CA1173816A - Fixed bed catalyst - Google Patents

Fixed bed catalyst

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Publication number
CA1173816A
CA1173816A CA000410141A CA410141A CA1173816A CA 1173816 A CA1173816 A CA 1173816A CA 000410141 A CA000410141 A CA 000410141A CA 410141 A CA410141 A CA 410141A CA 1173816 A CA1173816 A CA 1173816A
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Prior art keywords
catalyst
activated carbon
fixed bed
carbon fibers
reaction
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CA000410141A
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French (fr)
Inventor
Yoshihisa Fujimoto
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Asahi Kasei Corp
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Asahi Kasei Kogyo KK
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
    • C07C51/245—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of keto groups or secondary alcohol groups
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/18—Carbon
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/38—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals
    • B01J23/40—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of noble metals of the platinum group metals
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • B01J35/58—Fabrics or filaments
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/143—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones
    • C07C29/145—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones with hydrogen or hydrogen-containing gases
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/02—Monohydroxylic acyclic alcohols
    • C07C31/10—Monohydroxylic acyclic alcohols containing three carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C33/00—Unsaturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C33/18—Monohydroxylic alcohols containing only six-membered aromatic rings as cyclic part
    • C07C33/20—Monohydroxylic alcohols containing only six-membered aromatic rings as cyclic part monocyclic

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Catalysts (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

ABSTRACT OF THE DISCLOSURE
A fixed bed catalyst is described, comprising activated carbon fibers and an active catalyst component or components deposited thereon wherein the activated carbon fibers are formed in a structure in which they are interwined with each other and which has such a high space-retention force as to maintain a bulk density of 0.2 g/cm3 or less at a compression load of at least 1 kg/cm2. This fixed bed catalyst allows a fluid to pass therethrough smoothly and maintains an increased contact area between the fluid and the catalyst.

Description

~ 173~ 1 ~

FIXED BED CATALYST

FIELD O~ TE~E INVENTION
The present in~ention relates to a ~ixed bed catalyst, and more particularly, to a fixed bed catalyst which allows a fluid to pass therethrough without large lesistance, and which produces and maintains a large con~act area between the fluid and the catalyst, and fu~thermore, when the fluid contains a gas and a liquid, between the gas and ~he liquicl.
` BACKGROUND O~ THE INVENTION
Activated carbon has heretofoTe been used as a catalyst support in a powdery or granular :Form. Furthermore, acti~ated carbon powder o grains are solidified together : , wi-th ac-ti~r~ catalyst compo~en~s or components, which can be ~; 15 activated later,~by means of compression molding or the like to produce a porous solid product si~ilar tD a sintered metal. The porous solid product thus obtained has been used, ~or example, as an ~lectrode in a fuel cell.
These porous solid catalysts, howe~e~, produce :
large resis-tance when a flud is passed therethrough, and cannot be used in a tubular reactor in~which a reaction is carried out while ~lowing a ~luid over a long distance.
Thus, many d~f~:iculties have been encoun~ered in utilizing such pOTOUS solid catalysts in other industrial applications.
:
;

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, `
.

~173~l~
Catalytic reaction equipment generally used in the chemical industry can be divided into a fixed bed reactor and a fluidized bed reactor. Such a fixed bed reactor is widely used in a gas pllase fixed bed reaction system, for example, in hydrogenation reactions such as the production of aniline from nitrobenzene and the production of cyclohexane from benzene and, furthermore, in hydrogenation reactions in petroleum refining. Also, hydro-desulfurization of heavy oil is carried out in a liquid phase fixed bed reaction system.
The ixed bed reactor has the advantages that means adapted to separate ~he catalyst ~rom the reaction product is not needed~ and a reaction can be carried out at a high catalyst concentration. In the fixed bed reaction equipment, however, it is required that the catalyst be used in the form of pellets prepared by solidifying the catalyst or in the orm of coarse grains. This oten gives rise to problems such as brealcage of the pelle~s or grains and a reduction in activity which is caused by sinterlng o~ the surface of the pellets or grains. Furthelmore, in employing these pellets or grains, problems arise in tha~ the flow and diffusion of a 1uid in the interior thereo are not smooth because of their coarseness even though they are porous, and in that since their surace areas as a particle are small, the contact between gas and liquid is disadvantageously in-suicient.

.

-3 8 :~ ~
A fluidized bed reactor is used in hydrogenation of alkylanthraquinone for the production o hyd~ogen per-oxide, hydrogenation o~ glucose for the production o sorbitol, and so forth.
In the fluidized bed reactor, a finely dividea catalyst can be used and, thereore, it has the advantage that the contac~ between the catalyst and a fluid such as a liquid and a gas can be enhanced. Furthermore, there is no danger o the ca~alyst losing its activity by the accumula-tion of heat due to the reaction in the catalyst grains.
The fluidized bed reactor~ however, requires means to separate the catalyst from the reaction product, and this separation is troublesome since the catalyst is in a inely divided form. In particular, i~ a reaction is intended to be ef~icien~ly carried out at a high catalyst concentration, the separation of the catalyst will become more diicult and -troublesome.
- ~ In o~der to overcome the above-described problems, a method has been disclosed in U.S. Patent 4,182,919)~ in .. . .
~ 20 whlch a ilter is employed to separate a catalyst in a ., reactor. This method, however, suffers from various problems l such as blocking of the filter and ~everse-washing operation `; o-f the filteri When a reaction product has a low boiling point as in the production o cyclohexane~ ~he ca~alyst can be separated ~rom ~he reaction product by withdrawing the ~ ~ .
l ; - 3 -.,; .
., .

' 3 8 ~ 6 reaction product from an upper portion o~ the reactor in a gaseous form. In the production of reaction products having a high boiling point, such as sorbitol, however, the above-described method cannot be employed.
In a fluidized bed reactor using finely divided catalysts the contact between fluids, i~e., gas and liquid, is insufficient although the contact between the catalyst and the fluid can be improved. Thus, the fluidized bed reactor requires procedures consuming a large quantity of energy, such as the use of vigorous stirring while introducing a large amo~mk o~ gas in~o ~he liquid.
An object of the invention is to provide a ixed bed catalyst which provides a large contact area between a 1uid and the catalyst, and which allows the 1uid to 10w and di~fuse smoo~hly -therethrough although it is a catalyst -for use in a ixed bed reactor.
Another object of the lnvention is to provide a ~ fixed~bed catalyst which increases the contact area between ; ~ a gas and a liqu~id.
Still another object of the invention is to ~provide a catalyst having a high activity.
SUMMARY 0~ THE IN~ENTION
~ In accordance with the present invention there is provided a ~ixed bed ca~alyst comprising activated carbon ibers and an ac~ive ca~alyst component or components ,.', " .

, , .

:1 173~ 1 6 deposited on the activated carbon fibers. The activated carbon fibers are formed in a structure in which they are intertwined with each other. The structure has a high space-retention force such that a bulk density of 0.2 g/cm3 or less at a compression load of at least 1 kg/cm2 is maintained.
DETAILED DESCRIPTION OF TH~ INVENTION
The fixed bed catalyst according to the present invention is prepared by depositing an active catalyst component or components on fibrous activated carbon or activated carbon fibers having a large specific surface area and high adsorptivity. These activated carbon -ibers are prepared by subjecting carbon fibers obtained rom various ; materials, such as acryl fibers, cellulose fibers~ and pitch, or flame-resistant fibers which have not yet been sufficiently carbonized7 to an activation treatment, such as a steam : :
treatment, to make them active and porous. The fibers are .
used in a bulky condition wherein the fibers are intertwined with each other, e.g., in a felt-like form.
An activated carbon flber has stiffness as a single yarn, i.e., indi~idual fiber, and a bulky aggregation of such activated carbon fibers is characterized in that it can resist a strong compression force and in that a low bulk density is maintalned. Therefore, even if a fluid is passed under pressure khrough -~his fixed bed catalyst, no appre-ciable deformation will OCCUT and the bulkiness lS maintained.

5 _ ~ ~73~ 1 6 Thus, the fixed bed catalyst of the invention allows a fluidto pass therethrough withou~ large resistance. Furthermore, since the spaces between fibers remain uncollapsed, a large contact area between the fluid and the catalyst, and a large contact area between a liquid wetting the fiber and a gas are stably maintained.
Uniform deposition o an active catalyst component or components on activated carbon fibers having a structure such that they are intertwined with each other ~hereinater this structure is re-Eerred ~o as a "felt structure") requires techniques unlike ~hose employed for powdery or granular activated carbon. Such techniques include a method in which a liquid containing ~he catalyst component or components is circulated rapidly in a felt of activated carbon fibers to avoid~uneven adsorption of the catalyst9 a method in which the specific catalyst component is chosen so as to achieve slow adsorption thereof on the fibers, and a method in which, with a gradual increase in temperature, compounds which are sparingly adsorbed are converted into those which are easily adsorbed.
Various techniques can be developed depending on the type of the desired active catalyst component and pre-ferred ones can be selected.
In charging the fixed bed catalyst of the invention into a fixed bed reactor, it is preferred to pack felt sheets .

:~73~
one UpOTI another into a reactor wi~h compressing since a uniform fixed bed can be easily obtained.
By way of example, the relationship between compression force and bulk density when felts comprising activated carbon fibers having a single yarn diameter of 7 to 20 microns are packed, while compressing, in a cylinder having a diameter of 2 cm is shown in Table 1. A low bulk density is maintained at a fairly high compression force.
- Therefore, the structure remains unchanged also under the pressure of the flow of the ~luid, allowing the liquid to pass -therethrough smooth:ly, and main~ains an increased con-tact area between the -fluid and the catalyst or between the liquid wetting the fiber sur~ace and a gas. Thus, in combination with the properties of the activated carbon that produce a deposited ca~alyst having a high activi-ty, there ; can be obtained a ~ixed bed catalyst structure having a high reaction activi-ty.
Table l Compression Force ~ Bulk Density ~(kg/cm2) ~ (g/cm3) 1 0.08
2 0.10 4 0.12 8 0.16 12 0.20 - 7 - , ' ' ~
.

` ~'' '`, 1~L73~t6 In order to determine the pressure loss when a fluid is passed through a fixed bed having a bulk density as shown in Table 1 above, water and air were passed through the fixed bed at ~arious velocities. It has been found that the pressure loss can be represented by the ollowing formula ~1) QP = 0.9 x pl- (VL + 0.04 VG) ~1) wherein ~ P is a pressure loss ~kg/cm2-m~, p is a bulk de~si~y.(g/cm3), V~ is the volume of water passing per unit area of the inner cross sec~ion of the ixed bed (cm3/min-cm2), and : YG is the volume o air passing per unit area of the inner CTOSS section of ~he fixed bed ~cm31min cm2).
, lS : In general~ in ca.rrying out a reaction by the use o~
an~industrially employed reactar~column, it is preferred from ~; an~economic viewpoint that the~ helght of the column~is~about :~ ~ m and the:residence time of a reaction solution is within , ~ .
lO hours. When the ~ixed bed catalyst of the invention~is , charged tol.a~height of 5 m such that the bulk density lS
0.2 g/cm , and ~ liquid such.as water and a gas such as air are passed through the above-prepared catalyst bed at rates o~ 1 cm3/min-cm2 and 10 cm3/min cm2, respectively, the residence time of ~he liquid is within 10 hours and the , : - 8 -s ~ ~ ' i. ~

, ' ~1~38l~
pressure loss resulting rom the flow of the 1uid is l kg/cm2 or less according to the above-described for~ula (I). Thus 7 in order that the fixed bed remain unchanged and maintain a stable s-tructure, it is required that the fixed bed catalyst structure have a strength such that it retains a bulk density of 0.2 g/cm3 or less at a compression load of 1 kg/cm2. It is important that the fixed bed catalyst structure must not be deformed`by the flow pressure o~ fluid. Therefore, it is preferred that the fixed bed catalyst structure has lower bulk density at higher flow pressure of fluid. It can be readily seen fTom Table 1 that the fixed bed catalyst of the invention possesses such a strength.
When a fluid is passed through the fixed bed catalyst o the invention, the fluid exhibits a flow very similar to piston flow. This is supported by the ~act that even when wa-ter~and air are passed ~here~hrough, there is observed a s~arp pea~ in the residence tlme distrubution of the water.
This flow behavior indica~es ~ha~ TeveTse-mixing is reduced, and is suitable for obtaining the desired product at~a hlgh ::
~20 conversion. Depending on the type o~ reaction, substances to : be reacted tend~to flow more slowly than the fluid by lts , interaction with the acti~ated carbon. This is often preferred in a practical operation.
In order to change the flow of a fluid in a fixed bed of the catalys~ o the invention, or ~he flow of each o '! -- 9 '', .. . .

~ 1738~ 6 a gas and a liquid, other fillers such as wire mesh may be incroporated into the fixed bed to form therein a plate-like or spherical space. However, a fixed bed consisting of the actiuated carbon fiber structure alone is preferred in that it provides a most uniform piston ~low.
The activated carbon fibers employed in the present invention exhibit stiffness sufficient to withstand compression force as long as the single yarn diameter is at least 3 microns.
Furthermore~ when the single yarn diameter is 50 microns or less, the brittleness of the fiber is such that i~ does not cause a disadvantage. A commercially available activated carbon felt usually comprises intertwined fibers having single yarn diameters of several microns to several ten microns, and .

can be used satisfactorily in the invention. Moreover, its specific surface area is about 1,000 m2/g which is nearly equal to that of the usuat activated carbon, and its adsorption properties are as high as that of the usual activated carbon.
Various activated carbon fibers are commercially available and, there~ore, those fibers which exhibit the optimum actlvity when used in comblnation with an active catalyst component or components should be selected.
Various active catalyst components can be used in the invention depending on the type of reaction for which the ultimate activated carbon iber catalyst is used. Typical examples of catalyst components which can be used include ~:

~ ~3816 noble metals such as Pt, Pd, Rh, Ru, Os, and Ir, for which activated carbon is favorably used as a support.
These active components are used singly or as a mix~ure comprising two or more thereof to impregnate the activated carbon fibers therewith, or are deposited on the activated carbon fibers. The amount of the active component being deposited, when the activated carbon ~iber structure is used as a support, is generally from 0.01 to 10~ by weight, as calculated as the metallic element, of the support, which 0 lS the same as the range conventionally employed.
The following examples and comparative examples are given to illustrate the invention in greater detail although the invention is not intended to be limited thereto.

lS An activated carbon fiber felt (:produced by Toho Rayon Co., Ltd., containing 4 to 6% by weight of nitrogen) was impregnated with an aqueous solution of a noble metal chloride by circulating the aqueous solution therethrough.
After neutralizing with a 1 N aqueous caustic soda solution, 2a the felt was washed with water and~dried at 90C for 20 hours. Thereafter, the noble metal chloride was reduced in a stream of hydrogen at 150C for 1 hour to prepare an activated carbon fiber catalyst. Then, 6 g o -the catalyst thws produced was charged into a stainless steel pipe having 2S a diameter of 2 cm and a length o 20 cm to form a fixed ~ 1~38~
catalyst bed having a bulk density of 0.l0 g/cm3 at a compres-sion load of 2 kg/cm2, through which a 1% aqueous solution of acetone and hydrogen gas were passed downward at rates of l00 ml/min and l NL/min, respectively, at an ordinary tempera-ture and atmospheric pressure. In this way, a continuousreaction was per~ormed to convert acetone to isopropyl alcohol.
The resul~s are shown in Table 2.
Table 2 Noble Metal DepositedConversion ~) l~ 5% Ru l00 2% Ru -~ 3% Pd 95 2~ Ru ~ 3~ Pt l00
3% Ru ~ 2% Rh lO0 5~ Rh 52 Powdery ac~ivated carbon ~Norit) and an aqueous soIution o a noble me~al chloride were mixed and stirred~
neutralized with a l N aqueous caustic soda solution, ~iltered, wasiled with water, and thereafter treated in the same manner 20 as in Example 1 to prepare a catalyst. Then, a 1% aqueous solution o~ acetone containing 10% by weight of the catalyst as prepared above was passed upward through a stainless steel pipe having a diame~er of 2 cm and a length of 20 cm at a rate o~ l00 ml/min, and in addition, hydrogen gas was passed therethough at a ra~e of l NL/min at the inlet o the stainless ~k -~ra~ ~na~l( .

- ' ' ' 1;~738~6 steel pipe. At the outlet of the stainless steel pipe, the liquid and gas were separated from each other immediately.
In this way, a continuous reaction was perormed to convert acetone to isopropyl alcohol. The results are shown in Table 3.
Table 3 Noble Metal Deposited COnVeTSiOn 5% Ru 32 2% Ru + 3% Pd 25 2~ Ru ~ 3% Pt 46 3~ Ru ~ 2% Rh 35 5~ Rh 15 A ibrous activated carbon felt ~produced from cellulose fiber) was impregnated with an aqueous solution of a noble me~al chloride and dried. The noble metal chlo~ide was~ then reduced in a stream of hydrogen at 200C or~1 hour to prepare a catalyst. Then, 4.5 g of the catalyst was charged into a stalnless steel pipe having a diameter of 2 cm and a length of 20 cm to oTm~a ixed catalyst bed having a bulk density o~ 0.08 g/cm3 at a compression load of 1 kg/cm3, through which a 5% tert-butanol solution of phenylacetone and hydrogen gas were passed downward at ra-tes of 10 ml/min and 1.5 NL/min~ respectively, at an ordinary temperature and atmospheric pressure. In this way, a continuous reaction was , 3~

performed to con~ert phenylacetone to methylbenzyl carbinol.
The results are shown in Table 4 below.
Table 4 Noble Metal DepositedConversion (~) 5~ Ru 93 S% Os 100 5% Pt 90 Twelve grams of a~ca-talyst comprising a fibrous activated carbon elt (produced by Toyobo Co., Ltd.) with 5%
by weigh-t of Pd deposi~ed thereon was charged into a stainless .
steel pipe having a diameter of 2 cm and a length of 20 cm to form a ixed catalyst bed having a bulk density of 0.19 g/cm at a compression load of 12 kg/cm2, through which 150 ml ~ a 30% àqueous solu-tion o~ glucose~was circula~ed upward at a ~rate of 25 ml/min and air was passed upward at a rate of ; 0.8 NL/min. During the~reaction, the pH o the ~react~ion solution was maintained at~ 9 to lO~with a 1 N aqueous~ caustic ~ ;
~ soda solutlon. In~this way,~a reaction was performed at an ~ ~ ~
-~ 20 ordinary temper~ture and atmospheric pressure, and the ~:
conversion of glucose to gluconic~acid was 59.1 Into a s~ainless steel pipe having a diameter oX
2 cm and a leng~h of 20 cm was charged 8.5 g o~ a catalyst :, , ~ -' , :
- . .
.
': ' ' ' ' 1 ~738 ~ ~
comprising a fibrous activated carbon felt (produced by Toyobo Co., Ltd.) with 4.7% by weight of Ru and 0.3% by weight of Pd deposited thereon to form a fixed catalyst bed ha~ing a bulk density of 0~14 g/cm3 at a compression load of 6 kg/cm2. Then, 140 ml of a 50% aqueous solution of glucose was circulated downward in the stainless steel pipe at a rate of 8 ml/min and hydrogen was passed downward therethrough at a rate of 2.0 N~/min. During the reaction, the pressure was maintained at 7.5 kg/cm2 and the temperature at 120G. In this way, a reaction was performed for 3 hours. Glucose was reduced to sorbitol a~ a conversion of 100~.

A 100-ml autoclave provided with a stirrer was charged with 4.25 g of a catalyst comprising powdery activated carbon ~Norit) with 4.7~ by weight of Ru and 0.3~ by weight of Pd deposited -~hereon~ and 70 ml of a 50% aqueous solution of glucose. A reaction was performed while maintaining the pressure at 7.5 kg/cm2 by introducing hydrogen and the temperature at 120C, and while stirriDg for 3 hours. Glucose was reduced to sorbitol at a conversion of 32~.
While the invention~has been described in detail and ' with reference to specific embodiment thereof, it will be apparent to one skilled in the art that various changes and modificatio~s can be made therein without departing from the spirit and scope *hereof.

.

Claims (3)

WHAT IS CLAIMED IS:
1. A fixed bed catalyst comprising activated carbon fibers having at least one active catalyst component deposited on the activated carbon fibers and wherein the activated carbon fibers are formed in a structure in which they are interwined with each other to form a felt-like support, said structure being capable of maintaining a bulk density of 0.2 g/cm3 or less at a compression load of at least 1 kg/cm2.
2. The fixed bed catalyst of Claim 1, wherein said activated carbon fibers have a yarn diameter of about 3 to 50 microns.
3. The fixed bed catalyst of Claim l or 2, wherein said at least one active catalyst component is selected from the group consisting of Pt, Pd, Rh, Ru, Os and Ir, and compounds thereof.
CA000410141A 1982-02-25 1982-08-25 Fixed bed catalyst Expired CA1173816A (en)

Applications Claiming Priority (2)

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JP28083/82 1982-02-25
JP57028083A JPS58146446A (en) 1982-02-25 1982-02-25 Fixed bed catalyst

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FR (1) FR2521873A1 (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7041847B2 (en) 2001-01-31 2006-05-09 Basf Aktiengesellschaft Method for cleaning crude terephthalic acid and catalysts suitable for the same and containing carbon fibers
EP2816646A4 (en) * 2012-02-15 2015-10-21 Toppan Printing Co Ltd Carbon fiber composite, process for producing same, catalyst-carrying body and polymer electrolyte fuel cell
US11338271B2 (en) 2018-02-21 2022-05-24 Dexerials Corporation Porous carbon material, method for producing same, and catalyst for synthesis reaction

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB8716565D0 (en) * 1987-07-14 1987-08-19 British Petroleum Co Plc Catalyst
DE3931420A1 (en) * 1989-09-21 1991-04-04 Bayer Ag CATALYSTS BASED ON METAL-Doped CARBON FIBERS, THEIR PRODUCTION AND THEIR USE
BE1002971A3 (en) * 1990-06-22 1991-10-08 Catalysts & Chem Europ GRAIN CATALYSTS WITH IMPROVED MECHANICAL BEHAVIOR AND PROCESSES FOR THE PREPARATION THEREOF.
DE19748468A1 (en) * 1997-11-03 1999-05-06 Hoechst Ag Coated knitted fabrics as catalytic fillings for distillation columns
FR2771309B1 (en) * 1997-11-24 2000-02-11 Messier Bugatti ELABORATION OF ACTIVE CARBON FIBER CATALYST SUPPORT
DE10226969B4 (en) 2002-06-17 2006-05-18 Sgl Carbon Ag Activated carbon fibers and process for their preparation
JP4116891B2 (en) * 2003-02-03 2008-07-09 独立行政法人科学技術振興機構 Catalyst for reduction reaction, production method thereof, and selective hydrogenation method
WO2007029667A1 (en) * 2005-09-07 2007-03-15 National University Corporation Nagaoka University Of Technology Hydrogenation catalyst for carbonyl group, method for producing same, and method for producing unsaturated alcohol by using such catalyst
CN108299207B (en) * 2018-02-12 2019-06-18 中国科学院化学研究所 A kind of method of heterogeneous catalytic hydrogenation reduction unsaturated compound
JP6646087B2 (en) * 2018-02-21 2020-02-14 デクセリアルズ株式会社 Porous carbon material, method for producing the same, and catalyst for synthesis reaction

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1440817A (en) * 1965-04-22 1966-06-03 Produits Refractaires Improvements to catalytic devices
GB1436245A (en) * 1972-09-08 1976-05-19 Kanebo Ltd Catalysts for the oxidation of carbon monoxide and their pro duction
US4011651A (en) * 1973-03-01 1977-03-15 Imperial Chemical Industries Limited Fibre masses
JPS5018878B1 (en) * 1974-08-03 1975-07-02
JPS604151B2 (en) * 1975-09-29 1985-02-01 トヨタ自動車株式会社 Ceramic fiber moldings for manifolds and reactors

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7041847B2 (en) 2001-01-31 2006-05-09 Basf Aktiengesellschaft Method for cleaning crude terephthalic acid and catalysts suitable for the same and containing carbon fibers
EP2816646A4 (en) * 2012-02-15 2015-10-21 Toppan Printing Co Ltd Carbon fiber composite, process for producing same, catalyst-carrying body and polymer electrolyte fuel cell
US11338271B2 (en) 2018-02-21 2022-05-24 Dexerials Corporation Porous carbon material, method for producing same, and catalyst for synthesis reaction

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JPS58146446A (en) 1983-09-01
AU8649882A (en) 1983-09-01
DE3229905A1 (en) 1983-09-01
FR2521873A1 (en) 1983-08-26

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