A method of recovering an unreacted phenol from a bisphenol A production facility comprising: reacting an initial phenol and an initial acetone in the presence of a catalyst to produce a bisphenol A stream comprising the unreacted phenol of the initial phenol and a bisphenol A, separating a purge stream comprising the unreacted phenol, and wherein the unreacted phenol is present in the purge stream in an amount of 60 to 90 wt%, based on the total weight of the purge stream; adding the purge stream to a phenol purification section of a phenol production facility; and purifying the purge stream in the phenol purification section to form a purified phenol outlet stream in the phenol purification section, wherein the purified phenol outlet stream comprises a total phenol concentration of greater than or equal to 99.5 wt% based on the total weight of the purified phenol outlet stream; wherein the forming the purified phenol outlet stream comprises: heating a preheater inlet stream comprising cumene, a product phenol from the phenol production facility, and a product acetone from the phenol production facility in a preheater to form a splitter inlet stream; separating the splitter inlet stream into a splitter top outlet stream comprising the product acetone and the cumene and a splitter bottom outlet stream comprising the product phenol in a splitter column; separating the splitter bottom outlet stream into a crude top outlet stream comprising the product phenol and a crude bottom outlet stream comprising the cumene in a crude phenol column; hydro-extracting the crude top outlet stream in a hydro-extractor column to form an extractor primary outlet stream comprising the product phenol; and recovering the purified phenol outlet stream, from the extractor primary outlet stream in a finishing column; wherein the adding the purge stream comprises adding the purge stream to one or more of the preheater inlet stream, the splitter inlet stream; the splitter bottom outlet stream; and the crude top outlet stream. reacting an initial phenol and an initial acetone in the presence of a catalyst to produce a bisphenol A stream comprising the unreacted phenol of the initial phenol and a bisphenol A, separating a purge stream comprising the unreacted phenol, and wherein the unreacted phenol is present in the purge stream in an amount of 60 to 90 wt%, based on the total weight of the purge stream; adding the purge stream to a phenol purification section of a phenol production facility; and purifying the purge stream in the phenol purification section to form a purified phenol outlet stream in the phenol purification section, wherein the purified phenol outlet stream comprises a total phenol concentration of greater than or equal to 99.5 wt% based on the total weight of the purified phenol outlet stream; wherein the forming the purified phenol outlet stream comprises: heating a preheater inlet stream comprising cumene, a product phenol from the phenol production facility, and a product acetone from the phenol production facility in a preheater to form a splitter inlet stream; separating the splitter inlet stream into a splitter top outlet stream comprising the product acetone and the cumene and a splitter bottom outlet stream comprising the product phenol in a splitter column; separating the splitter bottom outlet stream into a crude top outlet stream comprising the product phenol and a crude bottom outlet stream comprising the cumene in a crude phenol column; hydro-extracting the crude top outlet stream in a hydro-extractor column to form an extractor primary outlet stream comprising the product phenol; and recovering the purified phenol outlet stream, from the extractor primary outlet stream in a finishing column; wherein the adding the purge stream comprises adding the purge stream to one or more of the preheater inlet stream, the splitter inlet stream; the splitter bottom outlet stream; and the crude top outlet stream. heating a preheater inlet stream comprising cumene, a product phenol from the phenol production facility, and a product acetone from the phenol production facility in a preheater to form a splitter inlet stream; separating the splitter inlet stream into a splitter top outlet stream comprising the product acetone and the cumene and a splitter bottom outlet stream comprising the product phenol in a splitter column; separating the splitter bottom outlet stream into a crude top outlet stream comprising the product phenol and a crude bottom outlet stream comprising the cumene in a crude phenol column; hydro-extracting the crude top outlet stream in a hydro-extractor column to form an extractor primary outlet stream comprising the product phenol; and recovering the purified phenol outlet stream, from the extractor primary outlet stream in a finishing column; wherein the adding the purge stream comprises adding the purge stream to one or more of the preheater inlet stream, the splitter inlet stream; the splitter bottom outlet stream; and the crude top outlet stream.