The reaction was conducted in a stainless-steel autoclave (Shanghai Yanzheng Experimental Instrument Co., Ltd. China) with one well (50 mL per well), one thermocouple, and one circulating water-cooling equipment. A glass reaction tube was added to the reaction kettle, which was equipped with a 10 mm magnetic stir bar, 0.5 mmol phenylacetylene, 10 mg catalyst, and 6 ml solvent. After that, the reactor was sealed and purged with H2 three times, and then the reactor was filled with hydrogen to the set pressure value. Put the reactor into the heating mantle and set the stirring speed to 300 rpm. Preheated the reactor from room temperature to the set reaction temperature (internal temperature detected by a thermocouple) at a heating rate of 2 ºC/min. After the reaction, the reaction kettle was cooled to room temperature, and the remaining gas was discharged, and then the reaction solution was collected with a dropper and filtered. The catalyst was immobilized on the magnetic stirring bar and washed thoroughly with ethanol and water. The catalyst (together with magnetic stirring bar) was then dried at -48 ºC for 12 h in a vacuum using a freeze dryer. The reaction products were identified by GC-MS and 1 H NMR. The yields of reaction products were determined by GC with 1,3,5-trimethoxybenzene as internal standard. For the 1 H NMR analysis, 2 mL reaction solutions were concentrated by rotary evaporation and then added with 0.6 mL of CDCl3 (pre-neutralized with basic Al2O3) for analysis. As shown in the representative scanning electron microscopy (SEM) images and transmission electron microscope (TEM) images (Figure -3), the structure and morphology of the carbon material-supported Ni-based metal catalysts prepared in situ with different biomass raw materials, shaddock peel, and lignin, or lignin pretreatment methods such as washed lignin were very different. The Ni/CL and Ni/CLW catalysts, which were prepared from lignin and washed lignin respectively, had dense lamellar and rod-like structures similar to petals, respectively. In addition, the nickel particles were uniformly distributed in the carrier and wrapped by the carbon shell, so that the catalyst had good reaction activity and stability under harsh reaction conditions. However, in the Ni/CSP catalyst prepared from the shaddock peel, the nickel particles were not dispersed evenly in the carrier, but gathered together, which could reduce the stability and reactivity of the catalysts. The BET surface areas of these different catalysts were detected by N2 adsorption with an adsorption analyzer (Tristar II 3020 volumetric) (Figure ). Before N2 adsorption measurements, the samples were evacuated at 200 °C for 12 h. And the specific surface area was calculated by the BET method. The average pore diameters and pore volumes were calculated by the BJH method with the desorption branches of the isotherms. The pore structure of carbon-supported Ni-based metal catalysts prepared in situ from different biomass materials had obvious differences. We could see that they all had distinct microporous structures. These mesoporous structures might promote the transfer process of reaction raw materials, and at the same time promote the diffusion process of the products. The average pore diameter of the Ni/CSP catalyst was 13.85nm, and the pore structure was very close to the loose structure, which was consistent with the dense structure in the above-mentioned SEM analysis. The average pore volume of Ni/CSP was lower than Ni/CLW, but the average pore size of Ni/CSP was higher than Ni/CLW, indicating a partial blockage of pores in Ni/CSP. As shown in the XRD patterns of these three catalysts (Figure ), the starting materials of the biomass had a great effect on the catalysts' structure and metal dispersions. The catalyst Ni/CSP prepared from the shaddock peel gave the highintensity peaks of Ni nanoparticles at 2θ= 44.6°,52.0° and 76.6°, which indicated that the Ni nanoparticles were not well dispersed like the other two catalysts Ni/CWL and Ni/CL. For the catalysts Ni/CWL and Ni/CL prepared from lignin, we could not observe high-intensity peaks of Ni-alloy, which showed that Ni nanoparticles had very good dispersion on these two catalysts. Other than that, we could also observe a broad peak of graphitic carbon shell peak at around 20°-30°, and this phenomenon was in accordance with the above-mentioned TEM analysis. In the XRD patterns of Ni/CSP and Ni/CL catalysts, we could also observe the diffraction peak of CaCO3 species located at 29.6°. This is because shaddock peel and lignin are both renewable biomass resources in nature and contain Ca elements, when they are used to prepare the carbonsupported Ni-based catalysts in situ, the small amount of the Ca element can still be retained. However, the carbon-supported Ni-based catalyst prepared from washed lignin did not show the diffraction peak of the Ca element, which indicated that the pretreatment process of lignin had removed Ca element to a certain extent. After the synthesis of these three biomass-based nickel catalysts, we evaluated their catalytic reactivity in the selective hydrogenation of benzene acetylene. As shown in Figure , the catalysts Ni/CL, Ni/CSP, and Ni/CLW which were prepared from the different biomass raw materials, shaddock peel and lignin, or different lignin pretreatment methods had a great difference in catalytic reactivity and product selectivity in selective hydrogenation of benzene acetylene. Under the selected reaction conditions (2Mpa H2, 80 °C, 4 h) (Figure ), only the Ni/CSP and Ni/CLW two catalysts showed better catalytic reactivity. The conversion rates and products selectivity of 1a reached 78% conversion, 42% selectivity, and 97% conversion, 84% selectivity respectively. However, the Ni/CL catalyst prepared by in-situ reduction of Ni salt supported by lignin showed no reactivity, and the raw materials did not change before and after the reaction. Since the Ni/CLW catalyst showed better conversion of benzene acetylene and the desired product 1a selectivity, we further evaluated it under a variety of reaction conditions. As shown in Figure , when the reaction time was 3 h and below, the raw materials were not completely transformed, but when the reaction time was longer than 7 h, we could obtain a high amount of over-hydrogenation product. Finally, we managed to obtain good catalytic reactivity and 1a product selectivity with 92.3% conversion, 87.2% selectivity, and 97.2% conversion, 84.3% selectivity in 5 h and 4 h respectively. Then we evaluated the H2 pressure, reaction temperature and solvent for the selective hydrogenation of benzene acetylene. As shown in Figure , when the reaction pressure increased from 1 Mpa to 4Mpa, the conversion increased from 28% to 100%, and the selectivity of 1a decreased from 87% to 76%. It could be seen that the selectivity of 1a decreased with the increase of hydrogen pressure. This was because the increase of hydrogen pressure caused the intermediate product styrene obtained from the reaction to be over-hydrogenated to benzene ethane, thereby reducing the selectivity of the styrene product. Overall, when the hydrogen pressure was 2 Mpa, the Ni/CLW catalyzed selective hydrogenation of phenyl acetylene achieved better results in the conversion rate and product 1a selectivity. Then we further investigated the reaction temperature factor for the Ni/CLW catalyzed selective hydrogenation of phenyl acetylene. As shown in Figure , when the reaction temperature was increased from 60 °C to 120 °C, the reaction conversion increased to 100%, but the selectivity of 1a gradually decreased. When the reaction temperature was 120 °C, we could only observe the over-hydrogenation products benzene ethane. When the reaction temperature was 80 °C, the Ni/CLW catalyzed semi-hydrogenated phenyl acetylene reaction had a good reaction effect, and the conversion rate and 1a selectivity reached 97% and 84%, respectively. As shown in Figure7c, the solvent had a great effect on the transformation of phenyl acetylene. Among all the screening solvents, the polar and protic solvent EtOH gave the best results with 93.9 % conversion and 88.4% 1a selectivity. Although the polar solvent CH3CN and DMSO also gave the excellent selectivity of 1a, the catalyst did not show good reactivity in these two solvents with a lower 20% conversion. The other two non-polar solvents toluene and cyclohexane gave a moderate conversion of 50% and excellent selectivity of 1a with 80%. Based on the experiments and previously reported mechanism of alkyne hydrogenation, we proposed the mechanism of lignin based carbon material support Ni catalyzed hydrogenation of phenyl acetylene. As shown in Figure , the H2 and phenyl acetylene were both first adsorbed on the Ni/CLW catalyst's surface. Then, one of H2 interacted with active Ni metal species and cleavage to give the Ni-H species. At the same time, the phenyl acetylene which was absorbed on the catalyst's surface could undergo nucleophilic addition with the Ni-H species and produce the alkenyl nickel intermediate. Then following the cleavage of the Ni-C bond of the alkenyl nickel intermediate, the (Z)-alkene product would be produced together with the Ni catalyst. While at the meantime, since nickel metal species had the strong hydrogenation ability, the 1a product also had the C=C and aromatic bond with the physical electron properties, the 1a product and H2 could again absorb onto the catalyst's active metal species and generate the Ni-H species. Then it would undergo the similar catalytic nucleophilic addition of Ni-H species to the C=C double bond, which generate the alkane product finally. During the hydrogenation of phenyl acetylene, the over-reduction is normally difficult to overcome, and generally, the alkane product easily occurs in the mixture of products. Here, using the facile synthesis lignin based carbon material supported nonnoble Ni catalysts, the adsorption and over-hydrogenation of olefins were inhibited, thereby achieving the selective production of olefins with high yields.