초록 ▼

A process for converting light alkanes from a natural gas production stream to higher molecular weight hydrocarbons is provided. The method includes transporting the natural gas stream to an electron beam reactor, such as a steel flow-type radiation reactor connected hermetically to an accelerator b

A process for converting light alkanes from a natural gas production stream to higher molecular weight hydrocarbons is provided. The method includes transporting the natural gas stream to an electron beam reactor, such as a steel flow-type radiation reactor connected hermetically to an accelerator beam window. The gas stream is exposed to electron beam radiation to generate an upgraded and substantially liquefied hydrocarbon stream. The method then includes transporting the substantially liquefied hydrocarbon stream into a scrubber to remove non-condensed gases. The remaining liquid hydrocarbon stream is then transported as condensate to a distillation tower, where high octane products are separated through fractionation.

대표청구항 ▼

1. A process for converting a gas stream comprising primarily a mixture of light alkanes into a high-octane liquid stream, comprising: transporting the gas stream to a reactor at a gas processing facility; introducing the gas stream into a reactor whereupon components of the gas stream are exposed t

1. A process for converting a gas stream comprising primarily a mixture of light alkanes into a high-octane liquid stream, comprising: transporting the gas stream to a reactor at a gas processing facility; introducing the gas stream into a reactor whereupon components of the gas stream are exposed to electron beam radiation within the reactor to increase the molecular weight of hydrocarbons in the gas stream, thereby producing an upgraded radiolysis fluid stream; transporting the radiolysis fluid stream into a separator, thereby producing a first gaseous stream comprising primarily light alkanes, and a second liquid stream comprising primarily heavy alkanes; re-circulating the first stream back into an inlet of the reactor for additional irradiation and upgrading; and transporting the liquid stream off-site for further processing or for commercial sale, wherein the liquid stream comprises a transportation fuel having an octane rating of at least 100; transporting the second liquid stream as condensate to a distillation column; and fractionating the condensate into separate products comprising at least heptane (and heptane isomers), hexane (and hexane isomers) and octane; and transporting the natural gas stream comprises moving at least a portion of the natural gas stream through a pipeline; and the process further comprises sweetening the gas stream before introduction into the reactor, wherein the gas stream originates from a natural gas stream incident to oil and gas production operations; and transporting the natural gas stream to a reactor comprises moving the natural gas stream from a wellhead or from a field gathering facility to the reactor, the separator comprises a shell-and-tube heat exchanger for chilling the radiolysis fluid stream, and a distillation column for capturing non-condensable fluids, and the electron beam is generated by 1 MeV at 400 kW. 2. The process of claim 1, wherein the gas stream is a natural gas stream, an artificial gaseous alkane mixture, or gaseous industrial waste. 3. The process of claim 1, wherein: the gas stream originates from a natural gas stream incident to oil and gas production operations; and transporting the natural gas stream to a reactor comprises moving the natural gas stream from a wellhead or from a field gathering facility to the reactor. 4. The process of claim 3, further comprising: (i) removing any H.sub.2O from the natural gas stream before introducing the natural gas stream into the reactor, (ii) removing any CO.sub.2 from the natural gas stream before introducing the natural gas stream into the reactor, (ii) removing any H.sub.2S from the natural gas stream before introducing the natural gas stream into the reactor, or (iii) combinations thereof. 5. The process of claim 4, further comprising: pressuring the natural gas stream to at least 15 psi, and heating the natural gas stream to at least 100.degree. F. before introducing the natural gas stream into the reactor. 6. The process of claim 5, wherein pressuring and heating the natural gas production stream is done through the use of at least one blower. 7. The process of claim 5, wherein the separate comprises one or more gas-liquid centrifugal separators in series. 8. The process of claim 5, further comprising: monitoring the hydrogen (H.sub.2) content in the first gaseous stream released from the separator; and when the hydrogen content reaches 10% by volume in the first gaseous stream, sending non-condensed gases of the first gaseous stream to a hydrogen separator for removal of hydrogen gases before the first gaseous stream is re-circulated back into the reactor for additional irradiation and upgrading. 9. The process of claim 8, wherein: monitoring the hydrogen (H. sub.2) content is done by using an H. sub.2 sensor proximate a discharge line from the reactor; and the hydrogen separator is removed from the gas mixture by either a membrane separator or a pressure swing absorption unit. 10. The process of claim 9, wherein: excess hydrogen is removed from the non-condensed gases by a pressure swing absorption unit; and the pressure swing absorption unit is operated at 100 psi and contains (i) activated carbon, (ii) zeolite, or (iii) a combination thereof. 11. The process of claim 10, wherein the pressure swing absorption unit is maintained at 120.degree. F. or higher. 12. The process of claim 1, further comprising: before re-circulating, removing hydrogen gas from the first gaseous stream using a membrane separator. 13. The process of claim 1, wherein the reactor is a steel flow-type reactor connected hermetically to an accelerator beam window. 14. The process of claim 1, wherein: the gas production stream is moved through an irradiation area within the reactor at a rate of 800 m.sup.3/hour; and a rate of energy consumption for an absorbed dose rate is 2.0 kW/m.sup.3. 15. The process of claim 1, further comprising: blending at least a portion of the liquid stream as a condensate product into a lower-octane fuel to generate a higher octane transportation fuel.