CN107090321A - 一种生物质沼气提纯工艺 - Google Patents
一种生物质沼气提纯工艺 Download PDFInfo
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Abstract
本发明属于沼气生产技术领域,提供了一种生物质沼气提纯工艺,厌氧罐发酵产生的沼气进入微粒滤过器,将颗粒物和冷凝物去除,得沼气一;沼气经干燥塔干燥,除去水蒸气,得沼气二;沼气二经脱氮塔,除去氮化物,得沼气三;沼气三经脱硫塔,除去硫化物,得沼气四;沼气四进入二氧化碳吸附塔,后过压缩机压缩,经第一回冷器降温,将降温后的沼气通入低温提纯塔,沼气中液化的二氧化碳从低温提纯塔下部析出,纯净的甲烷气体经低温提纯塔上方流入第二回冷器,与第二回冷器热交换后,即得到纯净的甲烷。本发明可以将原料气中的二氧化碳,硫化氢等硫化物,氮气,及少量颗粒物去除掉,提纯效率高。
Description
技术领域
本发明属于沼气生产技术领域,具体地,涉及一种生物质沼气提纯工艺。
背景技术
沼气是由微生物产生的一种可燃性混合气体,其主要成分是甲烷,含量约为50-75%,其次是25-45%的二氧化碳,此外还有其它气体,如硫化氢、一氧化碳、氮气、水蒸气、氧气等。
沼气的净化主要是对沼气中的硫化氢、二氧化碳、二氧化硫、卤化混合气体和硅氧烷的去除,如果沼气燃烧放出二氧化硫,会比硫化氢造成更大的危害,二氧化硫会降低露点,溶于水后生成亚硫酸有腐蚀性;如果导气管中积累了水会溶解硫化氢而腐蚀管道,此外当沼气被加压储存时,为了防止因为凝结水而冻坏储气罐,所以必须对水进行去除;去除二氧化碳是因为二氧化碳降低了沼气的能量密度,如果所用的沼气需要达到天然气标准或者被用作汽车燃料,那么就必须对其中的二氧化碳进行去除。在可再生能源发展受到高度重视的现状下,沼气提纯制取生物天然气,扩大沼气用途尤为重要,特别是沼气内一部分杂质未能彻底去除限制了沼气应用领域;又因成本和环境的原因,导致成本过高,工艺复杂,可循环性差,不能很好的发展沼气应用。
因此,需要提供一种净化效率高,操作简单,成本低廉,适应性好的生物质沼气提纯方法。
发明内容
针对现有技术中的缺陷,本发明的目的是提供一种生物质沼气提纯工艺,可以将原料气中的二氧化碳,硫化氢等硫化物,氮气,及少量颗粒物去除掉,提纯效率高。
根据本发明提供的一种生物质沼气提纯工艺,包括如下步骤:
(1)去除颗粒物:厌氧罐发酵产生的沼气进入微粒滤过器,将颗粒物和冷凝物去除,得沼气一;
(2)去除水蒸气:沼气经干燥塔干燥,除去水蒸气,得沼气二;
(3)去除氮化物:沼气二经脱氮塔,除去氮化物,得沼气三;
(4)去除硫化物:沼气三经脱硫塔,除去硫化物,得沼气四;
(5)去除二氧化碳:沼气四进入二氧化碳吸附塔,后过压缩机压缩,经第一回冷器降温,将降温后的沼气通入低温提纯塔,沼气中液化的二氧化碳从低温提纯塔下部析出,纯净的甲烷气体经低温提纯塔上方流入第二回冷器,与第二回冷器热交换后,即得到纯净的甲烷。
优选地,所述步骤(4)中所述脱硫是指在常温常压下采用烟气循环流化床法去除硫化物。
优选地,所述脱硫剂以干态的消石灰粉作为吸收剂。
优选地,所述步骤(5)压缩是将沼气压缩到20-21MPa。
优选地,所述步骤(5)所述低温提纯塔内温度控制在45-50℃。
优选地,所述步骤(5)经过第二回冷器热交换后的沼气温度为5-10℃。
优选地,所述步骤(5)交替对二氧化碳进行吸附,吸附剂为钙基二氧化碳吸附剂,是以碳酸钠和氯化钙为原料,吐温80及聚乙二醇作为添加剂,共同在水溶液中反应析出,得到吸附剂前驱体,吸附剂前驱体经煅烧,得到钙基二氧化碳吸附剂。
优选地,所述步骤(3)二氧化氮吸附剂包括氧化钙 55-60份、氧化铝 10-30份、氢氧化钠 20-40份。
与现有技术相比,本发明具有如下的有益效果:
(1)本发明可有效去除硫化氢、水蒸气、二氧化碳、二氧化氮等气体,且沼气提纯率高,采用本发明方法提纯后甲烷浓度达到99%以上;
(2)本发明与二氧化碳反应速率快,能在10分钟内达到总转化率的80%,从而大大降低了能耗;
(3)本发明二氧化氮吸附剂以氧化钙、氧化铝和氢氧化钾作为主体材料,对二氧化氮气体具有较好的吸附性能,吸附过程不产生副产物;
(4)本发明脱硫工艺采用烟气循环流化床法方法,操作简单,脱硫效率高;
(5)本发明通过有效的控制压力及温度,分离甲烷与二氧化碳气体,且是在低温提纯塔内来实现,不采用溶剂吸 附等复杂方式,成本低、操作简单。
具体实施方式
下面结合具体实施例,进一步阐述本发明。应理解,这些实施例仅用于说明本发明而不用于限制本发明的范围。
本发明的目的是提供一种生物质沼气提纯工艺,可以将原料气中的二氧化碳,硫化氢等硫化物,氮气,及少量颗粒物去除掉,提纯效率高。
根据本发明提供的一种生物质沼气提纯工艺,包括如下步骤:
(1)去除颗粒物:厌氧罐发酵产生的沼气进入微粒滤过器,将颗粒物和冷凝物去除,得沼气一;
(2)去除水蒸气:沼气经干燥塔干燥,除去水蒸气,得沼气二;
(3)去除氮化物:沼气二经脱氮塔,除去氮化物,得沼气三;
(4)去除硫化物:沼气三经脱硫塔,除去硫化物,得沼气四;
(5)去除二氧化碳:沼气四进入二氧化碳吸附塔,后过压缩机压缩,经第一回冷器降温,将降温后的沼气通入低温提纯塔,沼气中液化的二氧化碳从低温提纯塔下部析出,纯净的甲烷气体经低温提纯塔上方流入第二回冷器,与第二回冷器热交换后,即得到纯净的甲烷。
优选地,所述步骤(4)中所述脱硫是指在常温常压下采用烟气循环流化床法去除硫化物。
优选地,所述脱硫剂以干态的消石灰粉作为吸收剂。
优选地,所述步骤(5)压缩是将沼气压缩到20-21MPa。
优选地,所述步骤(5)所述低温提纯塔内温度控制在45-50℃。
优选地,所述步骤(5)经过第二回冷器热交换后的沼气温度为5-10℃。
优选地,所述步骤(5)交替对二氧化碳进行吸附,吸附剂为钙基二氧化碳吸附剂,是以碳酸钠和氯化钙为原料,吐温80及聚乙二醇作为添加剂,共同在水溶液中反应析出,得到吸附剂前驱体,吸附剂前驱体经煅烧,得到钙基二氧化碳吸附剂。
优选地,所述步骤(3)二氧化氮吸附剂包括氧化钙55-60份、氧化铝10-30份、氢氧化钠20-40份。
与现有技术相比,本发明具有如下的有益效果:
(1)本发明可有效去除硫化氢、水蒸气、二氧化碳、二氧化氮等气体,且沼气提纯率高,采用本发明方法提纯后甲烷浓度达到99%以上;
(2)本发明与二氧化碳反应速率快,能在10分钟内达到总转化率的80%,从而大大降低了能耗;
(3)本发明二氧化氮吸附剂以氧化钙、氧化铝和氢氧化钾作为主体材料,对二氧化氮气体具有较好的吸附性能,吸附过程不产生副产物;
(4)本发明脱硫工艺采用烟气循环流化床法方法,操作简单,脱硫效率高;
(5)本发明通过有效的控制压力及温度,分离甲烷与二氧化碳气体,且是在低温提纯塔内来实现,不采用溶剂吸 附等复杂方式,成本低、操作简单。
实施例1
本实施例提供的一种生物质沼气提纯工艺,包括如下步骤:
(1)去除颗粒物:厌氧罐发酵产生的沼气进入微粒滤过器,将颗粒物和冷凝物去除,得沼气一;
(2)去除水蒸气:沼气经干燥塔干燥,除去水蒸气,得沼气二;
(3)去除氮化物:沼气二经脱氮塔,除去氮化物,得沼气三;
(4)去除硫化物:沼气三经脱硫塔,除去硫化物,得沼气四;
(5)去除二氧化碳:沼气四进入二氧化碳吸附塔,后过压缩机压缩,经第一回冷器降温,将降温后的沼气通入低温提纯塔,沼气中液化的二氧化碳从低温提纯塔下部析出,纯净的甲烷气体经低温提纯塔上方流入第二回冷器,与第二回冷器热交换后,即得到纯净的甲烷。
所述步骤(4)中所述脱硫是指在常温常压下采用烟气循环流化床法去除硫化物。
所述脱硫剂以干态的消石灰粉作为吸收剂。
所述步骤(5)压缩是将沼气压缩到21MPa。
所述步骤(5)所述低温提纯塔内温度控制在45℃。
所述步骤(5)经过第二回冷器热交换后的沼气温度为10℃。
所述步骤(5)交替对二氧化碳进行吸附,吸附剂为钙基二氧化碳吸附剂,是以碳酸钠和氯化钙为原料,吐温80及聚乙二醇作为添加剂,共同在水溶液中反应析出,得到吸附剂前驱体,吸附剂前驱体经煅烧,得到钙基二氧化碳吸附剂。
所述步骤(3)二氧化氮吸附剂包括氧化钙60份、氧化铝10份、氢氧化钠40份。
实施例2
本实施例提供的一种生物质沼气提纯工艺,包括如下步骤:
(1)去除颗粒物:厌氧罐发酵产生的沼气进入微粒滤过器,将颗粒物和冷凝物去除,得沼气一;
(2)去除水蒸气:沼气经干燥塔干燥,除去水蒸气,得沼气二;
(3)去除氮化物:沼气二经脱氮塔,除去氮化物,得沼气三;
(4)去除硫化物:沼气三经脱硫塔,除去硫化物,得沼气四;
(5)去除二氧化碳:沼气四进入二氧化碳吸附塔,后过压缩机压缩,经第一回冷器降温,将降温后的沼气通入低温提纯塔,沼气中液化的二氧化碳从低温提纯塔下部析出,纯净的甲烷气体经低温提纯塔上方流入第二回冷器,与第二回冷器热交换后,即得到纯净的甲烷。
所述步骤(4)中所述脱硫是指在常温常压下采用烟气循环流化床法去除硫化物。
所述脱硫剂以干态的消石灰粉作为吸收剂。
所述步骤(5)压缩是将沼气压缩到20MPa。
所述步骤(5)所述低温提纯塔内温度控制在50℃。
所述步骤(5)经过第二回冷器热交换后的沼气温度为5℃。
所述步骤(5)交替对二氧化碳进行吸附,吸附剂为钙基二氧化碳吸附剂,是以碳酸钠和氯化钙为原料,吐温80及聚乙二醇作为添加剂,共同在水溶液中反应析出,得到吸附剂前驱体,吸附剂前驱体经煅烧,得到钙基二氧化碳吸附剂。
所述步骤(3)二氧化氮吸附剂包括氧化钙55份、氧化铝30份、氢氧化钠20份。
实施例3
本实施例提供的一种生物质沼气提纯工艺,包括如下步骤:
(1)去除颗粒物:厌氧罐发酵产生的沼气进入微粒滤过器,将颗粒物和冷凝物去除,得沼气一;
(2)去除水蒸气:沼气经干燥塔干燥,除去水蒸气,得沼气二;
(3)去除氮化物:沼气二经脱氮塔,除去氮化物,得沼气三;
(4)去除硫化物:沼气三经脱硫塔,除去硫化物,得沼气四;
(5)去除二氧化碳:沼气四进入二氧化碳吸附塔,后过压缩机压缩,经第一回冷器降温,将降温后的沼气通入低温提纯塔,沼气中液化的二氧化碳从低温提纯塔下部析出,纯净的甲烷气体经低温提纯塔上方流入第二回冷器,与第二回冷器热交换后,即得到纯净的甲烷。
所述步骤(4)中所述脱硫是指在常温常压下采用烟气循环流化床法去除硫化物。
所述脱硫剂以干态的消石灰粉作为吸收剂。
所述步骤(5)压缩是将沼气压缩到21MPa。
所述步骤(5)所述低温提纯塔内温度控制在48℃。
所述步骤(5)经过第二回冷器热交换后的沼气温度为8℃。
所述步骤(5)交替对二氧化碳进行吸附,吸附剂为钙基二氧化碳吸附剂,是以碳酸钠和氯化钙为原料,吐温80及聚乙二醇作为添加剂,共同在水溶液中反应析出,得到吸附剂前驱体,吸附剂前驱体经煅烧,得到钙基二氧化碳吸附剂。
所述步骤(3)二氧化氮吸附剂包括氧化钙59份、氧化铝20份、氢氧化钠3份。
以上对本发明的具体实施例进行了描述。需要理解的是,本发明并不局限于上述特定实施方式,本领域技术人员可以在权利要求的范围内做出各种变形或修改,这并不影响本发明的实质内容。
Claims (8)
1.一种生物质沼气提纯工艺,其特征在于,包括如下步骤:
(1)去除颗粒物:厌氧罐发酵产生的沼气进入微粒滤过器,将颗粒物和冷凝物去除,得沼气一;
(2)去除水蒸气:沼气经干燥塔干燥,除去水蒸气,得沼气二;
(3)去除氮化物:沼气二经脱氮塔,除去氮化物,得沼气三;
(4)去除硫化物:沼气三经脱硫塔,除去硫化物,得沼气四;
(5)去除二氧化碳:沼气四进入二氧化碳吸附塔,后过压缩机压缩,经第一回冷器降温,将降温后的沼气通入低温提纯塔,沼气中液化的二氧化碳从低温提纯塔下部析出,纯净的甲烷气体经低温提纯塔上方流入第二回冷器,与第二回冷器热交换后,即得到纯净的甲烷。
2.根据权利要求1所述的生物质沼气提纯工艺,其特征在于:所述步骤(4)中所述脱硫是指在常温常压下采用烟气循环流化床法去除硫化物。
3.根据权利要求2所述的生物质沼气提纯工艺,其特征在于:所述脱硫剂以干态的消石灰粉作为吸收剂。
4.根据权利要求1所述的生物质沼气提纯工艺,其特征在于:所述步骤(5)压缩是将沼气压缩到20-21MPa。
5.根据权利要求1所述的生物质沼气提纯工艺,其特征在于:所述步骤(5)所述低温提纯塔内温度控制在45-50℃。
6.根据权利要求1所述的生物质沼气提纯工艺,其特征在于:所述步骤(5)经过第二回冷器热交换后的沼气温度为5-10℃。
7.根据权利要求1所述的生物质沼气提纯工艺,其特征在于:所述步骤(5)交替对二氧化碳进行吸附,吸附剂为钙基二氧化碳吸附剂,是以碳酸钠和氯化钙为原料,吐温80及聚乙二醇作为添加剂,共同在水溶液中反应析出,得到吸附剂前驱体,吸附剂前驱体经煅烧,得到钙基二氧化碳吸附剂。
8.根据权利要求1所述的生物质沼气提纯工艺,其特征在于:所述步骤(3)二氧化氮吸附剂包括氧化钙55-60份、氧化铝10-30份、氢氧化钠20-40份。
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NL1020664C1 (nl) * | 2002-05-23 | 2003-11-25 | Em Engineering Fts B V | Werkwijze voor het reinigen van gassen. |
CN103623768A (zh) * | 2013-12-09 | 2014-03-12 | 王岩 | 钙基二氧化碳吸附剂及其制备方法 |
CN104087355A (zh) * | 2014-06-17 | 2014-10-08 | 吉林省惠泽燃气有限公司 | 一种生物质沼气提纯方法 |
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CN103623768A (zh) * | 2013-12-09 | 2014-03-12 | 王岩 | 钙基二氧化碳吸附剂及其制备方法 |
CN104087355A (zh) * | 2014-06-17 | 2014-10-08 | 吉林省惠泽燃气有限公司 | 一种生物质沼气提纯方法 |
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