CN1608167A - 利用自然分布型燃烧器对含烃岩层进行就地热处理的方法 - Google Patents

利用自然分布型燃烧器对含烃岩层进行就地热处理的方法 Download PDF

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CN1608167A
CN1608167A CNA028210514A CN02821051A CN1608167A CN 1608167 A CN1608167 A CN 1608167A CN A028210514 A CNA028210514 A CN A028210514A CN 02821051 A CN02821051 A CN 02821051A CN 1608167 A CN1608167 A CN 1608167A
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哈罗德·J·维内加
埃里克·P·德鲁菲格纳克
斯科特·L·韦林顿
罗伯特·M·范哈德维尔德
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Abstract

本发明提供了一种用于处理含烃岩层的就地方法，该方法包括由一处或多处热源向至少一部分岩层供热。热源包括一种自然分布型燃烧器。该自然分布型燃烧器包括一氧化流体源，以便向岩层内的一反应区提供氧化流体，从而在该反应区内产生热量。该热量由反应区传送至岩层的选定段，从而来自一处或多处热源的热量对选定段内的一部分烃进行热解，而所述烃则产自所述岩层。

Description

利用自然分布型燃烧器对含烃岩层 进行就地热处理的方法
技术领域
本发明主要涉及用于从各种含烃岩层开采烃类、氢和/或其他产品的方法和装置。某些具体实施方式涉及利用自然分布型燃烧器从地下含烃岩层开采烃、氢和/或新型产品流的就地烃类转化方法。
背景技术
通常将由地下岩层(例如沉积岩)获得的烃类用作能源、原料和消费产品。对现有烃资源枯竭以及对开采的烃的综合质量下降的关注已促使人们开发出各种方法，来更为有效地回收、加工和/或利用现有的烃资源。其中，就地处理方法可用于从地下岩层中提取烃原料。可能需要对地下岩层内烃原料的化学和/或物理性能加以改变，以使得烃原料更易于从地下岩层中提取。所述化学和物理的变化可包括开采可提取流体的就地反应、岩层内的烃原料的成分变化、溶解度变化、密度变化、相变和/或粘度变化。流体可为气体、液体、乳液、浆液和/或流动特性与液体流类似的固体颗粒流，但并不限于此。
美国专利No.2,634,961(Ljungstrom)、No.2,732,195(Ljungstrom)、No.2,780,450(Ljungstrom)、No.2,789,805(Ljungstrom)、No.2,923,535(Ljungstrom)以及No.4,886 118(VanMeurs等)描述了利用井底加热器的就地处理方法的实施例。
可用热源对地下岩层进行加热。美国专利No.2,548,360(Germain)、No.4,716,960(Eastlund等)、No.5,065,818(Van Egmond)以及No.4,570,715(Van Meurs等)描述了电加热器和/或电加热部件。
可通过燃烧燃料来加热地下岩层。通过燃烧燃料加热岩层比利用电力加热岩层更为经济。若干不同种类的加热器可使用燃料燃烧作为加热岩层的热源。该燃烧可在岩层内、井内和/或接近地面处进行。岩层内的燃烧可以采用火驱法。可向岩层内泵入一种氧化剂。可将该氧化剂点燃以朝着生产井方向向前移动燃烧前沿。泵入岩层内的氧化剂可沿着岩层内的断裂线流过岩层。点燃氧化剂可能不会导致燃烧前沿均匀流过岩层。
发明内容
在一具体实施方式中，含烃岩层(例如含有煤炭、油页岩、重质烃或其组合物的岩层)中的烃可在岩层内就地转化为品质较高的烃产品、氢和/或其他产品的混合物。可利用一处或多处热源将一部分含烃岩层加热至使得烃热解的温度。烃、氢以及其他岩层流体可通过一个或多个生产井从岩层中提取。在一些具体实施方式中，岩层流体可汽态提取。在其他一些具体实施方式中，岩层流体可在液体和气体状态下或在液态下被提取。在热解过程中，可对至少一部分岩层的温度与压力进行控制，以生产改良产品。
在一具体实施方式中，一种自然分布型燃烧器可向含烃岩层供热。该自然分布型燃烧器可包括一位于岩层开口内的加热器。该加热器可向至少一部分岩层供热。自然分布型燃烧器可包括一种氧化流体源。该氧化流体源可向岩层内的反应区提供氧化流体，以便在该反应区内产生热量。一部分反应区可能已由加热器预先加热。自然分布型燃烧器可包括位于开口内的第一管道。该第一管道可由氧化流体源向岩层内的反应区提供氧化流体。该氧化流体可氧化反应区内的至少一些烃以产生热量。反应区内产生的热量可由反应区传送至岩层。
在一具体实施方式中，氧化流体可基本通过扩散传过反应区。扩散速率可通过反应区的温度进行控制。在一些具体实施方式中，可基本上防止氧化流体由反应区流入岩层的周围部分。可允许热量基本上通过传导方式由反应区传送至岩层。可允许氧化产生的热量由反应区传送至岩层内的热解区。允许传送至热解区的热量可热解岩层热解区的至少一些烃。
在某些具体实施方式中，可沿至少一段第一管道对氧化流体的流量进行控制，以控制沿至少一段第一管道的温度。可对该流量进行控制，以控制至少一段岩层的加热速率。第一管道可包括向开口内提供氧化流体的孔道。在一些具体实施方式中，第一管道可包括控制氧化流体流量的临界流量孔道，以控制岩层内的氧化速率。
在某些具体实施方式中，可向反应区提供分子氢。至少一些供给氢可在反应区内产生。至少一些供给分子氢可在岩层的加热区内产生。可向反应区提供分子氢以防止二氧化碳产生。
在一具体实施方式中，自然分布型燃烧器可包括第二管道。第二管道可将氧化产物从岩层中提取。第二管道可将氧化产物除去以使得岩层内基本保持恒温。第二管道可控制开口内的氧浓度，从而氧浓度基本不变。第一管道可包括基本沿与第二管道的孔道清除氧化产物的相反方向引导氧化流体的孔道。第二管道朝第二管道上端的孔道可具有较大的浓度。第二管道可允许热量从氧化产物传送至第一管道内的氧化流体。可对第一和第二管道内的流体压力进行控制，从而氧化流体的浓度沿第一管道长度方向基本均匀。
在一具体实施方式中，一种用于向含烃岩层供热的就地处理方法可包括：将一部分岩层加热至足以维持该部分内的烃与氧化流体发生反应的温度。可向岩层内的一反应区提供氧化流体。该氧化流体可允许与反应区内的至少一部分烃发生反应，以在该反应区内产生热量。反应区内产生的热量可传送至岩层。
附图简要说明
结合下文中优选实施方式的详细说明，并参照附图，本领域技术人员可理解本发明的优点，其中：
图1示出了含烃岩层各加热阶段的图表；
图2示出了一用于处理含烃岩层的一部分就地转化装置的具体实施方式的概图；
图3示出了一自然分布型燃烧器热源的具体实施方式；
图4示出了一具有第二管道的自然分布型燃烧器的具体实施方式的横断面图；
图5示出了一位于含烃岩层内的加热器井的具体实施方式的概图；
图6示出了一具有自然分布型燃烧器热源的岩层上覆岩层的一部分；
图7示出了一自然分布型燃烧器热源的具体实施方式；
图8示出了一自然分布型燃烧器热源的具体实施方式；
图9示出了一用于加热岩层的自然分布型燃烧器系统的具体实施方式；
图10示出了一用于加热岩层的自然分布型燃烧器系统的具体实施方式；
虽然通过附图中的实施例示出了本发明的具体实施方式，并且可能在文中进行详细描述，但是仍然很容易对本发明作各种修改和替换。附图可能不是按比例进行绘制的。但是，应该理解的是，附图及其具体描述的目的并不在于将本发明限定在所公开的特殊形式中，相反，本发明将涵盖如所附权利要求书中所限定的精神和范围内的所有修改方案、等同方案以及备择方案。
具体实施方式
下文的描述主要涉及用于处理含烃岩层(例如，含有煤炭(包括褐煤、腐泥煤等)、油页岩、含碳页岩、次石墨、油母岩质、沥青、油、低渗透率母岩中的油母岩质和油、重质烃、沥青岩、自然石蜡的岩层、油母岩质为其他烃的阻滞产品的岩层等)。可对这类岩层进行处理以产出质量较高的烃产品、氢及其他产品。
“烃”通常定义为主要由碳和氢原子形成的分子。烃还可含有其他元素，例如卤素、金属元素、氮、氧和/或硫，但并不限于此。
“岩层”包括一层或多层含烃层、一层或多层非烃层、一层上覆岩层和/或一层下伏岩层。“上覆岩层”和/或“下伏岩层”包括一种或多种不同的不渗透性材料。例如，上覆岩层和/或下伏岩层可包括页岩、泥岩或湿/密封的碳酸盐(即不含烃的不渗透性碳酸盐)。在一些就地转化方法的具体实施方式中，上覆岩层和/或下伏岩层可包括一层含烃层或多层含烃层，所述含烃层相对不透水并且在就地转化过程中不受温度的影响，所述就地转化过程导致上覆岩层和/或下伏岩层的含烃岩层的特征发生明显变化。举例来说，下伏岩层可包含页岩或泥岩。在某些情况下，上覆岩层和/或下伏岩层也可有些渗透性。
“热源”是指任何通过传导和/或辐射传热方式向至少一部分岩层供热的装置。例如，热源可包括诸如绝缘导体、条形构件和/或置于导管内的导体一类的电加热器。热源也可包括通过在岩层外部或内部燃烧燃料来产生热量的热源，例如表面燃烧器、井底气体燃烧器、无焰分布燃烧器以及自然分布型燃烧器。另外，可以理解，在某些具体实施方式中，在一处或多处热源中所提供或产生的热量可由其他能源供应。其他能源可直接对岩层进行加热，或者该能量可施加至一直接或间接加热岩层的传送媒介上。应当理解，给岩层施加热量的一或多个热源可使用不同的热源。例如，对于给定的岩层而言，有些热源可由电阻加热器供热，有些热源可由燃烧器供热，而有些热源可由一或多种其他能源供热(例如，化学反应、太阳能、风能、生物燃料、或其他可再利用的能源)。化学反应可包括放热反应(例如氧化反应)。热源可包括一向例如加热器井的加热位置的附近和/或周围的区域供热的加热器。
“加热器”是指任何在井或钻井邻近区域产生热量的装置。加热器可为与岩层内的或从岩层中开采出的材料发生反应的电加热器、燃烧器、燃烧室，和/或它们的组合。“热源的单位”是指形成模板的热源数目，重复该模板以形成岩层内的热源分布图。
“自然分布型燃烧器”是指一种利用氧化剂来氧化岩层内的至少一部分烃以产生热量的加热器，其中，氧化作用出现在井眼附近。大多数在自然分布型燃烧器内产生的燃烧产品通过井眼去除。
“孔道”是指具有各种尺寸和横断面形状的开口(例如，管道内的开口)，横断面形状包括圆、椭圆、正方形、矩形、三角形、狭缝或者其他规则或不规则的形状，但并不限于此。
可以通过各种方式来处理岩层内的烃，以生产出多种不同的产品。在某些具体实施方式中，这种岩层可分阶段处理。图1示出了含烃岩层的多个加热阶段。图1还示出了由含烃岩层开采岩层流体的开采量(每吨的等价油桶数)(y轴)相对于岩层温度(℃)(x轴)的实施例。
在加热阶段1期间，甲烷出现脱附作用，而水分开始蒸发。岩层在阶段1的加热程序可尽可能快地完成。例如，当含烃岩层最初被加热时，岩层内的烃可脱附吸附的甲烷。脱附的甲烷可从岩层中产生。如果进一步加热含烃岩层，则含烃岩层内的水分将会蒸发。在一些含烃岩层中，水分可占岩层孔隙体积的约10％～50％。在其他一些具体实施方式中，水分所占孔隙体积的份量可能更大或更少。岩层内的水分一般会在约160℃～285℃、压力约6巴(绝对)～70巴(绝对)的情况下蒸发。在一些具体实施方式中，岩层内的压力在就地转化处理期间可保持在约2巴(绝对)～70巴(绝对)之间。在一些具体实施方式中，水分的蒸发使得岩层内的湿润性发生变化和/或使得岩层压力增加。湿润性的变化和/或压力的增加可能影响到岩层内的热解反应或其他反应。在某些具体实施方式中，蒸发的水分可从岩层中提取出来。在另外一些具体实施方式中，蒸发的水分可用于蒸汽反应和/或岩层内或岩层外的蒸馏过程。清除水分同时增加岩层内的孔隙体积可增加孔隙体积内的烃储存空间。
岩层在加热阶段1之后可被进一步加热，从而岩层内的温度升至(至少)初始热解温度(例如，如阶段2的温度范围下端的温度)。岩层内的烃可在整个阶段2被热解。热解温度范围可随着岩层内烃的类型而有所不同。热解温度范围可为约250℃～900℃。生产需求产品的热解温度范围可能仅贯穿整个热解温度范围的一部分。在一些具体实施方式中，生产需求产品的热解温度范围可为约250℃～400℃。如果岩层内烃的温度在约250℃～400℃的温度范围内缓慢升高，则当温度达到400℃时，热解产品的生产可基本完成。利用若干热源对含烃岩层进行加热可在热源周围建立起热梯度，从而使得岩层内烃的温度在热解温度范围内缓慢升高。
在一些就地转化方法的具体实施方式中，欲被热解的烃的温度可能不会在约250℃～400℃的整个温度范围内缓慢增加。岩层内的烃可被加热至一要求温度(例如，约为325℃)。也可选择其他温度作为要求温度。可对由热源输入岩层内的能量进行调节，以将岩层内的温度基本保持在要求温度。在热解作用减弱之前，烃可基本维持在要求温度，从而使得岩层内的需求岩层流体的开采变得不经济。
在一就地转化方法的具体实施方式中，加热速率可被控制在将与加热选定段相关的费用减至最小的状态。该费用例如可包括输入能费用和设备费用。在某些具体实施方式中，与加热选定段相关的费用可通过如下方式减至最小，即：当加热的相关费用较高时，减小加热速率，而当加热的相关费用较低时，增大加热速率。举例来说，当相关费用较高时，可采用约330瓦特/米的加热速率，而当相关费用较低时，可采用约1640瓦特/米m的加热速率。在某些具体实施方式中，当相关费用较高时，加热速率可在约300瓦特/米～约800瓦特/米之间变化，而当相关费用较低时，加热速率则在约1000瓦特/米～1800瓦特/米之间变化。加热的相关费用在能源消耗高峰期，例如在白天时可能较高。举例来说，由于能源消耗在空调上，所以能源消耗在气候温暖的夏日白天可能很高。能源消耗低的时段例如可能在晚上或周未期间，此时能量需要势必较低。在一具体实施方式中，加热速率可从例如在夜间的低能耗期的较高加热速率变化至例如在日间的高能耗期的较低加热速率。
如图2所示，除了热源100之外，通常还在该部分的含烃岩层内布置一或多个生产井106。岩层流体可通过生产井106开采。在一些具体实施方式中，生产井106可包括一热源。该热源可加热生产井处或其附近的岩层部分，并且使得岩层流体在汽态时清除。可减少或消除从生产井高温抽取流体的必要性。避免或限制高温抽取流体可显著降低开采成本。在生产井处或通过生产井供热可起到如下作用，即：(1)当采出液在靠近上覆岩层的生产井内移动时，防止该采出液冷凝和/或回流；(2)增加岩层内的输入热量；和/或(3)增加生产井处或其附近的岩层渗透性。在一些就地转化方法的具体实施方式中，生产井的供热量明显小于加热岩层的热源的供热量。
因为加热岩层内的渗透性和/或多孔性增加，所产生的蒸汽可在压差较小的岩层内流过相当长的距离。渗透性增加可能是由于水分的汽化、烃的提取和/或裂缝的产生而导致加热部质量减少的结果。流体可更易流过加热部。在一些具体实施方式中，生产井可设置于含烃层的上部。
含烃岩层内产生的流体可以蒸汽形式在含烃岩层内移动相当一段距离。视各种因素而定(例如，岩层的渗透性、流体的性质、岩层的温度、以及允许流体移动的压力梯度)，该相当一段距离可能大于1000米。由于经过就地转化并且岩层流体被提取，岩层内的渗透性得以增加，所以生产井可能仅需要每隔一个热源单位，或每隔三、四、五、或六个热源单位进行设置。
在一种就地处理过程中，可将生产井控制在生产井处的压力比岩层其他部分的压力低的状态。在一些具体实施方式中，生产井处可能为真空状态。将生产井维持在较低压力状态可阻止岩层内的流体流出就地处理区。
某些具体实施方式可能包括对向至少部分岩层所提供的热量进行控制，从而可基本上防止在该部分岩层内产生欠理想的产物。同时，对提供给至少部分岩层的热量进行控制还可增加岩层内渗透率的均匀性。例如，在某些实施方式中，通过控制岩层的热量来防止欠理想产物的产出包括将每天的加热速率控制在比一选定量(例如，10℃、5℃、3℃、1℃、0.5℃或0.1℃)小的状态。
在一些具体实施方式中，一处或多处热源的热量叠加(例如重叠)可导致一部分含烃岩层基本上均匀加热。由于加热期间的岩层一般会在整个岩层上具有温度剖面，在该专利的上下文中，“基本上均匀”加热是指加热的结果使得大部分加热断的温度相对于大部分选定处理段(体积)的估计平均温度的变化值不会大于100℃。
对含烃岩层基本均匀地进行加热可导致渗透率基本上均匀增加。例如，由于岩层内产生热应力，所以均匀加热可导致在加热部内产生一系列基本均匀的裂缝。加热基本上均匀可使得热解流体基本均匀地从加热部中产出。水分因汽化和开采而被提取可导致加热部的渗透率增加。除了因热应力而产生裂缝之外，因流体压力增加也可导致产生裂缝。随着流体在加热部内产生，加热部内的流体压力可能也会增大。随着流体压力接近加热部的静岩压力，可能产生裂缝。基本均匀的加热和流体的均匀产生可在加热部内产生基本均匀的裂缝。在一些具体实施方式中，含烃岩层加热段的渗透率的变化率可能约不大于10。
含有热解流体的岩层流体可从岩层中产出。热解流体可包括烃、氢、二氧化碳、一氧化碳、硫化氢、氨、氮、水及其混合物，但并不限于此。随着岩层温度的增加，产出岩层流体内的可冷凝烃含量势必减小。在高温条件下，岩层可能主要产出甲烷和/或氢。如果含烃岩层在整个热解范围内被加热，则岩层可能在接近热解范围的上限时仅产生少量的氢。待可用氢被全部耗尽后，岩层内一般会出现极少量的流体产物。
在用于处理渗透率较低的岩层内的重质烃的某些具体实施方式中，可包括从一处或多处热源提供热量来热解一些重质烃，然后使一部分重质烃汽化。热源可热解岩层选定段中的至少一些重质烃，并且可使得至少一部分选定段增压。在加热期间，岩层内的压力可显著增加。可对岩层内的压力进行控制，从而使得岩层内的压力可维持在能够产生具有需求成分的流体的状态。通过利用岩层加热所产生的反压力，热解流体能以蒸汽形式由一处或多处加热井从岩层中提取。
烃经热解后，岩层内可能仍然存在大量的碳和一些氢。岩层内的大部分残存碳可以合成气的形式从岩层内提取出。合成气的产生可在如图1所示的加热阶段3期间进行。阶段3可包括将含烃岩层加热至一足以产生合成气的温度。举例来说，合成气可在约400℃～约1200℃的温度范围内产生。合成气生成流体被引入岩层时的岩层温度可确定岩层内所产出的合成气的成分。如果合成气生成流体在一足以产生合成气的温度下被引入岩层，则岩层内可能产生合成气。所产生的合成气可通过一个生产井或多个生产井从岩层中取出。在合成气产生的过程中可能产生大量的合成气。
图2示出了用于处理含烃岩层的一部分就地转化系统的具体实施方式的概图。热源100可设置于至少一部分含烃岩层内。举例来说，热源100可包括例如绝缘导体的电加热器、管道内导体加热器、表面燃烧器、无焰分布燃烧器和/或自然分布型燃烧器。热源100还可包括其他类型的加热器。热源100可为至少一部分含烃岩层供热。能量可通过供应线116提供给热源100。供应线可根据用于加热岩层的一处或多处热源的类型而具有不同的结构。热源供应线可为电加热器输送电力、为燃烧器输送燃料、或输送在岩层内循环的热交换流体。
生产井106可用于从岩层内开采岩层流体。从生产井106中开采的岩层流体可通过采集管118输送至处理设备120。岩层流体也可从热源100产生。例如，流体可从热源100产生以控制靠近热源处的岩层的压力。从热源100产生的流体可通过管道或管路输送至采集管118，或所产生的流体可通过管道或管路直接输送至处理设备120。处理设备120可包括分离装置、反应装置、提升装置、燃料电池、涡轮、存储容器以及用于处理产出的岩层流体的其他系统或装置。
用于处理烃的就地转化系统可包括阻挡井122。在一些具体实施方式中，阻挡井可用于防止流体(例如，产出流体和/或深井水)在就地转化过程中流入一部分岩层内，或从中流出。阻挡物可包括自然存在部分(例如上覆岩层和/或下伏岩层)、冻结井、冻结阻挡带、低温阻挡带、灰浆壁、硫化井、脱水井、注入井、由岩层内产出的凝胶而形成的阻挡物、由岩层内盐类沉淀而形成的阻挡物、由岩层内的聚合反应而形成的阻挡物、打入岩层内的薄板或其组合，但并不限于此。
处理期间由含烃岩层产生的岩层流体可包括各种组分的混合物。为了提高产自岩层的产品的经济价值，可利用各种处理方法对岩层流体进行处理。用于处理岩层流体的方法包括蒸馏(例如，常压蒸馏、分解蒸馏和/或真空蒸馏)、冷凝(例如，分解蒸馏)、裂化(例如，热裂化、催化裂化、流化催化裂化、加氢裂化、渣油加氢裂化和/或蒸汽裂化)、重整(例如，热重整、催化重整和/或氢水蒸气重整)、氢化、焦化、溶剂萃取、溶剂脱腊、聚合(例如，催化聚合和/或催化异构化)、减粘裂化、烷化、异构化、脱沥青、加氢脱硫、催化脱蜡、脱盐、萃取(例如，萃取石炭酸、其他芳族化合物等)、和/或汽提。
岩层流体可如下区域进行处理，即当岩层流体产生并开采时在第一就地处理区、进行特定处理工艺的第二就地处理区、和/或在地面处理装置中。“地面处理装置”是指在地面上用于处理至少一部分岩层流体的装置。地面处理装置可包括反应器(例如，加氢处理装置、裂化装置、氨产生装置、肥料产生装置和/或氧化单位)、分离装置(例如，空气分离装置、液-液萃取装置、吸附装置、吸收器、氨回收和/或产生装置、蒸气/液体分离装置、蒸馏塔、活性蒸馏塔和/或凝结装置)、重沸装置、换热器、泵、管、存储装置、和/或能量产生装置(例如，燃料电池和/或燃气涡轮)。串联、并联和/或串并联组合的多个地面处理装置被称为地面设施配置。地面设施配置可根据岩层流体的成分以及产生的产品而极为不同。
地面处理组合可与各种地面处理系统中的处理方法相结合以产出大量产品。在某一地点产出的产品可随着当地和/或全球的市场情况、岩层特性、岩层与买方的接近度和/或可用的原料而有所变化。产出的产品可就地使用、运送至另一地点使用、和/或卖给购买方。
所产生产品的成分可通过控制一处理区内和/或一个或多个地面处理装置内的状况而有所变换。处理区和/或一个或多个地面处理装置中影响产品成分的状况包括：平均温度、流体压力、H2的局部压力、温度梯度、岩层材料的成分、加热速率、以及进入处理区和/或地面处理装置中的流体成分，但并不限于此。为了从岩层流体合成和/或分离出特殊的组分，还设置了许多不同的地面设施配置。
通过控制岩层状况来控制产出流体中氢的压力可提高产出流体的质量。在一些具体实施方式中，将产出流体中的氢分压控制在约大于0.5巴(绝对)的岩层状况下是较为合意的，上述数值为在一生产井处的测量值。
在一具体实施方式中，就地处理含烃岩层的方法可包括：在选定段温度达到至少约270℃之后，向选定段添加氢。其他的具体实施方式则可包括通过选择性地向岩层添加氢来控制岩层的温度。
在一具体实施方式中，可对一部分含烃岩层进行加热以增加H2分压。在一些具体实施方式中，增压后的H2分压约为0.5～7巴。备择地，增压后H2的分压约为5～7巴。作为一个实施例，H2分压约为5～7巴时，可产出大部分烃流体。热解H2分压范围内的H2分压范围可根据例如岩层加热部分的温度与压力情况而有所变化。
将岩层内的H2分压保持在大于大气压的情况下可增加所产出的可冷凝烃流体的API值。保持一增加的H2分压可使得所产出的可冷凝烃流体的API值约大于25，或者在有些情况下约大于30。保持含烃岩层的加热部分的H2分压增加可增加加热部分内的H2浓度。H2可用于与烃的热解组分发生反应。H2与烃的热解组分发生反应可减少烯烃与焦油和其他难以提升的交联制品的聚合作用。从而，可防止生产出API比重值较低的烃流体。
一种就地转化方法可在岩层内产生大量的H2和烃流体。由于岩层内所产生的氢以及岩层内足以使氢在岩层内进入液相的压力，所以可无需将还原流体(例如，H2和/或不凝结饱和烃)引入岩层内，便可在岩层内形成一还原状态。由岩层产出的岩层流体的氢成分可被分离并被用于预期目的。预期目的可包括用于燃料电池的燃料、用于燃烧器的燃料和/或用于地面氢化装置的原料流，但并不限于此。
在一具体实施方式中，一种用于就地处理含烃岩层的方法可包括：在选定段处于或经历某些状态时，向岩层的选定段添加氢。作为一个实施例，氢可通过位于选定段内或靠近选定段的加热器井或生产井添加。由于氢供应有时较为短缺(或制造及制作较为昂贵)，可在对岩层内添加氢的使用情况进行优化时进行添加。举例来说，在岩层经历合成气产生的断面内产生的氢可添加至经历热解作用的岩层段内。在岩层的热解段内添加的氢可促进脂族化合物形成，并防止形成使岩层所产生的烃的质量降低的烯烃化合物。
在一些具体实施方式中，待岩层的平均温度达到热解温度(例如，当选定段的温度至少约为270℃时)之后，可向选定段添加氢。在一些具体实施方式中，待平均温度至少达到约290℃、320℃、375℃或400℃之后，可向选定段添加氢。在岩层的平均温度达到约400℃之前，可向选定段添加氢。在一些具体实施方式中，在平均温度达到约300℃或约325℃之前，可向选定段添加氢。
岩层的平均温度可通过向岩层的选定段选择性地添加氢进行控制。添加至岩层内的氢可能在放热反应中发生反应。放热反应可加热岩层，并减少需要从热源向岩层提供的能量。在一些具体实施方式中，可向岩层的选定段添加的氢量应使得岩层的平均温度不大于约400℃。
阀门可维持、改变和/或控制含烃岩层加热部分的压力。作为一个实施例，置于含烃岩层内的热源可与阀门相结合。阀门可通过热源释放来自岩层的流体。此外，压力阀可与含烃岩层内的生产井结合使用。在一些具体实施方式中，由阀门所释放的流体可被收集并输送至一用于进一步加工和/或处理的地面装置。
一种用于烃的就地转化方法可包括向含烃岩层供热，以及对加热部分内的温度、增温率和/或压力进行控制。加热部分的温度和/或增温率可通过改变提供给岩层内热源的能量进行控制。
欲经受就地转化的烃可位于较大的区域之下。就地转化系统可被用来处置小部分的岩层，而其他部分的岩层可随着时间进程而被处理。在一岩层(例如油页岩岩层)处理装置的具体实施方式中，可将一24年开采情况的土地规划图划分为表示单个钻孔年度的24幅单独绘图。各图表可包括120块“瓷砖块(tiles)”(重复矩阵图案)，其中，各图表由6行20列瓷砖块组成。各瓷砖块可包括1个生产井和12或18个加热器井。加热器井可按井间距约为12m的等边三角形形式进行布置。生产井可位于加热器井的等边三角形的中心处，或者生产井可位于接近两个相邻加热器井之间的中点位置处。
加热器井、生产井等的准确位置将取决于岩层的具体变量(例如岩层层厚或岩层成分)、项目经济性等因素。在某些具体实施方式中，加热器井可基本上为水平向，而生产井则可为纵向，或者二者反过来布置。在一些具体实施方式中，各所述井的取向可为磁倾角方向或者岩层走向、或为磁倾角与走向之间的某一角度。
热源之间的间距可随许多因素而变化。这些因素可包括含烃岩层的类型、选取的加热速率和/或加热部分内所要获得的选定的平均温度，但并不限于此。在一些布井模式的具体实施方式中，热源之间的间隔可在约5m～25m的范围内。在一些布井模式的具体实施方式中，热源之间的间隔可在约8m～15m的范围内。
在某些具体实施方式中，可设置向岩层开口提供附加组分(例如，氮气、二氧化碳、诸如含氢体一类的还原剂等)的一个或多个管道，以便排放流体和/或控制压力。岩层压力在接近热源处趋向最高值。在热源内设置压力控制设备可能是较为有益的。在一些具体实施方式中，在靠近热源处添加还原剂有助于提供更为有利的热解环境(例如，氢分压更高)。由于渗透性和孔隙率势必在最接近热源处增加得更为迅速，所以在最接近热源的地方添加还原剂通常是最为优选的方案，从而还原剂可更容易地进入岩层内。
在一具体实施方式中，含烃岩层可利用岩层内的自然分布型燃烧器装置进行加热。所产生的热量可被传送至岩层的选定段。自然分布型燃烧器可氧化井眼附近的岩层内的烃，从而向选定的岩层段供热。
足以维持氧化的温度可能至少约为200℃或250℃。足以维持氧化的温度势必随着许多因素而变化(例如含烃岩层内的烃成分、岩层含水量、和/或氧化剂的类型及数量)。在加热之前可将一部分水从岩层中内除去。举例来说，可通过脱水井将水从岩层中抽出。岩层的加热部分可靠近或基本靠近含烃岩层的开口处。岩层内的开口可为形成于岩层内的加热器井。含烃岩层的加热部分可自开口处朝径向延伸约0.3m～约1.2m的宽度。当然，该宽度也可约小于0.9m。加热部分的宽度可随时间而变化。在某些具体实施方式中，该变化值所依据的因素包括：在碳氧化期间无需从另一热源供热而产生足以维持氧化反应的热量所必须的岩层宽度。
待岩层的加热部分到达足以维持氧化的温度之后，可向开口供应氧化流，以便在岩层内的反应区或热源区处对至少一部分烃进行加热。烃的氧化将在反应区处产生热量。在大多数的具体实施方式中，所产生的热量将从反应区传送至岩层内的热解区。在某些具体实施方式中，所产生的热量以约为650瓦特每米～1650瓦特每米的速度进行传送，该速度为沿反应区深度方向的测量数值。由于岩层内至少一部分烃被氧化，所以可以减少或停止向加热器供应用于将岩层初始加热至足以维持氧化的温度的能量。采用自然分布型燃烧器可显著减少能量的输入费用，从而为加热岩层提供更为明显高效的系统。
在一具体实施方式中，可在开口内布置一管道以向开口内供应氧化流体。该管道可能已具有流量孔道或其它流量控制机构(即，狭缝、文丘里流量计、阀等)，以允许氧化流体进入该开口。术语“孔道”包括具有各式各样横截面形状的孔口，该横截面形状包括圆、椭圆形、正方形、矩形、三角形、狭缝或其他规则或不规则的形状，但并不限于此。在一些具体实施方式中，流量孔道可为临界流量孔道。不论开口的压力大小，流量孔道均可向开口提供流量基本不变的氧化流体。
在一些具体实施方式中，流量孔道的数量可由孔道的直径和一节管道上孔道之间的要求间距来限制。举例来说，当孔道的直径减小时，流量孔道的数目可能增加，反之亦然。此外，当要求的间距增加时，流量孔道的数目可能减少，反之亦然。孔道的直径可由管道内的压力和/或通过该孔道的需求流速进行确定。举例来说，对于流速约为1.7标准立方米/分钟、压力约为7巴(绝对)的情况而言，孔道的直径可为约1.3毫米，孔道间距约为2米。直径较小的孔道比直径较大的孔道更易堵塞。孔道可能会因各种原因而被堵塞。这些原因可包括管道内液体流中的杂质和/或孔道内或附近的固体沉积物。
在一些具体实施方式中，选取的孔道数目及直径应使得沿岩层内开口的深度方向可获得更为均匀或近似均匀的加热断面。如果想获得近似均匀的加热断面，加热岩层的深度可约大于300米，或甚至约大于600米。当然，该深度可根据诸如加热岩层的类型和/或预期产出率一类的因素而有所变化。在一些具体实施方式中，流量孔道可绕开口内的管道周围呈螺旋线形式进行布置。螺旋线形布置形式中的流量孔道的孔道间距可约为0.3～3米。在一些具体实施方式中，该间距可约为1～2米，或作为一个实施例，约为1.5米。
可对孔道内氧化流体的流量进行控制，从而控制反应区的氧化速率。输入氧化剂和输出氧化产物之间所传送的热量可加热氧化流体。该传热过程也可将管道维持在低于管道最高运行温度的状态。
图3示出了一种自然分布型燃烧器的具体实施方式。可对开口132或反应区134长度方向上的氧化流体130的流量进行控制。开口132可被称为“细长开口”，从而反应区134和开口132沿开口的确定长度方向可具有一共同的边界。可利用一个或多个孔道(该孔道可为临界流量孔道)对氧化流体的流量进行控制。氧化流体的流量可通过孔道136的直径、孔道136的数目、和/或通过内管138内的压力(孔道136后面的压力)进行控制。通过控制氧化流体的流量这一方式可对开口132内的反应区134的表面温度进行控制。举例来说，氧化流体130流量的增加势必会使得反应区134的表面温度增加。孔道内氧化流体流量的增加势必会加快反应区内烃的氧化速率。由于烃的氧化反应是一种放热反应，所以氧化速率的加快势必会增加反应区内的温度。
在某些自然分布型燃烧器的具体实施方式中，氧化流体130的流量沿内管138的长度方向可有所变化(例如，利用临界流量孔道136)，从而反应区134的表面温度也会有所变化。可以改变反应区134表面处或开口132内的温度，以控制反应区134内的传热速率和/或选定段140内的加热速率。反应区134表面温度的增加可使得选定段140内的加热速率增加。可对氧化产物144的性能(例如含氧量、含氮量、温度等)进行监测。氧化产物144的性能可被监测，并且可被用于控制输入自然分布型燃烧器中的性能(例如，氧化流体输入性能)。
氧化流体130通过反应区134的扩散速率可随反应区的温度和临近反应区的温度而有所变化。一般而言，温度越高，随着气体中的能量增加，所以气体扩散的速度也就更快。开口内的温度可被确定(例如，通过热电偶进行测定)并与反应区的温度相关。开口内的温度可通过控制从内管138流入开口内的氧化流体的流量进行控制。举例来说，增加氧化流体进入开口的流量可提高开口内的温度。而减少氧化流体进入开口的流量可降低开口内的温度。在一具体实施方式中，氧化流体的流量可一直增加，直至达到低于使用设备的冶金温度极限的选定温度。举例来说，氧化流体的流量可一直增加，直至达到用于开口内所设管道的金属的工作温度极限。金属的温度可直接利用一热电偶或其他温度测量装置进行测量。
在一自然分布型燃烧器的具体实施方式中，可防止在反应区134内产生二氧化碳。反应区氢浓度的增加可防止反应区内产生二氧化碳。氢的浓度可通过向反应区内输送氢得以增加。在一具体实施方式中，氢可由选定段140传送至反应区内。氢可在烃热解的过程中于选定段内产生。氢可通过漫射和/或对流方式由选定段传送至反应区内。此外，附加的氢可通过开口内所设置的管道供入开口132内或岩层内的另一开口内。附加的氢可由开口132传入反应区内。
在一些自然分布型燃烧器的具体实施方式中，热量可由自然分布型燃烧器的井眼内的第二热源提供给岩层。举例来说，一用于对一部分岩层预加热的电加热器(例如，一绝缘导体加热器或一管道内导体加热器)也可用于随着来自自然分布型燃烧器的热量向岩层供热。此外，可将一附加的电加热器设置于岩层内的开口中，以便向岩层提供附加热。电加热器可用于向岩层供热，从而由电加热器和自然分布型燃烧器联合提供的热量可维持在一恒定的热量输入率水平上。由电加热器输入岩层内的热量可随着自然分布型燃烧器输入的热量变化而变化，或反之亦然。由一种以上的热源进行供热可使得岩层加热基本均匀。
在某些就地转化方法的具体实施方式中，可由电加热器向岩层输入总热量的10％、25％或50％。由电加热器输入岩层内的热量百分比可随着例如电费、自然分布型燃烧器的输入热量而有所变化。来自电加热器的热量可用于补偿来自的自然分布型燃烧器的低输出热量，从而使得岩层内的加热速率基本保持不变。如果电费增加，则从自然分布型燃烧器发出的热量可能会较多，以减少电加热器的供热量。在一些具体实施方式中，来自电加热器的热量可因电源(例如，太阳发电或风力发电)的不同而有所变化。在这些具体实施方式中，可通过自然分布型燃烧器来提供或多或少的热量来抵消电热输入量的变化。
在一热源的具体实施方式中，电加热器可用来防止自然分布型燃烧器“烧尽”。如果一部分岩层在足以维持燃烧的温度下冷却，则自然分布型燃烧器可能会“烧尽”。来自电加热器的附加热量可能需要向该部分岩层和/或其他部分岩层供热，以将一部分岩层加热至足以维持烃氧化、并且保持自然分布型燃烧器进行加热的温度。
在一些自然分布型燃烧器的具体实施方式中，电加热器可用于向接近岩层上部和/或下部的岩层提供更多的热量。利用来自电加热器的附加热可弥补岩层上部和/或下部的热量损失。用电加热器向接近上部和/或下部的部位提供附加热量可为岩层产生更加均匀的热量。在一些具体实施方式中，电加热器可与其他类型的燃料加热器，例如无焰分布燃烧器或井下燃烧器相结合来用于类似的目的(例如，在上部和/或下部供热、提供辅助热量、提供保持最小燃烧温度的热量等等)。
在一些就地转化方法的具体实施方式中，从燃料加热器(例如，自然分布型燃烧器或井下燃烧器)中排出的流体可用在空气压缩机中，该空气压缩机位于靠近用于燃料加热器的开口的岩层表面处。排出的流体可用于驱动空气压缩机，并且降低与供燃料加热器之用的压缩空气相关的费用。利用涡轮或类似装置排出的流体也可产生电流。在一些具体实施方式中，可利用一个压缩机或一系列的压缩机来提供一个或多个燃料加热器所使用的流体(例如，氧化流体和/或燃料)。压缩机可为一个或一个以上的加热器提供氧化流体和/或燃料。此外，可由供一个或一个以上的加热器使用的集中设备来提供氧化流体和/或燃料。
在选定加热段140中可进行烃的热解作用或其他加热-控制程序。选定段140可在约270℃～400℃之间进行热解。选定段140的温度可因从反应区134传送来的热量而升高。
开口132内的温度可通过一置于开口132内的热电偶进行监测。备择地，热电偶可与管道142相连，和/或可置于反应区134的表面处。引入岩层内的输入功率或氧化剂可基于监测温度进行控制，以维持选定范围内的温度。所选定的范围可根据热电偶的位置、含烃岩层108的预期加热速率及其他因素而有所不同。如果开口132内的温度降至选定温度范围的最低温度以下，则氧化流体130的流速可能增加，以增大燃烧程度，从而增加开口132内的温度。
在某些具体实施方式中，一个或多个自然分布型燃烧器可沿烃岩层的走向和/或水平向布置。沿走向或水平向布置的自然分布型燃烧器可减小热源加热长度方向上的压差。压差减小后可使得沿加热器长度方向产生的温度更均匀，也更容易控制。
在一些具体实施方式中，可以监测对氧化产物144中的空气或氧(2)的存在量。备择地，也可对氧化产物144中的氮气、一氧化碳、二氧化碳、氮氧化物、硫氧化物等的含量进行监测。排出产物(例如，氧化产物144)成分和/或数量的监测对于热量平衡、工艺识别、工艺控制等较为有用。
图4示出了表示一自然分布型燃烧器的具体实施方式的横断面图，该燃烧器具有置于含烃岩层108内开口132中的第二管道146。第二管道146可用于从开口132中取出氧化产物。第二管道146沿其长度方向可设置孔道136。在某些具体实施方式中，氧化产物通过第二管道146上设置的孔道136从开口132的上部区域被去除。孔道136可沿管道146的长度方向进行布置，从而从开口132的上部区域可去除更多的氧化产物。
在某些自然分布型燃烧器的具体实施方式中，第二管道146上的孔道136可避开管道138上的孔道136。其取向可防止通过管道138提供的氧化流体直接进入第二管道146。
在一些具体实施方式中，管道146朝开口132的上部区域方向可具有较密的孔道136(和/或较大直径的孔道136)。氧化产物由开口132的上部区域优先去除这一作法可使得沿开口132的长度方向所产生的氧化流体的浓度基本均匀。在靠近开口132的上部区域处，由反应区134所产生的氧化产物的浓度势必更大。开口132上部区域内的氧化产物144的巨大浓度势必稀释上部区域中氧化流体130的浓度。由开口132的上部区域去除相当份量的超浓缩氧化产物可为整个开口132形成浓度更加均匀的氧化流体130。氧化流体在整个开口范围内浓度更加均匀可使得流入反应区134内的氧化流体所产生的驱动力更加均匀。更加均匀的驱动力可使得反应区134内所产生的氧化速度更加均匀，并且因而使得选定段140内产生的加热速率更为均匀，和/或使得开口132内产生的温度更为均匀。
在一自然分布型燃烧器的具体实施方式中，可对反应区内的空气和/或氧的浓度进行控制。人们可能希望在反应区内分布的氧(或氧浓度)更加均匀。反应速率可作为反应区内氧的扩散速率的函数进行控制。氧的扩散速率与氧浓度相互关联。因而，通过对反应区内的氧浓度进行控制(例如，通过控制氧化流体的流动速率、沿反应区的一部分或全部长度去除氧化产物、和/或沿反应区的一部分或全部长度分配氧化流体)可控制反应区内的氧扩散，并从而控制反应区内的反应速率。
在所述具体实施方式中，导体170置于开口132内。导体170可由开口132的第一端148延伸至开口132的第二端150。在某些具体实施方式中，导体170可设置于烃岩层108中的开口132内。一处或多处低电阻截面174可与导体170相连并被用于上覆岩层158中。在一些具体实施方式中，导体170和/或低电阻截面174可延伸至岩层地面之上。
在一些热源的具体实施方式中，可向导体170通电，以增加导体的温度。热量可从导体170传送至烃岩层108的加热部分152。热量可基本通过辐射方式从导体170传送至加热部分152。也可通过对流方式或传导方式传送一部分热量。可向导体供电，直至加热部分152内的温度足以维持加热部分内烃的氧化作用。如图5所示，可在开口132的一端或两端148、150从氧化流体源154向导体170提供氧化流体。氧化流体由导体流入开口132的流量可通过孔道136进行控制。该孔道可为临界流量孔道。来自孔道136的氧化流体的流量可由孔道直径、孔道数目、和/或导体170内的压力(即，孔道后面的压力)进行控制。
氧化流体与反应区134内烃发生反应可产生热量。反应区134内的热量产生速率可由氧化流体进入岩层的流速、氧化流体通过反应区的扩散速率、和/或氧化产物从岩层中去除的速率进行控制。在一具体实施方式中，氧化流体与岩层内烃发生反应的氧化产物通过开口132的一端或两端去除。在一些具体实施方式中，管道可设置于开口132内以去除氧化产物。氧化产物的全部或部分可在其他氧化型加热器(例如，自然分布型燃烧器、表面燃烧器、井下燃烧器等)中回收或再利用。反应区134中产生的热量可传送至岩层的周围部分(例如，选定段)。反应区134和选定段之间的热量传送可基本上通过传导方式进行。在某些具体实施方式中，所传送的热量可使得选定段的温度增加至大于烃的最小流通温度和/或烃的最小热解温度。
在一些热源的具体实施方式中，管道可设置于开口内。开口可在第一位置和第二位置处延伸穿过接触地面的岩层。氧化流体可在第一位置和/或第二位置处从氧化流体源提供给管道，所述位置位于已由氧化流体加热至足以维持烃氧化的温度后的一部分岩层的后面。
图6示出了具有一如图3所示的自然分布型燃烧器的上覆岩层断面的具体实施方式。上覆岩层套管156可置于烃岩层108的上覆岩层158内。上覆岩层套管156可由防止上覆岩层158加热的材料(例如，诸如水泥一类的绝缘材料)所围绕。上覆岩层套管156可由金属材料，例如碳素钢或304不锈钢制成，但并不限于此。
上覆岩层套管156可置于上覆岩层158中的增强材料160内。增强材料160可为水泥、砂砾、沙和/或混凝土，但并不限于此。在上覆岩层套管156与岩层内的开口132之间可布置密封材料162。密封材料162可为任何基本无孔的材料(例如，水泥、混凝土、水泥浆等)。密封材料162可防止流体流到管道142之外以及开口132与地面110之间。内管138可将流体引入烃岩层108中的开口132内。管道142可从烃岩层108中的开口132去除燃烧产物(或过度氧化流体)。管道142的直径可通过在自然分布型燃烧器中因氧化作用而产生的燃烧产物的数量进行确定。举例来说，对于自然分布型燃烧器型加热器所产生的大量排出产物而言，可能需要较大的直径。
在一些热源的具体实施方式中，靠近井眼的一部分岩层可能以一定的加热速率被加热至一温度，从而通过第一热源在邻近井眼位置处，将烃转换成焦炭或木炭。焦炭和/或木炭可在温度约大于400℃时形成。氧化流体存在时，焦炭或木炭将氧化。井眼可在焦炭和/或木炭形成之后用作自然分布型燃烧器。通过焦炭或木炭的氧化作用可产生热量。
图7示出了一种自然分布型燃烧器型加热器的具体实施方式。绝缘导体164可与管道166相连并被置于含烃岩层108中的开口132内。绝缘导体164可置于管道166内(从而允许绝缘导体164取回)，或备择地，与管道166的外表面相连。导体所用的绝缘材料可包括无机涂层和/或陶瓷涂层，但并不限于此。管道166可在开口132内沿其长度方向布置有临界流量孔道136。可向绝缘导体164通电以在开口132内产生辐射热。管道166可用于回收电流。绝缘导体164可将含烃岩层108的一部分152加热至足以维持烃氧化的温度。
氧化流体源154可向管道166内供入氧化流体。氧化流体可通过管道166中的临界流量孔道136供入开口132内。氧化流体可氧化反应区134中的至少一部分含烃岩层。在反应区134中产生的一部分热量可通过对流、辐射和/或传导传送至选定段140。氧化产物可通过置于开口132内的单独管道去除，或通过上覆岩层套管156内的开口168去除。
图8示出了具有附加燃料管道的一自然分布型燃烧器型加热器的具体实施方式。燃料管道170可置于开口132内。在某些具体实施方式中，燃料管道可置于靠近管道172的位置处。燃料管道170可沿其长度方向在开口132内设置临界流量孔道174。管道172可在开口132内沿其部分长度设置临界流量孔道136。临界流量孔道174、136的位置应使得通过燃料管道170提供的燃料流体以与通过管道172提供的氧化流体不会发生反应从而造成对燃料管道和管道进行加热。如果在靠近燃料管道170和/或管道172处发生反应，则由于燃料流体与氧化流体发生反应而产生的热量可使得燃料管道170和/或管道172加热至一温度，该温度足以开始熔化燃料管道170和/或管道172内的冶金材料。燃料管道170上的临界流量孔道174以及管道172上的临界流量孔道136的位置应使得燃料流体和氧化流体在靠近上述管道时不会发生反应。作为一个实施例，管道170和172的位置应使得围绕上述孔道螺旋形布置的孔道取向相反。
燃料流体与氧化流体发生反应可产生热量。在一些具体实施方式中，燃料流体可为甲烷、乙烷、氢、或在岩层的其他部分通过就地转化而产生的合成气。所产生的热量可将部分152加热至足以维持烃氧化的温度。待所述部分152被加热至足以维持氧化作用的温度后，可减少或停止供应流入开口132内的燃料流体的流量。在一些具体实施方式中，燃料可在岩层的整个加热过程中持续供应。
氧化流体可氧化反应区134中的至少一部分烃。所产生的热量可通过辐射、对流和/或传导将热量传送至选定段140。氧化产物可通过设置于开口132内的单独管道去除，或通过上覆岩层套管156中的开口168去除。
图9示出了可加热含烃岩层的系统的具体实施方式。电加热器176可设置于含烃岩层108中的开口132内。开口132可穿过上覆岩层158形成于含烃岩层108内。开口132的直径可至少为约5厘米。作为一个实施例，开口132的直径可约为13厘米。电加热器176可将含烃岩层108的至少一部分152加热至足以维持氧化作用的温度(例如，约260℃)。部分152的宽度可约为1米。氧化流体可通过管道142或任何其他适当的流体输送机构供入开口内。管道142可沿管道长度方向设置临界流量孔道136。
管道142可为从氧化流体源154向开口132内提供氧化流体的导管或管子。在一具体实施方式中，可能接触高温的管道部分142为不锈钢管，而不可能接触高温的管道部分(即贯穿上覆岩层的管道部分)为碳素钢管。氧化流体可包括空气或任何其他含氧流体(例如，过氧化氢、氮氧化物、臭氧)。也可使用各种氧化流体的混合物。一种氧化流体混合物可为包含50％氧和50％氮气的流体。在一些具体实施方式中，氧化流体可包括加热时释放氧的化合物，例如过氧化氢。氧化流体可氧化岩层内的至少一部分烃。
图10示出了一种含烃岩层加热系统的具体实施方式。热交换器178可设置于含烃岩层108内的开口132的外部。开口132可穿过上覆岩层158形成于含烃岩层108内。热交换器178可根据另一地面方法提供热量，或可包括一加热器(例如，电加热器或燃气加热器)。氧化流体源154可向热交换器178提供氧化流体。热交换器178可对氧化流体进行加热(例如，加热至大于200℃或足以维持烃氧化作用的温度)。被加热的氧化流体可通过管道180供入开口132内。管道180可沿管道长度方向设置临界流量孔道136。加热后的氧化流体可使得至少部分岩层152被加热，或至少有助于使其被加热至一足以维持烃氧化的温度。氧化流体可氧化岩层内的至少一部分烃。在岩层温度足以维持氧化作用之后，可减少使用或逐渐停用热交换器178。
在一自然分布型燃烧器的具体实施方式中，可包括一表面燃烧器(例如，点火加热器)。燃料流体可在燃烧器内进行氧化。氧化燃料流体可通过管道由加热器供入岩层的开口内。氧化产品和未反应的燃料可通过另一管道返回地面。在一些具体实施方式中，管道中的一个可置于另一管道内。氧化流体可使得一部分岩层被加热，或至少有助于将其加热至一足以维持烃氧化的温度。在达到足以维持氧化作用的温度后，氧化燃料流体可替换为一种氧化流体。氧化流体可氧化岩层中的反应区内的至少一部分烃。
电加热器可将一部分含烃岩层加热至足以维持烃氧化的温度。该部分可能接近或基本接近岩层内的开口。该部分可能由开口沿径向延伸一约小于1m的宽度。可向该开口供入用于氧化烃的氧化流体。在自然分布型燃烧器的方法中，烃的氧化作用可使得含烃岩层被加热。随后，可减少使用或停掉通到电加热器的电流。自然分布型燃烧器可与一种电加热器结合使用，以提供一种相对于仅用一种电加热器加热含烃岩层而言输入能量成本减少的方法。
鉴于本说明书，本领域技术人员显然可对本发明作出各种进一步的修改或备择实施方式。因此，可认为本说明书仅为例证，目的在于教会本领域技术人员实施本发明的一般方式。可以理解，此处所图示和描述的发明形式应当认为是目前的优选实施方式。文中所示意和描述的配件和材料是可以替代的，零件和方法可以是相反的，本发明的有些特征可以独立使用，对于已从本发明的说明书中受益的本领域技术人员来说，所有这些都是显而易见的。在不背离如下权利要求书所述的本发明的精神和范围的前提下，可对文中所描述的配件进行改变。

Claims (32)

1.一种可配置成向一含烃岩层供热的系统，包括：
一可配置成位于所述岩层的一开口内的加热器，其中所述加热器可配置成在使用期间向至少一部分所述岩层供热；
一种氧化流体源，可配置成在使用期间向所述岩层的一反应区供应一种氧化流体，以便在所述反应区内产生热量；
一可配置成位于所述开口内的第一管道，其中所述第一管道可配置成在使用期间由所述氧化流体源向所述岩层内的反应区提供所述氧化流体；以及，
其中，所述系统可配置成使得所产生的热量在使用期间由所述反应区向所述岩层传送。
2.根据权利要求1所述的系统，其特征在于，至少一部分所述反应区在使用期间已由所述加热器预先加热。
3.根据权利要求1至2之一或多个所述的系统，其特征在于，所述氧化流体在使用期间对所述反应区内的至少一部分烃进行氧化。
4.根据权利要求1至3之一或多个的系统，其特征在于，所述氧化流体在使用期间基本上被阻止由所述反应区流入所述岩层的周围部分。
5.根据权利要求1至4之一或多个所述的系统，其特征在于，所述系统可配置成在使用期间使得所述氧化流体基本通过漫射方式传送通过所述反应区。
6.根据权利要求1至5之一或多个所述的系统，其特征在于，所述系统可配置成在使用期间使得所产生的热量由所述反应区传送至所述岩层内的一热解区。
7.根据权利要求1至6之一或多个所述的系统，其特征在于，所述系统可配置成在使用期间使得所产生的热量基本通过传导方式由所述反应区传送至所述岩层。
8.根据权利要求1至7之一或多个所述的系统，其特征在于，可沿至少一段所述第一管道对所述氧化流体的流量进行控制，从而在使用期间可沿至少一段所述第一管道对温度进行控制。
9.根据权利要求1至8之一或多个所述的系统，其特征在于，可沿至少一段所述第一管道对所述氧化流体的流量进行控制，从而在使用期间可对至少一段所述第一管道的加热速率进行控制。
10.根据权利要求1至9之一或多个所述的系统，其特征在于，所述氧化流体可配置成在使用期间基本通过扩散方式传送通过所述反应区，其中，可通过所述反应区的温度对扩散速率进行控制。
11.根据权利要求1至10之一或多个所述的系统，其特征在于，所述第一管道包括孔道，并且所述孔道在使用期间将所述氧化流体供入所述开口内。
12.根据权利要求1至11之一或多个所述的系统，其特征在于，所述第一管道包括临界流量孔道，并且所述临界流量孔道用于控制所述氧化流体的流量，从而在使用期间对所述岩层内的氧化速率进行控制。
13.根据权利要求1至12之一或多个所述的系统，其特征在于，至少一部分所述氧化流体的流量可沿至少一段所述第一管道进行控制。
14.根据权利要求1至13之一或多个所述的系统，其特征在于，至少部分所述岩层由所述开口沿径向延伸约小于3米的距离。
15.根据权利要求1至14之一或多个所述的系统，其特征在于，所述反应区由所述开口沿径向延伸约小于3米的距离。
16.根据权利要求1至15之一或多个所述的系统，其特征在于，所述系统使得所传送的热量在所述岩层的一热解区内热解至少一部分烃。
17.根据权利要求1至16之一或多个所述的系统，其特征在于，所述系统在使用期间向所述反应区提供分子氢。
18.根据权利要求17所述的系统，其特征在于，所述至少一部分供应氢在使用期间产生于一热解区内。
19.根据权利要求17至18之一或多个所述的系统，其特征在于，所述至少一部分供应氢在使用期间产生于所述反应区内。
20.根据权利要求17至19之一或多个所述的系统，其特征在于，所述至少一部分供应氢在使用期间产生于所述岩层的至少加热部分内。
21.根据权利要求17至20之一或多个所述的系统，其特征在于，所述系统在使用期间向所述反应区提供氢，从而防止在所述反应区产生二氧化碳。
22.根据权利要求1至21之一或多个所述的系统，其特征在于，所述系统还包括一可配置成位于所述开口内的第二管道，其中，所述第二管道可进一步配置成在使用期间去除一种氧化产物的形式。
23.根据权利要求22所述的系统，其特征在于，所述第二管道可进一步配置成在使用期间去除一种氧化产物的形式，从而所述反应区由一基本均匀的温度断面组成。
24.根据权利要求22至23之一或多个所述的系统，其特征在于，所述第二管道可配置成在使用期间对所述开口内的氧浓度进行控制，从而所述开口内的氧浓度在开口内基本为常量。
25.根据权利要求22至24之一或多个所述的系统，其特征在于，所述第二管道包括将所述氧化产物从一与所述第一管道基本相反的方法去除的孔道。
26.根据权利要求22至25之一或多个所述的系统，其特征在于，所述第二管道包括孔道，并且所述第二管道在朝第二管道的上端方向包括分布较密的孔道。
27.根据权利要求22至26之一或多个所述的系统，其特征在于，所述第一管道包括沿一与所述第二管道基本相反的方向引导氧化流体的孔道。
28.根据权利要求22至27之一或多个所述的系统，其特征在于，所述第二管道可进一步配置成在使用期间将所述氧化产物内的热量传送至第一管道内的氧化流体中。
29.根据权利要求22至28之一或多个所述的系统，其特征在于，所述第一管道内的氧化流体的压力与所述第二管道内的氧化产物的压力在使用期间受到控制，从而使得沿所述第一管道长度方向的氧化流体的浓度基本均匀。
30.一种根据权利要求1至29之一或多个所述的向含烃岩层供热的系统，包括：
一配置成位于所述岩层的一开口内的加热器，其中所述加热器在使用期间可向至少一部分所述岩层供热；
一种氧化流体源，可在使用期间向所述岩层的一反应区供应一种氧化流体，以便在所述反应区内产生热量；
一置于所述开口内的第一管道，其中，所述第一管道在使用期间由所述氧化流体源向所述岩层内的反应区提供所述氧化流体；以及，
其中，所述系统使得所产生的热量在使用期间由所述反应区向所述岩层传送。
31.一种根据权利要求1至29之一或多个所述的向含烃岩层供热的系统，包括：
一置于所述岩层的一开口内的加热器，其中，所述加热器在使用期间可向至少一部分所述岩层供热；
一种氧化流体源，其在使用期间向所述岩层的一反应区供应一种氧化流体，以便在所述反应区内产生热量；
一置于所述开口内的第一管道，其中，所述第一管道在使用期间由所述氧化流体源向所述岩层内的反应区提供所述氧化流体；以及，
其中，所述系统使得所产生的热量在使用期间由所述反应区向所述岩层传送。
32.根据权利要求1至31之一或多个所述的系统，其特征在于，所述开口的第一端在第一位置处与地面接触，并且所述开口的第二端在第二位置处与所述地面接触。
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