Process for solids waste landfill gas treatment and separation of methane and carbon dioxide

A process for Landfill gas treatment and separation of methane gas and carbon dioxide gas contained therein, and for producing liquid natural gas, liquid carbon dioxide, and compressed natural gas products, the process that comprises;

• gathering a landfill gas stream from solids waste treatment landfill site with a vacuum collection system and pressurizing the collected gas stream to above atmospheric pressure;
• cleaning the landfill gas stream flowing from said gas collection system to remove condensed water vapor and trace sulfur and hydrocarbon compounds contained therein;
• conducting the cleaned landfill gas flowing from the said gas cleaning step into a four stage gas compressor;
• increasing the pressure and simultaneously cooling the landfill gas stream at each compression stage, wherein the first stage compression increases the gas pressure from approximately atmospheric pressure to approximately 70 psig, the second stage compression cylinder increases the gas pressure to approximately 240 psig, the third stage compression increases the gas pressure to approximately 630 psig and the fourth stage compression increases the gas pressure to above 1800 psig;
• intercooling the compressed landfill gas stream flowing from the first to the second compression stage, from the second to the third compression stage, and from the third to the forth compression stage to maintain a near ambient temperature to effect cooling, condensing and removing water vapor and heavy hydrocarbon vapors contained in the gas stream flowing from a lower pressure to a succeeding higher pressure stage;
• cooling the compressed landfill gas stream flowing from the fourth compression stage at above 1800 psig to approximately 20.degree. F. temperature to substantially condense most of the carbon dioxide vapor contained therein;
• separating liquid carbon dioxide from a methane rich gas stream;
• scrubbing the methane rich gas stream flowing from the fourth compression stage with a solvent fluid injected at about 50.degree. F. and approximately 1800 psig into a contactor vessel to absorb most of the carbon dioxide remaining in the gas mixture forming a CO.sub.2 -rich solvent fluid stream and a purified compressed methane gas stream;
• conducting the CO.sub.2 -rich solvent fluid flowing from the contactor vessel at approximately 1800 psig into a first flash vessel to decrease its pressure to approximately 630 psig;
• recycling a gas mixture stream released from the first flash vessel at approximately 630 psig to the suction of the forth stage compression;
• conducting the CO.sub.2 -rich solvent flowing from the first flash vessel at approximately 630 psig to a second flash vessel where its pressure is decreased to approximately 240 psig;
• recycling a second gas mixture stream released from the second flash vessel at approximately 240 psig to the suction of the third stage compression;
• conducting the CO.sub.2 -rich solvent flowing from the second flash vessel at approximately 240 psig to a third flash vessel where its pressure is decreased to approximately 70 psig;
• recycling a third gas mixture stream released from the third flash vessel at approximately 70 psig to the suction of the second stage compression;
• heating the CO.sub.2 -rich solvent fluid flowing from the third flash vessel to a relatively higher temperature;
• spraying the heated CO.sub.2 -rich solvent into a regenerator vessel operating at near atmospheric pressure to release most of the carbon dioxide remaining in the solvent fluid;
• recycling the gas mixture stream flowing from the regenerator vessel to enter the suction of the first stage compression;
• pumping a CO.sub.2 -lean solvent fluid flowing from the regenerator vessel to increase its pressure from near atmospheric pressure to above 1800 psig;
• conducting the pressurized CO.sub.2 -lean solvent fluid into a reverse heat exchanger where the CO.sub.2 -rich solvent stream flowing from the third solvent flash vessel is heated and the CO.sub.2 -lean solvent stream flowing from the regenerator vessel is cooled;
• further cooling the CO.sub.2 -lean solvent stream flowing from said reverse heat exchanger to a temperature below 50.degree. F. before entering the contactor vessel to repeat the process of scrubbing the methane rich gas stream flowing from the carbon dioxide condensing step;
• transporting and storing the purified methane gas flowing from the gas contractor vessel to a high pressure gas storage vessel;
• treating the carbon dioxide liquid stream flowing from the fourth compression stage to remove most of the dissolved hydrocarbon contaminants contained therein through the steps of expansion in a flash vessel from above 1800 psig to approximately 200 psig and by physical adsorption of gases in an activated carbon bed.
• transporting and storing the purified liquid carbon dioxide into a liquid carbon dioxide storage vessel.