JP2020089866A - Olefin isomerization catalyst and method for producing the same, method for producing 2-butene and propylene production method using the same - Google Patents

Abstract

To obtain an olefin isomerization catalyst that has a high conversion rate, has high durability in repeated cycles of isomerization reaction-regeneration, and is available inexpensively.SOLUTION: An olefin isomerization catalyst has at least one alkali metal supported on a support that is made up of magnesium oxide with a purity of 56 wt.% or more and less than 99 wt.%.SELECTED DRAWING: Figure 1

Description

The present invention relates to an olefin isomerization catalyst, particularly a catalyst for isomerizing 1-butene to 2-butene, a method for producing the same, a method for producing 2-butene using the catalyst, and a method for obtaining propylene.

Attention has been focused on an olefin isomerization catalyst, particularly a catalyst for isomerizing 1-butene contained in natural gas and the like in a large amount into 2-butene. The reason is to increase the added value by isomerizing 1-butene, which has few uses, into 2-butene, which has many uses and usage amounts. The use of 2-butene is, for example, the use of obtaining propylene by bringing 2-butene and ethylene gas into contact with an olefin metathesis catalyst (Patent Document 1).

The following performances are required as an isomerization catalyst from 1-butene to 2-butene.
(1) High isomerization efficiency (conversion rate) and being maintained for a long time (degradation rate is low),
(2) It is possible to use the isomerization catalyst repeatedly a plurality of times by once again reacting and regenerating the deteriorated catalyst.
(3) The catalyst can be manufactured using inexpensive raw materials that are easily available. (4) The catalyst manufacturing process is a simple process without any dangerous process.

Particularly in recent years, there has been a strong demand for a catalyst that can be supplied at a low cost and that can be used repeatedly as a used catalyst so as to cope with mass production and cost reduction of polyolefin resins.

As a catalyst for isomerizing 1-butene to 2-butene, a catalyst containing a metal oxide as a main component has been used. As such a catalyst, there are two kinds of catalysts (patent document 2) in which an alkali metal such as potassium is supported on a metal oxide carrier such as alumina (patent document 2) and a catalyst using a magnesium oxide carrier (patent document 3). Form is known.

Patent Document 2 shows a high conversion rate close to an equilibrium composition by a catalyst supporting 25% by weight or more of an alkali metal with respect to 100 parts by weight of a γ-alumina carrier having a large surface area. In order to obtain this catalyst, γ-alumina with high purity and large surface area is pretreated with nitric acid and a large amount of alkali metal is used to support 25% or more of alkali. There is a problem that is prone to accidents. Further, it is said that a catalyst using an alumina carrier is likely to be deteriorated by coking. For these reasons, there are an increasing number of examples in which magnesium oxide is used as a carrier having catalytic activity instead of the γ-alumina carrier.

As an example of using magnesium oxide, a high-purity magnesium oxide catalyst having a sulfur content of 74 ppm or less and an iron content of 330 ppm or less is shown in Patent Document 3 (paragraph [0024]). However, the general-grade magnesium oxide produced by the electrolytic method, which is a typical magnesium oxide production method, contains several thousands ppm of sulfur, which is a catalyst poison in Patent Document 3, in terms of sulfur atoms. Therefore, it is necessary to purify the sulfur content to a high purity of 74 ppm or less, which is a major obstacle to obtaining an inexpensive isomerization catalyst.

On the other hand, Patent Document 4 discloses an isomerization catalyst that uses general-grade magnesium oxide containing high-concentration sulfur instead of high-purity magnesium oxide. In this document, a used catalyst is regenerated by using ultra-high purity nitrogen gas having an oxygen gas concentration of 1 ppm or less, and a conversion rate of 79.9%, which is almost equal to the equilibrium conversion rate, is obtained. (Patent Document 4, paragraph [0037], Table 2). Although high activity after regeneration was obtained by this method, the deterioration rate was 0.108%/hour, which is higher than that of high-purity magnesium oxide. This deterioration rate indicates that the conversion rate of 79.9% decreases to around 50% after the reaction for 300 hours (12.5 days), which is not practical because frequent catalyst replacement is required. Also, ultra-high purity nitrogen gas is required, which is not preferable in terms of cost.

As described above, an olefin isomerization catalyst using general-grade magnesium oxide, which has a high reaction activity and a low deterioration rate during repeated reactions after catalyst regeneration, in other words, an olefin isomer with good durability. The reality is that chemical catalysts have not been realized yet.

Japanese Patent No. 595965 Japanese Patent Publication No. 60-6333 Patent No. 4390556 Japanese Patent Publication No. 2005-506172

The first object of the present invention is to have a high isomerization efficiency and to maintain a small deterioration rate even if the isomerization reaction and regeneration (reactivation) are repeated twice or three times or more. To provide a good catalyst.

A second object of the present invention is to produce an inexpensive, highly active and highly durable catalyst using a general-grade magnesium oxide raw material containing a large amount of impurities such as sulfur, and to provide it to an olefin isomerization reaction. is there.

Other objects of the present invention will be apparent from the following description.

In view of the above situation, the inventors of the present invention have earnestly studied to solve the drawbacks of the prior art, and have obtained the following knowledge as a guideline for solving the problems of the present invention.
(1) First, the contents of Patent Documents 3 and 4 which are prior arts were analyzed. Since sulfur in the magnesium oxide catalyst acts as a catalyst poison, it is necessary to use high-purity magnesium oxide having a sulfur content of 74 ppm in order to obtain a catalyst with a low deterioration rate (Patent Document 3).
(2) On the other hand, when general-grade magnesium oxide having a sulfur content of 2300 ppm or more in the catalyst is used, the deterioration rate is improved by controlling the oxygen concentration in the regenerating nitrogen gas to 1 ppm or less. However, it is still 0.108%/hour (Patent Document 4, Table 2), which is much larger than 0.027%/hour (Patent Document 3, Table 3) in the case of high-purity magnesium oxide, which is large in practical use. It becomes an obstacle.
(3) The inventors of the present invention have developed a catalyst having isomerization-regeneration repetition durability equal to or higher than that of a high-purity magnesium oxide catalyst while using low-grade general-grade magnesium oxide having a high sulfur content as a raw material. We examined it as a target.
(4) First, in order to obtain a guideline for achieving a high conversion rate using general-grade magnesium oxide, high-purity magnesium oxide was supported on general-grade magnesium oxide to reduce the exposure of sulfur components. The conversion rate was improved and the deterioration rate was also reduced. From this, the result which supports the result of patent document 3 that the impurity in magnesium oxide, especially sulfur among them had reduced activity was obtained.
(5) Since the above-mentioned sulfur component exists mainly as SO ₃ which is acidic in magnesium oxide, it was expected that neutralizing the acidic would reduce the action as a catalyst poison. In order to support it, the alkali metal was supported on the surface of a general grade magnesium oxide and the effect was examined, and it was confirmed that the conversion efficiency was remarkably improved.
(6) Further, when the used alkali-supported catalyst was regenerated in (5) above, its deterioration rate hardly increased during the second use, and conversely, the deterioration rate decreased during the third use, The result was that the durability was improved.
(7) A similar test was conducted with a high-purity magnesium oxide catalyst, and comparison with a general grade product was performed. The deterioration efficiency of the first reaction of general grade products is slightly inferior to that of high-purity magnesium oxide, but the deterioration rate is lower than that of high-purity magnesium oxide when used twice or three times. High).
(8) In order to know the mechanism of the above phenomenon, when analyzed by thermal desorption-mass spectrometry of oxygen gas, by loading an alkali metal on general-grade magnesium oxide, the amount of oxygen adsorbed increases, and with it It was possible to obtain the result that the deterioration rate decreased sharply. From this, it was suggested that the oxygen gas adsorption was increased by supporting the alkali metal to prevent the coking during the isomerization reaction.
(9) Further, when the appearance of the catalyst after the completion of the isomerization reaction was observed, it was found that the catalyst of the present invention having a large sulfur content had a higher breaking strength than the catalyst of high-purity magnesia oxide. It was understood that this high breaking strength of the general grade product becomes a strong resistance to high temperature stress of about 400° C. during the isomerization reaction, which is one of the reasons for improving the durability of the catalyst.
(10) From the analysis results of the above (8) and (9), it is assumed that the deterioration rate of the catalyst after regeneration contributes to both suppression of coking due to adsorbed oxygen and improvement of fracture strength of the catalyst.
(11) From the above, a catalyst having an activity and durability equal to or higher than that of high-purity magnesium oxide was obtained by carrying a specific amount of an alkali metal on magnesium oxide containing high-concentration sulfur, and the present invention was reached.

That is, the present invention relates to the following:
1. An olefin isomerization catalyst in which at least one alkali metal is supported on a magnesium oxide carrier having a magnesium oxide purity of 56% by weight or more and less than 99% by weight.
2. The olefin isomerization catalyst according to 1 above, wherein the magnesium oxide carrier contains 500 ppm or more of a sulfur compound in terms of sulfur atom weight.
3. The olefin isomerization catalyst according to 1 above, wherein the magnesium oxide carrier contains 2000 ppm or more of a sulfur compound in terms of sulfur atom weight.
4. The olefin isomerization catalyst according to 1 above, wherein the magnesium oxide carrier contains 4000 ppm or more of a sulfur compound in terms of weight of sulfur atom.
5. The olefin isomerization catalyst according to any one of 1 to 4 above, wherein the at least one alkali metal is selected from the group consisting of potassium and sodium.
6. The olefin isomerization catalyst according to any one of 1 to 5 above, wherein 0.2 to 5 parts by weight of metal of at least one alkali metal is supported on the surface of the carrier based on 100 parts by weight of the magnesium oxide support. ..
7. The olefin isomerization catalyst according to any one of 1 to 5 above, wherein 0.5 to 3 parts by weight of metal, based on 100 parts by weight of the magnesium oxide support, is supported on the surface of at least one alkali metal. ..
8. Olefin isomerization according to any one of 1 to 5 above, in which 0.7 to 2.5 parts by weight of at least one alkali metal in terms of metal is supported on the surface of the carrier based on 100 parts by weight of the magnesium oxide support. Chemical catalyst.
9. The amount of oxygen adsorbed by the TPD-MASS measurement method is 0.5 to 20 μmol/g, more preferably 0.6 to 15 μmol/g, further preferably 0.7 to 10 μmol/g, and particularly preferably 0.8 to 4 μmol/g. The olefin isomerization catalyst according to any one of 1 to 8 above, which is g.
10. The olefin isomerization catalyst according to any one of 1 to 9 above, which is a pelletized, granular, cylindrical, cylindrical, or columnar molded body.
11. The olefin isomerization catalyst according to any one of 1 to 10 above, wherein the olefin isomerization is an isomerization reaction from 1-butene to 2-butene.
12. The olefin isomerization catalyst according to any one of 1 to 11 above, which has a breaking strength of at least 25N.
13. a) a step of molding magnesium oxide having a magnesium oxide purity of 56% by weight or more and less than 99% by weight to obtain a carrier,
b) spray-coating the carrier obtained in step a) with at least one alkali metal; and c) calcining the alkali-metal-supported carrier obtained in step b).
13. The method for producing an olefin isomerization catalyst according to any one of 1 to 12 above, which comprises:
14. 14. The method for producing an olefin isomerization catalyst according to the above 13, wherein the magnesium oxide is magnesium oxide produced by electrolysis using seawater as a raw material.
15. A method for producing 2-butene, which comprises contacting 1-butene with the olefin isomerization catalyst according to any one of 1 to 12 above.
16. After using the catalyst according to any one of the above 1 to 12 for the isomerization reaction of 1-butene to 2-butene, the used catalyst is regenerated and the isomerization of 1-butene to 2-butene is performed again. 16. The method for producing 2-butene as described in 15 above, which is used in the oxidization reaction.
17. 17. The method for producing 2-butene according to the above 16, wherein the isomerization reaction and the regeneration treatment are alternately performed twice or more.
18. For the regeneration of the catalyst, the catalyst is heated to 200° C. or higher, more preferably 350° C. or higher in a nitrogen gas containing 10 ppm or more, preferably 1,000 ppm or more, more preferably 10,000 ppm or more of oxygen in terms of volume. The method for producing 2-butene according to the above 16 or 17, which comprises:
19. i) a step of passing 1-butene to obtain 2-butene in a reaction tank filled with the catalyst according to any one of the above 1 to 12, and ii) the obtained 2-butene with ethylene gas A step of passing olefin metathesis catalyst in the latter stage together to obtain propylene,
A method for producing propylene, comprising:

According to the present invention, the olefin isomerization reaction, in particular, the conversion rate of the isomerization reaction from 1-butene to 2-butene is very high, and even if it is regenerated a plurality of times, its deterioration rate is very small and highly durable. A catalyst can be provided. Further, inexpensive magnesium oxide having a sulfur content of several thousand ppm or more can be used as a carrier raw material, and a catalyst having high breaking strength can be provided. The use of inexpensive raw materials and the ability to be used multiple times or more facilitates the production of 2-butene, which has extremely high productivity as compared with conventional magnesium oxide catalysts. By connecting 2-butene obtained by the method together with ethylene to a metathesis catalyst in the subsequent stage, propylene can be produced with high efficiency.

FIG. 1 shows an outline of a method for evaluating catalytic activity by a flow reactor (evaluation of catalytic activity by a flow reactor). FIG. 2 shows the type of alkali metal on a general-grade magnesium oxide carrier, the relationship between the amount of the alkali metal supported and the isomerization conversion rate (the type of alkali metal, the relationship between the amount supported and the isomerization activity). FIG. 3a shows the relationship between the oxygen adsorption amount and the conversion rate (FIG. 3a: relationship between the catalytic oxygen adsorption amount and the conversion rate). FIG. 3b shows the relationship between the oxygen adsorption amount and the deterioration rate (FIG. 3b: Relationship between the catalytic oxygen adsorption amount and the deterioration rate). The change of the catalyst deterioration rate with respect to the number of isomerization reactions is shown (change of the catalyst deterioration rate with respect to the number of catalyst reactions).

That is, the present invention is a catalyst that can be suitably used for an olefin isomerization reaction, and has a purity of 56% by weight or more and less than 99% by weight, preferably a sulfur compound such as SO ₃ is 500 ppm or more in terms of sulfur atom weight, Preferably 1000 ppm or more, more preferably 2000 ppm or more, further preferably 2500 ppm or more, even more preferably 3000 ppm, particularly preferably 4000 ppm or more, for example, a carrier made from magnesium oxide containing 4500 ppm or more or 5000 ppm or more, alkali metal, Preferably, the catalyst carries 0.2 to 5% by weight of alkali metal in terms of metal with respect to 100% by weight of the carrier. The upper limit of the sulfur compound content is not particularly limited as long as it is a range that can be generally contained in commercially available magnesium oxide, but can be, for example, 5400 ppm or less.

The above magnesium oxide is not particularly limited as long as its purity is 56% by weight or more and less than 99% by weight. Magnesium oxide is generally classified into a raw material refined by a thermal reduction method of dolomite ore or an electrolytic method from seawater. Although magnesium oxide of any method can be used in the present invention, the electrolytic method is advantageous in that there are few restrictions on the raw material procurement, is the mainstream of current world production, and has a large cost advantage. On the other hand, magnesium oxide obtained by the electrolysis method has a high concentration of impurities such as sulfur. Therefore, even if the sulfur concentration is, for example, 500 ppm or more, or 2000 ppm, or 4000 ppm or more, it is very preferable from the economical point of view that it can be used as an olefin isomerization catalyst material.

In the present invention, magnesium oxide obtained by an electrolysis method is preferably used, and more preferably magnesium oxide produced by an electrolysis method using seawater as a raw material is used.

As the magnesium oxide used as the catalyst carrier of the present invention, it is possible to use a high-purity product of 99% by weight or more, but from the economical viewpoint, the one having a purity of less than 99% by weight is used. .. The purity of magnesium oxide is 56% by weight or more, preferably 70% by weight or more, more preferably 80% by weight or more, even more preferably 90% by weight or more, and particularly preferably 95% by weight or more. Preferably, as the magnesium oxide, a general grade product of 95% by weight or more and less than 99% by weight, more preferably 96% by weight to 98% by weight is used. It is particularly preferred to use 96% or more of magnesium oxide in order to avoid unforeseen causes of product defects due to impurities. In addition to sulfur S, Ca, Si, Fe, Al, etc. are mentioned as an impurity element contained in magnesium oxide.

As general grade products of magnesium oxide, products sold by various manufacturers can be used in the present invention. For example, Tateho Chemical Industry Co., Ltd. product name TATEHOMAG, Kyowa Chemical Industry Co., Ltd. product name KYOWAMAG, Kamijima Chemical Industry Co., Ltd. product name Star Mag, etc. can be appropriately selected and used from products sold as general grade products. .. The components in these products and their composition ratios differ depending on the raw materials and conditions such as purification in the manufacturing process, but when the sulfur component is 300 ppm or less in terms of sulfur atom, it is often called a high-purity product. It will be the price. Generally, the price decreases as the residual sulfur content increases, and standard grade products often contain 2000 ppm or more of sulfur. The magnesium oxide raw material of the present invention has a sulfur content of, for example, 500 ppm or more, preferably 1000 ppm or more, more preferably 2000 ppm or more, and further preferably, in terms of sulfur atom weight, in order to reduce the price and the deterioration rate after regeneration. Can be used by selecting from general grades containing sulfur of 2500 ppm or more, more preferably 3000 ppm, particularly preferably 4000 ppm or more, for example 4500 ppm or more or 5000 ppm or more.

The sulfur content can be measured, for example, by a fluorescent X-ray analysis method or a combustion method. Preferably, it is measured by a fluorescent X-ray analysis method.

General grade magnesium oxide is usually supplied as a powder. The magnesium oxide is preferably molded into various shapes such as a columnar shape, a disk shape, and a cylindrical shape in order to increase the frequency of contact between the raw material olefin fluid and the catalyst in the reactor and reduce the pressure loss. Generally, a cylindrical pellet having a diameter of 1 to 6 mm and a length (height) of about 2 to 20 mm is preferably used. However, the present invention is not limited to this, and it can be used as various irregularly shaped pellets, tablet shapes, granules (granular) and crushed granules, and in some cases, it can be used as a fine particle catalyst by spray drying production. You can also In the present invention, the magnesium oxide may have an activity as an olefin isomerization catalyst, but typically, it is formed as described above to support another substance (for example, an alkali metal). Can also be responsible. Therefore, in the present specification, the magnesium oxide (preferably the shaped magnesium oxide) is also referred to as “magnesium oxide carrier”. This phrase does not mean that the magnesium oxide support according to the invention may not have catalytic activity by itself.

The magnesium oxide carrier of the present invention can be manufactured by a method in which a dispersion medium such as water is added, mixed and kneaded, molded, and then baked. When the dispersion medium is added to the powder, it is desirable that the mixture be dividedly added so that the mixture does not become non-uniform. The dispersion medium can be used to impart a cohesive force for maintaining a constant shape in the molding and firing steps. Water is preferably used as the dispersion medium, and if necessary, an organic solvent such as alcohol and other additives may be used.

The raw material kneaded with the dispersion medium can then be molded. Molding can be carried out using, for example, a tableting machine, a disk pelleter or a plunger extruder. The shaped body can then be fired. The calcination can be performed, for example, at a temperature of 500 to 1000°C, preferably 600 to 900°C, more preferably 700 to 800°C. The firing time is, for example, 30 minutes to 10 hours, preferably 1 to 5 hours, more preferably 2 to 4 hours.

At least one kind of alkali metal is supported on the formed magnesium oxide. The type of the alkali metal to be carried is not particularly limited, but sodium and/or potassium are particularly preferred. The amount of the alkali metal supported on the magnesium oxide carrier is preferably 0.2 to 5 parts by weight, and more preferably 0.5 to 3 parts by weight in terms of alkali metal, based on 100 parts by weight of the magnesium oxide carrier. %, more preferably 0.7 to 2.5 parts by weight, and particularly preferably 0.9 to 2 parts by weight. In the present invention, it has been found that a significantly higher isomerization conversion can be achieved when the amount of alkali metal is within these ranges.

The amount of the alkali metal, such as sodium or potassium, can be measured by a method known to those skilled in the art, for example, an atomic absorption photometry (AAS method) or a fluorescent X-ray analysis (XRF analysis). When the atomic absorption spectrophotometry (AAS method) is used, for example, a predetermined amount of the prepared catalyst is dissolved in an acid, the insoluble matter is filtered off, and then a predetermined amount of water is added to dilute the solution with an alkali metal. Minutes can be analyzed (for example, the amount of sample used for measurement can be 1 g, and the dilution factor can be 5000 times). In the case of the XRF method, for example, a predetermined amount of catalyst is crushed and molded into a disk, and then semi-quantitative analysis can be performed (for example, the sample amount is 4 g, and the disk size is 3 cm). The atomic absorption spectrophotometric method (AAS method) is preferable because of its high quantitativeness.

Although commercially available magnesium oxide, particularly general grade magnesium oxide, may already contain alkali metals such as sodium at a level of several hundred ppm, the amount of the alkali metal in the present invention is It is intended to specify the amount (addition amount) of the alkali metal added to the magnesium oxide carrier, independently of such potential impurities.

For example, the production of the catalyst of the present invention is carried out by treating, drying and/or calcining a magnesium oxide support molded into pellets, cylinders, cylinders or other shapes with an aqueous solution containing an alkali metal compound. As the alkali metal compound, there can be used alkali metal formate, acetate, carbonate, nitrate, hydrochloride, sulfate and other metal salts, alkali metal chlorides and other halogen compounds, alkali metal hydroxides and the like. .. As a method of treating the aqueous solution, a magnesium oxide carrier is dipped in an aqueous solution of an alkali metal compound for a predetermined time, then taken out, and then dried and/or baked. /A known method such as a spraying method of firing can be preferably used. In one preferred embodiment of the present invention, an aqueous solution of an alkali metal compound is spray-coated on a magnesium oxide carrier by a spray method, followed by drying and/or baking.

Magnesium oxide treated with an aqueous solution of an alkali metal salt can be calcined in air, in vacuum, or in an inert gas, but a method of heating and calcining in an oven in an air atmosphere is simple and preferable. The calcination can be carried out, for example, at a temperature of 250 to 700° C., preferably 300 to 600° C., more preferably 400 to 500° C., and particularly preferably 420 to 480° C. The firing time can be used if it is about 2 minutes depending on the temperature, but it is preferably 10 minutes or longer, more preferably 30 minutes or longer and 3 hours or shorter. The catalyst thus obtained can have, for example, pellet, granular, columnar, cylindrical or columnar morphology.

The catalyst prepared by the above method may then be subjected to a reaction pretreatment. The pretreatment is performed for the purpose of removing water and other components on the surface by heating the catalyst to improve the reaction activity. It is particularly preferable to carry out immediately before the olefin isomerization reaction, but it can also be carried out at any time after the catalyst production and before the isomerization reaction. For the purposes of the present invention, an inert gas having a low oxygen concentration, for example, a nitrogen gas having an oxygen concentration of 0.1 to 30 ppm, preferably 0.2 to 20 ppm, such as 0.3 ppm to 10 ppm, is used at 450 to 700°C. The heating can be performed at a temperature of preferably 480 to 600° C., more preferably 500 to 570° C. for 30 minutes to 15 hours, preferably 1 to 8 hours, more preferably 2 to 6 hours. Alternatively, it is desirable to perform heat treatment until the dew point of the outlet gas reaches −50° C. or lower, preferably −80° C. As an apparatus for heating, an ordinary apparatus such as a fixed bed or a fluidized bed can be used, and it is particularly preferable to use an apparatus used for an isomerization reaction.

In the present invention, the catalyst produced as described above, that is, a catalyst containing a magnesium oxide carrier having a purity of 56 wt% or more and less than 99 wt% and at least one alkali metal (for example, the magnesium oxide carrier and the alkali metal). Can be used for the olefin isomerization reaction. In the above catalyst, the at least one alkali metal may be supported on the magnesium oxide carrier, preferably on the surface of the magnesium oxide carrier.

In one embodiment of the present invention, the present invention provides a magnesium oxide having a purity of magnesium oxide of 56% by weight or more and less than 99% by weight, preferably a raw material of magnesium oxide containing 500 ppm or more of sulfur, and the impregnation method. The present invention relates to a method for producing the above catalyst, which includes a step of carrying an alkali metal and then calcining.

In another embodiment of the present invention, the present invention is
a) a step of molding magnesium oxide having a magnesium oxide purity of 56% by weight or more and less than 99% by weight, preferably 500 ppm or more in terms of sulfur atom weight, to obtain a carrier,
b) spray-coating the carrier obtained in step a) with at least one alkali metal; and c) calcining the alkali-metal-supported carrier obtained in step b).
And a method for producing the above catalyst.

In yet another embodiment of the present invention, the invention comprises
a) a step of molding magnesium oxide having a magnesium oxide purity of 56% by weight or more and less than 99% by weight, preferably 500 ppm or more in terms of sulfur atom weight, to obtain a carrier,
b) spray-coating the carrier obtained in step a) with at least one alkali metal; and c) calcining the alkali-metal-supported carrier obtained in step b).
And an olefin isomerization catalyst obtained by a method comprising

Here, the magnesium oxide may be magnesium oxide produced by electrolysis using seawater as a raw material.

Further, in another embodiment of the present invention, the present invention is preferably 0.5 to 20 μmol/g, more preferably 0.6 to 15 μmol/g, further preferably 0.7 to 10 μmol/g, and particularly preferably It relates to the above olefin isomerization catalyst having an oxygen adsorption amount of 0.8 to 4 μmol/g, for example 0.8 to 3 μmol/g. The oxygen adsorption amount can be measured by the TPD-MASS measurement method (thermal desorption-mass spectrometry) as described in the Example section. In the present invention, it was found that when the oxygen adsorption amount is within the above range, particularly when it is 0.8 to 4 μmol/g, a remarkably high isomerization conversion rate and minimization of deterioration rate can be simultaneously achieved. It was

In a further embodiment of the invention, the invention relates to an olefin isomerization catalyst having a puncture strength of at least 25N, preferably 30N-100N, more preferably 40N-80N, such as 40N-60N. The breaking strength can be measured, for example, by a load test as described in Examples.

The catalyst prepared as described above, preferably the catalyst subjected to activation pretreatment, can then be used in the olefin isomerization reaction. As the olefin to be subjected to the isomerization reaction using the catalyst of the present invention, for example, gaseous lower hydrocarbon gas such as propene, butene, and petene, for example, gaseous lower olefin gas is preferable, and 1-butene is particularly preferable. It is preferable because of its versatility. Therefore, in one preferred embodiment of the present invention, the olefin isomerization reaction is a 1-butene to 2-butene isomerization reaction. The type of reactor for the olefin isomerization reaction is not particularly limited, but among them, fixed bed reactors and fluidized bed reactors are preferable, and fixed bed reactors are particularly preferable.

The reaction can be started by supplying the raw material gas to the catalyst that has been charged into the reactor and subjected to the necessary pretreatment. Here, the isomerization reaction of 1-butene using a fixed bed reactor will be described below as an example. 1-butene gas is contacted with the catalyst charged in the apparatus at a rate of 1 to 50 WHSV (space velocity of the reaction gas with respect to the amount of the catalyst), preferably 3 to 30 WHSV, more preferably 5 to 20 WHSV, and reacted. it can. The reaction temperature is preferably 200 to 400°C, more preferably 220 to 350°C, and particularly preferably 250 to 320°C. The oxygen concentration in the gas at this time is preferably 30 ppm or less, more preferably 20 ppm or less, and particularly preferably 15 ppm or less.

By providing an analyzer (for example, a gas chromatograph) on the outlet side of the reactor, the components after the reaction can be continuously monitored. Usually, when the decrease in the conversion of 1-butene and the decrease in the amount of 2-butene produced exceed a predetermined value, the supply of the raw material gas is stopped and the reaction is stopped. The catalyst may be reactivated (regenerated) if necessary, and the isomerization reaction may be restarted when the recovery of the activity is confirmed. The regeneration treatment of this catalyst is carried out, for example, by bringing a high temperature inert gas (nitrogen gas) containing oxygen of 10 ppm or more, preferably 1000 ppm or more, more preferably 10000 ppm or more in terms of volume into contact with the deteriorated catalyst, It is performed by oxidizing and removing carbon and the like deposited on the surface. The upper limit of the oxygen content can be, for example, 10% or less, preferably 6% or less. The heating temperature is, for example, 350 to 550°C, preferably 400 to 500°C, more preferably 430 to 470°C. The treatment time is, for example, 10 minutes to 7 hours, preferably 20 minutes to 5 hours, and more preferably 30 minutes to 4 hours. In the present invention, it is possible to achieve sufficient regeneration of the catalyst of the present invention and maintain a low degradation rate even when the regeneration treatment is performed using an inert gas having the above oxygen concentration. Was found.

When the regeneration treatment is carried out, the isomerization reaction can be started by passing 1-butene, which is a raw material gas, through the regeneration-treated catalyst again under the conditions before the regeneration or the reaction conditions close thereto. .. For example, if the conversion rate at the time of restart is measured and it is confirmed that it is within the predetermined range, the reaction is continued, and conversely, if the conversion rate at the time of restart is smaller than the predetermined range, the regeneration process is performed. Repeatedly, when the predetermined activity value is confirmed, the isomerization reaction is restarted. Such regeneration treatment can be repeated 2 times or 3 times or more, and therefore, the isomerization reaction and the regeneration treatment can be alternately repeated 2 times or 3 times or more (for example, 2 to 5 times). .. If the recovery of the activity is small even after the regeneration treatment, it is desirable to stop the reaction and replace the catalyst.

Since the catalyst of the present invention has a high reaction conversion rate, a small deterioration rate after regeneration treatment, and excellent durability, the catalyst replacement frequency is low and high productivity is realized.

In one embodiment of the present invention, the present invention relates to a method for producing 2-butene, which comprises contacting 1-butene with the above olefin isomerization catalyst. In a further embodiment of the invention, the invention relates to the process for the preparation of 2-butene as described above, wherein 1-butene is contacted with the catalyst at a rate of 1-50 WHSV and/or at a temperature of 200-400°C.

In a further embodiment of the present invention, the present invention provides that the above olefin isomerization catalyst is used for the isomerization reaction of 1-butene to 2-butene, and then the used catalyst is regenerated, and 1-butene to 2-butene is used again. The present invention relates to a method for producing 2-butene used in an isomerization reaction to Here, the isomerization reaction and the regeneration treatment can be alternately performed twice or more. Further, the catalyst is regenerated by heating the catalyst to 200° C. or higher, more preferably 350° C. or higher in a nitrogen gas containing 10 ppm or more, preferably 1,000 ppm or more, more preferably 10,000 ppm or more of oxygen in terms of volume. Can be included.

Also, in another embodiment of the present invention, the present invention relates to the above catalyst for isomerization reaction of 1-butene, preferably for producing 2-butene from 1-butene. Furthermore, in a further embodiment of the present invention, the present invention relates to the use of the above catalyst for the isomerization reaction of 1-butene, preferably for producing 2-butene from 1-butene. The production may be carried out as described above, for example comprising contacting 1-butene with the olefin isomerization catalyst, preferably 1-butene with the catalyst at a rate of 1 to 50 WHSV and/or Contacting at a temperature of 200 to 400° C. is included.

Further, the olefin isomerization catalyst of the present invention can be suitably used in the step of producing propylene using ethylene and 2-butene obtained by the present catalyst as a raw material by combining with the olefin metathesis catalyst. By connecting the catalyst device of the present invention to the preceding stage of the olefin metathesis catalyst and flowing the raw material gas, it becomes possible to continuously produce propylene from 1-butene. The fact that the olefin isomerization catalyst of the present invention has higher activity and higher durability as compared with the prior art enables high productivity as a total system. When the activity after regeneration is low, it is necessary to stop the entire plant and replace the catalyst, but the catalyst of the present invention is, as shown in Examples described later, a catalyst using high-purity magnesium oxide, Durability after regeneration is equal or better. As a result, it is possible to make continuous operation at a low cost for a long time, thereby making it possible to greatly contribute to the improvement in the economical efficiency of propylene production. Therefore, in one embodiment of the present invention, the present invention relates to a method for producing propylene, comprising the steps of:
i) a step of passing 1-butene to obtain 2-butene in a reaction tank filled with the catalyst according to any one of claims 1 to 12, and ii) the obtained 2-butene with ethylene gas Together with the step of passing olefin metathesis catalyst directly or indirectly connected to the latter stage of the above catalyst to obtain propylene.

Hereinafter, the present invention will be described with reference to examples, but the present invention is not limited to these examples.

The composition is shown in Table 1, and general grade magnesium oxide containing 1.3% by weight (5200 ppm) of SO ₃ in terms of sulfur atom (Kamijima Chemical Industry Co., Ltd., product name Starmag G-2 (general grade)) is used. Example catalyst sample was prepared by using HP-30A (high purity grade) having a sulfur content of 0.004% to prepare Comparative Example 2 catalyst.

以下の実施例、比較例で使用する転化率、劣化速度の定義と測定方法を以下に示す。また触媒の表面特性評価、破壊強度測定等は、以下の方法によった。
（１）転化率、評価、測定方法
作成した触媒は前処理として、７０ｇの触媒を直径４ｃｍのＳＵＳ−３１６製流通反応器に充填され、５５０℃窒素気流下で４時間前処理を行い、次いで反応温度３００℃まで冷却した。所定の温度に調整されたところで、原料ガス（１−ブテン）を流速１７０ｍｌ／ｍｉｎ、３００℃温度の条件で触媒に流通させ、出口側のガス成分をガスクロマトグラフィーにより分析することにより、連続的に生成する２−ブテンの量を測定することにより、反応温度（３００℃）に到達後の時間ｔにおける１ブテン（１−Ｃ_４Ｈ_８）転化率Ｃｔを（１）式で定義した。

The definitions and measurement methods of the conversion rate and deterioration rate used in the following examples and comparative examples are shown below. The surface characteristics of the catalyst and the breaking strength were measured by the following methods.
(1) Conversion, evaluation, and measurement method As a pretreatment, the prepared catalyst was charged with 70 g of a catalyst in a SUS-316 flow reactor having a diameter of 4 cm, pretreated for 4 hours under a nitrogen stream at 550°C, and then, The reaction temperature was cooled to 300°C. After being adjusted to a predetermined temperature, the raw material gas (1-butene) was allowed to flow through the catalyst under the conditions of a flow rate of 170 ml/min and a temperature of 300° C., and the gas component on the outlet side was analyzed by gas chromatography to continuously obtain By measuring the amount of 2-butene formed in 1, the butene (1-C ₄ H ₈ ) conversion Ct at time t after reaching the reaction temperature (300° C.) was defined by the equation (1).

Ct=[(N ₀ −N _t )/N ₀ ]×100(%) (1)
N ₀ ; 1-butene mole number before reaction N _t ; (unreacted) 1-butene mole number at time t

Below, the conversion rate after 12 hours was described as C ₁₂ , and the conversion rate after 24 hours was described as C ₂₄ .

The principle of the flow reactor used in this example is shown in FIG. The raw material gas (1-butene) always flows in at the same concentration from one end of the catalyst packed bed, undergoes an isomerization reaction, and flows out from the other end. The outflowing gas is collected by a fixed amount gas chromatographic analysis while changing the time, the 1-butene concentration is measured, and the 1-butene addition rate Ct is calculated from the equation (1). Since the flow rate is constant, the number of moles of 1-butene gas N _{0 that} has flowed into the catalyst is constant, and it is isomerized by Nt moles during the time τ when it passes through the catalyst layer (N ₀ −N _t ). The conversion rate Ct is understood as a scale showing how much isomerization is performed during the catalyst layer passage time τ, that is, an index showing the catalytic activity, and its time change represents the change over time of the catalyst activity or the deterioration rate. It will be an index.
(2) Catalyst deterioration rate Dv
The change per hour in the 1-butene conversion rate at arbitrary times t1 and t2 after reaching the predetermined temperature was used as an index of the durability of the catalyst as (2).

Degradation rate _{Dv = (C t1- C t2)} / (t2-t1) (2)

In this example, the conversion rate at t ₁ =12 and t ₂ =24 was used, and the value calculated by the equation (3) was used as the catalyst deterioration rate.

Degradation rate _{D V = (C 12 -C 24} ) / 12 ···· (3)

As described above, since the conversion rates C ₁₂ and C ₂₄ by the flow reaction method are the conversion amounts within the flow passage time τ after 12 hours and 24 hours, respectively, the difference C ₁₂ -C ₂₄ is the difference within the time τ. It is an index representing the change in the conversion amount at 1, that is, the change in the catalyst activity. That is, the expression (3) serves as an index representing a decrease in catalyst activity during 12 to 14 hours, that is, a catalyst deterioration rate.
(3) Evaluation of catalyst activity after catalyst retreatment After the first isomerization reaction (Run #1) of the catalyst, the catalyst was heated at a high temperature for regeneration (reactivation) treatment. Using the catalyst after the regeneration treatment, the (1) and in the same way was circulated 1- Butengasu to perform the isomerization reaction, the conversion rate after 12 hours C _12, after 24 hours the conversion C _24, degradation The speed Dv was calculated.
(4) O ₂ adsorption amount The oxygen adsorption capacity of the catalyst was investigated by combining a thermal desorption system model BELCAT manufactured by Microtrac Bell Co., Ltd. and a mass spectrometer. After pretreating the catalyst sample at 550° C. for 5 hours, while heating at 50° C., nitrogen gas containing 0.4 volume% of oxygen was irradiated in a pulsed manner, and the amount of oxygen gas desorbed from the nitrogen gas was measured. The peak of m/z=32 (m; ion mass, z: ionic charge number) was measured by the analysis method to examine the oxygen adsorption amount.
(5) Measurement of Fracture Strength of Catalyst Crush strength was measured with a MAX automatic load tester manufactured by Nippon Keizai System Co., Ltd. The strength of the catalyst when it was collapsed by pushing it in with a piston was defined as the crush strength.

20 ml of water was added to 1 kg of a general-grade magnesium oxide raw material having the composition shown in Table 1, stirred in a vinyl bag, and then molded into a 3.2 mm cylindrical shape using a Kikusui tableting machine. Then, it was heated to 750° C. in an air atmosphere and calcined for 3 hours to obtain a columnar carrier having a diameter of 3.2 mm and a height of 3.2 mm. Next, a 1.3% aqueous solution of potassium nitrate was prepared and spray-coated on the carrier so as to be 0.5% by weight based on 100 parts of the carrier in terms of potassium metal by a spray method using a glass sprayer. A catalyst sample A was prepared by firing at 450°C.

Next, as a pretreatment of the catalyst, 70 g of the catalyst was charged into a SUS-316 reactor having a diameter of 4 cm and pretreated for 4 hours under a nitrogen stream at 550°C. Then, the reaction temperature was cooled to 300°C. After being adjusted to a predetermined temperature, the raw material gas (1-butene) was passed through the catalyst under the conditions of a flow rate of 170 ml/min and a temperature of 300° C., and the gas components on the outlet side were analyzed by gas chromatography to show the conversion rate and deterioration. The speed was calculated. The results are shown in Table 2.

A catalyst B was prepared in the same manner as in Example 1 except that potassium was loaded so that the amount of potassium metal was 1% by weight based on 100 parts of the carrier. This catalyst B was pretreated in the same manner as in Example 1, then 1-butene gas was subjected to an isomerization reaction, and the conversion C ₂₄ was measured. The results are shown in Table 2.

A catalyst C was prepared in the same manner as in Example 1 except that potassium was loaded so that the amount of potassium metal was 1.5% by weight based on 100 parts of the carrier. This catalyst C was pretreated in the same manner as in Example 1, and then an isomerization reaction of 1-butene gas was performed to measure the conversion C ₂₄ . The results are shown in Table 2.

A catalyst D was prepared in the same manner as in Example 1 except that potassium was loaded so that the amount of potassium metal was 3% by weight based on 100 parts of the carrier. This catalyst D was pretreated in the same manner as in Example 1, then 1-butene gas was subjected to an isomerization reaction, and the conversion rate was measured. The results are shown in Table 2.

A catalyst E was prepared in the same manner as in Example 1 except that potassium was supported so that the amount of potassium metal was 5% by weight based on 100 parts of the carrier. This catalyst E was pretreated in the same manner as in Example 1, and then an isomerization reaction of 1-butene gas was performed, and a conversion measurement C ₂₄ was performed. The results are shown in Table 2.

A catalyst F having a sodium supported amount of 1% was prepared in the same manner as in Example 2 except that sodium (Na) was used as the alkali metal instead of potassium (K). This catalyst F was pretreated in the same manner as in Example 1, and then an isomerization reaction of 1-butene gas was performed to measure the conversion C ₂₄ . The results are shown in Table 2.

A catalyst G having a supported lithium amount of 1% was prepared in the same manner as in Example 2 except that lithium (Li) was used as the alkali metal instead of potassium (K). This catalyst G was pretreated in the same manner as in Example 1, and then an isomerization reaction of 1-butene gas was performed to measure the conversion C ₂₄ . The results are shown in Table 2.
[Comparative Example 1]

After preparing a carrier under the same conditions by using the same raw material as in Example 1, the same treatment was carried out without applying an alkali metal to prepare a catalyst H. This catalyst H was pretreated in the same manner as in Example 1, then subjected to an isomerization reaction of 1-butene gas, and a conversion measurement C ₂₄ was performed. The results are shown in Table 2.
[Comparative example 2]

Catalyst J having a potassium supported amount of 1% by weight was prepared in the same manner as in Example 2 by using the high-purity magnesium shown in Table 1 instead of the general grade magnesium oxide raw material. This catalyst J was pretreated in the same manner as in Example 1, then an isomerization reaction of 1-butene gas was performed, and the conversion C ₂₄ after 24 hours was measured. The results are shown in Table 2.

表２において、アルカリ金属担持量に対して１−ブテンの２４時間後の転化率Ｃ_２４をプロットすると図２になる。このグラフから、アルカリ金属担持量が０．２〜５重量％で活性が高くなり、０．５〜３重量％で好ましい転化率が得られるようになり、更に０．７〜２．５重量％で平衡転化率に近い高い転化率が得られることがわかる。

In Table 2, the conversion C ₂₄ of 1-butene after 24 hours is plotted against the amount of supported alkali metal, and the result is shown in FIG. 2. From this graph, the activity becomes high when the amount of the alkali metal supported is 0.2 to 5% by weight, and the preferable conversion rate is obtained when the amount is 0.5 to 3% by weight, and further 0.7 to 2.5% by weight is obtained. It can be seen that a high conversion rate close to the equilibrium conversion rate can be obtained.

In order to analyze by what mechanism the results in Table 2 and FIG. 2 occur, several catalysts were selected and the oxygen gas adsorption amount was measured by TPD-MASS (thermal desorption-mass spectrometry). It was The results are shown in Table 3. The relationship between the oxygen gas adsorption amount and the conversion rate is shown in FIG. 3a, and the relationship between the oxygen gas adsorption amount and the deterioration rate is shown in FIG. 3b. From this, it is understood that the oxygen adsorption amount increases with the increase of the amount of the alkali supported, and the conversion rate also improves accordingly. When the oxygen adsorption amount is 0.5 to 20 μmol/g, the conversion rate is about 40%, and when the oxygen adsorption amount is 0.6 to 15 μmol/g, and further 0.7 to 10 μmol/g, the conversion rate is further improved. Particularly, when the oxygen adsorption amount is around 0.8 to 4 μmol/g, the conversion rate becomes maximum and the deterioration rate becomes minimum. When the amount of oxygen adsorbed increases to 20 μmol/g or more, the conversion rate decreases and the deterioration rate increases. From these results, it was considered that the oxygen adsorbed on the surface oxidizes carbon generated by the isomerization reaction and delays the progress of coking, which is one of the major reasons for suppressing the deterioration and improving the conversion rate.

69 ml of the used Example catalyst B after the first isomerization reaction (Run #1) in Example 2 was filled in a glass container and regenerated. The regeneration treatment was carried out by a method in which the treatments from the first stage to the third stage shown in Table 4 were continuously performed for a total of 7 hours and then naturally cooled.

比較例２で最初の反応（Ｒｕｎ＃１）させた触媒Ｊについても表４と同じ条件で再生処理を行った。これらの再生処理済の触媒Ｂ、触媒ＪをＲｕｎ＃１と同じ条件で２回目の異性化反応（Ｒｕｎ ＃２）を行った。更に続けて２度目の再処理を表４と同じ条件で行い、Ｒｕｎ＃１，Ｒｕｎ＃２と同じ条件で、再生後の触媒Ｂ，Ｊを用いて３回目の異性化反応（Ｒｕｎ＃３）を行わせた．Ｒｕｎ＃１〜Ｒｕｎ＃３における触媒Ｂ，Ｊによる異性化転化率、劣化速度を調べ、表５に示した。

The catalyst J, which was subjected to the first reaction (Run #1) in Comparative Example 2, was also regenerated under the same conditions as in Table 4. A second isomerization reaction (Run #2) was performed on these regenerated catalysts B and J under the same conditions as Run #1. Then, the second re-treatment is performed under the same conditions as in Table 4, and the third isomerization reaction (Run #3) is performed using the regenerated catalysts B and J under the same conditions as Run #1 and Run #2. Was done. The isomerization conversion rates and deterioration rates of catalysts B and J in Run #1 to Run #3 were examined and shown in Table 5.

表５について、反応回数と劣化速度との関係を図４に示す。これから、標準グレードの酸化マグネシウム担体を用いた触媒は、高純度酸化マグネシウムを用いた触媒に比べ１回目の劣化速度はやや大きいものの、再生繰り返し後の劣化速度は小さくなり、その耐久性が著しく良好であることが見て取れる。酸素濃度の高い一般グレードの窒素ガスを使用した再生処理により、高純度酸化マグネシウムと同等、もしくはそれ以上の優れた耐久性が確認された。

Regarding Table 5, the relationship between the number of reactions and the deterioration rate is shown in FIG. From this, it can be seen that the catalyst using the standard-grade magnesium oxide carrier has a slightly higher deterioration rate at the first time than the catalyst using high-purity magnesium oxide, but the deterioration rate after repeated regeneration is small, and its durability is extremely good. It can be seen that By the regeneration treatment using general-grade nitrogen gas with high oxygen concentration, excellent durability equal to or higher than that of high-purity magnesium oxide was confirmed.

In order to investigate the reason for the improvement in durability during the repeated reaction-regeneration shown in Example 9, catalyst B (general grade magnesium oxide carrier 1% potassium supported) and catalyst J (high-purity magnesium oxide carrier) before the isomerization reaction were used. The fracture strength of 1% potassium supported) was measured, and the results are shown in Table 5. Further, when the appearance of the catalyst after repeating the reaction three times was observed, the surface of the catalyst J was partially collapsed, while the catalyst B was slightly decomposed. The catalyst B has a high fracture strength of the carrier and therefore can withstand stress such as high temperature during the isomerization reaction, while the catalyst J was partially worn due to high temperature stress. It is considered that one of the causes of the decrease in the catalyst activity is that the wear causes the deterioration of the surface due to the peeling of the alkali metal on the surface.

As described above, the results of Example 8 (FIG. 4) and Example 9 are considered as follows.
1) A catalyst using magnesium oxide having a large sulfur content as a carrier raw material has a low olefin isomerization conversion rate because the sulfur acts as a catalyst poison.
2) On the other hand, when an alkali metal such as potassium is supported on magnesium oxide using a general grade having a large sulfur content, the conversion rate is increased and the deterioration rate is improved to the same level as that of high-purity magnesium oxide. It is estimated that this effect is mainly due to the increase in oxygen adsorption amount due to the addition of alkali.
3) After the first isomerization reaction, when regenerating treatment with nitrogen gas having a high oxygen concentration and repeating isomerization, high-purity magnesium oxide shows a deterioration increasing phenomenon, whereas general grade magnesium oxide repeats three times. Until then, almost no increase in the deterioration rate was observed, and good durability results were shown.
4) From the above, when general grade magnesium oxide having a large sulfur content is used as a carrier material and an appropriate amount of alkali is supported, the oxygen adsorption amount is increased and coking during isomerization is suppressed, It has been understood that the two effects of increasing the crush strength of the catalyst using the general-purpose magnesium oxide carrier and contributing to preventing the deterioration of the catalyst.

Claims (19)

An olefin isomerization catalyst in which at least one alkali metal is supported on a magnesium oxide carrier having a magnesium oxide purity of 56% by weight or more and less than 99% by weight. The olefin isomerization catalyst according to claim 1, wherein the magnesium oxide carrier contains 500 ppm or more of a sulfur compound in terms of sulfur atom weight. The olefin isomerization catalyst according to claim 1, wherein the magnesium oxide carrier contains 2000 ppm or more of a sulfur compound in terms of sulfur atom weight. The olefin isomerization catalyst according to claim 1, wherein the magnesium oxide support contains 4000 ppm or more of a sulfur compound in terms of sulfur atom weight. The olefin isomerization catalyst according to any one of claims 1 to 4, wherein the at least one alkali metal is selected from the group consisting of potassium and sodium. Olefin isomerization according to any one of claims 1 to 5, wherein 0.2 to 5 parts by weight of metal, based on 100 parts by weight of the magnesium oxide support, of at least one alkali metal is supported on the surface of the support. catalyst. Olefin isomerization according to any one of claims 1 to 5, wherein 0.5 to 3 parts by weight of metal, based on 100 parts by weight of the magnesium oxide support, is supported on the surface of at least one alkali metal. catalyst. The olefin according to any one of claims 1 to 5, wherein 0.7 to 2.5 parts by weight of at least one alkali metal in terms of metal is supported on the surface of the support based on 100 parts by weight of the magnesium oxide support. Isomerization catalyst. The amount of oxygen adsorbed by the TPD-MASS measurement method is 0.5 to 20 μmol/g, more preferably 0.6 to 15 μmol/g, further preferably 0.7 to 10 μmol/g, and particularly preferably 0.8 to 4 μmol/g. The olefin isomerization catalyst according to any one of claims 1 to 8, which is g. The olefin isomerization catalyst according to any one of claims 1 to 9, which is a pelletized, granular, columnar, cylindrical, or columnar molded body. The olefin isomerization catalyst according to any one of claims 1 to 10, wherein the olefin isomerization is an isomerization reaction from 1-butene to 2-butene. The olefin isomerization catalyst according to any one of claims 1 to 11, which has a breaking strength of at least 25N. a) a step of molding magnesium oxide having a magnesium oxide purity of 56% by weight or more and less than 99% by weight to obtain a carrier,
b) spray-coating the carrier obtained in step a) with at least one alkali metal; and c) calcining the alkali-metal-supported carrier obtained in step b).
The method for producing an olefin isomerization catalyst according to claim 1, which comprises: The method for producing an olefin isomerization catalyst according to claim 13, wherein the magnesium oxide is magnesium oxide produced by an electrolysis method using seawater as a raw material. A method for producing 2-butene, which comprises contacting 1-butene with the olefin isomerization catalyst according to claim 1. After using the catalyst according to any one of claims 1 to 12 for the isomerization reaction of 1-butene to 2-butene, the used catalyst is regenerated to convert 1-butene to 2-butene again. The method for producing 2-butene according to claim 15, which is used in an isomerization reaction. The method for producing 2-butene according to claim 16, wherein the isomerization reaction and the regeneration treatment are alternately performed twice or more. For the regeneration of the catalyst, the catalyst is heated to 200° C. or higher, more preferably 350° C. or higher in a nitrogen gas containing oxygen of 10 ppm or more, preferably 1,000 ppm or more, more preferably 10,000 ppm or more in terms of volume. The method for producing 2-butene according to claim 16 or 17, which comprises: i) a step of passing 1-butene to obtain 2-butene in a reaction tank filled with the catalyst according to any one of claims 1 to 12, and ii) the obtained 2-butene with ethylene gas A step of passing olefin metathesis catalyst in the latter stage together with to obtain propylene,
A method for producing propylene, comprising:

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