CN101636627B - 使用交叉波纹规整填料塔分离气体混合物的分离方法 - Google Patents

使用交叉波纹规整填料塔分离气体混合物的分离方法 Download PDF

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CN101636627B
CN101636627B CN2008800023805A CN200880002380A CN101636627B CN 101636627 B CN101636627 B CN 101636627B CN 2008800023805 A CN2008800023805 A CN 2008800023805A CN 200880002380 A CN200880002380 A CN 200880002380A CN 101636627 B CN101636627 B CN 101636627B
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M·科尔伯格
F·勒克莱尔
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Abstract

本发明涉及一种气体的低温分离方法，所述气体的主要成分包括选自下列组的至少两种成分：氢、一氧化碳、氮和甲烷，该方法使用至少一个具有交叉波纹规整填料的蒸馏塔(K02/K03)和/或至少一个具有交叉波纹规整填料的吸收塔(K01)，其中至少一个区段用于下降的液体和上升的气体之间的热量和/或物质交换，所述区段的参数S的范围介于50×10-6和70000×10-6之间，更特别地介于150×10-6和1500×10-6之间，其中S＝T×m/σ，T是液/汽界面处的剪切应力(kgm-1s-2)，m是在填料上流动的液膜厚度(m)以及σ是液/汽界面处的表面张力(kgs-2)。

Description

使用交叉波纹规整填料塔分离气体混合物的分离方法
本发明涉及一种使用交叉波纹规整填料塔分离气体混合物的分离方法。
用于分离一氧化碳和氢的混合物的传统装置仅包括具有板的塔，而新一代的这类装置使用不具有改良/修改界面的交叉波纹规整填料塔的技术(EP-A-0 837 031)。由于以下事实，在这些装置中填料的使用仍然棘手，即，对分离效率、可湿性和发泡性能等具有影响的物理特性与空气的物理特性不具有可比性。这些规整填料在界面上具有局部压降，这可能是待分离混合物的可能的发泡源。发泡的存在妨碍了各种待生产的产品的正确的分离运行。
本发明的优点在于防止在专门用于混合物分离的部分中有泡沫生成。可以控制可能的泡沫生成的参数之一可由下列无量纲数概括得到：S＝τm/σ，其中τ是液/汽界面上的剪切应力(kgm-1s-2)，m是在填料上流过的液体膜厚度(m)以及σ是液/汽界面上的表面张力(kgs-2)。因此，如专利US-A-5644932所述，该参数使气体在液体上形成的剪切应力与液体的表面张力相关联。看来，在本发明的应用中，这个因子/系数S的值的范围应当介于50×10-6和7000×10-6之间，优选是介于150×10-6和1500×10-6之间。
该参数可以通过几种方式进行调节：
●通过调节填料的几何参数(在同一区段之内或在两个不同的区段之间)，也就是说：
○通道相对于水平方向的倾斜角度δ(优选是介于30°和70°之间)；
○波纹的弯折角度γ(优选是介于40°和150°之间)；
○至少在填料中心区域的填料密度(优选是介于300m2/m3和1000m2/m3之间)；
○填料的开孔率(优选是介于3％和20％之间)；
○填料的孔的直径(优选是介于1mm和4mm之间)；以及
○波纹在从其中波纹相对于垂直方向倾斜一给定角度的中心区域到其中波纹相对于垂直方向倾斜一较小角度、或者甚至是垂直的边缘区域的曲率半径(优选是介于0.5mm和3mm之间)；
●通过逐渐改变通道的倾斜角度，如专利WO 97/16247所述，以使所述通道在所述角度的高、低末端越来越垂直。
在这些运行范围(通过调节一个或多个前文提到的参数而运行)内工作的主要优点在于分离能力的优化，或更特别地在于对于给定分离能力的塔直径的减小。因此，通过这些调节手段可以大大地减少塔的投资费用，从而大大减少冷箱的投资费用。低温设备的总体减小也容许在启动和转换阶段中提高设备的灵活性，这是第二个优点。
根据本发明的一个主题，提供了一种气体的低温分离方法，所述气体的主要成分包括选自下列组中的一组的至少两种成分：i)氢、一氧化碳、氮和甲烷；ii)氮、氧、氩；以及iii)二氧化碳、氢、氮、氧、氩，该方法使用至少一个具有交叉波纹规整填料的蒸馏塔和/或至少一个具有交叉波纹规整填料的吸收塔，其中至少一个区段用于下降的液体和上升的气体之间的热量和/或质量交换，其特征在于，该区段的参数S介于50×10-6和70000×10-6之间，其中S＝τm/σ，τ是液/汽界面上的剪切应力(kgm-1s-2)，m是在填料上流过的液膜厚度(m)以及σ是液/汽界面上的表面张力(kgs-2)。
根据该方法的其他特征：
-在所述用于热量和/或质量交换的区段中的至少一个填料体包括中心区域和下部区域和可选的上部区域，所述下部区域和可选的上部区域相对于中心区域被改良/修改为使得其中液体的上升阻力相对于中心区域的上升阻力而减小；
-所述气体的主要成分包括氢、一氧化碳、甲烷以及可选的氮；
-所述气体的主要成分包括氢、一氧化碳和可选的甲烷以及氮；
-填料在以下条件下操作，即，进气量F介于0.2-2.5(Nm-2)0.5之间，其中F＝(ρvvgas)0.5，并且/或者填料中的以L/dm2/h为单位的液体流率可从50变化至高达600L/dm2/h；
-所述气体的主要成分包括选自下列组的至少两种成分：氢，一氧化碳，氮和甲烷，其中，该区段中的参数S介于50×10-6和7000×10-6之间，更特别地介于150×10-6和1500×10-6之间；
-所述气体的主要成分包括选自下列组的至少两种成分：氮、氧、氩，如前述权利要求1-5中的任一项权利要求所述，其中，该区段中的参数S介于500×10-6和70000×10-6之间；
-在用于热量和/或质量交换的区段中的至少一个填料体包括中心区域和下部区域，所述下部区域相对于中心区域被改良为使得其中液体上升的阻力相对于中心区域中的上升阻力减小；
-塔的内径随着进气量和用于待分离气体的进液量而从一个区段至另一个区段变化；
-填料的密度至少在一个中心区域为300m2/m3至1000m2/m3；
-填料的至少一个特征在同一区段中变化，所述特征选自下列组：
○填料密度；
○倾斜角度；
○弯折角度；
○曲率半径；以及
○开孔率，
-填料的至少一个特征从一个区段至另一个区段变化，所述特征选自下列组：
○填料密度；
○倾斜角度；
○弯折角度；
○曲率半径；以及
○开孔率。
本发明将参照附图更详细地加以描述，其中，图1示出根据本发明的甲烷洗涤/涤气过程，图2示出根据本发明的部分冷凝过程，图3示意性地示出波纹轴(axe des ondes)上的波纹的视图，图4是波纹片(lamelleondulée)的示意性俯视图，图5示出根据本发明的用于分离二氧化碳的方法，以及图6示出根据本发明的空气分离方法。
在甲烷洗涤系统(图1)中，通过塔K01内的液态甲烷对受压并冷却至-180℃的合成气进行洗涤，所述塔K01在高压(介于12和50bara之间)和尽可能低的温度下运行，一氧化碳被羁留在塔的底部而在顶部生成氢。
塔K01具有至少一个如WO 97/16247所描述的填料体。使用具有改良界面的这种填料尤其有利，因为与其他气体相比具有很低压降的氢允许在很高的进气量下运行而不会明显降低分离效率。具有改良界面的填料段之间的界面处的较小突变可使运行的参数S更稳定，降低了在两个填料体之间的界面上发泡的风险，并使塔在稳定的状态和更可靠的转换下运行。
溶解的氢随后排入中压闪蒸塔K02。CO/CH4的二元混合物随后在低压蒸馏塔K03中分离。在顶部生成气态CO，在底部生成的液态甲烷被泵送并再循环以用于K01中的洗涤操作。
在CO循环中产生制冷能力。
其他塔K02、K03也可容纳具有改良或未经改良的界面的交叉波纹规整填料。
所有塔都在因子S介于50×10-6和3000×10-6之间，更特别地介于150×10-6和1500×10-6之间的情况下运行。
在带有部分冷凝的系统(图2)中，在K11中通过来自B01的液态CO洗涤去除其甲烷的合成气被冷却至可能的最低温度，所述最低温度受CO的固化温度所限；在B02中冷凝的液体主要是CO。
闪蒸塔K12和K13分别除去在K11的底部液体(富含甲烷)中和在来自罐B02的液体(富含CO)中溶解的氢。
来自塔K12和K13的液体随后流入蒸馏塔K14中，在所述蒸馏塔K14中进行CO/CH4的分离。在该CO/CH4分离塔(K14)——该分离塔具有至少两个在截然不同的回流下运行的填料区段——中，使用具有不同密度和/或倾斜角度的填料区段可以优化整个塔的参数S。
其他塔K02、K03也可容纳具有改良或未经改良的界面的交叉波纹规整填料。
通过氢在涡轮机中的膨胀获得制冷能力。
在有氮存在的特别情况下，可在CO/CH4塔的下游添加N2/CO分离塔。
所有塔都在因子S介于50×10-6和7000×10-6之间，更特别地介于150×10-6和1500×10-6之间的情况下运行。
下面是甲烷洗涤塔的因子S的计算示例。
在密度为650m2/m3的规整填料中，不纯的/含杂质的氢的线性压降为1.2mbar/m：
τ = D h 4 · ΔP ΔL = 0.0062 m 4 · 120 N m 3 = 0.186 N m 2
在上升的氢中，(温度为)93K的液态甲烷的层流液膜厚度为：
m = [ 3 · μ L · Γ ρ L · ( ρ L - ρ V ) · g ] 1 / 3 = [ 3 · 0.00021 kg / m · s · 0.0052 kg / m · s 460 kg / m 3 · ( 460 kg / m 3 - 7.7 kg / m 3 ) · 9.81 m / s 2 ] 1 / 3 = 0.000117 m
对于(温度为)93K的液态甲烷，表面张力σ＝0.018N/m
S = τ · m σ = 0.186 N / m 2 · 0.000117 m 0.018 N / m = 1209 * 10 - 6
ReL＜2000的下降液膜/降膜中层流条件的验证：
R e L = 4 · Γ μ L = 4 · 0.0052 kg / m · s 0.00021 kg / m · s = 99
符号表
τ       汽/液界面处的剪切应力(N/m2)
σ       液体的表面张力(N/m)
γ       交换表面区域每单位宽度的液体质量流量(kg/m/s)
μL      气体的动力粘度(kg/m/s)
ρL      液体的密度(kg/m3)
ρV      蒸汽的密度(kg/m3)
Dh       规整填料通道的水力直径(m)
ΔP/ΔL  气体在垂直方向上的线性压降(N/m3)
m        液膜的厚度(m)
g        重力常数(9.81m/s2)
S        无量纲参数，表征汽/液界面处的内力和外力
ReL      下降液膜的雷诺数(无量纲)
图3示出具有高H、弯折角γ的波纹的填料片(lamelle de garnissage)。
图4所示是薄片1，具有倾斜的平行波纹，其中波峰2用粗线示出，波谷3用细线示出。
波纹的倾度由波峰2与中心区域C的下边缘4之间形成的角度δ限定。上部区域S从元件的上边缘4a延伸到中心区域C的上限，而下部区域I从该元件的下边缘延伸到中心区域C的下限，每个区域S、I都具有高度h’。波峰和边缘4之间形成的角度为δ1＝90°，但也可以取其他值。
图5示出根据本发明通过蒸馏分离二氧化碳的工艺。混合有氮、氧和氩的二氧化碳流1在交换器3中冷却，在具有塔顶冷凝器和塔底再沸器的蒸馏塔5中分离。将来自塔5的底部液体7送入具有塔顶冷凝器和塔底再沸器的塔9中。在塔9的顶部生成流11，并在底部生成流13。流13是富含二氧化碳的液体产品，流11中含有氮、氩和氧。EP-A-503910中详细描述了该工艺。专利申请US 60/890233、US 11/695422、US 11/695446、US11/695455和US 11/695471给出了可以按照本发明的方法运行的装置的其他示例。
图6示出了按照本发明的方法运行的双塔式空气分离塔。其他类型的塔也能够按照本发明运行，例如单塔、混合塔、三塔、氩分离塔等。
经冷却、压缩和净化的空气601被送到与低压塔609热连接的中压塔605的底部。来自该中压塔的回流607和603被送入低压塔。从低压塔抽出富含氧的流613和富含氮的流611。

Claims (9)

1.一种气体的低温分离方法，所述气体包括选自下列组中的一组的至少两种成分作为该气体的主要成分：i)氢、一氧化碳、氮和甲烷；ii)氮、氧、氩；以及iii)二氧化碳、氢、氮、氧、氩，该方法使用至少一个具有交叉波纹规整填料的蒸馏塔(K02、K03、505、509、605、609)和/或至少一个具有交叉波纹规整填料的吸收塔(K01)，其中至少一个区段用于下降的液体和上升的气体之间的热量和/或质量交换，其特征在于：该区段的参数S介于50×10-6和70000×10-6之间，其中S＝τm/σ，τ是以kgm-1s-2为单位的液/汽界面处的剪切应力，m是以m为单位的在填料上流过的液膜厚度，以及σ是以kgs-2为单位的液/汽界面处的表面张力。
2.如权利要求1所述的方法，其特征在于，在所述用于热量和/或质量交换的区段中的至少一个填料体包括中心区域(C)和下部区域(I)，所述下部区域相对于中心区域被改良为使得其中液体的上升阻力相对于中心区域中的上升阻力减小。
3.如权利要求2所述的方法，其特征在于，所述至少一个填料体包括上部区域(S)，所述上部区域相对于中心区域被改良为使得其中液体的上升阻力相对于中心区域中的上升阻力减小。
4.如权利要求1-3之一所述的方法，其特征在于，所述气体包括氢、一氧化碳作为该气体的主要成分。
5.如权利要求4所述的方法，其特征在于，所述气体包括甲烷和氮作为该气体的主要成分。
6.如权利要求1-3之一所述的方法，其特征在于，填料在以下条件下操作，即，进气量F介于0.2-2.5(Nm-2)0.5之间，其中F＝(ρvvgas)0.5，并且/或者填料中的以L/dm2/h为单位的液体流率在50L/dm2/h到600L/dm2/h之间的范围变化，其中ρv是以kg/m3为单位的蒸汽的密度。
7.如权利要求1-3之一所述的方法，所述气体包括选自下列组的至少两种成分作为该气体的主要成分：氢，一氧化碳，氮和甲烷，其中，所述区段中的参数S介于50×10-6和7000×10-6之间。
8.如权利要求7所述的方法，其特征在于，所述区段中的参数S介于150×10-6和1500×10-6之间。
9.如前述权利要求1-3之一所述的方法，所述气体包括选自下列组的至少两种成分作为该气体的主要成分：氮、氧、氩，其中，所述区段中的参数S介于500×10-6和70000×10-6之间。
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FR2911391A1 (fr) 2008-07-18
WO2008099105A2 (fr) 2008-08-21
EP2126500B1 (fr) 2018-10-10
US20100107688A1 (en) 2010-05-06
EP2126500A2 (fr) 2009-12-02
CN101636627A (zh) 2010-01-27
WO2008099105A3 (fr) 2009-06-25

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