CN101641462B - 烟气冷却和净化系统 - Google Patents
烟气冷却和净化系统 Download PDFInfo
- Publication number
- CN101641462B CN101641462B CN2008800094336A CN200880009433A CN101641462B CN 101641462 B CN101641462 B CN 101641462B CN 2008800094336 A CN2008800094336 A CN 2008800094336A CN 200880009433 A CN200880009433 A CN 200880009433A CN 101641462 B CN101641462 B CN 101641462B
- Authority
- CN
- China
- Prior art keywords
- flue gas
- gas
- cooler
- gas cooler
- cooling
- Prior art date
Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 149
- 239000003546 flue gases Substances 0.000 title claims abstract description 148
- 238000001816 cooling Methods 0.000 title claims abstract description 89
- 238000004140 cleaning Methods 0.000 title abstract description 4
- 239000007789 gases Substances 0.000 claims abstract description 117
- 239000002826 coolants Substances 0.000 claims abstract description 41
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminum Chemical compound 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[Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 38
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 37
- 239000004411 aluminium Substances 0.000 claims abstract description 36
- 239000003507 refrigerants Substances 0.000 claims description 20
- 238000005108 dry cleaning Methods 0.000 claims description 9
- 238000009792 diffusion process Methods 0.000 claims description 5
- 239000011257 shell materials Substances 0.000 claims description 3
- 238000005452 bending Methods 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 230000004087 circulation Effects 0.000 abstract description 9
- 239000000428 dust Substances 0.000 abstract description 3
- 238000005203 dry scrubbing Methods 0.000 abstract 1
- 239000011159 matrix materials Substances 0.000 abstract 1
- 239000011901 water Substances 0.000 description 43
- 239000003570 air Substances 0.000 description 18
- 238000010521 absorption reactions Methods 0.000 description 14
- 238000005057 refrigeration Methods 0.000 description 12
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- VOPWNXZWBYDODV-UHFFFAOYSA-N Chlorodifluoromethane Chemical compound 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Classifications
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- 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
- F28F9/02—Header boxes; End plates
- F28F9/04—Arrangements for sealing elements into header boxes or end plates
- F28F9/16—Arrangements for sealing elements into header boxes or end plates by permanent joints, e.g. by rolling
- F28F9/18—Arrangements for sealing elements into header boxes or end plates by permanent joints, e.g. by rolling by welding
- F28F9/182—Arrangements for sealing elements into header boxes or end plates by permanent joints, e.g. by rolling by welding the heat-exchange conduits having ends with a particular shape, e.g. deformed; the heat-exchange conduits or end plates having supplementary joining means, e.g. abutments
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25C—PROCESSES FOR THE ELECTROLYTIC PRODUCTION, RECOVERY OR REFINING OF METALS; APPARATUS THEREFOR
- C25C3/00—Electrolytic production, recovery or refining of metals by electrolysis of melts
- C25C3/06—Electrolytic production, recovery or refining of metals by electrolysis of melts of aluminium
- C25C3/22—Collecting emitted gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste 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
- F28D7/16—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 the conduits being arranged in parallel spaced relation
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- 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
- F28F1/02—Tubular elements of cross-section which is non-circular
- F28F1/025—Tubular elements of cross-section which is non-circular with variable shape, e.g. with modified tube ends, with different geometrical features
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B21/00—Obtaining aluminium
- C22B21/0038—Obtaining aluminium by other processes
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
- C22B7/02—Working-up flue dust
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- 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
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- 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
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Abstract
一种改进的烟气冷却器(10)或冷却器(10)组，其处理来自炼铝炉设备中的铝电解槽的烟气G。所述或每个烟气冷却器(10)具有进气室(14)；出气室(16)；以及在进气室和出气室之间延伸的气体冷却管(18)阵列。每个冷却管(18)具有钟形进口端(19)，其包括空气动力学弯曲的气体加速轮廓，其用于便于烟气G流线地流入管中。改进的烟气冷却器使其能够连接烟气冷却器以接收从铝电解槽引导来的热原始烟气G而不会被烟气中存在的烟尘和升华物阻塞。烟气一旦冷却，即可安全地送到干法净化型烟气净化设备。改进的烟气冷却器为使用来自烟气热能的系统的有利部分，其中闭路冷却剂循环系统使冷却剂循环经过烟气冷却器和热交换装置(24)。由热交换装置(24)从冷却剂中提取的热能用于增加连接到热交换装置的进一步设备的效率。
Description
烟气冷却和净化系统
技术领域
[0001] 本发明涉及对来自炼铝炉的烟气进行冷却的改进的气体冷却器。其进一步涉及用于炼铝炉设备的改进的烟气冷却和净化系统，以及用于从烟气中提取热量的系统。
背景技术
[0002] 炼铝炉，其包括很多铝电解槽（俗称“罐”），产生大量包含氟化氢，其他气体，颗粒，和升华物的热烟气。例如，每年生产300,000吨铝金属的炼铝炉将包括布置成四行的大约400个电解槽。这种电解槽系列每小时将产生大约3，600, 000标准立方米（Nm3/h) 烟气。必须净化原始烟气，在这方面使用的公知类型的气体净化工艺是所谓的“干法净化”工艺。使用此工艺的气体净化设备是可行的，例如，Drammensveien 165,0277 Oslo, Norway (Tel. +47 22 12 70 00)的 ALSTOM 电力环境控制系统。
[0003] 铝生产工业中的技术发展趋势是带风罩预烘类型的电解槽。这些增加了尺寸和能量输入，导致了烟气温度增加。最新型的电解槽系列中的烟气温度已经从原来的70-90摄氏度水平提高到现在的120-180摄氏度范围或更高。遗憾地，这种烟气温度相对于工艺和设备超过了使用干法净化工艺的气体净化设备的可接受温度水平。因此，包含烟尘或杂质的原始烟气必须在进入净化设备前被冷却。
[0004] 已知的是通过将冷环境空气混合到气体净化设备上游的烟气管道中来冷却铝电解槽产生的热原始烟气。气体/空气混合是简单且廉价的，但是当气体温度上升到或超过 150摄氏度，需要用于充分冷却的环境空气量变大并且冷却气体量增加。因此，气体净化设备的尺寸，推动气体经过净化设备的下游风扇的尺寸，以及设备能耗都相应地增加。这在建造和操作过程中都对设备经济性产生了不利影响。
[0005] 还已知的是通过使用直径喷射雾化水的蒸发冷却铝电解槽的烟气。尽管此系统减小了总的烟气量，还必须考虑由此产生的流量。此冷却系统的直接成本是适中的，但是其需要大量压缩空气来雾化喷射水，所以空气压缩的能耗是高的。此外，系统需要非常大量的新鲜纯净的冷却水，其在新鲜干净的水是珍贵资源的地区在经济上和环境上是不利的。另外， 假定过滤袋用于随后的气体净化设备，冷却烟气中的高湿度会水解标准聚酯型过滤袋，迫使过滤袋使用化学惰性更强并且非常昂贵的材料。
[0006] 在一些现有的炼铝炉设备中，已知的是在烟气被净化后通过使其经过热交换器以产生温水而用于加热，从而从烟气中回收热量。迄今为止，这种热量回收只在气体被净化后才可行，因为要不然原始烟气中的烟尘，升华物和其他杂质将趋于在热交换器表面上沉积为硬垢，这导致了热交换器中的阻塞和传热减小。而且，目前新的或更大的炼铝能力的厂房主要局限于热带或亚热带国家，其中用于加热的能量需求是有限的或不存在的，更大的需要一般为用于冷却的能量。
[0007] 已知的是使用气管型气体冷却器来冷却钢，硅铁和硅金属炉的热烟气。在这种冷却器中，烟气（其从炉经过烟气管道至冷却器）流经平行管束，而冷却剂在管的外部流过。这些气体中的烟雾和颗粒趋于形成冷却器管壁上的烟尘绝热层，其减小了冷却器中的
4传热。这类烟尘层可向下吹到可接受的厚度并且可通过沿管保持高气体速度而几乎完全去除，以此来在冷却器中保持可接受的传热。
[0008] 来自铝电解槽的烟气中的烟雾和颗粒相比于上述炉气中的烟雾和颗粒，当冲击湍流气流区域的表面和与气流成横向的表面时，具有强烈的形成如石头硬的硬垢的趋势。这些硬垢太硬且太致密，从而不能吹走以及通过管中或其他气体输送系统部分中的任何实际气体速度去除。除了在气体冷却器中具有绝热效果，这种硬垢趋于持续在冲击表面上和湍流区域中增长，直到冷却器完全阻塞。
[0009] 因此将理解的是上述气管型气体冷却器（以用于冷却来自金属炉的热烟气的形式）不适于用于净化来自铝电解槽的烟气。
发明内容
[0010] 根据本发明的一个方面，能够处理来自炼铝炉设备中的铝电解槽的热原始烟气的气体冷却器包括：
[0011] a)进气室；
[0012] b)出气室；以及
[0013] c)多个气体冷却管，每个冷却管在进气室中具有进口端并且在出气室具有出口端，所述进口端为钟形并包括空气动力学弯曲的气体加速轮廓，其用于便于热原始烟气流线地流入所述管中。
[0014] 原始烟气意味着烟气从炼铝炉电解槽系列未处理地排出，包含氟化氢，烟尘，升华物和其他杂质。
[0015] 冷却管的钟形进口设计成将从进入管的烟气流均勻加速，由此基本上防止了在管内部形成硬垢。也就是说，每个冷却管进口的上述钟形空气动力学弯曲加速区域促进了流线型流（或称层流，streamlined flow)加速并防止了流收缩（缩流效果）。在没有这种预防措施的情况下，湍流将导致烟气与冷却管的内表面冲突，引起了结垢。我们最佳的估计是优选实施例的冷却管中的气体速度将在大约20-30m/sec的范围内，其取决于气体温度。
[0016] 优选地，冷却管形成相互平行隔开的管阵列。冷却应在进气室和出气室的横截面大小上均勻隔开并且它们的进口和出口端应分别突出到进气室和出气室中。
[0017] 气体冷却器应包括围绕冷却管的冷却剂容器或套管，所述容器设有冷却剂进入和排出管道。因此，冷却器容器形成气体冷却器的部分外壳。优选地，冷却剂为水或其他适合液体。为了最大化热交换效率，冷却剂在管的外表面流经冷却剂容器的方向应与气体流经管的方向相反。
[0018] 在操作中，进气室连接到进口烟道，其将热烟气从铝电解槽送到气体冷却器，而出气室连接到出口烟道，其将输送冷却的烟气离开气体冷却器到气体净化设备中。
[0019] 进气室经由扩散的展开进口部分接收热原始烟气，其使从进口管道进入的烟气减速到相对低的速度使得烟气被稳定并均勻地流入冷却管的钟形进口阵列。进气室和出气室的相关横截面流区域和冷却管阵列被明智地选择使得进气室的扩散部分使热烟气减速到相对低的速度，而不产生将导致进气室中不可接受的结垢的湍流区域。我们最佳的估计是进气室中的气体速度应在大约8-12m/sec的范围内，其取决于气体温度。出口室从冷却管的出口端接收冷却烟气，经过收敛出口部分逐步地使其加速，并将其排放到烟道。优选地，进气室和出气室可从气体冷却器的冷却套管部分拆卸。其优点在于允许气室和冷却管的进入和排出部分的容易的拆卸和清洁（如果需要的话）。然而，这种清洁的需要被降到最低限度，因为上述措施避免了湍流。
[0020] 在本发明的另一方面，炼铝炉设备的烟气冷却和净化系统包括：
[0021] 多个铝电解槽，其在操作中排放热原始烟气；
[0022] 成气管热交换器形式的至少一个烟气冷却器，其包括多个冷却管，每个冷却管具有纵向延伸主轴线并且配置成接收并在其中通过流线型流形式的烟气，其速度矢量基本平行于管的主轴线；以及
[0023] 干法净化型烟气净化设备；
[0024] 连接至少一个烟气冷却器来从电解槽接收热原始烟气并将冷却的原始烟气送到烟气净化设备。
[0025] 想到烟气冷却器将接收120-250摄氏度温度范围的原始烟气，并将它们在60-120 摄氏度温度范围传到烟气净化设备。60-120摄氏度温度范围适于干法净化型烟气净化设备。
[0026] 烟气在进入烟气净化设备之前冷却是有利的，因为烟气从电解槽排出的温度超过了干法净化设备的可用范围。为了实现所需的烟气冷却，我们利用围绕烟气冷却器的冷却管的冷却剂套管作为闭路冷却剂循环系统的一部分，其将烟气冷却器连接到热交换装置， 所述热交换装置从冷却剂中提取热能并将其排放到环境中和/或将其送到进一步的设备。 优选地，闭路冷却剂循环系统使冷却剂流经冷却剂套管的方向与烟气流经冷却管的方向相反。方便的是闭路冷却剂循环系统中的冷却剂为水。
[0027] 热原始烟气在被送到干法净化设备之前冷却将对环境有利，因为这种冷却将改进净化媒介的吸热效率，由此改进从烟气中回收氟化氢的效率，所以减少了有害排放。另外， 烟气在气体净化工艺之前冷却将延长用于干法净化工艺的过滤袋的使用寿命。
[0028] 可存在进一步的有效优点，因为烟气在进入气体净化工艺之前冷却将允许电解槽系列的操作者增加电解槽系列的电流而对气体净化工艺没有不利效果。
[0029] 炼铝炉可具有大量电解槽，并处理产生烟气的大体积流率，我们倾向于多个烟气冷却器相互平行地连接以从电解槽接收烟气。例如，每个这种烟气冷却器可从大约50到 100个电解槽接收烟气。
[0030] 在进一步的方面，本发明提供了一种炼铝炉设备的原始烟气冷却和净化方法，所述炼铝炉设备设有干法净化型烟气净化设备，所述方法包括以下步骤：
[0031] a)将初始温度超过烟气净化设备可接受范围的原始烟气经过多个气体冷却器，所述气体冷却器相互平行布置以接收原始烟气，所述气体冷却器包括冷却管阵列，其配置成接收并在其中通过流线型流形式的原始烟气；
[0032] b)在冷却管外部流过冷却剂以通过将烟气热量传到冷却剂而冷却原始烟气，由此将烟气冷却至烟气净化设备可接受的温度；以及
[0033] c)将冷却的原始烟气送到烟气净化设备。
[0034] 热能可由热交换装置从冷却剂中提取并用于增加连接到热交换装置的进一步设备的效率。
[0035] 在本发明的另一方面，炼铝炉设备设有烟气冷却系统，所述系统包括：[0036] 成气管热交换器形式的至少一个烟气冷却器，其包括多个冷却管，每个冷却管具有纵向延伸主轴线并且配置成接收并在其中通过流线型流形式的烟气，其速度矢量基本平行于所述管的主轴线；以及
[0037] 冷却剂循环系统，其使冷却剂流过冷却管外部。
[0038] 我们倾向于冷却剂循环系统为闭路冷却剂循环系统并且热交换装置经过闭路冷却剂循环系统连接到烟气冷却器以冷却所述冷却剂。热交换装置通过将热量排放到环境中和/或与进一步的设备热交换而冷却所述冷却剂。因此，热交换装置可接下来通过进一步的闭路冷却剂循环系统连接到进一步的设备并且由热交换装置从冷却剂中提取的热能然后可用于增加进一步设备的效率。这种进一步的设备可包括下列的至少一个：
[0039] 组合式循环发电设备（例如锅炉水的预热器）；
[0040] 脱盐设备；
[0041] 区域加热线路（district heating scheme)。
[0042] 通过研读下面的描述和权利要求，本发明的其他方面将变得明显。
附图说明
[0043] 现在将参照附图描述本发明的示例性实施例，其中：
[0044] 图1是根据本发明构建的炼铝炉设备的部分的方框图；
[0045] 图2是图1中使用的烟气冷却系统的示意图；以及
[0046] 图3是图2的烟气冷却器的部分的纵剖图。
具体实施方式
[0047] 应理解的是附图仅示出了本发明的示例性实施例。图中所示以及如下所述的每个特征或系统参数在系统的具体设计中将易于变化，以适应特殊炼铝炉电解槽系列的需要。
[0048] 在图1中，炼铝炉电解槽系列2产生携带颗粒和升华物的热烟气G。这种热的原始烟气经过气体冷却器10，该气体冷却器10在烟气经过干法净化型烟气净化设备4之前将其冷却。在气体冷却器10中，冷却剂22将热量从热原始烟气G中带走。将能够使用环境水作为冷却剂22来通过开路冷却剂循环系统直接冷却烟气G。然而如所示的，优选的是通过在热交换装置M中从冷却剂22提取热量来冷却冷却剂22，所述热交换装置M通过闭路冷却剂循环系统连接至气体冷却器10。热交换装置M然后可通过将热量排放到环境E和/ 或通过进一步的闭路冷却剂循环系统与进一步的设备44热交换来冷却冷却剂，如下所述。
[0049] 现在转向图2，热原始烟气由烟气管道从炼炉电解槽系列收集，在此实施例中为通过4个主烟气联管管道12收集。假定炼炉量为每年300，000吨铝，电解槽系列将生产大约 3，600，000Nm7h烟气G。因此每个管道12将处理大约900，000Nm7h烟气G。每个联管管道 12直径为大约5-6m并且在本例中示出为具有其自己的气体冷却器10。如下所述，每个气体冷却器包括气管型热交换器，其尤其适于处理热原始烟气。
[0050] 每个气体冷却器10具有进气室14以使从相应联管管道12接收的热烟气减速并稳定；并且具有出气室16以将冷却烟气排放到烟气联管管道的延伸管20。进气室14直径为大约6-7m并且每个都具有扩散展开进口部分15，其使烟气基本没有湍流地减速到大约 8-12m/sec的相对低的速度。出气室16具有收敛收缩轮廓以增加冷却烟气G进入烟气管道20的速度。
[0051] 烟气G的冷却通过将热量从烟气传递到在闭循环系统中流通的冷却水22(或其他冷却剂）而实现。泵（未示出）使冷却剂通过管道23流通，所述管道23将热交换装置 M (其例子如下所述）连接到形成每个气体冷却器10的部分外壳或外罩的冷却剂容器或套管沈。冷却剂套管沈连接到相互平行的冷却系统中，它们的进观和出口 30分别连接到冷却系统的“冷”和“热”支架32，34。
[0052] 在此实施例中，气体冷却器10将在其进口 14的烟气温度从大约150摄氏度降低至在其出口 16的大约115摄氏度。在出口 16的温度下，烟气充分冷却以进入前述的干法净化型的气体净化设备。同时，冷却水22的温度从在吸热冷却站M出口的大约85摄氏度增加至在冷却套管沈出口的大约120摄氏度。
[0053] 通常，气体冷却器10将为圆柱形，冷却剂套管沈与进气室和出气室14，16的直径相同。顶部气体冷却器10的部分冷却剂套管沈壁在图2中剖开示出以显示占据气体冷却器内部并在进气室和出气室14，16之间连接的一捆气体冷却管18。在每个气体冷却器10 内将有比图2所示更多的冷却管18 ；大约500-900个管（取决于管直径)，将在冷却剂套管 26和进气室和出气室14，16的横截面上等距隔开。还如图2所示，为了使从烟气G到冷却剂22的热传递最有效，冷却剂流经冷却剂套管沈的大体方向布置成与烟气G流经热交换管18的方向相反。
[0054] 图2中为了便于显示，气体冷却器10以其水平对齐的主要纵向延伸轴线示出。然而，在图3中，气体冷却器10垂直定向，此为气管型热交换器的优选定向。烟气G在冷却管 18的顶部端进入冷却管18，而水或其他冷却剂在其底部端进入冷却剂套管26，向上流过冷却管18来将其冷却，并且在套管的顶部端离开套管。事实上因为水冷却剂与管接触而加热，其变得不再密集并且自然地升到导管顶部，所以辅助了水冷却剂的流通。
[0055] 因为冷却管18携带来自电解槽系列的热原始烟气，它们被精心地空气动力学设计以控制烟尘沉积并将由烟气产生的硬垢控制在最小量，其保持了通过冷却管18壁到流过冷却剂套管26的冷却剂22的有效传热。在本文中，空气动力学设计使烟气流线或速度矢量保持基本上平行于冷却管18的壁，即基本上平行于其纵向轴线。
[0056] 如图3清晰所示，每个冷却管18具有突出到进气室14中的进口端19和突出到出气室16中的出口端。管壁除了进口端19以外都是直的，每个进口端19包括空气动力学轮廓的钟口收敛部分，其设计成将进入冷却管18的烟气从上述进气室中大约8-12m/sec的速度均勻加速为冷却管中大约20-30m/sec的速度。保持流线型流向冷却管18同时增加流速， 避免了湍流并防止了在其内壁上形成硬垢。
[0057] 获得最佳烟气速度的冷却管18的尺寸将为若干变量（例如压力损失，热交换效率，污垢因素，以及气体冷却器10的总体尺寸）之间的折衷。最佳化将在实践测试过程中产生。如涉及尺寸的一个例子，每个冷却管18直径可为大约6. 4m,长为大约20-30m。
[0058] 将从图3注意到进气室和出气室14，16可从气体冷却器10的冷却套管部分沈拆除。通过提供具有端板观，30的冷却套管部分沈为其提供了便利。端板观，30不仅将增压冷却剂套管部分26分别从进气室和出气室14，16分开，还提供了螺栓连接法兰31，32与进气室和出气室14，16上的类似螺栓连接法兰33，34连接。这种构造最终在需要的情况下， 允许气室的容易的拆卸，维护和除垢。[0059] 注意到联管管道12和气体冷却器10不是必须为图2所示的一一对应关系。实际上其可优选的为将来自一个联管管道12的烟气流分到两个或多个垂直布置的气体冷却器 10。这使其更容易控制经过水套管沈的水流并且将使每个气体冷却器10的尺寸和复杂性
更易管理。
[0060] 本领域技术人员将想到在工艺参数范围内的可能气体冷却器10操作。下面的表给出了上述实施例的可能范围和优选参考值的例子。
[0061]表
[0062]
[0063] 如图1和2所示，上述烟气冷却器有利地为使用来自烟气的热能的系统的一部分， 其中闭路冷却剂循环系统使冷却剂循环经过烟气冷却器和热交换装置对。由热交换装置对从冷却剂提取的热能可用于增加连接到热交换装置的进一步设备的效率。现在将描述这种使用提取热能的例子。
[0064]例子 1
[0065] 如前所述，新的炼铝炉趋于在全球的热带或亚热带建造。在这些地区，用于电解槽的电能在燃气发电站中由发电设备产生，所述发电设备包括燃气轮机驱动发电机。用于这种电站的典型的燃气轮机为在简单循环下操作的总功率输出为180MW的ALSTOM® GT13 E2M。
[0066] 简单循环燃气轮机的效率和功率输出的限制因素为到压缩机的进气温度。在热带地区，它们被设计用于+35摄氏度的压缩机进气温度。如果压缩机进气温度从35摄氏度减小到15摄氏度，典型的简单循环发电设备（仅燃气轮机）的能量输出可增加多于10%。 上述气体冷却器便于为发电设备提供这种进气冷却，因为由气管热交换器从烟气回收的热量可用作包括热交换装置M的吸热型工业制冷站的能量源。这种工业制冷站可输出制冷水，其可用于降低压缩机进气温度。将想起的是，对于前面列举的工艺参数，每个气体冷却器10可将900，OOONmVh烟气从150摄氏度的温度冷却到115摄氏度的温度。这意味着近似45MW的热能由吸热制冷站M从烟气中去除，并且在所示布局中，此能量由制冷站用于大约产生5摄氏度的1450m3/h的制冷水36。制冷水36经过绝热管道38流通到位于三个燃气轮机发电设备44的进口 42处的热交换器40 ( S卩，空气冷却器组，其自身在发电行业中是公知的）。热交换器40连接到相互平行的水冷系统，它们的进口 46和出口 48分别连接到闭路水冷系统的“冷”和“热”的支架50，52。当在正常连续运转额定值操作时，上述GT13 E2M燃气轮机发电设备经过其压缩机/涡轮机系统吸取1. 548 X IO6NmVh空气。标准的热力学计算示出了此气流可使用上述量制冷水从35摄氏度冷却到15摄氏度，从而显著地增大燃气轮机（并因此增加发电设备）的效率和功率输出。
[0067] 如前所述，从烟气回收的热可用于使简单循环燃气轮机发电设备的功率产生量增加10%或更多。这种额外的功率可用于例如增加炼铝炉的生产量而无需投入进一步的发电设备。
[0068] 应注意到以上述方式可替换地或额外地产生的制冷水可用于建筑物或区域的空气调节和冷却，这种目的在热带和亚热带地区得到了高度认同。
[0069] 而发电设备44在上面为了示出被描述为简单循环，它们可替换地包括组合式循环发电设备，其中燃气轮机的废热用于产生驱动连接到发电机的蒸汽涡轮机的蒸汽。由于组合式循环相对于简单循环的更高热效率，来自连接的炼铝炉的烟气热量将——当在上述吸热制冷站回收并利用时——具有超出连接的组合式循环发电设备的压缩空气冷却需求 50%的冷却量。这种超出的冷却量可再次用于进一步的设备，例如建筑物或区域的空气调节和冷却。
[0070] 不论使用简单循环还是组合式循环发电设备，我们都预计燃气轮机热交换器10 与吸热冷却站M和燃气轮机进气冷却器40的组合将对于热带和亚热带地区的炼铝炉设备具有经济利益。
[0071] 在图2中，冷却站M使用一组8个吸热型工业制冷器，例如^rk Millennium™ YIA-14F3单效吸热制冷器，或其他制造商的等同产品。取决于吸热制冷器的所需冷却量和冷却能力，可使用小于8个或多于8个的制冷器。为了从气体冷却器10返回的120摄氏度的水中以及从进气热交换器40返回的25摄氏度的水中去除低温热量，制冷器使用大量的水。这些可为海水，因为目前很多炼炉为了便于铝土矿和精炼铝的大批运输而在海岸附近建造。以30摄氏度进入制冷站M的8000m3/h海水将以40摄氏度返回海中，从而完成两个闭路水冷系统的所需冷却。作为将热量排放到环境中的可替换方法，假定环境气温足够低， 一个或多个冷却塔可用于冷却在吸热制冷器中作为冷却剂来冷凝工作流体的水。为了避免由蒸发导致的水损失，这种冷却塔将为“干式”冷却塔，其中被冷却的水不是直接暴露于向上经过塔的空气中。
[0072] 而上面提到了单效吸热冷却器的使用，但并不因此排除双效或多效吸热冷却器的可能使用。但是后两种类型尽管比单效吸热冷却器更有效，但是需要比单效冷却器更高级的热量输入。吸热冷却器的可行热量输入级别主要取决于烟气温度，因为其控制到吸热制冷器的进水温度。
[0073] 如果代替吸热制冷站，热交换器装置M简单地包括用于加热处理水的适合的热交换器或热交换器组，那么由气体冷却器10回收的热能可用于需要热输入的进一步的设备，如下面的例子所述。
[0074]例子 2
[0075] 由气体冷却器10从烟气抽取的热量用于通过预热用于组合式循环的蒸汽升高部分的锅炉水而增加组合式循环发电设备的效率。
[0076]例子 3
[0077] 由气体冷却器10从烟气抽取的热用于在脱盐设备中预热水从而脱盐。
[0078] 例子 4
[0079] 由气体冷却器10从烟气抽取的热用于加热用于围绕区域加热线路循环的水。
[0080] 本发明的广度和范围不应由任意上述示例性实施例限制，并可在所要求的本发明范围内修改。说明书（包括权利要求和附图）中公开的每个特征可由用于相同，等价或类似目的的可替换特征代替，除非以其他方式明确声明。
[0081] 除非在本文中清楚地要求，否则在说明书和权利要求的全文中，词语“包括”、“包含”等被解释为与排他的或穷尽的意思相对的包括；也就是说是“包括，但不限于”的意思。
Claims (16)
1. 一种气体冷却器（10)，其被构造成用于处理来自炼铝炉设备中的铝电解槽的热原始烟气（G)，所述气体冷却器包括：(a)进气室(14)；(b)出气室(16)；以及(c)隔开的相互平行的气体冷却管（18)阵列，每个冷却管在所述进气室中具有进口端 (19)并且在所述出气室中具有出口端；其特征在于，所述气体冷却管的进口端（19)为钟形且包括空气动力学弯曲的气体加速轮廓，以便于热原始烟气流线地流入所述气体冷却管中。
2.根据权利要求1所述的气体冷却器，其特征在于，所述进气室（14)具有用于接收所述热原始烟气（G)的扩散进口（15)，从而使流经进气室的气体被减速并稳定，以便均勻地流入所述气体冷却管（18)的进口端（19)。
3.根据权利要求2所述的气体冷却器，其特征在于，所述进气室的扩散进口使进气室中的热烟气减速到8-12m/sec范围内的相对低的速度。
4.根据前述权利要求1-3中任一项所述的气体冷却器，其特征在于，所述冷却管进口将所述烟气加速至20-30m/sec范围内的速度。
5.根据前述权利要求1-3中任一项所述的气体冷却器，其特征在于，所述冷却管的进口端和出口端分别突出到所述进气室和出气室中。
6.根据前述权利要求1-3中任一项所述的气体冷却器，包括围绕所述冷却管的冷却剂容器，所述容器设有冷却剂进入和排出管道。
7.根据权利要求6所述的气体冷却器，其特征在于，所述冷却器容器形成所述气体冷却器的部分外壳。
8.根据权利要求6所述的气体冷却器，其特征在于，所述冷却剂流经所述冷却剂容器的方向与气体流经所述管的方向相反。
9.根据前述权利要求1-3中任一项所述的气体冷却器，其特征在于，所述进气室和出气室可从所述冷却剂容器上拆卸。
10. 一种对炼铝炉设备中的热原始烟气（G)进行冷却和净化的方法，所述炼铝炉设备设有干法净化型烟气净化设备G)，所述方法包括以下步骤：(a)将初始温度超过烟气净化设备（4)可接受范围的原始烟气（G)经过多个相互平行布置以接收原始烟气的气体冷却器（10)，所述气体冷却器包括冷却管（18)阵列，其配置成接收并在其中通过流线型流形式的原始烟气；(b)在所述冷却管外部流过冷却剂0¾以通过将烟气热量传到所述冷却剂而冷却所述原始烟气，由此将所述烟气冷却至所述烟气净化设备（4)可接受的温度；以及(c)将冷却的原始烟气送到所述烟气净化设备。
11.根据权利要求10所述的方法，其特征在于，所述烟气冷却器接收120-250摄氏度温度范围的原始烟气，并将它们在60-120摄氏度范围的温度下传到所述烟气净化设备。
12.根据权利要求10所述的方法，其特征在于，为了便于均勻流入所述气体冷却管，所述原始烟气首先通过扩流过程被减速并稳定化。
13.根据权利要求12所述的方法，其特征在于，所述扩流过程使气流减速到8-12m/sec 范围内的相对低的速度。
14.根据权利要求12所述的方法，其特征在于，进入所述冷却管时，所述烟气受到流加速过程影响而产生经过其中流线型流。
15.根据权利要求14所述的方法，其特征在于，所述流加速过程将所述气流加速至 20-30m/sec范围内的速度。
16.根据权利要求10-15中任一项所述的方法，其特征在于，热能由热交换装置从所述冷却剂中提取，并用于增加连接到所述热交换装置的进一步设备的效率。
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| GB0705439.8 | 2007-03-22 | ||
| GB0705439A GB0705439D0 (en) | 2007-03-22 | 2007-03-22 | Improved flue gas cooling and cleaning arrangment |
| PCT/EP2008/001953 WO2008113496A1 (en) | 2007-03-22 | 2008-03-12 | Flue gas cooling and cleaning system |
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| Publication Number | Publication Date |
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| CN101641462A CN101641462A (zh) | 2010-02-03 |
| CN101641462B true CN101641462B (zh) | 2011-12-14 |
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| CN2008800094336A CN101641462B (zh) | 2007-03-22 | 2008-03-12 | 烟气冷却和净化系统 |
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| US (1) | US8894921B2 (zh) |
| EP (1) | EP2122013B1 (zh) |
| CN (1) | CN101641462B (zh) |
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| GB (1) | GB0705439D0 (zh) |
| RU (1) | RU2455399C2 (zh) |
| WO (1) | WO2008113496A1 (zh) |
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| FR2946666B1 (fr) * | 2009-06-10 | 2015-08-07 | Solios Environnement | Systeme et procede de recuperation d'energie |
| CN101928963A (zh) * | 2009-06-23 | 2010-12-29 | 沈阳铝镁设计研究院 | 降低电解烟气温度的系统及方法 |
| FR2948128B1 (fr) * | 2009-07-20 | 2011-12-23 | Solios Environnement | Dispositif de collecte des gaz emis par des cuves d'electrolyse d'aluminium, et systeme de production d'aluminium associe |
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| EP2458035A1 (en) | 2010-01-21 | 2012-05-30 | Alstom Technology Ltd | A method of ventilating an aluminium production electrolytic cell |
| FR2960053B1 (fr) * | 2010-05-12 | 2015-07-17 | Solios Environnement | Procede et dispositif de desencrassement d'echangeur de chaleur |
| FR2960289B3 (fr) * | 2010-05-21 | 2012-05-11 | Solios Environnement | Procede et dispositif de desencrassement |
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| US20140112834A1 (en) * | 2012-10-23 | 2014-04-24 | Babcock & Wilcox Power Generation Group, Inc. | System and method for controlling scale build-up in a wfgd |
| CN102901384B (zh) * | 2012-10-31 | 2015-11-25 | 张勤福 | 一种设置有排气孔的高温烟气热回收器 |
| IN2015DN03103A (zh) * | 2012-11-12 | 2015-10-02 | Univation Tech Llc | |
| FR3018826A1 (fr) * | 2014-03-21 | 2015-09-25 | Solios Environnement | GAS TREATMENT FACILITY FOR ELECTROLYTIC TANKS FOR THE PRODUCTION OF ALUMINUM |
| RU2602556C2 (ru) * | 2014-05-26 | 2016-11-20 | Борис Павлович Самойлов | Способ прекращения выбросов вредных веществ в атмосферу промышленной дымовой трубой |
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- 2008-03-12 EP EP08716459.6A patent/EP2122013B1/en active Active
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- 2008-03-12 WO PCT/EP2008/001953 patent/WO2008113496A1/en active Application Filing
- 2008-03-12 US US12/529,355 patent/US8894921B2/en active Active
- 2008-03-12 BR BRPI0809152-8A2A patent/BRPI0809152A2/pt not_active Application Discontinuation
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Also Published As
| Publication number | Publication date |
|---|---|
| RU2009138939A (ru) | 2011-04-27 |
| GB0705439D0 (en) | 2007-05-02 |
| AU2008228516B2 (en) | 2010-10-28 |
| EP2122013B1 (en) | 2015-08-05 |
| CA2679692A1 (en) | 2008-09-25 |
| CA2679692C (en) | 2011-12-13 |
| US20100101760A1 (en) | 2010-04-29 |
| RU2455399C2 (ru) | 2012-07-10 |
| CN101641462A (zh) | 2010-02-03 |
| EP2122013A1 (en) | 2009-11-25 |
| BRPI0809152A2 (pt) | 2014-09-16 |
| US8894921B2 (en) | 2014-11-25 |
| WO2008113496A1 (en) | 2008-09-25 |
| AU2008228516A1 (en) | 2008-09-25 |
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