JP2018536035A - 産業施設における廃エネルギーの回収及び再利用 - Google Patents
産業施設における廃エネルギーの回収及び再利用 Download PDFInfo
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- JP2018536035A JP2018536035A JP2018510744A JP2018510744A JP2018536035A JP 2018536035 A JP2018536035 A JP 2018536035A JP 2018510744 A JP2018510744 A JP 2018510744A JP 2018510744 A JP2018510744 A JP 2018510744A JP 2018536035 A JP2018536035 A JP 2018536035A
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- heat exchanger
- stream
- plant
- aromatic hydrocarbon
- heated
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Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
- F28D7/0083—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids with units having particular arrangement relative to a supplementary heat exchange medium, e.g. with interleaved units or with adjacent units arranged in common flow of supplementary heat exchange medium
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
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- B01D51/10—Conditioning the gas to be cleaned
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- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
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- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
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- B01D53/343—Heat recovery
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- C07C7/04—Purification; Separation; Use of additives by distillation
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Abstract
Description
602 硫黄回収プラント
604 ガス分離プラント
606 アミン再生プラント
608 天然ガススチーム改質水素プラント
610 サワーウォータストリッパプラント
618 芳香族炭化水素複合施設ベンゼン抽出ユニット
620 芳香族炭化水素複合施設キシレン生成物分離ユニット
1〜9 第1〜9の熱交換器
Claims (32)
- 原油精製施設で実施される方法であって:
複数の油精製プラントであって、それぞれが少なくとも1つの油精製プロセスを実行するように構成され、それぞれが複数の相互接続した油精製サブシステムを備える油精製プラントを備え、それぞれの温度の複数のストリームが前記複数の油精製サブシステム間を流れる原油精製施設において:
ガス分離プラントストリーム、酸性ガス再生塔底ストリーム、及び芳香族炭化水素複合施設ストリームを、前記複数の油精製プラントのガス分離プラント、アミン再生プラント、及び芳香族炭化水素複合施設から1つ以上の熱交換器へ流すステップと;
芳香族炭化水素複合施設ストリームを、前記複数の油精製プラントの芳香族炭化水素複合施設から前記1つ以上の熱交換器へ流すステップであって、前記1つ以上の熱交換器は、前記ガス分離プラントストリーム、前記酸性ガス再生塔底ストリーム、及び前記芳香族炭化水素複合施設ストリームのうちの少なくとも1つから前記芳香族炭化水素複合施設ストリームへ熱を伝達する、芳香族炭化水素複合施設ストリームを、前記複数の油精製プラントの芳香族炭化水素複合施設から前記1つ以上の熱交換器へ流すステップと;
前記芳香族炭化水素複合施設ストリームで、前記加熱された芳香族炭化水素複合施設ストリームを、油精製プロセスに利用するステップと;
を備える、
方法。 - 前記第1の複数のプラントは、ガス分離プラント、アミン再生プラント、硫黄回収プラント、サワーウォータストリッパプラント、及び芳香族炭化水素複合施設を備え、
前記第2の複数のプラントは、芳香族炭化水素複合施設キシレン生成物分離ユニットを備える前記芳香族炭化水素複合施設、芳香族炭化水素複合施設ベンゼン抽出ユニット、ディーゼル水素処理プラントストリッパ区画、及び水素プラント反応区画を備える、
請求項1の方法。 - 前記1つ以上の熱交換器が:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内のラフィネート塔頂ストリームの第1の分岐を用いて、酸性ガス再生塔底ストリームを加熱するステップと;
第2の熱交換器において、前記ラフィネート塔頂ストリームの第2の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット複合施設内のベンゼン塔底ストリームを加熱するステップと;
第3の熱交換器において、前記ラフィネート塔頂ストリームの第3の分岐を用いて、前記芳香族炭化水素複合施設内のラフィネートスプリッタ塔底ストリームを加熱するステップと;
第4の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第1の分岐を用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第5の熱交換器において、前記芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第2の分岐を用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
前記加熱された酸性ガス再生塔底ストリームを、前記アミン再生プラントへ流すステップと;
前記加熱されたベンゼン塔底低温ストリームを、前記芳香族炭化水素複合施設内の前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップ;
前記加熱されたラフィネートスプリッタ塔底ストリームを、前記芳香族炭化水素複合施設内の前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
前記加熱されたC3/C4スプリッタ塔底ストリームと、前記加熱された脱エタン塔底ストリームとを、前記ガス分離プラントへ流すステップと;
によって直接的に熱を伝達する、
請求項2の方法。 - 前記第1の熱交換器、前記第2の熱交換器及び前記第3の熱交換器が流体的に互いに並列に連結され、前記第4の熱交換器及び前記第5の熱交換器が流体的に互いに並列に連結される、
請求項3の方法。 - 前記1つ以上の熱交換器が:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内のラフィネート塔頂ストリームの第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
第2の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の前記ラフィネート塔頂ストリームの第2の分岐を用いて、前記サワーウォータストリッパプラント内のサワーウォータストリッパ塔底ストリームを加熱するステップと;
第3の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の前記ラフィネート塔頂ストリームの第3の分岐を用いて、アミン再生塔底ストリームを加熱するステップと;
第4の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のラフィネートスプリッタ塔底ストリームを加熱するステップと;
第5の熱交換器において、前記芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第2の分岐を用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第6の熱交換器において、前記芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第3の分岐を用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
前記加熱されたベンゼン塔底ストリームと、前記加熱されたラフィネートスプリッタ塔底ストリームとを、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
前記加熱されたサワーウォータストリッパ塔底ストリームを前記サワーウォータストリッパプラントへ流すステップ;
前記加熱されたアミン再生塔底ストリームを前記硫黄回収プラントへ流すステップと;
前記加熱されたC3/C4スプリッタ塔底ストリームと、前記加熱された脱エタン塔底ストリームとを、前記ガス分離プラントへ流すステップと;
によって直接的に熱を伝達する、
請求項2の方法。 - 前記第1の熱交換器、前記第2の熱交換器及び前記第3の熱交換器が流体的に互いに並列に連結され、前記第4の熱交換器、前記第5の熱交換器及び前記第6の熱交換器が流体的に互いに並列に連結される、
請求項5の方法。 - 前記1つ以上の熱交換器が:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内のラフィネート塔頂ストリームの第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
第2の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の前記ラフィネート塔頂ストリームの第2の分岐を用いて、前記アミン再生プラント内の酸性ガス再生塔底ストリームを加熱するステップと;
第3の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の前記ラフィネート塔頂ストリームの第3の分岐を用いて、前記硫黄回収プラント内の硫黄回収塔底低温ストリームを加熱するステップと;
第4の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のラフィネートスプリッタ塔底ストリームを加熱するステップと;
第5の熱交換器において、前記芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第2の分岐を用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第6の熱交換器において、前記芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第3の分岐を用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
前記加熱されたベンゼン塔底ストリームと、前記加熱されたラフィネートスプリッタ塔底ストリームとを、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
前記加熱された酸性ガス再生塔底ストリームを前記アミン再生プラントへ流すステップと;
前記加熱された硫黄回収塔底低温ストリームを、前記硫黄回収プラントのストリームへ流すステップと;
前記加熱されたC3/C4スプリッタ塔底ストリームと、前記加熱された脱エタン塔底ストリームとを前記ガス分離プラントへ流すステップと;
によって直接的に熱を伝達する、
請求項2の方法。 - 前記第1の熱交換器、前記第2の熱交換器及び前記第3の熱交換器は流体的に互いに並列に連結され、前記第4の熱交換器、前記第5の熱交換器及び前記第6の熱交換器は流体的に互いに並列に連結される、
請求項7の方法。 - 前記1つ以上の熱交換器が:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームの第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
第2の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームの第2の分岐を用いて、前記サワーウォータストリッパプラント内のサワーウォータストリッパ塔底低温ストリームを加熱するステップと;
第3の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームの第3の分岐を用いて、前記アミン再生プラント内の酸性ガス再生塔底ストリームを加熱するステップと;
第4の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第1の分岐を用いて、前記硫黄回収プラント内のアミン再生塔底低温ストリームを加熱するステップと;
第5の熱交換器において、前記芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第2の分岐を用いて、ラフィネートスプリッタ塔底ストリームを加熱するステップと;
第6の熱交換器において、前記水素プラント内の低温シフト(LTS)後水素プラントストリームを用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第7の熱交換器において、前記第6の熱交換器を出るLTS後水素プラントストリームを用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
前記加熱されたベンゼン塔底ストリームと、前記加熱されたラフィネートスプリッタ塔底ストリームとを、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
前記加熱されたサワーウォータストリッパ塔底低温ストリームを前記サワーウォータストリッパプラントへ流すステップと;
前記加熱された酸性ガス再生塔底ストリームを前記アミン再生プラントへ流すステップと;
前記加熱されたアミン再生塔底低温ストリームを前記硫黄回収プラントのストリームへ流すステップと;
前記加熱されたC3/C4スプリッタ塔底ストリームと、前記加熱された脱エタン塔底ストリームとを前記ガス分離プラントへ流すステップと;
によって直接的に熱を伝達する、
請求項2の方法。 - 前記第1の熱交換器、前記第2の熱交換器及び前記第3の熱交換器が流体的に互いに並列に連結され、前記第4の熱交換器及び前記第5の熱交換器が流体的に互いに並列に連結され、前記第6の熱交換器及び前記第7の熱交換器が流体的に互いに直列に連結される、
請求項9の方法。 - 前記1つ以上の熱交換器が:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームの第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
第2の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームの第2の分岐を用いて、前記サワーウォータストリッパプラント内のサワーウォータストリッパ塔底低温ストリームを加熱するステップと;
第3の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームの第3の分岐を用いて、前記アミン再生プラント内の酸性ガス再生塔底ストリームを加熱するステップと;
第4の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第1の分岐を用いて、前記硫黄回収プラント内のアミン再生塔底低温ストリームを加熱するステップと;
第5の熱交換器において、前記芳香族炭化水素複合施設キシレン分離区画抽出塔頂ストリームの第2の分岐を用いて、ラフィネートスプリッタ塔底ストリームを加熱するステップと;
第6の熱交換器において、前記ディーゼル水素処理プラント内の生成物ストリッパ塔底留分ストリームを用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第7の熱交換器において、前記第6の熱交換器から受け入れた前記ディーゼル水素処理プラント内の前記生成物ストリッパ塔底留分ストリームを用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
前記加熱されたベンゼン塔底ストリームと、前記加熱されたラフィネートスプリッタ塔底ストリームとを、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
前記加熱されたサワーウォータストリッパ塔底低温ストリームを、前記サワーウォータストリッパプラントへ流すステップと;
前記加熱された酸性ガス再生塔底ストリームを、前記アミン再生プラントへ流すステップと;
前記加熱されたアミン再生塔底低温ストリームを、前記硫黄回収プラントのストリームへ流すステップと;
前記加熱されたC3/C4スプリッタ塔底ストリームと、前記加熱された脱エタン塔底ストリームとを、前記ガス分離プラントへ流すステップと;
によって直接的に熱を伝達する、
請求項2の方法。 - 前記第1の熱交換器、前記第2の熱交換器及び前記第3の熱交換器が流体的に互いに並列に連結され、前記第4の熱交換器及び前記第5の熱交換器が流体的に互いに並列に連結され、前記第6の熱交換器及び前記第7の熱交換器が流体的に互いに直列に連結される、
請求項11の方法。 - 前記1つ以上の熱交換器が、緩衝流体を介し:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームを用いて、前記緩衝流体を加熱するステップと;
前記加熱された緩衝流体の第1の分岐を前記アミン再生プラントへ流すステップと;
第2の熱交換器において、前記加熱された緩衝流体の前記第1の分岐を用いて、前記アミン再生プラント内の酸性ガス再生塔底ストリームを加熱するステップと;
前記加熱された緩衝流体の第2の分岐を、前記芳香族炭化水素複合施設へ流すステップと;
第3の熱交換器において、前記加熱された緩衝流体の前記第2の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
前記第3の熱交換器を出る前記第2の分岐を、前記芳香族炭化水素複合施設へ流すステップと;
第4の熱交換器において、前記第3の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐を用いて、前記芳香族炭化水素複合施設内のラフィネートスプリッタ塔底ストリームを加熱するステップと;
前記第4の熱交換器を出る前記第2の分岐を、前記ガス分離プラントへ流すステップと;
第5の熱交換器において、前記第4の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐を用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
前記第2の分岐を前記ガス分離プラント内の第6の熱交換器へ流すステップと;
前記第6の熱交換器において、前記第5の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐を用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
によって間接的に熱を伝達する、
請求項2の方法。 - 前記第1の熱交換器及び前記第2の熱交換器が流体的に互いに直列に連結され、前記第1の熱交換器及び前記第3の熱交換器が流体的に互いに直列に連結され、前記第3の熱交換器及び前記第4の熱交換器が流体的に互いに直列に連結され、前記第4の熱交換器及び前記第5の熱交換器が流体的に互いに直列に連結され、前記第4の熱交換器及び前記第6の熱交換器が流体的に互いに直列に連結され、前記第2の熱交換器と、前記第3の熱交換器、前記第4の熱交換器、前記第5の熱交換器及び前記第6の熱交換器の組み合わせとが流体的に互いに並列に連結される、
請求項13の方法。 - 前記第1の分岐と前記第2の分岐とが並列に流され、
前記方法は:
前記第2の熱交換器を出る前記第1の分岐と前記第6の熱交換器を出る前記第2の分岐とを合流させるステップと;
前記合流された前記第1の分岐と前記第2の分岐を緩衝流体タンクへ流すステップと;
を更に備える、
請求項13の方法。 - 前記1つ以上の熱交換器が、緩衝流体を介し:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームを用いて、前記緩衝流体を加熱するステップと;
前記第1の熱交換器を出る前記加熱された緩衝流体を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第2の熱交換器において、前記第1の熱交換器を出る前記加熱された緩衝流体を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
前記第2の熱交換器を出る前記加熱された緩衝流体の第1の分岐を、前記サワーウォータストリッパプラントへ流すステップと;
第3の熱交換器において、前記第2の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を用いて、前記サワーウォータストリッパプラント内のサワーウォータストリッパ塔底ストリームを加熱するステップと;
前記第2の熱交換器を出る前記加熱された緩衝流体の第2の分岐を、前記硫黄回収プラントへ流すステップと;
第4の熱交換器において、前記第2の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐を用いて、前記硫黄回収プラント内のアミン再生塔底ストリームを加熱するステップと;
前記第3の熱交換器を出る前記緩衝流体と、前記第4の熱交換器を出る緩衝流体とを合流させて、合流された緩衝流体を形成するステップと;
前記合流された緩衝流体を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第5の熱交換器において、前記合流された緩衝流体を用いて、ラフィネートスプリッタ塔底ストリームを加熱するステップと;
前記第5の熱交換器を出る前記合流された緩衝流体を前記ガス分離プラントへ流すステップと;
第6の熱交換器において、前記第5の熱交換器を出て前記ガス分離プラントへ入る前記緩衝流体を用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第7の熱交換器において、前記第6の熱交換器を出る前記加熱された緩衝流体を用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
によって間接的に熱を伝達する、
請求項2の方法。 - 前記第1の熱交換器及び前記第2の熱交換器が流体的に互いに直列に連結され、前記第2の熱交換器及び前記第3の熱交換器が流体的に互いに直列に連結され、前記第2の熱交換器及び前記第4の熱交換器が流体的に互いに直列に連結され、前記第3の熱交換器及び前記第4の熱交換器が流体的に互いに並列に連結され、前記第5の熱交換器が前記第3の熱交換器と前記第4の熱交換器との組み合わせに直列に流体的に連結され、前記第5の熱交換器及び前記第6の熱交換器が流体的に互いに直列に連結され、前記第6の熱交換器及び前記第7の熱交換器が流体的に互いに直列に連結される、
請求項16の方法。 - 前記第7の熱交換器を出る前記緩衝流体を緩衝流体タンクへ流すステップを更に備える、
請求項17の方法。 - 前記1つ以上の熱交換器が、緩衝流体を介し:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームを用いて、前記緩衝流体の第1の分岐を加熱するステップと;
前記第1の熱交換器を出る前記加熱された第1の分岐を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第3の熱交換器において、前記加熱された第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
前記第3の熱交換器を出る前記緩衝流体の前記第1の分岐を前記硫黄回収プラントへ流すステップと;
第4の熱交換器において、前記第3の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を用いて、前記硫黄回収プラント内のアミン再生塔底ストリームを加熱するステップと;
前記第4の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を、前記アミン再生プラントへ流すステップと;
第5の熱交換器において、前記第4の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を用いて、酸性ガス再生塔底ストリームを加熱するステップと;
によって間接的に熱を伝達する、
請求項2の方法。 - 前記1つ以上の熱交換器が、緩衝流体を介し:
第2の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の抽出塔頂ストリームを用いて、前記緩衝流体の第2の分岐を加熱するステップと;
前記第2の熱交換器を出る前記加熱された第2の分岐を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第6の熱交換器において、前記加熱された第2の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のラフィネートスプリッタ塔底ストリームを加熱するステップと;
前記第6の熱交換器を出る前記加熱された第2の分岐を、前記ガス分離プラントへ流すステップと;
第7の熱交換器において、前記第6の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐を用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第8の熱交換器において、前記第7の熱交換器を出る前記加熱された緩衝流体を用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
によって間接的に熱を伝達する、
請求項19の方法。 - 前記第5の熱交換器を出る前記加熱された緩衝流体と、前記第8の熱交換器を出る前記加熱された緩衝流体とを、緩衝流体タンクへ流すステップを更に備える、
請求項20の方法。 - 前記第1の熱交換器及び前記第3の熱交換器が流体的に互いに直列に連結され、前記第3の熱交換器及び前記第4の熱交換器が流体的に互いに直列に連結され、前記第4の熱交換器及び前記第5の熱交換器が流体的に互いに直列に連結され、前記第2の熱交換器及び前記第6の熱交換器が流体的に互いに並列に連結され、前記第6の熱交換器と、前記第3の熱交換器、前記第4の熱交換器及び前記第5の熱交換器の組み合わせとが流体的に互いに並列に連結され、前記第6の熱交換器及び前記第7の熱交換器が流体的に互いに直列に連結され、前記第7の熱交換器及び前記第8の熱交換器が流体的に互いに直列に連結され、前記第6の熱交換器、前記第7の熱交換器及び前記第8の熱交換器の組み合わせと、前記第3の熱交換器、前記第4の熱交換器及び前記第5の熱交換器の組み合わせとが流体的に互いに並列に連結される、
請求項20の方法。 - 前記1つ以上の熱交換器が、緩衝流体を介し:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームを用いて、前記緩衝流体の第1の分岐を加熱するステップと;
前記第1の熱交換器を出る前記加熱された第1の分岐を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第3の熱交換器において、前記加熱された第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
前記第3の熱交換器を出る前記緩衝流体の前記第1の分岐を、前記サワーウォータストリッパプラントへ流すステップと;
第4の熱交換器において、前記第3の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を用いて、前記サワーウォータストリッパプラント内のサワーウォータストリッパ塔底ストリームを加熱するステップと;
前記第4の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を、前記アミン再生プラントへ流すステップと;
第5の熱交換器において、前記第4の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を用いて、酸性ガス再生塔底ストリームを加熱するステップと;
第2の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の抽出塔頂ストリームを用いて、前記緩衝流体の第2の分岐を加熱するステップと;
前記第2の熱交換器を出る前記加熱された第2の分岐を、前記硫黄回収プラントへ流すステップと;
第6の熱交換器において、前記加熱された第2の分岐を用いて、前記硫黄回収プラント内のアミン再生塔底ストリームを加熱するステップと;
前記第6の熱交換器を出る前記加熱された第2の分岐を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第7の熱交換器において、前記第6の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のラフィネートスプリッタ塔底ストリームを加熱するステップと;
によって間接的に熱を伝達する、
請求項2の方法。 - 前記第5の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐と、前記第7の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐とを、緩衝流体タンクへ流すステップを更に備える、
請求項23の方法。 - 第8の熱交換器において、前記水素プラント内の低温シフト(LTS)後水素プラントストリームの第1の分岐を用いて、前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第9の熱交換器において、前記水素プラント内の前記LTS後水素プラントストリームの第2の分岐を用いて、前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
を更に備える、
請求項24の方法。 - 前記第1の熱交換器及び前記第3の熱交換器が流体的に互いに直列に連結され、前記第3の熱交換器及び前記第4の熱交換器が流体的に互いに直列に連結され、前記第4の熱交換器及び前記第5の熱交換器が流体的に互いに直列に連結され、前記第2の熱交換器及び前記第6の熱交換器が流体的に互いに直列に連結され、前記第6の熱交換器及び前記第7の熱交換器が流体的に互いに直列に連結され、前記第8の熱交換器及び前記第9の熱交換器が流体的に互いに直列に連結される、
請求項25の方法。 - 前記1つ以上の熱交換器が、緩衝流体を介し:
第1の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の芳香族炭化水素複合施設キシレン生成物分離ラフィネート塔頂ストリームを用いて、前記緩衝流体の第1の分岐を加熱するステップと;
前記第1の熱交換器を出る前記加熱された第1の分岐を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第3の熱交換器において、前記加熱された第1の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のベンゼン塔底ストリームを加熱するステップと;
前記第3の熱交換器を出る前記緩衝流体の前記第1の分岐を、前記サワーウォータストリッパプラントへ流すステップと;
第4の熱交換器において、前記第3の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を用いて、前記サワーウォータストリッパプラント内のサワーウォータストリッパ塔底ストリームを加熱するステップと;
前記第4の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を、前記アミン再生プラントへ流すステップと;
第5の熱交換器において、前記第4の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐を用いて、酸性ガス再生塔底ストリームを加熱するステップと;
第2の熱交換器において、前記芳香族炭化水素複合施設キシレン生成物分離ユニット内の抽出塔頂ストリームを用いて、前記緩衝流体の第2の分岐を加熱するステップと;
前記第2の熱交換器を出る前記加熱された第2の分岐を、前記硫黄回収プラントへ流すステップと;
第6の熱交換器において、前記加熱された第2の分岐を用いて、前記硫黄回収プラント内の硫黄回収アミン再生塔底ストリームを加熱するステップと;
前記第6の熱交換器を出る前記加熱された第2の分岐を、前記芳香族炭化水素複合施設ベンゼン抽出ユニットへ流すステップと;
第7の熱交換器において、前記第6の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐を用いて、前記芳香族炭化水素複合施設ベンゼン抽出ユニット内のラフィネートスプリッタ塔底ストリームを加熱するステップと;
によって間接的に熱を伝達する、
請求項2の方法。 - 前記第5の熱交換器を出る前記加熱された緩衝流体の前記第1の分岐と、前記第7の熱交換器を出る前記加熱された緩衝流体の前記第2の分岐とを、緩衝流体タンクへ流すステップを更に備える、
請求項27の方法。 - 第8の熱交換器において、前記ディーゼル水素処理プラント内の生成物ストリッパ塔底留分ストリームの第1の分岐を用いて前記ガス分離プラント内のC3/C4スプリッタ塔底ストリームを加熱するステップと;
第9の熱交換器において、前記ディーゼル水素処理プラント内の前記生成物ストリッパ塔底留分ストリームの第2の分岐を用いて前記ガス分離プラント内の脱エタン塔底ストリームを加熱するステップと;
を備える、
請求項27の方法。 - 前記第1の熱交換器及び前記第3の熱交換器が流体的に互いに直列に連結され、前記第3の熱交換器及び前記第4の熱交換器が流体的に互いに直列に連結され、前記第4の熱交換器及び前記第5の熱交換器が流体的に互いに直列に連結され、前記第2の熱交換器及び前記第6の熱交換器が流体的に互いに直列に連結され、前記第6の熱交換器及び前記第7の熱交換器が流体的に互いに直列に連結され、前記第8の熱交換器及び前記第9の熱交換器が流体的に互いに直列に連結される、
請求項29の方法。 - 原油精製施設で実施されるシステムであって、請求項1に記載の方法を実施するように構成される、
システム。 - 前記システムが流量制御システムを備える、
請求項31のシステム。
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