Process for sulfur production

Claim 2

A process for the production of sulfur with control of process temperature by use of a liquid heat transfer fluid which comprises: (a) providing a closed loop heat transfer system including a liquid heat transfer fluid; (b) condensing sulfur from a product gas stream containing sulfur, sulfur dioxide, and hydrogen sulfide by indirect heat exchange with cooled liquid heat transfer fluid stream in a first indirect heat exchange zone to provide a cooled residual gas comprising hydrogen sulfide and sulfur dioxide and a heated liquid heat transfer fluid stream, said product gas stream being formed by contacting, in a catalytic selective oxidation zone, a feed gas heated, at least in part, for feed to said catalytic selective oxidation zone by indirect heat exchange with a first portion of the heated liquid heat transfer fluid stream in a second indirect heat exchange zone, said feed gas comprising an acid gas stream containing from about 1 to 100 percent by volume hydrogen sulfide in admixture with oxygen present in an amount of from about 70 to 130 percent of the stoichiometric amount required for oxidation of the hydrogen sulfide to elemental sulfur and a recycle gas which is a portion of a residual gas comprising hydrogen sulfide and sulfur dioxide resulting from condensation of sulfur from the effluent of the catalytic selective oxidation zone, with a selective oxidation catalyst capable of selectively oxidizing hydrogen sulfide to sulfur dioxide substantially without formation of sulfur trioxide and catalytically converting introduced hydrogen sulfide to sulfur dioxide and sulfur at a temperature above the kindling temperature of the catalyst and below an upper reaction temperature of about 850° F., the upper reaction temperature being selectively controlled by the amount of recycle gas introduced to the catalytic selective oxidation zone; (c) indirectly heating the balance of cooled residual gas exiting the first heat exchange zone in a third indirect heat exchange zone with a second portion of the heated liquid heat transfer fluid stream to a temperature for feed to a Claus conversion stage; (d) passing the heated balance of the residual gas stream to at least one Claus conversion zone to form additional sulfur; and (e) combining liquid heat transfer fluid streams from the second and third indirect heat exchange zones and cooling the combined liquid heat transfer fluid streams for recycle to the process.

Claim 3

A process as claimed in claim 1 in which the upper reaction temperature is below about 700° F.

Claim 4

A process as claimed in claim 1 in which the amount of cooled residual gas returned to the catalytic selective oxidation zone is about 0.1 to about 10 moles per mole of acid gas feed.

Claim 5

A process as claimed in claim 1 in which the amount of oxygen introduced is about the stoichiometric amount required for conversion of hydrogen sulfide to sulfur.

Claim 6

A process as claimed in claim 1 in which the feed gas is introduced to the catalytic selective oxidation zone at a temperature from about 270° F. to about 450° F.

Claim 7

A process as claimed in claim 1 in which the feed gas is introduced to the catalytic selective oxidation zone at a temperature from about 325° F. to about 400° F.

Claim 8

A process as claimed in claim 1 in which the oxygen is provided as air.

Claim 9

A process for the production of sulfur with control of process temperature by use of a liquid heat transfer fluid which comprises: (a) providing a closed loop heat transfer system containing a liquid heat transfer fluid; (b) condensing sulfur from a product gas stream containing sulfur, sulfur dioxide, and hydrogen sulfide by indirect heat exchange with cooled liquid heat transfer fluid stream in a first indirect heat exchange zone to provide a cooled residual gas comprising hydrogen sulfide and sulfur dioxide and a heated liquid heat transfer fluid stream, said product gas stream being formed by introducing to a catalytic selective oxidation zone, a feed gas heated, at least in part, for feed to said catalytic selective oxidation zone by indirect heat exchange with a first portion of the heated liquid heat transfer fluid stream in a second indirect heat exchange zone, said feed gas comprising an acid gas stream containing from about 1 to 100 percent by volume hydrogen sulfide in admixture with oxygen present in an amount of from about 70 to 130 percent of the stoichiometric amount required for oxidation of the hydrogen sulfide to elemental sulfur and a recycle gas which is a portion of a residual gas comprising hydrogen sulfide and sulfur dioxide resulting from condensation of sulfur from the effluent of the catalytic selective oxidation zone, at an inlet temperature of from about 270° F. to about 450° F. and contacting the feed gas with a selective oxidation catalyst capable of selectively oxidizing hydrogen sulfide to sulfur dioxide substantially without formation of sulfur trioxide, said catalyst comprising vanadium oxide and/or sulfide as an essential active ingredient supported on a non-alkaline porous refractory oxide, and catalytically converting introduced hydrogen sulfide to sulfur dioxide and sulfur below an outlet temperature of about 850° F., said outlet temperature controlled by the amount of recycle gas introduced to the catalytic selective oxidation zone; (c) indirectly heating the balance of cooled residual gas exiting the first heat exchange zone in a third indirect heat exchange zone with a second portion of the heated liquid heat transfer fluid stream to a temperature for feed to a Claus conversion stage; (d) passing the heated balance of the residual gas stream to at least one Claus conversion zone to form additional sulfur; and (e) combining liquid heat transfer fluid streams from the second and third indirect heat exchange zones and cooling the combined liquid heat transfer fluid streams for recycle to the process.

Claim 10

A process for the production of sulfur with control of process temperature by use of a liquid heat transfer fluid which comprises: (a) providing a closed loop heat transfer system containing a liquid heat transfer fluid; (b) condensing sulfur from a product gas stream containing sulfur, sulfur dioxide, and hydrogen sulfide by indirect heat exchange with cooled liquid heat transfer fluid stream in a first indirect heat exchange zone to provide a cooled residual gas comprising hydrogen sulfide and sulfur dioxide and a heated liquid heat transfer fluid stream, said product gas stream being formed by introducing to a catalytic selective oxidation zone, a feed gas heated, at least in part, for feed to said catalytic selective oxidation zone by indirect heat exchange with a first portion of the heated liquid heat transfer fluid stream in a second indirect heat exchange zone, said feed gas comprising an acid gas stream containing from about 1 to 100 percent by volume hydrogen sulfide in admixture with oxygen present in an amount of from about 70 to 130 percent of the stoichiometric amount required for oxidation of the hydrogen sulfide to elemental sulfur and a recycle gas which is a portion of a residual gas comprising hydrogen sulfide and sulfur dioxide resulting from condensation of sulfur from the effluent of the catalytic selective oxidation zone, at an inlet temperature of from about 270° F. to about 450° F. and contacting the feed gas with a selective oxidation catalyst capable of selectively oxidizing hydrogen sulfide to sulfur dioxide substantially without formation of sulfur trioxide, said catalyst comprising vanadium oxide and/or sulfide as an essential active ingredient supported on a non-alkaline porous refractory oxide, and catalytically converting introduced hydrogen sulfide to sulfur dioxide and sulfur below an outlet temperature of about 850° F., said outlet temperature controlled by the amount of recycle gas introduced to the catalytic selective oxidation zone; (c) indirectly heating the balance of cooled residual gas exiting the first heat exchange zone in a third indirect heat exchange zone with a second portion of the heated liquid heat transfer fluid stream to a temperature for feed to a Claus conversion stage; (d) passing the heated balance of the residual gas stream to at least one Claus conversion zone to form additional sulfur; and (e) combining liquid heat transfer fluid streams from the second and third indirect heat exchange zones and cooling the combined liquid heat transfer fluid streams for recycle to the process.

Claim 11

A process as claimed in claim 8 in which the catalyst comprises from about 1 to about 30 percent by weight of vanadium oxide and/or sulfide, calculated as the oxide, based on the weight of vanadium oxide and the non-alkaline porous refractory oxide support.

Claim 12

A process as claimed in claim 8 in which the catalyst comprises from about 1 to about 15 percent by weight vanadium oxide and/or sulfide, calculated as the oxide, based on the weight of vanadium oxide and the non-alkaline porous refractory oxide support.

Claim 13

A process as claimed in claim 8 in which the non-alkaline porous refractory oxide support is selected from the group consisting of alumina, titania, silica, silica-alumina, magnesia, silica-magnesia, zirconia, silica-zirconia, silica-titania, silica-zirconia-titania, acid metal phosphates, acid metal arsenates, crystalline or amorphous aluminosilicate hydrogen zeolites having a silica to alumina ratio between about 4:1 and 100:1, and mixtures thereof.

Claim 14

A process as claimed in claim 8 in which at least a portion of the vanadium is in the form of V 2 O 5 .

Claim 15

A process as claimed in claim 8 in which the upper reaction temperature is below about 700° F.

Claim 16

A process as claimed in claim 8 in which the amount of cooled residual gas returned to the catalytic selective oxidation zone is about 0.1 to about 10 moles per mole of acid gas feed.

Claim 17

A process as claimed in claim 8 in which the amount of oxygen introduced is about the stoichiometric amount required for conversion of hydrogen sulfide to sulfur.

Claim 18

A process as claimed in claim 8 in which the feed gas is introduced to the catalytic selective oxidation zone at a temperature from about 325° F. to about 400° F.

Claim 19

A process as claimed in claim 8 in which the oxygen is provided as air.

Claim 20

A process for the production of sulfur with control of process temperature by use of a liquid heat transfer fluid which comprises: (a) providing a closed loop heat transfer system containing a liquid heat transfer fluid; (b) condensing sulfur from a product gas stream containing sulfur, sulfur dioxide, and hydrogen sulfide by indirect heat exchange with cooled liquid heat transfer fluid stream in a first indirect heat exchange zone to provide a cooled residual gas comprising hydrogen sulfide and sulfur dioxide and a heated liquid heat transfer fluid stream, said product gas stream being formed by introducing to a catalytic selective oxidation zone, a feed gas heated, at least in part, for feed to said catalytic selective oxidation zone by indirect heat exchange with a first portion of the heated liquid heat transfer fluid stream in a second indirect heat exchange zone, said feed gas comprising an acid gas stream containing from 1 to about 100 percent by volume hydrogen sulfide in admixture with sufficient air to provide oxygen in an amount of from about 70 to 130 percent of the stoichiometric amount required for oxidation of the hydrogen sulfide to elemental sulfur and a recycle gas which is a portion of a residual gas comprising hydrogen sulfide and sulfur dioxide resulting from condensation of sulfur from the effluent of the catalytic selective oxidation zone, at an inlet temperature of from about 270° F. to about 450° F. and contacting the feed gas with a selective oxidation catalyst capable of selectively oxidizing hydrogen sulfide to sulfur dioxide substantially without formation of sulfur trioxide, said catalyst comprising vanadium oxide and/or sulfide as an essential ingredient deposited on a non-alkaline porous refractory oxide support, said support containing from about 1 to about 30 percent by weight of vanadium oxide and/or vanadium sulfide, calculated as vanadium oxide, based on the weight of the vanadium oxide and the support, said support selected from the group consisting of alumina, titania, silica, silica-alumina, magnesia, zirconia, silica-zirconia, silica-titania, silica-zirconia-titania, acid metal phosphates, and metal arsenates, crystalline or amorphous aluminosilicate hydrogen zeolites having a silica to alumina ratio between about 4:1 and 100:1 and mixtures thereof, and catalytically converting the introduced hydrogen sulfide to sulfur dioxide and sulfur at a temperature below about 850° F., maintained by the introduction of from about 0.1 to about 10 moles of recycle gas per mole of acid gas feed; (c) indirectly heating the balance of cooled residual gas exiting the first heat exchange zone in a third indirect heat exchange zone with a second portion of the heated liquid heat transfer fluid stream to a temperature for feed to a Claus conversion stage; (d) passing the heated balance of the residual gas stream to at least one Claus conversion zone to form additional sulfur; and (e) combining liquid heat transfer fluid streams from the second and third indirect heat exchange zones and cooling the combined liquid heat transfer fluid streams for recycle to the process.

Claim 21

A process for the production of sulfur with control of process temperature by use of a liquid heat transfer fluid which comprises: (a) providing a closed loop heat transfer system containing a liquid heat transfer fluid; (b) condensing sulfur from a product gas stream containing sulfur, sulfur dioxide, and hydrogen sulfide by indirect heat exchange with cooled liquid heat transfer fluid stream in a first indirect heat exchange zone to provide a cooled residual gas comprising hydrogen sulfide and sulfur dioxide and a heated liquid heat transfer fluid stream, said product gas stream being formed by introducing to a catalytic selective oxidation zone, a feed gas heated, at least in part, for feed to said catalytic selective oxidation zone by indirect heat exchange with a first portion of the heated liquid heat transfer fluid stream in a second indirect heat exchange zone, said feed gas comprising an acid gas stream containing from 1 to about 100 percent by volume hydrogen sulfide in admixture with sufficient air to provide oxygen in an amount of from about 70 to 130 percent of the stoichiometric amount required for oxidation of the hydrogen sulfide to elemental sulfur and a recycle gas which is a portion of a residual gas comprising hydrogen sulfide and sulfur dioxide resulting from condensation of sulfur from the effluent of the catalytic selective oxidation zone, at an inlet temperature of from about 270° F. to about 450° F. and contacting the feed gas with a selective oxidation catalyst capable of selectively oxidizing hydrogen sulfide to sulfur dioxide substantially without formation of sulfur trioxide, said catalyst comprising vanadium oxide and/or sulfide as an essential ingredient deposited on a non-alkaline porous refractory oxide support, said support containing from about 1 to about 30 percent by weight of vanadium oxide and/or vanadium sulfide, calculated as vanadium oxide, based on the weight of the vanadium oxide and the support, said support selected from the group consisting of alumina, titania, silica, silica-alumina, magnesia, zirconia, silica-zirconia, silica-titania, silica-zirconia-titania, acid metal phosphates, and metal arsenates, crystalline or amorphous aluminosilicate hydrogen zeolites having a silica to alumina ratio between about 4:1 and 100:1 and mixtures thereof, and catalytically converting the introduced hydrogen sulfide to sulfur dioxide and sulfur at a temperature below about 850° F., maintained by the introduction of from about 0.1 to about 10 moles of recycle gas per mole of acid gas feed; (c) indirectly heating the balance of cooled residual gas exiting the first heat exchange zone in a third indirect heat exchange zone with a second portion of the heated liquid heat transfer fluid stream to a temperature for feed to a Claus conversion stage; (d) passing the heated balance of the residual gas stream to at least one Claus conversion zone to form additional sulfur; and (e) combining liquid heat transfer fluid streams from the second and third indirect heat exchange zones and cooling the combined liquid heat transfer fluid streams for recycle to the process.

Claim 22

A process as claimed in claim 18 in which the catalyst comprises from about 1 to about 15 percent by weight vanadium oxide and/or sulfide, calculated as the oxide, based on the weight of vanadium oxide and the non-alkaline porous refractory oxide support.

Claim 23

A process as claimed in claim 18 in which at least a portion of the vanadium is in the form of V 2 O 5 .

Claim 24

A process as claimed in claim 18 in which the upper reaction temperature is below about 700° F.

Claim 25

A process as claimed in claim 18 in which the amount of oxygen introduced is about the stoichiometric amount required for conversion of hydrogen sulfide to sulfur.

Claim 26

A process as claimed in claim 18 in which the feed gas is introduced to the catalytic selective oxidation zone at a temperature from about 325° F. to about 400° F.

Claim 27

A process for the production of sulfur with control of process temperature by use of a heat transfer fluid which comprises: (a) providing a closed loop heat transfer system containing a liquid heat transfer fluid; (b) condensing sulfur from a product gas stream containing sulfur, sulfur dioxide, and hydrogen sulfide by indirect heat exchange with cooled heat transfer fluid stream in a first indirect heat exchange zone to provide a cooled residual gas comprising hydrogen sulfide and sulfur dioxide and a heated heat transfer fluid stream, said product gas stream being formed by contacting, in a catalytic selective oxidation zone, a feed gas heated, at least in part, for feed to said catalytic selective oxidation zone by indirect heat exchange with a first portion of the heated heat transfer fluid stream in a second indirect heat exchange zone, said feed gas comprising an acid gas stream containing from about 1 to 100 percent by volume hydrogen sulfide in admixture with oxygen present in an amount of from about 70 to 130 percent of the stoichiometric amount required for oxidation of the hydrogen sulfide to elemental sulfur and a recycle gas which is a portion of the cooled residual gas comprising hydrogen sulfide and sulfur dioxide exiting the first indirect heat exchange zone, with a selective oxidation catalyst capable of selectively oxidizing hydrogen sulfide to sulfur dioxide substantially without formation of sulfur trioxide and catalytically converting introduced hydrogen sulfide to sulfur dioxide and sulfur at a temperature above the kindling temperature of the catalyst and below an upper reaction temperature of about 850° F., the upper reaction temperature being selectively controlled by the amount of recycle gas introduced to the catalytic selective oxidation zone; (c) indirectly heating the balance of cooled residual gas exiting the first heat exchange zone in a third indirect heat exchange zone with a second portion of the heated heat transfer fluid stream to a temperature for feed to a Claus conversion stage; (d) passing the heated balance of the residual gas stream to at least one Claus conversion zone to form additional sulfur; and (e) combining heat transfer fluid streams from the second and third indirect heat exchange zones and cooling the combined heat transfer fluid streams for recycle to the process.

Claim 28

A process for the production of sulfur with control of process temperature by use of a heat transfer fluid which comprises: (a) providing a closed loop heat transfer system containing a liquid heat transfer fluid; (b) condensing sulfur from a product gas stream containing sulfur, sulfur dioxide, and hydrogen sulfide by indirect heat exchange with cooled heat transfer fluid stream in a first indirect heat exchange zone to provide a cooled residual gas comprising hydrogen sulfide and sulfur dioxide and a heated heat transfer fluid stream, said product gas stream being formed by contacting, in a catalytic selective oxidation zone, a feed gas heated, at least in part, for feed to said catalytic selective oxidation zone by indirect heat exchange with a first portion of the heated heat transfer fluid stream in a second indirect heat exchange zone, said feed gas comprising an acid gas stream containing from about 1 to 100 percent by volume hydrogen sulfide in admixture with oxygen present in an amount of from about 70 to 130 percent of the stoichiometric amount required for oxidation of the hydrogen sulfide to elemental sulfur and a recycle gas which is a portion of the cooled residual gas comprising hydrogen sulfide and sulfur dioxide exiting the first indirect heat exchange zone, with a selective oxidation catalyst capable of selectively oxidizing hydrogen sulfide to sulfur dioxide substantially without formation of sulfur trioxide and catalytically converting introduced hydrogen sulfide to sulfur dioxide and sulfur at a temperature above the kindling temperature of the catalyst and below an upper reaction temperature of about 850° F., the upper reaction temperature being selectively controlled by the amount of recycle gas introduced to the catalytic selective oxidation zone; (c) indirectly heating the balance of cooled residual gas exiting the first heat exchange zone in a third indirect heat exchange zone with a second portion of the heated heat transfer fluid stream to a temperature for feed to a Claus conversion stage; (d) passing the heated balance of the residual gas stream to at least one Claus conversion zone to form additional sulfur; and (e) combining heat transfer fluid streams from the second and third indirect heat exchange zones and cooling the combined heat transfer fluid streams for recycle to the process.

Claim 29

A process as claimed in claim 24 in which a portion of the cooled heat transfer fluid is utilized to condense sulfur from the effluent of at least a first Claus conversion zone following the catalytic selective oxidation zone by indirect heat exchange in a fourth heat exchange zone with the effluent of said first Claus conversion zone and combining the heat transfer fluid from the fourth heat exchange zone with the heat exchange fluids from the second and third heat exchange zones.

Claim 30

A process as claimed in claim 24 in which the upper reaction temperature is below about 700° F.

Claim 31

A process as claimed in claim 24 in which the catalyst comprises a vanadium oxide and/or sulfide supported on a non-alkaline porous refractory oxide.

Claim 32

A process as claimed in claim 27 in which the amount of oxygen introduced is about the stoichiometric amount required for conversion of hydrogen sulfide to sulfur.

Claim 33

A process as claimed in claim 1 in which a portion of the cooled liquid heat transfer fluid is utilized to condense sulfur from the effluent of at least a first Claus conversion zone following the catalytic selective oxidation zone by indirect heat exchange in a fourth heat exchange zone with the effluent of said first Claus conversion zone and combining the liquid heat transfer fluid from the fourth heat exchange zone with the liquid heat exchange fluids from the second and third heat exchange zones.

Claim 34

A process as claimed in claim 8 in which a portion of the cooled liquid heat transfer fluid is utilized to condense sulfur from the effluent of at least a first Claus conversion zone following the catalytic selective oxidation zone by indirect heat exchange in a fourth heat exchange zone with the effluent of said first Claus conversion zone and combining the liquid heat transfer fluid from the fourth heat exchange zone with the liquid heat exchange fluids from the second and third heat exchange zones.

Claim 35

A process as claimed in claim 18 in which a portion of the cooled liquid heat transfer fluid is utilized to condense sulfur from the effluent of at least a first Claus conversion zone following the catalytic selective oxidation zone by indirect heat exchange in a fourth heat exchange zone with the effluent of said first Claus conversion zone and combining the liquid heat transfer fluid from the fourth heat exchange zone with the liuqid heat exchange fluids from the second and third heat exchange zones.