CN1624077A - 用泵搅拌器系统输入能量来催化解聚废料中的柴油 - Google Patents
用泵搅拌器系统输入能量来催化解聚废料中的柴油 Download PDFInfo
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Abstract
在具有固体物质排放和柴油产物蒸馏的油循环中从含烃废料中生产柴油,其通过用泵和搅拌器输入能量并使用由钾-、钠-、和镁-硅酸铝完全结晶的催化剂,其中通过搅拌器不断清洁所有的表面。
Description
本发明包括在300-400℃的温度下采用经碱性掺杂的硅酸铝作为催化剂,采用主要以泵和搅拌器结合形式的能量输入,用于催化裂解烃和矿物质分离的方法和设备,连有一个矿物质伴随物的排放口。
从德国专利No.10049377已知采用来自钠掺杂硅酸铝的特定催化剂的催化解聚。此裂解能、以柴油和汽油形式经裂解的烃的汽化热的加热和热损是通过壁加热积聚的。
此方法的缺点是,通过所必须的比反应温度更高的温度的温度差通过壁进行。由此总是形成一些反应焦炭。当升高相对于反应混合物更高的壁的温度,即要达到某种生产能力时,焦炭的量也随之增加。
此反应焦炭就此与钠掺杂硅酸铝反应成非反应性的残余物,其使装置变脏并使反应停止。这种催化剂和反应焦炭的反应混合物与装置壁粘结成硬残余物并在操作间隙要求高的清洁支出。此发明只是描述一种工序,而非一种经济的方法。
因此采用壁的深度加热和由此热量通过壁通过加热的主动输入是不可能经济的。在循环中的反应油的微弱的热传导决定壁外的加热与油中的反应之间较高的温差,其用以满足裂解能(解聚)、汽化热和加热的需要。
在油循环中,废油和焦油的情形下,每公斤汽化的柴油需要约0.4kWh/kg能量用于裂解、汽化和加热到从初始温度250℃至390℃的反应温度。在加入塑料的情形下,所需的能量几乎成倍,因为那是以冷的材料加入的,还需要额外的熔解热。
现在令人惊奇地发现热量输入的方法和对此适宜的催化剂体系,完全避免了所述缺点。该系统不由壁导热,而是将热量直接在反应系统中释放。
所述能量输入是在水力旋流器中排放柴油蒸汽的一个由泵和相对运行的搅拌系统组成的体系中进行的。所述搅拌系统在此也用于全面清洁在循环中排列的表面。
催化剂也是新开发的,仅用于塑料、沥青和废油,用钠完全结晶的Y-分子的掺杂是最理想的。对于生物材料,如脂肪和生物油,发现采用钙的掺杂是最理想的。对于木材的转化,需要采用镁的掺杂,以生产高价值柴油。对于卤素含量高的材料,如用于变压器油和PVC,需要钾的掺杂。
由于从300-400℃的循环中的产物排放不在系统中留有其它易挥发的产物,装置的产物是柴油。此产物的10%通过发电机以电流形式用于操作中的能量。这种能量转换的优点在于同时解决了在装置中产生少量气体的问题,该气体被导向抽吸空气并将废气的热量用于初始材料的预干燥和预热。
图1显示根据本发明的方法。1表示泵,其具有在抽吸侧2的材料输入口3和与循环油4的连接。在排放侧,压力管5切向进入搅拌容器6接口。其中有以旋转方向相对的搅拌器7,由电机8推动搅拌器7转动。搅拌器7含有另外的向上伸展的清洁臂,该臂刷洗搅拌容器的整个表面。
搅拌容器6通过连接管线9与水力旋流器10连接。在连接管线中设置控制阀11,它调节后续装置部分中的压力。在本发明的特殊形式中,也在此管线中设置另外的泵,通过随同泵1一起的频率变换器的压力调节该泵。水力旋流器10在其内部具有一个贴附在内壁上的文杜利管喷嘴12,它同样降低剩余的正压并增加排放效果。
在水力旋流器上方是具有油料位测量仪15的料位控制器14的安全容器13。在安全容器13上设置有一个由电机推动的搅拌器,其具有用于安全容器下部、旋流器和旋流器之下的容器的清洁臂。
在安全容器13的侧面是将产生的汽化柴油导向具有冷凝器26的蒸馏装置17的产物蒸汽管16。冷凝器26是管式水散热器,它的水在冷却回路中被再冷却。
在冷凝器26的前部,分离可能出现的水,该水由被调节的排液阀经一个电导率传感器单独分离,使得在产物中不包含水。产物柴油在塔顶部通过上部采用而导出。通过回流管,通过回流量控制柴油的质量。
所述回流管具有与发电机27的柴油贮存容器的连接,其向装置提供电能。其使用约10%所产生的柴油用于自电流供应并且通过发动机废气还产生用于预干燥和油的预热的热量。
所有的容器都出于方便加热阶段的目的采用外部电加热。在水力旋流器10下方具有带斜片层19的排放容器18,其用于分离在柴油中不能转化的起始材料的组成成份。
所述排放容器18与虹吸管2连接。在排放容器18的底部具有温度测量仪19,它将排放蜗形轮20投入操作,条件是当残余物质的分离使温度下降到在温度表25中的极限值下。
排放蜗形轮20在容器中含有过滤部件21,其使得液体部分通过滤筛22流回排放容器18,并使得一个在容器18外部的电热的闷烧部件23将来自固体相的剩余油部分汽化。对此设计温度能提高到600℃。从所述闷烧蜗形轮23逸出的油蒸汽经蒸汽管24进入安全容器13。
在一实施例中将进一步描述本发明。具有200kW驱动功率的离心泵通过在吸管(2)以5000l/h吸入油并通过材料入口(3)将以废油和沥青形式的600kg废料,以总共5,600l/h经压力管(5)切向送到直径为1,400mm的搅拌容器(6)中。其中具有旋转方向相对的搅拌器7,由40kW的电机(8)推动搅拌器7转动。搅拌器(7)带有另外的向上伸展的清洁臂,该臂刷洗搅拌容器的整个表面,即1400mm的搅拌容器下部,和500mm直径的顶部。
搅拌容器(6)由直径200mm的连接管(9)与水力旋流器(10)连接。在连接管中设置被调节的控制阀(11),它后续装置部分中的压力。水力旋流器(10)的直径为1000mm且其内壁附有最狭小横截面为100×200mm的文杜利管喷嘴(12),它同样降低剩余的正压并增加排放效果。
在水力旋流器上方是具有油料位测量仪15的料位控制器14直径2000mm的安全容器(13)。在安全容器(13)上设置有一个搅拌器,其用电机以10kW推动并具有用于安全容器下部、旋流器和旋流器之下的容器的清洁臂。
在安全容器(13)的侧面是将产生的汽化柴油导向塔直径为500mm的蒸馏装置(17)的产物蒸汽管(16)。所有的容器都出于方便加热阶段的目的采用总输出50kW的外部电加热。
在水力旋流器(10)下方是直径为2000mm具有斜片层(19)的排放容器(18)。其用于分离在柴油中不能转化的起始材料的组成成份。此排放容器(18)与直径200mm的虹吸管(2)连接。在排放容器的底部是温度测量以(19),它将排放蜗形轮(20)投入操作,条件是当残余物质的分离使温度下降到一个极限值下。
直径为80mm和处理能力要求为10-20kg/h的排放蜗形轮(20)含有在容器中的过滤部件(21),其使得液体部分通过滤筛(22)流回排放容器(18),并使得一个在容器(18)外部的电热的闷烧部件(23)以45kW的加热功率将来自固体相的剩余油部分汽化。对此设计温度能提高到600℃。从闷烧蜗形轮(23)逸出的油蒸汽经蒸汽管(24)进入安全容器(13)。
图1的标示
1.用于能量输入的泵
2.泵的抽吸侧
3.材料装载(输入)
4.供应循环油(输入2)
5.切向压力管
6.搅拌容器
7.搅拌器(在压力管切向的相对方向运动)
8.用于搅拌器的电机
9.到水力旋流器的连接管
10.水力旋流器
11.用于压力调节的控制阀
12.在水力旋流器中内部贴附的文杜利管喷嘴
13.安全容器
14.料位控制器
15.料位指示和调节
16.产物蒸汽导管
17.蒸馏装置
18.排放容器
19.在排放容器中的斜片层
20.排放蜗形轮
21.排放蜗形轮的过滤部件
22.排放蜗形轮的过滤部件的过滤筛
23.排放蜗形轮的闷烧部件(至600℃)
24.到安全容器的闷烧蒸汽管
25.在固体排放下方的温度测量
26.冷凝器
27.发电机
Claims (6)
1.一种在具有固体物质排放和柴油产物蒸馏的油循环中从含烃废料中生产柴油的方法,其特征在于,通过一个或多个泵输入主要能量和由此获得主要加热源。
2.根据权利要求1的方法,其特征在于,泵的流动能量通过相对方向运动的搅拌器阻断并转化成热量。
3.根据权利要求1和2的方法,其特征在于,对于催化转化分别根据应用,对于矿物质烃,如沥青、油和塑料,催化剂采用完全结晶的Y-分子的形式用钠掺杂的,对于生物材料,如脂肪和生物油,用钙掺杂,和对于木材的转化,采用镁的掺杂,在此对于卤素含量高的材料,如用于变压器油和PVC,采用钾的掺杂。
4.根据权利要求1的方法,其特征在于,通过在上部的循环管中的可调节的阀门和通过旋流器中的文杜利管喷嘴调节泵的剩余流动能量。
5.根据权利要求1的方法,其特征在于,装置具有温度控制仪和料位控制器,它们彼此交织,即,投料和能量输入系统是如此调节的,以保持料位。
6.一种进行所述方法的设备,其特征在于,装置具有以下组件,高功率输送泵、相对方向运动的搅拌器,节流调节阀门,在循环中的排放旋流器和在装置的两个出口具有加热的排放蜗形轮和蒸馏装置的排放容器。
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US20110235460A1 (en) * | 2005-07-22 | 2011-09-29 | Schlumberger Technology Corporation | Method and apparatus to optimize the mixing process |
EP1745840A1 (en) * | 2005-07-22 | 2007-01-24 | Services Petroliers Schlumberger | Apparatus and method for mixing a liquid material and a flowable powdery material to obtain a slurry |
DE102005056735B3 (de) * | 2005-11-29 | 2006-08-10 | Koch, Christian, Dr. | Hochleistungskammermischer für katalytische Ölsuspensionen als Reaktor für die Depolymerisation und Polymerisation von kohlenwasserstoffhaltigen Reststoffen zu Mitteldestillat im Kreislauf |
EP2134812A1 (de) * | 2006-11-20 | 2009-12-23 | Christian Koch | Hochleistungskammermischer für katalytische ölsuspensionen |
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- 2004-02-26 AT AT04090070T patent/ATE522590T1/de active
- 2004-02-26 EP EP04090070A patent/EP1538191B1/de not_active Expired - Lifetime
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- 2004-03-23 CN CNA2004100302703A patent/CN1624077A/zh active Pending
- 2004-03-30 RU RU2004109567/04A patent/RU2360946C2/ru active IP Right Revival
- 2004-03-31 BR BRPI0400912-6B1A patent/BRPI0400912B1/pt not_active IP Right Cessation
- 2004-07-15 CA CA002474523A patent/CA2474523A1/en not_active Abandoned
- 2004-07-15 US US10/891,971 patent/US7473348B2/en active Active - Reinstated
- 2004-10-08 JP JP2004295764A patent/JP2005163013A/ja active Pending
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CN102325857A (zh) * | 2009-02-20 | 2012-01-18 | 克里斯蒂安·科赫 | 用于预处理的浆状残留物的催化油化反应的带有液压垫片的油料反应器真空泵及其方法 |
CN102325857B (zh) * | 2009-02-20 | 2016-01-20 | 克里斯蒂安·科赫 | 用于预处理的浆状残留物的催化油化反应的带有液压垫片的油料反应器真空泵及其方法 |
CN104334690A (zh) * | 2012-03-26 | 2015-02-04 | 阿克塞尔·特劳特曼 | 对含烃材料进行催化解聚的装置及方法 |
US10723956B2 (en) | 2017-07-21 | 2020-07-28 | 1888711 Alberta Inc. | Enhanced distillate oil recovery from thermal processing and catalytic cracking of biomass slurry |
US10961465B2 (en) | 2017-07-21 | 2021-03-30 | 1888711 Alberta Inc. | Enhanced distillate oil recovery from thermal processing and catalytic cracking of biomass slurry |
US11859134B2 (en) | 2017-07-21 | 2024-01-02 | Cielo Waste Solutions Corp. | Enhanced distillate oil recovery from thermal processing and catalytic cracking of biomass slurry |
Also Published As
Publication number | Publication date |
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EP1538191B1 (de) | 2011-08-31 |
US7473348B2 (en) | 2009-01-06 |
ES2376573T3 (es) | 2012-03-15 |
BRPI0400912B1 (pt) | 2015-01-27 |
US20050115871A1 (en) | 2005-06-02 |
DE10356245B4 (de) | 2007-01-25 |
RU2360946C2 (ru) | 2009-07-10 |
CA2474523A1 (en) | 2005-06-02 |
JP2005163013A (ja) | 2005-06-23 |
MXPA04002431A (es) | 2005-09-08 |
BRPI0400912A (pt) | 2005-08-30 |
CY1112093T1 (el) | 2015-11-04 |
EP1538191A1 (de) | 2005-06-08 |
DE10356245A1 (de) | 2005-07-21 |
ATE522590T1 (de) | 2011-09-15 |
RU2004109567A (ru) | 2005-10-20 |
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