CN102378808A - 用以再循环尾气的方法和设备 - Google Patents
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- 238000000034 method Methods 0.000 title claims abstract description 50
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 56
- 239000002253 acid Substances 0.000 claims abstract description 28
- 238000002309 gasification Methods 0.000 claims abstract description 25
- 238000004064 recycling Methods 0.000 claims abstract description 17
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 15
- 239000011593 sulfur Substances 0.000 claims abstract description 13
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 59
- 239000005864 Sulphur Substances 0.000 claims description 42
- 238000001816 cooling Methods 0.000 claims description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 15
- 238000004140 cleaning Methods 0.000 claims description 15
- 150000001412 amines Chemical class 0.000 claims description 13
- 235000011089 carbon dioxide Nutrition 0.000 claims description 13
- 238000005984 hydrogenation reaction Methods 0.000 claims description 13
- 238000001035 drying Methods 0.000 claims description 7
- 239000007789 gas Substances 0.000 description 193
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 52
- 230000015572 biosynthetic process Effects 0.000 description 31
- 238000003786 synthesis reaction Methods 0.000 description 30
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 22
- 229910002091 carbon monoxide Inorganic materials 0.000 description 21
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 19
- 239000000463 material Substances 0.000 description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 11
- 239000000446 fuel Substances 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 9
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 8
- 238000011084 recovery Methods 0.000 description 8
- 239000002893 slag Substances 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000003250 coal slurry Substances 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000003245 coal Substances 0.000 description 5
- 239000007859 condensation product Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000007599 discharging Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000000047 product Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000004291 sulphur dioxide Substances 0.000 description 4
- 235000010269 sulphur dioxide Nutrition 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000002378 acidificating effect Effects 0.000 description 3
- 239000000567 combustion gas Substances 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000007800 oxidant agent Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- RBORURQQJIQWBS-QVRNUERCSA-N (4ar,6r,7r,7as)-6-(6-amino-8-bromopurin-9-yl)-2-hydroxy-2-sulfanylidene-4a,6,7,7a-tetrahydro-4h-furo[3,2-d][1,3,2]dioxaphosphinin-7-ol Chemical compound C([C@H]1O2)OP(O)(=S)O[C@H]1[C@@H](O)[C@@H]2N1C(N=CN=C2N)=C2N=C1Br RBORURQQJIQWBS-QVRNUERCSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000002817 coal dust Substances 0.000 description 2
- 238000006477 desulfuration reaction Methods 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000013618 particulate matter Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000003570 air Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- WABPQHHGFIMREM-OIOBTWANSA-N lead-204 Chemical compound [204Pb] WABPQHHGFIMREM-OIOBTWANSA-N 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 238000007634 remodeling Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
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Abstract
一种再循环尾气的方法包括:将存在于酸性气流中的硫转化成元素硫以产生尾气,以及将尾气再循环至气化反应器和气体去除子***中的至少一个。
Description
技术领域
本发明主要涉及气化***,并且更具体地涉及用于再循环尾气以通过去除酸性气体而有助于利用气化***提高合成气体产出的方法和设备。
背景技术
至少一些公知的气化设备包括气化***,该气化***与至少一个产生动力的涡轮***形成一体,从而形成整体气化联合循环(IGCC)动力生成设备。例如,公知的气化***将燃料、空气或氧、蒸汽和/或CO2的混合物转化为合成气体或″合成气″。合成气导送到燃气涡轮发动机的燃烧器中,该燃气涡轮发动机向将电功率供送至电网的发电机供能。来自至少一些公知燃气涡轮发动机的排气供送至产生蒸汽以便驱动蒸汽轮机的热回收蒸汽发生器(HRSG)。由蒸汽轮机所产生的动力也驱动向电网提供电功率的发电机。
与IGCC设备相关联的至少一些公知的气化***最初产生″原料(raw)″合成气燃料,该″原料″合成气燃料包括一氧化碳(CO)、氢(H2)、二氧化碳(CO2)、氧硫化碳(COS)以及硫化氢(H2S)。CO2、COS和H2S通常称为酸性气体。酸性气体通常从原料合成气燃料中除去以产生用于在燃气涡轮发动机内燃烧的″清洁″合成气燃料。
通常,在公知的IGCC设备中,含烃进料与高纯氧(通常为95%的氧纯度)反应以产生温度范围在2200℉至2700℉内的合成气。所产生的合成气然后冷却和洗涤以产生原料合成气,该原料合成气适于引入到酸性气体去除(AGR)子***。酸性气体去除利用酸性气体去除子***来进行,该酸性气体去除子***通常包括至少一个主吸收器用以除去大部分H2S和COS。酸性气体去除子***吸收存在(呈H2S和COS的形式)的大部分硫和存在的一部分CO2。这产生了清洁的合成气流和主要由吸收的H2S、COS和CO2所构成的酸性气流。
酸性气流在降硫子***中处理,以将存在的硫通过克劳斯反应转化成元素硫。该步骤由首先使存在的一部分硫化氢氧化以形成二氧化硫且然后通过以下反应形成元素硫而构成:
2H2S+SO2→3S+2H2O
该反应发生在串接的若干反应器中。在各反应器之后,硫作为液体产物而除去。来自于降硫子***的流出物主要由二氧化碳、氮和水蒸气构成,以及未反应的硫化氢和二氧化硫。这种流出物称为克劳斯尾气。
克劳斯尾气通常需要进一步处理以在释放之前除去硫。该步骤称为尾气处理。最常使用的过程称为SCOT(壳牌克劳斯废气处理)。SCOT过程由首先使克劳斯尾气氢化以将二氧化硫转化成硫化氢而构成。氢化气体然后冷却以能够将水蒸气作为冷凝物而除去。胺溶剂用于俘获硫化氢。最终,该溶剂再生以产生含有硫化氢的流用于再循环至硫回收单元。未吸收的废气传送至热氧化器并排出。
现已发现通过使克劳斯尾气再循环至气化反应器,有可能消除尾气处理单元。这种过程有助于消除处理克劳斯尾气的成本和复杂性。此外,降低成本的克劳斯单元可利用较低回收或例如较少回收级而使用,因为尾气再循环至气化反应器。因此,本发明提供了一种用于处理在诸如IGCC***的气化反应器中产生的气体的方法和设备,包括使经历酸性气体去除和降硫的气体在没有中间氢化的情况下再循环至***的气化单元。
发明内容
一方面,提供了一种再循环尾气的方法。该方法包括将存在于酸性气流中的硫转化成元素硫以产生尾气,以及将尾气再循环到气化反应器和气体去除子***中的至少一个中。
另一方面,一种处理由气化反应器产生的气体的方法包括将由气化反应器产生的原料气体引导至气体去除子***中。从原料气体中除去组分以产生酸性气流和清洁气流。所产生的酸性气流引导至降硫子***中,以将存在于酸性气流中的硫转化成元素硫而产生尾气。尾气再循环至气化反应器和气体去除子***中的至少一个中。
又一方面,提供了一种整体气化联合循环(IGCC)动力生成设备。IGCC动力生成设备包括构造成用以生成包括酸性气体的原料气流的至少一个气化反应器。至少一个气体去除子***与至少一个气化反应器成流动连通地联接。该至少一个气体去除子***构造成用以从原料气流中除去至少一部分酸性气体。至少一个降硫子***与至少一个气体去除子***成流动连通地联接。降硫子***有助于降低气流内的硫浓度而产生尾气以便再循环到气化反应器和气体去除子***中的至少一个中。
附图说明
图1为示例性整体气化联合循环(IGCC)动力生成设备的示意图;
图2为常规气化单元和处理由气化单元所产生的气体的方法的示意图;以及
图3为示例性气化单元和处理由气化单元所产生的气体的方法的示意图。
具体实施方式
图1为示例性整体气化联合循环(IGCC)动力生成设备100的示意图。在示例性实施例中,IGCC动力生成设备100包括燃气涡轮发动机110。燃气涡轮发动机110包括经由第一转子120可旋转地联接到第一发电机118上的涡轮114。涡轮114与至少一个燃料源和至少一个空气源(两者在下文中更为详细描述)成流动连通地联接,且构造成用以分别从燃料源和空气源接收燃料和空气。涡轮114构造成用以混合空气和燃料,产生热燃烧气体(未示出),以及将气体内的热能转化成旋转能。旋转能经由转子120传输至发电机118,其中发电机118构造成有助于将旋转能转化成电能(未示出)以传输至至少一个负载,包括但不限于电力网(未示出)。
IGCC动力生成设备100还包括蒸汽涡轮发动机130。在示例性实施例中,发动机130包括蒸汽涡轮132,该蒸汽涡轮132经由第二转子136联接到第二发电机134上。
IGCC动力生成设备100还包括蒸汽生成***140。在示例性实施例中,***140包括至少一个热回收蒸汽发生器(HRSG)142,其经由至少一个加热锅炉给水导管146而与至少一个热传递设备144成流动连通地联接。HRSG 142从设备144经由导管146接收锅炉给水(未示出),以便将锅炉给水加热成蒸汽。HRSG 142还从涡轮114经由排出气体导管(未示出)接收排出气体(未示出),以便将锅炉给水进一步加热成蒸汽。HRSG 142经由蒸汽导管150而与涡轮132成流动连通地联接。过量的气体和蒸汽从HRSG 142经由烟道气体导管152排至大气。
导管150将蒸汽(未示出)从HRSG 142导送至涡轮132。涡轮132从HRSG 142接收蒸汽且将蒸汽中的热能转化成旋转能。旋转能经由转子136传输至发电机134,其中发电机134将旋转能转化成电能(未示出)以便传输至至少一个负载,包括但不限于电力网。蒸汽冷凝,且经由冷凝物导管(未示出)作为锅炉给水返回。
IGCC动力生成设备100还包括气化***200。在示例性实施例中,***200包括至少一个空气分离单元202,该空气分离单元202经由空气导管204而与空气源成流动连通地联接。这种空气源可包括但不限于专用空气压缩机和压缩空气储存单元(均未示出)。单元202将空气分成氧(O2)、氮(N2)和经由通风口(未示出)释放的其它组分(均未示出)。氮经由N2导管导送至燃气涡轮114以有助于燃烧。
***200包括气化反应器208,该气化反应器208与单元202成流动连通地联接以便接收经由O2导管210从单元202导送来的氧。***200还包括煤粉碎和造浆单元211。单元211分别经由煤供送导管212和水供送导管213而与煤源和水源(均未示出)成流动连通地联接。单元211将煤和水混合以形成煤浆流(未示出),该煤浆流经由煤浆导管214导送至反应器208。
反应器208分别经由导管214和210接收煤浆流和O2流。反应器208产生热的原料合成气体(合成气)流(未示出),该原料合成气体流包括一氧化碳(CO)、氢(H2)、二氧化碳(CO2)、氧硫化碳(COS)以及硫化氢(H2S)。尽管CO2、COS和H2S通常共同称为酸性气体或原料合成气的酸性气体组分,但在这里CO2将与其余的酸性气体组分分开描述。此外,反应器208还产生作为合成气生产的副产物的热渣料流(未示出)。渣料流经由热渣料导管216导送至渣料处理单元215。单元215使渣料骤冷并使渣料破碎成较小的渣料块,在单元215中产生除渣流且将该除渣流导送穿过导管217。
反应器208经由热合成气导管218而与热传递设备144成流动连通地联接。设备144接收热的原料合成气流,且经由导管146将至少一部分热传递至HRSG 142。随后,设备144产生冷却的原料合成气流(未示出),该原料合成气流经由合成气导管219导送至洗涤器和低温气体冷却(LTGC)单元221。单元221除去携带在原料合成气流内的颗粒物质,且将所除去物质经由飞灰(或飞尘)导管222排放。单元221有助于冷却原料合成气流,且将原料合成气流中的至少一部分COS通过水解转化成H2S和CO2。
***200还包括酸性气体去除子***300,其与单元221成流动连通地联接且经由原料合成气导管220接收冷却的原料合成气流。如下文进一步所述,子***300从原料合成气流中除去至少一部分酸性组分(未示出)。这种酸性气体组分可包括但不限于CO2、COS和H2S。子***300还将至少一些酸性气体组分分离成包括但不限于CO2、COS和H2S的组分。此外,子***300经由导管223而与降硫子***400成流动连通地联接。子***400接收至少一些酸性气体组分且将至少一些酸性气体组分分离成包括但不限于CO2、COS和H2S的组分。此外,子***400将最终综合气流(未示出)经由子***300和最终综合气流导管224导送至反应器208。如下文进一步所述,最终综合气流包括由前述的综合气流(未示出)所产生的预定浓度的CO2、COS和H2S。
子***300经由导管224而与反应器208成流动连通地联接,其中,最终综合气流导送至反应器208的预定部分。通过子***300和400分离和除去CO2、COS和H2S有助于产生清洁的合成气流(未示出),该清洁的合成气流经由清洁合成气导管228导送至燃气涡轮114。
在操作中,空气分离单元202经由导管204接收空气。空气分离成O2、N2和其它组分。其它组分经由通风口排出,N2经由导管206导送至涡轮114,以及O2经由导管210导送至气化反应器208。另外,在操作中,煤粉碎和造浆单元211分别经由导管212和213接收煤和水,形成煤浆流,且将煤浆流经由导管214导送至反应器208。
反应器208经由导管210接收O2,经由导管214接收煤,以及经由导管224接收来自于子***300的最终综合气流。反应器208产生热的原料合成气流,其经由导管218导送至设备144。形成在反应器208中的渣料副产物经由渣料处理单元215和导管216和217除去。设备144有助于冷却热的原料合成气流以产生冷却的原料合成气流,该冷却的原料合成气流经由导管219导送至洗涤器和LTGC单元221,其中,颗粒物质经由飞灰导管222从合成气除去,合成气进一步冷却,且至少一部分COS通过水解转化成H2S和CO2。冷却的原料合成气流导送至酸性气体去除子***300,在其中大致除去酸性气体组分,使得形成清洁合成气流且将其经由导管228导送至涡轮114。
此外,在操作期间,从合成气流除去的至少一部分酸性组分经由导管223导送至子***400,在其中除去且分离酸性组分,使得最终综合的气流经由子***300和导管224导送至反应器208。此外,涡轮发动机110分别经由导管206和228接收N2和清洁的合成气。燃气涡轮发动机110燃烧合成气燃料,产生热燃烧气体,且将热燃烧气体向下游导送以引起涡轮114旋转,这随后通过转子120使第一发电机118旋转。
经由热传递设备144从热合成气除去的至少一部分热经由导管146导送至HRSG 142,在其中热用于使水沸腾以形成蒸汽。蒸汽经由导管150导送至蒸汽涡轮132,且引起涡轮132旋转。涡轮132通过第二转子136使第二发电机134旋转。
图2为常规气化反应器和处理由诸如IGCC动力生成设备100(图1中所示)的气化***的气化反应器208所产生的气体的方法的示意图。通常,气化反应器208中所产生的合成气在常规洗涤单元(未示出)中冷却和洗涤以产生原料合成气,该原料合成气供送至酸性气体去除(AGR)子***300。AGR子***300吸收呈硫化氢和COS形式的硫,连同一定量的二氧化碳一起以产生经由导管228的清洁合成气和经由导管223的酸性气流,该酸性气流主要由所吸收的硫化氢、COS和二氧化碳构成。酸性气体导送至降硫子***400以用于将存在的硫通过克劳斯反应转化成元素硫。在克劳斯反应中,初始存在的一些硫化氢经氧化以形成二氧化硫。还形成元素硫,其可以大约95%至99%的收率而予以回收。克劳斯反应存在于串接的若干反应器中,例如三个串接的反应器。在串接的各反应器中,硫作为液体产物而除去。从降硫子***排放的流出物412主要由二氧化碳、氮和水蒸气以及连同未反应的硫化氢和二氧化硫一起构成。称为克劳斯尾气的流出物412通常需要附加处理以除去硫。该过程称为尾气处理,且最常用的方法称为SCOT(壳牌克劳斯废气处理)。在此种过程中,流出物412导送至氢化单元414,在其中克劳斯尾气412氢化以将二氧化硫转化成硫化氢。氢化气体然后在冷却单元416中冷却,以便容许除去作为冷凝物418的水蒸气,且冷却气体导送至胺接触单元420,在其中俘获硫化氢。溶剂再生以产生再循环至降硫子***400的含有硫化氢的流422。任何未吸收的废气都传送至热氧化器424。
图3示出了示例性气化单元205和处理由气化单元205如单元200(图1中所示)所产生的气体的方法。在示例性实施例中,氢化单元414为可选的(如虚线框所示),且除去了胺接触单元420(如图2中所示),且克劳斯尾气412再循环至气化反应器208和酸性气体去除子***300中的至少一个。
此外,在示例性实施例中,在气化反应器208中产生的合成气经冷却和洗涤以产生原料合成气,该原料合成气导送至酸性气体去除子***300。酸性气体去除子***300吸收作为硫化氢和COS的硫,连同一定量的二氧化碳。清洁合成气流经由导管228产生,且酸性气流经由导管223产生。酸性气流主要包括吸收的硫化氢、COS和二氧化碳。如上文更为详细描述的那样,酸性气体经由导管223供送至降硫子***400,该降硫子***400将存在的硫通过克劳斯反应转化成元素硫。例如,一个、两个或三个串接的反应器可用于该反应。在各反应器之后,硫作为液体产物而除去。从降硫子***400排放的流出克劳斯尾气412主要由二氧化碳、氮和水蒸气连同未反应的硫化氢和二氧化硫一起构成。在实施例中,流出尾气412然后直接导送或引导至冷却单元416,而没有中间氢化过程且不与胺接触。在备选实施例中,流出尾气412引导至氢化单元414中,在其中尾气氢化以将二氧化硫转化成硫化氢而不与胺接触,且然后引导至冷却单元416。在冷却单元416内,气体冷却以将作为冷凝物418的水蒸气有效地除去。
冷却的尾气然后供送至气体干燥单元430,例如乙二醇或甲醇接触器,以有助于除去剩余的痕量的水,且因此最大限度地减小尾气的腐蚀效应。在气体干燥单元430中干燥之后,尾气传送至压缩机426,且在再循环到气化反应器208和酸性气体去除子***300中的至少一个中之前经受压缩。
在一个实施例中,所有再循环的气体都引导至气化反应器208。在另一实施例中,所有再循环的气体都引导至酸性气体去除子***300。在又一实施例中,部分的再循环气体引导至气化反应器208,且对应部分的再循环气体引导至酸性气体去除子***300。例如,如果25%的再循环气体引导至气化反应器208,则对应的75%的再循环气体引导至酸性气体去除子***300。
在示例性实施例中,提供了一种用于再循环所产生的尾气的方法。在该过程中,存在于酸性气流中的硫可在没有中间氢化的情况下转化成元素硫以产生尾气,该尾气再循环至气化反应器208和酸性气体子***300中的至少一个中。由气化反应器208产生的原料气体引导至酸性气体去除子***300中且将来自于原料气体的部分组分除去以产生酸性气流和清洁气流。酸性气流传送至降硫子***400,且存在于酸性气流中的硫转化成元素硫以产生尾气。在实施例中,尾气引导至冷却单元416中,以有助于降低尾气的操作温度。在备选实施例中,流出尾气412引导至氢化单元414中,在其中尾气氢化以将二氧化硫转化成硫化氢而不与胺接触,且然后引导至冷却单元416。在冷却单元416内,尾气冷却以有效地除去作为冷凝物418的水蒸气。冷却的尾气从冷却单元416引导至气体干燥单元430中以有助于干燥尾气。
在另一示例性实施例中,该方法包括将来自降硫子***400的尾气引导至压缩机426。压缩机426在气体再循环至气化反应器208和酸性气体去除子***300中的至少一个之前压缩尾气。
在示例性实施例中,来自于酸性气体去除子***300的再循环的二氧化碳428可选为传送至压缩机426,且在这些气体再循环至气化反应器208和酸性气体去除子***300中的至少一个之前与尾气一起压缩。作为备选,尾气在进入气化反应器208和酸性气体去除子***300中的至少一个之前可在不与胺接触的情况下再循环。
在另一示例性实施例中,由于尾气中少量的二氧化硫可能仍未反应或未转化,故可添加COS水解催化剂以确保所有硫都反应或转化以形成硫化氢。
如本文所述,将尾气流再循环至气化反应器208和酸性气体去除子***300中的至少一个中有助于消除如在常规设备中常用的那样在氢化单元和胺接触单元中处理克劳斯尾气的成本和复杂性。此外,降低成本的克劳斯反应可利用较低回收或例如较少回收级来使用,因为尾气再循环至气化反应器208和酸性气体去除子***300中的至少一个中。成本还通过使用完全吹氧克劳斯反应而不是通过使用富集空气来利用最少的级降低,以便例如实现大约90%至95%的硫回收的收率。
与可选的尾气氢化单元和胺接触的消除(如果期望的话)相关联的节省表现为大于执行气体干燥和压缩中增加的成本,以及与将氢化催化剂加至现有COS单元相关联的任何成本。此外,干燥尾气的压缩应当具有高可靠性且使得能够消除热氧化器424及其排放物,以及正常的燃料气体能量消耗。此外,将二氧化碳从酸性气体去除单元加至尾气,以及将高二氧化碳含量的尾气再循环至气化单元和酸性气体去除子***中的至少一个有助于提高碳转化和CO的产出,这导致整体IGCC效率的进一步提高。
如本文所述的用于合成气体或合成气的生产的方法及设备有助于整体气化联合循环(IGCC)动力生成设备的操作,且具体是合成气生产***的操作。具体而言,增加从合成气生产流体流去除的硫化氢(H2S)和氧硫化碳(COS)会提高合成气的生产效率。更具体而言,降低通向气化反应器的二氧化碳(CO2)进料流中的H2S和COS浓度有助于降低导送至燃气涡轮的清洁合成气内的杂质的浓度。此外,如本文所述,构造一体式吸收器以在大致连续的基础上除去H2S和COS有助于最佳地操作合成气生产过程,以有助于改善IGCC设备的生产效率,从而有助于降低操作成本。此外,这种方法有助于避免过度的排放物释放,因为降低H2和COS的浓度有助于将操作裕度增大至这些复合物的环境符合极限。在没有将尾气排放至环境的情况下,大致所有气体都再循环至气化反应器和酸性气体去除子***中的至少一个。另外,如本文所述的用于产生这种合成气的方法和设备有助于降低与制造此种IGCC设备相关联的资金成本。
上文详细描述了与IGCC设备相关的合成气生产的示例性实施例。该方法、设备和***不限于本文所述的特定实施例,或具体示出的IGCC设备。此外,这些方法、设备和***不限于IGCC设备,并且可装入在通常包括但不限于生产氢的费托燃料生产过程以及气化***和气体清洁***的设施内。
尽管已根据各种具体实施例描述了本发明,但本领域的普通技术人员将认识到,本发明可利用在权利要求的精神和范围内的改型而予以实施。
本书面说明使用了包括最佳模式的实例来公开本发明,且还使本领域的普通技术人员能够实施本发明,包括制作和使用任何装置或***以及执行任何所结合的方法。本发明可取得专利的范围由权利要求限定,并且可包括本领域的普通技术人员所构思出的其它实例。如果这些其它实例具有与权利要求的字面语言并无不同的结构元件,或者如果这些其它实例包括与权利要求的字面语言无实质差异的同等结构元件,则认为这些实例处在权利要求的范围之内。
Claims (20)
1.一种再循环尾气的方法,所述方法包括:
将存在于酸性气流中的硫转化成元素硫而产生尾气;以及
将所述尾气再循环至气化反应器和气体去除子***中的至少一个中。
2.根据权利要求1所述的方法,其特征在于,所述方法还包括:
将由所述气化反应器产生的原料气体引导至所述气体去除子***中;以及
除去由所述气化反应器产生的所述原料气体中的组分,以便产生所述酸性气流和清洁气流。
3.根据权利要求1所述的方法,其特征在于,所述方法还包括将所述尾气引导至冷却单元中,以有助于降低所述尾气的操作温度。
4.根据权利要求3所述的方法,其特征在于,所述方法还包括将所述尾气从所述冷却单元引导至干燥单元以有助于干燥所述尾气。
5.根据权利要求1所述的方法,其特征在于,所述方法还包括将所述尾气从气化反应器和所述气体去除子***中的至少一个引导至压缩机。
6.根据权利要求5所述的方法,其特征在于,在再循环所述尾气之前对所述尾气压缩。
7.根据权利要求5所述的方法,其特征在于,在再循环所述尾气之前,对所述尾气与来自于气化反应器和所述气体去除子***中的所述至少一个的二氧化碳一起压缩。
8.根据权利要求1所述的方法,其特征在于,所述尾气在再循环之前不接触胺。
9.根据权利要求1所述的方法,其特征在于,存在于所述酸性气流中的硫在没有中间氢化的情况下转化成元素硫而产生所述尾气。
10.一种再循环由气化反应器产生的尾气的方法,所述方法包括:
将由所述气化反应器产生的原料气体引导至气体去除子***中;
从所述原料气体除去组分以产生酸性气流和清洁气流;
将产生的所述酸性气流引导至降硫子***中,以便将存在于所述酸性气流中的硫转化成元素硫而产生尾气;以及
将所述尾气再循环至所述气化反应器和所述气体去除子***中的至少一个。
11.根据权利要求10所述的方法,其特征在于,所述方法还包括:
将所述尾气引导至冷却单元以有助于降低所述尾气的操作温度。
12.根据权利要求11所述的方法,其特征在于,所述方法还包括:
将来自于所述冷却单元的冷却尾气引导至干燥单元中以有助于干燥所述尾气。
13.根据权利要求10所述的方法,其特征在于,所述尾气在再循环至所述气化反应器和所述气体去除子***中的至少一个之前不接触胺。
14.根据权利要求10所述的方法,其特征在于,在所述尾气再循环至所述气化反应器和所述气体去除子***中的至少一个之前对所述尾气压缩。
15.根据权利要求10所述的方法,其特征在于,所述尾气在没有中间氢化的情况下再循环至所述气化反应器和所述气体去除子***中的至少一个。
16.一种整体气化联合循环(IGCC)动力生成设备,包括:
构造成用以生成包括酸性气体的原料气流的至少一个气化反应器;
与所述至少一个气化反应器成流动连通地联接的至少一个气体去除子***,所述至少一个气体去除子***构造成用以从所述原料气流中除去至少一部分酸性气体;以及
与所述至少一个气体去除子***成流动连通地联接的至少一个降硫子***,所述至少一个降硫子***有助于降低气流内的硫浓度而产生尾气以便再循环至所述至少一个气化反应器和所述至少一个气体去除子***中的至少一个。
17.根据权利要求16所述的IGCC动力生成设备,其特征在于,所述至少一个气体去除子***和所述至少一个降硫子***将所述尾气再循环至所述至少一个气化反应器和所述至少一个气体去除子***中的至少一个而不会将所述尾气引导至氢化单元中。
18.根据权利要求16所述的IGCC动力生成设备,其特征在于,所述至少一个气体去除子***和所述至少一个降硫子***将所述尾气再循环至所述至少一个气化反应器和所述至少一个气体去除子***中的至少一个,且在再循环之前所述尾气不接触胺。
19.根据权利要求16所述的IGCC动力生成设备,其特征在于,所述至少一个气体去除子***和所述至少一个降硫子***再循环所述尾气而不会将所述尾气引导到胺接触单元中。
20.根据权利要求16所述的IGCC动力生成设备,其特征在于,所述IGCC动力生成设备还包括联接到所述酸性气体去除子***上的压缩机。
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