초록

The invention provides an improved process and apparatus for integrating the heat transfer zones of spiral-wound, plate fin, tube and finned tube exchangers thus increasing the overall effectiveness of the process.

대표청구항 ▼

1. A process for recovering energy from a hydrogen-bearing synthesis gas stream comprising: a. providing a first heat exchanger having at least four separate flow circuits;b. supplying a first hot hydrogen-bearing synthesis gas stream to a first flow circuit of said first heat exchanger;c. supplying

1. A process for recovering energy from a hydrogen-bearing synthesis gas stream comprising: a. providing a first heat exchanger having at least four separate flow circuits;b. supplying a first hot hydrogen-bearing synthesis gas stream to a first flow circuit of said first heat exchanger;c. supplying a first cool heat exchange medium to a second flow circuit of said first heat exchanger whereby said hot hydrogen-bearing synthesis gas stream is cooled by indirect heat exchange with said first cool heat exchange medium;d. feeding a second cool heat exchange medium to a third flow circuit of said first heat exchanger whereby said hot hydrogen-bearing synthesis gas stream is cooled by indirect heat exchange with said second cool heat exchange medium;e. feeding a third cool heat exchange medium to a fourth flow circuit of said first heat exchanger whereby said hot hydrogen-bearing synthesis gas stream is cooled by indirect heat exchange with said third cool heat exchange medium; andf. removing cooled hydrogen-bearing synthesis gas stream from said heat exchanger; wherein said first heat exchanger is divided into at least a first section and a second section; indirect heat exchange between the hot hydrogen-bearing synthesis gas stream and the second cool heat exchange medium is performed only in said first section of said first heat exchanger and indirect heat exchange between the hot hydrogen-bearing synthesis gas stream and the third cool heat exchange medium is performed only in said first section of said first heat exchanger and indirect heat exchange between the hot hydrogen-bearing synthesis gas stream and the first cool heat exchange medium is performed in both the first section and the second section of said first heat exchanger. 2. The process as claimed in claim 1, wherein said first hot hydrogen-bearing synthesis gas stream is obtained from process selected from the group consisting of a steam/hydrocarbon reforming process, a coal gasification process and a partial oxidation process. 3. The process as claimed in claim 2 wherein said first cool heat exchange medium is a hydrocarbon feed stream selected from the group consisting of a steam/hydrocarbon reforming process, a coal gasification process and a partial oxidation process. 4. The process as claimed in claim 1 wherein said first cool heat exchange medium is a hydrocarbon feed stream, said second cool heat exchange medium is a boiler water stream and said third cool heat exchange medium is a water stream of sufficient quality to produce steam for reforming reactions and export steam purity. 5. The process as claimed in claim 1 further comprising removing at least a portion of the hot hydrogen-bearing synthesis gas from said first heat exchanger; subjecting the hot hydrogen-bearing synthesis removed from said first heat exchanger to heat exchange in a second heat exchanger, and returning at least a portion of the resultant cooled hydrogen-bearing synthesis to said first heat exchanger for further cooling by indirect heat exchange. 6. The process as claimed in claim 1 wherein said first heat exchanger is selected from the group consisting of a spiral-wound tube heat exchanger, a plate-fin heat exchanger and a shell-tube heat exchanger. 7. The process as claimed in claim 1 wherein said hot hydrogen-bearing synthesis gas undergoes indirect heat exchange with more than one heat exchange medium at the same time. 8. The process as claimed in claim 1 further comprising: removing all or a portion of the hydrogen-bearing synthesis gas stream from said first section of said first heat exchanger; subjecting the hydrogen-bearing synthesis gas removed from said first section of said first heat exchanger to heat exchange in a second heat exchanger; removing the hydrogen-bearing synthesis gas from said second heat exchanger and introducing it into a gas/liquid separator, and removing uncondensed hydrogen-bearing synthesis gas stream from said gas/liquid separator and introducing it into said second section of said first heat exchanger. 9. The process as claimed in claim 1 further comprising: removing at least a portion of the hot hydrogen-bearing synthesis gas stream from said first heat exchanger,subjecting the hot hydrogen-bearing synthesis gas stream removed from said first heat exchanger to heat exchange in a second heat exchanger,returning at least a portion of the resultant cooled hydrogen-bearing synthesis gas stream to said first heat exchanger for further cooling by indirect heat exchange, andremoving condensate, formed during the cooling of said first hot hydrogen-bearing synthesis gas stream in said second heat exchanger, from second heat exchanger. 10. The process as claimed in claim 1 wherein said hydrogen-bearing synthesis gas comprises 35 to 75 mol % hydrogen, 0 to 2 mol % nitrogen, 2 to 45 mol % carbon monoxide, 12 to 40 mol % carbon dioxide, 0 to 10 mol % hydrogen sulfide and less than 3 mol % C+2 hydrocarbons. 11. The process as claimed in claim 1 wherein said hydrogen-bearing synthesis gas contains up to 11 mol % methane and up to 10 mol % hydrogen sulfide. 12. The process as claimed in claim 1 wherein said hydrogen-bearing synthesis gas is cooled from a temperature of 250° to 450° C. to a temperature of 30° to 50° C. 13. The process as claimed in claim 1 wherein said flow circuits defining the cooling portions of said heat exchanger are in a configuration selected from the group consisting of intertwined, alternated sequentially or in a pattern and overlapped. 14. A process for recovering energy from a hydrogen-bearing synthesis gas stream comprising: a. providing a first heat exchanger having at least four separate flow circuits;b. supplying a first hot hydrogen-bearing synthesis gas stream to a first flow circuit of said first heat exchanger;c. supplying a first cool heat exchange medium to a second flow circuit of said first heat exchanger whereby said hot hydrogen-bearing synthesis gas stream is cooled by indirect heat exchange with said first cool heat exchange medium;d. feeding a second cool, heat exchange medium to a third flow circuit of said first heat exchanger whereby said hot hydrogen-bearing synthesis gas stream is cooled by indirect heat exchange with said second cool heat exchange medium;e. feeding a third cool heat exchange medium to a fourth flow circuit of said first heat exchanger whereby said hot hydrogen-bearing synthesis gas stream is cooled by indirect heat exchange with said third cool heat exchange medium; andf. removing cooled hydrogen-bearing synthesis gas stream from said heat exchanger; wherein said first heat exchanger is divided into at least a first section and a second section and said process further comprising removing condensate, formed during the cooling of said first hot hydrogen-bearing synthesis gas stream, from said first section and said second section;wherein the process further comprises:removing at least a portion of the hot hydrogen-bearing synthesis from said first section of said first heat exchanger,subjecting the hot hydrogen-bearing synthesis removed from said first section of said first heat exchanger to heat exchange in a second heat exchanger,returning at least a portion of the resultant cooled hydrogen-bearing synthesis to said first heat exchanger for further cooling by indirect heat exchange, and removing condensate, formed during the cooling of said first hot hydrogen-bearing synthesis gas stream in said second heat exchanger, from second heat exchanger. 15. The process as claimed in claim 14 wherein in said first section of said first heat exchanger, indirect heat exchange is performed between the hot hydrogen-bearing synthesis gas stream and the second cool heat exchange medium, and between the hot hydrogen-bearing synthesis gas stream and the third cool heat exchange medium. 16. The process as claimed in claim 14 wherein indirect heat exchange between the hot hydrogen-bearing synthesis gas stream and the first cool heat exchange medium is performed in both the first section and the second section of said first heat exchanger. 17. The process as claimed in claim 14 wherein said first hot hydrogen-bearing synthesis gas stream is obtained from process selected from the group consisting of a steam/hydrocarbon reforming process, a coal gasification process and a partial oxidation process. 18. The process as claimed in claim 17 wherein said first cool heat exchange medium is a hydrocarbon feed stream selected from the group consisting of a steam/hydrocarbon reforming process, a coal gasification process and a partial oxidation process. 19. The process as claimed in claim 14 wherein said first cool heat exchange medium is a hydrocarbon feed stream, said second cool heat exchange medium is a boiler water stream and said third cool heat exchange medium is a water stream of sufficient quality to produce steam for reforming reactions and export steam purity. 20. The process as claimed in claim 14 wherein said first heat exchanger is selected from the group consisting of a spiral-wound tube heat exchanger, a plate-fin heat exchanger and a shell-tube heat exchanger. 21. The process as claimed in claim 14 wherein said hot hydrogen-bearing synthesis gas undergoes indirect heat exchange with more than one heat exchange medium at the same time. 22. The process as claimed in claim 14 further comprising: removing all or a portion of the hydrogen-bearing synthesis gas stream from said first section of said first heat exchanger; subjecting the hydrogen-bearing synthesis gas removed from said first section of said first heat exchanger to heat exchange in a second heat exchanger; removing the hydrogen-bearing synthesis gas from said second heat exchanger and introducing it into a gas/liquid separator, and removing uncondensed hydrogen-bearing synthesis gas stream from said gas/liquid separator and introducing it into said second section of said first heat exchanger. 23. The process as claimed in claim 14 further comprising: removing the hydrogen-bearing synthesis gas from said second heat exchanger and introducing it into a gas/liquid separator; removing uncondensed hydrogen-bearing synthesis gas stream from said gas/liquid separator and introducing it into a third heat exchanger; and removing hydrogen-bearing synthesis gas from said third heat exchanger and introducing it into a second gas/liquid separator, from which cooled product hydrogen-bearing synthesis gas is removed. 24. The process as claimed in claim 14 wherein said hydrogen-bearing synthesis gas comprises 35 to 75 mol % hydrogen, 0 to 2 mol % nitrogen, 2 to 45 mol % carbon monoxide, 12 to 40 mol % carbon dioxide, 0 to 10 mol % hydrogen sulfide and less than 3 mol % C+2 hydrocarbons. 25. The process as claimed in claim 14 wherein said hydrogen-bearing synthesis gas contains up to 11 mol % methane and up to 10 mol % hydrogen sulfide. 26. The process as claimed in claim 14 wherein said hydrogen-bearing synthesis gas is cooled from a temperature of 250° to 450° C. to a temperature of 30° to 50° C. 27. The process as claimed in claim 14 wherein said flow circuits defining the cooling portions of said heat exchanger are in a configuration selected from the group consisting of intertwined, alternated sequentially or in a pattern and overlapped.