Abstract: Hydrocarbon distillation columns with heat pumps and methods of operating them are described. The overhead stream is compressed to increase temperature so that it can be used both to heat the reboiler and to superheat the overhead stream before it enters the heat pump compressor.

Abstract: One exemplary embodiment can be a process for separating a plurality of naphtha components. The process can include first and second columns. The first column may include a dividing imperforate wall with one surface facing a feed and another surface facing a side stream. Typically, the wall extends a significant portion of the column height to divide the portion into at least two substantially vertical, parallel contacting sections. Also, the second column can communicate with the first column so as to provide a feed to or receive a feed from the first column. Generally, the second column is non-divided. The process may provide at least four product streams.

Abstract: Light naphtha distillation columns with heat pumps and methods of operating them are described. The overhead stream is compressed to increase temperature so that it can be used both to heat the reboiler and to superheat the overhead stream before it enters the heat pump compressor.

Abstract: A process is disclosed for recovering product from catalytically converted product streams. Gaseous unstabilized naphtha from an overhead receiver from a main fractionation column is compressed in a compressor. Liquid unstabilized naphtha from the overhead receiver and liquid naphtha fraction from the compressor are sent to a naphtha splitter column upstream of a primary absorber. Consequently, less naphtha is circulated in the gas recovery system.

Abstract: A process is disclosed for recovering hydroprocessing effluent from a hydroprocessing unit utilizing a hot stripper and a cold stripper. The cold stripper and the hot stripper utilize a common overhead recovery apparatus.

Abstract: An apparatus is disclosed for recovering hydroprocessing effluent from a hydroprocessing unit utilizing a hot stripper and a cold stripper. The cold stripper and the hot stripper utilize a common overhead recovery apparatus.

Abstract: A process is disclosed for recovering hydroprocessing effluent from a hydroprocessing unit utilizing a hot stripper and a cold stripper. Only the hot hydroprocessing effluent is heated in a fired heater prior to product fractionation, resulting in substantial operating and capital savings.

Abstract: A process is disclosed for recovering hydroprocessing effluent from a hydroprocessing unit utilizing a hot stripper and a cold stripper. The cold stripper and the hot stripper are contained in the same vessel. A barrier prevents material from the hot stripper from entering into the cold stripper.

Abstract: An apparatus is disclosed for recovering hydroprocessing effluent from a hydroprocessing unit utilizing a hot stripper and a cold stripper. The cold stripper and the hot stripper are contained in the same vessel. A barrier prevents material from the hot stripper from entering into the cold stripper.

Abstract: An apparatus is disclosed for recovering hydroprocessing effluent from a hydroprocessing unit utilizing a hot stripper and a cold stripper. Only the hot hydroprocessing effluent is heated in a fired heater prior to product fractionation, resulting in substantial operating and capital savings.

Abstract: One exemplary embodiment can be a process for separating a plurality of naphtha components. The process can include first and second columns. The first column may include a dividing imperforate wall with one surface facing a feed and another surface facing a side stream. Typically, the wall extends a significant portion of the column height to divide the portion into at least two substantially vertical, parallel contacting sections. Also, the second column can communicate with the first column so as to provide a feed to or receive a feed from the first column. Generally, the second column is non-divided. The process may provide at least four product streams.

Abstract: One exemplary embodiment can be a separation zone for separating a plurality of naphtha components. The separation zone can include first and second columns. The first column may include a dividing imperforate wall with one surface facing a feed and another surface facing a side stream. Typically, the wall extends a significant portion of the column height to divide the portion into at least two substantially vertical, parallel contacting sections. Also, the second column can communicate with the first column so as to provide a feed to or receive a feed from the first column. Generally, the second column is non-divided. The separation zone may provide at least four product streams.

Abstract: An apparatus is disclosed for recovering product from catalytically converted product streams. Gaseous unstabilized naphtha from an overhead receiver from a main fractionation column is compressed in a compressor. Liquid unstabilized naphtha from the overhead receiver and liquid naphtha fraction from the compressor are sent to a naphtha splitter column upstream of a primary absorber. Consequently, less naphtha is circulated in the gas recovery system.

Abstract: One exemplary embodiment can be a system for separating a plurality of naphtha components. The system can include a column, an overhead condenser, and a side condenser. Generally, the column includes a dividing imperforate wall with one surface facing a feed and another surface facing at least one side stream. Typically, the wall extends a significant portion of the column height to divide the portion into at least two substantially vertical, parallel contacting sections. Typically, the overhead condenser receives an overhead stream including a light naphtha from the column. Usually, a side condenser receives a process stream from the column and returns the stream to the column to facilitate separation. A cooling stream may pass through the overhead condenser and then the side condenser.

Abstract: An apparatus is disclosed for recovering product from catalytically converted product streams. An integrated debutanizer column provides an LPG stream, a light naphtha stream and a heavy naphtha stream. The integrated debutanizer column may comprise a dividing wall column. The light naphtha stream may be used as an absorbent for a primary absorber column which provides advantageous operation.

Abstract: A process is disclosed for recovering product from catalytically converted product streams. An integrated debutanizer column provides an LPG stream, a light naphtha stream and a heavy naphtha stream. The integrated debutanizer column may comprise a dividing wall column. The light naphtha stream may be used as an absorbent for a primary absorber column which provides advantageous operation.

Abstract: One exemplary embodiment can be a system for separating a plurality of naphtha components. The system can include a column, an overhead condenser, and a side condenser. Generally, the column includes a dividing imperforate wall with one surface facing a feed and another surface facing at least one side stream. Typically, the wall extends a significant portion of the column height to divide the portion into at least two substantially vertical, parallel contacting sections. Typically, the overhead condenser receives an overhead stream including a light naphtha from the column. Usually, a side condenser receives a process stream from the column and returns the stream to the column to facilitate separation. A cooling stream may pass through the overhead condenser and then the side condenser.

Abstract: An aromatics complex producing one or more xylene isomers offers a large number of opportunities to conserve energy by heat exchange within the complex. One previously unrecognized opportunity is through providing two parallel distillation columns operating at different pressures to separate C8 aromatics from C9+ aromatics. The parallel columns offer additional opportunities to conserve energy within the complex through heat exchange in associated xylene recovery facilities.

Abstract: A process for recovering waste heat in an organic Rankine cycle system which comprises passing a liquid phase working fluid through heat exchange in successive communication with two or more process streams which thus heat the working fluid, removing a vapor phase working fluid from the heat exchanger, passing the vapor phase working fluid to an expander wherein the waste heat is converted into mechanical energy, and passing the vapor phase working fluid from the expander to a condenser wherein the vapor phase working fluid is condensed into the liquid phase working fluid.

Abstract: Methods are described for generating electrical power from low grade heat sources from refining and petrochemical processes, including overhead vapors from vapor-liquid contacting apparatuses such as distillation columns, absorbers, strippers, quenching towers, scrubbers, etc. In many cases, these overhead vapors exit the apparatuses at a temperature from about 90° C. (194° F.) to about 175° C. (347° F.). Rather than rejecting the low temperature heat contained in these vapors to cooling air and/or cooling water, the vapors may instead be used to evaporate an organic working fluid. The vapors of the working fluid may then be sent to a turbine to drive a generator or other load.