WO2012009965A1 - 低温甲醇洗原料气冷却器 - Google Patents

低温甲醇洗原料气冷却器 Download PDF

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Publication number
WO2012009965A1
WO2012009965A1 PCT/CN2011/001202 CN2011001202W WO2012009965A1 WO 2012009965 A1 WO2012009965 A1 WO 2012009965A1 CN 2011001202 W CN2011001202 W CN 2011001202W WO 2012009965 A1 WO2012009965 A1 WO 2012009965A1
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WIPO (PCT)
Prior art keywords
heat exchange
heat exchanger
tube
casing
heat
Prior art date
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Ceased
Application number
PCT/CN2011/001202
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English (en)
French (fr)
Inventor
张贤安
王健良
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Zhenhai Petrochemical Jianan Engineering Co Ltd
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Zhenhai Petrochemical Jianan Engineering Co Ltd
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Application filed by Zhenhai Petrochemical Jianan Engineering Co Ltd filed Critical Zhenhai Petrochemical Jianan Engineering Co Ltd
Priority to JP2013519939A priority Critical patent/JP5480450B2/ja
Priority to US13/812,673 priority patent/US20130206366A1/en
Priority to KR1020127033779A priority patent/KR20130105311A/ko
Priority to EP11809154.5A priority patent/EP2597411A4/en
Priority to CN2011800090731A priority patent/CN103025406A/zh
Publication of WO2012009965A1 publication Critical patent/WO2012009965A1/zh
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F1/00—Tubular elements; Assemblies of tubular elements
    • F28F1/10—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses
    • F28F1/12—Tubular elements and assemblies thereof with means for increasing heat-transfer area, e.g. with fins, with projections, with recesses the means being only outside the tubular element
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
    • C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/001—Casings in the form of plate-like arrangements; Frames enclosing a heat exchange core
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/202—Alcohols or their derivatives
    • B01D2252/2021—Methanol
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • 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
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0022—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for chemical reactors
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the invention relates to a cooler, in particular to a low temperature methanol washing feed gas cooler. Background technique
  • the existing cooler includes a heat exchanger, as shown in FIG. 1 , wherein the heat exchanger further comprises a casing and a heat exchange tube supported by the tube plate in the casing.
  • the heat exchanger When cooling, the raw material is taken away from the shell.
  • the heat exchange medium takes the tube process, that is, the raw material gas inlet and the raw material gas outlet are opened on the shell, and the heat exchange medium inlet connected to one end of the heat exchange tube is also connected to the shell and connected to the other end of the heat exchange tube.
  • the outlet of the heat exchange medium when there are multiple heat exchange mediums, the inlet and outlet of the heat exchange medium are correspondingly arranged to meet different heat exchange medium flow in the corresponding heat exchange tubes.
  • the current heat exchange medium mainly uses C02 product gas (operating pressure is usually: 0.19Mpa), H2S concentration tower tail gas (operating pressure is usually: 0.08Mpa), and syngas (operating pressure is usually: 5.0Mpa), so 40°C 5.5Mpa of raw material gas enters the shell of the raw material gas cooler, and after cooling through the heat exchanger, it is cooled to between -13 °C and -20 °C.
  • the above heat exchanger can achieve the purpose of cooling the low-temperature methanol washing raw material gas, but since the raw material gas is a high-pressure medium, the heat exchanger shell and the tube sheet can withstand higher pressure, that is, heat exchange.
  • the housing of the device needs to be made into a thick-walled container that is resistant to rolling, and the tube sheet is made of a thick tube sheet. Obviously, such a structure will inevitably increase the manufacturing cost of the cooler, and there is a defect of high investment cost. Summary of the invention
  • the technical problem to be solved by the present invention is to provide a low-cost low-temperature methanol washing raw material gas cooler in view of the above state of the art.
  • the low temperature methanol washing feed gas cooler comprising a heat exchanger, wherein: the heat exchanger is composed of a first heat exchanger and a second heat exchanger
  • the first heat exchanger comprises a first housing and a first heat exchange tube supported by the first tube sheet in the first housing, the first housing having a raw material gas inlet and a raw material gas outlet; Further, on the first casing, a heat exchange medium inlet communicating with one end of the first heat exchange tube and a heat exchange medium outlet communicating with the other end of the first heat exchange tube are further disposed;
  • the second heat exchanger a second housing and a second heat exchange tube supported by the second tube sheet in the second housing, wherein the second housing is provided with a raw material gas inlet communicating with one end of the second heat exchange tube And a raw material gas outlet communicating with the other end of the second heat exchange tube, and at the same time, a heat exchange medium inlet and a heat exchange medium outlet are further opened on the second casing.
  • the heat exchange medium inlet and the heat exchange medium outlet on the first heat exchanger housing respectively have A plurality of heat exchange medium inlets are respectively a CO 2 product gas inlet and a syngas inlet, and a plurality of heat exchange medium outlets are correspondingly a CO 2 product gas outlet and a syngas outlet.
  • the tail gas of the H2S concentration tower is taken away from the shell side of the second heat exchanger, so that the second shell and the second tube sheet of the second heat exchanger can adopt relatively thinner plates to further reduce the manufacturing cost.
  • the heat exchange medium is configured to be a shell, and thus, in actual use,
  • the H2S concentration tower tail gas with lower operating pressure can be taken to the shell side of the second heat exchanger, so that although the first casing still needs to be a thick-walled container with high pressure resistance, the first tube sheet still uses a thick tube sheet, but Since the volume of the first heat exchanger at this time is much smaller than the volume of the original heat exchanger, and the second casing and the second tube sheet can be made of thinner plates, the material cost and production cost of the invention will be greatly improved. Low, in meeting the requirements of the production process, can significantly save the material and manufacturing cost of the cooler, and the structure is reasonable and reliable, which makes the product more competitive in the market.
  • FIG. 1 is a schematic structural view of a prior art cooler.
  • FIG. 2 is a schematic structural view of an embodiment of the present invention. detailed description
  • the low temperature methanol washing feed gas cooler comprises a first heat exchanger 1, a second heat exchanger 2 and a spray methanol device 3, wherein the two heat exchangers adopt a conventional structure, that is, a first heat exchange
  • the first housing 11 and a plurality of first heat exchange tubes 12 supported by the first tube sheet in the first housing 11 are provided with a raw material gas inlet gl and a raw material gas outlet g2.
  • a heat exchange medium inlet and a heat exchange medium outlet are further disposed on the first casing.
  • the heat exchange medium inlet and the heat exchange medium outlet on the first heat exchanger shell are respectively provided, that is, There are two syngas inlets fl, ⁇ and two syngas outlets el, e2, two C02 product gas inlets bl, b2 and two C02 product gas outlets a1, a2.
  • the plurality of first heat exchange tubes are divided into two groups, one end of the first heat exchange tube is connected to the synthesis gas inlet, and the other end of the first heat exchange tube is connected to the synthesis gas outlet, so that the synthesis gas flows in the first
  • One part of the first heat exchange tube is connected to the C02 product gas inlet, and the other end of the other first heat exchange tube is connected to the C02 product gas outlet, so that the C02 product gas flows.
  • the heat exchange tube of the first heat exchanger In another part of the heat exchange tube of the first heat exchanger.
  • the second heat exchanger 2 includes a second housing 21 and a second heat exchange tube 22 supported by the second tube plate in the second housing, and the second housing is opened and replaced by the second
  • the second housing 21 is further provided with a heat exchange medium inlet and a heat exchange medium outlet, where the heat exchange medium is the H2S concentration tower exhaust gas, that is, the H2S concentration tower Exhaust gas inlet hi and H2S concentration tower exhaust gas outlet h2.
  • the heat exchange medium is the H2S concentration tower exhaust gas, that is, the H2S concentration tower Exhaust gas inlet hi and H2S concentration tower exhaust gas outlet h2.
  • the above-described spray methanol apparatus 3 is the same as the prior art, and methanol is injected to prevent moisture from freezing during cooling.
  • the raw material gas is divided into two paths after spraying the methanol device, and all the way into the first heat exchanger, that is, the shell side of the first heat exchanger, and the syngas and C02 product gas of the first heat exchanger tube. Perform heat exchange.
  • the other way enters the second heat exchanger, that is, the tube path of the second heat exchanger is exchanged with the tail gas of the H2S concentration tower that goes through the shell side of the second heat exchanger.
  • the raw material gas cooled by the heat exchange between the first heat exchanger and the second heat exchanger is combined and proceeds to the next process.
  • the second heat exchanger shell side only needs to adopt a thin wall plate with a design pressure of 0.3 MPa, and the tube plate adopts a thin tube plate.
  • the total cost of the invention can be reduced by 30. % ⁇ 40%, the material cost and production cost are significantly reduced.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Geometry (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Description

低温甲醇洗原料气冷却器
技术领域
本发明涉及一种冷却器， 具体指一种低温甲醇洗原料气冷却器。 背景技术
为了满足下一步工艺的需求，需要对低温甲醇洗原料气进行冷却，通常该冷却工艺 是通过冷却器来实现的。 现有的冷却器包括有一台换热器， 如图 1所示， 其中， 换热器 又包含有壳体和位于壳体内由管板支撑的换热管， 冷却时， 原料气走壳程， 换热介质走 管程， 即在壳体上开有原料气入口和原料气出口， 同时在壳体上还开有与换热管一端相 连通的换热介质入口和与换热管另一端相连通的换热介质出口， 当换热介质有多种时， 换热介质的入口和出口就相应的设置有多个， 以满足不同换热介质在相应的换热管中流 动。 目前的换热介质主要采用 C02产品气 (操作压力通常为： 0.19Mpa)、 H2S浓缩塔尾 气 (操作压力通常为： 0.08Mpa)、 合成气 (操作压力通常为： 5.0Mpa)， 这样 40°C、 5.5Mpa 原料气进入原料气冷却器壳程， 经过换热器后冷却到 -13°C〜- 20°C之间。
采用上述换热器，虽然能达到冷却低温甲醇洗原料气的目的，但由于原料气为高压 介质， 这就要求换热器的壳体和管板能承受较高的压力， 也就是， 换热器的壳体需要做 成耐髙压的厚壁容器， 管板采用厚管板。 显然， 这样的结构必然会提高冷却器的制作成 本， 而出现投资费用高的缺陷。 发明内容
本发明所要解决的技术问题是针对上述现有技术现状而提供一种成本低的低温甲 醇洗原料气冷却器。
本发明解决上述技术问题所采用的技术方案为： 该低温甲醇洗原料气冷却器， 包括 换热器， 其特征在于： 所述的换热器由第一换热器和第二换热器组成， 其中第一换热器 包含有第一壳体和位于第一壳体内由第一管板支撑的第一换热管，所述第一壳体上开有 原料气入口和原料气出口， 同时在该第一壳体上还开有与所述第一换热管一端相连通的 换热介质入口和与该第一换热管另一端相连通的换热介质出口； 上述第二换热器包含有 第二壳体和位于第二壳体内由第二管板支撑的第二换热管，所述第二壳体上则开有与所 述第二换热管一端相连通的原料气入口和与所述第二换热管另一端相连通的原料气出 口， 同时在该第二壳体上还开有换热介质入口和换热介质出口。 优先地，由于 H2S浓缩塔尾气的操作压力要低于 C02产品气和合成气的操作压力， 因此， 在所述的第一换热器壳体上的换热介质入口和换热介质出口分别有多个， 多个换 热介质入口分别为 C02产品气入口和合成气入口，而多个换热介质出口则相应地为 C02 产品气出口和合成气出口。这样让 H2S浓缩塔尾气走第二换热器的壳程，使第二换热器 的第二壳体和第二管板可以采用相对更薄的板材， 以进一步降低制作成本。
与现有技术相比， 由于本发明改成两台换热器进行冷却， 且其中第二换热器改为原 料气走管程， 换热介质走壳程的结构， 因而在实际使用时， 可以使操作压力较低的 H2S 浓缩塔尾气走第二换热器的壳程， 这样， 虽然第一壳体仍需要做成耐高压的厚壁容器， 第一管板仍采用厚管板， 但由于此时的第一换热器体积远小于原先一台的换热器体积， 且第二壳体和第二管板可以采用较薄的板材， 故本发明的材料费用和制作成本将大大较 低， 在满足生产工艺的要求下， 能明显节省冷却器的材料及制造费用， 且结构合理、 可 靠， 而使该产品更具市场竞争力。 附图说明
图 1为现有技术中冷却器的结构示意图。
图 2为本发明实施例的结构示意图。 具体实施方式
以下结合附图实施例对本发明作进一步详细描述。
如图 2所示， 该低温甲醇洗原料气冷却器包括第一换热器 1、 第二换热器 2和喷淋 甲醇装置 3，该两换热器采用常规的结构， 即第一换热器 1包含有第一壳体 11和位于第 一壳体内由第一管板支撑的多个第一换热管 12，第一壳体 11上开有原料气入口 gl和原 料气出口 g2，同时在该第一壳体上还开有换热介质入口和换热介质出口，在本实施例中， 第一换热器壳体上的换热介质入口和换热介质出口分别有多个， 即分别有两个合成气入 口 fl、 β和两个合成气出口 el、 e2， 两个 C02产品气入口 bl、 b2和两个 C02产品气 出口 al、 a2。 上述多个第一换热管分成两组， 一组第一换热管的一端连于合成气入口， 一组第一换热管的另一端连于合成气出口， 使合成气流动在第一换热器的部分换热管 内； 而另一组第一换热管的一端连于 C02产品气入口， 另一组第一换热管的另一端连 于 C02产品气出口， 使 C02产品气流动在第一换热器的另一部分换热管内。
同样， 上述第二换热器 2包含有第二壳体 21和位于第二壳体内由第二管板支撑的 第二换热管 22，第二壳体上则开有与所述第二换热管一端相连通的原料气入口和与所述 第二换热管另一端相连通的原料气出口， 在本实施例中第二换热管的原料气入口有四 个， 如图 2中标号为 dl、 d2、 d3、 d4， 对应地第二换热管的原料气出口也有四个， 如图 2中标号为 cl、 c2、 c3、 c4; 同时在该第二壳体 21上还开有换热介质入口和换热介质出 口， 在这里换热介质为 H2S浓缩塔尾气， 即为 H2S浓缩塔尾气入口 hi和 H2S浓缩塔 尾气出口 h2。
上述喷淋甲醇装置 3与现有技术相同， 注入甲醇以防止水分在冷却过程中结冰。 冷却时， 原料气经喷淋甲醇装置后分成两路，一路进入第一换热器， 即走第一换热 器的壳程， 与走第一换热器管程的合成气和 C02产品气进行热交换。 另一路进入第二 换热器， 即走第二换热器的管程， 与走第二换热器壳程的 H2S浓缩塔尾气进行热交换。 经第一换热器和第二换热器换热冷却后的原料气又合成一起， 进入下一工序。 这样， 第 二换热器壳程仅需要采用设计压力为 0.3Mpa的薄壁板材， 管板采用薄管板， 在与现有 冷却器同等的换热效果下， 本发明的总费用能降低 30%~40%, 使材料费用和制作成本 得到明显地降低。

Claims

权 利 要 求
1、 一种低温甲醇洗原料气冷却器， 包括换热器， 其特征在于： 所述的换热器由第 一换热器 (1)和第二换热器 (2)组成，其中第一换热器 (1)包含有第一壳体 (11)和位于第一壳 体 (11)内由第一管板支撑的第一换热管 (12)， 所述第一壳体 (11)上开有原料气入口 (gl)和 原料气出口 (g2)， 同时在该第一壳体 (11)上还开有与所述第一换热管 (12)—端相连通的换 热介质入口和与该第一换热管 (12)另一端相连通的换热介质出口； 上述第二换热器 (2)包 含有第二壳体 (21)和位于第二壳体 (21)内由第二管板支撑的第二换热管 (22),所述第二壳 体 (21)上则开有与所述第二换热管 (22)—端相连通的原料气入口和与所述第二换热管 (22) 另一端相连通的原料气出口 (g2)， 同时在该第二壳体 (21)上还开有换热介质入口和换热 介质出口。
2、 根据权利要求 1所述的低温甲醇洗原料气冷却器， 其特征在于： 所述的第一换 热器 (1)壳体上的换热介质入口和换热介质出口分别有多个，所述多个换热介质入口分别 为 C02产品气入口和合成气入口， 所述多个换热介质出口为相应地 C02产品气出口和 合成气出口。
PCT/CN2011/001202 2010-07-23 2011-07-22 低温甲醇洗原料气冷却器 Ceased WO2012009965A1 (zh)

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JP2013519939A JP5480450B2 (ja) 2010-07-23 2011-07-22 低温メタノール洗浄用原料ガスの冷却装置
US13/812,673 US20130206366A1 (en) 2010-07-23 2011-07-22 Cooler for Feed Gas Of Low-Temperature Methanol Washing
KR1020127033779A KR20130105311A (ko) 2010-07-23 2011-07-22 저온 메탄올 세척 원료가스 냉각기
EP11809154.5A EP2597411A4 (en) 2010-07-23 2011-07-22 COOLER FOR A FILLING GAS IN A LOW TEMPERATURE METHANOL WASHING
CN2011800090731A CN103025406A (zh) 2010-07-23 2011-07-22 低温甲醇洗原料气冷却器

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