RECYCLE CONTENT (C4)ALKANOIC ACID

1 - 47 . (canceled)

48 . A method of making recycle (C 4 )alkanoic acid (r-(C 4 )alkanoic acid), said method comprising carboxylating a recycle propylene composition (r-propylene) to thereby produce a carboxylation effluent comprising (C 4 )alkanoic acid, wherein said r-propylene is derived directly or indirectly from cracking recycle pyoil composition (r-pyoil).

49 . A method of making recycle (C 4 )alkanoic acid (r-(C 4 )alkanoic acid), said method comprising oxidizing a recycle (C 4 )alkanal (r-(C 4 )alkanal) to thereby produce an oxidation effluent comprising (C 4 )alkanoic acid, wherein said r-(C 4 )alkanal is produced from a recycled propylene composition (r-propylene) and said r-propylene is derived directly or indirectly from cracking recycle pyoil composition (r-pyoil).

50 . A method of obtaining a recycle content in (C 4 )alkanoic acid comprising:

method 1:

a. obtaining a propylene composition designated as having recycle content, and

b. feeding said propylene to a reactor under conditions effective to make (C 4 )alkanoic acid, and

wherein, whether or not the designation so indicates, at least a portion of said propylene composition is derived directly or indirectly from cracking a recycle pyoil composition (r-pyoil); or

method 2:

a. obtaining an (C 4 )alkanal designated as having recycle content, and

b. feeding said (C 4 )alkanal to a reactor under conditions effective to make (C 4 )alkanoic acid, and

wherein, whether or not the designation so indicates, at least a portion of said (C 4 )alkanal is produced from a recycle propylene composition that is derived directly or indirectly from cracking a recycle pyoil composition (r-pyoil).

51 . The method of claim 48 , wherein the r-propylene is directly or indirectly derived from cracking r-pyoil.

52 . The method of claim 49 , wherein the r-propylene is directly or indirectly derived from cracking r-pyoil in a gas furnace.

53 . The method of claim 50 , wherein the r-propylene is directly or indirectly derived from cracking r-pyoil in a split furnace or a thermal steam gas furnace.

54 . The method of claim 53 , wherein a cracker facility in which the r-propylene made is in fluid communication, continuously or intermittently, with an (C 4 )alkanal formation facility.

55 . The method of claim 54 , wherein the manufacturer of the (C 4 )alkanal has acquired:

a. a propylene volume made from r-pyoil under a certification, representation, or as advertised, orb. has transferred credits with the supply of propylene to the manufacturer of the (C 4 )alkanal sufficient to allow the manufacturer of the (C 4 )alkanal to satisfy the certification requirements or to make its representations or advertisements, or

b. the propylene has allocated to it a recycle content where such allocation was obtained, through one or more intermediary entities, from a cracked propylene volume at least part of which is obtained by cracking r-pyoil.

56 . The process method of claim 54 , wherein the r-pyoil is a liquid at 25° C. and 1 atm., and predominantly comprises C 5 to C 25 hydrocarbons.

57 . The method 55 , wherein the r-pyoil comprises:

(1) C 4 -C 12 aliphatic compounds (branched or unbranched alkanes and alkenes including diolefins, and alicyclics) and C 13 -C 22 aliphatic compounds in a weight ratio of more than 1:1 and based on the weight of the r-pyoil;

(2) C 13 -C 22 aliphatic compounds (branched or unbranched alkanes and alkenes including diolefins, and alicyclics) and C 4 -C 12 aliphatic compounds in a weight ratio of more than 1:1 and based on the weight of the r-pyoil;

(3) paraffins in an amount of 5 based on the weight of the r-pyoil;

(4) naphthenes or cyclic aliphatic hydrocarbons in amount of 0-35 as wt. % based on the weight of the r-pyoil composition;

(5) not more than 30 weight percent of aromatics, based on the total weight of the r-pyoil;

(6) olefins present in an amount ranging from 40-85 as wt. % based on the weight of the r-pyoil; or

(7) oxygenated compounds or polymers in amount ranging from 0-20 wt. % based on the weight of the r-pyoil.

58 . The method of claim 57 , wherein:

(1) the amount of oxygen atoms in the r-pyoil is from 0-8, or 0-5 wt. % based on the weight of the r-pyoil;

(2) the amount of heteroatoms in the r-pyoil is not more than 5 wt. %, based on the weight of the r-pyoil; or

(3) the sulfur content of the r-pyoil does not exceed 2.5 wt. % based on the weight of the r-pyoil.

59 . The method of claim 58 , wherein the solubility of water in the r-pyoil at 1 atm and 25° C. is less than 2 wt. %, water based on the weight of the r-pyoil.

60 . The method of claim 59 , wherein the r-pyoil can have the following compositional content:

a. carbon atom content of at least 75 wt. %;

b. hydrogen atom content of at least 10 wt %,

c. an oxygen atom content not to exceed 10 wt. %,

in each case based on the weight of the r-pyoil.

61 . The method of claim 60 wherein the weight ratio of paraffin to naphthene can be at least 1:1, based on the weight of the r-pyoil.

62 . The method of claim 61 , wherein the r-pyoil the 90% boiling point of the cracker feed stream or composition to a cracker furnace is not more than 350° C.

63 . The method of claim 62 , wherein the r-pyoil may be introduced into a cracking furnace or coil or tube alone, or combined with one or more non-recycle cracker feed streams.

64 . The method of claim 63 , wherein the r-pyoil is present in an amount of not more than 40 weight percent based on the total weight of the combined stream with a non-recycle cracker feed stream.

65 . The method of claim 64 , comprising feeding a cracker feed stream to a furnace comprising r-pyoil, said cracker feed stream comprising a predominantly C 2 to C 4 hydrocarbon containing composition.

66 . The method of claim 65 , wherein the r-pyoil is cracked in a gas furnace.

67 . The method of claim 66 , wherein the r-pyoil is fed to at least one coil in a furnace which receives (or is operated to receive), at the inlet of the coil at the entrance to a convection zone in the furnace, a predominately vapor-phase feed (more than 50% of the weight of the feed is vapor) (“gas coil”).

68 . The method of claim 67 , wherein the gas coil receives a predominately C 2 -C 4 feedstock, or a predominately a C 2 -C 3 feedstock to the inlet of the coil in the convection section, or alternatively, having at least one coil receiving more than 50 wt. % ethane and/or more than 50% propane and/or more than 50% LPG, or in any one of these cases at least 60 wt % based on the weight of the cracker feed to the coil, or alternatively based on the weight of the cracker feed to the convection zone.