NOVELTY - A butadiene (1) hydrogenation device comprises: first hydrogenation reactor (4), second hydrogenation reactor (14), gas-liquid separation tank, and recycle hydrogen compressor (20) and the recycle hydrogen compressor further comprises machine pump, heater, cooler and pipeline. The bottom section of the first hydrogenation reactor is connected to first gas-liquid separation tank (6). The bottom section of the second hydrogenation reactor is connected to second cooler (16) and second gas-liquid separation tank (17).    USE - As butadiene hydrogenation device (claimed).    ADVANTAGE - The butadiene hydrogenation device reduces olefin content in hydrogenation product; and provides low operation cost.    DETAILED DESCRIPTION - A butadiene (1) hydrogenation device comprises: first hydrogenation reactor (4), second hydrogenation reactor (14), gas-liquid separation tank, and recycle hydrogen compressor (20) and the recycle hydrogen compressor further comprises machine pump, heater, cooler and pipeline. The liquefied butadiene feed line is entered into the exhaust gas via a feed pump (2). The outlet of feed pump is connected to inlet of the first hydrogenation reactor. The bottom section of the first hydrogenation reactor is connected to first gas-liquid separation tank (6). The bottom section of the second hydrogenation reactor is connected to second cooler (16) and second gas-liquid separation tank (17). The top section of the second hydrogenation reactor is connected to second heater (12) and second hydrogenation reactor feed inlet (13). An INDEPENDENT CLAIM is included for hydrogenation method of butadiene by using hydrogenation device involving passing butadiene into first hydrogenation reactor, where the first hydrogenation reactor using hydrogenation catalyst comprises titanium oxide-alumina composite as a carrier loaded on metallic nickel, and the amount of metallic nickel is 5-35% of the total weight of catalyst and the amount of titanium oxide is 5-40 wt.% of the total weight of titanium oxide-alumina composite carrier, and the reaction condition of the first hydrogenation reactor is as follows: hydrogenation reactor temperature: 3-170 degrees C; reaction pressure: 2.2-2.9 MPa; liquid space velocity: 16 hours-1; and feed volume ratio: 5-40; passing the hydrogenation product obtained from first hydrogenation reactor to first gas-liquid separation tank, cooling it to 3-50 degrees C, and then entering it into second hydrogenation reactor, where the second hydrogenation reactor using hydrogenation catalyst comprising titanium oxide-aluminium oxide composite as carrier loaded on metallic nickel, where the amount of metallic nickel is 5-30% of the total weight of catalyst and the amount of titanium oxide is 5-40 wt.% of the total weight of titanium oxide-alumina composite carrier, and the reaction condition of the second hydrogenation reactor is as follows: hydrogenation reactor temperature: 17-230 degrees C; and reaction pressure: 2.2.8 MPa; and then entering into second gas-liquid separation tank.    DESCRIPTION OF DRAWING(S) - The figure shows flow diagram of method for hydrogenation of butadiene exhaust gas.    Butadiene (1)    Feed pump (2)    First hydrogenation reactor (4)    First gas-liquid separation tank (6)    Second heater (12)    Second hydrogenation reactor feed inlet (13)    Second hydrogenation reactor (14)    Second cooler (16)    Second gas-liquid separation tank (17)    Recycle hydrogen compressor (20)