CN1313182C - 对废的苛性碱炼油厂排放物的处理 - Google Patents
对废的苛性碱炼油厂排放物的处理 Download PDFInfo
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Abstract
一种处理苛性碱排放物的方法,废的苛性碱炼油厂排放物从源(14)供给到浸没式燃烧气体蒸发器(10)中,在浸没式燃烧气体蒸发器中,包含二氧化碳的热的燃烧气体被注入到苛性碱液体中,以浓缩该液体并将氢氧化物成分转化为碳酸盐。其中苛性碱排放物来自炼油厂,在浓缩处理之前、过程中或之后,将废液中的油在油分离器(20)中从含水成分中分离出来。
Description
技术领域
本申请要求2002年9月4日提交的美国专利申请10/234,559的优先权,并包含在此作为参考。
本发明涉及一种用于处理废的苛性碱排放物的工艺,例如,处理来自于炼油厂、铝制品制造、食品加工等的排放物。
背景技术
许多工业操作会产生稀的废的苛性碱排放物,比如石油加工处理。从这些炼油厂排放的典型的稀释的苛性碱排放物,可包含大约5%到12%(w/w)的氢氧化钠和成分不定的大量的有机化合物,其中有机化合物包括一定量的硫醇、硫化物油、环烷酸、甲苯基酸及其衍生物。混合物中还包含少量的其它无机和有机化合物。另外,炼油厂排放物中伴随着含水的苛性碱溶液可能包含大约5%到20%体积的油。通常,这种排放物已经被认为是基本上无用的废液,但需要在排放之前进行有效处理,以避免环境污染。
Helleur的专利4,079,585描述了一种从工业和市政废液中去除和回收某种成分的方法和装置,该方法和装置通过废液和由洗涤塔中燃烧产生的热气之间的密切和紊流接触,从而蒸发和浓缩该成分,并陈述了浸没燃烧技术也可以有利地用于本方法。根据该专利,不需进行蒸发,可以去除不需要的挥发性污染物,通过加入诸如石灰或苛性碱等碱性物质使诸如二氧化硫、硫化氢等的酸性挥发性污染物保留在溶液中,从而使这些物质以液体形式排放。Helleur的专利描述了应用于来自诸如石油工业等工业的废料的处理方法,并指明,为了避免所选的可燃的挥发物的蒸发,在与液体接触之前,通过冷却助燃气体使助燃气体的温度保持在挥发物的闪点之下。
Young等人的专利4,016,028公开了一种浸没式燃烧蒸发器,用于浓缩工业废液处理的第一阶段。
Ohkawa等人的专利3,966,594描述了以各种方式对包含水溶性有机物质的废水的处理,并陈述了浸没燃烧方法在工业上对浓缩和燃烧是不足够的。相反,该专利描述了一种废水处理方法,使用一种水不溶性有机溶剂以溶解有机成分。
根据Anderson的专利4,188,291,工业废水可以通过浸没式燃烧蒸发器进行处理,并且供给到废水中的燃烧气体中的二氧化碳被氢氧化钙所消耗,氢氧化钙被加入以产生碳酸钙,然后再将碳酸钙从废水流中分离出来。
DeRoeck等人的专利5,244,576所描述的废碱处理方法,将包含二氧化碳和硫化氢的炼厂气引入到氢氧化钠溶液中,以将二氧化碳转化为碳酸钠。
在Connally的专利3,985,609中,待浓缩的液体中的成分的浓缩处理通过将该液体供给到浸没式燃烧蒸发器中来实现。
Echols的专利5,934,207描述了浸出液的蒸发,通过从燃烧器引出火焰,其中将填埋场气体供给到燃烧器的浸没在容纳浸出液的储罐中的火管加热器中,以在排除填埋场气体的同时加热和蒸发该液体成分。
Duesel的专利5,342,482公开了使用填埋场气体作为燃料源,在浸出液蒸发处理中用于浸没式燃烧气体蒸发器。
发明内容
因此,本发明的一个目的在于提供一种克服现有技术缺点的处理废的苛性碱炼油厂排放物的方法。
本发明的另一目的在于提供一种处理来自炼油厂的苛性碱排放物的方法,以将苛性碱成分转化为有用的商业产品。
本发明进一步的目的在于提供一种处理炼油厂排放物的方法,以产生可再利用的油产品和转化的苛性碱产品。
本发明的又一目的在于提供一种处理苛性碱排放物的方法,该方法利用燃烧气体中的二氧化碳供给到排放物中将苛性碱成分转化为碳酸盐。
本发明的这些和其它目的可以通过将苛性碱排放物供给到浸没式燃烧气体蒸发器来实现,其中,助燃气体以一定的温度和量供给到浸没式燃烧气体蒸发器,所选的温度和量可以去除不需要的蒸气和气体,同时保留排放物中的需要的液体成分,并从排放物保留的成分中分离出所需的成分。在本发明特殊的实施例中,苛性碱排放物是炼油厂排放物,并且,供给到排放物的燃烧气体中的二氧化碳将排放物中的苛性碱成分转化为碳酸盐,比如碳酸钠。另外,在蒸发处理之前、过程中或之后,将油从其它排放物成分中分离出来,用于再利用或进一步精炼。
根据本发明的另一方面,至少部分供给到浸没式燃烧气体蒸发器的用于燃烧气体的燃料是填埋场气体,并且,燃烧气体所含的二氧化碳用于将排放物的苛性碱成分转化为碳酸盐,从而防止二氧化碳散布到大气中。
在本发明的代表性实施例中,供给到浸没式燃烧气体蒸发器中废的排放物含有重量百分比为大约5%到12%的等价的氢氧化钠和体积百分比大约为5%到20%的油,并且,通过蒸发可以减少废的排放物的液体含量,从而产生所需的碳酸盐的浓度。浓缩的液体可以包含大约20%到30%的碳酸钠,并且油成分在浓缩处理之后通过重力沉降分离器分离以再利用。附图说明
结合附图阅读下面的描述,可以更清楚地理解本发明的进一步的目的和优点,其中:
图1是用于实施根据本发明的处理苛性碱排放物的方法的代表性实施例的布置的结构示意图;
图2是用于实施本发明方法的浸没式燃烧气体蒸发器的代表性实施例的截面示意图;
图3是用于实施根据本发明的处理苛性碱排放物的方法的另一代表性实施例的布置的结构示意图。
具体实施方式
在图1所示的实施本发明方法的代表性布置中,在图2中更详细描述的浸没式燃烧气体蒸发器10,接收来自填埋场或其它生物气体源11或者可替代燃料源12或者来自两者的可燃气体,其中可替代燃料源12可提供天然气、丙烷、丁烷等,或者供给诸如废弃石油燃料油等的液态燃料。蒸发器10可以间歇、间歇-连续或连续运行,并且可以根据蒸发器的需要将来自源11和12的可燃气体收集并存储而后使用,或者连续供给。在一个实施例中,该系统设置在紧邻填埋场的地方,从填埋场可以方便地提供填埋场气体,但是,如果需要,可以将处理站设置在邻近于诸如炼油厂或其它制造设备等苛性碱排放物液体源的地方,将填埋场气体从远处的一个或多个填埋场用管子输送或运输到处理站。
图1所示的实施例中,从诸如来自炼油厂、铝制品制造工厂或食品加工设备的废的苛性碱排放物的源14供给的苛性碱液体通过管道15传送到热交换单元16,由热废气进行预热,然后通过管子17输送到浸没式燃烧气体蒸发器10的入口。废的排放物中的苛性碱可以是氢氧化钠或任何其它碱性物质,并且废的排放物可以来自炼油厂、铝制品制造工厂或食品加工设备,或者来自诸如洗涤等各种工业操作。来自源14的废的排放物中的苛性碱物质的氢氧化钠等价物的含量范围优选为大约1%到大约50%,理想地是大约1%到15%,更理想地是大约2%到12%。如果废的排放物来自炼油厂,并包含大量的油,那么废的排放物可以通过预先的油水分离器(未示出),以便在输送到蒸发器10之前,至少去除一部分油。
在蒸发器10中进行废的排放物的可蒸发成分的蒸发之后,浓缩液体通过出口18排除,并通过泵19输送通过油分离器20,以从浓缩液体的水溶液成分中分离油,其中水溶液成分穿过分离器到出口31。如果必要,一些或全部水溶液成分可以通过管道21再循环回到蒸发器10,以便在油分离后进行进一步处理。分离的油从分离器通过管道22排除,然后进行销售、进一步处理或再循环。油分离器20可以是任何通常的不互溶液体分离器,比如重力沉降槽、斜板分离器或离心分离机。
由鼓风机23驱动并通过管道24供给的助燃空气,循环通过热交换单元25进行预热,其中浓缩液体从出口18穿过该热交换单元25,预热的助燃空气通过管道26供给到蒸发器10。在热交换单元25中的热交换可以用于提高燃烧器的效率。如果需要,鼓风机23的助燃空气可以转入到管道17中的在线空气吹提器(未示出)中,以便从被供给到蒸发器的废的排放物中去除挥发性化合物,并将这些挥发性化合物连同助燃空气一起供给到蒸发器10的燃烧器中。废气通过管道27从蒸发器10中抽出,然后穿过去雾器28,以去除夹带的液体成分。通过去雾器28后,该气体穿过废气净化单元29,比如封闭燃烧器(enclosed flare)。在废气净化单元29中,将挥发性有机化合物和其它废气成分进行热氧化,或者在将这些成分通过管道30释放到大气中之前,将这些成分处理成无味无害,其中管道30穿过热交换单元16。
本发明方法中所使用的浸没式燃烧气体蒸发器的优选形式的结构如图2所示。如图所示,蒸发器10具有外壳40,外壳40具有向下收缩的、通向排出阀42的锥形底41,通过排出阀42,浓缩的含水的苛性碱液体和油(如果有的化),进入排出管道18。液体和夹带的固体可以沉淀在外壳40内部,并由锥形外壳部分41导入到排出阀42。在外壳40的顶部,使用密封垫48将盖47与外壳壁间密封,并将燃烧器49安装到盖上。
来自燃烧器49的燃烧气体通过火焰和燃烧气体下导管51向下导入到具有一系列混合喷射管53的分配器52。分配器的喷射管具有喷嘴54,热的燃烧气体通过喷嘴可以注射到外壳内部废的苛性碱排放物池55中,以便通过直接接触热传导来蒸发容纳在蒸发区45中的液体,提供并将二氧化碳分散到废的排放物中以完成碳酸盐的转化,并驱散可汽化的成分。优选地,蒸发器中的操作压力在大约1270mm(50英寸)负水压到2540mm(100英寸)正水压的范围之内。
通过控制从源14由管道17进入到蒸发器中的废的排放物的供给量,将外壳内部的废的苛性碱废液池的上表面56保持在所需的水平面。优选地,上表面56的水平面的范围为在分配器52的水平面之上大约127mm(5英寸)到大约2540mm(100英寸)范围内,并且废的排放物池55的温度在大约37.7℃(100)到大约121.1℃(250)范围内。如果蒸发器连续运行,废的排放物将以适当的速率连续供给到蒸发器中,以使表面56保持在蒸发器内所指定的液面上。
另一方面,如果蒸发器间歇运行,将以适当的速率连续供给要处理的排放物,以便将表面56保持在所指定的水平面上,直到排放物中所需的成分的浓度达到所选定的值。然后中断供给,关闭蒸发器并清空,或者继续运行蒸发器直到蒸发器中的排放物的表面下降到气体分配器52的最上部分之上的较低水平面(未示出),这时,关闭蒸发器并排除浓缩的排放物,然后再次开始运行蒸发器。
在优选实施例中,分配器52中燃烧气体的入口温度的范围为226.2℃(600)到678.6℃(1800),所述温度和量需要足够高以蒸发废的排放物中的水分和挥发性成分,以便以所需速率浓缩所需的成分,比如油和/或转化后的苛性碱。
当以间歇-连续模式操作时,操作过程与连续模式相同,只是浓缩的排放物周期性地从排出阀42排出,而并不降低液体液面或关闭蒸发器。如图1所示,通过管道13将燃料供给到燃烧器49中,通过管道26以足够的压力将助燃空气供给到燃烧器,优选地,压力范围从大约127mm(5英寸)到5080mm(200英寸)的水压,以便提供高效燃烧,并使燃烧气体通过分配器52,且通过排除管道27传送废气。
应该注意的是,除了作用泵,只需要一个的运动构件来实施本方法,以在足够压力下提供燃料供给,即鼓风机23加压供给助燃空气。因此,本发明对废的苛性碱排放物的处理过程,不仅可以从排放物中去除有气味的成分,而且可以生产商业有用的含水浓缩物,并以简单而有效的方式分离有用的油成分,而无需复杂的运动部件,这些复杂的运动部件导致现有技术中废的苛性碱排放物处理系统难以实施。
而且,虽然图1所公开的结构中,废的苛性碱排放物穿过热交换单元16和25,但是并没有在这些单元中遇到现有技术使用热交换蒸发器产生的困难,因为没有在这些单元中进行蒸发,因而避免了在热交换表面发生积垢。根据本发明更简单形式的废的苛性碱排放物处理系统中,可以省略热交换单元16和25,并且,如果排放的废气满足直接排放到大气的环境标准,那么也可以省略废气处理单元28和29。
图3说明了可替换的实施例,该实施例除了与蒸发器隔开的热气源,比如热气发生器13’之外,其他均类似前述的图1所示的实施例。热气发生器13’可以是内燃机,通过管道13将热气供给到改进的浸没式热气蒸发器10’中的热气分配装置52,空气供应管道26被连接到热气发生器13’,而不是蒸发器10’。在这种情况下,来自热气发生器的热气在大约1254mm(60英寸)负水压到大约3048mm(120英寸)的正水压的压力下,供给到蒸发器。在所有其它方面,图3所示的苛性碱液体处理系统与图1所示系统是相同的,并且蒸发器10’与图2所示的蒸发器10相同。
根据本发明,来自从炼油厂等的废的苛性碱排放物,可以被高效和有效地浓缩,而无需使用在常规的废的苛性碱排放物系统中使用的热交换蒸发器,这种热交换蒸发器具有可能被排放物残留物结垢的表面,因而需要周期性清洁或更换。可以用于本发明方法的典型的炼油厂废的苛性碱排放物包括硫化物的、甲苯酚的和环烷的排放物。
如由Merichem化学和精炼服务有限责任公司所著述的、标题为“使用MERICONSM技术的排放物苛性碱处理系统(Effluent Caustic TreatingSystems Using MERICONSM Technologies)”的文章中所述的,硫化物的苛性碱排放物通过可燃气体、液化石油气(LPG)和汽油的处理过程生产。典型的炼油厂硫化物的苛性碱液流具有如下表1所示的组成成分。常见的污染物是硫化钠和硫醇钠。这些化合物在处理过程中要求高的化学和生物氧,并在被中和时会产生气味和危险气体。
表1
游离的NaOH,wt% | 2~10 |
以S计的硫化物和二硫化物,wt% | 0.5~4 |
以S计的硫醇盐,wt% | 0.1~4 |
以CO3计的碳酸盐,wt% | 0~4 |
pH | 13~14 |
氨 | 痕量 |
根据本发明浓缩的硫化物的苛性碱溶液的商业应用是作为纸浆和纸加工中的处理剂和在采矿业中用于对某些金属矿进行提纯。
甲苯酚的苛性碱排放物包含芳香烃酸性油,是通过对裂化的汽油和裂化的馏分进行碱处理而生产的。甲苯酚的苛性碱流包含酚类、甲酚类和其它通常呈现为水溶性甲酚盐的有机酸,其中水溶性甲酚盐在中性pH时可从苛性碱中作为酸性油而分离出来。从处理裂化的汽油生产的甲苯酚的苛性碱溶液通常有如下两个来源:1)使用强碱的硫醇提取系统或氧化系统;和2)使用弱碱的硫醇氧化系统。下面的表2示出了典型甲苯酚的苛性碱排放物的特性。
表2
强碱操作 | 稀碱操作 | |
NaOH,wt% | 10~15 | 1~4 |
以S计的硫化物,wt% | 0~1 | 0~0.2 |
以S计的硫醇盐,wt% | 0~4 | 0~0.5 |
甲苯酚的酸,wt% | 10~25 | 2~5 |
以CO3计的碳酸盐,wt% | 0~0.5 | 0~0.1 |
pH | 12~14 | 12~14 |
浓缩的甲苯酚的苛性碱溶液的商业价值是作为化学中间体。
环烷的苛性碱溶液是用碱处理从环烷基原油板岩切削的煤油和柴油而生成的。下面的表3示出了来源于煤油和柴油原料的环烷的液流的典型特性。
表3
喷气发动机燃料/煤油 | 柴油 | |
NaOH,wt% | 1~4 | 1~4 |
以S-计的硫化物,wt% | 0~0.1 | 痕量 |
以S+计的硫醇盐,wt% | 0~0.5 | 0~0.5 |
环烷酸,wt% | 2~10 | 2~15 |
甲酚,wt% | 1~3 | 0~1 |
pH | 12~14 | 12~14 |
浓缩的环烷基苛性碱溶液对加工者具有潜在的商业价值,加工者可精制浓缩的环烷基苛性碱溶液销售给环烷基金属盐的生产者。
炼油厂通常需要为未加工的、包括废的苛性碱的工业废液的运输、处理和排放支付费用。炼油厂将会发现,如果苛性碱液体和油可以去除臭味,并且氢氧化钠等价物被浓缩到可接受的值,那么在处理中购回苛性碱液体和油以再利用是有益的。根据本发明,可以处理炼油厂废的苛性碱来有效并高效地满足这些要求。
在本发明的小规模试验过程中,与供给原料相比,浓缩液体的气味水平显著减少。浓缩液体是油相和水相的两相混合物,这两相可以容易地通过重力分离比如倾析进行分离。在倾析之后,对水相的分析表明可以实现苛性碱的显著浓缩。该分析也表明,由于如下讨论的燃烧气体中二氧化碳和氢氧化物之间的反应,废的苛性碱排放物中的氢氧化钠几乎100%转化为碳酸钠。在这个试验中,浓缩的水相中碳酸钠的浓度大约为30%(w/w)。在这点上,处理过程中在浸没式燃烧气体蒸发器中发生的直接燃烧气体喷射,引起在处理过程中在蒸发器中的水中形成碳酸,并且碳酸接着与苛性碱成分,氢氧化钠发生反应,从而以下面描述的形式形成碳酸钠。
用于小规模试验的稀的苛性碱供给原料是炼油操作中的两种副产物,即通常所说的“硫化物”和“甲苯酚”的废的苛性碱液流,以大约1∶1的比率混和。用于小规模试验原料的这些液流和物质的分析如表4所示。
表4
供给液流和混合平均的成分的构成 | |||
稀的苛性碱 | 液流1 | 液流2 | 试验单位供给 |
硫化物 | 甲酚盐 | (液流1和液流2的1∶1混合物) | |
试验结果,%1 | |||
氢氧化钠 | 10.82 | 10.04 | 10.43 |
碳酸钠 | 2.65 | 4.14 | 3.40 |
钠 | 7.66 | 7.66 | 7.66 |
CO2 | 1.1 | 1.72 | 1.41 |
无机碳 | 0.29 | 0.47 | 0.38 |
硫化氢 | 0.37 | 0.15 | 0.26 |
以S计的总硫量 | 0.62 | 1.06 | 0.84 |
总碳量 | 0.45 | 7.76 | 4.11 |
水 | 86.87 | 76.12 | 81.50 |
总烃 | 0 | 0 | 0 |
总硫醇 | 0.12 | 0.55 | 0.34 |
甲酚 | 0.04 | 2.82 | 1.43 |
苯酚 | 0.02 | 1.31 | 0.67 |
烷基酚 | 0.03 | 2.74 | 1.39 |
1:所有百分比的总和大于100,这是因为重复计算了各种化合物中的一些元素。
小规模试验的目标是去除臭味并浓缩苛性碱物质中氢氧化钠含量,其中苛性碱物质在炼油操作中作为副产物而产生。因为供给到蒸发器的燃烧气体含有二氧化碳,可以预料,部分氢氧化钠将被转化为碳酸钠。然而,尚不知道苛性碱原料物质中包含的油混合物是如何影响处理或被处理影响的。
小规模试验的结果表明,氢氧化钠几乎全部转化为碳酸钠,并且产生了油相,油相与含水的碳酸钠相是不互溶的。倾析能容易地分离这两个不互溶的相。可以判定,与供给原料相比,试验中产生的每一相的气味已经显著地减少了,从而证明处理过程中去除稀的苛性碱原料的臭味的目的已经实现了。
下面表5示出了用作试验单元的供给原料中与由将这些物质用于合并的去除臭味/蒸发过程产生的水相中选定的成分之间的比较。在试验中,供给原料的体积减少到原始的废的苛性碱排放物液体体积的约三分之一。
表5
供给物质与浓缩物的比较 | |||
第一小规模试验的水相 | 原料 | 最后 | 备注 |
试验结果,%1 | |||
氢氧化钠 | 10.43 | 0.5 | |
碳酸钠 | 3.4 | 29.71 | |
钠 | 7.66 | 未检测 | |
CO2 | 1.41 | 未检测 | |
无机碳 | 0.38 | 未检测 | |
硫化氢 | 0.26 | 未检测 | |
以S计的总硫量 | 0.84 | 0.41 | |
总碳量 | 4.11 | 未检测 | |
水 | 81.5 | 未检测 | |
总烃 | 0 | 未检测 | |
总硫醇 | 0.34 | 未检测 | |
甲酚 | 1.43 | 0.38 | |
苯酚 | 0.67 | 0.44 | |
烷基酚 | 1.39 | 未检测 |
1:所有百分比的总和大于100,这是因为重复计算了各种化合物中的一些元素。
随后的两个小规模试验的结果是类似的。在每次试验中,在合并的去除臭味/蒸发过程浓缩供给原料的总体积之后,所回收的油占所处理的供给原料总体积的10%和15%之间。
在蒸发过程中,包含在被注入到含水的废的苛性碱液体中的燃烧气体中的二氧化碳,根据如下方程式与水发生反应产生碳酸:
并且,碳酸根据如下方程式与氢氧化钠发生反应产生碳酸钠和水:
从上面可以看出,注入到苛性碱液体中的燃烧气体中的每摩尔二氧化碳,将2摩尔氢氧化钠转化为1摩尔碳酸钠和2摩尔水。二氧化碳的分子量为44,氢氧化钠的分子量为80,而碳酸的分子量为62,碳酸钠的分子量为106和水的分子量为18。因此,10,000磅的10%氢氧化钠溶液生产1,325磅碳酸钠和450磅水,并消耗550磅或者4,488标准立方英尺的二氧化碳。结果,如果使用每加仑重量为9.237磅、且包含10%氢氧化钠(w/w)的废的苛性碱原料,那么每10,000加仑待处理的原料可以消耗1,451立方英尺的二氧化碳;或者对于每天平均30,000加仑待处理的废的苛性碱原料,每年可以消耗2,781吨的二氧化碳,从而可以防止二氧化碳释放到大气中。因此,该过程的商业价值包括直接的环境和经济效应,即用于管理废的苛性碱排放物的潜在收入,回收的一种或多种产品的潜在销售,导致温室效应的气体排放的缓解,和正比于所消耗的导致温室效应的气体量而产生商业上有价值的“碳信用(carbon credits)”的潜力。
本发明方法可以用于处理苛性碱排放物,可产生或不产生回收产品,或者仅用于消耗包含在供给到蒸发器的燃烧气体中二氧化碳的目的。
虽然这里参考具体实施例描述了本发明,但是本领域技术人员容易对其进行许多修改或改变。因此,所有这样的改变和修改均包括在本发明意欲保护的范围之内。
Claims (19)
1、一种处理废的苛性碱排放物的方法,包括
将废的苛性碱排放物供给到浸没式燃烧气体蒸发器中;和
将燃烧气体供给到所述浸没式燃烧气体蒸发器,所述燃烧气体的温度和量足够高以蒸发废的苛性碱排放物中的水和挥发性成分,并浓缩废的苛性碱排放物的成分。
2、根据权利要求1所述的方法,进一步包括热氧化从废的苛性碱排放物中除去的蒸发的成分,以从释放到大气的气体成分中消除有气味的和其它挥发性物质。
3、根据权利要求1所述的方法,其中废的苛性碱排放物包括含水的苛性碱液体和油,该方法进一步包括在不互溶液体分离器中从含水成分中分离至少一部分油的步骤。
4、根据权利要求3所述的方法,其中所述不互溶液体分离器至少包括重力沉降槽、斜板分离器和离心分离机中的一个。
5、根据权利要求1所述的方法,其中所述供给到浸没式燃烧气体蒸发器的燃烧气体中包含二氧化碳,该方法进一步包括以下步骤:所述二氧化碳与废的苛性碱排放物中的苛性碱成分发生反应,将苛性碱成分转化为碳酸盐,从而从燃烧气体中消耗二氧化碳。
6、根据权利要求1所述的方法,其中所述供给到浸没式燃烧气体蒸发器中的苛性碱废液中的苛性碱物质含量为1wt%到50wt%的氢氧化钠等价物。
7、根据权利要求1所述的方法,进一步包括将浸没式燃烧气体蒸发器中废的苛性碱排放物的液面保持在燃烧气体注入到蒸发器中的水平面之上127mm到2540mm之间。
8、根据权利要求1所述的方法,进一步包括将浸没式燃烧气体蒸发器内的操作压力保持在从1270mm负水压到2540mm正水压的范围内。
9、根据权利要求1所述的方法,进一步包括以127mm到5080mm水压的压力,将燃料和空气的混合物供给到燃烧器以产生所述的燃烧气体。
10、根据权利要求1所述的方法,进一步包括以1524mm负水压到2540mm正水压的压力,将炉外燃烧过程的烟道气供给到所述浸没式燃烧气体蒸发器。
11、根据权利要求1所述的方法,进一步包括将所述浸没式燃烧气体蒸发器内的操作温度保持在从37.7℃到121.1℃的范围内。
12、根据权利要求1所述的方法,其中所述的废的苛性碱排放物包含油,该方法进一步包括以下步骤:在将苛性碱废液供给到所述浸没式燃烧气体蒸发器之前,从所述苛性碱废液中去除至少部分油。
13、根据权利要求1所述的方法,进一步包括将硫化物的废的苛性碱排放物供给到所述浸没式燃烧气体蒸发器中。
14、根据权利要求1所述的方法,进一步包括将甲苯酚的废的苛性碱排放物供给到所述浸没式燃烧气体蒸发器中。
15、根据权利要求1所述的方法,进一步包括将环烷基的废的苛性碱排放物供给到所述浸没式燃烧气体蒸发器中。
16、根据权利要求1所述的方法,进一步包括将硫化物、甲苯酚和环烷基的废的苛性碱排放物的任意混合物供给到所述浸没式燃烧气体蒸发器中。
17、根据权利要求1所述的方法,进一步包括通过将苛性碱排放物成分从氢氧化物转化为碳酸盐,从燃烧气体中至少消耗部分二氧化碳。
18、根据权利要求1所述的方法,进一步包括在将废的苛性碱排放物供给到所述蒸发器之前,至少汽提部分挥发性成分,并将来自空气吹提器的包含挥发性成分的空气供给到用于产生燃烧气体的燃烧器中。
19、一种用于处理苛性碱物质的方法,包括将具有1%到50%的氢氧化钠等价物的苛性碱溶液供给到浸没式燃烧气体蒸发器,和将包含二氧化碳的燃烧气体供给到所述浸没式燃烧气体蒸发器,其中所述二氧化碳与所述废液发生反应,将废液中的氢氧化物成分转化为碳酸盐,从而从燃烧气体中消耗二氧化碳。
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- 2003-09-02 JP JP2004534466A patent/JP2005537917A/ja active Pending
- 2003-09-02 RU RU2005109408/04A patent/RU2327502C2/ru not_active IP Right Cessation
- 2003-09-02 BR BR0314333-3A patent/BR0314333A/pt not_active Application Discontinuation
- 2003-09-02 NZ NZ538565A patent/NZ538565A/en unknown
- 2003-09-02 CA CA002497677A patent/CA2497677C/en not_active Expired - Fee Related
- 2003-09-02 CN CNB038211165A patent/CN1313182C/zh not_active Expired - Fee Related
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- 2003-09-02 AU AU2003268396A patent/AU2003268396A1/en not_active Abandoned
- 2003-09-02 WO PCT/US2003/027517 patent/WO2004022194A2/en active Application Filing
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2005
- 2005-03-02 ZA ZA200501803A patent/ZA200501803B/en unknown
- 2005-03-03 NO NO20051143A patent/NO20051143L/no not_active Application Discontinuation
- 2005-03-30 CO CO05028020A patent/CO5720978A2/es not_active Application Discontinuation
- 2005-04-04 EC EC2005005716A patent/ECSP055716A/es unknown
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2007
- 2007-04-13 US US11/786,824 patent/US20070251650A1/en not_active Abandoned
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Also Published As
Publication number | Publication date |
---|---|
EP1545731A2 (en) | 2005-06-29 |
ECSP055716A (es) | 2005-08-11 |
CA2497677C (en) | 2008-12-09 |
CO5720978A2 (es) | 2007-01-31 |
ZA200501803B (en) | 2006-05-31 |
BR0314333A (pt) | 2005-08-02 |
RU2327502C2 (ru) | 2008-06-27 |
NO20051143L (no) | 2005-03-21 |
CA2497677A1 (en) | 2004-03-18 |
WO2004022194A3 (en) | 2004-06-17 |
MXPA05002543A (es) | 2005-10-19 |
EP1545731A4 (en) | 2008-12-24 |
US20040040671A1 (en) | 2004-03-04 |
NZ538565A (en) | 2007-09-28 |
WO2004022194A2 (en) | 2004-03-18 |
US20070251650A1 (en) | 2007-11-01 |
US7214290B2 (en) | 2007-05-08 |
CN1688371A (zh) | 2005-10-26 |
AU2003268396A1 (en) | 2004-03-29 |
RU2005109408A (ru) | 2006-08-10 |
JP2005537917A (ja) | 2005-12-15 |
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