CN103691302A - 一种干法脱硫装置及脱硫方法 - Google Patents
一种干法脱硫装置及脱硫方法 Download PDFInfo
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- CN103691302A CN103691302A CN201310748325.3A CN201310748325A CN103691302A CN 103691302 A CN103691302 A CN 103691302A CN 201310748325 A CN201310748325 A CN 201310748325A CN 103691302 A CN103691302 A CN 103691302A
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- CN
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- Prior art keywords
- desulfurization
- flue gas
- dry
- multicomponent
- dust
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- 230000003009 desulfurizing Effects 0.000 title claims abstract description 136
- 238000006477 desulfuration reactions Methods 0.000 title claims abstract description 108
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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[O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 83
- 239000003546 flue gases Substances 0.000 claims abstract description 73
- 239000000428 dust Substances 0.000 claims abstract description 36
- 239000007789 gases Substances 0.000 claims abstract description 30
- 239000003513 alkali Substances 0.000 claims abstract description 9
- 238000000889 atomisation Methods 0.000 claims description 24
- 238000000034 methods Methods 0.000 claims description 20
- 239000003795 chemical substances by application Substances 0.000 claims description 18
- 239000007921 sprays Substances 0.000 claims description 11
- 239000008187 granular materials Substances 0.000 claims description 7
- 239000000953 sodium hydroxide Substances 0.000 claims description 7
- 229910001856 sodium hydroxide Inorganic materials 0.000 claims description 7
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 7
- 239000002956 ash Substances 0.000 claims description 5
- 239000011901 water Substances 0.000 claims description 5
- 238000006243 chemical reactions Methods 0.000 claims description 4
- 239000007924 injections Substances 0.000 claims description 4
- 239000002893 slag Substances 0.000 claims description 4
- 238000002347 injection Methods 0.000 claims description 3
- 239000002245 particles Substances 0.000 abstract description 6
- 239000007788 liquids Substances 0.000 abstract description 5
- 238000007599 discharging Methods 0.000 abstract 2
- 239000011593 sulfur Substances 0.000 description 7
- 229910052717 sulfur Inorganic materials 0.000 description 7
- AKEJUJNQAAGONA-UHFFFAOYSA-N Sulfur trioxide Chemical compound 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O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 5
- NINIDFKCEFEMDL-UHFFFAOYSA-N sulfur Chemical compound 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[S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 229910001891 sulfur trioxide Inorganic materials 0.000 description 5
- 230000002745 absorbent Effects 0.000 description 4
- 239000002250 absorbents Substances 0.000 description 4
- 229910001890 sulfur dioxide Inorganic materials 0.000 description 4
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulphur dioxide Chemical compound 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- 238000006386 neutralization reactions Methods 0.000 description 3
- 239000002002 slurries Substances 0.000 description 3
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- 239000003518 caustics Substances 0.000 description 2
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- AXCZMVOFGPJBDE-UHFFFAOYSA-L Calcium hydroxide Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
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Abstract
本发明涉及本发明涉及一种脱硫装置及脱硫方法，包括：将含硫气体切向输入烟气脱硫反应器；将通入烟气脱硫反应器内的含硫气体在烟气脱硫反应器内离心旋转，并对落入到脱硫反应器底部的粉尘颗粒雾化；将从脱硫反应器顶部输出的气体进行除尘后排入大气，同时将收集到的粉尘与碱液均化并加湿；将粉尘与碱液均化加湿后产生的大颗粒粉渣排出，同时将较小颗粒粉尘重新送入到脱硫反应器底部进行雾化，然后重新进行步骤1。因此，本发明具有如下优点：1.脱硫效率高，脱硫率达到85%以上；2.操作简单，易于使用。
Description
一种干法脱硫装置及脱硫方法
技术领域
[0001] 本发明涉及一种脱硫装置及脱硫方法，尤其是涉及一种干法脱硫装置及脱硫方法。
背景技术
[0002] 随着环保法规的日趋严格与环境问题的加剧，为了有效降低烟气中硫化物的排放，遏制酸雨的蔓延，燃煤电厂纷纷采用不同的脱硫脱硝装置与工艺对烟气进行处理以减少对环境的污染。
[0003] 目前烟气脱硫工艺主要有湿法脱硫和干法脱硫两大类。湿法脱硫与干法脱硫工艺的基本原理都是酸碱中和，但是实现过程却有所不同。
[0004] 湿法脱硫工艺是通过洗涤塔中的浆液将烟气中的二氧化硫洗涤到浆液池中，进而在浆液池中与石灰石反应生成稳定的化合物；而干法脱硫工艺一般采用循环流化床工艺，其以氢氧化钙为吸收剂，以文丘里流化床塔作为脱硫反应器。在脱硫塔文丘里上部建立高密度、激烈湍动的颗粒床层，通过注水降温，使烟气温度降低到露点以上15〜20°C，利用烟气与吸收剂颗粒之间产生的相对滑动速度，实现高效脱硫的目的。上述脱硫方法在对烟气中三氧化硫的脱除方面，湿法脱硫效率极低，而干法脱硫则可几乎完全脱除烟气中的三氧化硫。但是烟气中的SOx大部分是以二氧化硫的形式存在，三氧化硫的比例较低，而三氧化硫的酸性较二氧化硫强，在干法烟气脱硫装置中更快更容易与碱性吸收剂接触反应，因此干法脱硫工艺虽然对烟气中的三氧化硫的吸收率较高，但是对烟气中的二氧化硫的吸收脱除效率较低，同时操作也复杂。
发明内容
[0005] 本发明主要是解决现有技术所存在的脱硫效率低、操作复杂等问题，提供了一种易于使用且脱硫效率较高的干法脱硫方法。
[0006] 本发明的上述技术问题主要是通过下述技术方案得以解决的:
一种干法脱硫装置，包括烟气粉尘雾化器、多组分烟气脱硫器、除尘器、雾化与混合增湿器、脱硫剂雾化喷射管、脱硫剂发生器，其中:多组分烟气脱硫器上部为圆柱形，下部为锥形；烟气粉尘雾化器位于多组分烟气脱硫器的锥形底部；多组分烟气脱硫器的底部有一含硫气体入口 ；除尘器上部一端与多组分烟气脱硫器顶部相通，另一端有一大气排气口，雾化与混合增湿器位于除尘器的底部并与多组分烟气脱硫器相通；雾化与混合增湿器底部还有一灰渣出口 ；脱硫剂雾化喷射管位于雾化与混合增湿器的上部并与脱硫剂发生器相通。
[0007] 上述干法脱硫装置中，还包括一与含硫气体入口相通的换热器。
[0008] 上述干法脱硫装置中，所述雾化与混合增湿器包括旋转增湿搅拌机和旋转碱性加湿器，其中旋转增湿搅拌机位于除尘器底部并通过旋转碱性加湿器与多组分烟气脱硫器相通。
[0009] 上述干法脱硫装置中，所述旋转碱性加湿器通向多组分烟气脱硫器的一端还有一位于多组分烟气脱硫器内并且开口向下的环形高压风喷吹系统。
[0010] 上述干法脱硫装置中，雾化与混合增湿器与多组分烟气脱硫器的相通的部位设在多组分烟气脱硫器圆柱形底部。
[0011] 上述干法脱硫装置中，所述多组分烟气脱硫器的锥形底部设有同向旋转变频式挡料圆盘机。
[0012] 上述干法脱硫装置中，所述除尘器为布袋除尘器。
[0013] 上述干法脱硫装置中，在所述多组分烟道多组分烟气脱硫器和换热器的连接处装有温度与压力传感器。
[0014] 上述干法脱硫装置中，在所述多组分烟道多组分烟气脱硫器和除尘器的连接处装有温度与压力传感器。
[0015] 一种干法脱硫方法，包括如下步骤:
步骤1:将含硫气体切向输入烟气脱硫反应器；
步骤2:将步骤I中通入烟气脱硫反应器内的含硫气体在烟气脱硫反应器内离心旋转，并对落入到脱硫反应器底部的粉尘颗粒雾化；
步骤3:对从脱硫反应器顶部输出的气体进行除尘后排入大气，同时将收集到的粉尘与碱液均化并加湿。
[0016] 步骤4:将步骤3中粉尘与碱液均化加湿后产生的大颗粒粉渣排出，同时将较小颗粒粉尘重新送入到脱硫反应器底部进行雾化，然后重新进行步骤I。
[0017] 上述的干法脱硫方法中，所述步骤I中控制切向输入烟气脱硫反应器内的含硫气体温度低于150°C。
[0018] 上述的干法脱硫方法中，所述步骤3中控制从脱硫反应器顶部输出的气体温度低于 120。。。
[0019] 上述的干法脱硫方法中，所述步骤3中控制粉尘与碱液均化并加湿后得到的粉尘的含湿量为3〜7%。
[0020] 因此，本发明具有如下优点:1.脱硫效率高，脱硫率达到85%以上；2.操作简单，易于使用。
附图说明
[0021] 图1为本发明专用脱硫装置的主视图。
[0022] 图2为本发明脱硫装置的多组分烟气脱硫器主视图。
[0023] 图3为本发明脱硫装置的雾化与混合增湿器主视图。
具体实施方式
[0024] 为了进一步理解本发明，下面结合实施例对本发明优选实施方案进行描述，但是应当理解，这些描述只是为进一步说明本发明的特征和优点，而不是对本发明权利要求的限制。
[0025] 如图1所示的一种干法脱硫装置，包括烟气粉尘雾化器4、多组分烟气脱硫器3、除尘器6、雾化与混合增湿器8、脱硫剂雾化喷射管9、脱硫剂发生器10，其中:多组分烟气脱硫器3上部为圆柱形，下部为锥形；烟气粉尘雾化器4位于多组分烟气脱硫器3的锥形底部；多组分烟气脱硫器3的底部有一含硫气体入口 5 ;除尘器6上部一端与多组分烟气脱硫器3顶部相通，另一端有一大气排气口 7，雾化与混合增湿器8位于除尘器6的底部并与多组分烟气脱硫器3相通；雾化与混合增湿器8底部还有一灰渣出口 14 ;脱硫剂雾化喷射管9位于雾化与混合增湿器8的上部并与脱硫剂发生器10相通。
[0026] 在本实施例中，还包括一与含硫气体入口 5相通的换热器2 ;雾化与混合增湿器8优选包括旋转增湿搅拌机11和旋转碱性加湿器12，其中旋转增湿搅拌机11位于除尘器6底部并通过旋转碱性加湿器12与多组分烟气脱硫器3相通。旋转增湿搅拌机11用于将除尘器6收集的粉尘和脱硫剂雾化喷射管9喷射的脱硫剂液体喷雾混合，旋转碱性加湿器12用于控制粉尘含湿量；旋转碱性加湿器12优选通向多组分烟气脱硫器3的一端还有一位于多组分烟气脱硫器3内并且开口向下的环形高压风喷吹系统13 ;雾化与混合增湿器8与多组分烟气脱硫器3的相通的部位优选设在多组分烟气脱硫器3圆柱形底部。
[0027] 工业锅炉I中燃烧后产生的含硫等气体经过换热器2后，气体温度降至150°C以下，将废烟气切向进入具有一定的厚度耐火浇注料涂层的多组分烟气脱硫器3，在一定旋转离心力的作用下，大颗粒的烟气粉尘颗粒落入发生器下部锥斗后被烟气粉尘雾化器4旋转雾化，并形成强烈的旋向气流，进而进入除尘器6。除尘器6收集气体中的粉尘并将处理后的气体从大气排气口 7排出。除尘器6收集下的粉尘落入底部的混合增湿器8并与脱硫剂雾化喷射管9喷射的脱硫剂液体喷雾发生强烈旋转、交合、均化，产生的大颗粒渣由混合增湿器8底部的灰渣出口 14排出，小颗粒含碱粉尘进入多组分烟气脱硫器3内继续与含硫气体中和反应，如此反复循环这一过程。
[0028] 在多组分烟气脱硫器3的锥形底部设有同向旋转变频式挡料圆盘机，以便达到烟气中的硫化物与外来的碱性吸收剂，进一步雾化的目的，这样，两种不同酸碱物料，进一步增加均化接触面积，以达到提高脱硫效率；除尘器6为布袋除尘器；在多组分烟道多组分烟气脱硫器3和换热器2的连接处装有温度与压力传感器。
[0029] 在多组分烟道多组分烟气脱硫器3和除尘器6的连接处装有温度与压力传感器。
[0030] 通过安装温度与压力传感器，随时监测该机的温度与压力，既保证反应器内的负压状态与适当的反应温度，同时控制除尘器6的烟气入口温度在120°C以下，以防止除尘器的布袋被烧坏。
[0031] 工作时，首先将工业锅炉I中燃烧后产生的含硫等气体经过换热器2降温至150°C以下，然后将废烟气切向进入具有一定的厚度耐火浇注料涂层的多组分烟气脱硫器3，在一定旋转离心力的作用下，大颗粒的烟气粉尘颗粒落入发生器下部锥斗后被烟气粉尘雾化器4旋转雾化，并形成强烈的旋向气流，进而进入除尘器6。除尘器6收集气体中的粉尘并将处理后的气体从大气排气口 7排出。除尘器6收集下的粉尘落入底部的混合增湿器8并与脱硫剂雾化喷射管9喷射的脱硫剂液体喷雾发生强烈旋转、交合、均化，产生的大颗粒渣由混合增湿器8底部的灰渣出口 14排出，小颗粒含碱粉尘进入多组分烟气脱硫器3内继续与含硫气体中和反应，如此反复循环这一过程。
[0032] 在本实施例中，控制从脱硫反应器顶部输出的气体温度低于120°C，以防止烧坏除尘器；控制粉尘与碱液均化并加湿后得到的粉尘的含湿量为3〜7%，以达到更好的除硫效
果O
[0033] 本文中所描述的具体实施例仅仅是对本发明精神作举例说明。本发明所属技术领域的技术人员可以对所描述的具体实施例做各种各样的修改或补充或采用类似的方式替代，但并不会偏离本发明的精神或者超越所附权利要求书所定义的范围。
Claims (13)
1.一种干法脱硫装置，其特征在于，包括烟气粉尘雾化器(4)、多组分烟气脱硫器(3)、除尘器(6)、雾化与混合增湿器(8)、脱硫剂雾化喷射管(9)、脱硫剂发生器(10)，其中:多组分烟气脱硫器(3)上部为圆柱形，下部为锥形；烟气粉尘雾化器(4)位于多组分烟气脱硫器(3)的锥形底部；多组分烟气脱硫器(3)的底部有一含硫气体入口(5);所述除尘器(6)上部一端与多组分烟气脱硫器(3)顶部相通，另一端有一大气排气口(7);所述雾化与混合增湿器(8)位于除尘器(6)的底部并与多组分烟气脱硫器(3)相通，雾化与混合增湿器(8)底部还有一灰渣出口(14);所述脱硫剂雾化喷射管(9)位于雾化与混合增湿器(8)的上部并与脱硫剂发生器(10)相通。
2.根据权利要求1所述的一种干法脱硫装置，其特征在于，还包括一与含硫气体入口(5)相通的换热器(2)。
3.根据权利要求1所述的一种干法脱硫装置，其特征在于，所述雾化与混合增湿器(8)包括旋转增湿搅拌机(11)和旋转碱性加湿器(12)，其中旋转增湿搅拌机(11)位于除尘器(6)底部并通过旋转碱性加湿器(12)与多组分烟气脱硫器(3)相通。
4.根据权利要求3所述的一种干法脱硫装置，其特征在于，所述旋转碱性加湿器(12)通向多组分烟气脱硫器(3)的一端还有一位于多组分烟气脱硫器(3)内并且开口向下的环形高压风喷吹系统(13)。
5.根据权利要求3所述一种干法脱硫装置，其特征在于，雾化与混合增湿器(8)与多组分烟气脱硫器(3)的相通的部位设在多组分烟气脱硫器(3)圆柱形底部。
6.根据权利要求1所述的一种干法脱硫装置，其特征在于，所述多组分烟气脱硫器(3)的锥形底部设有同向旋转变频式挡料圆盘机。
7.根据权利要求1所述的一种干法脱硫装置，其特征在于，所述除尘器(6)为布袋除尘器。
8.根据权利要求2所述的一种干法脱硫装置，其特征在于，在所述多组分烟道多组分烟气脱硫器(3)和换热器(2)的连接处装有温度与压力传感器。
9.根据权利要求1所述的一种干法脱硫装置，其特征在于，在所述多组分烟道多组分烟气脱硫器(3 )和除尘器(6 )的连接处装有温度与压力传感器。
10.一种干法脱硫方法，其特征在于，包括如下步骤: 步骤1:将含硫气体切向输入烟气脱硫反应器； 步骤2:将步骤I中通入烟气脱硫反应器内的含硫气体在烟气脱硫反应器内离心旋转，并对落入到脱硫反应器底部的粉尘颗粒雾化； 步骤3:对从脱硫反应器顶部输出的气体进行除尘后排入大气，同时将收集到的粉尘与碱液均化并加湿后； 步骤4:将步骤3中粉尘与碱液均化加湿后产生的大颗粒粉渣排出，同时将较小颗粒粉尘重新送入到脱硫反应器底部进行雾化，然后重新进行步骤I。
11.根据权利要求10所述的一种干法脱硫方法，其特征在于，所述步骤I中控制切向输入烟气脱硫反应器内的含硫气体温度低于150°C。
12.根据权利要求10所述的一种干法脱硫方法，其特征在于，所述步骤3中控制从脱硫反应器顶部输出的气体温度低于120°C。
13.根据权利要求10所述的一种干法脱硫方法，其特征在于，所述步骤3中控制粉尘与碱液均化 并加湿后得到的粉尘的含湿量为3~7%。
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