CN111748380A - 一种可再生孤网能源*** - Google Patents
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Abstract
本发明公开了一种可再生孤网能源***,包括生物质气化单元、水电解单元、甲烷化单元、燃气发电机组发电单元和热量利用单元,生物质气化单元将固体生物质在高温下热解气化转化成合成气;水电解单元借助弃风弃水将水电解为高纯氢气和高纯氧气;经过脱硫清洁后的合成气与高纯氢气一同送入甲烷化单元进行甲烷化反应生成合成天然气储存起来,当孤网***其他新能源发电容量不足时,将合成天然气送入燃气发电设备发电,维护能源***的稳定性。本发明实现100%可再生能源,甲烷化反应单元过热蒸汽,实现在孤网能源***中耦合热网,能提高能源转化效率和***灵活性,有效提高整个孤网的供电能力和运行经济性。
Description
技术领域
本发明属于储能技术领域,具体涉及一种基于生物质气化耦合电转气技术的100%可再生能源孤网能源***工艺。
背景技术
在我国距离陆地较远的小型海岛以及偏远山区,如果铺设长距离电缆进行供电非常不经济,因而一般在当地建立孤岛分布式能源网,以解决当地的能源供给问题。在海岛和高原地区,通常拥有非常丰富的光伏、风能、水能、生物质等多种清洁能源,因此可有效利用可再生能源对该地区进行供能。但是由于风、光等资源的波动性与随机性,不能满足全天候需求,一般配备较大容量的燃料发电机组作为整个电网基本的动力来源,以保证供电的稳定性和可靠性。因此,可再生能源在孤岛电网中占比受到限制,造成了可再生能源的大量浪费和对化石燃料的依赖。如果能借助高效的储能手段,将可再生能源灵活储存起来以抑制其波动,不仅能增强电网对清洁能源的接纳能力,还能提高整个孤网的供电能力和运行经济性。
现有技术有将电转气技术与煤制天然气工艺集成(CN104531246A);有将煤制天然气排放的CO2与水电解的氢气发生反应,既避免了CO2的排放,又大幅增加了天然气产量;还有利用生物质能(CN104845691A)热力发电厂烟气中的CO2(CN107141189A,CN110649650A);或从空气中补集(CN107998840A)作为甲烷化碳源。但在偏远的孤岛能源网当中,一般缺乏煤制天然气工厂或者火力发电,从空气中补集二氧化碳能耗又极高,所以充分利用偏远地区丰富的生物质能提供碳源相对经济合理。
针对上述情况,设计一种能高效利用可再生能源的稳定孤网能源***对于电力电网在偏远地区或者孤岛的电力搭建尤为重要。
发明内容
本发明的目的在于克服现有技术对孤网能源***利用效率不高、存在不经济的缺点,提出了一种可再生孤网能源***。
本发明采用如下技术方案:
一种可再生孤网能源***,其关键在于:包括生物质气化单元、甲烷化单元、发电单元和热量利用单元;
所述生物质气化单元用于将固体生物质在高温下热解气化生成合成气;
所述甲烷化单元用于将上述合成气转化生成天然气;
所述发电单元用于利用上述天然气进行发电;
所述热量利用单元用于利用副产高温水蒸气为***供热或供能。
该方案的效果是:生物质气化单元能为甲烷化单元生成天然气提供原料,发电单元利用天然气能进行火力发电,热量利用单元能将***副产的高温水蒸气进行利用,为***供热或者供能;利用生物质能来提高偏远孤网***的稳定性;实现100%可再生能源,避免对化石燃料的依赖度;甲烷化反应单元过热蒸汽,实现在孤网能源***中耦合热网,既提高能源转化效率,又提高了能源***的灵活性。
作为优选方案,上述***还包括水电解单元,所述水电解单元用于将水电解为高纯氢气和高纯氧气,所述高纯氢气用于与所述合成气反应生成所述天然气。该方案的效果是:水电解单元利用孤网***中弃风弃水将水电解为高纯氢气和高纯氧气,合理利用废弃能源,氢气与合成气通过甲烷化反应能形成天然气储存,保证孤网***在能源稳定,高纯度氧气能用于发电单元最大化能量转换。
作为优选方案,所述生物质气化单元包括管道连接的气化炉、飞灰脱除装置、焦油脱除装置、脱硫装置、水汽变换装置、水蒸气冷凝脱除装置;
所述气化炉采用流化床双床气化炉或固定床气化炉;
所述飞灰脱除装置采用高温旋风分离装置,操作温度为600℃,将所述合成气中包含的飞灰脱除;
所述焦油脱除装置采用多级油洗涤塔,操作温度为400℃,将所述合成气中的焦油脱除,防止堵塞后续设备和催化剂失活;
所述脱硫装置采用活性炭脱除方法、溶液吸附法中的任一种;
所述水汽变换装置用于调节气化合成器中的氢碳比;
所述水蒸气冷凝脱除装置将所述合成气中的水蒸气冷凝分离脱除。
该方案的效果是:生物质气化单元通过焦油脱除、脱硫能保证合成天然气的清洁度,同时水汽变换装置和水蒸气冷凝脱除装置能调整合适碳氢比并且脱出合成气中水分,利于储存。
作为优选方案,所述水电解单元包括水电解装置、氢气储罐和氧气储罐,其中水电解装置可采用碱性电解技术、质子交换膜电解技术、固体氧化物电解技术中的任一种。
作为优选方案,所述甲烷化单元包括精脱硫装置、甲烷化反应器、气液分离装置、蒸汽发生设备;
所述精脱硫装置与所述水蒸气冷凝脱除装置出口管道连接;
所述甲烷化反应器为多级串联固定床反应器或者流化床反应器中的一种或组合;
所述甲烷化反应器中装填甲烷化催化剂,优选镍基催化剂;
所述气液分离装置包括气体冷却器和气液分离罐;
所述蒸汽发生设备借助换热设备利用甲烷化反应热量副产过热水蒸气。
作为优选方案,所述发电单元可为内燃机、燃气轮机中的任一种。
作为优选方案,热量利用单元借助换热器将副产水蒸气为当地热用户供热或者作为动力源。
作为优选方案,所述合成气经水汽变换装置调节氢碳比后,可水电解单元直接送入甲烷化单元中产出合成天然气。该方案的效果是:当孤网环境中弃风弃水量较小,而生物质能丰富时,可以不需要利用水电解单元产生氢气,经水汽变换装置调节氢碳比后的所述合成气可以直接送入甲烷化单元中产出合成天然气,增加整个***的稳定性和灵活性。
有益效果:本发明的一种可再生孤网能源***,将弃风弃水、生物质能整合起来提高偏远孤网***的稳定性;实现100%可再生能源,避免对化石燃料的依赖度;甲烷化反应单元过热蒸汽,实现在孤网能源***中耦合热网,既提高能源转化效率,又提高了能源***的灵活性,从而有效提高整个孤网的供电能力和运行经济性。
附图说明
图1为本发明的***模块简示图;
图2为本发明的工艺流程图。
具体实施方式
下面结合实施例和附图对本发明作进一步的详细说明:
如附图1所示,一种可再生孤网能源***,包括生物质气化单元A、水电解单元B、甲烷化单元C、发电单元D和热量利用单元E,生物质气化单元A用于将固体生物质在高温下热解气化生成合成气,水电解单元B用于将水电解为高纯氢气和高纯氧气,甲烷化单元C用于将上述合成气转化生成天然气,发电单元D用于利用上述天然气进行发电,热量利用单元E用于利用副产高温水蒸气为***供热或供能。
在具体实施时,生物质气化单元A包括管道连接的气化炉A1、飞灰脱除装置A2、焦油脱除装置A3、脱硫装置A4、水汽变换装置A5、水蒸气冷凝脱除装置A6;
气化炉A1采用流化床双床气化炉或固定床气化炉;
飞灰脱除装置A2采用高温旋风分离装置,操作温度为600℃,将合成气中包含的飞灰脱除;
焦油脱除装置A3采用多级油洗涤塔,操作温度为400℃,将合成气中的焦油脱除,防止堵塞后续设备和催化剂失活;
脱硫装置A4采用活性炭脱除方法、溶液吸附法中的任一种;
水汽变换装置A5用于调节气化合成器中的氢碳比,合成气经水汽变换装置A5调节氢碳比后,可独立于水电解单元B直接连接到精脱硫装置C1入口处,送入甲烷化单元C中产出合成天然气;
水蒸气冷凝脱除装置A6通过换热器将合成气中的水蒸气冷凝分离脱除。
水电解单元B包括水电解装置B1、氢气储罐B2和氧气储罐B3,其中水电解装置可采用碱性电解技术、质子交换膜电解技术、固体氧化物电解技术中的任一种。
甲烷化单元C包括精脱硫装置C1、甲烷化反应器C2、气液分离装置C3、蒸汽发生设备C4;
精脱硫装置C1与水蒸气冷凝脱除装置A6出口管道连接;
甲烷化反应器C2为多级串联固定床反应器或者流化床反应器中的一种或组合;
甲烷化反应器C2中装填甲烷化催化剂,优选镍基催化剂;
气液分离装置C3包括气体冷却器和气液分离罐;
蒸汽发生设备C4借助换热设备利用甲烷化反应热量副产过热水蒸气。
发电单元D可为内燃机、燃气轮机中的任一种。
热量利用单元E借助换热器将副产水蒸气为当地热用户供热或者作为动力源。
本***的具体工作原理如附图2所示,水电解装置B1出口高纯氧气与副产水蒸气一起送入气化炉A1中发生气化反应,气化炉A1出口高温合成气首先被降温到飞灰分离器A2的工作温度,从飞灰分离器A2出来的合成气继续被冷却到焦油脱除装置A3工作温度,脱除焦油后的合成气送入到脱硫装置A4中脱硫,洁净后的合成气被充分冷凝,分离出水以后与水电解装置B1出口高纯氢气混合,首先混合气经过精脱硫装置C1脱硫,接着依次经过换热器升温后送入甲烷化反应器C2进行甲烷化反应,甲烷化反应器C2出口气体经换热器冷却后,经气液分离装置C3分离出凝结水,分离出的合成天然气被储存,在***电力不足时送入燃气发电机组D发电。
图2中锅炉气泡E将***冷却给水加热成饱和蒸汽整合收集,分离出的饱和蒸汽继续送入气化炉A1前端的过热器中继续吸热生成中、高温高压过热水蒸气,副产水蒸气可用于生物质气化、拖动工艺中涉及的泵和风机、送入热网供给当地热用户。
图2中虚线连接的为水汽变换装置A6,当储备合成天然气和其他能源发电容量皆不足时,保持气化炉A1运行,水电解装置B1关闭,通过水汽变换装置A6调节氢碳比,所需水蒸气由副产蒸汽提供,并将多余二氧化碳脱除后送入甲烷化反应器C2,产出合成天然气送入燃气发电机组D发电。
实施例:
假设气化炉A1操作温度为900℃,气化炉A1出口合成气典型比例H2:CO:CO2:CH4:H2O=25:10:13:7:45,气化炉A1出口产气流量为1000kmol/h,该工艺包括以下步骤:
水电解装置B1需要匹配生成570kmol/h氢气流量,对应生成285kmol/h高纯氧气;
甲烷化反应器C2选定为鼓泡流化床反应器,进口反应器温度设为300℃,反应器内温度为320℃,反应器出口干气组成中CO2+CO体积分数小于百分之二,氢气体积小于10%,符合管道气储存标准;
假定飞灰分离器A2工作温度为615℃,焦油脱除装置A3工作温度为400℃,脱硫装置A4工作温度为230℃,合成气依次经过这些设备需要通过换热器调节温度,选定给水压力为8Mpa,借助换热器,以及甲烷化反应器内置换热盘管实现换热配置优化,可副产21t/h、8Mpa、500℃的中高压高温水蒸气,副产水蒸气可用于生物质气化、拖动工艺中涉及的泵和风机、送入热网供给热用户。
最后需要说明的是,上述描述仅仅为本发明的优选实施例,本领域的普通技术人员在本发明的启示下,在不违背本发明宗旨及权利要求的前提下,可以做出多种类似的表示,这样的变换均落入本发明的保护范围之内。
Claims (8)
1.一种可再生孤网能源***,其特征在于:包括生物质气化单元(A)、甲烷化单元(C)、发电单元(D)和热量利用单元(E);
所述生物质气化单元(A)用于将固体生物质在高温下热解气化生成合成气;
所述甲烷化单元(C)用于将上述合成气转化生成天然气;
所述发电单元(D)用于利用上述天然气进行发电;
所述热量利用单元(E)用于利用副产高温水蒸气为***供热或供能。
2.根据权利要求1所述的一种可再生孤网能源***,其特征在于:还包括水电解单元(B),所述水电解单元(B)用于将水电解为高纯氢气和高纯氧气,所述高纯氢气用于与所述合成气反应生成所述天然气。
3.根据权利要求1或2所述的一种可再生孤网能源***,其特征在于:所述生物质气化单元(A)包括管道连接的气化炉(A1)、飞灰脱除装置(A2)、焦油脱除装置(A3)、脱硫装置(A4)、水汽变换装置(A5)、水蒸气冷凝脱除装置(A6);
所述气化炉(A1)采用流化床双床气化炉或固定床气化炉;
所述飞灰脱除装置(A2)采用高温旋风分离装置,操作温度为600℃,将所述合成气中包含的飞灰脱除;
所述焦油脱除装置(A3)采用多级油洗涤塔,操作温度为400℃,将所述合成气中的焦油脱除,防止堵塞后续设备和催化剂失活;
所述脱硫装置(A4)采用活性炭脱除方法、溶液吸附法中的任一种;
所述水汽变换装置(A5)用于调节气化合成器中的氢碳比;
所述水蒸气冷凝脱除装置(A6)通过换热器将所述合成气中的水蒸气冷凝分离脱除。
4.根据权利要求3所述的一种可再生孤网能源***,其特征在于:所述水电解单元(B)包括水电解装置(B1)、氢气储罐(B2)和氧气储罐(B3),其中水电解装置可采用碱性电解技术、质子交换膜电解技术、固体氧化物电解技术中的任一种。
5.根据权利要求3所述的一种可再生孤网能源***,其特征在于:所述甲烷化单元(C)包括精脱硫装置(C1)、甲烷化反应器(C2)、气液分离装置(C3)、蒸汽发生设备(C4);
所述精脱硫装置(C1)与所述水蒸气冷凝脱除装置(A6)出口管道连接;
所述甲烷化反应器(C2)为多级串联固定床反应器或者流化床反应器中的一种或组合;
所述甲烷化反应器(C2)中装填甲烷化催化剂,优选镍基催化剂;
所述气液分离装置(C3)包括气体冷却器和气液分离罐;
所述蒸汽发生设备(C4)借助换热设备利用甲烷化反应热量副产过热水蒸气。
6.根据权利要求1所述的一种可再生孤网能源***,其特征在于:所述发电单元(D)可为内燃机、燃气轮机中的任一种。
7.根据权利要求1所述的一种可再生孤网能源***,其特征在于:所述热量利用单元(E)借助换热器将副产水蒸气为当地热用户供热或者作为动力源。
8.根据权利要求3所述的一种可再生孤网能源***,其特征在于:所述合成气经水汽变换装置(A5)调节氢碳比后,可独立于水电解单元(B)直接送入甲烷化单元(C)中产出合成天然气。
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