A process for producing bisphenol-A comprises reacting acetone and phenol in the presence of a catalyst system comprising an acidic heterogeneous catalyst and a catalyst promoter comprising at least one organic sulfur-containing compound to produce a reaction effluent comprising bisphenol-A, water, unreacted acetone, unreacted phenol and at least part of the catalyst promoter. At least part of the reaction effluent is distilled to remove water, catalyst promoter and unreacted acetone, and leave a residual stream containing bisphenol A. At least part of the residual stream is then contacted with a basic anion exchange resin to produce a purified stream, from which bisphenol-A is recovered.

A purification module configured to separate and purify a liquid solution is provided. The purification module may include a vessel configured to receive a predetermined amount of a liquid solution. The purification module may also include a heating apparatus configured to apply heat to the vessel at a temperature of a first boiling point, and a column apparatus configured to separate the liquid solution into a first liquid and a second liquid and purify the first liquid and the second liquid to a determined purity level. The column apparatus may include a first heating chamber, a second heating chamber, and a distillation chamber. The distillation chamber may be located between the first heating chamber and the second heating chamber. The first heating chamber and second heating chamber may be configured to receive a heat transfer liquid to apply heat to the distillation chamber at the temperature of the first boiling point.

A purification module configured to separate and purify a liquid solution is provided. The purification module may include a vessel configured to receive a predetermined amount of a liquid solution. The purification module may also include a heating apparatus configured to apply heat to the vessel at a temperature of a first boiling point, and a column apparatus configured to separate the liquid solution into a first liquid and a second liquid and purify the first liquid and the second liquid to a determined purity level. The column apparatus may include a first heating chamber, a second heating chamber, and a distillation chamber. The distillation chamber may be located between the first heating chamber and the second heating chamber. The first heating chamber and second heating chamber may be configured to receive a heat transfer liquid to apply heat to the distillation chamber at the temperature of the first boiling point.

A purification module configured to separate and purify a liquid solution is provided. The purification module may include a vessel configured to receive a predetermined amount of a liquid solution. The purification module may also include a heating apparatus configured to apply heat to the vessel at a temperature of a first boiling point, and a column apparatus configured to separate the liquid solution into a first liquid and a second liquid and purify the first liquid and the second liquid to a determined purity level. The column apparatus may include a first heating chamber, a second heating chamber, and a distillation chamber. The distillation chamber may be located between the first heating chamber and the second heating chamber. The first heating chamber and second heating chamber may be configured to receive a heat transfer liquid to apply heat to the distillation chamber at the temperature of the first boiling point.

A purification module configured to separate and purify a liquid solution is provided. The purification module may include a vessel configured to receive a predetermined amount of a liquid solution. The purification module may also include a heating apparatus configured to apply heat to the vessel at a temperature of a first boiling point, and a column apparatus configured to separate the liquid solution into a first liquid and a second liquid and purify the first liquid and the second liquid to a determined purity level. The column apparatus may include a first heating chamber, a second heating chamber, and a distillation chamber. The distillation chamber may be located between the first heating chamber and the second heating chamber. The first heating chamber and second heating chamber may be configured to receive a heat transfer liquid to apply heat to the distillation chamber at the temperature of the first boiling point.

A method for cultivating Monarda fistulosa for production of thymoquinone includes planting seeds at rates between about 2.5 and about 5 pounds per acre, preferably about 4 pounds per acre. The heavy rate of planting produces plants bearing oil without weed contamination and reduces herbicide use due to production of natural herbicides by the monarda plants. Seeding and mowing the first season, and harvesting in seasons thereafter reduce costs. The method results in increased production of essential oils including thymoquinone and thymohydroquinone at levels up to about 40% or more of recovered oils, and which may be distilled from the plant.

A method for cultivating Monarda fistulosa for production of thymoquinone includes planting seeds at rates between about 2.5 and about 5 pounds per acre, preferably about 4 pounds per acre. The heavy rate of planting produces plants bearing oil without weed contamination and reduces herbicide use due to production of natural herbicides by the monarda plants. Seeding and mowing the first season, and harvesting in seasons thereafter reduce costs. The method results in increased production of essential oils including thymoquinone and thymohydroquinone at levels up to about 40% or more of recovered oils, and which may be distilled from the plant.

The present disclosure provides a method for decomposing a phenolic by-product, the method including: a step S10 of injecting and mixing a bisphenol A by-product produced in a bisphenol A production process, a mixed by-product stream of phenol by-products produced in a phenol production process, a decomposition apparatus side discharge stream, and a process water stream in a mixing apparatus; a step S20 of injecting a mixing apparatus discharge stream discharged from the mixing apparatus into a phase separation apparatus and phase-separating the mixing apparatus discharge stream into an oil-phase stream and a liquid-phase stream; a step S30 of feeding the oil-phase stream, which is phase-separated in the step S20 and discharged from the phase separation apparatus, to a decomposition apparatus to decompose the oil-phase stream; and a step S40 of circulating the decomposition apparatus side discharge stream obtained by the decomposition in the step S30 to the mixing apparatus in the step S10.

The present disclosure provides a method for decomposing a phenolic by-product, the method including: a step S10 of injecting and mixing a bisphenol A by-product produced in a bisphenol A production process, a mixed by-product stream of phenol by-products produced in a phenol production process, a decomposition apparatus side discharge stream, and a process water stream in a mixing apparatus; a step S20 of injecting a mixing apparatus discharge stream discharged from the mixing apparatus into a phase separation apparatus and phase-separating the mixing apparatus discharge stream into an oil-phase stream and a liquid-phase stream; a step S30 of feeding the oil-phase stream, which is phase-separated in the step S20 and discharged from the phase separation apparatus, to a decomposition apparatus to decompose the oil-phase stream; and a step S40 of circulating the decomposition apparatus side discharge stream obtained by the decomposition in the step S30 to the mixing apparatus in the step S10.

Process for reducing the water and carboxylic acid content of an alcohol composition containing at least one C.sub.1-4 alcohol, water and at least one C.sub.1-4 carboxylic acid by (a) forming a vapor phase alcohol composition A and a liquid phase alcohol composition B, (b) separating a second vapor phase alcohol composition C and an aqueous phase D from the liquid phase alcohol composition B, the aqueous phase D containing the majority of the carboxylic acid that was present in the liquid phase alcohol composition B; (c) passing the vapor phase alcohol composition A to a drying unit, (d) passing the vapor phase alcohol composition C to a drying unit; and (e) recovering an alcohol composition from the drying units of steps (c) and (d). The recovered alcohol composition of step (e) has a reduced water and carboxylic acid content.