CN203342628U - 集装箱式沼气净化膜法提纯*** - Google Patents
集装箱式沼气净化膜法提纯*** Download PDFInfo
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Abstract
本实用新型公开了一种集装箱式沼气净化膜法提纯***,其包括:设置在可移动集装箱内依次连接的脱硫脱水单元、压缩机、净化单元、热交换器和膜组提纯制气单元,所述脱硫脱水单元连接厌氧发酵罐产生的沼气气源。本实用新型把提纯设备集成在集装箱内,工艺流程短,节约了占地面积,可小型化、移动化;沼气提纯采用高分子膜对二氧化碳和甲烷进行分离,投资少、能耗低;沼气在进入膜提纯之前先进行净化去杂,保证了提纯后气体的品质。
Description
技术领域
本实用新型涉及沼气处理技术,特别是涉及一种集装箱式沼气净化膜法提纯***。
背景技术
沼气是有机物质在厌氧条件下,经过微生物的发酵作用而生成的一种可燃气体。由于这种气体最先是在沼泽中发现的,所以称为沼气。人畜粪便、农作物秸秆、污水等各种有机物在密闭的沼气发酵装置内,在厌氧条件下进行发酵,被种类繁多的沼气发酵微生物分解转化,从而产生沼气。沼气是多种气体的混合物,一般含有甲烷50%-70%,二氧化碳20%-40%,其余为少量的水蒸气、氮气、氢气和硫化氢等。经过净化去除杂质气体,提纯去除二氧化碳气体,得到的产品气可达国家车用天然气标准。
根据国家标准GB18047-2000车用压缩天然气技术指标,车用压缩天然气中二氧化碳含量应≤3.0%。二氧化碳是沼气中的不可燃组分,含量过高会降低天然气的燃烧热值,沼气中的二氧化碳的去除,称为沼气提纯。
目前,实际应用的沼气提纯的方法主要分为以下几种:
物理法:变压吸附法,加压水洗法,高分子膜分离法等;
化学法:本菲尔法,复合催化法,空间位阻按法,BV钾碱液法,氨水法等;
物理化学法:环丁砜—乙醇胺法,MDEA法等。
化学法的工作原理是用化学试剂对沼气中的二氧化碳进行吸收,由于需要化学试剂量较大,成本较高。
物理法中的三种沼气提纯方法在目前沼气提纯领域应用较多:
变压吸附法的工作原理是利用沼气中各组分在吸附剂上吸附特性的差异以及吸附量随压力变化的原理,通过周期性的压力变化实现气体的分离。为了保证对气体的连续处理要求,变压吸附法至少需要两个吸附塔,也可是三塔、四塔或更多。
加压水洗法的工作原理是利用原料沼气中的CO2在加压的条件下用水吸收。根据亨利定律的理论,等温下气体在水中的溶解度与压力成正比。水吸收CO2时采用高压及低温,气体解吸时采用低压或加温。
膜分离法的工作原理是利用沼气中各种气体的分压在高分子膜-聚酰亚胺中空纤维丝管的高压侧(原料侧)与低压侧(渗透侧)所形成的驱动力--分压差作用下,溶解系数和扩散系数大的气体(如CO2、H2S)优先透过管壁,其余气体(CH4)相对受到阻隔,从而达到分离的目的。
变压吸附法和加压水洗法都具有占地面积大、不可移动、工艺复杂的缺点。加压水洗操作费用高、高压、低温、技术难度大,吸收塔易堵塞。
脱硫、除杂、粗脱水后的沼气采用变压吸附法进行提纯,先对沼气进行压缩,然后进入冷干机脱出水分,然后进入由两台吸附塔组成的变压吸附装置,利用两台吸附塔中中装填的专用碳分子筛吸附剂选择性地吸附掉O2、CO2等杂质气体组分,甲烷从塔顶排出。
脱硫、除杂、粗脱水后的沼气采用加压水洗法进行提纯,进入沼气压缩机将气体压缩送入吸收塔下部,与上部喷淋下来的冷却水逆流接触进行热质交换,吸收CO2气体。吸收塔出塔气一部分返回到三级解吸塔;另一部分送入分子筛吸附器,除去气体中残余水分和微量CO2残余,即为合格的产品气。
脱硫、除杂、粗脱水后的沼气采用膜分离法进行提纯,先对沼气进行压缩,压缩后的沼气进入冷干机脱水,经过过滤器精细去除灰尘、油分进行净化,净化后的沼气换热后进入膜组进行提纯。
变压吸附提纯沼气因需要定期更换分子筛及阀门,维修费用高。加压水洗需要大量的循环水对CO2进行吸收,所需控制仪表阀门也需定期更换,维修费用高。变压吸附与加压水洗都需建造庞大的吸附塔(吸收塔),占地面积大,不可移动,工艺复杂。
实用新型内容
(一)要解决的技术问题
本实用新型的目的是提供一种集装箱式沼气净化膜法提纯***,以克服传统的沼气提纯方法变压吸附、加压水洗等占地面积大、投资高、能耗高、运行成本高的缺陷,实现没有污染物、废水等的排放,经济环保,移动性好,灵活性好等优势。
(二)技术方案
为了解决上述技术问题,本实用新型提供一种集装箱式沼气净化膜法提纯***,其包括:设置在可移动集装箱内依次连接的脱硫脱水单元、压缩机、净化单元、热交换器和膜组提纯制气单元,所述脱硫脱水单元连接厌氧发酵罐产生的沼气气源。
其中,所述净化单元包括依次连接的拦截式预过滤器、冷冻干燥机、聚结式过滤器、活性炭罐、初级油水分离过滤器和精密终端过滤器,所述拦截式预过滤器与所述压缩机连接,所述精密终端过滤器与所述热交换器连接。
其中,所述压缩机为无油压缩机。
其中,所述热交换器由不锈钢材料制成,其上设置有自动恒温控制模块,温度控制范围在25-40℃之间。
其中,所述膜组提纯制气单元包括至少两级依次连接的膜组件,每级膜组件并列设置多根。
其中,所述膜组提纯制气单元还包括:
分气管路,两端分别与热交换器和膜组件入口连接,将热交换器排出的气体均匀的分配给每一根膜组件;
集气管路,与膜组件出口连接,将每一根膜组件产出的产品甲烷气进行汇集处理;
排放气管路,与膜组件连接;
渗透气回流管路,其两端分别与膜组件和压缩机连接。
其中,所述分气管路在每个膜组件的入口处均设有独立的不锈钢球阀。
(三)有益效果
上述技术方案所提供的集装箱式沼气净化膜法提纯***,把提纯设备集成在集装箱内,工艺流程短,节约了占地面积,可小型化、移动化;沼气提纯采用高分子膜对二氧化碳和甲烷进行分离,投资少、能耗低;沼气在进入膜提纯之前先进行净化去杂,保证了提纯后气体的品质。
附图说明
图1是本实用新型实施例集装箱式沼气净化膜法提纯***的结构原理图;
图2是本实用新型实施例净化单元的结构原理图。
具体实施方式
下面结合附图和实施例,对本实用新型的具体实施方式作进一步详细描述。以下实施例用于说明本实用新型,但不用来限制本实用新型的范围。
参照图1和图2所示,本实施例集装箱式沼气净化膜法提纯***包括设置在可移动集装箱内依次连接的脱硫脱水单元、压缩机、净化单元、热交换器和膜组提纯制气单元,所述脱硫脱水单元连接厌氧发酵罐产生的沼气气源。
从厌氧发酵罐出来的沼气气源,一般压力在1.6-2.0KPa之间,中温发酵沼气原料气温度为38℃左右,原料气组分为CH4为55%-65%,CO2为35-40%,H2S浓度由于物料不同而不同,从几百ppm至几千ppm不等,O2<0.5%,N2<3%,氨气微量、一氧化碳微量。
膜法提纯后的产品气中CH4>95%,CO2<3%,H2S<10ppm,O2<0.5%。
经过脱硫脱水单元脱硫、脱水的沼气经无油压缩机压缩后,通过过滤器、冷冻式干燥机、活性炭罐除油器等净化单元以去除饱和水蒸汽和灰尘微粒、油分等。
净化单元依次为拦截式预过滤器、冷冻干燥机、聚结式过滤器、活性炭罐、初级油水分离过滤器、精密终端过滤器。
拦截式过滤器,过滤精度为3μm,气源在过滤器流向为由外向内,过滤器耐压34bar。对压缩气体进行初步过滤、拦截掉灰尘颗粒,滤除大量液体,过滤效率大于92%。
冷冻式干燥机是根据空气冷冻析水原理,利用制冷设备使压缩沼气冷却到一定的露点温度,析出相应所含的水分,并通过分离器进行气液分离,再由自动排水阀将水排出,从而达到冷冻除湿的目的。
聚结式过滤对压缩气体进一步过滤,过滤精度0.5μm,过滤器内气源流向为由内向外,除油、除水,过滤效率达99.925%,过滤器耐压34bar。
活性炭罐内装有活性炭颗粒,以深度去除压缩沼气中的异味如氨及油分,设计压力1.6MPa。
初级油水分离过滤器,过滤精度1μm,过滤器内气源流向为由内向外,以去除活性炭吸附后的粉尘颗粒。
精密终端过滤器,过滤精度为0.01μm,过滤器内气源流向为由内向外,对压缩沼气进行更精密一级除尘、除油处理。
在过滤器上均带有压差指示器,可指示更换滤芯的最佳时间,提高过滤器的利用率,减小压降;还带有自动排污装置,可靠地排出积聚的杂物。
净化后沼气进入热交换器进行温度调节,以达到进膜前温度的要求25℃-40℃之间。换热器由316不锈钢材料制成,具有自动恒温控制,温度控制范围:25-40℃(温度控制精度可达±1℃),控制压缩沼气的旁通流量,由PLC通过温度传感器获得气体温度,通过自动或手动控制调节阀开合大小来获得所需的控制换热气体流量来控制加热后的压缩沼气温度。
净化、换热后的沼气进入膜组提纯制气单元进行二氧化碳与甲烷的分离,膜组提纯***采用框架安装结构,连接紧凑,占用空间小。
膜组提纯制气单元分为四种管路,一是分气管路,两端分别与热交换器和膜组件入口连接,将压缩气体均匀的分配给每一根膜组件,使每一根膜组件都在相同的状态下工作,保证膜组件的工作效率,并且分气管路在每个膜组件的入口处均设有独立的不锈钢球阀,当产气量不需要很大时,可以关闭一定数量的球阀,从而关闭相应的膜组件,避免了不必要的浪费,延长了膜组件的使用寿命。二是集气管路,与膜组件出口连接,将每一根膜组件产出的产品甲烷气进行汇集处理,便于产品气的输送。三是排放气管路,与膜组件连接,因排放气管路中的CO2浓度较高,可以集中回收利用或排放。四是渗透气回流管路,其两端分别与膜组件和压缩机连接,渗透气中因含有约49%的CH4,故集中汇集后回流至压缩机再次处理。
通过沼气在线分析仪监测提纯后气体中的CO2含量来控制产品气的输出。在线沼气分析仪可连续检测CH4、CO2、O2等含量,H2S间歇测量。各路气体独立的4-20mA信号输出。
本实施例中还设置有控制单元,控制单元由可编程逻辑控制器、模拟量模块、触摸屏、压力变送器、温度变送器及电动切断阀等组成。采用自动控制方式,控制整套设备的正常运行,实时显示机组运行状态、气体压力、温度、流量、纯度等参数等。同时,可集中设置膜入口温度保护值和二氧化碳纯度保护值、控制冷冻式干燥机的启停、检测冷冻式干燥机的运行和故障信号,预留RS485和RJ45通讯接口,可与远程监控中心组网连接。
冷冻式干燥机选择远程控制时,机组控制单元可完成联锁保护和控制任务,实现启停控制冷冻式干燥机,检测冷冻式干燥机的运行和故障状态。
压缩气体超温保护控制,通过膜入口管路上的温度变送器检测压缩气体温度值,当温度超过设定保护值时,电动三通切断阀停止向膜供气,同时,切换到旁路回流管道,避免膜在高温下老化而失效。
二氧化碳纯度过高保护控制,通过膜组出口管路上的纯度分析仪检测产品气中二氧化碳含量,当二氧化碳纯度大于设定的合格值时,电动比例调节阀开度减少,以增加膜组对二氧化碳的分离,得到合格的产品气;当二氧化碳纯度在设定的范围内时,向后端储罐送气。
触摸屏显示和设定参数功能,集成显示气体温度、压力、纯度、冷干机运行状态,还可在触摸屏上设置膜入口温度保护值和二氧化碳纯度保护值,实现报警信息查询功能等。
通讯功能,CPU224CN控制器本体集成的RS485通讯接口和以太网通讯模块,可分别配置成MODBUS和以太网通讯方式,与集中监控***组网连接,远程可在集中控制单元计算机上对机组控制、参数设置、监视、数据采集记录、报表管理。
通过试验发现,采用膜法对沼气进行提纯,提纯后的气体中甲烷含量在95%以上,二氧化碳小于3%,硫化氢小于10ppm,达到的国家车用天然气的气体要求,没有污染物产生。相比变压吸附和加压水洗,同样13000Nm3/d原始沼气进行提纯的项目,膜法提纯大大节约了占地面积,降低了能耗。整套膜法提纯***里仅有一台去除水分的冷冻干燥机,功率在6kw。而加压水洗就需要工艺水泵、冷水循环泵及循环水泵对循环水进行泵送,功率总和约在63.5kw。
膜法提纯集装箱面积仅约10m2,整个沼气压缩净化膜法提纯工程占地总面积约为500m2,而加压水洗整个工程占地面积约1630m2。
上述技术于2012年12月,在北京市延庆县张山营镇德青源生态园进行实施,采用的沼气膜法提纯工艺,属国内第一套沼气采用膜法提纯制取生物燃气的案例。整套提纯***放置在一个长4米,宽2米,高2米的特制集装箱内。
沼气原料气为13000Nm3/d,沼气在进入压缩提纯***之前先进行脱硫、脱水处理,脱硫后硫化氢含量降至10ppm以下。提纯后的沼气需要进行压缩处理,以达到膜组分离的压缩要求,压力为1.2MPa,压缩后的沼气进入沼气净化提纯集装箱。
沼气进入膜组进行二氧化碳和甲烷的分离之前,先要进行净化以去除油分、水分和灰尘。采用过滤器、冷冻式干燥机和活性炭罐对这些杂质进行去除,净化后油分、灰尘级别达到0.01ppm,没有液态水。净化后的沼气在进入膜组之前换热至25℃-40℃之间,然后进入膜组提纯。提纯后的产品气中甲烷含量大于95%、二氧化碳小于3%、硫化氢小于10ppm,达到了国家车用压缩天然气的气体要求。
由以上实施例可以看出,相比变压吸附和加压水洗技术,膜提纯技术具有明显的优势,由于可以集成在集装箱内,因此设备结构紧凑,比变压吸附和加压水洗占地面积小;因设备的生产、组装都在工厂内完成,现场安装工作量少,只需完成接口管道及外部电气的连接,故安装方便;由于功能组件集成于一个整体底座,可以方便地整体迁移;工艺流程短、设备维护简单;投资、运行成本低。
以上所述仅是本实用新型的优选实施方式,应当指出,对于本技术领域的普通技术人员来说,在不脱离本实用新型技术原理的前提下,还可以做出若干改进和替换,这些改进和替换也应视为本实用新型的保护范围。
Claims (7)
1.一种集装箱式沼气净化膜法提纯***,其特征在于,包括:设置在可移动集装箱内依次连接的脱硫脱水单元、压缩机、净化单元、热交换器和膜组提纯制气单元,所述脱硫脱水单元连接厌氧发酵罐产生的沼气气源。
2.如权利要求1所述的集装箱式沼气净化膜法提纯***,其特征在于,所述净化单元包括依次连接的拦截式预过滤器、冷冻干燥机、聚结式过滤器、活性炭罐、初级油水分离过滤器和精密终端过滤器,所述拦截式预过滤器与所述压缩机连接,所述精密终端过滤器与所述热交换器连接。
3.如权利要求1所述的集装箱式沼气净化膜法提纯***,其特征在于,所述压缩机为无油压缩机。
4.如权利要求1所述的集装箱式沼气净化膜法提纯***,其特征在于,所述热交换器由不锈钢材料制成,其上设置有自动恒温控制模块,温度控制范围在25-40℃之间。
5.如权利要求1所述的集装箱式沼气净化膜法提纯***,其特征在于,所述膜组提纯制气单元包括至少两级依次连接的膜组件,每级膜组件并列设置多根。
6.如权利要求5所述的集装箱式沼气净化膜法提纯***,其特征在于,所述膜组提纯制气单元还包括:
分气管路,两端分别与热交换器和膜组件入口连接,将热交换器排出的气体均匀的分配给每一根膜组件;
集气管路,与膜组件出口连接,将每一根膜组件产出的产品甲烷气进行汇集处理;
排放气管路,与膜组件连接;
渗透气回流管路,其两端分别与膜组件和压缩机连接。
7.如权利要求6所述的集装箱式沼气净化膜法提纯***,其特征在于,所述分气管路在每个膜组件的入口处均设有独立的不锈钢球阀。
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CN101028579A (zh) * | 2006-11-12 | 2007-09-05 | 张晓忠 | 膜分离技术净化沼气的方法 |
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CN202460429U (zh) * | 2011-11-17 | 2012-10-03 | 黑龙江省森林工程与环境研究所 | 一种同步分离纯化沼气中甲烷与二氧化碳的膜装置 |
CN102559316B (zh) * | 2011-12-31 | 2013-11-13 | 浙江工业大学 | 净化沼气的方法及其设备 |
CN102533369B (zh) * | 2012-01-13 | 2013-08-21 | 北京昊海天际科技有限公司 | 一种用于沼气提纯的工艺方法 |
US8999036B2 (en) * | 2012-09-26 | 2015-04-07 | Stearns Conrad Schmidt Consulting Engineers, Inc. | Method for production of a compressed natural gas equivalent from landfill gas and other biogases |
US9133068B2 (en) * | 2012-11-26 | 2015-09-15 | Neo Energy, Llc | System and method for producing fertilizer from organic waste |
CN103232871A (zh) * | 2013-05-08 | 2013-08-07 | 山西汾西机电有限公司 | 一种沼气提纯***及其沼气提纯工艺 |
CN203342628U (zh) * | 2013-06-24 | 2013-12-18 | 北京合力清源科技有限公司 | 集装箱式沼气净化膜法提纯*** |
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- 2014-06-20 US US14/392,164 patent/US9975085B2/en active Active
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CN103881779A (zh) * | 2014-03-24 | 2014-06-25 | 北京三益能源环保发展股份有限公司 | 沼气膜法提纯加热*** |
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CN106669377A (zh) * | 2016-12-28 | 2017-05-17 | 宁波兴光新能源投资有限公司 | 一种填埋气提纯装置 |
CN109593582A (zh) * | 2018-12-03 | 2019-04-09 | 中国船舶重工集团公司第七〇九研究所 | 沼气膜提纯集成装置及其沼气提纯方法 |
CN112295373A (zh) * | 2019-08-02 | 2021-02-02 | 陈刚 | 一种集成化设计的气体分离*** |
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CN113354464A (zh) * | 2021-06-08 | 2021-09-07 | 广州城建职业学院 | 肠道式发酵装置及包含其的有机废物处理设备 |
CN115367867A (zh) * | 2022-07-19 | 2022-11-22 | 武汉天源环保股份有限公司 | 高浓度有机废水资源化处理***及方法 |
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WO2014206248A1 (zh) | 2014-12-31 |
US20160166980A1 (en) | 2016-06-16 |
US9975085B2 (en) | 2018-05-22 |
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