PROCESS FOR OBTAINING VANADIUM OXIDE FROM A GASIFIER SLAG FIELD

A process for obtaining vanadium component in the form of vanadium oxide from gasifier slag is disclosed. The process comprises pulverizing the slag to obtain pulverized slag, which is blended with water and an alkali salt to obtain a slurry. The slurry is dried and then roasted in the presence of air to obtain a roasted slag. The roasted slag is leached to obtain a first filtrate comprising the vanadium component. The first filtrate is reacted with a magnesium salt to remove a silica component in the form of a precipitate. The silica free second filtrate is reacted with an ammonium salt to obtain ammonium metavanadate, which is further calcined to obtain the significant amount of vanadium pentoxide (VO). 1. A process for obtaining vanadium oxide from gasifier slag having vanadium component;the process comprising the following steps:a) pulverizing the gasifier slag to a particle size less than 100 μm to obtain a pulverized slag;b) blending the pulverized slag with water and at least one alkali salt to obtain a slurry;c) drying the slurry to remove water therefrom;d) roasting the dried slurry in the presence of air and at a temperature in the range of 750° C. to 1000° C. to obtain a roasted slag;e) leaching the roasted slag with water to obtain a first filtrate comprising the vanadium component;f) separating a silica component from the first filtrate to obtain a second filtrate;g) reacting the second filtrate with an ammonium salt to obtain ammonium metavanadate in the form of a precipitate; andh) separating the precipitate and calcining at a temperature in the range of 400 to 600° C. to obtain vanadium oxide having purity greater than 95%.2. The process as claimed in claim 1 , wherein in the step (b) the alkali salt is at least one selected from the group consisting of sodium carbonate (NaCO) and sodium sulphate (NaSO) and the amount of the alkali salt is in the range of 20 wt % to 50 wt % of the total slag.3. The process as claimed in claim 1 , wherein in the step ...

AN APPARATUS FOR CULTURING PHOTOSYNTHETIC ORGANISMS

The present disclosure provides an apparatus for culturing photosynthetic organisms. The apparatus comprising body of liquid of predetermined shape for holding ingredients required for culturing the photosynthetic organisms. The apparatus further comprises a mixing device for mixing ingredients in a body of liquid. The mixing device comprises at least one mixing plate of predetermined shape comprising a plurality of perforations. The mixing plate is adapted to be movably disposed within the body of liquid. Further, at least one drive mechanism coupled to the at least one mixing plate. The drive mechanism is configured to move the at least mixing plate in the body of liquid to accomplish turbulence in the body of liquid for maintaining the photosynthetic organisms in a suspended state to facilitate uniform exposure of photosynthetic organisms to light. 117-. (canceled)19. The apparatus as claimed in claim 18 , wherein the perforations are distributed substantially on entire surface of the at least one mixing plate.20. The apparatus as claimed in claim 18 , wherein the perforations are distributed on a portion of surface of the at least one mixing plate.21. The apparatus as claimed in claim 18 , wherein the drive mechanism is at least one of motorized mechanism and actuator mechanism.22. The apparatus as claimed in claim 18 , wherein the drive mechanism moves the at least one mixing plate in at least one of horizontal claim 18 , vertical claim 18 , rotational claim 18 , and angular motion in the body of liquid.23. The apparatus as claimed in claim 18 , wherein the body of liquid is at least one of a manmade body of liquid and a natural body of liquid.24. The apparatus as claimed in claim 18 , wherein the body of liquid comprises a guide rail for moving the drive mechanism.25. The apparatus as claimed in claim 24 , wherein the guide rail is at least one of a rail with substantially flat surface claim 24 , a cable and a pipe.26. The apparatus as claimed in comprises at ...

A PROCESS FOR CATALYTIC GASIFICATION OF CARBONACEOUS FEEDSTOCK

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support iand heat carrier in the gasification zone (). The gasification zone () is operated at 700-750° C. to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably KCO, so that conversion proportional to total KCOto solid carbon ratio is achieved with as high KCOloading as 50 wt % on the solid support. The combustion zone () is operated at 800°-840° C., to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles. 1. A process for catalytic gasification of a carbonaceous feedstock to synthesis gas , said process comprising the following steps:{'b': 102', '202, 'i. gasifying a primary portion of said carbonaceous feedstock in a fluidized gasification zone (, ) at a temperature between 600-800° C. with steam and in the presence of an alkali metal catalyst impregnated on a solid particulate carrier, to produce synthesis gas; wherein heat for the endothermic gasification reaction is supplied by heated solid particulate carrier provided in said gasification zone at a carrier to feedstock ratio of 10 to 50;'}{'b': 102', '202, 'ii. discharging heat-extracted solid particulate carrier impregnated with said alkali metal catalyst from the operative top of the fluidized gasification zone (, ); and'}{'b': 140', '240, 'iii. combusting a secondary portion of said carbonaceous feedstock and unreacted carbon from said gasification zone in a fluidized combustion zone (, ) at a temperature between 800-840° C. with air, wherein heat generated during the exothermic combustion reaction is transferred to said heat-extracted solid particulate carrier to provide said heated solid ...

PROCESS FOR RECOVERING VANADIUM IN THE FORM OF IRON VANADATE FROM A GASIFIER SLAG

The present disclosure relates to a process for recovering vanadium in the form of iron vanadate from a gasifier slag. The process comprises pulverizing the slag to obtain pulverized slag (). The pulverized slag () is soaked in water () and an alkali salt () to obtain a slurry (), followed by roasting the slurry in the presence of air to obtain roasted slag () which is leached () to obtain a first solution (). The first solution () is heated at a temperature in the range of 60° C. to 80° C. while adding an iron salt () in an amount in the range of 10 wt % to 60 wt % at a pH in the range of 4 to 10, to obtain a second solid residue () which is dried to obtain iron vanadate (). 1. A process for recovering vanadium in the form of iron vanadate from a gasifier slag , said process comprising the following steps:a) pulverizing gasifier slag to a particle size less than 100 μm to obtain pulverized slag;b) soaking said pulverized slag in water and alkali salt to obtain a slurry;c) roasting said slurry in the presence of air at a temperature in the range of 750° C. to 1100° C. to obtain roasted slag;d) leaching said roasted slag in water heated to a temperature below its boiling point to obtain a first biphasic mixture comprising a first solid phase and a first liquid phase;e) filtering said first biphasic mixture to obtain a first solid residue and a first solution comprising vanadium compounds;f) heating said first solution to a temperature in the range of 60° C. to 80° C. while adding therein, an iron salt in an amount in the range of 10 wt % to 60 wt % at a pH in the range of 4 to 10, to obtain a second biphasic mixture comprising a second solid phase and a second liquid phase;g) filtering said second biphasic mixture to obtain a second solid residue comprising iron vanadate and a second solution comprising said alkali salt; andh) drying said second solid residue at a temperature in the range of 300° C. to 500° C. to obtain iron vanadate.2. The process as claimed in ...

Conversion of methanol to olefins using large size catalyst particles

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support and heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

Process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support i and heat carrier in the gasification zone ( 102 ). The gasification zone ( 102 ) is operated at 700-750° C. to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt % on the solid support. The combustion zone ( 140 ) is operated at 800°-840° C., to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support and heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the γ-alumina to α-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

A process and a system for producing synthesis gas

The present disclosure relates to a process and a system for producing synthesis gas. The carbonaceous feedstock is gasified, in the presence of at least one of oxygen and steam, in a first reactor to obtain a gaseous mixture comprising H

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses .gamma.-alumina as a catalyst support iand heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of .gamma.-alumina to .alpha.-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K2CO3, so that conversion proportional to total K2CO3 to solid carbon ratio is achieved with as high K2CO3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the .gamma.-alumina to a-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

Process for preparing dialkylnaphthalene

2,6-Dialkylnaphthalene is prepared from a feedstock comprising naphthalene and an alkylating agent, by a process comprising the steps: (I) transalkylating isomers of dialkylnaphthalene and naphthalene to produce monoalkylnaphthalene and isomers of dialkylnaphthalene; (II) separating the product obtained in step (I) into naphthalene, monoalkylnaphthalene, dialkylnaphthalene and other components; (III) alkylating the monoalkylnaphthalene fraction from step (II) with an alkylating agent to produce dialkylnaphthalene; and (IV) separating 2,6-dialkylnaphthalene from the dialkylnaphthalene fraction in step (II), wherein at least step (I) or step (III) is conducted in the presence of a catalyst having a composition comprising a synthetic zeolite having an X-ray diffraction pattern with an interplanar d-spacing (.ANG.) 12.36 ~ 0.4 11.03 ~ 0.2 8.83 ~ 0.14 6.18 ~ 0.12 6.00 ~ 0.10 4.06 ~ 0.07 3.91 ~ 0.07 3.42 ~ 0.06.

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses γ-alumina as a catalyst support iand heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of γ-alumina to α-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K 2 CO 3 , so that conversion proportional to total K 2 CO 3 to solid carbon ratio is achieved with as high K 2 CO 3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the γ-alumina to a-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

A method for catalytic conversion of waste plastic into liquid fuel

A process for catalytic gasification of carbonaceous feedstock

An improved process for the catalytic gasification of a carbonaceous feedstock in a dual fluidized bed reactor for producing synthesis gas is disclosed. The disclosure uses .gamma.-alumina as a catalyst support iand heat carrier in the gasification zone (102). The gasification zone (102) is operated at 700 - 750 °C to prevent substantial conversion of .gamma.-alumina to .alpha.-alumina, which would manifest in the enablement of high catalyst loading and high recyclability. The catalyst is an alkali metal, preferably K2CO3, so that conversion proportional to total K2CO3 to solid carbon ratio is achieved with as high K2CO3 loading as 50 wt% on the solid support. The combustion zone (140) is operated at 800° - 840° C, to prevent any conversion of the .gamma.-alumina to a-alumina, so that catalyst recyclability of up to 98% is achieved between two successive cycles.

Process for preparing 2,6-dialkylnaphtalene

A process for producing 2,6-dialkylnaphtalene from a hydrocarbon feedstock that contains at least one component selected from the group consisting of dialkylnaphtalene isomers, monoalkynaphtalene isomers, polyalkylnaphtalenes, and naphtalene, is provided that includes the following steps: I) separating the hydrocarbon feedstock and/or a dealkylation product fed from step III in to a naphtalene fraction, a monoalkylnaphtalene fraction, a dialkylnaphtalene fraction and a remaining products fraction; II) separating and purifying 2,6 - dialkylnaphtalene from the dialkylnaphtalene fraction of step I; III) dealkylating the hydrocarbon feedstock and/or the remaining products fractio n of step I and feeding the dealkylation product to step I; and IV) alkylating the naphtalene and monoalkylnaphtalene fractions of step I; wherein the hydrocarbon feedstock is fed to step I or step III.

Process for preparing 2,6-dialkylnaphthalene

The present invention relates to a process of preparing dialkylnaphthylenes and polyalkylenenaphthyleneates dialkylnaphthalenes and polyalkylenenaphthalates.

A process for catalytic gasification of carbonaceous feedstock

公開了一種旨在雙流化床式反應器中生產合成氣體之催化氣化一種含碳原料之改善的工藝。此工藝在氣化區域(102)中使用γ-氧化鋁作為一種催化劑輔料及熱載體。氣化區域(102)運行於700至750℃下，旨在預防γ-氧化鋁大量轉化成α-氧化鋁，由此實現高催化劑載入及高再迴圈率。催化劑是一種鹼金屬，首選K2CO3，以此達成轉化率與K2CO3對固體碳料之比率成正比，且高達50%重量比之K2CO3載入於固體輔料上。燃燒區域(140)運行於800至840℃下，旨在預防任何γ-氧化鋁大量轉化成α-氧化鋁，並使在兩次連續迴圈之間的催化劑再迴圈率達98%。

Process for preparing 2,6-dialkylnaphtalene

A process for producing 2,6-dialkylnaphtalene from a hydrocarbon feedstock that contains at least one component selected from the group consisting of dialkylnaphtalene isomers, monoalkynaphtalene isomers, polyalkylnaphtalenes, and naphtalene, is provided that includes the following steps: I) separating the hydrocarbon feedstock and/or a dealkylation product fed from step III into a naphtalene fraction, a monoalkylnaphtalene fraction, a dialkylnaphtalene fraction and a remaining products fraction; II) separating and purifying 2,6-dialkylnaphtalene from the dialkylnaphtalene fraction of step I; III) dealkylating the hydrocarbon feedstock and/or the remaining products fraction of step I and feeding the dealkylation product to step I; and IV) alkylating the naphtalene and monoalkylnaphtalene fractions of step I; wherein the hydrocarbon feedstock is fed to step I or step III.

Verfarhen for the production of dialkylnaphthalene

Process for preparing 2,6-dialkylnaphthalene

The present invention relates to a process of preparing dialkylnaphthylenes and polyalkylenenaphthyleneates.

Process for preparing 2,6-dialkylnaphthalene

The present invention relates to a process of preparing 2,6-dialkylnaphthalene comprising steps of alkylating monoalkylnaphthalene with an alkylating agent in an alkylation zone and transalkylating naphthalene with dialkylnapthalene other than 2,6-dialkylnaphthalene in a transalkylation zone.

Method for catalytic conversion of waste plastic into liquid fuel

The present disclosure provides a method for catalytic conversion of waste plastic into liquid fuel. The method comprises thermally decomposing the waste plastic at a temperature in the range of 350 to 650° C. and under a pressure in the range of 0.0010 psi to 0.030 psi, to obtain a gaseous stream. The gaseous stream is further subjected to four stage sequential cooling to a temperature in the range of −5 to −15° C. to obtain a gas-liquid mixture comprising a gaseous fraction and a liquid fraction. The gas-liquid mixture is fed to the gas-liquid separator to obtain the gaseous fraction comprising C1 to C4 hydrocarbons and the liquid fraction comprising liquid fuel. The method of the present disclosure is simple, economical and energy efficient, which provides a high value liquid fuel with enhanced yield.

A catalytic cracking process

In a catalytic cracking process for a heavy feed comprising non-distillable and distillable hydrocarbons the feed is initially fract ionated into a heavy fraction comprising at least 10 % by weight non-distillable hyd rocarbons and at least one lighter fraction containing d istillable hydrocarbons. The heavy fraction is then contacted with hot regenerated crac king catalyst in a first zone of a riser reactor at a ca talyst:feed weight ratio of a least 5:1 and a temperature of at least 565 .degree.C (105 0.degree.F), such that the heavy fraction undergoes both thermal and catalytic reactions. The catalyst/feed mixture is then quenched in a quench zone of sa id riser reactor within 2 seconds of said contacting ste p with an amount of the lighter fraction at least equal to 100 wt.% of said non-distil lable hydrocarbons added to said first zone. Catalytical ly cracked products and spent cracking catalyst are subsequently removed from the riser reactor, the spent cracking catalyst is regenerated in a catalyst regeneration zone to produce hot regenerated cracking catalyst which is recy cled to contact said heavy fraction and cracked products are recovered.

Catalytic cracking process and apparatus with improved catalyst flow in swirl regenerator

Processo de recuperação de vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador

a presente divulgação refere-se a um processo para recuperar vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador. o processo compreende pulverizar a escória para obter a escória pulverizada (2). a escória pulverizada (2) é imergida em água (6) e em um sal alcalino (4) para obter uma pasta (8), seguida de torrefação da pasta na presença de ar para obter a escória torrada (12) que é lixiviada (14) para obter uma primeira solução (18). a primeira solução (18) é aquecida a uma temperatura na faixa de 60ºc a 80ºc, enquanto se adiciona um sal de ferro (17) em uma quantidade na faixa de 10% em peso a 60% em peso a um ph na faixa de 4 a 10, para se obter um segundo resíduo sólido (21), que é seco para se obter vanadato de ferro (24).

Process for preparing 2,6-dimethylnaphthalene

Process for recovering vanadium in the form of iron vanadate from a gasifier slag

The present disclosure relates to a process for recovering vanadium in the form of iron vanadate from a gasifier slag. The process comprises pulverizing the slag to obtain pulverized slag (2). The pulverized slag (2) is soaked in water (6) and an alkali salt (4) to obtain a slurry (8), followed by roasting the slurry in the presence of air to obtain roasted slag (12) which is leached (14) to obtain a first solution (18). The first solution (18) is heated at a temperature in the range of 60° C. to 80° C. while adding an iron salt (17) in an amount in the range of 10 wt % to 60 wt % at a pH in the range of 4 to 10, to obtain a second solid residue (21) which is dried to obtain iron vanadate (24).

Conversion of methanol to olefins in a tubular reactor

Processo para obter óxido de vanádio a partir de uma escória de gaseificador

PROCESSO PARA OBTER ÓXIDO DE VANÁDIO A PARTIR DE UMA ESCÓRIA DE GASEIFICADOR. É divulgado um processo para obter componente de vanádio na forma de óxido de vanádio a partir de escória de gaseificador. O processo compreende pulverizar a escória para obter escória pulverizada, que é misturada com água e um sal alcalino para obter uma pasta. A pasta é seca e depois torrada na presença de ar para obter uma escória torrada. A escória torrada é lixiviada para se obter um primeiro filtrado compreendendo o componente de vanádio. O primeiro filtrado reage com um sal de magnésio para remover um componente de sílica na forma de um precipitado. O segundo filtrado livre de sílica reage com um sal de amônio para obter metavanadato de amônio, que é posteriormente calcinado para se obter uma quantidade significativa de pentóxido de vanádio (V2O5).

Processo de recuperação de vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador

A presente divulgação refere-se a um processo para recuperar vanádio na forma de vanadato de ferro a partir de uma escória de gaseificador. O processo compreende pulverizar a escória para obter a escória pulverizada (2). A escória pulverizada (2) é imergida em água (6) e em um sal alcalino (4) para obter uma pasta (8), seguida de torrefação da pasta na presença de ar para obter a escória torrada (12) que é lixiviada (14) para obter uma primeira solução (18). A primeira solução (18) é aquecida a uma temperatura na faixa de 60°C a 80°C, enquanto se adiciona um sal de ferro (17) em uma quantidade na faixa de 10% em peso a 60% em peso a um pH na faixa de 4 a 10, para se obter um segundo resíduo sólido (21), que é seco para se obter vanadato de ferro (24).

Process for obtaining vanadium oxide from a gasifier slag field

A process for obtaining vanadium component in the form of vanadium oxide from gasifier slag is disclosed. The process comprises pulverizing the slag to obtain pulverized slag, which is blended with water and an alkali salt to obtain a slurry. The slurry is dried and then roasted in the presence of air to obtain a roasted slag. The roasted slag is leached to obtain a first filtrate comprising the vanadium component. The first filtrate is reacted with a magnesium salt to remove a silica component in the form of a precipitate. The silica free second filtrate is reacted with an ammonium salt to obtain ammonium metavanadate, which is further calcined to obtain the significant amount of vanadium pentoxide (V2O5).

Un procedimiento para la conversión catalítica de residuos de plástico en combustible líquido

La presente divulgación proporciona un método para la conversión catalítica de residuos de plástico en combustible líquido. El método comprende descomponer térmicamente el plástico de desecho a una temperatura en el rango de 350 a 650 °C y bajo una presión en el rango de 0,0010 psi a 0,030 psi, para obtener una corriente gaseosa. La corriente gaseosa se somete además a un enfriamiento secuencial de cuatro etapas a una temperatura en el intervalo de -5 a -15ºC para obtener una mezcla gas-líquido que comprende una fracción gaseosa y una fracción líquida. La mezcla gas-líquido se alimenta al separador gas-líquido para obtener la fracción gaseosa que comprende hidrocarburos C1 a C4 y la fracción líquida que comprende combustible líquido. El método de la presente divulgación es simple, económico y eficiente desde el punto de vista energético, lo que proporciona un combustible líquido de alto valor con un rendimiento mejorado. (Traducción automática con Google Translate, sin valor legal)

Process for obtaining vanadium oxide from a gasifier slag

Reduction of benzene content of reformate in a catalytic cracking unit

A process for reducing the benzene content of a reformate stream in a conventional catalytic cracking reactor (4) wherein a heavy hydrocarbon feed is cracked to lighter products by contact with a supply of hot regenerated cracking catalyst from a regenerator (6) is disclosed. The reformate can be mixed with the heavy feed to the cracking reactor (4), but preferably reformate contacts hot regenerated cracking catalyst before the heavy feed is added. Benzene removal can be enhanced by adding a light reactive gas such as ethylene to the cracking reactor (4), by adding heavier aromatics, such as a light cycle oil, or both. The reaction is preferably conducted in an FCC riser reactor, but may be conducted in a moving bed reactor.

A catalytic cracking process

Reduction of benzene content of reformate in a catalytic cracking unit

２−メチルナフタレンの製造方法

(57)【要約】 【課題】 2-ＭＮへの選択性が高いと共に、メチルナフ タレン以外の副生成物への転化率が低く、しかも長期に 亘って触媒活性を維持することのできる2-ＭＮのナフタ レンの製造方法を提供する。 【解決手段】 1-ＭＮを含有する原料を触媒組成物を用 いて異性化し2-ＭＮを製造するにあたり、上記触媒組成 物として、Ｘ線回折で実質的に下記の格子面間隔（Å） にピークを示す合成ゼオライトを用いる。１２．３６± ０．４，１１．０３±０．２，８．８３±０．１４， ６．１８±０．１２，６．００±０．１０，４．０６± ０．０７，３．９１±０．０７，３．４２±０．０６

Process for preparing 2-methylnaphthalene