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The present invention relates to a process for the production of a blended syngas feed with a variable H 2 /CO ratio for use in a syngas conversion reactor. In this process a H 2 /CO ratio of from approximately 1.0 to 3.0 for the blended syngas feed is selected. A first syngas is formed with a H

The present invention relates to a process for the production of a blended syngas feed with a variable H 2 /CO ratio for use in a syngas conversion reactor. In this process a H 2 /CO ratio of from approximately 1.0 to 3.0 for the blended syngas feed is selected. A first syngas is formed with a H 2 /CO ratio of at least 2.0 by reacting methane with an oxygen source. A second syngas is formed with a H 2 /CO ratio of no more than 1.5 by reacting LPG with CO 2 . The first syngas and the second syngas are blended to form a blended syngas feed with the selected H 2 /CO ratio, and this blended syngas feed may be used in the syngas conversion reactor.

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1. A process for the production of a blended syngas feed with a desired H 2 /CO ratio comprising the steps of:(a) selecting a desired H 2 /CO ratio of a blended syngas feed;(b) forming a first syngas with a H 2 /CO ratio of at least 2.0 by reacting methane with an oxygen source, wherein the H 2

1. A process for the production of a blended syngas feed with a desired H 2 /CO ratio comprising the steps of:(a) selecting a desired H 2 /CO ratio of a blended syngas feed;(b) forming a first syngas with a H 2 /CO ratio of at least 2.0 by reacting methane with an oxygen source, wherein the H 2 /CO ratio of the first syngas is greater than the desired H 2 /CO ratio;(c) forming a second syngas with a H 2 /CO ratio of no more than 1.5 by reacting LPG with CO 2 , wherein the H 2 /CO ratio of the second syngas is less than the desired H 2 /CO ratio; and(d) blending the first syngas and the second syngas to form a blended syngas feed with the desired H 2 /CO ratio. 2. The process of claim 1, further comprising the step of converting the blended syngas feed in a syngas conversion reactor. 3. The process of claim 2, wherein the syngas conversion reactor is a Fischer-Tropsch reactor. 4. The process of claim 2, wherein the syngas conversion reactor is a methanol synthesis reactor. 5. The process of claim 1, wherein the desired H 2 /CO ratio of the blended syngas feed is in the range of 1.0 to 3.0. 6. The process of claim 5, wherein the desired H 2 /CO ratio of the blended syngas feed is in the range of 1.25 to 2.1. 7. The process of claim 6, wherein the desired H 2 /CO ratio of the blended syngas feed is in the range of 1.4 to 1.75. 8. The process of claim 1, wherein the first syngas is formed by an autothermal reformer and has a H 2 /CO ratio in the range of 2.0 to 2.5. 9. The process of claim 1, wherein the second syngas is formed by a dry reforming reaction and has a H 2 /CO ratio of no more than 1.0. 10. The process of claim 9, wherein the second syngas has a H 2 /CO ratio in the range of 0.5 to 1.0. 11. The process of claim 1, wherein at least a portion of the LPG reacted to form the second syngas in step (c) is recovered from a source selected from the group consisting of a natural gas asset, a syngas conversion reactor, a Fischer-Tropsch product upgrading reactor, and combinations thereof. 12. The process of claim 1, wherein at least a portion of the CO 2 reacted to form the second syngas in step (c) is recovered from a source selected from the group consisting of an effluent of a Fischer-Tropsch synthesis reactor, a syngas stream from a methane conversion process, a natural gas asset, a furnace flue gas, and combinations thereof. 13. The process of claim 1, wherein the oxygen reacted to form the first syngas in step (b) is obtained from a source selected from the group consisting of air, enriched air, purified oxygen, water, CO 2 , and combinations thereof. 14. The process of claim 13, wherein the oxygen reacted to form the first syngas in step (b) is obtained from purified oxygen, which contains at least 90% oxygen. 15. The process of claim 14, wherein the oxygen reacted to form the first syngas in step (b) is obtained from purified oxygen, which contains at least 95% oxygen. 16. The process of claim 15, wherein the oxygen reacted to form the first syngas in step (b) is obtained from purified oxygen, which contains at least 99% oxygen. 17. The process of claim 13, wherein the oxygen reacted to form the first syngas in step (b) is obtained from water. 18. A process of using LPG and CO 2 in preparing a syngas feed for a Fischer-Tropsch reactor, comprising the steps of:(a) contacting LPG and CO 2 at reforming reaction conditions to form a first syngas with a H 2 /CO ratio of no more than 1.5;(b) blending the first syngas with a second syngas, said second syngas having a H 2 /CO ratio of no less than 2.0, to form a blended syngas feed, wherein the blended syngas feed has a H 2 /CO ratio greater than the H 2 /CO ratio of the first syngas and less than the H 2 /CO ratio of the second syngas; and(c) feeding the blended syngas feed into a Fischer-Tropsch reactor. 19. The process of claim 18, wherein the second syngas is generated from a methane conversion process. 20. The process of claim 18, wherein the CO 2 contacted with LPG to form the first syngas in step (a) is recovered from a source selected from the group consisting of an effluent from a Fischer-Tropsch reactor, a syngas stream from a methane conversion process, a natural gas asset, a furnace flue gas, and combinations thereof. 21. The process of claim 20 wherein the CO 2 contacted with LPG to form the first syngas in step (a) is recovered from the effluent from a Fischer-Tropsch reactor. 22. The process of claim 18, wherein the LPG contacted with CO 2 to form the first syngas in step (a) is recovered from a source selected from the group consisting of a natural gas asset, an effluent from a Fischer-Tropsch reactor, a Fischer-Tropsch product upgrading reactor, and combinations thereof. 23. The process of claim 22, wherein the LPG contacted with CO 2 to form the first syngas in step (a) is recovered from an effluent from a Fischer-Tropsch reactor or a natural gas asset. 24. The process of claim 18, wherein the blended syngas feed has a H 2 /CO ratio in the range of 1.4 to 1.75. 25. An integrated process for producing a blended syngas feed with a desired H 2 /CO ratio for a Fischer-Tropsch reactor comprising the steps of:(a) selecting a desired H 2 /CO ratio of a blended syngas feed to a Fischer-Tropsch reactor;(b) reacting methane, oxygen, and steam to form a first syngas with a H 2 /CO ratio of at least 2.0, wherein the H 2 /CO ratio of the first syngas is greater than the desired H 2 /CO ratio;(c) reacting LPG and CO 2 to form a second syngas with a H 2 /CO ratio of no more than 1.5, wherein the H 2 /CO ratio of the second syngas is less than the desired H 2 /CO ratio;(d) blending the first syngas and the second syngas to form a blended syngas feed having the desired H 2 /CO ratio;(e) feeding the blended syngas feed into the Fischer-Tropsch reactor;(f) performing a Fischer-Tropsch synthesis process using the blended syngas feed;(g) recovering a third syngas comprising unreacted CO 2 , H 2 , CO, and CH 4 from the Fischer-Tropsch reactor;(h) recovering LPG from the Fischer-Tropsch reactor; and(i) recycling at least a portion of the third syngas to provide a feed to form the first syngas in step (b), to form the second syngas in step (c), to form the blended syngas feed in step (d), or combinations thereof. 26. The process of claim 25, wherein the LPG recovered from the Fischer-Tropsch reactor and the third syngas are used in forming the second syngas in step (c). 27. The process of claim 25, wherein at least a portion of the third syngas is reacted with the methane, oxygen, and steam of step (b) to form the first syngas with a H 2 /CO ratio of no less than 2.0. 28. The process of claim 25, wherein at least a portion of the third syngas is blended with the first syngas and the second syngas to form the blended syngas feed in step (d). 29. The process of claim 25, wherein the desired H 2 /CO ratio of the blended syngas feed is in the range of 1.0 to 3.0. 30. The process of claim 25, wherein the desired H 2 /CO ratio of the blended syngas feed is in the range of 1.4 to 1.75, the first syngas has a H 2 /CO ratio of 2.0 to 2.5, and the second syngas has a H 2 /CO ratio of between 0.5 and 1.0. 31. The process of claim 25, wherein the Fischer-Tropsch reactor contains a non-shifting Fischer-Tropsch catalyst. 32. The process of claim 31, wherein the non-shifting catalyst is a cobalt catalyst. 33. A process for the production of a blended syngas feed with a desired H 2 /CO ratio using a multiplicity of Fischer-Tropsch reactors in series comprising the steps of:(a) feeding a first syngas comprising H 2 and CO and having a H 2 /CO ratio in the range of 1.4 to 1.75 into a first Fischer-Tropsch synthesis reactor containing a cobalt containing catalyst and recovering at least one effluent therefrom;(b) recovering a second syngas comprising H 2 and CO from the effluent, wherein the second syngas has a lower H 2 /CO ratio than that of the first syngas;(c) formin g a third syngas with a H 2 /CO ratio of at least 2.0 by reacting methane with an oxygen source;(d) blending the second syngas with the third syngas to form a blended syngas feed having a desired H 2 /CO ratio in the range of 1.4 to 1.75 wherein the desired H 2 /CO ratio of the blended syngas feed is greater than the H 2 /CO ratio of the second syngas and less than the H 2 /CO ratio of the third syngas; and(e) feeding the blended syngas feed into a second Fischer-Tropsch reactor. 34. The process of claim 33, wherein the third syngas is formed by an autothermal reformer and has a H 2 /CO ratio in the range of 2.0 to 2.5. 35. A process for the production of a blended syngas feed with a desired H 2 /CO ratio using a multiplicity of Fischer-Tropsch reactors in series comprising the steps of:(a) feeding a first syngas, comprising H 2 and CO and having a H 2 /CO ratio in the range of 1.25 to 2.1, into a first Fischer-Tropsch synthesis reactor containing an iron containing catalyst and recovering at least one effluent therefrom;(b) recovering a second syngas from the effluent, wherein the second syngas has a higher H 2 /CO ratio than that of the first syngas;(c) forming a third syngas with a H 2 /CO ratio of no more than 1.5 by reacting LPG with CO 2 ;(d) blending the second syngas with the third syngas to form a blended syngas feed having a desired H 2 /CO ratio in the range of 1.4 to 1.75 wherein the desired H 2 /CO ratio of the blended syngas feed is less than the H 2 /CO ratio of the second syngas and greater than the H 2 /CO ratio of the third syngas; and(e) feeding the blended syngas feed into a second Fischer-Tropsch reactor. 36. The process of claim 35, wherein the third syngas is formed by a dry reforming reaction and has a H 2 /CO ratio of no more than 1.0. 37. The process of claim 35, wherein the H 2 /CO ratio of the first syngas is in the range of 1.4 to 1.75. 38. A process for producing fuel comprising:(a) reacting LPG and CO 2 to form a first syngas with a H 2 /CO ratio of no more than 1.5;(b) blending the first syngas with a second syngas, having a H 2 /CO ratio of at least 2.0, to form a blended syngas, wherein the blended syngas has a H 2 /CO ratio greater than the H 2 /CO ratio of the first syngas and less than the H 2 /CO ratio of the second syngas;(c) reacting the blended syngas in a Fischer-Tropsch process to produce a hydrocarbonaceous effluent; and (d) converting at least a portion of the hydrocarbonaceous effluent into at least one fuel. 39. The process of claim 38, further comprising converting a portion of the hydrocarbonaceous effluent into at least one lubricant base stock. 40. The process of claim 38, wherein the second syngas is formed in a reaction between CH 4 and an oxygen source. 41. The integrated process of claim 25, wherein the integrated process has a carbon efficiency of greater than 75%.