NOVELTY - Producing liquefied natural gas (LNG) and hydrogen comprises using a compressor to carry out first-grade compression for a coke oven gas, sending the raw material gas after deoiling and naphthalene-removal into a desulfurization adsorption tower, performing first-grade hydro-conversion and second-grade hydro conversion, sending the raw material gas after desulfurization to a hydramine-method deacidification device, removing the water to dew point, and sending the rich hydrogen from a liquefying and separating device to a pressure-transformation and adsorption hydrogen-extraction device.    USE - The method is useful for producing LNG and hydrogen from coke oven gas (claimed).    ADVANTAGE - The method is capable of producing the LNG and hydrogen with high purity in a simple and energy-efficient manner.    DETAILED DESCRIPTION - Producing liquefied natural gas (LNG) and hydrogen from coke oven gas comprises: (a) using a compressor to carry out first-grade compression for the coke oven gas from an external area and sending it to a rough deoiling and naphthalene-removal machine to carry out primary deoiling and naphthalene-removal, using another compressor to continuously increase a pressure and sending it to a fine deoiling and naphthalene-removal machine to carry out further deoiling and naphthalene-removal, where the deoiling and naphthalene-removal are realized by taking active carbon as adsorbent, and the steam is used for carrying out regeneration when a rough deoiling and naphthalene-removal absorbent absorbs in a saturated condition; (b) sending the raw material gas after deoiling and naphthalene-removal into a desulfurization adsorption tower, and taking the active carbon as adsorbent to adsorb and remove sulfur; (c) sending the raw material gas to a first-grade hydro-conversion machine, performing first-grade hydro-conversion in presence of iron-molybdenum (FeMo) hydro-conversion catalyst so that majority of the organic sulfur is transformed into inorganic sulfur, then sending it into a desulfurization tank filled by zinc powder or medium-temperature iron manganese (FeMn) desulfurizer to absorb and remove the inorganic sulfur by the zinc oxide or the medium-temperature FeMn desulfurizer, then optionally entering a second-grade hydro-conversion machine to perform the hydro-conversion in presence of FeMo hydro-conversion catalyst, further transforming a residual organic sulfur, then sending it into the desulfurization tank filled by zinc powder or medium-temperature FeMn desulfurizer to absorb the hydrogen sulfide, reducing a volume percentage of the sulfur-containing compound in the raw material gas to less than 4 parts per million (ppm), where more than 99 vol.% of organic sulfur in the raw material gas is removed by the first-grade hydrogen desulfurization, and the second grade hydrogen desulfurization is saved if the volume percentage of the sulfur-containing compound in the raw material gas is less than a target value that is less than 4 ppm after the first-grade hydrogen desulfurization; (d) sending the raw material gas after desulfurization to a hydramine-method deacidification device so that the content of carbon dioxide in the raw material gas is reduced to less than 50 ppm; (e) sending the raw material gas after desulfurization to an adsorption and dehydration device, and removing the water to dew point of less than or equal to 76 degrees C at normal pressure; (f) sending the raw material gas after dehydration and drying to a deep cold liquefying and separating device to pass through a mixing refrigeration liquefying and low-temperature separation technique to obtain the liquefied natural gas that is rich in carbon monoxide and nitrogen and rich hydrogen; and (g) sending the rich hydrogen from the deep cold liquefying and separating device to a pressure-transformation and adsorption hydrogen-extraction device to obtain a product of hydrogen using an adsorption effect of the adsorbent. An INDEPENDENT CLAIM is included for a technique device for production of LNG and hydrogen from coke oven gas, including: a raw material gas compression and normal-temperature deoiling and naphthalene-removal device comprising a first-grade compressor and a rough deoiling and naphthalene-removal machine, a second-grade compressor or a second-grade or third-grade compressor, and a fine deoiling and naphthalene removal machine; a fine desulfurization device; a hydro-conversion and fine desulfurization device comprising a first-grade hydro-conversion machine filled with FeMo hydro-conversion catalyst, a desulfurization tank serially filling the zinc oxide or medium-temperature FeMn desulfurizer, a second-grade hydro conversion machine filled with nickel molybdenum hydro-conversion catalyst and a desulfurization tank serially filling the zinc oxide; a hydramine method deacidification device; an adsorption and dehydration device; a purification gas deep cold liquefying and separation device including a mixed refrigeration liquefying device and a low-temperature fine fraction separation device; and a pressure-transformation adsorption hydrogen-extraction device.