifter (T n), a z buffer tank (Da z), a z pressure locking pipe (G z), an upper hopper (De Z) and a z reactor (R z), and the lower catalyst discharging pipeline of the z reactor is sequentially and reversely connected with the buffer tank, the pressure locking pipe, the upper hopper and the z reactor corresponding to other reactors except the nth reactor (R n) forwards after the lower catalyst discharging pipeline of the nth reactor (T3428);
The lower catalyst discharging pipeline of the first reactor is sequentially connected with a first lower hopper (Dc 1), a first lifter (T 1), a separation hopper (Df 1) and a metering tank (Dg 1), and the metering tank (Dg 1) is connected with a regenerator (H) through a regenerator catalyst feeding pipeline;
the corresponding locking pressure pipe of each reactor is independently a light pipe or a locking pressure system with a special structure.
4. A moving bed hydrocarbon reforming apparatus according to any one of claims 1 to 3, wherein the apparatus comprises four reactors, namely a first reactor (R 1), a second reactor (R 2), a third reactor (R 3) and a fourth reactor (R 4), and the regenerator catalyst take-off line connects first to the second reactor (R 2) or the third reactor (R 3).
5. A process for moving bed hydrocarbon reforming, characterized in that it is carried out with the moving bed hydrocarbon reforming apparatus according to any one of claims 1 to 4, comprising the steps of:
(1) The mixed material of hydrocarbon raw material and hydrogen-containing gas sequentially enters a plurality of reactors (R 1……Rn……Rz) and contacts with a solid catalyst in the reactors;
(2) The regenerated catalyst of the regenerator (H) is firstly conveyed to an nth reactor (R n), then enters a z-th reactor (R z), sequentially enters other reactors except the nth reactor (R n) in a forward and reverse direction, and finally enters a first reactor (R 1);
(3) The carbon deposition catalyst at the bottom of the first reactor (R 1) is conveyed to a regenerator (H) for catalyst regeneration.
6. The process for reforming hydrocarbons by moving bed according to claim 5, wherein the mixture of hydrocarbon feedstock and hydrogen-containing gas is heated by a first heating device (F 1) after heat exchange by a reaction feed/product heat exchanger (E 1), and enters a first reactor (R 1) where it contacts the solid catalyst, the reaction product sequentially enters a corresponding reactor through a subsequent heating device where it contacts the solid catalyst, and the reaction product of the z-th reactor (R z) enters a reaction feed/product heat exchanger (E 1) where it exchanges heat with the mixture of hydrocarbon feedstock and hydrogen-containing gas, and then enters a subsequent re-contact and fractionation system.
7. The process for reforming hydrocarbons with moving bed according to claim 5, wherein the regenerated catalyst of the regenerator (H) enters a sealed tank (Dh 1), is lifted to an nth buffer tank (Da n) by a regenerator lifter (T H), enters a reduction tank (De 1) by an nth lock pressure pipe (G n), and then enters an nth reactor (R n) to be contacted with the nth reactor reactant;
the catalyst after contact enters an nth lower hopper (Dc n), is lifted to a zth buffer tank (Da z) through an nth lifter (T n), enters a zth upper hopper (Db z) through a zth locking pressure pipe (Gz), then enters a zth reactor (R z), contacts with reaction materials of the zth reactor, then enters the zth lower hopper (Dc z), is lifted to a zth-1 buffer tank (Da z-1) of a zth-1 reactor (R z-1) through the zth lifter (T z), enters a zth-1 reactor (R z-1) through a zth-1 locking pressure pipe (G z-1) and a zth-1 upper hopper (Db z-1), sequentially forwards, finally enters a1 st buffer tank (Da 1) of a first reactor (R 1) except for the nth reactor (R n), and enters the zth buffer tank (R 1) through a zth locking pressure pipe (G 1) and the 1 st upper hopper (Db 1); when z-1 = n, the z-th riser (T z) lifts the catalyst to the z-2 buffer tank (Da z-2) of the z-2 reactor (R z-2);
The carbon deposition catalyst at the bottom of the first reactor (R 1) enters a first lower hopper (Dc 1), is lifted to a separation hopper (Df 1) by a first lower lifter (T 1), and enters a regenerator (H) by a metering tank (Dg 1) for catalyst regeneration.
8. The moving bed hydrocarbon reforming process of claim 7, wherein the plant pressure relationship is as follows:
PDh1＞PH,PDh1＞PTH＞PDa3,PDe1＞PDan,PDe1＞PRn,PDcn＞PRn,PTn＞
PDaZ＞PRZ,PDcZ＞PRZ,PTZ＞PDaZ-1,PDbZ-1＞PRZ-1,PDbZ-1＞PDaZ-1,PDcZ-1＞PRZ,PTX＞PDa1,PDb1＞PR1,PDb1＞PDa1,PDc1＞PR1,PT1＞PDf1＞PDg1＞PH;
Wherein, when n=2, X is 3; when n > 2, X is 2.
9. The process for moving bed hydrocarbon reforming according to claim 7, wherein the first reactor riser is elevated with nitrogen and the remaining reactor risers and regenerator risers are elevated with hydrogen;
all the upper hoppers of the reactors are filled with hydrogen, and the lower hopper (Dc 1), the sealing tank (Dh 1) and the separating hopper (Df 1) of the first reactor are filled with nitrogen;
The reduction pot (De 1) was introduced with hydrogen gas and the reduction reaction of the catalyst metal center was performed at 400-480 ℃.
10. The process for moving bed hydrocarbon reforming according to claim 7, wherein the heating devices corresponding to the respective reactors are each independently heated by a heating furnace or an electric heater, and the outlet temperatures of the heating devices are each independently 500 to 550 ℃, preferably 520 to 545 ℃; the corresponding pressure locking pipes of each reactor independently enable the catalyst to be conveyed to overcome 20-200kPa counter-pressure difference.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211292058.9A CN117946736A (en) | 2022-10-20 | 2022-10-20 | Device and process for reforming hydrocarbons in moving bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202211292058.9A CN117946736A (en) | 2022-10-20 | 2022-10-20 | Device and process for reforming hydrocarbons in moving bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN117946736A true CN117946736A (en) | 2024-04-30 |
Family
ID=90803648
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202211292058.9A Pending CN117946736A (en) | 2022-10-20 | 2022-10-20 | Device and process for reforming hydrocarbons in moving bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN117946736A (en) |
-
2022
- 2022-10-20 CN CN202211292058.9A patent/CN117946736A/en active Pending
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8282814B2 (en) | Fired heater for a hydrocarbon conversion process | |
| US5211838A (en) | Fixed-bed/moving-bed two stage catalytic reforming with interstage aromatics removal | |
| CN103459564B (en) | Improve the method for Benzene and Toluene output | |
| TWI410486B (en) | A process for heating a stream for a hydrocarbon conversion process | |
| US5221463A (en) | Fixed-bed/moving-bed two stage catalytic reforming with recycle of hydrogen-rich stream to both stages | |
| NO140067B (en) | CATALYTIC LIQUID CRACKING PROCESS FOR SAME CRACKING OF A GAS OIL HYDROCARBON OUTPUT MATERIAL AND IMPROVEMENT OF A PETROL OUTPUT MATERIAL | |
| CN105316029A (en) | Reforming process with optimized distribution of the catalyst | |
| CN101665710A (en) | Method and device for catalytic conversion of light dydrocarbon | |
| US4325807A (en) | Multiple stage hydrocarbon conversion with gravity flowing catalyst particles | |
| CN115537231B (en) | Method for realizing oil reduction and oil increase by changing material flow direction | |
| CN117946736A (en) | Device and process for reforming hydrocarbons in moving bed | |
| CN105349180B (en) | Hydro carbons continuous reforming process | |
| CN103492533A (en) | High temperature reforming process | |
| CN111689829B (en) | Method and device for preparing ethylene by catalytic conversion of petroleum hydrocarbon | |
| CN114736090A (en) | Method and system for preparing paraxylene | |
| US4250018A (en) | Multiple stage hydrocarbon conversion process | |
| WO2018022300A1 (en) | Process for increasing hydrocarbon yield from catalytic reformer | |
| CN109722297B (en) | Catalytic reforming process system and process method | |
| US11028328B2 (en) | Systems and processes for catalytic reforming of a hydrocarbon feed stock | |
| US4250019A (en) | Multiple stage hydrocarbon conversion process | |
| US20240228892A1 (en) | Process with continuous catalytic regeneration for treating a hydrocarbon feedstock | |
| CN114456830B (en) | Continuous reforming method of naphtha countercurrent moving bed | |
| CN115992004B (en) | Reaction method and reactor for preparing low-carbon olefin and aromatic hydrocarbon by catalytic conversion of hydrocarbon raw material as reaction raw material | |
| CN102559259A (en) | Method for hydrotreatment of secondary processed inferior gasoline fraction | |
| CN109722298B (en) | Energy-saving catalytic reforming process system and process method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |