Patent Description:
<NUM>,<NUM>-butadiene, a major basic product of petroleum fraction, is a representative raw material used in preparation of synthetic rubber, and the price thereof fluctuates rapidly in connection with supply and demand of the petrochemical industry. Examples of methods of preparing <NUM>,<NUM>-butadiene include naphtha cracking, direct dehydrogenation of normal butene, oxidative dehydrogenation of normal butene, and the like.

According to the method of preparing <NUM>,<NUM>-butadiene by oxidative dehydrogenation of normal butene, butene and oxygen react in the presence of a metal oxide catalyst to generate <NUM>,<NUM>-butadiene and water. In this case, water generated as a result of the reaction is stable. Thus, the method is thermodynamically very advantageous. In addition, since oxidative dehydrogenation of normal butene is an exothermic reaction unlike direct dehydrogenation, reaction can be performed at a low temperature. Thus, <NUM>,<NUM>-butadiene can be obtained in high yield while reducing energy consumption. In addition, in the case of oxidative dehydrogenation, since an oxidizing agent is added, the generation amount of carbon deposits which shorten catalyst life by poisoning the catalyst is reduced. Further, since removal of the oxidizing agent is easy, the method of preparing <NUM>,<NUM>-butadiene using oxidative dehydrogenation is very suitable for commercialization.

However, heat generated during oxidative dehydrogenation is accumulated in a catalyst bed, deteriorating a catalyst, thereby degrading catalyst life, and side reaction is promoted by excess heat, thereby reducing reaction efficiency. As a result, butadiene yield, selectivity for butadiene, and the conversion rate of butene can be lowered.

To solve these problems, a method of controlling space velocity by controlling the amount of gas fed to a reactor has been proposed. However, this method was unsatisfactory in terms of productivity and yield. Thus, development of a system for oxidative dehydrogenation of butene that can effectively control heat generated inside a reactor while having high productivity is still required.

[Patent Document] (Patent Document <NUM>) <CIT>.

<CIT> relates to improved yields and high selectivities of unsaturated hydrocarbons obtained by dehydrogenating under certain specified conditions hydrocarbons in the vapor phase at elevated temperatures in the presence of oxygen and a catalyst containing magnesium ferrite. <CIT> relates to a process for the dehydrogenation of a hydrocarbon in the presence of a catalyst containing nickel ferrite.

<CIT> discloses a process of producing a conjugated diene including a step of mixing a raw material gas containing a monoolefin having a carbon atom number of <NUM> or more with a molecular oxygen-containing gas and supplying the mixture into a reactor, and a step of obtaining a corresponding conjugated diene-containing product gas produced by the oxidative dehydrogenation reaction of the monoolefin having a carbon atom number of <NUM> or more in the presence of a catalyst, wherein the concentration of a combustible gas in the gas supplied to the reactor is not less than the upper explosion limit and the oxygen concentration in the product gas is from <NUM> to <NUM> vol %.

<CIT> relates to a catalyst which comprises a catalytically active multimetal oxide which comprises molybdenum and at least one further metal and a process for the oxidative dehydrogenation of n-butenes to butadiene.

<CIT> relates to heat dissipating diluents in fixed bed reactors.

<CIT> provides a catalyst molded product including an inert support, an intermediate layer positioned on the surface of the inert support, and an active layer positioned on the surface of the intermediate layer, wherein the active layer includes a catalyst powder and a binder; a method for producing same; and a <NUM>,<NUM>-butadiene production method using same.

<CIT> relates to a catalyst system for oxidative dehydrogenation, a reactor for oxidative dehydrogenation including the catalyst system, and a method of performing oxidative dehydrogenation using the reactor. More specifically, it relates to a catalyst system in which a fixed-bed reactor is filled with a catalyst for oxidative dehydrogenation in an n-stage structure (n being an integer of <NUM> or more), wherein each stage of the n-stage structure satisfies Equations <NUM> and <NUM>.

Therefore, the present invention has been made in view of the above problems, and it is one object of the present invention to provide a catalyst system for oxidative dehydrogenation capable of effectively controlling heat generated inside a reactor to prevent catalyst deterioration, thereby improving conversion rate, selectivity, and yield.

It is another object of the present invention to provide a reactor for preparing butadiene including the catalyst system for oxidative dehydrogenation and a method of preparing <NUM>,<NUM>-butadiene using the reactor.

In accordance with one aspect of the present invention, provided is a catalyst system for oxidative dehydrogenation, wherein a reactor is filled with a catalyst for oxidative dehydrogenation in an n-layer structure, wherein n is an integer of <NUM> or more, wherein the catalyst is diluted and the reactor is filled with the diluted catalyst so that each layer of the n-layer structure satisfies Equations <NUM> and <NUM> below. <MAT>
wherein X represents a content of AB<NUM>O<NUM> and is <NUM> to <NUM>, wherein AB<NUM>O<NUM> is an active ingredient of a catalyst, wherein A is one or more selected from the group consisting of copper (Cu), radium (Ra), barium (Ba), strontium (Sr), calcium (Ca), beryllium (Be), zinc (Zn), magnesium (Mg), manganese (Mn), cerium (Ce), zirconium (Zr), lanthanum (La), and cobalt (Co) and B is iron (Fe); Y is an amount of a porous support and is <NUM> to <NUM>; and Z is an amount of one or more dilution fillers selected from alumina, silica, silicon carbide, zirconia, titania, and cordierite and is <NUM> to <NUM>, wherein the diluted catalyst is a mixture of the dilution filler and the coating catalyst, the coating catalyst having a porous support coated with the active ingredient AB<NUM>O<NUM>. <MAT> wherein, with respect to the direction in which reactants are fed into the reactor, Xn represents X for the n-th layer, and Xn-<NUM> represents X for the (n-<NUM>)th layer, wherein at least one of the n layers has a Z value greater than <NUM>, and wherein the porous support has a packing density of <NUM> to <NUM>/cm<NUM>.

In accordance with another aspect of the present invention, provided is a catalyst system for oxidative dehydrogenation, wherein a reactor is filled with a catalyst for oxidative dehydrogenation, wherein the catalyst is diluted and the reactor is filled with the diluted catalyst so as to satisfy Equation <NUM> below. <MAT>
wherein X is an amount of AB<NUM>O<NUM> and is <NUM> to <NUM>, wherein AB<NUM>O<NUM> is an active ingredient of a catalyst, wherein A is one or more selected from the group consisting of copper (Cu), radium (Ra), barium (Ba), strontium (Sr), calcium (Ca), beryllium (Be), zinc (Zn), magnesium (Mg), manganese (Mn), cerium (Ce), zirconium (Zr), lanthanum (La), and cobalt (Co) and B is iron (Fe); Y is an amount of a porous support and is <NUM> to <NUM>; and Z is an amount of one or more dilution fillers selected from alumina, silica, silicon carbide, zirconia, titania, and cordierite and is <NUM> to <NUM>, wherein the diluted catalyst is a mixture of the dilution filler and the coating catalyst, the coating catalyst having a porous support coated with the active ingredient AB<NUM>O<NUM>, and wherein the porous support has a packing density of <NUM> to <NUM>/cm<NUM>.

In accordance with another aspect of the present invention, provided is a reactor for preparing butadiene including the catalyst system for oxidative dehydrogenation.

As apparent from the foregoing, the present invention advantageously provides a catalyst system for oxidative dehydrogenation, wherein a catalyst having a porous support on which an active ingredient is uniformly and firmly coated is diluted in a dilution filler and a reactor is filled with the diluted catalyst, or a reactor is filled with a catalyst for oxidative dehydrogenation so that the concentration of an active ingredient included in the catalyst gradually increases in the direction from reactants inlet in which reactants are fed into the reactor to products outlet. When the catalyst system according to the present invention is used, it is possible to effectively control distribution of heat generated inside a reactor during oxidative dehydrogenation without adding a separate apparatus or changing the conventional manufacturing facilities, and thus to improve conversion rate, selectivity, and yield. In addition, catalyst deterioration can be reduced, thereby improving long-term stability of a catalyst.

Hereinafter, the catalyst system for oxidative dehydrogenation according to the present invention will be described in detail.

In the catalyst system for oxidative dehydrogenation according to the present invention, wherein a reactor is filled with a catalyst for oxidative dehydrogenation in an n-layer structure, wherein n is an integer of <NUM> or more, the catalyst is diluted and the reactor is filled with the diluted catalyst so that each layer of the n-layer structure satisfies Equations <NUM> and <NUM> below. <MAT>
wherein X represents an amount of AB<NUM>O<NUM> and is <NUM> to <NUM>, wherein AB<NUM>O<NUM> is an active ingredient of a catalyst, wherein A is one or more selected from the group consisting of copper (Cu), radium (Ra), barium (Ba), strontium (Sr), calcium (Ca), beryllium (Be), zinc (Zn), magnesium (Mg), manganese (Mn), cerium (Ce), zirconium (Zr), lanthanum (La), and cobalt (Co) and B is iron (Fe); Y is an amount of a porous support and is <NUM> to <NUM>; and Z is an amount of one or more dilution fillers selected from alumina, silica, silicon carbide, zirconia, titania, and cordierite and is <NUM> to <NUM>, wherein the diluted catalyst is a mixture of the dilution filler and the coating catalyst, the coating catalyst having a porous support coated with the active ingredient AB<NUM>O<NUM>. <MAT>
wherein, with respect to the direction in which reactants are fed into the reactor, Xn represents X for the n-th layer, and Xn-<NUM> represents X for the (n-<NUM>)th layer, wherein at least one of the n layers has a Z value greater than <NUM>, and wherein the porous support has a packing density of <NUM> to <NUM>/cm<NUM>.

According to the present invention, AB<NUM>O<NUM> is the active ingredient of a catalyst, and the catalyst for oxidative dehydrogenation is a coating catalyst having a porous support coated with the active ingredient AB<NUM>O<NUM>.

For example, AB<NUM>O<NUM> can be a zinc ferrite (ZnFe<NUM>O<NUM>) wherein A is zinc (Zn) and B is iron (Fe). In this case, the catalyst can exhibit excellent activity in oxidative dehydrogenation of normal butene, and can have high selectivity for <NUM>,<NUM>-butadiene.

For example, AB<NUM>O<NUM> can have an average particle diameter of <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, or <NUM> to <NUM>. Within this range, coating of the active ingredient on the porous support can be easily performed, and the catalyst can have excellent activity, thereby improving reaction efficiency.

According to the present invention, AB<NUM>O<NUM> having an average particle diameter within the above range can be selected, for example, using a sieving method.

In Equation <NUM>, X is <NUM> to <NUM>, preferably, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, or <NUM> to <NUM>. Within this range, reaction efficiency can be excellent, thereby improving yield, selectivity, and conversion rate.

For example, the porous support can have an average particle diameter of <NUM> to <NUM> or <NUM> to <NUM>. Within this range, reaction efficiency can be excellent, thereby improving conversion rate and selectivity.

For example, the porous support can have an average pore size of <NUM> to <NUM> or <NUM> to <NUM>. Within this range, coating of AB<NUM>O<NUM> powder can be easy performed and desorption of the powder can be prevented.

According to the present invention, the average particle diameter and average pore size of the porous support can be measured, for example, using a method of calculating a surface area and an average pore size through adsorption isotherm of nitrogen by the BET method and the BJH (Barret-Joyner-Halenda) method, respectively, or using a mercury impregnation method.

The porous support has a packing density of <NUM> to <NUM>/cm<NUM> or, preferably, <NUM> to <NUM>/cm<NUM>. Coating rate is determined based on the packing density. When the porous support has a packing density within this range, separation or desorption of the AB<NUM>O<NUM> powder can be prevented, and the support can be easily coated with the powder. Further, when oxidative dehydrogenation is performed, the conversion rate of butene or <NUM>,<NUM>-butadiene yield can be increased, and excessive increase in the temperature inside a catalyst bed can be suppressed, thereby increasing thermal stability.

According to the present invention, packing density is calculated by dividing mass capable of filling a tubular measuring cylinder to <NUM> cc by a volume value of <NUM> cc thereof.

The porous support is preferably spherical, hollow, or in the form of pellets. In this case, reaction efficiency can be excellent, thereby improving yield, selectivity, and conversion rate.

In the present invention, spherical, pellet, and hollow shapes are not particularly limited as long as they are within the ordinary range of those skilled in the art of porous support technology, and these shapes are clearly distinguished.

For example, the porous support can be one or more selected from the group consisting of alumina, silica, titania, zirconia, silicon carbide, and cordierite, and is preferably alumina or silica. In this case, mechanical strength for filling a reactor is satisfied and side reaction can be reduced.

More preferably, the porous support is alumina. In this case, mechanical strength can be ensured, and butadiene yield and selectivity can be prevented from being lowered by side reaction during oxidative dehydrogenation.

In Equation <NUM>, Y is <NUM> to <NUM>, preferably, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, or <NUM> to <NUM>. Within this range, catalytic activity and heat generation control can be excellent.

The coating catalyst of the present invention can further include an organic/inorganic binder when necessary. In this case, the binder can be included in an amount of <NUM> parts by weight or less, <NUM> to <NUM> parts by weight, or <NUM> to <NUM> parts by weight based on <NUM> parts by weight of AB<NUM>O<NUM>. Within this range, the abrasion resistance of the catalyst can be improved without significantly lowering the efficiency of oxidative dehydrogenation.

For example, the binder can include aluminum-silicate, methylcellulose, hydroxypropyl methylcellulose, or both. When the binder is contained in an appropriate amount, the abrasion resistance of the catalyst can be improved without significantly lowering the efficiency of oxidative dehydrogenation.

As another example, the coating catalyst of the present invention can be a binder-free catalyst. In this case, since side reaction is not caused by the binder, the conversion rate of normal butene and selectivity for butadiene can be greatly increased. In addition, since introduction of some components is omitted, a process of preparing the catalyst can be simplified, thereby reducing process costs.

According to the present invention, binder-free means that an organic or inorganic binder is omitted when preparing a catalyst and/or that a catalyst is prepared without the binder.

For example, a fixed-bed reactor can be filled with the catalyst for oxidative dehydrogenation according to the present invention in a <NUM>- to <NUM>-layer, <NUM>- to <NUM>-layer, <NUM>- to <NUM>-layer, or <NUM>- to <NUM>-layer structure. Within this range, distribution of heat generated inside the reactor can be effectively controlled without significantly increasing process costs. Thus, when butadiene is prepared, conversion rate, selectivity, and yield can be greatly improved, and long-term stability of the catalyst can be improved.

For example, the catalyst system of the present invention satisfies Equation <NUM> below. In this case, excessive heat generation in the catalyst bed can be effectively prevented during reaction. As a result, when butadiene is prepared, conversion rate, selectivity, yield, and long-term stability of the catalyst can be improved. <MAT>
wherein Xn represents X for the n-th layer, and Xn-<NUM> represents X for the (n-<NUM>)th layer.

According to the present invention, at least one of the n layers has a Z value greater than <NUM>. When the coating catalyst is mixed with a dilution filler and a reactor is filled with the coating catalyst so that the concentration of the catalyst is gradually decreased, heat generation control can be effectively performed during reaction, thereby improving reaction efficiency.

According to the present invention, the dilution filler is one or more selected from alumina, silica, silicon carbide, zirconia, titania, and cordierite, and is preferably one or more selected from alumina and silica. In this case, it is possible to suppress generation of excessive reaction heat while minimizing side reaction, thereby greatly improving the efficiency of oxidative dehydrogenation.

The catalyst system of the present invention satisfies Equation <NUM> below when at least one layer has a Z value other than <NUM>. In this case, excessive temperature increase of the catalyst bed due to excessive heat may be suppressed, and thus productivity such as conversion rate, selectivity, and yield can be greatly improved when butadiene is prepared. <MAT>
wherein Yn represents Y for the n-th layer, and Yn-<NUM> represents Y for the (n-<NUM>)th layer.

In addition, the catalyst system of the present invention satisfies Equation <NUM> below. In this case, heat generation due to oxidative dehydrogenation can be effectively controlled so that the activity or stability of the catalyst can be continuously maintained high and reaction efficiency can be improved. <MAT>
wherein Zn represents Z for the n-th layer, and Zn-<NUM> represents Z for the (n-<NUM>)th layer.

As another example, in the catalyst system for oxidative dehydrogenation according to the present invention, a reactor is filled with the catalyst for oxidative dehydrogenation in an n-layer structure, wherein n is an integer of <NUM> or more. In this case, the catalyst is diluted and the reactor is filled with the diluted catalyst so that each layer satisfies Equations <NUM> and <NUM>. In addition, the porous support has a packing density of <NUM> to <NUM>/cm<NUM> or, preferably <NUM> to <NUM>/cm<NUM>. In this case, separation or peeling of AB<NUM>O<NUM> powder from the porous support can be prevented, and the support can be uniformly and firmly coated with the catalyst. In addition, heat generation inside the catalyst bed during oxidative dehydrogenation can be effectively controlled, and side reaction can be suppressed, thereby improving the conversion rate of butene, butadiene yield, and selectivity.

As a specific example, in the catalyst system for oxidative dehydrogenation according to the present invention, a reactor is filled with the catalyst for oxidative dehydrogenation in a three-layer structure. In this case, the catalyst is diluted and the reactor is filled with the diluted catalyst so that each layer satisfies Equations <NUM> and <NUM> below. With respect to the direction in which reactants are fed into the reactor, in the case of the first layer, X is <NUM> to <NUM>; Y is <NUM> to <NUM>; and Z is <NUM> to <NUM>, in the case of the second layer, X is <NUM> to <NUM>; Y is <NUM> to <NUM>; and Z is <NUM> to <NUM>, and in the case of the third layer, X is <NUM> to <NUM>; Y is <NUM> to <NUM>; and Z is <NUM> to <NUM>. In this case, excessive temperature rise inside the catalyst bed can be effectively suppressed. Consequently, compared to the conventional catalyst system, the conversion rate of butene and selectivity for <NUM>,<NUM>-butadiene can be improved. <MAT>
wherein X is a content of zinc ferrite powder wherein A is Zn and B is Fe, Y is a content of a porous support, and Z is a content of one or more dilution fillers selected from alumina, silica, silicon carbide, and zirconia, wherein the porous support is alumina having a packing density of <NUM> to <NUM>/cm<NUM>. <MAT>
wherein, with respect to the direction in which reactants are fed into the reactor, Xn represents X for the n-th layer, and Xn-<NUM> represents X for the (n-<NUM>)th layer, wherein n is the total number of layers and is <NUM>.

As a preferred example, in the first layer, X is <NUM> to <NUM>; Y is <NUM> to <NUM>; and Z is <NUM> to <NUM>, in the second layer, X is <NUM> to <NUM>; Y is <NUM> to <NUM>; and Z is <NUM> to <NUM>, and in the third layer, X is <NUM> to <NUM>; Y is <NUM> to <NUM>; and Z is <NUM> to <NUM>. In this case, excessive temperature rise inside the catalyst bed can be effectively suppressed. When oxidative dehydrogenation is performed using the catalyst system, side reaction can be suppressed, and the conversion rate of butene, selectivity for butadiene, and yield can be improved.

In addition, according to another aspect of the present invention, in the catalyst system of the present invention, the catalyst for oxidative dehydrogenation is diluted and a reactor is filled with the catalyst so as to satisfy Equation <NUM> below. <MAT>
wherein X is an amount of AB<NUM>O<NUM> and is <NUM> to <NUM>, wherein AB<NUM>O<NUM> is an active ingredient of a catalyst, wherein A is one or more selected from the group consisting of copper (Cu), radium (Ra), barium (Ba), strontium (Sr), calcium (Ca), beryllium (Be), zinc (Zn), magnesium (Mg), manganese (Mn), cerium (Ce), zirconium (Zr), lanthanum (La), and cobalt (Co) and B is iron (Fe); Y is an amount of a porous support and is <NUM> to <NUM>; and Z is a content of one or more dilution fillers selected from alumina, silica, silicon carbide, zirconia, titania, and cordierite and is <NUM> to <NUM>, wherein the diluted catalyst is a mixture of the dilution filler and the coating catalyst, the coating catalyst having a porous support coated with the active ingredient AB<NUM>O<NUM>, and wherein the porous support has a packing density of <NUM> to <NUM>/cm<NUM>.

Hereinafter, a catalyst system for oxidative dehydrogenation according to another embodiment of the present invention, wherein the catalyst is diluted and a reactor for oxidative dehydrogenation is filled with the diluted catalyst so as to satisfy Equation <NUM>, will be described. In explaining the system, the overlapping description with the incremental dilution filling system of the above-mentioned catalyst for oxidative dehydrogenation will be omitted.

In Equation <NUM>, X is <NUM> to <NUM>, preferably, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, or <NUM> to <NUM>. Within this range, reaction efficiency can be excellent, thereby improving yield, selectivity, and conversion rate.

In Equation <NUM>, Y is <NUM> to <NUM>, preferably, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, or <NUM> to <NUM>. Within this range, catalytic activity and catalyst stability can be maintained high, and the productivity of butadiene can be increased.

In Equation <NUM>, Z is <NUM> to <NUM>, preferably, <NUM> to <NUM>, or <NUM> to <NUM>. Within this range, excessive heat generation due to oxidative dehydrogenation can be effectively suppressed, thereby improving catalyst stability and reaction efficiency.

According to the invention, the porous support has a packing density of <NUM> to <NUM>/cm<NUM> or, preferably <NUM> to <NUM>/cm<NUM>. Within this range, the mechanical strength of the coating catalyst can be excellent, and separation or peeling of AB<NUM>O<NUM> powder from the porous support can be prevented. In addition, heat generation in the catalyst bed during oxidative dehydrogenation can be effectively suppressed, and butadiene yield and selectivity for butadiene can be improved.

The catalyst system can be an oxidative-dehydrogenation catalyst system for preparation of <NUM>,<NUM>-butadiene.

In addition, the present invention provides a reactor for preparing butadiene including the catalyst system and a method of preparing <NUM>,<NUM>-butadiene using the reactor.

For example, the method of preparing <NUM>,<NUM>-butadiene according to the present invention includes i) filling a reactor with the catalyst for oxidative dehydrogenation as a fixed bed; and ii) performing oxidative dehydrogenation while continuously passing reactants containing a C4 compound including normal butene through the catalyst bed of the reactor filled with the catalyst, wherein the reactor in step i) is a fixed-bed reactor filled with the catalyst for oxidative dehydrogenation in an n-layer structure (n being an integer of <NUM> or more) in a progressive dilution manner, wherein each stage of the n-stage structure satisfies Equations <NUM> and <NUM>.

As another example, the method of preparing <NUM>,<NUM>-butadiene according to the present invention includes i) filling a reactor with the catalyst for oxidative dehydrogenation as a fixed bed; and ii) performing oxidative dehydrogenation while continuously passing reactants containing a C4 compound including normal butene through the catalyst bed of the reactor filled with the catalyst, wherein the reactor in step i) is a fixed-bed reactor, wherein the catalyst for oxidative dehydrogenation is diluted and the fixed-bed reactor is filled with the diluted catalyst so as to satisfy Equation <NUM>.

When a specific catalyst is diluted and a reactor is filled with the diluted catalyst, or a reactor is filled with a specific catalyst in a progressive dilution manner, and then oxidative dehydrogenation is performed, heat generation inside the reactor can be effectively controlled. In particular, when a fixed-bed reactor is filled with a specific catalyst for oxidative dehydrogenation in a progressive dilution manner, heat generation control effect can be maximized, allowing catalytic activity and catalyst stability to remain high over a long period of time. In addition, the conversion rate of butene, selectivity for butadiene, and yield can be greatly improved.

The C4 compound can include, for example, one or more normal butene selected from <NUM>-butene (trans-<NUM>-butene, cis-<NUM>-butene) and <NUM>-butene, and can optionally further include normal butane or C4 raffinate-<NUM>.

For example, the reactants can further include one or more selected from air, nitrogen, steam, and carbon dioxide, and preferably further includes nitrogen and steam.

As a specific example, the reactants can include a C4 compound, oxygen, steam, and nitrogen in a molar ratio of <NUM>:<NUM> to <NUM>:<NUM> to <NUM>:<NUM> to <NUM> or <NUM>:<NUM> to <NUM>:<NUM> to <NUM>:<NUM> to <NUM>. In addition, the method of preparing butadiene according to the present invention shows excellent reaction efficiency and little generation of wastewater even when steam is used in a small amount (e.g., <NUM> to <NUM> mol or <NUM> to <NUM> mol based on <NUM> mol of the C4 compound). Ultimately, the method provides the effect of reducing wastewater treatment cost and the effect of reducing energy consumed in the process.

For example, the oxidative dehydrogenation reaction can be performed at a reaction temperature of <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, <NUM> to <NUM>, or <NUM> to <NUM>. Within this range, reaction efficiency can be excellent without greatly increasing energy cost, thereby increasing the productivity of <NUM>,<NUM>-butadiene.

In addition, in oxidative dehydrogenation, the ΔT value calculated by Equation <NUM> below can be <NUM> or less, <NUM> or less, <NUM> or less, <NUM> or less, <NUM> or less, <NUM> or less, <NUM> or less, <NUM> or less, <NUM> to <NUM>, or <NUM> to <NUM>.

According to the present invention, the maximum temperature inside the catalyst bed means the part of the catalyst bed with the highest temperature during reaction.

In addition, the maximum temperature inside the catalyst bed can be measured, for example, by connecting a thermocouple (TC) to a transfer device and then performing scanning while moving the thermocouple from the top of the reactor to the bottom of the reactor at constant velocity.

For example, oxidative dehydrogenation can be performed at a gas hourly space velocity (GHSV) of <NUM> to <NUM>,<NUM>-<NUM>, <NUM> to <NUM>,<NUM>-<NUM>, or <NUM> to <NUM>,<NUM>-<NUM> based on normal butene. Within this range, reaction efficiency can be excellent, thereby improving conversion rate, selectivity, and yield.

In the present invention, the reactor is not particularly limited as long as the reactor includes the catalyst system for oxidative dehydrogenation, but can be, for example, a multi-tube reactor or a plate reactor.

However, these examples are provided for illustrative purposes only.

<NUM> of aqueous ammonia adjusted to have a pH of <NUM> was prepared. In a separate container, a metal precursor solution containing <NUM> of distilled water, <NUM> of zinc chloride (ZnCl<NUM>), and <NUM> of iron chloride (FeCl<NUM>) was prepared. The prepared metal precursor solution was added dropwise to the prepared aqueous ammonia, and at the same time, <NUM> wt% aqueous ammonia was added thereto to adjust the pH to <NUM>. To obtain a sample having a uniform composition, all of the metal precursor solution was added dropwise with stirring for <NUM> hour using an agitator, aged for <NUM> hour, and then the solution including precipitate was washed with <NUM> of distilled water and the precipitate was separated by filtration. The separated precipitate was dried for <NUM> hours, and then burned at <NUM> to obtain ZnFe<NUM>O<NUM> powder. The obtained powder was pulverized, and then powder having a size of <NUM> or less was selected using a sieving method.

ZnFe<NUM>O<NUM> powder quantified so that ZnFe<NUM>O<NUM> has a ratio of <NUM> wt% or <NUM> wt% based on <NUM> wt% in total of ZnFe<NUM>O<NUM> and alumina balls was dispersed in distilled water to prepare a catalyst slurry having a concentration of <NUM> to <NUM> wt%. Alumina balls having a packing density of <NUM> to <NUM>/cm<NUM> were added to a rotary chamber under a vacuum atmosphere. Then, the catalyst slurry was coated on the alumina balls having an average particle diameter of <NUM> by spraying the catalyst slurry while rotating the rotary chamber at about <NUM> to <NUM> rpm. When coating was performed, the rotary chamber was set to a temperature of <NUM> to <NUM>. After the coating process was completed, a coating catalyst was prepared by drying the catalyst slurry-coated alumina balls in an oven set to <NUM> to <NUM> so that distilled water was evaporated.

The coating catalyst having ZnFe<NUM>O<NUM> in an amount of 14wt% was mixed with alumina as a dilution filler as shown in Table <NUM>, and a tubular reactor was filled with the catalyst in a three-layer structure and in a gradual dilution manner. Then, the conversion rate of butene, selectivity for <NUM>,<NUM>-butadiene, <NUM>,<NUM>-butadiene yield, and selectivity for COx were measured.

The C4 compound containing trans-<NUM>-butene and cis-<NUM>-butene, oxygen, steam, and nitrogen as reactants were mixed in a molar ratio of <NUM>:<NUM>:<NUM>:<NUM>. At this time, the amount of each of the C4 compound, oxygen, and nitrogen was controlled using a mass flow controller, and the injection rate of steam was controlled using a liquid pump. The feed rate of reactants was set so that a gas hourly space velocity (GHSV) was <NUM>-<NUM> based on normal butene in the C4 compound. The reaction was performed at the reaction temperature shown in Table <NUM> below.

A reactor was filled with the catalyst composition in a gradual dilution manner in a three-layer structure as shown in Table <NUM> below. Then, reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that the reaction was performed at the temperature specified in Table <NUM> below.

The coating catalyst containing ZnFe<NUM>O<NUM> in an amount of <NUM> wt% was diluted by mixing with a dilution filler as shown in Table <NUM> and a tubular reactor was filled with the diluted catalyst. Then, reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that reaction temperature was set to <NUM>.

ZnFe<NUM>O<NUM> powder prepared in the same manner as in Preparation Examples was kneaded with distilled water and an alcohol and then extrusion-molded to obtain pellets having a diameter of <NUM> and a length of <NUM>, followed by drying at <NUM> for <NUM> hours to obtain a catalyst in the form of pellets. <NUM> volume% of the prepared catalyst was mixed with <NUM> volume% of alumina balls, and the mixture was loaded into a reactor. Then, reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that reaction temperature was set to <NUM>.

ZnFe<NUM>O<NUM> powder prepared in the same manner as in Preparation Examples was kneaded with distilled water and an alcohol and then extrusion-molded to obtain pellets having a diameter of <NUM> and a length of <NUM>, followed by drying at <NUM> for <NUM> hours to obtain a catalyst in the form of pellets. A reactor was filled with the prepared catalyst in a gradual dilution manner as shown in Table <NUM>. Then, reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that reaction temperature was set to <NUM>.

A tubular reactor was filled with the coating catalyst containing ZnFe<NUM>O<NUM> in an amount of <NUM> wt%. In this case, addition of a dilution filler was omitted. Then, reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that reaction temperature was set to <NUM>.

The products according to Examples and Comparative Examples were analyzed using gas chromatography. The conversion rate of butene, selectivity for <NUM>,<NUM>-butadiene, <NUM>,<NUM>-butadiene yield, selectivity for COx were calculated according to Equations <NUM>, <NUM>, and <NUM> below, respectively. The results are shown in Tables <NUM> and <NUM>.

In addition, when oxidative dehydrogenation was performed using the catalyst systems according to Examples and Comparative Examples, the maximum temperature inside a catalyst bed was analyzed while moving a thermocouple in a thermo-well at the center of a reactor from the inlet of the reactor to the outlet of the reactor at a constant velocity of <NUM> per second. <MAT> <MAT> <MAT>.

As shown in Table <NUM>, compared with Comparative Examples <NUM> and <NUM>, in the case of Examples <NUM> and <NUM> using the catalyst system according to the present invention, although oxidative dehydrogenation was performed at a relatively low reaction temperature, it was confirmed that the conversion rate of butene, selectivity for <NUM>,<NUM>-butadiene, and <NUM>,<NUM>-butadiene yield were excellent. In particular, when the catalyst system according to Example <NUM> was used, the efficiency and activity of oxidative dehydrogenation were excellent. In addition, considering that the difference between the maximum temperature inside a catalyst bed and the reaction temperature was small, it was confirmed that heat generated inside a reactor was effectively controlled.

On the other hand, in the case of the catalyst system according to Comparative Example <NUM>, wherein the catalyst in the form of pellets prepared using ZnFe<NUM>O<NUM> powder was diluted by mixing a dilution filler and a reactor was filled with the diluted catalyst, although reaction was performed at a relatively high reaction temperature, it was confirmed that reaction activity was significantly lower than in the cases of Examples. In addition, in the case of Comparative Example <NUM>, although the catalyst in the form of pellets prepared using ZnFe<NUM>O<NUM> powder was diluted by mixing with a dilution filler and a reactor was filled with the diluted catalyst in a gradual dilution manner, it was confirmed that reaction activity was lower than in Examples.

From the above results, it can be seen that, when the catalyst system, in which a catalyst having a porous support on which ZnFe<NUM>O<NUM> is coated in a predetermined ratio is diluted with a dilution filler and a reactor is filled with the diluted catalyst in a gradual dilution manner, is used to perform oxidative dehydrogenation, the activity of oxidative dehydrogenation is greatly improved. In addition, it can be judged that this is because heat generation inside the reactor is controlled by the novel catalyst system according to the present invention, thereby providing a reaction system with a stable temperature gradient. In addition, from the results of Examples <NUM> and <NUM>, it can be seen that, when the reactor is filled with the coating catalyst in a gradual dilution manner, dilution ratio affects reaction activity.

As shown in Table <NUM>, in the case of the catalyst systems (Examples <NUM> and <NUM>) in which the coating catalyst is homogeneously diluted with a dilution filler, compared with the systems of Comparative Examples <NUM> and <NUM> in which the same coating catalyst was used, but the coating catalyst was not diluted, it was confirmed that the conversion rate of butene, selectivity for <NUM>,<NUM>-butadiene, and <NUM>,<NUM>-butadiene yield were excellent, and selectivity for COx as a side reaction product and the maximum temperature inside a catalyst bed were significantly decreased. In addition, it was confirmed that this improvement effect was even better when a coating catalyst having a coating ratio of <NUM> wt% was used.

On the other hand, compared with Example <NUM>, in the case of Comparative Example <NUM> in which the same concentration of the coating catalyst was used as in Example <NUM>, even though reaction temperature was set to be as low as <NUM>, it was confirmed that the maximum temperature inside a catalyst bed was higher by <NUM>, and reaction activity was significantly decreased. In the case of Comparative Example <NUM>, although the maximum temperature inside a catalyst bed was the highest, it was confirmed that reaction activity was significantly decreased.

Reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that silicon carbide was used as a dilution filler.

Reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that zirconia was used as a dilution filler.

Reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that, when a coating catalyst was prepared, alumina balls having a packing density of <NUM>/cm<NUM> were used.

ZnFe<NUM>O<NUM> powder prepared in the same manner as in Preparation Examples was kneaded with distilled water and an alcohol and then extrusion-molded to obtain pellets having a diameter of <NUM> and a length of <NUM>, followed by drying at <NUM> for <NUM> hours to obtain a catalyst in the form of pellets. A reactor was filled with the prepared catalyst. In this case, addition of a dilution filler was omitted. Then, reaction was performed under the same conditions and in the same manner as in Example <NUM>, except that reaction temperature was set to <NUM>.

The products prepared according to the Additional Examples and Additional Comparative Examples were analyzed in the same manner as described above, and the results are shown in Table <NUM>.

As shown in Table <NUM>, in the case of Additional Examples <NUM> and <NUM> in which silicon carbide and zirconia were used as the dilution filler, respectively, the maximum temperature inside a catalyst bed was equal to or lower than that of Additional Comparative Examples <NUM> and <NUM>, and the conversion rate of butene, selectivity for <NUM>,<NUM>-butadiene, and <NUM>,<NUM>-butadiene yield were excellent.

In addition, when alumina having a packing density outside the range of the present invention was used as the porous support, it was confirmed that the effect of suppressing overheating of the catalyst bed was insufficient even though the catalyst was diluted and supplied to satisfy Equations <NUM> and <NUM>, and that the conversion rate of butene and butadiene yield were significantly reduced. In particular, when the packing density was less than the lower limit of the present invention (Additional Comparative Example <NUM>), it was confirmed that the conversion rate of butene and butadiene yield were significantly reduced.

In addition, when mixing of the porous support and the dilution filler was omitted, as shown in Table <NUM>, it was confirmed that the temperature inside the catalyst bed was considerably high because heat generation was not effectively controlled, and selectivity for COx as a side reaction product was considerably increased. The lifespan of the catalyst is expected to be considerably short.

<FIG> is a graph showing the temperature distribution of the catalyst bed when oxidative dehydrogenation is performed using the catalyst system according to Example <NUM>, and <FIG> is a graph showing the temperature distribution of the catalyst bed when oxidative dehydrogenation is performed using the catalyst system according to Additional Comparative Example <NUM> (conventional technology).

Referring to these results, when the catalyst system according to the present invention was used, heat generation was effectively controlled, and thus the temperature inside the catalyst bed was kept relatively stable. On the other hand, when the catalyst system of Additional Comparative Example <NUM> was used, it was confirmed that the temperature inside the catalyst bed was drastically increased at the beginning of reaction, and thereafter was drastically decreased.

Claim 1:
A catalyst system for oxidative dehydrogenation, wherein a reactor is filled with a catalyst for oxidative dehydrogenation in an n-layer structure, wherein n is an integer of <NUM> or more,
wherein the catalyst is diluted and the reactor is filled with the diluted catalyst so that each layer of the n-layer structure satisfies Equations <NUM> and <NUM> below: <MAT>
wherein X represents an amount of AB<NUM>O<NUM> and is <NUM> to <NUM>, wherein AB<NUM>O<NUM> is a active ingredient of a catalyst, wherein A is one or more selected from the group consisting of copper (Cu), radium (Ra), barium (Ba), strontium (Sr), calcium (Ca), beryllium (Be), zinc (Zn), magnesium (Mg), manganese (Mn), cerium (Ce), zirconium (Zr), lanthanum (La), and cobalt (Co) and B is iron (Fe);
Y is an amount of a porous support and is <NUM> to <NUM>; and
Z is an amount of one or more dilution fillers selected from alumina, silica, silicon carbide, zirconia, titania, and cordierite and is <NUM> to <NUM>, wherein the diluted catalyst is a mixture of the dilution filler and the coating catalyst, the coating catalyst having a porous support coated with the active ingredient AB<NUM>O<NUM>; <MAT>
wherein, with respect to a direction in which reactants are fed into the reactor, Xn represents X for an n-th layer, and Xn-<NUM> represents X for an (n-<NUM>)th layer, wherein at least one of the n layers has a Z value greater than <NUM>, and
wherein the porous support has a packing density of <NUM> to <NUM>/cm<NUM>.