NO861647L - VERTICAL RADIAL FLOW REACTOR. - Google Patents
VERTICAL RADIAL FLOW REACTOR.Info
- Publication number
- NO861647L NO861647L NO861647A NO861647A NO861647L NO 861647 L NO861647 L NO 861647L NO 861647 A NO861647 A NO 861647A NO 861647 A NO861647 A NO 861647A NO 861647 L NO861647 L NO 861647L
- Authority
- NO
- Norway
- Prior art keywords
- catalyst
- reaction vessel
- passage
- reactor
- annular space
- Prior art date
Links
- 239000003054 catalyst Substances 0.000 claims description 57
- 238000006243 chemical reaction Methods 0.000 claims description 43
- 229930195733 hydrocarbon Natural products 0.000 claims description 22
- 150000002430 hydrocarbons Chemical class 0.000 claims description 22
- 239000012530 fluid Substances 0.000 claims description 18
- 239000004215 Carbon black (E152) Substances 0.000 claims description 16
- 239000000463 material Substances 0.000 claims description 12
- 238000000034 method Methods 0.000 claims description 9
- QRRWWGNBSQSBAM-UHFFFAOYSA-N alumane;chromium Chemical compound [AlH3].[Cr] QRRWWGNBSQSBAM-UHFFFAOYSA-N 0.000 claims description 2
- 229910052782 aluminium Inorganic materials 0.000 claims description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims 1
- 239000004411 aluminium Substances 0.000 claims 1
- 238000007789 sealing Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 10
- 238000006356 dehydrogenation reaction Methods 0.000 description 8
- 230000003197 catalytic effect Effects 0.000 description 6
- 238000010276 construction Methods 0.000 description 6
- 239000000376 reactant Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 239000011449 brick Substances 0.000 description 4
- 239000000919 ceramic Substances 0.000 description 4
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229910000975 Carbon steel Inorganic materials 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 239000010962 carbon steel Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 239000011470 perforated brick Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000003575 carbonaceous material Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- NJPPVKZQTLUDBO-UHFFFAOYSA-N novaluron Chemical compound C1=C(Cl)C(OC(F)(F)C(OC(F)(F)F)F)=CC=C1NC(=O)NC(=O)C1=C(F)C=CC=C1F NJPPVKZQTLUDBO-UHFFFAOYSA-N 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/24—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions with moving solid particles
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
-
- 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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0207—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal
- B01J8/0214—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly horizontal in a cylindrical annular shaped bed
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
- C07C5/333—Catalytic processes
- C07C5/3332—Catalytic processes with metal oxides or metal sulfides
-
- 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
- C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
- C10G47/02—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions characterised by the catalyst used
- C10G47/04—Oxides
Description
Foreliggende oppfinnelse vedrører en forbedret konstruksjon av reaktorer brukt i katalytiske hydrokarbonbehandlingsoperasjoner. Den vedrører også den tilknyttede prosess for behandling av hydrokarboner ved bruk av den forbedrede reaktorkonstruksjon. The present invention relates to an improved construction of reactors used in catalytic hydrocarbon treatment operations. It also relates to the associated process for treating hydrocarbons using the improved reactor design.
Hydrokarbonbehandlingsreaktorer innbefatter vanligvis en isolert horisontal karbonstål- eller lignende beholder med et omfattende katalysatorsjikt på en eller annen type støtte-innretning i det nedre parti av beholderen. Mursteinsgulv med motstandsdyktige hvelvinger er oppbygd i bunnen av beholderen for å tilveiebringe tilstrekkelig støtte for katalysatorsjiktet. Noen reaktorkonstruksjoner har erstattet mursteinsgulvet og det motstandsdyktige, understøttende hvelvingssystem med alternative støtteanordninger slik som tverrgående støttebjelker i metall som spenner tvers over reaktoren bg som holder oppe en perforert stålplatedekk-støtte eller méd et stort, i snitt halvsirkulært perforert rør anbragt i lengderetningen i reaktoren og dekket med kjeramiske støttekuler. Alternativt har den nedre tredjedel av reaksjonsbeholderen ganske enkelt blitt fylt med kjeramiske støttekuler uten noen underliggende støtteanordning. Hydrocarbon processing reactors typically include an insulated horizontal carbon steel or similar vessel with an extensive catalyst bed on some type of support device in the lower portion of the vessel. Brick floors with resistant vaults are constructed in the bottom of the vessel to provide adequate support for the catalyst bed. Some reactor designs have replaced the brick floor and the resistant, supporting vault system with alternative support devices such as transverse support beams in metal that span across the reactor bg supporting a perforated steel plate deck support or with a large, on average semi-circular perforated tube placed longitudinally in the reactor and covered with ceramic support balls. Alternatively, the lower third of the reaction vessel has simply been filled with ceramic support balls without any underlying support device.
En typisk katalytisk reaksjonsbeholder for behandling av hydrokarboner er beskrevet i US-patent nr. 4.126.539. Denne beskrivelse innbefatter et fast katalysatorsjiktreaktor-arrangement som har en innebygget gass/væskefordelingsinn-retning. Et horisontalt katalysatorsjikt støttes av en kombinasjon av kjeramiske kuler innbefattende et bunnlag med 19,0 mm kuler, et midtlag med 12,7 mm kuler og et topplag med 6,3 mm kuler over et perforert mursteinsgulv og hvelvinger som danner et plenum for produktuttrekking. A typical catalytic reaction vessel for treating hydrocarbons is described in US Patent No. 4,126,539. This disclosure includes a fixed catalyst bed reactor arrangement having a built-in gas/liquid distribution device. A horizontal catalyst bed is supported by a combination of ceramic balls comprising a bottom layer of 19.0 mm balls, a middle layer of 12.7 mm balls and a top layer of 6.3 mm balls over a perforated brick floor and vaults forming a plenum for product extraction.
I en utførelse er katalysatorsjiktet, innbefattende enIn one embodiment, the catalyst layer is, including a
gruppe VI-metalloksyd og/eller sulfid på aluminium omkring 4,2 6 m i diameter og omkring 9,14 m høyt. group VI metal oxide and/or sulphide on aluminum about 4.2 6 m in diameter and about 9.14 m high.
I den ovenfor angitte reaktorkonstruksjon tilføres hydrokar- bon som skal behandles vanligvis til reaksjonsbeholderen via et innløp plassert ved toppen eller i siden av beholderen. Det skapes først kontakt med toppen av katalysatorsjiktet og reaktanttilførslen penetrerer i det minste delvis sjiktet for ytterligere katalysatorkontakt. In the above-mentioned reactor construction, hydrocarbon to be treated is usually supplied to the reaction vessel via an inlet located at the top or in the side of the vessel. Contact is first made with the top of the catalyst bed and the reactant supply at least partially penetrates the bed for further catalyst contact.
Den foreliggende oppfinnelse tilveiebringer en effektiv og økonomisk reaktorkonstruksjon for bruk i katalytiske om-dannelsesprosesser. Denne nye reaktor er av en vertikal type og med radiell strømning hvor reaktoren innbefatter en vertikalt orientert reaksjonsbeholder som har et fluidinnløp for innføring av reaktanter, og et fluidutløp for utslipp av produkter. En massiv støttebasis, slik som en betong-pidestall, er plassert ved bunnpartiet av beholderen. To sirkulære, konsentriske sikter, eller enhver ekvivalent struktur slik som motstandsdyktig murstein, forløper vertikalt fra støttebasisen i reaksjonsbeholderen. Siktene er plassert slik at et plenumsområde dannes mellom den ytre sikt og veggen av reaksjonsbeholderen, og et ringformet rom, i hvilket et granulært katalysatorsjikt kan anbringes, dannes mellom de to sikter. En passasje dannet i det indre av den indre sikt er forbundet til fluidinnløpet av reaksjonsbeholderen. Både det ringformede rom dannet mellom de to konsentriske sikter og den indre passasje er avtettet ved toppen for å forhindre fluid fra å strømme ut gjennom den øvre ende. Et katalysatorinnløp; dvs. innmatningsdyse, forløper fra toppen av katalysatorsjiktet til det ytre av reaksjonsbeholderen for å tillate katalysatoren å bli anbragt i det ringformede rom mellom siktene fra utsiden av beholderen. Likeledes forløper et katalysatorutløp fra bunnen av katalysatorsjiktet til det ytre av reaksjonsbeholderen gjennom hvilke katalysatoren kan fjernes fra sjiktet. The present invention provides an efficient and economical reactor design for use in catalytic conversion processes. This new reactor is of a vertical type and with radial flow where the reactor includes a vertically oriented reaction vessel which has a fluid inlet for the introduction of reactants, and a fluid outlet for the release of products. A massive support base, such as a concrete pedestal, is placed at the bottom of the container. Two circular, concentric screens, or any equivalent structure such as resistive bricks, extend vertically from the support base in the reaction vessel. The sieves are positioned so that a plenum area is formed between the outer sieve and the wall of the reaction vessel, and an annular space, in which a granular catalyst layer can be placed, is formed between the two sieves. A passage formed in the interior of the inner screen is connected to the fluid inlet of the reaction vessel. Both the annular space formed between the two concentric screens and the internal passage are sealed at the top to prevent fluid from flowing out through the upper end. A catalyst inlet; i.e. feed nozzle, extends from the top of the catalyst bed to the outside of the reaction vessel to allow the catalyst to be placed in the annular space between the screens from the outside of the vessel. Likewise, a catalyst outlet extends from the bottom of the catalyst layer to the outside of the reaction vessel through which the catalyst can be removed from the layer.
Denne type reaktorkonstruksjon tilveiebringer for radiell strømning av reaksjonsfluidet gjennom det vertikalt orienterte katalysatorsjikt. Reaktoren er vel egnet for tallrike operasjoner, og særlig for hydrokarbonbehandling slik som fjerning av hydrogen, hydrofiming og katalytisk avsvovling. This type of reactor construction provides for radial flow of the reaction fluid through the vertically oriented catalyst bed. The reactor is well suited for numerous operations, and in particular for hydrocarbon treatment such as hydrogen removal, hydrofiming and catalytic desulphurisation.
Fig. 1 er et snittskisse gjennom reaktoren oppbygd og anordnet i samsvar med den foreliggende oppfinnelse, og fig. 2 er en tverrsnittsskisse langs linje 2-2 i fig. 1. Fig. 1 is a sectional view through the reactor constructed and arranged in accordance with the present invention, and fig. 2 is a cross-sectional sketch along line 2-2 in fig. 1.
Den .foreliggende oppfinnelse er en forbedret reaktorkon-struks jon og en fremgangsmåte for anvendelse av den samme. Den forbedrede reaktor er særlig nytting for katalytiske hydrokarbonbehandlingsoperasjoner. Oppfinnelsen kan best forstås med henvisning til fig. 1 som er en snittskisse av en reaktor i samsvar med en foretrukket utførelse av den foreliggende oppfinnelse. The present invention is an improved reactor construction and a method for using the same. The improved reactor is particularly useful for catalytic hydrocarbon processing operations. The invention can best be understood with reference to fig. 1 which is a sectional sketch of a reactor in accordance with a preferred embodiment of the present invention.
En vertikalt orientert reaktorbeholder 4 har et fluidinn-løp 6 for tilførsel av reaktanter slik som en hydrokarbon-holdig gasstrøm,- inn i reaksjonsbeholderen 4. Reaksjonsbeholderen 4 er tilvirket av ethvert stivt materiale som kan motstå reaksjonstemperaturene; dvs. mellom omkring 600-675°C for C 3 og C^-dehydrogenering. Vanlige reaksjonsbeholdere er oppbygd av "en ytre kappe av karbonstål med motstandsdyktig isolasjon innenfor. Metallstøtteringen 5 er ofte brukt i tillegg for å gi beholderen ytterligere styrke. To sirkulære konsentriske sikter 8 og 9 forløper vertikalt i reaksjonsbeholderen 4 fra en massiv støttebasis 10 plassert ved bunnen av reaksjonsbeholderen. Fortrinnsvis forløper de to konsentriske sikter i det minste omkring halvveis opp i det indre av reaksjonsbeholderen 4, men når ikke toppen av beholderen. A vertically oriented reactor vessel 4 has a fluid inlet 6 for supplying reactants such as a hydrocarbon-containing gas stream into the reaction vessel 4. The reaction vessel 4 is made of any rigid material that can withstand the reaction temperatures; ie between about 600-675°C for C 3 and C 2 dehydrogenation. Conventional reaction vessels are constructed of "an outer shell of carbon steel with resistant insulation within. The metal support ring 5 is often used in addition to give the vessel additional strength. Two circular concentric screens 8 and 9 extend vertically into the reaction vessel 4 from a massive support base 10 located at the bottom Preferably, the two concentric sieves extend at least about halfway up the interior of the reaction vessel 4, but do not reach the top of the vessel.
Det indre av beholderkonstruksjonen kan best forstås ved henvisning til fig. 2 som er en tverrsnittsskisse langs linje 2-2 i fig. 1. Identiske konstruksjoner i fig. 1 og 2 er angitt med de samme henvisningsnummer. Som det kan sees i fig. 2, er to konsentriske sirkulære sikter 8 og 9 plassert i reaksjonsbeholderen 4 slik at et plenumsområde 12 dannes mellom den ytre sikt 8 og beholderveggen 14, og en passasje 16 dannes innenfor den indre sikt 9. Selv om det ikke er noen størrelseskrav for plenumsområdet dannet mellom den ytre sikt 8 og reaktorveggen 14, er i et vanlig reaktorarrangement dette område vanligvis mellom 152 mm til 762 mm bredt. Likeledes kan passasjen 16 som er i det indre av den indre sikt 9 være av enhver diameter som tillater den ønskede gassvolumstrømning gjennom nevnte passasje. Imid-lertid er i en typisk reaktoroppbygning passasjen 16 vanligvis mellom 1,06 m til 2,29 m i diameter. The interior of the container structure can best be understood by reference to fig. 2 which is a cross-sectional sketch along line 2-2 in fig. 1. Identical constructions in fig. 1 and 2 are indicated with the same reference number. As can be seen in fig. 2, two concentric circular sieves 8 and 9 are placed in the reaction vessel 4 so that a plenum area 12 is formed between the outer sieve 8 and the vessel wall 14, and a passage 16 is formed within the inner sieve 9. Although there are no size requirements for the plenum area formed between the outer sieve 8 and the reactor wall 14, in a normal reactor arrangement this area is usually between 152 mm to 762 mm wide. Likewise, the passage 16 which is in the interior of the inner sieve 9 can be of any diameter that allows the desired gas volume flow through said passage. Meanwhile, in a typical reactor structure, the passage 16 is usually between 1.06 m to 2.29 m in diameter.
De to konsentriske sikter 8 og 9 er anordnet slik at et ringformet rom 18 dannes mellom de to sikter inn i hvilke granulært katalysatormateriale 20 kan plasseres. Siktene 8 og 9 er vanligvis tilvirket av en eller annen type metallduk, slik som type 310 rustfritt stål, som tillater strømning av gass og likevel ikke tillater granulært katalysatormateriale å strømme gjennom. Den indre sikt 9 er dimensjonert i for-hold til dampstrømningsgraden av de innkommende reaktanter og trykkdifferansen i beholderen. Dimensjonen på den ytre sikt 8 er fastlagt ved den mengde av katalysatormateriale som er nødvendig for å behandle mengden og sammensetningen av tilførselsmateriale. I en vanlig reaktor er avstanden mellom den indre sikt 9 og den ytre sikt 8 som danner det ringformede rom mellom 1,83 til 2,44 m. Katalysatormaterialet anbragt i dette ringformede rom 18 kan derfor variere avhengig av type reaksjon som skal utføres i beholderen, hvor den eneste begrensning er at nevnte katalysatorpellets skal være tilstrekkelig store slik at de ikke strømmer gjennom siktedukene 8 og 9. I tilfelle av propan- eller butan-dehydrogeneringsreaksjoner brukes ofte kromaluminium-katalysatorer. The two concentric sieves 8 and 9 are arranged so that an annular space 18 is formed between the two sieves into which granular catalyst material 20 can be placed. The screens 8 and 9 are usually made of some type of metal cloth, such as type 310 stainless steel, which allows the flow of gas and yet does not allow granular catalyst material to flow through. The internal sieve 9 is dimensioned in relation to the steam flow rate of the incoming reactants and the pressure difference in the container. The dimension of the outer screen 8 is determined by the amount of catalyst material that is necessary to treat the amount and composition of feed material. In a normal reactor, the distance between the inner sieve 9 and the outer sieve 8 which forms the annular space is between 1.83 and 2.44 m. The catalyst material placed in this annular space 18 can therefore vary depending on the type of reaction to be carried out in the container , where the only limitation is that said catalyst pellets must be sufficiently large so that they do not flow through the sieve cloths 8 and 9. In the case of propane or butane dehydrogenation reactions, chromium aluminum catalysts are often used.
Det vises til fig. 1 hvor passasjen 16 er forbundet til fluidinnløpet 6 slik at reaktanter som entrer reaksjonsbeholderen 4 via innløpet 6 passeres inn i passasjen 16. Topp-partiet av både det ringformede rom 18 mellom de to sikter 8 og 9 og den indre passasje 16 er avtettet ved toppen for å forhindre gass-strømning. Følgelig når den reaktantinneholdende gass-strøm entrer den indre passasje 16, strømmer den deretter gjennom det katalysatorinnehold-ehde ringformede rom 18 mellom de to sikter 8 og 9 på en i hovedsak radiell strømningsmåte. Den ønskede reaksjon, slik som dehydrogenering finner sted i dette ringformede rom 18 som inneholder den granulære katalysator 20. Den behandlede gass-strømning som nå inneholder reaksjonsprodukter, forlater det ringformede rom 18 ved forskjellige punkter, og entrer plenumsområdet mellom den ytre sikt 8 og reaktorveggen 14. Den produktinneholdende gass-strøm passerer deretter oppad gjennom plenumsområdet 12 og utgår av reaksjonsbeholderen 4 gjennom et fluidutløp 22 plassert ved det øvre parti av reaksjonsbeholderen 4. Produktet som forlater reaksjonsbeholderen 4 gjennom fluidutløpet 22 kan oppsamles som et utnyttbart produkt, eller alternativt brukes i en påfølgende'behandlingsoperasjon. Reference is made to fig. 1 where the passage 16 is connected to the fluid inlet 6 so that reactants entering the reaction container 4 via the inlet 6 are passed into the passage 16. The top part of both the annular space 18 between the two sieves 8 and 9 and the inner passage 16 is sealed at the top to prevent gas flow. Accordingly, when the reactant-containing gas stream enters the inner passage 16, it then flows through the catalyst-containing annular space 18 between the two screens 8 and 9 in a substantially radial flow manner. The desired reaction such as dehydrogenation takes place in this annular space 18 containing the granular catalyst 20. The treated gas stream, now containing reaction products, leaves the annular space 18 at various points and enters the plenum area between the outer screen 8 and the reactor wall 14. The product-containing gas stream then passes upwards through the plenum area 12 and exits the reaction vessel 4 through a fluid outlet 22 located at the upper part of the reaction vessel 4. The product that leaves the reaction vessel 4 through the fluid outlet 22 can be collected as a usable product, or alternatively used in a subsequent' treatment operation.
Den foreliggende reaksjonsbeholder er særlig anvendelig i hydrokarbondehydrogeneringsreaksjoner, og reaktordriften kan ; være cyklisk for en fast tidsperiode som kan variere avhengig av størrelsen på anlegget. Som beskrevet ovenfor, når reaktoren er igang, entrer oppvarmet hydrokarbondamp oppstrømningsreaktoren gjennom det sentrale bunninnløp 6. Hydrokarbondampen passerer opp gjennom den indre passasje 16, gjennom katalysatorsjiktet 20 til plenumsområdet 12 hvor reaksjonsprodukter oppsamles og deretter utgår via fluidutløpet 22. Under dehydrogeneringsreaksjoner, vil oppbygning av karbonholdig materiale på overflaten av katalysatoren bevirke en minskning i katalytisk aktivitet. Katalytisk regenerering kan utføres ved å ta reaktoren ut av strømmen og sirkulere luft eller en lignende oksyderingsgass langs den samme bane som hydrokarbondampen beskrevet ovenfor. Vanlige dehydrogeneringsreaksjoner anvender et antall slike reaksjonsbeholdere slik at ved ethvert gitt tidspunkt er en eller flere beholdere i strømningen mens andre undergår regenerering. The present reaction vessel is particularly applicable in hydrocarbon dehydrogenation reactions, and the reactor operation can; be cyclical for a fixed period of time which may vary depending on the size of the facility. As described above, when the reactor is running, heated hydrocarbon vapor enters the upflow reactor through the central bottom inlet 6. The hydrocarbon vapor passes up through the inner passage 16, through the catalyst bed 20 to the plenum area 12 where reaction products are collected and then exit via the fluid outlet 22. During dehydrogenation reactions, build-up of carbonaceous material on the surface of the catalyst cause a reduction in catalytic activity. Catalytic regeneration can be performed by taking the reactor off stream and circulating air or a similar oxidizing gas along the same path as the hydrocarbon vapor described above. Common dehydrogenation reactions use a number of such reaction vessels so that at any given time one or more vessels are in the flow while others are undergoing regeneration.
Etter en tidsperiode; f.eks. omkring 2 år for vanlig dehyd-rogeneringskatalysatorer, blir katalysatorene deaktivert til et punkt hvor de ikke lenger kan regenerere effektivt. Når dette oppstår, tappes den brukte katalysator fra reaktoren via en katalysatordrenering eller utløp 26 som for-løper fra bunnen av katalysatorsjiktet 20 til det ytre av reaksjonsbeholderen 4. Katalysatorsjiktet etterfylles ved å påføre katalysatormaterialet gjennom et katalysatorinnløp, slik som innføringsdysen 24, som forløper fra det ytre av reaksjonsbeholderen 4 til toppen av det ringformede rom 18 som inneholder katalysatorsjiktet. After a period of time; e.g. around 2 years for conventional dehydrogenation catalysts, the catalysts are deactivated to the point where they can no longer regenerate efficiently. When this occurs, the spent catalyst is drained from the reactor via a catalyst drain or outlet 26 which extends from the bottom of the catalyst bed 20 to the outside of the reaction vessel 4. The catalyst bed is replenished by applying the catalyst material through a catalyst inlet, such as the introduction nozzle 24, which extends from the outside of the reaction vessel 4 to the top of the annular space 18 containing the catalyst layer.
Både reaksjons- og regenereringstemperaturene kan overvåkes ved en eller flere termobrønner 28 for katalysatorsjiktet som forløper fra katalysatorsjiktet til det ytre av reaksjonsbeholderen 4. Det er særlig viktig å overvåke reak-sjonstemperaturen under reaksjoner i hvilke temperaturene nærmer seg deaktiveringstemperaturen av katalysatormaterialet. Temperaturen styres ved å regulere matestrømningen under reaksjonen eller strømningen av oksyderingsgass under regenerering . Both the reaction and regeneration temperatures can be monitored by one or more thermowells 28 for the catalyst layer that extend from the catalyst layer to the outside of the reaction vessel 4. It is particularly important to monitor the reaction temperature during reactions in which the temperatures approach the deactivation temperature of the catalyst material. The temperature is controlled by regulating the feed flow during the reaction or the flow of oxidizing gas during regeneration.
Den foreliggende reaksjonsbeholder er fordelaktig overfor tidligere beholdere ved at den samme størrelse (volum) for katalysatorsjiktet som vanligvis brukes i dehydrogenerings-reaks joner, kan brukes i en beholderkappe som er signifikant mindre i lengde enn hva som tidligere var nødvendig. Dette gir en mer effektiv og økonomisk reaktorkonstruksjon. I tillegg skapes støtte for katalysatorsjiktet ved både betong- eller en lignende type basis såvel som ved de konsentriske sikter, og derfor trengs ikke utarbeidelse av mursteinshvelvinger og perforerte teglstein eller stål-plater eller kjeramiske kuler som støtter. The present reaction container is advantageous over previous containers in that the same size (volume) for the catalyst layer that is usually used in dehydrogenation reactions can be used in a container jacket that is significantly smaller in length than was previously necessary. This results in a more efficient and economic reactor construction. In addition, support for the catalyst layer is created by both a concrete or a similar type of base as well as by the concentric sieves, and therefore there is no need to prepare brick vaults and perforated bricks or steel plates or ceramic balls as supports.
Claims (15)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US72765985A | 1985-04-26 | 1985-04-26 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NO861647L true NO861647L (en) | 1986-10-27 |
Family
ID=24923495
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO861647A NO861647L (en) | 1985-04-26 | 1986-04-25 | VERTICAL RADIAL FLOW REACTOR. |
Country Status (4)
| Country | Link |
|---|---|
| KR (1) | KR900000860B1 (en) |
| DE (1) | DE3613903A1 (en) |
| FI (1) | FI861694A (en) |
| NO (1) | NO861647L (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3939544A1 (en) * | 1989-11-30 | 1991-06-06 | Uhde Gmbh | Reactor for catalytic gas reactions or physical sepn. - has spherical catalyst bed with central distributor from which there is radial outward gas flow |
| DE4135018A1 (en) * | 1990-11-30 | 1992-06-04 | Otto Oeko Tech | Passing fluid over bed of catalyst or adsorbent - by dividing fluid into two for radial flow of fluids in reactor, for cleaning car exhaust, industrial effluent or processing etc. |
| CN105623733B (en) * | 2014-10-27 | 2017-03-01 | 中国石油化工股份有限公司 | A kind of desulfurizing method by adsorption of petroleum hydrocarbon |
| FR3033264B1 (en) * | 2015-03-05 | 2017-03-03 | Ifp Energies Now | RADIAL REACTOR WITH FIXED CATALYTIC BEDS |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3027244A (en) * | 1959-02-09 | 1962-03-27 | Union Oil Co | Radial flow catalytic reactor |
| US4033727A (en) * | 1976-07-06 | 1977-07-05 | Phillips Petroleum Company | Separator ring in fixed bed radial flow catalytic reactor |
| US4244922A (en) * | 1978-09-05 | 1981-01-13 | Chevron Research Company | Hold-down device for vertically movable member in apparatus which contains contact material |
-
1986
- 1986-04-22 FI FI861694A patent/FI861694A/en not_active Application Discontinuation
- 1986-04-24 DE DE19863613903 patent/DE3613903A1/en not_active Ceased
- 1986-04-25 NO NO861647A patent/NO861647L/en unknown
- 1986-04-25 KR KR1019860003212A patent/KR900000860B1/en active IP Right Grant
Also Published As
| Publication number | Publication date |
|---|---|
| FI861694A (en) | 1986-10-27 |
| DE3613903A1 (en) | 1986-10-30 |
| FI861694A0 (en) | 1986-04-22 |
| KR900000860B1 (en) | 1990-02-17 |
| KR860008255A (en) | 1986-11-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| KR890002862B1 (en) | Gas circulation method for moving bed catalyst regeneration zones | |
| US3425810A (en) | Hydrotreating apparatus | |
| US3541000A (en) | Method and means for treating mixed phase vapor and liquid reactants under exothermic reaction conditions and temperature control | |
| CA2262449C (en) | Hydroprocessing in a countercurrent reaction vessel | |
| US4478793A (en) | Radial flow reactor with operating temperature profile | |
| US2532756A (en) | Tower reactor | |
| JPH04363132A (en) | Catalyst device for distillation reactor | |
| US5099085A (en) | Chlorination reactions and oxychlorination reactions in the presence of honeycomb monolithic catalyst supports | |
| GB574892A (en) | Process and apparatus for the conversion of fluid reactants | |
| US5202517A (en) | Process for production of ethylene from ethane | |
| JP3942664B2 (en) | Hydrocarbon conversion method | |
| CA2262370C (en) | Countercurrent reaction vessel | |
| US3482946A (en) | Reactor for contacting vaporous reactants with fluidized solids | |
| US5948240A (en) | Process for controlling reaction temperatures | |
| NO861647L (en) | VERTICAL RADIAL FLOW REACTOR. | |
| US3556989A (en) | Hydrocarbon oil treatment process and apparatus therefor | |
| JP2010051960A (en) | Method for chemical conversion of raw material through endothermic reaction using reactor | |
| US4411870A (en) | Reactor system | |
| US2604384A (en) | Apparatus for regenerating a fluidized catalyst | |
| KR890700045A (en) | Fluidized bed | |
| KR101652597B1 (en) | Catalyst screen with reinforced plates | |
| KR101651756B1 (en) | Catalyst screen with reinforced wires | |
| US3622281A (en) | High-temperature reaction vessel | |
| EP0238107B1 (en) | Process and apparatus for contacting gas, liquid and solid particles | |
| Ragaini et al. | Upflow reactor for the selective hydrogenation of pyrolysis gasoline a comparative study with respect to downflow |