Low emissions oxidative dehydrogenation process for producing butadiene
Butadiene is formed by dehydrogenation of butenes which are mixed with steam and oxygen then converted to butadiene by oxidative dehydrogenation over a ferritic oxide catalyst, wherein the sensible heat in the oxidative dehydrogenation reaction product is utilized along with heat produced by thermal oxidation of low value volatile products formed to reduce energy requirements and CO 2 emissions. Sensible heat is utilized at high temperature for purposes of superheating feed and at somewhat lower temperatures for purposes of vaporizing feed at sequential locations in the process.
1. An improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene, wherein the improvement comprises the steps of:
vaporizing said hydrocarbonaceous butene rich feed, mixing the vaporized hydrocarbonaceous butene rich feed with steam to produce a combined stream, and superheating the combined stream to provide a reactor feed stream;
oxidatively dehydrogenating said reactor feed stream with an oxygen rich gas over a ferritic catalyst, thereby forming a butadiene enriched product stream, wherein the temperature of the butadiene enriched product stream is at least about 510° C. (950° F.);
passing the butadiene enriched product stream at a temperature of at least about 510° C. (950° F.) first through a reactor feed superheater in which the reactor feed stream is superheated by indirect heat exchange with said butadiene enriched product stream to at least 345° C. (650° F.);
passing the butadiene enriched product stream exiting said reactor feed superheater through a steam generator in which water is vaporized by indirect heat exchange with said butadiene enriched product stream exiting said reactor feed superheater to provide vaporized and/or superheated steam;
passing the butadiene enriched product stream exiting said steam generator through a C4 absorber, wherein C4 compounds including butadiene are absorbed in an absorption oil,
passing the absorption oil through: (i) a degasser tower in which non-C4 volatiles are removed and (ii) a C4 stripper in which C4 compounds including butadiene are desorbed/stripped from said absorption oil under reduced pressure,
passing the non-C4 volatiles to a thermal oxidizer to generate steam, wherein the steam from the thermal oxidizer is used to supply heat to the reactor feed stream,
stripping aqueous liquid from the butadiene enriched product stream to provide an aqueous stream containing dispersed volatile organics,
stripping the dispersed volatile organics from the aqueous stream to produce a resultant aqueous stream, wherein the resultant aqueous stream is recycled to the steam generator;
such that in steady operation, the energy content of said butadiene enriched product stream supplies at least 40% of the energy needed for:
vaporizing and superheating said hydrocarbonaceous butene rich feed; and
vaporizing and superheating the water used to supply superheated steam in said reactor feed stream.
2. The improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene of claim 1 , wherein the heat required to vaporize water supplied to the steam generator is supplied at least in part by heat generated by thermal oxidation of the non-C4 volatiles separated from the butadiene enriched product stream.
3. The improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene of claim 1 , wherein the ferritic catalyst is a ferritic oxide catalyst consisting essentially of: oxygen, a major proportion of iron, a minor proportion of zinc, manganese, phosphorus, and the residue of a nitrate free calcium precursor.
4. The improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene of claim 1 , wherein during steady operation, the energy content of said butadiene enriched product stream supplies at least 45% of the energy required for:
vaporizing and superheating said hydrocarbonaceous butene rich feed; and
vaporizing and superheating the water used to supply superheated steam in said reactor feed stream.
5. The improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene of claim 1 , wherein during steady operation, the energy content of said butadiene enriched product stream supplies at least 50% of the energy required for:
vaporizing and superheating said hydrocarbonaceous butene rich feed; and
vaporizing and superheating the water used to supply superheated steam in said reactor feed stream.
6. The improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene of claim 1 , wherein the energy content of said butadiene enriched product stream supplies such a proportion of the energy required for:
(a) vaporizing and superheating said hydrocarbonaceous butene rich feed; and
(b) vaporizing and superheating the water used to supply superheated steam in said reactor feed stream,
that less than 0.35 kg of natural gas is consumed in steps (a) and (b) for each kg of butadiene produced.
7. The improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene of claim 1 , wherein the energy content of said butadiene enriched product stream supplies such a proportion of the energy required for:
(a) vaporizing and superheating said hydrocarbonaceous butene rich feed; and
(b) vaporizing and superheating the water used to supply superheated steam in said reactor feed stream,
that less than 0.3 kg of natural gas is consumed in steps (a) and (b) for each kg of butadiene produced.
8. The improved low emissions method of converting a hydrocarbonaceous butene rich feed into butadiene of claim 1 , wherein the energy content of said butadiene enriched product stream supplies such a proportion of the energy required for:
(a) vaporizing and superheating said hydrocarbonaceous butene rich feed; and
(b) vaporizing and superheating the water used to supply superheated steam in said reactor feed stream,
that less than 0.25 kg of natural gas is consumed in steps (a) and (b) for each kg of butadiene produced.
9. An improved low emissions method of manufacturing butadiene by oxidative dehydrogenation of a hydrocarbonaceous butene rich feed, wherein the improvement comprises the steps of:
vaporizing said hydrocarbonaceous butene rich feed, mixing the vaporized hydrocarbonaceous butene rich feed with superheated steam and an oxygen rich gas to form a reactor feed stream, superheating said reactor feed stream to a temperature of at least 345° C. (650° F.);
oxidatively dehydrogenating said reactor feed stream over a ferritic oxide catalyst, thereby forming a butadiene enriched product stream, wherein the temperature of the butadiene enriched product stream is at least about 510° C. (950° F.);
passing the butadiene enriched product stream at a temperature of at least about 510° C. (950° F.) first through a reactor feed superheater in which the reactor feed stream is superheated by indirect heat exchange with said butadiene enriched product stream to at least 345° C. (650° F.);
passing the butadiene enriched product stream exiting said reactor feed superheater through a steam generator in which water is vaporized by indirect heat exchange with said butadiene enriched product stream exiting said reactor feed superheater to provide vaporized and/or superheated steam;
passing the butadiene enriched product stream exiting said steam generator through a quench tower, a compressor, an aldehyde scrubber, and a C4 absorber, wherein butadiene and C4 compounds are absorbed into an absorption oil,
passing an overhead from said C4 absorber to a thermal oxidizer to generate steam, wherein the steam from the thermal oxidizer is used to supply heat used in the method;
passing the absorption oil to: (i) a degasser tower wherein residual nitrogen, hydrogen, and carbon dioxide are removed from the absorption oil and (ii) a C4 stripper wherein butadiene and the C4 compounds are stripped from the absorption oil and recovered as a crude butadiene product stream,
stripping aqueous liquid from the butadiene enriched product stream to provide an aqueous stream containing dispersed volatile organics,
stripping the dispersed volatile organics from the aqueous stream to produce a resultant aqueous stream, wherein at various stages of the method the resultant aqueous stream is provided to the steam generator;
wherein, during steady operation, any additional heat required to:
vaporize and superheat said hydrocarbonaceous butene rich feed; and
vaporize and superheat the water used to supply superheated steam in said reactor feed stream;
is no more than 130% of the sum of (1) the sensible heat extracted from the butadiene enriched product stream and (2) the heat generated by thermal oxidation of the overhead from the C4 absorber separated from the butadiene enriched product stream.
10. The improved low emissions method of manufacturing butadiene by oxidative dehydrogenation of a hydrocarbonaceous butene rich feed of claim 9 , wherein any additional energy required for conversion of said hydrocarbonaceous butene rich feed into said butadiene enriched product stream is no more than 110% of the sum of: (1) the sensible heat extracted from the butadiene enriched product stream and (2) the heat generated by thermal oxidation of the overhead from the C4 absorber separated from the butadiene enriched product stream.
11. In a process for producing butadiene by converting butenes from a butene rich feed stream into butadiene by oxidatively dehydrogenating said butenes in a reaction system which includes a superheater for superheating feed and one or more steam generators for vaporizing water, the improvement comprising:
(a) reacting said butene rich feed stream in an oxidative dehydrogenation reactor to form a butadiene enriched product effluent stream which exits said oxidative dehydrogenation reactor;
(b) feeding said butadiene enriched product effluent stream to a feed superheater, wherein the butadiene enriched product effluent stream is provided to the feed superheater at a temperature of 425° C. (800° F.) or more, oxidative dehydrogenation reactor feed also being provided to the feed superheater;
(c) superheating the oxidative dehydrogenation reactor feed in the feed superheater to a temperature of at least 260° C. (500° F.) with indirect heat transfer of sensible heat from the butadiene enriched product effluent stream to the oxidative dehydrogenation reactor feed;
(d) subsequent to step (c), feeding the butadiene enriched product effluent stream exiting the feed superheater to a steam generator, wherein the butadiene enriched product effluent stream entering the steam generator is at a temperature of at least 205° C. (400° F.); and
(e) vaporizing water in the steam generator with indirect heat transfer of sensible heat from the butadiene enriched product effluent stream to the water.
12. The improvement according to claim 11 , wherein the butadiene enriched product effluent stream is provided to the feed superheater at a temperature of from 480° C. to 760° C. (900° F. to 1400° F.).
13. The improvement according to claim 11 , wherein the butadiene enriched product effluent stream is provided to the steam generator at a temperature of at least 290° C. (550° F.).
14. The improvement according to claim 11 , wherein at least 2300 kJ/kg (1000 BTU/LB) butadiene produced is transferred from the butadiene enriched product effluent stream to the oxidative dehydrogenation reactor feed in the feed superheater by indirect heat exchange.
15. The improvement according to claim 11 , wherein from 2300 to 5800 kJ/kg (1000 to 2500 BTU/LB) butadiene produced is transferred from the butadiene enriched product effluent stream to the oxidative dehydrogenation reactor feed in the feed superheater by indirect heat exchange and from 2300 to 7000 kJ/kg (1000 to 3000 BTU/LB) butadiene produced is transferred from the butadiene enriched product effluent stream to the water in the steam generator by indirect heat exchange.