Lower olefins refer to ethylene, propylene and butylene, which are vital building block in the chemical industry. They are fundamental chemicals of the greatest consumption among the organic chemicals all over the world. Large amount of chemical products, such as packing materials, cosmetics, synthetic rubber, coatings are the derivatives of lower olefins. In traditional petrochemical industry, lower olefins are mainly derived from oil-based feedstocks. With the rapid depletion of the limited petroleum, there is an urgent need for processes that can produce lower olefins from alternative feedstocks. The syngas, which is a promising alternative feedstock as it can be obtained from reforming of natural gas, gasification of coal or biomass, can be transformed into lower olefins through indirect or direct reaction. The indirect process mainly refers to the methanol to olefins (MTO) technology [1]. The direct conversion of syngas to lower olefins is one of the most challenging subjects in the field of C1 chemistry. It is considered as an attractive alternative non-petroleum-based production route due to its process simplicity and low energy consumption [2]. Bifunctional catalysis used composite catalysts, such as OX-ZEO and Fischer-Tropsch to olefins (FTO) reaction are twomain routes for the direct conversion of syngas to lower olefins [3]. Recent work by Bao et al. [4] and Wang et al. [5] reported that oxides-molecular sieve coupling catalysts exhibited very high selectivity toward lower olefins at relative high temperature of ca. 400°C, but this method is not yet in commercial use. As the reaction process for FTO is very similar to that for typical FT synthesis, FT catalysts can be used for production of lower olefins after suitable catalyst modification. De Jong et al. [6] reported that Fe-based catalysts promoted by S andNa and using α-alumina or carbon nanofiber as weakly interactive supports exhibited excellent performance for selective formation of lower olefins (61 C%). They also found the particle size of iron carbide plays a crucial role for direct production of lower olefins via syngas, and they suggested lower olefins are produced at promoted terrace sites [7]. However, these reactions normally need temperatures from 300°C to 350°C, which would cause carbon deposition on the catalyst surface and catalyst sintering, deactivating the catalyst and shortening its lifetime [2]. The primary aims of FTO are to maximize lower olefins selectivity while reduce methane production with high stability. The maximum selectivity toward C2−C4 olefins is achieved with an alpha value of about 0.5 according to the ordinary Anderson–Schulz–Flory (ASF) model [8,9]. One of the most efficient ways of shifting product selectivity to low alpha values is by increasing reaction temperature. However, a decrease on the chain growth probability results in an increase of methane selectivity as indicated by the ASF product distribution. In addition, the produced olefins were prone to be further hydrogenated to paraffins especially at high temperature and resulted in decreased selectivity to lower olefins. Moreover, the particle sintering and coke formation at high temperature would lead to serious deactivation [10]. Due to the above limitation, there was no catalyst suitable for the industrial application of the direct conversion of syngas into lower olefins via the Fischer-Tropsch synthesis. Based on the general analysis, most of the reported FTO catalysts are still a kind of FT catalyst with low alpha value. The product distribution still obeys the ordinary ASF model. Obviously, with the goal of high selectivity to lower olefin, lowmethane selectivity and high stability simultaneously, it is necessary to develop new FTO catalyst which deviates from ASF distribution at mild reaction conditions.