JP2001009296A - Catalyst composition and production of lower isoparaffin from synthetic gas by using the same - Google Patents

Abstract

PROBLEM TO BE SOLVED: To obtain a catalyst composition with which a lower isoparaffin can be produced from a synthetic gas while keeping the activity of the catalyst high, and to provide a method for the production of a lower isoparaffin by using this catalyst. SOLUTION: By this method, a hydrogenation catalyst 14 is brought into contact with a Fischer-Tropsch(FT) synthesis catalyst 10 which synthesizes straight-chain hydrocarbons from the synthetic gas of hydrogen and carbon monoxide and with a solid acid catalyst 12 which hydrogenates, decomposes and isomerizes the straight-chain hydrocarbons. Then, hydrogen is supplied from the hydrogenation catalyst 14 to the FT synthesis catalyst 10 and to the solid acid catalyst 12 to increase the catalytic activity of the FT synthesis catalyst 10 and the solid acid catalyst 12 while suppressing deactivation.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

The present invention relates to a catalyst composition for producing lower isoparaffins from a synthesis gas of hydrogen and carbon monoxide, and a method for producing lower isoparaffins using this catalyst composition.

[0002]

2. Description of the Related Art A method for producing a lower aliphatic saturated hydrocarbon (lower paraffin) from a synthesis gas of hydrogen and carbon monoxide has been known. For example, as an example of such a manufacturing method, Cu—Zn based, Cr—Zn based, P
There is a method in which a lower aliphatic saturated hydrocarbon is generated in one pass from a synthesis gas via methanol using a catalyst obtained by physically mixing a methanol synthesis catalyst such as d-type and a methanol conversion catalyst such as zeolite. However, such a method for producing a lower aliphatic saturated hydrocarbon via methanol involves problems such as severe reaction conditions.

On the other hand, there has been proposed a method for producing lower isoparaffins under relatively mild reaction conditions without passing through methanol. In this method, higher paraffins and lower olefins are synthesized from synthesis gas using a Fischer-Tropsch synthesis catalyst (FT synthesis catalyst), and the resultant is hydrocracked and isomerized using a solid acid catalyst such as zeolite to produce lower isoparaffins. DIR
ECT SYNTHESIS OF ISOPARAF
FINS FROM SYNTHESIS GAS ",
Kaoru FUJIMOTO et al. , CHE
MISTRYLETTERS, pp. 783-786,
1985.

In this synthesis method, lower isoparaffins can be produced from synthesis gas in one pass by using a mixed catalyst of the FT synthesis catalyst and a solid acid catalyst such as zeolite. The lower isoparaffin produced in this manner has a high octane number and can be used as a high-performance transportation fuel.

[0005]

However, in the above conventional method for synthesizing lower isoparaffins, there is a problem that tar or the like adheres to the surfaces of the FT synthesis catalyst and the solid acid catalyst, and the activity of the catalyst decreases over time. was there.

The present invention has been made in view of the above-mentioned conventional problems, and has as its object to provide a catalyst composition capable of producing lower isoparaffins from synthesis gas while maintaining the activity of the catalyst at a high level, and a lower isoparaffin using the same. It is to provide a manufacturing method of.

[0007]

In order to achieve the above-mentioned object, the present invention provides a catalyst composition, which comprises a Fischer-Tropsch synthesis for synthesizing a linear hydrocarbon from a synthesis gas of hydrogen and carbon monoxide. The hydrogenation catalyst is characterized by contacting the catalyst with a solid acid catalyst for hydrocracking and isomerizing this linear hydrocarbon.

[0008] The catalyst composition is characterized in that a Fischer-Tropsch synthesis catalyst, a solid acid catalyst, and a hydrogenation catalyst are physically mixed.

Further, in the above catalyst composition, the hydrogenation catalyst is characterized in that a Fischer-Tropsch synthesis catalyst and a solid acid catalyst are bound as a binder.

[0010] In the above catalyst composition, the hydrogenation catalyst is silica or alumina supporting a noble metal.

A method for producing lower isoparaffins from a synthesis gas, comprising contacting a synthesis gas of hydrogen and carbon monoxide with the catalyst composition to synthesize a linear hydrocarbon;
Hydrocracking and isomerization of this linear hydrocarbon,
It is characterized by producing lower isoparaffin.

[0012]

Embodiments of the present invention (hereinafter referred to as embodiments) will be described below with reference to the drawings.

FIG. 1 shows an example of a catalyst composition according to the present invention. In FIG. 1, a Fischer-Tropsch synthesis catalyst (FT synthesis catalyst) 10 for synthesizing a linear hydrocarbon from a synthesis gas of hydrogen and carbon monoxide, and a linear hydrocarbon synthesized by the FT synthesis catalyst are converted into hydrogen. The solid acid catalyst 12 for hydrolytic decomposition and isomerization includes a hydrogenation catalyst 14
Are arranged to be in contact with each other. Such a catalyst composition can be obtained, for example, by physically mixing the FT synthesis catalyst 10, the solid acid catalyst 12, and the hydrogenation catalyst 14.

When a synthesis gas of hydrogen and carbon monoxide is brought into contact with the FT synthesis catalyst 10, a reaction represented by the following formula occurs, and a linear hydrocarbon is synthesized.

[0015]

Embedded image The linear hydrocarbon generated on the FT synthesis catalyst 10 in this manner moves to the adjacent solid acid catalyst 12,
It undergoes hydrocracking and isomerization where it is converted to isoparaffin as described below.

[0016]

Embedded image As described above, by converting the linear hydrocarbon generated by the FT synthesis catalyst 10 to lower isoparaffins by the solid acid catalyst 12, a high-performance transport fuel having a high octane value can be obtained. The FT synthesis catalyst 10 described above
The conditions for the synthesis of linear hydrocarbons from synthesis gas in
The reaction temperature is 200-300 ° C and the pressure is 10-20 atm. Further, isoparaffins produced after being subjected to hydrocracking and isomerization with the solid acid catalyst 12 mainly have C4 to C10 carbon atoms.

The hydrogenation catalyst 14 receives hydrogen in the synthesis gas and converts it into hydrogen atoms or hydrogen ions. These hydrogen atoms or hydrogen ions move on the surface of the hydrogenation catalyst 14 toward the FT synthesis catalyst 10 and the solid acid catalyst 12. As described above, when atomic or ionic hydrogen is received from the hydrogenation catalyst 14, the catalytic activity of the FT synthesis catalyst 10 can be improved. Also, in the solid acid catalyst 12, by receiving hydrogen,
The activity and stability of hydrocracking and isomerization can be greatly improved. Also, on the surface of the solid acid catalyst 12,
Although there was a problem that tar and the like adhered and the catalyst activity was reduced, by supplying hydrogen from the hydrogenation catalyst 14,
The adhesion of tar and the like can be prevented, and the deactivation of the solid acid catalyst 12 can be prevented.

Further, the hydrocarbons produced on the FT synthesis catalyst 10 include olefins containing unsaturated bonds, but the atomic or ionic hydrogen supplied from the hydrogenation catalyst 14 is used as described above. By hydrogenation to produce saturated paraffins. It is considered that the reason why the adhesion of tar to the surface of the solid acid catalyst 12 can be suppressed is that these olefins are hydrogenated, the polymerization thereof is suppressed, and the generation of high molecular hydrocarbons is suppressed. .

As the above-mentioned FT synthesis catalyst 10, for example, cobalt (Co), iron (Fe), ruthenium (Ru)
And the like supported on silica (SiO ₂ ) can be used. As the solid acid catalyst 12, MFI (trade name: HFI)
-ZSM-5), zeolite such as HM, HY, and H-β, or amorphous SiO ₂ —Al ₂ O ₃ can be used. As the hydrogenation catalyst 14, palladium (P
d), platinum (Pt), rhodium (Rh), ruthenium (Ru) and other noble metals supported on SiO ₂ can be used.

FIG. 2 shows a modification of the catalyst composition according to the present invention. In FIG. 2, the hydrogenation catalyst 14 is used as a binder, and the FT synthesis catalyst 10 and the solid acid catalyst 1 are used.
And 2 are combined. Even with such a configuration, as in the example shown in FIG.
The catalytic activities of the T synthesis catalyst 10 and the solid acid catalyst 12 are improved, and the deactivation of the catalyst can be suppressed. Further, according to the configuration as in this example, the bond between the FT synthesis catalyst 10 and the solid acid catalyst 12 can be strengthened, and the physical strength of the catalyst composition can be greatly increased.

Hereinafter, specific examples of the catalyst composition according to the present invention and a method for producing lower isoparaffin from synthesis gas using the same will be described as examples.

EXAMPLE In this example, a catalyst in which cobalt was supported on silica (SiO ₂ ) was used as the FT synthesis catalyst 10. The FT synthesis catalyst 10 was prepared by filling the pores of a silica gel carrier with an aqueous solution of cobalt nitrate and then evaporating and removing only the water to carry cobalt on silica. That is, after impregnating a silica gel carrier with an aqueous solution of cobalt nitrate, drying at 120 ° C. for 12 hours,
The supported cobalt metal salt was converted into an oxide by performing air calcination treatment at 0 ° C. for 2 hours. In this case, the loading amount of cobalt on the silica was 20% by weight.

As the solid acid catalyst 12, zeolite was used.

Further, as the hydrogenation catalyst 14, one obtained by supporting palladium on silica at 2.5% by weight was used.
It was prepared using silica and Pd (NH ₃ ) ₄ Cl ₂ . At this time, in order to expel chlorine, 4
A dechlorination treatment was performed at 00 ° C. for 1 hour.

As described above, three kinds of catalysts used in the catalyst composition according to the present invention were prepared. Among them, the effect of Pd / SiO ₂ (hereinafter, referred to as a supported palladium catalyst), which is a hydrogenation catalyst 14, was used. In order to investigate the above, normal heptane (n-heptane) was hydrocracked using zeolite alone or a mixed catalyst of zeolite and a supported palladium catalyst. The result is shown in FIG. In FIG. 3, the horizontal axis shows the reaction time, and the vertical axis shows the conversion of n-heptane. As can be seen from FIG. 3, when the hydrocracking reaction is carried out using zeolite alone, the activity is low even under a hydrogen atmosphere, and the activity is rapidly reduced. It is considered that this decrease in activity is mainly due to the accumulation of carbonaceous substances (such as tar) on the zeolite.

On the other hand, when a mixed catalyst of zeolite and a supported palladium catalyst was used in a hydrogen atmosphere, it was found that the conversion of n-heptane was high and the activity of the catalyst was high. . In addition, it was also found that this high activity state was maintained, and the activity deterioration, that is, deactivation was small. In this case, almost no accumulation of carbonaceous material on the zeolite was observed. This is presumably because hydrogen was transferred from the supported palladium catalyst to the zeolite, and the deposition of carbonaceous substances on the zeolite was suppressed. Also,
When the same mixed catalyst was used under a nitrogen atmosphere, the catalyst activity and deactivation state were almost the same as when zeolite was used alone under a hydrogen atmosphere, unlike under a hydrogen atmosphere. This is presumably because in a nitrogen atmosphere, even if a supported palladium catalyst is present, there is no supply of hydrogen to the zeolite, so that the accumulation of carbonaceous substances on the zeolite cannot be suppressed.

FIG. 4 shows the distribution of the carbon number of the product in the decomposition reaction of n-heptane using the various catalysts shown in FIG. FIG. 5 shows the proportions of isoparaffins, n-paraffins and olefins of C4 hydrocarbons among the decomposition products shown in FIG. As can be seen from FIGS. 4 and 5, when a mixed catalyst of zeolite and a supported palladium catalyst was used in a hydrogen atmosphere, the decomposition products were concentrated on C4 and C7, whereas the decomposition products were concentrated on C4 and C7. When the catalyst is used under a nitrogen atmosphere, the decomposition products are distributed in many types of C3 to C11 hydrocarbons. The ratio of isoparaffins in the decomposition product was 98% in the case of a mixed catalyst under a hydrogen atmosphere.
As described above, n-paraffin was 2% and olefin was not produced, whereas isoparaffin and n-paraffin were produced at almost the same ratio and olefin was contained in the other two catalysts. The difference between these effects is that when a mixed catalyst of zeolite and a supported palladium catalyst is used in a hydrogen atmosphere, hydrogen is supplied to the acid sites of the zeolite by the spillover effect, and the solid acid catalyst function is significantly promoted. It is thought to be. Therefore, such an effect makes it possible to synthesize isoparaffin from synthesis gas with high selectivity.

Next, in order to examine the effect of the combination of the supported palladium catalyst and Co / SiO ₂ as the FT synthesis catalyst 10, the mixed catalyst was used to convert hydrocarbons from the synthesis gas of hydrogen and carbon monoxide. The time change of the conversion of carbon monoxide and the yield of carbon dioxide when was synthesized was measured. The result is shown in FIG. As can be seen from FIG. 6, by introducing a supported palladium catalyst, Co /
The stability of SiO ₂ is improved, and the conversion of carbon monoxide hardly decreases with the passage of reaction time.

7 (a), 7 (b) and 7 (c) show the distribution of the carbon number of the hydrocarbon produced in this case. FIG. 7 (a) shows the values at the reaction time of 30 minutes, and FIG. 7 (b)
Shows the value at the time of 127 minutes, and FIG. 7C shows the value at the time of 405 minutes. At any time, the hydrocarbons are distributed from C1 to C13, all hydrocarbons are straight paraffins and straight olefins, and do not contain isoparaffins. Then, if these hydrocarbons are hydrocracked and isomerized with the above-mentioned zeolite, a desired lower isoparaffin can be obtained.

Therefore, a catalyst composition according to the present invention is constituted by the above-mentioned Co / SiO ₂ , supported palladium catalyst (Pd / SiO ₂ ) and zeolite, and contacted with a synthesis gas of hydrogen and carbon monoxide to lower the catalyst composition. Isoparaffin was synthesized.

First, the above three types of catalysts were used in a weight ratio of Co / SiO ₂ : zeolite: supported palladium catalyst =
After being crushed and mixed at a ratio of 4: 4: 1, 20-40 me
Reformed to sh (mesh). As described above, the hybrid catalyst obtained by mixing the three types of catalysts was reduced by flowing hydrogen at 400 ° C. for 12 hours in a reactor before use to obtain a catalyst composition according to the present invention. In this case, MFI zeolite was used as the zeolite.

The thus prepared catalyst composition according to the present invention was brought into contact with a synthesis gas, and the time-dependent change in the reaction activity of the catalyst composition and the carbon number distribution of the reaction product were measured. These results are shown in FIGS. 8 and 9A, 9B, and 9C, respectively. Further, as a comparative example, a catalyst composition using only SiO ₂ as a mere binder instead of the supported palladium catalyst was also prepared, and the time course of the reaction activity and the carbon number distribution were measured in the same manner as described above. These results are shown in FIGS. 10 and 11 (a), (b) and (c), respectively.

As shown in FIG. 8, when the catalyst composition according to the present invention was used, the conversion of carbon monoxide in the synthesis gas was maintained at a high level, and the catalyst of Co / SiO ₂ was maintained. It can be seen that the activity is stable for a long time. Further, it can be seen that the selectivity and the yield of isoparaffin in the reaction product are stable at each reaction time shown in FIGS. 9 (a), (b) and (c). In this case, by the hydrogen supplied from the supported palladium catalyst as the hydrogenation catalyst 14,
As the olefins are hydrogenated, the proportion of olefins in the reaction product is very low.

On the other hand, in the comparative example shown in FIG. 10, there is no supported palladium catalyst as the hydrogenation catalyst 14 and only SiO ₂ is used as a mere binder. The conversion is lower than in the case of FIG. 8, and the conversion further decreases over time. 11 (a), (b),
As shown in (c), the selectivity of the target isoparaffin decreases as the reaction time elapses. These are considered to be because, as described above, since no supported palladium catalyst is present, hydrogen is not supplied to Co / SiO ₂ or zeolite, and the catalytic activity decreases with time.

Although the supported palladium catalyst in the catalyst composition according to the present invention is contained in the catalyst composition in the form of Pd / SiO _{2 in} the above example, palladium is directly added to the solid acid catalyst 12.
A method of supporting the zeolite on a zeolite is also conceivable.
FIG. 12 shows the results obtained by preparing a catalyst composition according to the present invention using zeolite carrying palladium together with an FT synthesis catalyst (Co / SiO ₂ ) and measuring the change over time in the reaction activity. 13 (a), (b),
(C) shows the carbon number distribution of the reaction product when this catalyst composition is used.

As shown in FIG. 12, when the present catalyst composition is used, the conversion of carbon monoxide is slightly lower than that in the example of FIG. 8, but the activity of the catalyst decreases after the reaction time has elapsed. Also kept high. 13 (a), (b),
As shown in (c), the selectivity and yield of the target isoparaffin are maintained at a high level even after the reaction time has elapsed. Also, the proportion of olefins is kept very low.

FIG. 14 shows that the FT synthesis catalyst 10 is made of Co.
Investigation of the effect of reaction pressure on contacting synthesis gas with a catalyst composition according to the present invention using / SiO ₂ , zeolite as solid acid catalyst 12 and supported palladium catalyst as hydrogenation catalyst 14 Is shown. FIG.
In the graph, the reaction pressure is shown on the horizontal axis, and the conversion rate of CO and the selectivity of CO ₂ and CH ₄ are shown on the vertical axis. As can be seen from FIG. 14, the reaction pressure was increased from 5 atm to 2 atm.
As the pressure rose to 0 atm, the conversion of CO increased from 90% to almost 100%. At this time, CO ₂ and CH ₄
Selectivity has not changed much. Therefore, it is considered that the activity of the hybrid catalyst can be sufficiently increased if the reaction pressure is 10 atm or more.

FIG. 15 shows the effect of the synthesis gas contact time when the same catalyst composition as in FIG. 14 is used. In FIG. 15, the horizontal axis shows the contact time, and the vertical axis shows the conversion rate of CO and the selectivity of CH ₄ and CO ₂ . FIG.
As can be seen, as the contact time increases from 3 g · h / mol to 9.3 g · h / mol, the conversion of CO increases from about 50% to 80%. In this case CO ₂ ,
CH ₄ selectivity was almost constant. As can be seen from FIG. 15, a longer contact time was more advantageous.

FIG. 16 shows the effect of the reaction temperature when the same catalyst composition was used. In FIG. 16, the horizontal axis represents the reaction temperature, and the vertical axis represents the conversion rate of CO and C
The selectivities of O ₂ and CH ₄ are shown respectively. As shown in FIG. 16, the conversion rate of CO is the highest at 260 ° C. However, in this case, the selectivity of CO ₂ and CH ₄ also increased. FIG. 17 shows the distribution of hydrocarbons as reaction products when the reaction temperature is 230 ° C. and 270 ° C. FIG. 17A shows the result at 230 ° C.
(B) shows the results at 270 ° C., respectively. As can be seen from FIG. 17B, when the reaction temperature increases to 270 ° C., light hydrocarbons such as CH ₄ increase. On the other hand, at 230 ° C., the selectivity of these light hydrocarbons is not high. 16 and 17, it is considered that the reaction temperature is optimally 260 ° C.

FIG. 18 shows the effect of the composition ratio of H ₂ and CO when the same catalyst composition as described above is used. FIG.
In FIG. 8, the horizontal axis shows the composition ratio (H ₂ / CO),
The vertical axis indicates the conversion rate of CO and the selectivity of CO ₂ and CH ₄ . FIGS. 19A and 19B show the distribution of hydrocarbons as reaction products when the composition ratio is 2.5 and 3.0. As shown in FIGS. 18 and 19, when the composition ratio increases from 2 to 3, CO 2
Was nearly constant, but the selectivity for CO ₂ increased slightly. In contrast, no olefin was formed. In general, in the hydrocracking reaction, excess hydrogen is required more than stoichiometry in order to prevent the formation of olefin. Therefore, in order to suppress the formation of olefin in the FT synthesis reaction, the stoichiometric value, that is, H ₂ It is necessary to make the condition more hydrogen rich than / CO = 2.

Cobalt has been used in the FT synthesis catalyst constituting the above-described catalyst composition, but iron or ruthenium is considered to be effective. For example, in the case of iron, it is inexpensive, and the optimum reaction temperature is about 50 ° C. higher than that of cobalt. An increase in the reaction temperature is advantageous because the activity of the zeolite for hydrocracking and isomerizing hydrocarbons can be increased.

[0042]

As described above, according to the present invention,
A linear olefin or paraffin is generated from synthesis gas by a Fischer-Tropsch synthesis catalyst, and the linear hydrocarbon is transferred onto an adjacent zeolite to perform hydrocracking and isomerization. This allows efficient conversion to lower isoparaffins of about C4 to C10. In this case, since Pd / SiO ₂ is mixed with the above catalyst,
The activity of the Fischer-Tropsch synthesis catalyst and the zeolite can be increased, and their deactivation can be prevented.

[Brief description of the drawings]

FIG. 1 is a view showing an example of a catalyst composition according to the present invention.

FIG. 2 is a view showing another example of the catalyst composition according to the present invention.

FIG. 3 is a view showing a result when heptane is decomposed by a mixed catalyst obtained by mixing Pd / SiO ₂ with zeolite.

FIG. 4 is a view showing a distribution of carbon number of a decomposition product of heptane shown in FIG. 3;

5 is a view showing the ratio of isoparaffin, n-paraffin and olefin in C4 hydrocarbons among the decomposition products shown in FIG.

FIG. 6 is a diagram showing a change over time in the reaction activity of a mixed catalyst obtained by mixing FT synthesis catalyst and Pd / SiO ₂ .

FIG. 7 shows the reaction time shown in FIG.
It is a figure which shows the carbon number distribution in 7 minutes and 405 minutes.

FIG. 8 is a graph showing the change over time in the reaction activity of a hybrid catalyst obtained by mixing FT synthesis catalyst, zeolite and Pd / SiO ₂ , which is a catalyst composition according to the present invention.

FIG. 9: 33 minutes, 99% of the reaction times shown in FIG.
It is a figure which shows the carbon number distribution in 414 minutes.

FIG. 10 is a diagram showing, as a comparative example of FIG. 8, a change over time of the reaction activity of a catalyst composition using only SiO ₂ instead of Pd / SiO ₂ .

FIG. 11 shows that 30% of the reaction times shown in FIG.
It is a figure which shows the carbon number distribution in minutes, 99 minutes, and 377 minutes.

FIG. 12 shows F as a modification of the catalyst composition according to the present invention.
It is a figure which shows the time-dependent change of the reaction activity of the hybrid catalyst which mixed the T synthesis catalyst and the thing which carried the palladium on zeolite.

FIG. 13 shows 30 minutes of the reaction time shown in FIG.
It is a figure which shows the carbon number distribution at 88 minutes and 348 minutes.

FIG. 14 is a graph showing the influence of reaction pressure in a method for producing lower isoparaffin from synthesis gas using the catalyst composition according to the present invention.

FIG. 15 is a view showing the influence of contact time in a method for producing lower isoparaffin from synthesis gas using the catalyst composition according to the present invention.

FIG. 16 is a graph showing the influence of reaction temperature in a method for producing lower isoparaffin from synthesis gas using the catalyst composition according to the present invention.

FIG. 17 shows a method for producing lower isoparaffin from synthesis gas using the catalyst composition according to the present invention.
It is a figure which shows the carbon number distribution at the time of reaction temperature of 0 degreeC and 270 degreeC.

FIG. 18 is a view showing the influence of the composition ratio of H ₂ and CO in the method for producing lower isoparaffin from synthesis gas using the catalyst composition according to the present invention.

FIG. 19 is a view showing a carbon number distribution when the composition ratio of hydrogen and CO is 2.5 and 3.0 in FIG. 18;

[Explanation of symbols]

10 FT synthesis catalyst, 12 solid acid catalyst, 14 hydrogenation catalyst.

Continued on the front page (51) Int.Cl. ⁷ Identification symbol FI Theme coat II (reference) C07C 4/06 C07C 4/06 5/13 5/13 9/12 9/12 9/16 9/16 // C07B 61 / 00 300 C07B 61/00 300 F term (reference) 4G069 AA02 AA03 AA08 AA11 BA02A BA02B BA07A BA07B BA45A BB02B BB04B BC67B BC72B CC23 DA05 FB06 FB07 FB61 4H006 AA02 AC25 AC27 BA19 BA20 BA26 BA26 4H039 CA19 CJ10 CL35

Claims (5)

[Claims] 1. A Fischer-Tropsch synthesis catalyst for synthesizing a linear hydrocarbon from a synthesis gas of hydrogen and carbon monoxide, and a solid acid catalyst for hydrocracking and isomerizing the linear hydrocarbon. A catalyst composition, which is in contact with a conversion catalyst. 2. The catalyst composition according to claim 1, wherein the Fischer-Tropsch synthesis catalyst, the solid acid catalyst, and the hydrogenation catalyst are physically mixed. 3. The catalyst composition according to claim 1, wherein the hydrogenation catalyst binds the Fischer-Tropsch synthesis catalyst and the solid acid catalyst as a binder. 4. The catalyst composition according to claim 1, wherein the hydrogenation catalyst is silica or alumina supporting a noble metal. 5. The catalyst composition according to any one of claims 1 to 4, wherein a synthesis gas of hydrogen and carbon monoxide is brought into contact with the catalyst composition to produce a linear hydrocarbon, and A method for producing lower isoparaffins from synthesis gas, comprising performing hydrogenolysis and isomerization of hydrogen to produce lower isoparaffins.