CN108138591A - 工业设备中废弃能量的回收和再利用 - Google Patents
工业设备中废弃能量的回收和再利用 Download PDFInfo
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- CN108138591A CN108138591A CN201680061004.8A CN201680061004A CN108138591A CN 108138591 A CN108138591 A CN 108138591A CN 201680061004 A CN201680061004 A CN 201680061004A CN 108138591 A CN108138591 A CN 108138591A
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- heat exchanger
- stock
- tributary
- heated
- heat
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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
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- 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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D51/00—Auxiliary pretreatment of gases or vapours to be cleaned
- B01D51/10—Conditioning the gas to be cleaned
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- 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
- B01D53/04—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 with stationary adsorbents
- B01D53/047—Pressure swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/14—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 absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
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- B01D—SEPARATION
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- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
- C01B3/24—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds of hydrocarbons
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- C—CHEMISTRY; METALLURGY
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- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
- C02F1/586—Treatment of water, waste water, or sewage by removing specified dissolved compounds by removing ammoniacal nitrogen
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
- C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
- C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
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- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F01D17/00—Regulating or controlling by varying flow
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- F01D17/12—Final actuators arranged in stator parts
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Abstract
描述了用于在综合精炼‑石化设备中的热能消耗减少的特定装置间以及混合型装置内和装置间废热回收方案的配置和相关加工方案,其整合用于草根中级原油半转化精炼厂以提高来自低级废热源的特定部分的能量效率。还描述了用于综合精炼‑石化设备中的热能消耗减少的特定装置间以及混合型装置内和装置间废热回收方案的配置和相关加工方案,其整合用于综合中级原油半转化精炼厂和芳烃联合装置以提高来自低级废物源的特定部分的能量效率。
Description
相关申请的交叉引用
本申请要求于2015年8月24日提交的美国临时专利申请号62/209,217、于2015年8月24日提交的美国临时专利申请号62/209,147、于2015年8月24日提交的美国临时专利申请号62/209,188和于2015年8月24日提交的美国临时专利申请号62/209,223的优先权。将这些在先申请中的每一个的整个内容以它们各自的整体通过引用并入本文。
技术领域
本说明书涉及运行工业设备(工业设施,industrial facilities),例如,原油精炼设备或包括运行产生热量的装置(plant)的其他工业设备。
背景
石油精炼过程(工艺,process)是在石油精炼厂(refineries)中用于将原油转化为产物,例如,液化石油气(LPG)、汽油、煤油、喷气燃料、柴油、燃料油和其他产物的化工过程和其他设备。石油精炼厂是涉及许多不同加工单元和辅助设备例如公用工程单元、储罐和其他辅助设备的大型工业联合装置(industrial complex)。各个精炼厂都可以具有例如通过精炼厂位置、所需产物、经济考虑或其他因素决定的其自身独特的精炼过程的布置和组合。被实施(执行,implement)以将原油转化为产物如先前列举的那些的石油精炼过程可以产生可能不被再利用的热量,和可能污染大气的副产物,例如温室气体(GHG)。据信,世界环境已经受部分由于GHG释放到大气中造成的全球变暖负面影响。
概述
本说明书描述与用于来自工业设备中的废弃能量(waste energy)的能量消耗减少的特定直接或间接装置间以及混合型装置内和装置间联合(集成或一体化,integration)相关的技术。
本说明书中描述的主题的一种或多种实施方式的细节在附图和之后的描述中提出。所述主题的其他特征、方面和优点根据该描述、附图和权利要求书将变得明显。
附图简述
图1A-1O举例说明了用于热联合原油精炼设备中的不同精炼装置的配置和相关方案细节。
图1P-1AC举例说明了用于热联合原油精炼设备中的不同精炼装置的配置和相关方案细节。
详述
工业废热是在许多工业设备,例如原油精炼厂、石化和化学联合装置以及其他工业设备中用于可能的无碳发电的来源。例如,对于沿原油和芳烃位置延伸的空气冷却器的网络,具有多达4000MM英热单位/小时(British Thermal Units per hour,Btu/h)的芳烃的中等尺寸综合原油精炼厂可能是浪费的。废热中的一些可以被再利用以加热在该原油精炼厂的精炼子单元中的流股(流或物流,stream),由此减少在其他方面将需要被使用以加热这些流股的热量的量。以此方式,可以降低被原油精炼厂消耗的热量的量。另外,也可以降低温室气体(GHG)排放的量。在一些实施方式中,在不影响原油精炼厂的经营理念的情况下,可以实现加热公用工程消耗的约34%的减少和冷却公用工程消耗的约20%的减少。
此处描述的废热回收和再利用技术可以在中级原油精炼半转化设备以及综合中级原油精炼半转化炼油和芳烃设备中实施。这些实施方式可以导致可以消耗由现有和新的原油精炼设备的现有技术设计所消耗的加热公用工程的约66%的能量高效系统。这些实施方式还可以导致相对于来自现有和新的原油精炼设备的现有技术设计的GHG排放的约三分之一的污染和GHG排放的降低。
在某些现有炼油设备中,装置(例如,石脑油加氢处理装置、酸性污水(含硫的污水,sour water)汽提塔装置或其他装置)中的流股使用蒸汽再沸器(steam reboiler)加热。在此处描述的主题的一些实施方式中,所述装置中的流股可以使用由另一装置(例如,加氢裂化装置、加氢处理装置、制氢装置或其他装置)中的另一流股携带的废热加热。通过这样做,可以减少或消除在蒸汽再沸器中产生的热能。换言之,蒸汽再沸器不需要是用于加热所述装置中的流股的热能的唯一来源。由其他装置中的其他流股携带的废热可以替代蒸汽再沸器中产生的热能或者补充热能,由此减少来自蒸汽再沸器的所需热能的量。
此处描述的主题可以以不同装置的特定操作模式实施,并且可以在不需要改变原油精炼厂中的现有热交换器设计的网络设计的情况下进行改造。在废热回收和再利用过程中使用的最小接近温度可以低至3℃。在一些实施方式中,在初始阶段以较少的废弃热量/能量回收为代价可以使用较高的最小接近温度,同时在后续阶段在使用对于特定热源使用的最小接近温度时实现相对较好的节能。
总之,本公开内容描述了多种用于提高加热/冷却公用工程的能效的原油精炼厂领域的分离/蒸馏网络、配置和加工方案。通过再利用全部或部分废热,例如由多个分散的低级能量品质过程流股携带的低级废热,实现了能效提高。
原油精炼厂装置的实例
1.制氢装置(hydrogen Plant)
氢通常在精炼厂中用于烃产物的硫去除和质量改善。随着对汽油和柴油的硫限制变得严格,对于氢的精炼需求持续增长。在特地产氢装置中采用两种过程方案-常规过程和基于变压吸附(PSA)的过程。氢制备可以包括加氢脱硫、蒸汽重整、变换(shiftconversion)和纯化。常规过程制得中等纯度的氢,而基于PSA的过程将氢回收并且纯化至高纯度,例如大于99.9%的纯度。
2.芳烃联合装置(aromatics complex)
典型的芳烃联合装置包括用于使用利用连续催化重整(CCR)技术的石脑油的催化重整来制备苯、甲苯和二甲苯(BTX)的基础石化中间体的过程单元的组合。
3.气体分离装置
气体分离装置包括脱乙烷塔和脱丙烷塔,其是分别用于分离在气体装置和精炼厂中的天然气液体(NGL)和轻端馏分中的乙烷和丙烷的蒸馏塔。脱乙烷塔从丙烷、丁烷和其他较重组分的混合物中去除乙烷。将脱乙烷塔的输出进料到脱丙烷塔中以从该混合物中分离丙烷。
4.胺再生装置
硫化氢和二氧化碳是天然气中存在的最常见污染物,并且与其他污染物(如果未去除可能负面影响天然气加工设备)相比以相对较大的量存在。胺在酸性气体吸收塔(acidgas absorber)和再生塔(再生器,regenerator)中用于使化学过程中的酸性气体脱臭(脱硫,sweeten),在所述化学过程中弱碱(例如,胺)与弱酸如硫化氢和二氧化碳反应而形成弱盐。
5.加氢裂化装置
加氢裂化是将催化裂化和氢化进行组合的两阶段过程。在该过程中,重质原料(进料,feedstock)在氢的存在下裂化而产生更理想的产物。该过程采用高压、高温、催化剂和氢。加氢裂化用于难以通过催化裂化或重整进行加工的原料,因为这些原料的特征通常在于高的多环芳烃含量或高浓度的两种主要催化剂毒物,即硫和氮化合物(或它们的组合)。
加氢裂化过程依赖于原料的性质和两种竞争性反应(氢化和裂化)的相对速率。重质芳烃原料在宽范围的高压力和高温度下在氢和特殊催化剂的存在下转化为较轻的产物。当原料具有高的烷烃含量时,氢防止多环芳烃化合物的形成。氢还减少焦油形成并且防止炭在催化剂上的积聚。氢化另外将在原料中存在的硫和氮化合物转化为硫化氢和氨。加氢裂化产生用于烷基化原料的异丁烷,以及进行异构化用于倾点控制和烟点控制,它们两者在高品质喷气燃料中都是重要的。
6.柴油加氢处理装置
加氢处理是用于减少硫、氮和芳烃同时提高十六烷值、密度和烟点的精炼过程。加氢处理帮助精炼工业的工作以符合严格的清洁燃料规格的全球趋势、运输燃料的增长需求和朝向柴油的转变。在该过程中,将新鲜的进料加热并与氢混合。反应器流出物与合并的进料交换热量并且加热循环气和汽提塔装填物。然后将硫化物(例如,二硫化铵和硫化氢)从进料中去除。
7.酸性污水汽提塔公用工程装置(SWSUP)
SWSUP接收来自酸性气体去除、硫回收和燃烧单元(放空单元,flare unit)的酸性污水流股,以及经汽提且由烟灰水闪蒸容器释放的酸性气体(sour gas)。SWSUP汽提来自酸性污水流股的酸性组分,主要为二氧化碳(CO2)、硫化氢(H2S)和氨(NH3)。
8.硫回收装置
精炼厂中的脱硫设备运行以调控硫化合物至大气的排放从而满足环境规章。在硫回收装置中,可以例如通过加热、用冷凝器冷却、使用硫转化催化剂、以及通过其他加工技术来加工包括硫的燃烧产物。一种技术是使用胺来提取(抽提,extract)硫和其他酸性气体化合物。
9.石脑油加氢处理装置和连续催化重整装置
石脑油加氢处理(NHT)产生101研究法辛烷值(RON)重整油(reformate),其具有最大4.0psi(磅/平方英寸)雷德蒸气压(Reid Vapor Pressure)(RVP),作为汽油总合中的调合料。其通常具有用于加工来自原油蒸馏装置(Crude Unit)、气体冷凝物分割塔(GasCondensate Splitter)、加氢裂化装置(Hydrocracker)、轻质直馏石脑油(LightStraight-Run Naphtha)(LSRN)和减粘裂化装置(Visbreaker Plant)的石脑油的共混物的灵活性。NHT加工石脑油以产生用于CCR铂重整装置(platformer)和汽油共混的脱硫进料。
热交换器(换热器,heat exchanger)
在本公开内容中描述的配置中,热交换器用于将热量从一种介质(例如,流过原油精炼设备中的装置的流股、缓冲流体或其他介质)转移至另一种介质(例如,缓冲流体或流过原油设备中的装置的不同流股)。热交换器是典型地将热量从较热的流体流股转移(交换)至相对较不热的流体流股的装置。热交换器可以用于加热和冷却应用,例如用于冰箱、空调或其他冷却应用。热交换器可以基于其中液体流动的方向区分彼此。例如,热交换器可以是并流、错流或逆流。在并流热交换器中,所涉及的两种流体在相同方向上的移动,并排地进入和离开热交换器。在错流热交换器中,流体路径彼此垂直地行进。在逆流热交换器中,流体路径以相反方向流动,其中一种流体离开而另一流体进入。逆流热交换器有时比其他类型的热交换器更有效。
除了基于流体方向分类热交换器之外,热交换器还可以基于它们的构造分类。一些热交换器由多个管构成。一些热交换器包括具有用于流体在其间流动的空间的板。一些热交换器能够实现液体至液体的热交换,同时一些热交换器能够实现使用其他介质的热交换。
在原油精炼和石化设备中的热交换器通常是包括液体流过的多个管的壳管型热交换器。管分为两组-第一组容纳待加热或冷却的液体;第二组容纳负责激发热交换的液体,即通过将热量吸收和传送离开而从第一组管移出热量或者通过将其自身的热量传送至内部的液体而使第一组升温的流体。当设计此类型的交换器时,必须注意确定适当的管壁厚度以及管径,以允许最佳的热交换。就流动而言,壳管式热交换器可以采取三种流路方式中的任一种。
在原油精炼和石化设备中的热交换器也可以是板框型热交换器。板式热交换器包括其间具有通常通过橡胶衬垫保持的少量空间的结合在一起的薄板。表面积大,并且各个矩形板的角落以流体可以在板间流动通过的开口为特征,随着其流动从板提取热量。流体通道本身使热和冷的液体交替,意味着热交换器可以有效地冷却以及加热流体。因为板式热交换器具有大的表面积,所以它们有时可以比壳管式热交换器更有效。
其他类型的热交换器可以包括再生热交换器(回热式热交换器,regenerativeheat exchanger)和绝热轮式热交换器。在再生热交换器中,相同的流体沿着热交换器的两侧通过,所述热交换器可以是板式热交换器或壳管式热交换器。因为流体可以变得非常热,所以离开的流体被用于使进入的流体升温,保持接近恒温。在再生热交换器中节省能量,因为该过程是循环的,其中几乎所有相关的热量从离开的流体转移至进入的流体。为了保持恒温,需要少量的额外能量以升高和降低整体流体温度。在绝热轮式热交换器中,中间流体被用于储存热量,该热量然后转移至热交换器的相对侧。绝热轮由具有旋转穿过液体(热和冷的两者)以提取或转移热量的线状体(threats)的大轮组成。本公开内容中描述的热交换器可以包括先前描述的热交换器、其他热交换器或它们的组合中的任一种。
在每种配置中的各个热交换器都可以与各自的热负荷(热力负荷)相关联。热交换器的热负荷可以定义为可以由热交换器从热流股转移至冷流股的热量的量。热量的量可以由热和冷流股两者的条件和热性质计算。从热流股的角度看,热交换器的热负荷是热流股流速、热流股比热和在至热交换器的热流股入口温度与来自热交换器的热流股出口温度之间的温度差的乘积。从冷流股的观点出发,热交换器的热负荷是冷流股流速、冷流股比热和来自热交换器的冷流股出口温度与来自热交换器的冷流股入口温度之间的温度差的乘积。在多种应用中,假定对于这些单元没有至环境的热量损失,特别地,在这些单元良好绝热的情况下,可以认为这两个量相等。可以以瓦(W)、兆瓦(MW)、百万英热单位/小时(Btu/h)或百万千卡/小时(Kcal/h)测量热交换器的热负荷。在此处描述的配置中,热交换器的热负荷作为“约X MW”提供,其中“X”表示数字热负荷值。数字热负荷值不是绝对的。即,热交换器的实际热负荷可以大致等于X、大于X或小于X。
其中热交换器被描述为串联的配置可以具有多种实施方式。在一些实施方式中,热交换器可以以一种顺序(例如,按顺序的第一热交换器、第二热交换器和第三热交换器)串联布置,而在其他实施方式中,热交换器可以以不同顺序(例如,按顺序的第三热交换器、第一热交换器和第二热交换器)串联布置。换言之,在一个实施方式中被描述为与第二热交换器串联且在其下游的第一热交换器在第二种不同的实施方式中可以与第二热交换器串联且在其上游。
流动控制系统
在之后描述的配置的每一种中,过程流股(也称作“流股”)在原油精炼设备中的各个装置内以及在原油精炼设备中的装置之间流动。可以使用在整个原油精炼设备实施的一个或多个流动控制系统使过程流股流动。流动控制系统可以包括一个或多个用于泵送过程流股的泵、一个或多个过程流股流过的流动管和一个或多个用于调节流股穿过管的流动的阀门。
在一些实施方式中,流动控制系统可以手动操作。例如,操作人员可以设定各个泵的流速(流率,flow rate)并且设定阀门打开或关闭位置以调节过程流股穿过流动控制系统中的管的流动。一旦操作人员已经设定分布在原油精炼设备上的所有流动控制系统的流速和阀门打开或关闭位置,流动控制系统就可以使流股在装置内或在装置之间在恒流条件例如恒定体积速率或其他流动条件下流动。为了改变流动条件,操作人员可以例如通过改变泵流速或者阀门打开或关闭位置来手动地操作流动控制系统。
在一些实施方式中,流动控制系统可以自动操作。例如,流动控制系统可以连接至计算机系统以操作流动控制系统。计算机系统可以包括存储由一个或多个处理器可执行的指令(如流动控制指令和其他指令)的计算机可读介质以进行操作(如流动控制操作)。操作人员可以使用计算机系统来设定分布在原油精炼设备上的所有流动控制系统的流速和阀门打开或关闭位置。在这样的实施方式中,操作人员可以通过经由算机系统提供输入而手动改变流动条件。另外,在这样的实施方式中,计算机系统可以例如使用在一个或多个装置中实施且连接至计算机系统的反馈系统自动(即,无需手动干预)控制所述流动控制系统中的一个或多个。例如,传感器(如压力传感器、温度传感器或其他传感器)可以连接至过程流股流过的管道。传感器可以监测并提供过程流股的流动条件(如压力、温度或其他流动条件)至计算系统。响应于超过阈值(如阈值压力值、阈值温度值或其他阈值)的流动条件,计算机系统可以自动进行操作。例如,如果管道中的压力或温度分别超过阈值压力值或阈值温度值,则计算机系统可以向泵提供用于降低流速的信号,提供用于打开阀门以释放压力的信号,提供用于关闭过程流股流的信号,或提供其他信号。
本公开内容描述了用于综合中级原油半转化精炼设备和芳烃联合装置的先进的能量高效配置和相关加工方案。
在一些实施方式中,半转化中级原油精炼设备包括在精炼设备中的几乎所有装置,包括例如芳烃联合装置和加氢裂化装置。本公开内容描述了用于这样的精炼设备的废热回收和再利用网络。如后文描述的,可以从原油精炼设备中的多个装置(包括加氢裂化装置)回收废热。这样的精炼厂典型地在加热公用工程中消耗几百兆瓦的能量。实施此处描述的配置不仅可以减少能量消耗,而且可以减少基于能量的温室气体(GHG)排放。特别地,本公开内容描述了在原油精炼设备中实施以使用在原油精炼设备中的多个第二装置中的多个第二流股加热在原油精炼设备的多个第一装置中的多个第一流股的方法。后文参照以下附图来描述用于这样做的过程方案的多种配置。
方案A
图1A-1O举例说明了用于热联合原油精炼设备中的不同精炼装置的配置和相关方案细节。在这些配置中描述且在图1A-1O中举例说明的热联合可以减少原油精炼设备的能量消耗(例如,加热和冷却公用工程)。例如,约166MW(例如166MW)的能量消耗减少可以转换为原油精炼设备中至少约25%(例如25.5%)的能量消耗。在某些方案中,来自一个精炼装置的过程流股可以用于直接加热来自另一不同精炼装置的另一过程流股。在某些配置中,过程流股之间的热交换可以使用中间缓冲流体,例如,水、油或其他缓冲流体来实施。在其他方案中,两种技术彼此组合地使用。
在一些实施方式中,可以使用在多个第二装置中的多个第二流股直接加热在多个第一装置中的多个第一流股。在一些实施方式中,多个第一装置可以包括胺再生装置、芳烃联合装置子单元(包括苯提取单元)、石脑油加氢处理装置、酸性污水汽提塔装置、硫回收装置和气体分离装置。多个第二流股包括提余液塔塔顶产物、提取塔塔顶产物(extractcolumn overheads)、柴油产物、柴油汽提塔塔底、(流动或进料)到第一阶段反应冷高压分离器的进料流股(feed stream)、到第二阶段反应冷高压分离器的进料流股、柴油汽提塔塔顶、产物汽提塔塔顶、煤油产物和煤油循环回流(中段回流,pumparound)流股。多个第二装置可以包括另一芳烃联合装置子单元(包括芳烃联合装置二甲苯产物分离单元(有时称作二甲苯分离单元))、加氢裂化装置和柴油加氢处理装置。多个第一流股包括酸性气体再生塔塔底产物(acid gas regenerator bottoms)、酸性污水汽提塔塔底产物、胺再生塔塔底产物、C3/C4分割塔塔底产物、脱乙烷塔塔底产物、苯塔塔底产物(benzene columnbottoms)、提余液分割塔塔底产物和石脑油分割塔塔底产物流股。在一些实施方式中,通过来自第二装置中的三个的多个第二流股直接加热来自第一装置中的一个的第一装置流股中的一个。在一些实施方式中,通过来自第二装置中的两个的多个第二流股直接加热来自第一装置中的一个的第一装置流股中的一个。
图1A示出了原油精炼设备中的芳烃联合装置二甲苯产物分离单元820。提余液塔塔顶产物流股可以作为单一流股在装置中流动并且分裂成多个流股,或者其可以作为多个流股流动到装置中以有利于热回收。第一提余液塔塔顶流股可以在具有可以为约45MW至55MW(例如,47.8MW)的热负荷的第一热交换器中直接加热酸性气体再生塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。
图1G示出了原油精炼设备中的柴油加氢处理装置800。图1J示出了原油精炼设备中的酸性污水汽提塔装置810。酸性污水汽提塔塔底产物流股可以作为单一流股在装置中流动并且分裂成多个流股,或者其可以作为多个流股流动到装置中以有利于热回收。如图1G中所示,柴油汽提塔塔底产物流股可以在具有可以为约5MW至15MW(例如,8MW)的热负荷的第二热交换器中直接加热第一酸性污水汽提塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。在此情形中,使离开第二热交换器的柴油汽提塔塔底产物流股流动到如后文描述的第五热交换器。
如图1A中所示,提取塔塔顶产物流股可以在具有可以为约20MW至30MW(例如,24MW)的热负荷的第三热交换器中直接加热第二酸性污水汽提塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将提取塔塔顶流股返回到二甲苯分离单元820用于进一步加工(处理,processing)。
如图1J中所示,用于酸性污水汽提塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径(流程,flow path)可以满足用于该酸性污水汽提塔的操作(运行,operation)的整个热负荷。在一个备选实施方案中,可以减少用于酸性污水汽提塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该酸性污水汽提塔的操作的热负荷。
图1B-1F示出了原油精炼设备中的加氢裂化装置816。具体地,图1D示出了到加氢裂化装置812中的第一阶段反应冷高压分离器的进料流股可以在具有可以为约15MW至25MW(例如,21MW)的热负荷的第四热交换器中直接加热胺再生塔塔底流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将到第一阶段反应冷高压分离器的进料流股返回到加氢裂化装置用于进一步加工。
图1K示出了原油精炼设备中的硫回收装置802。用于胺再生塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该胺再生塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于胺再生塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该胺再生塔的操作的热负荷。
如图1G中所示,柴油汽提塔塔底流股可以在具有可以为约5MW至15MW(例如,9.9MW)的热负荷的第五热交换器中直接加热C3/C4分割塔塔底流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。使离开第五热交换器的柴油汽提塔塔底流股流动到如后文描述的第六热交换器。
图1M示出了原油精炼设备中的气体分离装置804。用于C3/C4分割塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该C3/C4分割塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于C3/C4分割塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该C3/C4分割塔的操作的热负荷。
如图1G中所示,柴油汽提塔塔底流股可以在具有可以为约1MW至10MW(例如,4.3MW)的热负荷的第六热交换器中直接加热脱乙烷塔塔底流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将柴油汽提塔塔底产物流股返回到柴油加氢处理装置800用于进一步加工。
如图1M中所示,用于脱乙烷塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该脱乙烷塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于脱乙烷塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该脱乙烷塔的操作的热负荷。
如图1A中所示,第二提余液分割塔塔顶流股可以在具有可以为约1MW至10MW(例如,6MW)的热负荷的第七热交换器中直接加热苯塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。
图1N示出了原油精炼设备中的芳烃联合装置苯提取单元818。用于苯塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该苯塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于苯塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该苯塔的操作的热负荷。
如图1C中所示,到第二阶段反应冷高压分离器的进料流股可以在具有可以为约5MW至15MW(例如,9MW)的热负荷的第八热交换器中直接加热提余液分割塔塔底流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将到第二阶段反应冷高压分离器的进料流股返回到加氢裂化装置812用于进一步加工。
图1N还示出了原油精炼设备中的芳烃联合装置苯提取单元818。用于提余液分割塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该提余液分割塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于提余液分割塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该提余液分割塔的操作的热负荷。
在这些情形中,相对于提余液塔塔顶产物流股的流动,第一热交换器和第七热交换器(图1A)彼此并联地连接。相对于柴油汽提塔塔底产物流股的流动,第五热交换器和第六热交换器(图1G)彼此串联地连接。相对于酸性污水汽提塔塔底产物的流动,第二热交换器和第三热交换器(图1J)彼此并联地连接。
在一些实施方式中,可以使柴油汽提塔塔底产物流股按顺序流过不同的装置。例如,可以使柴油汽提塔塔底产物流股首先流过气体分离装置,然后流过酸性污水汽提塔装置。在另一实施方式中,在气体分离装置内,柴油汽提塔塔底产物流股可以首先流过脱乙烷塔(de-euthanizer)交换器,然后流过C3/C4分割塔交换器。
图1H-1I示出了原油精炼设备中的石脑油加氢处理装置814。石脑油分割塔塔底产物流股可以作为单一流股在装置中流动并且分裂成多个流股,或者其可以作为多个流股流动到装置中以有利于热回收。如图1G中所示,柴油汽提塔塔顶流股可以在具有可以为约1MW至10MW(例如,7.46MW)的热负荷的热交换器A中直接加热第一石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将柴油汽提塔塔顶流股返回到柴油加氢处理装置800用于进一步加工。
如图1A中所示,提余液塔塔顶产物流股可以在具有可以为约5MW至15MW(例如,8.5MW)的热负荷的热交换器B中直接加热第二石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将第一、第二和第三提余液塔塔顶产物流股重新合并,并且返回到二甲苯分离单元820用于进一步加工。
如图1E(由图1E-1和1E-2共同代表)中(具体地在图1E-1中)所示,产物汽提塔塔顶流股可以在具有可以为约1MW至10MW(例如,3.38MW)的热负荷的热交换器C中直接加热第三石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将产物汽提塔流股返回到加氢裂化装置812用于进一步加工。
如图1B中所示,柴油产物流股可以在具有可以为约1MW至10MW(例如,6.6MW)的热负荷的热交换器D中直接加热第四石脑油分割塔流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将柴油产物流股返回到加氢裂化装置812用于进一步加工。
如图1F中所示,煤油产物流股可以在具有可以为约1MW至10MW(例如,5.4MW)的热负荷的热交换器E中直接加热第五石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将煤油产物流股返回到加氢裂化装置812用于进一步加工。
如图1E中(具体地在图1E-2中)所示,煤油循环回流流股可以在具有可以为约1MW至10MW(例如,5.7MW)的热负荷的热交换器F中直接加热第六石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将煤油循环回流流股返回到加氢裂化装置812用于进一步加工。
如图1H和1I中所示,用于石脑油分割塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该石脑油分割塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于石脑油分割塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该石脑油分割塔的操作的热负荷。
相对于石脑油分割塔塔底产物流的流动,所述热交换器A、所述热交换器B、所述热交换器C、所述热交换器D、所述热交换器E和所述热交换器F(图1I)彼此并联地连接。相对于提余液塔塔顶产物流股的流动,第一热交换器、第七热交换器和热交换器B(图1A)彼此并联地连接。
如图1H-1I中所示,使经加热的(加热后的,heated)石脑油分割塔塔底产物流股流动到石脑油加氢处理装置814。如图1J中所示,使经加热的酸性污水汽提塔流股流动到酸性污水汽提塔装置810。如图1M中所示,使经加热的C3/C4分割塔塔底流股和脱乙烷塔塔底流股流动到气体分离装置804。如图1K中所示,使经加热的胺再生单元汽提塔塔底流股流动到硫回收装置802。如图1L中所示,使经加热的酸性气体再生塔塔底产物流股流动到胺再生装置806。如图1N和1O中所示,使苯塔塔底产物和提余液分割塔塔底产物流动到苯提取单元818。
如图1A-1O中所示,通过来自芳烃联合装置二甲苯产物分离单元、加氢裂化装置和柴油加氢处理装置的多个第二流股直接加热来自石脑油加氢处理装置的石脑油分割塔塔底产物流股。在一些实施方式中,通过来自二甲苯产物分离单元和柴油加氢处理单元的多个第二流股直接加热来自酸性污水汽提塔装置的酸性污水汽提塔塔底产物中的一种。
这样的来自芳烃联合装置二甲苯产物分离单元、加氢裂化装置和柴油加氢处理装置的废热的回收和再利用可以导致减少或消除用于加热在胺再生装置、苯提取单元、石脑油加氢处理装置、酸性污水汽提汽提塔装置、硫回收装置、气体分离装置或它们的组合中的流股的热能如约166MW。
方案B
在一些实施方式中,在原油精炼设备中的多个第一装置,如在芳烃联合装置子单元中存在的那些(如苯提取单元)、酸性污水汽提塔装置、硫回收装置、胺再生装置和气体分离装置中的多个第一流股可以使用在其他芳烃联合装置子单元(包括二甲苯分离单元)、加氢裂化装置和柴油加氢处理装置中的第二装置中的多个第二流股直接加热。在相同的配置中,在原油精炼设备中的第一装置(如石脑油加氢处理装置)中的其他多个第一流股可以例如使用类似于早先描述的那些的技术,使用柴油加氢处理装置、加氢裂化装置和芳烃联合装置二甲苯产物分离单元直接加热。在这样的实施方案中,一种第一装置(如石脑油加氢处理装置)可以通过三个第二装置直接加热,并且其他第一装置可以通过第二装置中的两个(如加氢裂化装置和芳烃联合装置二甲苯产物分离单元)直接加热。
图1P-1AC举例说明了用于热联合原油精炼设备中的不同精炼装置的配置和相关方案细节。在这些配置中描述且在图1A-1P中举例说明的热联合可以减少原油精炼设备的能量消耗(例如,加热和冷却公用工程)。例如,约166MW(例如166MW)的能量消耗减少可以转换为原油精炼设备中至少约25%(例如25.5%)的能量消耗。如之后描述的,所述配置描述了其中间接回收一些废弃能量(即,使用缓冲流体)以及直接回收一些废弃能量(即,从过程流股)的混合型方案。
间接加热流股可以包括经由缓冲流体,例如,油、水或其他缓冲流体加热流股。来自缓冲流体罐(例如,热水罐)的缓冲流体(例如,高压水)流动到二甲苯分离单元820。缓冲流体可以作为单一流股流入到装置中并且分裂成多个流股,或者其可以作为多个流股流入到装置中。
图1P示出了原油精炼设备中的芳烃装置二甲苯产物分离单元820。可以在具有可以为约75MW至85MW(例如,82.36MW)的热负荷的第一热交换器中使用提余液塔塔顶产物流股加热第一缓冲流体。热量从过程流股到缓冲流体中的转移捕获否则将被排出到环境中的热量。将提余液塔塔顶产物流股返回到二甲苯分离单元820用于进一步加工。
可以在具有可以为约30MW至40MW(例如,33MW)的热负荷的第二热交换器中使用提取塔塔顶流股加热第二缓冲流体流股。热量从该过程流股到缓冲流体中的转移捕获否则将被排出到环境中的热量。如图1P中所示,提取塔塔顶产物流股的冷却需求(coolingrequirement)可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该提取塔的操作的提取塔塔顶流股的整个冷却需求。将提取塔塔顶产物流股返回到二甲苯分离单元820用于进一步加工。
图1Q-1T示出了原油精炼设备中的加氢裂化装置单元812。具体地,图1R示出了可以在具有可以为约10MW至20MW(例如,14.64MW)的热负荷的第三热交换器中使用到冷高压分离器的第一阶段反应进料流股加热第三缓冲流体流股。热量从该过程流股到缓冲流体中的转移捕获否则将被排出到环境中的热量。使第一阶段反应进料流股流动到加氢裂化装置812用于进一步加工。在所有情形中,缓冲流体吸收否则将被排出到环境中的热量。
将第一、第二和第三经加热的缓冲流体支流在收集集管中合并为合并的经加热的缓冲流体。以此方式,相对于缓冲流体的流动,第一热交换器、第二热交换器和第三热交换器彼此并联地连接。
可以使来自收集集管(或在一些实施方案中,是可以将经加热的所收集缓冲流体在使用前保持一段时间的经加热或绝热的缓冲流体罐或储存单元)的合并的经加热的缓冲流体流动到苯提取单元818、酸性污水汽提塔装置810、硫回收装置802、胺再生装置806和气体分离装置804。
在一个实施方案中,使缓冲流体流动到芳烃联合装置苯提取单元818。图1X示出了原油精炼设备中的芳烃联合装置苯提取单元818。可以在具有可以为约1MW至10MW(例如,6MW)的热负荷的第四热交换器中使用合并的经加热的缓冲流体加热苯塔塔底流股。相对于缓冲流体流动,第四热交换器与第一、第二和第三热交换器的组(组合,set)连接、与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。
如图1X中所示,用于苯塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该苯塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于苯塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该苯塔的操作的热负荷。
图1Y也示出了原油精炼设备中的芳烃联合装置苯提取单元818。可以在具有可以为约5MW至15MW(例如,8.6MW)的热负荷的第五热交换器中使用离开第四热交换器的经加热的缓冲流体加热提余液分割塔塔底产物流股(图1Y)。相对于缓冲流体流动,第五热交换器与第一、第二和第三热交换器的组连接,与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。
如图1Y中所示,用于提余液分割塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该提余液分割塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于提余液分割塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该提余液分割塔的操作的热负荷。
图1Z也示出了原油精炼设备中的酸性污水汽提塔装置810。可以在具有可以为约25MW至35MW(例如,32MW)的热负荷的第六热交换器中使用经加热的缓冲流体加热酸性污水汽提塔塔底流股。相对于缓冲流体流动,第六热交换器与第一、第二和第三热交换器的组连接,与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。
如图1Z中所示,用于酸性污水汽提塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该酸性污水汽提塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于酸性污水汽提塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该酸性污水汽提塔的操作的热负荷。
图1AA也示出了原油精炼设备中的硫回收装置802。可以在具有可以为约15MW至25MW(例如,21MW)的热负荷的第七热交换器中使用经加热的缓冲流体加热胺再生塔塔底产物流股。相对于缓冲流体流动,第七热交换器与第一、第二和第三热交换器的组连接,与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。
如图1AA中所示,用于胺再生塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该胺再生塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于胺再生塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该胺再生塔的操作的热负荷。
图1AB也示出了原油精炼设备中的胺再生装置806。可以在具有可以为约45MW至55MW(例如,47.8MW)的热负荷的第八热交换器中使用经加热的缓冲流体加热酸性气体再生塔塔底产物流股。相对于缓冲流体流动,第八热交换器与第一、第二和第三热交换器的组连接,与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。
如图1AB中所示,用于酸性气体再生塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该酸性气体再生塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于酸性气体再生塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该酸性气体再生塔的操作的热负荷。
图1AC也示出了原油精炼设备中的气体分离装置804。可以在具有可以为约5MW至15MW(例如,9.9MW)的热负荷的第九热交换器中使用经加热的缓冲流体加热C3/C4分割塔塔底产物流股。相对于缓冲流体流动,第九热交换器与第一、第二和第三热交换器的组连接,与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。
如图1AC中所示,用于C3/C4分割塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该C3/C4分割塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于C3/C4分割塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该C3/C4分割塔的操作的热负荷。
如图1AC中所示,可以用可以为约1MW至10MW(例如,4.3MW)的热负荷使用经加热的缓冲流体加热脱乙烷塔塔底产物流股。相对于缓冲流体流动,第十热交换器与第一、第二和第三热交换器的组连接,与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。相对于缓冲流体流动,第十热交换器与第一、第二和第三热交换器的组连接,与第一、第二和第三热交换器的组串联,并且在第一、第二和第三热交换器的组的下游。
如图1AC中所示,用于脱乙烷塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该脱乙烷塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于脱乙烷塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该脱乙烷塔的操作的热负荷。
使离开第十热交换器的经加热的缓冲流体流动到收集集管或缓冲液体罐。以此方式,第四热交换器、第五热交换器、第六热交换器、第七热交换器、第八热交换器、第九热交换器和第十热交换器彼此串联地流体连接。
在一些实施方式中,可以使经加热的缓冲流体按顺序流过不同的装置。例如,可以使经加热的缓冲流体首先流动到苯提取单元,然后流动到酸性污水汽提塔装置,然后流动到硫回收装置,然后流动到胺再生装置,然后流动到气体分离装置。在另一实施方式中,在气体分离装置内,经加热的缓冲流体流股可以首先流过脱乙烷塔交换器,然后流过C3/C4分割塔交换器。可以使离开第十热交换器的经加热的缓冲流体流动到缓冲流体罐。来自缓冲流体罐的缓冲流体然后可以流动到不同的装置以重新开始废热回收和再利用循环。
图1V-1W示出了原油精炼设备中的石脑油加氢处理装置814。石脑油分割塔塔底产物流股可以作为单一流股在装置中流动并且分裂成多个流股,或者其可以作为多个流股流动到装置中以有利于热回收。如图1U中所示,柴油汽提塔塔顶产物流股可以在具有可以为约1MW至10MW(例如,7.46MW)的热负荷的热交换器A中直接加热石脑油分割塔塔底产物的第一流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将柴油汽提塔塔顶产物流股返回到柴油加氢处理装置800用于进一步加工。
如图1P中所示,提余液塔塔顶产物流股可以在具有可以为约5MW至15MW(例如,8.5MW)的热负荷的热交换器B中直接加热第二石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。相对于提余液塔塔顶产物流股的流动,第一热交换器和热交换器B彼此串联地连接,并且在此情形中第一热交换器在热交换器B的下游。如图1P中所示,提余液塔塔顶产物流股的冷却需求可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该提余液塔的操作的提余液塔塔顶流股的整个冷却需求。将提余液塔塔顶流股返回到二甲苯分离单元820用于进一步加工。
在一些实施方式中,可以使提余液塔塔底产物流股按顺序流过不同的装置。例如,使提余液塔塔顶产物流股首先流过缓冲流体热交换器,然后流过石脑油加氢处理装置。
如图1S(由图1S-1和1S-2共同代表)中(具体地在图1S-1中)所示,产物汽提塔塔顶产物流股可以在具有可以为约1MW至10MW(例如,3.38MW)的热负荷的热交换器C中直接加热第三石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将产物汽提塔塔顶产物流股返回到加氢裂化装置812用于进一步加工。
如图1Q中所示,柴油产物流股可以在具有可以为约1MW至10MW(例如,6.6MW)的热负荷的热交换器D中直接加热第四石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将柴油产物流股返回到加氢裂化装置812用于进一步加工。
如图1T中所示,煤油产物流股可以在具有可以为约1MW至10MW(例如,5.4MW)的热负荷的热交换器E中直接加热第五石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将煤油产物流股返回到加氢裂化装置812用于进一步加工。
如图1S中(具体地在图1S-2中)所示,煤油循环回流流股可以在具有可以为约1MW至10MW(例如,5.7MW)的热负荷的热交换器F中直接加热第六石脑油分割塔塔底产物流股。热量直接至另一过程流股的转移捕获否则将被排出到环境中的热量。将煤油循环回流流股返回到加氢裂化装置812用于进一步加工。
如图1V和1W两者中所示,用于石脑油分割塔的蒸汽热输入可以是0MW,因为在该配置中公开的备选流动路径可以满足用于该石脑油分割塔的操作的整个热负荷。在一个备选实施方案中,可以减少用于石脑油分割塔的蒸汽热输入,因为在该配置中公开的备选流动路径可以部分地满足用于该石脑油分割塔的操作的热负荷。
如图1P-1AC中所示,通过来自芳烃联合装置二甲苯产物分离单元、加氢裂化装置和柴油加氢处理装置的多个第二流股直接加热来自石脑油加氢处理装置的石脑油分割塔塔底产物流股。相对于石脑油分割塔塔底产物的流动,热交换器A、热交换器B、热交换器C、热交换器D、热交换器E和热交换器F彼此并联地连接。
这样的间接来自芳烃联合装置二甲苯产物分离单元和加氢裂化装置两者以及直接来自芳烃联合装置、柴油加氢处理装置和加氢裂化装置的废热的回收和再利用可以导致减少或消除用于加热在胺再生装置、苯提取单元、石脑油加氢处理装置、酸性污水汽提塔装置、硫回收装置、气体分离装置或它们的组合中的流股的热能如约166MW。
总之,本公开内容描述了用于能量消耗减少的特定直接或间接装置间以及混合型装置内和装置间联合的配置和相关加工方案,其整合用于草根中级原油半转化精炼厂以提高来自低级废热源的特定部分的能量效率。本公开内容还描述了用于能量消耗减少的特定直接或间接装置间联合的配置和相关加工方案,其整合用于综合中级原油半转化精炼厂和芳烃联合装置以提高来自低级废物源的特定部分的能量效率。
对于所有工业,工业生产的经济性、全球能量供应的局限性和环境保护的现实都是关注点。据信,世界环境已经受部分由GHG到大气中的释放造成的全球变暖负面影响。此处描述的主题的实施方式可以缓解这些问题中的一些,并且在一些情况下,防止在减少它们的GHG排放方面有困难的某些精炼厂不得不关闭。通过实施此处描述的技术,可以通过来自低级废热源的特定部分的回收和再利用使精炼厂中的特定装置或精炼厂作为整体更高效并且污染性更低。
因此,已经描述了所述主题的特定实施方式。其他实施方式在所附权利要求的范围内。
Claims (25)
1.一种在原油精炼设备中实施的方法,所述方法包括:
利用多个热交换器,使用在原油精炼设备中的第二多个装置中的第二多个流股加热在所述原油精炼设备中的第一多个装置中的第一多个流股,所述多个热交换器接收所述第一多个流股中的至少一个和所述第二多个流股中的至少一个。
2.根据权利要求1所述的方法,其中所述第一多个装置包括胺再生装置、芳烃联合装置苯提取单元、酸性污水汽提塔装置、硫回收装置、气体分离装置,并且其中所述第二多个装置包括芳烃装置二甲苯产物分离单元、加氢裂化装置、柴油加氢处理装置。
3.根据权利要求2所述的方法,其中加热所述第一多个流股包括使用所述第二多个流股直接加热所述第一多个流股。
4.根据权利要求3所述的方法,其中直接加热所述流股包括:
在第一热交换器中,使用在所述芳烃装置二甲苯产物分离单元中的提余液塔塔顶产物流股的支流加热在所述胺再生装置中的酸性气体再生塔塔底产物流股;
在第二热交换器中,使用在所述柴油加氢处理装置中的柴油汽提塔塔底流股加热在所述酸性污水汽提塔装置中的汽提塔塔底流股的支流;
在第三热交换器中,使用在所述芳烃装置二甲苯产物分离单元中的提取塔塔顶产物流股的支流加热所述汽提塔塔底流股的支流;
在第四热交换器中,使用进料到第一阶段反应冷高压分离器的进料流股加热在所述硫回收装置中的胺再生塔塔底产物流股的支流;
在第五热交换器中,使用离开所述第二热交换器的所述柴油汽提塔塔底流股加热在所述气体分离装置中的C3/C4分割塔塔底流股的支流;
在第六热交换器中,使用离开所述第五热交换器的所述柴油汽提塔塔底流股加热在所述气体分离装置中的脱乙烷塔塔底产物流股的支流;
在第七热交换器中,使用所述提余液塔塔顶产物流股的支流加热在所述芳烃联合装置苯提取单元中的苯塔塔底产物流股的支流;和
在第八热交换器中,使用进料到在所述加氢裂化装置中的第二阶段反应冷高压分离器的进料流股加热在所述芳烃联合装置苯提取单元中的提余液塔塔底流股的支流。
5.根据权利要求4所述的方法,其中所述第一热交换器和所述第七热交换器彼此并联地流体连接,其中所述第二热交换器、所述第五热交换器和所述第六交换器彼此串联地流体连接,其中所述第二热交换器和所述第三热交换器彼此并联地流体连接。
6.根据权利要求4所述的方法,其中直接加热所述流股包括:
在热交换器A中,使用在所述柴油加氢处理装置中的柴油汽提塔塔顶流股加热所述石脑油分割塔塔底产物流股的支流;
在热交换器B中,使用所述提余液塔塔顶产物流股加热在所述芳烃联合装置苯提取单元中的石脑油分割塔塔底流股的支流;
在热交换器C中,使用在所述加氢裂化装置中的产物汽提塔流股加热所述石脑油分割塔塔底产物流股的支流;
在热交换器D中,使用在所述加氢裂化装置中的柴油产物流股加热所述石脑油分割塔塔底产物流股的支流;
在热交换器E中,使用来自在所述加氢裂化装置中的主分馏塔的煤油产物冷却流股加热所述石脑油分割塔塔底产物流股的支流;和
在热交换器F中,使用在所述加氢裂化装置中的煤油循环回流流股加热所述石脑油分割塔塔底产物流股的支流。
7.根据权利要求6所述的方法,其中使所述石脑油分割塔塔底产物流股的支流并行地流动到所述热交换器A、所述热交换器B、所述热交换器C、所述热交换器D、所述热交换器E和所述热交换器F。
8.根据权利要求5所述的方法,其中所述热交换器、所述热交换器B、所述热交换器C、所述热交换器D、所述热交换器E和所述热交换器F彼此并联地流体连接,其中所述第一热交换器和所述第七热交换器的组合与所述热交换器B彼此串联地流体连接。
9.根据权利要求6所述的方法,所述方法还包括:
使经加热的所述石脑油分割塔塔底产物流股的支流流动到所述芳烃联合装置苯提取单元;
使经加热的所述酸性污水汽提塔流股的支流的支流流动到所述酸性污水汽提塔装置;
使经加热的所述C3/C4分割塔塔底流股和所述脱乙烷塔塔底产物流股的支流流动到所述气体分离装置;
使经加热的所述胺再生塔塔底产物流股的支流流动到所述硫回收装置;和
使经加热的所述酸性气体再生塔塔底冷流股的支流流动到所述胺再生装置。
10.根据权利要求2所述的方法,其中加热所述第一多个流股包括使用所述第二多个流股间接加热所述第一多个流股。
11.根据权利要求10所述的方法,其中所述缓冲流体包括油或水中的至少一种。
12.根据权利要求10所述的方法,其中加热所述第一多个流股包括使用所述第二多个流股经由缓冲流体间接加热所述第一多个流股。
13.根据权利要求12所述的方法,其中经由缓冲流体间接加热所述第一多个流股包括:
在第一热交换器中,使用提余液塔塔顶产物流股加热所述缓冲流体的支流;
在第二热交换器中,使用在所述芳烃装置二甲苯产物分离单元中的提取塔塔顶产物流股加热所述缓冲流体的支流;
在第三热交换器中,使用进料到在所述加氢裂化装置中的冷高压分离器的第一阶段反应进料流股加热所述缓冲流体的支流;和
将经加热的所述缓冲流体的支流收集在缓冲流体收集集管中。
14.根据权利要求13所述的方法,其中所述第一热交换器、所述第二热交换器和所述第三热交换器彼此并联地流体连接。
15.根据权利要求14所述的方法,所述方法还包括直接加热所述流股,其中直接加热所述流股包括:
在热交换器A中,使用在所述柴油加氢处理装置中的柴油汽提塔塔顶流股加热所述石脑油分割塔塔底产物流股的支流;
在热交换器B中,使用所述提余液塔塔顶产物流股的支流加热在所述芳烃联合装置苯提取单元中的石脑油分割塔塔底流股的支流;
在热交换器C中,使用在所述加氢裂化装置中的产物汽提塔流股加热所述石脑油分割塔塔底产物流股的支流;
在热交换器D中,使用在所述加氢裂化装置中的柴油产物流股加热所述石脑油分割塔塔底产物流股的支流;
在热交换器E中,使用来自在所述加氢裂化装置中的主分馏塔的煤油产物冷却流股加热所述石脑油分割塔塔底产物流股的支流;和
在热交换器F中,使用在所述加氢裂化装置中的煤油循环回流流股加热所述石脑油分割塔塔底产物流股的支流。
16.根据权利要求15所述的方法,其中使所述石脑油分割塔塔底产物流股的支流并行地流动到所述热交换器A、所述热交换器B、所述热交换器C、所述热交换器D、所述热交换器E和所述热交换器F。
17.根据权利要求15所述的方法,其中所述热交换器A、所述热交换器B、所述热交换器C、所述热交换器D、所述热交换器E和所述热交换器F彼此并联地流体连接。
18.根据权利要求15所述的方法,其中所述提余液塔塔顶产物流股不需要额外的冷却。
19.根据权利要求18所述的方法,其中使用所述第一热交换器通过间接加热来冷却所述提余液塔塔顶产物流股的一部分,并且使用所述热交换器B通过直接加热来冷却所述提余液塔塔顶产物流股的一部分。
20.根据权利要求16所述的方法,所述方法还包括:
使来自所述缓冲流体收集集管的经加热的缓冲流体流动到所述芳烃联合装置苯提取单元、所述酸性污水汽提塔装置、所述硫回收装置、所述胺再生装置和所述气体分离装置;
在第四热交换器中,使用经加热的所述缓冲流体的支流加热在所述芳烃联合装置苯提取单元中的苯塔塔底产物流股;
在第五热交换器中,使用经加热的所述缓冲流体的支流加热在所述芳烃联合装置苯提取单元中的提余液分割塔塔底产物流股;
在第六热交换器中,使用经加热的所述缓冲流体的支流加热在所述酸性污水汽提塔装置中的酸性污水汽提塔塔底产物流股;
在第七热交换器中,使用经加热的所述缓冲流体的支流加热在所述硫回收装置中的胺再生塔塔底产物流股;
在第八热交换器中,使用经加热的所述缓冲流体的支流加热在所述胺再生装置中的酸性气体再生塔塔底产物流股;
在第九热交换器中,使用经加热的所述缓冲流体的支流加热在所述气体分离装置中的C3/C4分割塔塔底流股;和
在第十热交换器中,使用经加热的所述缓冲流体的支流加热在所述气体分离装置中的脱乙烷塔塔底产物流股。
21.根据权利要求20所述的方法,其中使经加热的所述缓冲流体首先流动到所述芳烃联合装置苯提取单元,然后流动到所述酸性污水汽提塔装置,然后流动到所述硫回收装置,然后流动到所述胺再生装置,然后流动到所述气体分离装置。
22.根据权利要求21所述的方法,所述方法还包括使离开所述第十热交换器的经加热的所述缓冲流体流动到缓冲流体罐。
23.根据权利要求13所述的方法,其中所述提取塔塔顶产物流股的冷却需求基本上为0MW。
24.一种在原油精炼设备中实施的系统,所述系统被配置为实施根据权利要求1所述的方法。
25.根据权利要求24所述的系统,其中所述系统包括流动控制系统。
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