CN114459204A - 煤化工二氧化碳尾气低温捕集提纯液化与分离***及方法 - Google Patents
煤化工二氧化碳尾气低温捕集提纯液化与分离***及方法 Download PDFInfo
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 289
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 145
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 144
- 239000003245 coal Substances 0.000 title claims abstract description 37
- 239000000126 substance Substances 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 23
- 238000000746 purification Methods 0.000 title claims description 13
- 238000000926 separation method Methods 0.000 title claims description 11
- 239000007789 gas Substances 0.000 claims abstract description 269
- 238000001179 sorption measurement Methods 0.000 claims abstract description 106
- 230000008929 regeneration Effects 0.000 claims description 64
- 238000011069 regeneration method Methods 0.000 claims description 64
- 238000010926 purge Methods 0.000 claims description 46
- 239000007788 liquid Substances 0.000 claims description 43
- 238000010438 heat treatment Methods 0.000 claims description 31
- 239000003463 adsorbent Substances 0.000 claims description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 10
- 208000005156 Dehydration Diseases 0.000 claims description 10
- 230000018044 dehydration Effects 0.000 claims description 10
- 238000006297 dehydration reaction Methods 0.000 claims description 10
- 229920006395 saturated elastomer Polymers 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 8
- 230000001172 regenerating effect Effects 0.000 claims description 8
- 238000001035 drying Methods 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 238000010992 reflux Methods 0.000 claims description 4
- 125000004122 cyclic group Chemical group 0.000 claims description 3
- 238000012856 packing Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims 2
- 239000002994 raw material Substances 0.000 claims 1
- 239000005431 greenhouse gas Substances 0.000 abstract description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 3
- 239000001257 hydrogen Substances 0.000 abstract description 3
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 3
- 238000011084 recovery Methods 0.000 abstract description 2
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001882 dioxygen Inorganic materials 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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Abstract
本发明涉及一种煤化工二氧化碳尾气低温捕集提纯液化与分离***及方法,所述***包括原料气压缩机、再沸器、一号吸附塔、二号吸附塔、再生气加热器、换热器、高压分离器、低压分离器、冷凝换热器和二氧化碳精馏塔;本***将煤化工装置产生的低浓度二氧化碳尾气通过低温的方法进行捕集、提纯、液化与分离,生产工业级标准的二氧化碳产品,可以与氢气通过甲烷化装置转化为甲烷,从而实现二氧化碳的回收与综合利用,减少温室气体的,提高二氧化碳资源利用率,具有显著的经济和社会价值。
Description
技术领域
本发明涉及低碳能源环保技术领域,具体地讲,涉及一种煤化工二氧化碳尾气低温捕集提纯液化与分离***及方法。
背景技术
二氧化碳(CO2)作为温室气体,过量的排放已经造成全球环境的不断变暖。燃气发电厂、燃煤发电厂、煤化工装置每年都要排放大量的二氧化碳尾气,其中主要成分为二氧化碳、氮气,还有少量的氧气、一氧化碳和氢气。二氧化碳作为一种重要的化工原料,如果能够将尾气中的二氧化碳进行捕集、回收与利用,不仅能够减少温室气体的排放,而且提高碳资源的循环利用。
针对煤化工装置产生的二氧化碳尾气,其中二氧化碳组分的体积分数为70%~90%、氮气组分的体积分数为10%~30%、CO+H2组分体积分数约为1%,目前还没有针对煤化工装置产生的二氧化碳尾气进行回收处理的装置。
因此有必要开发一种煤化工二氧化碳尾气低温捕集提纯液化与分离***,同时生产工业级液体二氧化碳和气体二氧化碳,CO2纯度达到体积分数为99.5%的工业级标准。
发明内容
本发明的目的在于克服现有技术中存在的上述不足,而提供一种***完善的煤化工二氧化碳尾气低温捕集提纯液化与分离***,并提供其方法。
本发明解决上述问题所采用的技术方案是:一种煤化工二氧化碳尾气低温捕集提纯液化与分离***,其特征在于:包括原料气压缩机、再沸器、一号吸附塔、二号吸附塔、再生气加热器、换热器、高压分离器、低压分离器、冷凝换热器和二氧化碳精馏塔;所述原料气压缩机的进气口连接煤化工二氧化碳尾气输入管路,所述原料气压缩机的出气口与再沸器接通,所述二氧化碳精馏塔安装在再沸器上面,所述冷凝换热器安装在二氧化碳精馏塔上面; 所述换热器具有通道A、通道B、通道C、通道D、通道E和通道F,所述一号吸附塔和二号吸附塔并行设置,所述再沸器的出气口与一号吸附塔和二号吸附塔的底部进气口均接通,所述一号吸附塔和二号吸附塔的顶部出气口均与通道A的进口端接通,通道A的出口端与冷凝换热器的进气口接通,所述冷凝换热器还具有中部出气口和底部出液口,所述冷凝换热器的中部出气口接通至二氧化碳精馏塔的中部,所述冷凝换热器的底部出液口接通至二氧化碳精馏塔的顶部;所述二氧化碳精馏塔的顶部出气口与通道B的进口端接通,通道B的出口端与高压分离器的进口接通,高压分离器的顶部出口与通道C接通,高压分离器的底部出口与低压分离器的进口接通,低压分离器的顶部出口与通道D接通,通道D接通至煤化工二氧化碳尾气输入管路,低压分离器的底部出口与通道E接通,通道E与气体二氧化碳产品输送管路接通;所述二氧化碳精馏塔的底部出液口接通至液体二氧化碳产品输送管路;所述通道C的出口端与一条吸附剂加热再生气体输送管路接通,所述再生气加热器安装在吸附剂加热再生气体输送管路上,所述吸附剂加热再生气体输送管路的输出末端分别连接至一号吸附塔和二号吸附塔的顶部出气口处,一号吸附塔和二号吸附塔的底部进气口处均与驰放气排放管路连接;所述通道F的进口端与二氧化碳精馏塔的底部出液口接通,通道F的出口端与气体二氧化碳产品输送管路接通。
优选的,所述再生气加热器的进气口处设置有一号程控阀,所述一号程控阀安装在吸附剂加热再生气体输送管路上。
优选的,在再生气加热器和一号程控阀的侧旁设置有再生气体输送旁路,所述再生气体输送旁路与吸附剂加热再生气体输送管路的一个接通点位于再生气加热器的出气口处,再生气体输送旁路与吸附剂加热再生气体输送管路的另一个接通点位于一号程控阀的进口处,所述再生气体输送旁路上安装有二号程控阀。
优选的,所述二氧化碳精馏塔采用规则波纹填料。
优选的,所述冷凝换热器为列管换热器,再沸器为U型管换热器。
本发明还提供了一种煤化工二氧化碳尾气低温捕集提纯液化与分离的方法,采用上述***进行实施,其步骤如下:
步骤一:煤化工二氧化碳尾气经过原料气压缩机增压后,进入再沸器,为再沸器提供热源;
步骤二:从再沸器出来的二氧化碳尾气经过一号吸附塔或二号吸附塔深度脱除微量的水,达到干燥、净化指标;
步骤三:干燥后的二氧化碳尾气进入换热器的通道A被降温冷却后,随后经过节流阀降低压力后进入冷凝换热器顶部壳程,为冷凝换热器提供冷源;从冷凝换热器壳程出来的气体从二氧化碳精馏塔中部进入进行精馏分离,从冷凝换热器壳程出来的液体从二氧化碳精馏塔顶部进入作为精馏塔回流液;
步骤四:从二氧化碳精馏塔顶部出来的气体进入换热器的通道B中被降温冷却后进入高压分离器;从高压分离器顶部出来的气体经过节流阀降低压力,降压后的气体进入换热器的通道C进行复温,通道C中的经过复温出来的气体去一号吸附塔或二号吸附塔作为吸附剂加热再生气体;
步骤五:从高压分离器底部出来的液体经过节流阀降低压力后进入低压分离器,从低压分离器顶部出来的气体经过调节阀控制后进入换热器的通道D进行复温,通道D中的经过复温后的气体返回原料气压缩机入口,实现二氧化碳循环压缩低温捕集提纯与分离;
步骤六:从低压分离器底部出来的液体经过节流阀降低压力后进入换热器的通道E进行复温,通道E中的经过复温后的气体作为气体二氧化碳产品去界外;
步骤七:从二氧化碳精馏塔底部出来的一部分液体作为液体二氧化碳产品去界外,另外一部分液体经过调节阀控制压力后进入换热器的通道F中,为换热器提供冷量,通道F中的经过复温后的气体作为气体二氧化碳产品去界外。
优选的,在步骤二中,利用一号吸附塔或二号吸附塔对二氧化碳尾气进行脱水干燥净化是采用二塔切换工艺,具体方法为:
当一号吸附塔吸附水饱和时,此时进行切换,从再沸器出来的二氧化碳尾气仅进入到二号吸附塔中进行脱水处理,而一号吸附塔依次进行加热再生和冷却吹扫,从高压分离器顶部出来的气体作为驰放气经换热器的通道C进行复温后,然后再经过再生气加热器加热,加热后的驰放气进入一号吸附塔进行加热再生,再生后的驰放气去火炬排放,一号吸附塔的吸附剂加热再生完成时,来自换热器的通道C的驰放气通过一号程控阀的控制而不经过再生气加热器,而是直接经过再生气体输送旁路对一号吸附塔进行冷却吹扫,吹扫后的驰放气去火炬排放;
当二号吸附塔吸附水饱和时,此时进行切换,从再沸器出来的二氧化碳尾气仅进入到一号吸附塔中进行脱水处理,而二号吸附塔依次进行加热再生和冷却吹扫,从高压分离器顶部出来的气体作为驰放气经换热器的通道C进行复温后,然后再经过再生气加热器加热,加热后的驰放气进入二号吸附塔进行加热再生,再生后的驰放气去火炬排放,二号吸附塔的吸附剂加热再生完成时,来自换热器的通道C的驰放气通过一号程控阀的控制而不经过再生气加热器,而是直接经过再生气体输送旁路对二号吸附塔进行冷却吹扫,吹扫后的驰放气去火炬排放。
优选的,所述煤化工二氧化碳尾气的组成为二氧化碳组分的体积分数为70%~90%、氮气组分的体积分数为10%~30%、CO+H2组分体积分数约为1%和饱和态水。
本发明与现有技术相比,具有以下优点和效果:将煤化工装置产生的低浓度二氧化碳尾气通过低温的方法进行捕集、提纯、液化与分离,生产工业级标准的二氧化碳产品,可以与氢气通过甲烷化装置转化为甲烷,从而实现二氧化碳的回收与综合利用,减少温室气体的,提高二氧化碳资源利用率,具有显著的经济和社会价值。
附图说明
为了更清楚地说明本发明具体实施方式或现有技术中的方案,下面将对具体实施方式或现有技术描述中所需要使用的附图作简单的介绍,显而易见地,下面描述中的附图是本发明的一些实施方式,对于本领域技术人员来讲,在不付出创造性劳动的前提下,还可以根据这些附图获得其他的附图。
图1是本发明实施例的结构示意图。
附图标记说明:原料气压缩机1;再沸器2;一号吸附塔3;二号吸附塔4;再生气加热器5;换热器6;高压分离器7;低压分离器8;冷凝换热器9;二氧化碳精馏塔10;煤化工二氧化碳尾气输入管路11;气体二氧化碳产品输送管路12;液体二氧化碳产品输送管路13;吸附剂加热再生气体输送管路14;驰放气排放管路15;一号程控阀16;再生气体输送旁路17;二号程控阀18。
具体实施方式
下面结合附图并通过实施例对本发明作进一步的详细说明,以下实施例是对本发明的解释而本发明并不局限于以下实施例。
实施例。
参见图1。
本实施例公开了一种煤化工二氧化碳尾气低温捕集提纯液化与分离***,用于将煤化工装置产生的低浓度二氧化碳尾气通过低温的方法进行捕集、提纯、液化与分离,生产工业级标准的二氧化碳产品,本实施例中的低浓度二氧化碳尾气的具体组成为二氧化碳组分的体积分数为70%~90%、氮气组分的体积分数为10%~30%、CO+H2组分体积分数约为1%和饱和态水。
本实施例中,煤化工二氧化碳尾气低温捕集提纯液化与分离***包括原料气压缩机1、再沸器2、一号吸附塔3、二号吸附塔4、再生气加热器5、换热器6、高压分离器7、低压分离器8、冷凝换热器9、二氧化碳精馏塔10和与之配套的管道、阀门等。原料气压缩机1采用往复压缩机,一号吸附塔3和二号吸附塔4结构相同,内部分层填充脱水专用活性氧化铝、4A分子筛。换热器6采用铝制板翅式换热器,其具有通道A、通道B、通道C、通道D、通道E和通道F。二氧化碳精馏塔10采用规则波纹填料。冷凝换热器9为列管换热器,再沸器2为U型管换热器。
本实施例中,原料气压缩机1的进气口连接煤化工二氧化碳尾气输入管路11,原料气压缩机1的出气口与再沸器2接通,原料气压缩机1用于对二氧化碳尾气进行压缩,压缩后的二氧化碳尾气进入到再沸器2中,为再沸器2提供热源。
本实施例中,二氧化碳精馏塔10安装在再沸器2上面,冷凝换热器9安装在二氧化碳精馏塔10上面。二氧化碳精馏塔10用于对二氧化碳尾气精馏分离,分离出气体和液体。
本实施例中,一号吸附塔3和二号吸附塔4并行设置,用于对二氧化碳尾气深度脱除微量的水等杂质,达到净化指标。再沸器2的出气口与一号吸附塔3和二号吸附塔4的底部进气口均接通,并在接通管道上均设置有相应的阀门,用于控制再沸器2放出的二氧化碳尾气是进入到一号吸附塔3中还是进入到二号吸附塔4中。
本实施例中,一号吸附塔3和二号吸附塔4的顶部出气口均与通道A的进口端接通,并在接通管道上均设置有相应的阀门,用于控制两者与通道A的通断。通道A对干燥后的二氧化碳尾气进行降温,通道A的出口端与冷凝换热器9的进气口接通,降温后的二氧化碳尾气进入到冷凝换热器9,为冷凝换热器9提供冷源。
本实施例中,冷凝换热器9还具有中部出气口和底部出液口,冷凝换热器9的中部出气口接通至二氧化碳精馏塔10的中部,从冷凝换热器9的中部出气口出来的气体进入到二氧化碳精馏塔10的中部进行精馏分离。冷凝换热器9的底部出液口接通至二氧化碳精馏塔10的顶部,从冷凝换热器9的底部出液口出来的液体进入到二氧化碳精馏塔10的顶部,作为精馏塔回流液。
本实施例中,二氧化碳精馏塔10的顶部出气口与通道B的进口端接通,通道B的出口端与高压分离器7的进口接通,通道B也是起到对气体进行降温的作用。高压分离器7的顶部出口与通道C接通,高压分离器7的底部出口与低压分离器8的进口接通,低压分离器8的顶部出口与通道D接通,通道D接通至煤化工二氧化碳尾气输入管路11,低压分离器8的底部出口与通道E接通,通道E与气体二氧化碳产品输送管路12接通。
本实施例中,二氧化碳精馏塔10的底部出液口接通至液体二氧化碳产品输送管路13;通道F的进口端与二氧化碳精馏塔10的底部出液口接通,通道F的出口端与气体二氧化碳产品输送管路12接通。
本实施例中,通道C的出口端与一条吸附剂加热再生气体输送管路14接通,再生气加热器5安装在吸附剂加热再生气体输送管路14上,吸附剂加热再生气体输送管路14的输出末端分别连接至一号吸附塔3和二号吸附塔4的顶部出气口处,一号吸附塔3和二号吸附塔4的底部进气口处均与驰放气排放管路15连接,再生气加热器5的进气口处设置有一号程控阀16,一号程控阀16安装在吸附剂加热再生气体输送管路14上。
本实施例中,在再生气加热器5和一号程控阀16的侧旁设置有再生气体输送旁路17,再生气体输送旁路17与吸附剂加热再生气体输送管路14的一个接通点位于再生气加热器5的出气口处,再生气体输送旁路17与吸附剂加热再生气体输送管路14的另一个接通点位于一号程控阀16的进口处,再生气体输送旁路17上安装有二号程控阀18。
本实施例中,煤化工二氧化碳尾气低温捕集提纯液化与分离的方法为:
步骤一:煤化工二氧化碳尾气经过原料气压缩机1增压后,进入再沸器2,为再沸器2提供热源;
步骤二:从再沸器2出来的二氧化碳尾气经过一号吸附塔3或二号吸附塔4深度脱除微量的水,达到干燥、净化指标;
步骤三:干燥后的二氧化碳尾气进入换热器6的通道A被降温冷却后,随后经过节流阀降低压力后进入冷凝换热器9顶部壳程,为冷凝换热器9提供冷源;从冷凝换热器9壳程出来的气体从二氧化碳精馏塔10中部进入进行精馏分离,从冷凝换热器9壳程出来的液体从二氧化碳精馏塔10顶部进入作为精馏塔回流液;
步骤四:从二氧化碳精馏塔10顶部出来的气体进入换热器6的通道B中被降温冷却后进入高压分离器7;从高压分离器7顶部出来的气体经过节流阀降低压力,降压后的气体进入换热器6的通道C进行复温,通道C中的经过复温出来的气体去一号吸附塔3或二号吸附塔4作为吸附剂加热再生气体;
步骤五:从高压分离器7底部出来的液体经过节流阀降低压力后进入低压分离器8,从低压分离器8顶部出来的气体经过调节阀控制后进入换热器6的通道D进行复温,通道D中的经过复温后的气体返回原料气压缩机1入口,实现二氧化碳循环压缩低温捕集提纯与分离;
步骤六:从低压分离器8底部出来的液体经过节流阀降低压力后进入换热器6的通道E进行复温,通道E中的经过复温后的气体作为气体二氧化碳产品去界外;
步骤七:从二氧化碳精馏塔10底部出来的一部分液体作为液体二氧化碳产品去界外,另外一部分液体经过调节阀控制压力后进入换热器6的通道F中,为换热器6提供冷量,通道F中的经过复温后的气体作为气体二氧化碳产品去界外。
在步骤二中,利用一号吸附塔3或二号吸附塔4对二氧化碳尾气进行脱水干燥净化是采用二塔切换工艺,具体方法为:
当一号吸附塔3吸附水饱和时,此时进行切换,从再沸器2出来的二氧化碳尾气仅进入到二号吸附塔4中进行脱水处理,而一号吸附塔3依次进行加热再生和冷却吹扫,从高压分离器7顶部出来的富含N2、H2、CO等不凝气体的气体作为驰放气经换热器6的通道C进行复温后,然后再经过再生气加热器5加热,加热后的驰放气进入一号吸附塔3进行加热再生,再生后的驰放气去火炬排放,一号吸附塔3的吸附剂加热再生完成时,来自换热器6的通道C的驰放气通过一号程控阀16的控制而不经过再生气加热器5,而是直接经过再生气体输送旁路17对一号吸附塔3进行冷却吹扫,吹扫后的驰放气去火炬排放;
当二号吸附塔4吸附水饱和时,此时进行切换,从再沸器2出来的二氧化碳尾气仅进入到一号吸附塔3中进行脱水处理,而二号吸附塔4依次进行加热再生和冷却吹扫,从高压分离器7顶部出来的气体作为驰放气经换热器6的通道C进行复温后,然后再经过再生气加热器5加热,加热后的驰放气进入二号吸附塔4进行加热再生,再生后的驰放气去火炬排放,二号吸附塔4的吸附剂加热再生完成时,来自换热器6的通道C的驰放气通过一号程控阀16的控制而不经过再生气加热器5,而是直接经过再生气体输送旁路17对二号吸附塔4进行冷却吹扫,吹扫后的驰放气去火炬排放。
此外,需要说明的是,本说明书中所描述的具体实施例,其零、部件的形状、所取名称等可以不同,本说明书中所描述的以上内容仅仅是对本发明结构所作的举例说明。凡依据本发明专利构思的构造、特征及原理所做的等效变化或者简单变化,均包括于本发明专利的保护范围内。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,只要不偏离本发明的结构或者超越本权利要求书所定义的范围,均应属于本发明的保护范围。
Claims (8)
1.一种煤化工二氧化碳尾气低温捕集提纯液化与分离***,其特征在于:包括原料气压缩机(1)、再沸器(2)、一号吸附塔(3)、二号吸附塔(4)、再生气加热器(5)、换热器(6)、高压分离器(7)、低压分离器(8)、冷凝换热器(9)和二氧化碳精馏塔(10);
所述原料气压缩机(1)的进气口连接煤化工二氧化碳尾气输入管路(11),所述原料气压缩机(1)的出气口与再沸器(2)接通,所述二氧化碳精馏塔(10)安装在再沸器(2)上面,所述冷凝换热器(9)安装在二氧化碳精馏塔(10)上面;
所述换热器(6)具有通道A、通道B、通道C、通道D、通道E和通道F,
所述一号吸附塔(3)和二号吸附塔(4)并行设置,
所述再沸器(2)的出气口与一号吸附塔(3)和二号吸附塔(4)的底部进气口均接通,
所述一号吸附塔(3)和二号吸附塔(4)的顶部出气口均与通道A的进口端接通,通道A的出口端与冷凝换热器(9)的进气口接通,所述冷凝换热器(9)还具有中部出气口和底部出液口,所述冷凝换热器(9)的中部出气口接通至二氧化碳精馏塔(10)的中部,所述冷凝换热器(9)的底部出液口接通至二氧化碳精馏塔(10)的顶部;
所述二氧化碳精馏塔(10)的顶部出气口与通道B的进口端接通,通道B的出口端与高压分离器(7)的进口接通,高压分离器(7)的顶部出口与通道C接通,高压分离器(7)的底部出口与低压分离器(8)的进口接通,低压分离器(8)的顶部出口与通道D接通,通道D接通至煤化工二氧化碳尾气输入管路(11),低压分离器(8)的底部出口与通道E接通,通道E与气体二氧化碳产品输送管路(12)接通;
所述二氧化碳精馏塔(10)的底部出液口接通至液体二氧化碳产品输送管路(13);
所述通道C的出口端与一条吸附剂加热再生气体输送管路(14)接通,所述再生气加热器(5)安装在吸附剂加热再生气体输送管路(14)上,所述吸附剂加热再生气体输送管路(14)的输出末端分别连接至一号吸附塔(3)和二号吸附塔(4)的顶部出气口处,一号吸附塔(3)和二号吸附塔(4)的底部进气口处均与驰放气排放管路(15)连接;
所述通道F的进口端与二氧化碳精馏塔(10)的底部出液口接通,通道F的出口端与气体二氧化碳产品输送管路(12)接通。
2.根据权利要求1所述的煤化工二氧化碳尾气低温捕集提纯液化与分离***,其特征在于:所述再生气加热器(5)的进气口处设置有一号程控阀(16),所述一号程控阀(16)安装在吸附剂加热再生气体输送管路(14)上。
3.根据权利要求2所述的煤化工二氧化碳尾气低温捕集提纯液化与分离***,其特征在于:在再生气加热器(5)和一号程控阀(16)的侧旁设置有再生气体输送旁路(17),所述再生气体输送旁路(17)与吸附剂加热再生气体输送管路(14)的一个接通点位于再生气加热器(5)的出气口处,再生气体输送旁路(17)与吸附剂加热再生气体输送管路(14)的另一个接通点位于一号程控阀(16)的进口处,所述再生气体输送旁路(17)上安装有二号程控阀(18)。
4.根据权利要求1所述的煤化工二氧化碳尾气低温捕集提纯液化与分离***,其特征在于:所述二氧化碳精馏塔(10)采用规则波纹填料。
5.根据权利要求1所述的煤化工二氧化碳尾气低温捕集提纯液化与分离***,其特征在于:所述冷凝换热器(9)为列管换热器,再沸器(2)为U型管换热器。
6.一种煤化工二氧化碳尾气低温捕集提纯液化与分离的方法,采用权利要求1-5任一项所述的***进行实施,其特征在于:步骤如下:
步骤一:煤化工二氧化碳尾气经过原料气压缩机(1)增压后,进入再沸器(2),为再沸器(2)提供热源;
步骤二:从再沸器(2)出来的二氧化碳尾气经过一号吸附塔(3)或二号吸附塔(4)深度脱除微量的水,达到干燥、净化指标;
步骤三:干燥后的二氧化碳尾气进入换热器(6)的通道A被降温冷却后,随后经过节流阀降低压力后进入冷凝换热器(9)顶部壳程,为冷凝换热器(9)提供冷源;从冷凝换热器(9)壳程出来的气体从二氧化碳精馏塔(10)中部进入进行精馏分离,从冷凝换热器(9)壳程出来的液体从二氧化碳精馏塔(10)顶部进入作为精馏塔回流液;
步骤四:从二氧化碳精馏塔(10)顶部出来的气体进入换热器(6)的通道B中被降温冷却后进入高压分离器(7);从高压分离器(7)顶部出来的气体经过节流阀降低压力,降压后的气体进入换热器(6)的通道C进行复温,通道C中的经过复温出来的气体去一号吸附塔(3)或二号吸附塔(4)作为吸附剂加热再生气体;
步骤五:从高压分离器(7)底部出来的液体经过节流阀降低压力后进入低压分离器(8),从低压分离器(8)顶部出来的气体经过调节阀控制后进入换热器(6)的通道D进行复温,通道D中的经过复温后的气体返回原料气压缩机(1)入口,实现二氧化碳循环压缩低温捕集提纯与分离;
步骤六:从低压分离器(8)底部出来的液体经过节流阀降低压力后进入换热器(6)的通道E进行复温,通道E中的经过复温后的气体作为气体二氧化碳产品去界外;
步骤七:从二氧化碳精馏塔(10)底部出来的一部分液体作为液体二氧化碳产品去界外,另外一部分液体经过调节阀控制压力后进入换热器(6)的通道F中,为换热器(6)提供冷量,通道F中的经过复温后的气体作为气体二氧化碳产品去界外。
7.根据权利要求6所述的煤化工二氧化碳尾气低温捕集提纯液化与分离的方法,其特征在于:在步骤二中,利用一号吸附塔(3)或二号吸附塔(4)对二氧化碳尾气进行脱水干燥净化是采用二塔切换工艺,具体方法为:
当一号吸附塔(3)吸附水饱和时,此时进行切换,从再沸器(2)出来的二氧化碳尾气仅进入到二号吸附塔(4)中进行脱水处理,而一号吸附塔(3)依次进行加热再生和冷却吹扫,从高压分离器(7)顶部出来的气体作为驰放气经换热器(6)的通道C进行复温后,然后再经过再生气加热器(5)加热,加热后的驰放气进入一号吸附塔(3)进行加热再生,再生后的驰放气去火炬排放,一号吸附塔(3)的吸附剂加热再生完成时,来自换热器(6)的通道C的驰放气通过一号程控阀(16)的控制而不经过再生气加热器(5),而是直接经过再生气体输送旁路(17)对一号吸附塔(3)进行冷却吹扫,吹扫后的驰放气去火炬排放;
当二号吸附塔(4)吸附水饱和时,此时进行切换,从再沸器(2)出来的二氧化碳尾气仅进入到一号吸附塔(3)中进行脱水处理,而二号吸附塔(4)依次进行加热再生和冷却吹扫,从高压分离器(7)顶部出来的气体作为驰放气经换热器(6)的通道C进行复温后,然后再经过再生气加热器(5)加热,加热后的驰放气进入二号吸附塔(4)进行加热再生,再生后的驰放气去火炬排放,二号吸附塔(4)的吸附剂加热再生完成时,来自换热器(6)的通道C的驰放气通过一号程控阀(16)的控制而不经过再生气加热器(5),而是直接经过再生气体输送旁路(17)对二号吸附塔(4)进行冷却吹扫,吹扫后的驰放气去火炬排放。
8.根据权利要求6所述的煤化工二氧化碳尾气低温捕集提纯液化与分离的方法,其特征在于:所述煤化工二氧化碳尾气的组成为二氧化碳组分的体积分数为70%~90%、氮气组分的体积分数为10%~30%、CO+H2组分体积分数约为1%和饱和态水。
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