Process for maximizing production of xylenes from heavy reformate without purge

A method for producing mixed xylenes from a heavy reformate feed, the method comprising the steps of:

• introducing the heavy reformate feed and a hydrogen feed to a dealkylation reactor, wherein the dealkylation reactor comprises a dealkylation catalyst, wherein the heavy reformate feed comprises aromatic hydrocarbons with nine or more carbon atoms (C9+ aromatics), wherein the hydrogen feed comprises hydrogen gas;
• reacting the heavy reformate feed with the hydrogen feed in the presence of the dealkylation catalyst in the dealkylation reactor to produce a dealkylation effluent, wherein the dealkylation reactor is at a dealkylation temperature, wherein the dealkylation reactor is at a dealkylation pressure, wherein the dealkylation reactor has a liquid hourly space velocity;
• introducing the dealkylation effluent to a splitter unit, where the dealkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics;
• separating the dealkylation effluent into a light gas stream, a toluene stream, a benzene stream, a C9 aromatics stream, a C10+ aromatics stream, and a mixed xylene stream in the splitter unit, wherein the light gas stream comprises light hydrocarbons and hydrogen, wherein the toluene stream comprises toluene, wherein the benzene stream comprises benzene, wherein the mixed xylene stream comprises mixed xylenes, wherein the C9 stream comprises C9 aromatics, wherein the C10+ aromatics stream comprises C10+ aromatics;
• introducing the toluene stream, the C9 aromatics stream, and a hydrogen stream into a transalkylation reactor, wherein the transalkylation reactor comprises a transalkylation catalyst, wherein the hydrogen stream comprises hydrogen gas;
• reacting the toluene stream, the C9 aromatics stream, and the hydrogen stream in the presence of the transalkylation catalyst in the transalkylation reactor to produce a transalkylation effluent, wherein the transalkylation reactor is at a transalkylation temperature, wherein the transalkylation reactor is at a transalkylation pressure, wherein the transalkylation reactor has a liquid hourly space velocity;
• introducing the transalkylation effluent to the splitter unit, wherein the transalkylation effluent comprises light gases, toluene, benzene, mixed xylenes, and C9+ aromatics;
• separating the transalkylation effluent in the splitter unit such that mixed xylenes in the transalkylation effluent exit the splitter unit as part of the mixed xylene stream;
• introducing the C10+ aromatics stream to a hydrocracking reactor;
• introducing a hydrogen gas stream to the hydrocracking reactor;
• reacting the C10+ aromatics stream and the hydrogen gas stream in the presence of a selective hydrocracking catalyst to produce a treated aromatics stream, wherein the hydrocracking reactor is at a hydrocracking temperature, wherein the hydrocracking reactor is at a hydrocracking pressure, wherein the hydrocracking reactor has a liquid space velocity, wherein the treated aromatics stream comprises single ring aromatic compounds;
• and
• recycling the treated aromatics stream to the dealkylation reactor.