초록 ▼

Recent experimental work with currently available adsorbents indicates that operating the adsorption section at lower temperatures improves the para-xylene productivity. As a result, an aromatics complex and heat recovery network for a low temperature adsorptive separation-isomerization loop is disc

Recent experimental work with currently available adsorbents indicates that operating the adsorption section at lower temperatures improves the para-xylene productivity. As a result, an aromatics complex and heat recovery network for a low temperature adsorptive separation-isomerization loop is disclosed resulting in adsorbents savings in combination with higher capacity thereby enabling smaller adsorbents chambers, a smaller total heat exchanger area and a lower heat exchanger shell count.

대표청구항 ▼

What is claimed: 1. A process for producing para-xylene from a feed stream comprising a mixture of C8 aromatic isomers and heavies, the method comprising: a) introducing a feed stream to a xylene fractionation zone to produce a xylenes enriched stream; b) cooling the xylenes enriched stream by tran

What is claimed: 1. A process for producing para-xylene from a feed stream comprising a mixture of C8 aromatic isomers and heavies, the method comprising: a) introducing a feed stream to a xylene fractionation zone to produce a xylenes enriched stream; b) cooling the xylenes enriched stream by transferring heat from the xylenes enriched stream to one or more of a first raffinate stream and an isomerization reactor product stream; c) introducing the xylenes enriched stream and a desorbent stream to a para-xylene separation zone and producing a first para-xylene enriched stream and the first raffinate stream from the xylenes enriched stream and desorbent stream; d) heating the first para-xylene enriched stream by transferring heat from the desorbent stream to the first para-xylene enriched stream and feeding the heated first para-xylene enriched stream into a distillation zone to produce a second para-xylene enriched stream and part of the desorbent stream; e) introducing the first raffinate stream to a raffinate column to produce another part of the desorbent stream and a second raffinate stream; f) heating the second raffinate stream by transferring heat from the isomerization reactor product stream to the second raffinate stream and feeding the heated second raffinate stream into an isomerization zone that converts the second raffinate stream to the isomerization reactor product stream; g) heating at least a portion of the isomerization reactor product stream by transferring heat from one or more of a para-xylene product stream, the xylenes enriched stream and the desorbent stream, to the isomerization reactor product stream; h) heating the second para-xylene enriched stream by transferring heat from the para-xylene product stream to the second para-xylene enriched stream; i) feeding the second para-xylene enriched stream to a finishing column to produce the para-xylene product stream. 2. The method of claim 1, further comprising feeding the isomerization reactor product stream to a deheptanizer column to produce a light overhead stream and a second feed stream; feeding the second feed stream to the xylene separation zone with the feed stream. 3. The method of claim 2, further comprising combining the part of the desorbent stream from the raffinate column and the part of the desorbent stream from the distillation zone to produce the desorbent stream; and wherein the isomerization reactor product stream is heated prior to being fed to the deheptanizer column by transferring heat to the isomerization reactor product stream from the desorbent stream. 4. The method of claim 3, wherein the isomerization reactor product stream is also heated by transferring heat from the para-xylene product stream and the xylenes enriched stream to the isomerization reactor product stream. 5. The method of claim 1, wherein the transfer of heat from the xylenes enriched stream to the first raffinate stream of part (b) is carried out in a first heat exchanger. 6. The method of claim 5, wherein the transfer of heat from the xylenes enriched stream to the deheptanizer stream of part (b) is carried out in a second heat exchanger. 7. The method of claim 6, wherein the transfer of heat from the desorbent stream to the first para-xylene enriched stream of part (d) is carried out in a third heat exchanger. 8. The method of claim 7, wherein the transfer heat from the isomerization reactor product stream to the second raffinate stream of part (f) is carried out in a fourth heat exchanger. 9. The method of claim 1, wherein the heating of the isomerization reactor product stream by transferring heat from the para-xylene product stream to the isomerization reactor product stream of part (g) is carried out in a fifth heat exchanger. 10. The method of claim 9, wherein the heating of the isomerization reactor product stream by transferring heat from the desorbent stream to the isomerization reactor product stream of part (g) is carried out in a sixth heat exchanger. 11. The method of claim 10, wherein the heating of the second para-xylene enriched stream by transferring heat from the para-xylene product stream to the second para-xylene enriched stream of part (h) is carried out in a seventh heat exchanger. 12. The method of claim 1 wherein the xylenes enriched stream is cooled in part (b) to a temperature ranging from about 121° C. to about 204° C. prior to being introduced to the para-xylene separation zone in part (c). 13. The method of claim 1 wherein the feed comprises a reformate splitter bottoms stream. 14. The method of claim 1 wherein the feed comprises a combination of a reformate splitter bottoms stream and a toluene column bottoms stream. 15. The method of claim 14 wherein the reformate splitter bottoms stream and toluene column bottoms stream have each been passed through a clay treater prior to being introduced to the xylene fractionation zone. 16. The method of claim 1 further comprising passing the second raffinate stream through a heater prior to feeding the second raffinate stream to an isomerization zone. 17. The method of claim 1 further comprising passing the isomerization reactor product stream through a cooler prior to feeding the isomerization reactor product stream to an effluent separator that produces an effluent recycle stream and a deheptanizer feed stream. 18. A process for producing para-xylene from a feed stream comprising a mixture of C8 aromatic isomers and heavies, the method comprising: introducing a first feed stream to a xylene fractionation zone to produce a xylenes enriched stream; cooling the xylenes enriched stream to a temperature of between about 155° C. and about 182° C. in a first heat exchanger by transferring heat from the xylenes enriched stream to a raffinate stream and further cooling the xylenes enriched stream in a second heat exchanger by transfer ring heat from the xylenes enriched stream to a cooled isomerization reactor product stream; feeding the xylenes enriched stream and a desorbent stream to a para-xylene separation zone to produce a first para-xylene enriched stream and the raffinate stream from the xylenes enriched stream and desorbent stream; heating the first para-xylene enriched stream in a third heat exchanger by transferring heat from the desorbent stream to the first para-xylene enriched stream and feeding the heated first para-xylene enriched stream to a distillation column to produce a second para-xylene enriched stream; heating the raffinate stream in a fourth heat exchanger by transferring heat from an isomerization effluent stream to the second raffinate stream and feeding the heated raffinate stream to an isomerization reactor that converts the raffinate stream to the isomerization reactor product stream; cooling the isomerization reactor product stream in the fourth heat exchanger before heating at least a portion of the isomerization reactor product stream in a fifth heat exchanger by transferring heat from a para-xylene product stream to the isomerization reactor product stream, further heating at least a portion of the isomerization reactor, product stream in the second heat exchanger by transferring heat from the xylenes enriched stream to the isomerization reactor product stream and still further heating at least a portion of the isomerization reactor product stream in a sixth heat exchanger by transferring heat from the desorbent stream to the isomerization reactor product stream; heating the second para-xylene enriched stream in a seventh heat exchanger by transferring heat from the para-xylene product stream to the second para-xylene enriched stream; feeding the second para-xylene enriched stream to a finishing column to produce the para-xylene product stream. 19. The method of claim 18 the xylenes enriched stream is cooled to a temperature ranging from about 150° C. to about 170° C. prior to being fed to the para-xylene separation zone. 20. A process for producing para-xylene from a feed stream comprising a mixture of C8 aromatic isomers and heavies, the method comprising: feeding first and second feed streams to a xylene fractionation zone to produce a xylenes enriched stream and first bottoms stream; cooling the xylenes enriched stream in a first heat exchanger by transferring heat from the xylenes enriched stream to a first raffinate stream; further cooling the xylenes enriched stream to a temperature in the range of from about 150 to about 170° C. in a second heat exchanger by transferring heat from the xylenes enriched stream to a deheptanizer feet stream; feeding the xylenes enriched stream and a combined desorbent stream to a para-xylene separation zone to produce a first para-xylene enriched stream and the first raffinate stream from the xylenes enriched stream and combined desorbent stream; heating the first para-xylene enriched stream in a third heat exchanger by transferring heat from the combined desorbent stream to the first para-xylene enriched stream and feeding the heated first para-xylene enriched stream into a distillation column to produce a second para-xylene enriched stream and a first desorbent stream; feeding the first raffinate stream, after it has been heated in the first heat exchanger, to a raffinate column to produce a second desorbent stream and a second raffinate stream; combining the first and second desorbent streams to produce the combined desorbent stream; heating the second raffinate stream in a fourth heat exchanger by transferring heat from an isomerization reaction product stream to the second raffinate stream and feeding the heated second raffinate stream into an isomerization reactor that converts the second raffinate stream to the isomerization reaction product stream; cooling the isomerization reaction product stream in the fourth heat exchanger before feeding the cooled isomerization reaction product stream to an effluent separator to produce an effluent recycle stream and the deheptanizer feed stream; combining the effluent recycle stream and second raffinate stream upstream of the fourth heat exchanger; heating the deheptanizer feed stream in a fifth heat exchanger by transferring heat from a para-xylene product stream to the deheptanizer feed stream, further heating the deheptanizer feed stream in the second heat exchanger by transferring heat from the xylenes enriched stream to the deheptanizer feed stream and still further heating the deheptanizer feed stream in a sixth heat exchanger by transferring heat from the combined desorbent stream to the deheptanizer feed stream; feeding the deheptanizer feed stream to a deheptanizer column to produce a light overhead stream and the second feed stream; heating the second para-xylene enriched stream in a seventh heat exchanger by transferring heat from the para-xylene product stream to the second para-xylene enriched stream; feeding the second para-xylene enriched stream to a finishing column to produce the para-xylene product stream and a toluene enriched stream.