CN117480232A - 废合成树脂乳化装置 - Google Patents
废合成树脂乳化装置 Download PDFInfo
- Publication number
- CN117480232A CN117480232A CN202180099374.1A CN202180099374A CN117480232A CN 117480232 A CN117480232 A CN 117480232A CN 202180099374 A CN202180099374 A CN 202180099374A CN 117480232 A CN117480232 A CN 117480232A
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- Prior art keywords
- synthetic resin
- waste synthetic
- heavy oil
- heat exchanger
- decomposing furnace
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 229920003002 synthetic resin Polymers 0.000 title claims abstract description 103
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- 238000010438 heat treatment Methods 0.000 claims abstract description 60
- 239000003921 oil Substances 0.000 claims abstract description 49
- 238000003860 storage Methods 0.000 claims abstract description 11
- 238000004891 communication Methods 0.000 claims abstract description 9
- 230000001678 irradiating effect Effects 0.000 claims abstract description 5
- 239000007791 liquid phase Substances 0.000 claims abstract description 5
- 239000000919 ceramic Substances 0.000 claims description 53
- 239000002131 composite material Substances 0.000 claims description 47
- 239000000463 material Substances 0.000 claims description 14
- 239000000203 mixture Substances 0.000 claims description 9
- 239000000843 powder Substances 0.000 claims description 9
- 229910052771 Terbium Inorganic materials 0.000 claims description 5
- GZCRRIHWUXGPOV-UHFFFAOYSA-N terbium atom Chemical compound [Tb] GZCRRIHWUXGPOV-UHFFFAOYSA-N 0.000 claims description 5
- 229910052684 Cerium Inorganic materials 0.000 claims description 4
- GWXLDORMOJMVQZ-UHFFFAOYSA-N cerium Chemical compound [Ce] GWXLDORMOJMVQZ-UHFFFAOYSA-N 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 229910018072 Al 2 O 3 Inorganic materials 0.000 claims description 3
- 229910052692 Dysprosium Inorganic materials 0.000 claims description 3
- 229910052693 Europium Inorganic materials 0.000 claims description 3
- KBQHZAAAGSGFKK-UHFFFAOYSA-N dysprosium atom Chemical compound [Dy] KBQHZAAAGSGFKK-UHFFFAOYSA-N 0.000 claims description 3
- OGPBJKLSAFTDLK-UHFFFAOYSA-N europium atom Chemical compound [Eu] OGPBJKLSAFTDLK-UHFFFAOYSA-N 0.000 claims description 3
- 125000001183 hydrocarbyl group Chemical group 0.000 claims 1
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- 229910052799 carbon Inorganic materials 0.000 description 7
- 238000000354 decomposition reaction Methods 0.000 description 7
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- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 4
- 239000000395 magnesium oxide Substances 0.000 description 4
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 4
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- 239000004215 Carbon black (E152) Substances 0.000 description 2
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- BMMGVYCKOGBVEV-UHFFFAOYSA-N oxo(oxoceriooxy)cerium Chemical compound [Ce]=O.O=[Ce]=O BMMGVYCKOGBVEV-UHFFFAOYSA-N 0.000 description 2
- RVTZCBVAJQQJTK-UHFFFAOYSA-N oxygen(2-);zirconium(4+) Chemical compound [O-2].[O-2].[Zr+4] RVTZCBVAJQQJTK-UHFFFAOYSA-N 0.000 description 2
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- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
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- 229920000122 acrylonitrile butadiene styrene Polymers 0.000 description 1
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- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
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- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
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- 239000000460 chlorine Substances 0.000 description 1
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- 229910003440 dysprosium oxide Inorganic materials 0.000 description 1
- NLQFUUYNQFMIJW-UHFFFAOYSA-N dysprosium(iii) oxide Chemical compound O=[Dy]O[Dy]=O NLQFUUYNQFMIJW-UHFFFAOYSA-N 0.000 description 1
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- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
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- 239000013585 weight reducing agent Substances 0.000 description 1
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- C04B35/10—Shaped ceramic products characterised by their composition; Ceramics compositions; Processing powders of inorganic compounds preparatory to the manufacturing of ceramic products based on oxide ceramics based on aluminium oxide
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- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
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- C04B35/48—Shaped ceramic products characterised by their composition; Ceramics compositions; Processing powders of inorganic compounds preparatory to the manufacturing of ceramic products based on oxide ceramics based on zirconium or hafnium oxides, zirconates, zircon or hafnates
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- C10G15/00—Cracking of hydrocarbon oils by electric means, electromagnetic or mechanical vibrations, by particle radiation or with gases superheated in electric arcs
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- C10G32/00—Refining of hydrocarbon oils by electric or magnetic means, by irradiation, or by using microorganisms
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Abstract
公开了一种废合成树脂乳化装置。根据本发明一实施例的废合成树脂乳化装置包括:分解炉,容纳废合成树脂,对所述废合成树脂加热的同时用紫外线照射生成作为重质油的油蒸汽;热交换器,与所述分解炉连通地设置,用于冷却从所述分解炉流入的作为重质油的油蒸气,并将其转化为液相的重质油;以及存储罐,与所述热交换器连通地设置,用于接收并储存在所述热交换器中转化的重质油。
Description
技术领域
本发明涉及一种废合成树脂乳化装置。
背景技术
一般来说,由聚乙烯、聚丙烯、聚苯乙烯等作为原料制成的废塑料的再利用率较低,大多通过焚烧或填埋的方式处理。
由于废塑料的焚烧或填埋造成严重的环境污染,且需要大量时间才能分解至自然状态,因此需要开发环保且经济的废塑料处理技术。
废乙烯或废塑料等废合成树脂的原料是原油,汽油、柴油、液化气也是从原油中蒸馏提取的。废合成树脂的原料是分子量较大的烃类聚合物,而炼油厂生产的汽油、柴油是相对分子质量较小的烃类聚合物,因此可以将废合成树脂液化,然后裂解将其转化为石油。
作为裂解方法,通常部分地采用在无氧条件下加热高分子材料的热分解乳化工艺,但这不仅会产生公害物质,而且产出的油中还含有蜡、焦油、焦化物、灰分、铝箔以及重金属等,因为低质量的问题目前禁止使用。
现有的高温热分解乳化工艺中,将细碎的废合成树脂供给到高温熔融炉中熔融成凝胶状,然后将凝胶状熔融液在热分解反应炉中加热到450℃以上的高温,将其分离成气体和液体,然后将其配置为从具有油类成分的气态气体中分离出含有蜡成分的重油,并且将已分离出重油的气体再次冷凝以获得具有高粘度的混合重质油。由在此获得的混合重质油作为热分解过程中想要生产的主要生成物,混合了多种具有低沸点到高沸点的重质油成分,具有高粘度的深黑褐色混合油含有大量的重金属、有害物质等。
例如下面的专利文献1公开了“利用废油的直接加热式废合成树脂乳化装置”。
根据下面专利文献1的利用废油的直接加热式废合成树脂乳化装置被供给有包含废合成树脂和废油的原料,所述利用废油的直接加热式废合成树脂乳化装置包括:反应炉,在高温及高压下发生热分解而产生气体;第一加热部件,包含与上述反应炉以排管连接的第一加热单元,从而加热从所述反应炉排出的原料并将加热的原料循环回到所述反应炉;以及冷却单元,冷却并冷凝从所述反应炉中产生的气体以提取再生油。
所述反应炉在高温高压下发生热分解后随着减压而产生气体,在所述第一加热部件中所述排管的一端穿过所述应炉的侧面并与所述反应炉的内部连接,另一端与所述第一加热单元连接,所述反应炉包括将所述反应炉内部的所述原料向所述第一加热单元排出的排出管;以及一端与所述第一加热单元连接,另一端连接所述反应炉内部,使所述第一加热单元中加热的所述原料向所述反应炉循环的循环管。
所述循环管的另一端分别形成有第一排出口和第二排出口,用于将所述原料循环至反应炉,当所述原料在所述反应炉中进行热分解时使用所述第一排出口,当所述原料在所述反应炉内进行热分解后,减压下将所述原料循环气化的过程中使用所述第二排出口,所述第一排出口形成为使得端部不向外展开,并且所述第二排出口的端部向外侧方向展开,使得循环的原料横向扩散并撞击反应炉的内壁。
下面的专利文献2公开了“废合成树脂乳化装置”。
根据下面专利文献2的废合成树脂乳化装置可投入废合成树脂,其包括:加热炉,搅拌所述废合成树脂并可以对其进行热分解;热交换器,与所述加热炉连接,并将废合成树脂在所述加热炉中热分解时产生的油类气体冷却液化并生成混合油;分离单元,与所述热交换器连接地构成,并利用沸点差将所述混合油分离成轻质油和重质油。
所述分离单元包括:倾斜流路单元,与所述热交换器连接,并以设定角度向上倾斜;辅助加热单元,安装在所述倾斜流路单元的前起始端侧,用于加热所述混合油;辅助冷却单元,安装在从所述倾斜流路单元而言所述辅助加热单元的后方,用于冷却根据所述辅助加热单元汽化的混合油气;第一分支流路,在所述辅助冷却单元的后方连接至所述倾斜流路单元,分离根据所述辅助冷却单元液化的重质油;第二分支流路,连接至所述倾斜流路单元的末端,分离根据所述辅助冷却单元液化的轻质油。
但是在上述现有的热分解乳化工艺中,供应到反应炉的废合成树脂在每个工序中必须采用间接加热的方式加热至450℃以上,因此加热时间相对较长,存在无法将大量的废弃合成树脂快速处理的问题。
现有技术文献
专利文献
专利文献1:韩国公开发明专利第10-2012-0019346号
专利文献2:韩国公开实用新型专利第20-2012-0007128号
发明内容
技术问题
因此,本发明要解决的技术问题是提供一种废合成树脂乳化装置,其通过将废合成树脂在较低温度下裂解分解的方式,快速生产混合重质油(C24~C60)。
技术方案
本发明的一方面提供一种废合成树脂乳化装置,其包括:分解炉,容纳废合成树脂,对所述废合成树脂加热的同时用紫外线照射生成作为重质油的油蒸汽;热交换器,与所述分解炉连通地设置,用于冷却从所述分解炉流入的作为重质油的油蒸气,并将其转化为液相的重质油;以及存储罐,与所述热交换器连通地设置,用于接收并储存在所述热交换器中转化的重质油。
所述分解炉可包括:主体,容纳废合成树脂;加热单元,设置在所述主体的内部,加热所述废合成树脂;紫外线发射单元,设置在所述主体的内部,并被所述加热单元加热,以发射紫外线照射所述废合成树脂;以及油蒸汽排出口,设置在所述主体的上部,将生成的上述作为重质油的油蒸汽排出至所述热交换器中。
所述加热单元可以将所述主体的内部温度加热至180至270℃,所述紫外线发射单元被所述加热单元加热并发射波长为120nm至250nm的紫外线以分解废合成树脂中含有的烃链。
所述紫外线发射单元可以包括一个以上的容纳多个陶瓷复合体的陶瓷复合体容纳部,所述陶瓷复合体可以由选自Al2O3、ZrO2以及MgO中的一种或两种以上的陶瓷粉末和选自LiF、MgF2及CaF2中的一种或两种以上的混合物的氟化物粉末,以及选自铽(Terbium,Tb)、铈(cerium,Ce)、铕(europium,Eu)以及镝(dysprosium,Dy)中的一种或两种以上的混合物之热荧光稀土类的荧光体材料混合并成型后烧结而制造,所述陶瓷复合体可以在180至270℃的温度下发射波长120至250nm的紫外线。
所述废合成树脂乳化装置可以进一步包括:温度传感器,与所述分解炉连接并测量所述分解炉内部的温度;压力传感器,与所述分解炉连接并测量所述分解炉内部的气压;以及控制单元,接收所述温度传感器和所述压力传感器测量的温度值和气压值并调节所述加热单元的温度。
所述废合成树脂乳化装置可以进一步包括流量计,所述流量计连接到所述热交换器,用于测量从所述热交换器供应到所述存储罐的重质油的流量,并将测量的流量值供应到所述控制单元,其中,当所述流量值小于设定值时,所述控制单元可以中断运行加热单元。
发明效果
根据本发明,同时利用加热具有热荧光特性的陶瓷复合体释放的光波能和热能,通过直接裂解分解反应,将废合成树脂气化成为重质油的油蒸气细颗粒(oil mist)后,可以冷凝而获得混合重质油(C24~C60)。由于同时利用热能和光波能,可在较低温度条件下快速获得优质重质油,能耗少且经济,并且由于低温过程不产生污染物(二恶英等),具有可以以环保方式生产优质重质油的效果。
附图说明
图1是根据本发明一实施例的废合成树脂的乳化装置的示意图。
图2示出根据本发明一实施例的分解炉的示图。
图3是显示根据本发明一实施例的陶瓷复合体发射的光的波长和强度的测量结果的曲线图。
图4是显示用于确认根据本发明一实施例的陶瓷复合体的废合成树脂分解性能的热重分析结果的曲线图。
图5是显示用于确认根据本发明一实施例的陶瓷复合体的废合成树脂分解性能的热重分析结果的曲线图。
图6是显示根据本发明一实施例生产的重质油的GC-MS(气相色谱-质谱联用仪,gas chromatograph-mass spectrometer)分析谱的曲线图。
具体实施方式
在下文中,将参考附图和实施例对本发明进行更详细地描述。下面描述的术语和说明仅仅是示例性的,以清楚地说明本发明,并且不应被解释为限制本发明的权利范围。
本发明的描述中使用的诸如第一和第二等的术语仅用于区分一个构成要素与另一个构成要素的目的。例如在不脱离本发明的权利范围的情况下,第一构成要素可以被命名为第二构成要素,类似地,第二构成要素也可以被命名为第一构成要素。术语“和/或”包括多个相关陈述项目中的任何一个或多个相关陈述项目的组合。
本发明中使用的术语仅用于描述特定的实施例,并不旨在限制本发明。除非上下文对单数表达另有明确指示,否则包括复数表达。在本申请中“包括”或“具有”等术语旨在表示说明书中所记载的特征、数字、步骤、操作、构成要素、部件或其组合的存在,应当理解为这并不预先排除一个或更多个其他特征、数字、步骤、操作、构成要素、部件或其组合的存在或附加的可能性。
除非另外定义,本文中使用的所有术语,包括技术或科学术语,具有与本发明所属技术领域的普通技术人员通常理解的含义相同的含义。常用词典中定义的术语应被解释为具有与它们在相关技术的上下文中具有的含义一致的含义,并且除非在本申请中明确定义,否则不应以理想化或过于形式的含义来解释。
图1是根据本发明一实施例的废合成树脂的乳化装置的示意图。
参考图1,根据本发明一实施例的废合成树脂乳化装置,其包括:分解炉10,容纳废合成树脂,对所述废合成树脂加热的同时用紫外线照射生成作为重质油的油蒸汽;热交换器20,与所述分解炉10连通地设置,用于冷却从所述分解炉10流入的作为重质油的油蒸气,并将其转化为液相的重质油;以及存储罐40,与所述热交换器20连通地设置,用于接收并储存在所述热交换器20中转化的重质油。
根据本发明一实施例的废合成树脂乳化装置通过分解废合成树脂生成作为重质油的油蒸汽,然后将生成的作为重质油的油蒸汽液化以获取重质油,从而从废合成树脂提取重质油。
与现有的热分解乳化工艺需要450℃以上的高温工艺不同,本发明的废合成树脂乳化装置通过利用热能的同时照射紫外线波能,在较低的温度下也可以迅速分解废合成树脂,从而在短时间内可以生产大量的重质油。
在这里废合成树脂可以包括废塑料、废乙烯等,其意指通过加热裂解成低分子材料的热塑性树脂。
热塑性树脂例如可以为聚乙烯、聚丙烯、聚苯乙烯、ABS树脂、丙烯腈苯乙烯、聚对苯二甲酸乙二醇酯、聚对苯二甲酸丁二醇酯、聚苯亚硫酸酯、聚苯醚、聚缩醛、聚碳酸酯、丙烯酸树脂、尼龙、聚酰胺、聚四氟乙烯、合成橡胶、聚氯乙烯等。
这里的重质油可以定义为含有蜡成分的油类,可以例如为船用C级油。
根据本发明一实施例的所述废合成树脂乳化装置的构成包括分解炉10以及热交换器20,对其构成分别说明如下。
根据本发明一实施例的所述分解炉10接收废合成树脂的供给并对其加热生成作为重质油的油蒸汽。
所述分解炉10可以包括:主体11,容纳废合成树脂;加热单元13,设置在所述主体11内部,用于加热所述废合成树脂;紫外线发射单元14,设置在所述主体11内部,并被所述加热单元加热13,以发射紫外线照射所述废合成树脂;以及油蒸汽排出口16,设置在所述主体11的上部,将上述生成的作为重质油的由蒸汽排出至所述热交换器20中。
所述主体11具有其内部能够注入废合成树脂的结构,并且可以被构造成圆柱形或长方体形状。
废合成树脂可以装载在推车17上,并通过安装在所述分解炉10一面的投入口12移动到所述主体11,所述主体11的内底部可以设置用于移动装载有废合成树脂的推车17的轨道18。
所述加热单元13将所述主体11的内部温度加热至180℃至270℃,所述紫外线发射单元14被所述加热单元13加热并可以发射波长为120nm至250nm的紫外线以分解废合成树脂中含有的烃链。
所述主体11内部设置有可将所述主体11内部温度加热至180℃至270℃的加热单元13,所述加热单元13可以是板状或圆筒状。
例如,所述加热单元13可以以板状在所述主体11的两侧内壁和底面上留有一定间隔地设置,所述加热单元13可以以圆柱形邻近所述主体11的内壁,与底面垂直或水平地设置一个或以一定间隔设置多个。所述加热单元13的形状不限于此,并且可以考虑分解炉10的形状、容量、目标温度等来适当地设计和改变。
所述紫外线发射单元14包括容纳有多个陶瓷复合体15b的一个以上的陶瓷复合体容纳单元15a。
所述陶瓷复合体15b由选自Al2O3、ZrO2以及MgO中的一种或两种以上的陶瓷粉末和选自LiF、MgF2及CaF2中的一种或两种以上的混合物的氟化物粉末,以及选自铽(Terbium,Tb)、铈(cerium,Ce)、铕(europium,Eu)以及镝(dysprosium,Dy)中的一种或两种以上的混合物之热荧光稀土类的荧光体材料混合并成型后烧结而制造,所述陶瓷复合体15b在180℃至270℃的温度可以下发射波长120nm至250nm的紫外线。
较详细而言,所述分解炉10的内部设置发射紫外线以分解废合成树脂中含有的烃链的紫外线发射单元14。所述紫外线发射单元14可以以片状或块状设置在所述主体11的内壁上。
所述紫外线发射单元14包括容纳有多个陶瓷复合体15b的一个以上的陶瓷复合体容纳单元15a。所述陶瓷复合体容纳单元15a由能够承受从所述加热单元13施加的热量而不阻挡从容纳的陶瓷复合体15b发出的紫外线的材料制成,例如可以使用金属网。
所述陶瓷复合体15b根据热荧光(Thermo-fluorescence)特性,在180至270℃的温度下发射对应于UV-C的波长为120至250nm的紫外线。发射的UV-C的波长在所述120至250nm范围内不连续地存在,并且对应于具有强波能的脉冲波(pulse wave)。所述发射的紫外线(脉冲波)的波能量根据波长换算时,相当于989至480kJ/mol。
由于所述废合成树脂中通常含有的聚乙烯、聚丙烯、聚苯乙烯等聚合物中含有的碳间单键结合(C-C)能为347kJ/mol,因此从所述陶瓷复合体15b发出的紫外线有引起碳元素之间单键结合的直接分解(direct cracking)的足够的能量。
因此,与现有的热分解乳化过程中必须有450℃以上的高温工艺不同,本发明的废合成树脂乳化装置在从所述陶瓷复合体15b发出的波能中添加热能,使得即使在180至270℃的较低温度下也能分解废合成树脂,因此可以缩短加热时间,并且还可获得可以减少维持450℃以上高温所需的能量的效果。不仅如此,与仅使用热能分解废合成树脂的情况不同,由于同时使用来自紫外线照射的波能,因此废合成树脂的分解发生得更快并且具有可以快速产生大量重质油的优点。
另外,现有的高温热分解工艺中,会产生焦炭、焦油、灰分并沉积在热分解反应炉内壁上,为了进行下一步工作,必须每次清除反应炉内壁上的残留物,由此导致无法连续运行反应炉的问题。但是本发明的废合成树脂乳化装置可以解决这个问题,因为该工艺是在相对较低的温度下进行的,并且不会产生焦炭、焦油、灰分等。
另外,高温热分解工艺必然地伴随释放二恶英、粉尘等有害物质,而本发明通过低温工艺不释放任何有害物质,对环境友好,并且节省了防止排放有害物质和回收有害物质的成本,具有经济效益。
废合成树脂中含有的烃链被所述加热单元13供给的热能及所述陶瓷复合体15b发出的紫外线的波能量分解,并且大多数分子量降低的烃链汽化成碳原子数为24至60的为重质油的油蒸汽。
更详细地描述所述陶瓷复合体15b的制造方法,制造所述陶瓷复合体15b可以包括:将所述陶瓷粉末、所述氟化物粉末及热荧光稀土类荧光体材料混合并成型以产生成型体的步骤;以及将所述成型体在1300至1450℃的温度下进行烧结的步骤。
所述陶瓷复合体15b可以具有板状或直径为8至15mm的球形,但不限于此,并且为了便于安装,可以适当地选择陶瓷复合体15b的形状。
所述油蒸汽排出口16排出通过热能和波能汽化的作为重质油的油蒸气。考虑到汽化的作为重质油的油蒸气上升,所述油蒸汽排出口16可以优选地安装在所述主体11的上部,但不限于此。
所述分解炉10可包括液压缸以密封内部。由于外部空气不会被引入到由所述液压缸密封的分解炉10中并且形成无氧气氛,因此除了由所述陶瓷复合体15b发射的紫外线引起的废合成树脂的碳间键的裂解反应之外,不会发生任何额外的反应。因此,废合成树脂不需要预处理过程,不产生污染物,分解残渣转化为诸如木炭状的碳块。未被所述陶瓷复合体15b分解的无机物或金属等杂质可以从分解残渣中分离出来并单独收集,并且分解残渣还可以作为高碳含量的高热量固体燃料重新利用。
所述主体11的下部可以形成有排出异物或废合成树脂中含有的水分的异物排出口。
另外,所述废合成树脂乳化装置可以进一步包括:温度传感器51,与所述分解炉10连接并测量所述分解炉10内部的温度;压力传感器52,与所述分解炉10连接并测量所述分解炉10内部的气压;以及控制单元50,接收所述温度传感器51和所述压力传感器52测量的温度值和气压值并调节所述加热单元13的温度。
所述温度传感器51和所述压力传感器52设置为与分解炉10的内部连接,以便于测量分解炉10内部的温度和压力。
所述控制单元50识别从所述温度传感器51和所述压力传感器52测量的温度值和压力值,并且当温度和压力过高时,可以控制为升高加热单元13的温度,而当测量的温度及压力过低时,可以控制为降低加热单元13的温度。
根据本发明一实施例的所述热交换器20与所述分解炉10连通,从而冷却和液化从所述分解炉10流入的作为重质油的油蒸气以生成重质油。
所述热交换器20可以与所述分解炉10的油蒸汽排出口16连接。所述热交换器20可以包括存储有冷却水的冷却水槽,流入到所述热交换器20的作为重质油的油蒸气被冷却水槽夺去热量,被冷却及液化,从而可以转化为重质油。
由于这样的热交换器20由本领域广泛已知的公知技术的热交换器20构成,因此将省略关于热交换器20本身的构造的更详细的描述。
所述废合成树脂乳化装置进一步包括流量计53,流量计53连接到所述热交换器20,用于测量从所述热交换器20供应到所述存储罐40的重质油的流量,并将测量的流量值供应到所述控制单元50,当流量值小于设定值时,所述控制单元50可以中断加热单元13的运行。
当根据所述流量计53测得的重质油流量小于一定值时,意味着可以从废合成树脂中提取的作为重质油的油蒸气已经耗尽,此时,所述控制单元50可以通过中断所述加热单元13的运行而终止废合成树脂乳化工艺。所述设定值可以根据投入到所述分解炉10的废合成树脂的量来不同地设定,例如当投入6000kg废合成树脂时,可以将设定值设定为100l/hr。
所述控制单元50优选地与前述的从所述温度传感器51和所述压力传感器52接收温度和压力值的控制单元50相同,并且可以自动或手动操作。
所述废合成树脂乳化装置还可以包括油水分离器30,其与所述热交换20连通地设置,除去从所述热交换器20供给的重质油中所含的水分,并将除去水分后的重质油供给给所述存储罐40。
所述油水分离器30通过利用密度差的重力方式或利用离心分离将由所述热交换器20液化的重质油中含有的水分分离。
由于这样的油水分离器30由本领域广泛已知的公知技术的油水分离器30构成,因此将省略关于油水分离器30本身的构造的更详细的描述。
上述生成的重质油可以移送到与所述热交换器或所述油水分离器30连接的存储罐40存储。
由于上述构造,本发明的废合成树脂乳化装置即使在180至270℃的低温下也可以利用从陶瓷复合体15b发射的紫外线的波能来分解废塑料中所含的碳-碳键,碳数减少的碳氢化合物可以顺利地油蒸汽汽化。产生的油蒸气经冷却液化过程可得到碳数为C24~C60的优质重质油。
下面,对如上所述构成的本发明的废合成树脂乳化装置的操作及优选实施例进行详细说明。
将废合成树脂装载到自动运输的推车17上并投入到分解炉10内部。将废合成树脂装入2辆推车17(各3个)上的共6个塑料袋,投入到分解炉10内部,装料后,使用液压缸密封投入口12,当热交换器20的冷却水流量速度达到一定状态时,开始启动加热单元13。
所述加热单元13呈圆柱形,在所述主体11内部的两侧部沿垂直于下表面的方向安装有12个(各6个)以及在所述主体11内部的下表面沿与下表面水平的方向上安装有24个。
所述主体11的内部温度最初设定为60℃,并且在投入废合成树脂之后,运行所述加热单元13将所述主体11内部的温度升高到270℃。
与安装在所述主体11内部的上表面和两侧面上的加热单元13相邻设置的紫外线发射单元14吸收热能,并且容纳在包含于所述紫外线发射单元14中的所述陶瓷复合体容纳单元15a的陶瓷复合体15b发射具有120至250nm波长的紫外线。由于所述发射的紫外线的波能,废合成树脂中所含的碳之间的键被分解,蒸发成碳数为24至60的作为重质油的油蒸气,并通过安装在所述分解炉10上部的一侧的油蒸汽排出口16排出。
上述排出的作为重质油的油蒸气通过热交换器20,被冷却和冷凝,并转化为液相的重质油。然后,将重质油供给到油水分离器30,在油水分离器30中分离除去重质油中含有的少量水分。所述经过油水分离器30的重质油被供给并存储在存储罐中。
连接至所述热交换器20的流量计53测量所产生的重质油的流量并将其供应至控制单元50。当流量减少到低于一定值时,所述控制单元50中断所述加热单元13的运行以结束该工艺。
实施例1.测量陶瓷复合体发射紫外线实验
为了分析所述陶瓷复合体的紫外线发射特性,测量了在180至270℃的温度下从所述陶瓷复合体发射的光的波长和强度。
陶瓷复合体通过以下方法制备。将纯度为99.99%以上的氧化铝(Al2O3)、氧化锆(ZrO2)、氧化镁(MgO)与以100重量份的粉碎至筛目#2400以上的陶瓷粉末为基准而混合的7重量份的LiF、MgF2及CaF2的氟化物粉末以及3重量份的由氧化铽(Tb3O)粉末、氧化镝(Dy2O3)粉末和氧化铈(CeO2)粉末混合的热荧光稀土材料混合。将混合物成型成直径为10毫米的球状,然后在1400℃下烧结制造陶瓷复合体。
图3是显示当所述陶瓷复合体被加热到180至270℃的温度时发射的光的波长和强度的测量结果的曲线图。如上述图3所示,发射波长在120至250nm范围内的紫外线,并且可以确认在所述波长范围中观察到不连续的波长分布(121、124、130、220、225、249nm)。
另外,下表1显示了根据包含在一般废合成树脂中的聚乙烯、聚丙烯和聚苯乙烯等的混合塑料类中存在的化学键类型的键能,下表2显示了根据所述陶瓷复合体发出的光的波长的波能转换值。转换通过下面数学式1而进行。
数学式1
其中,E是能量,h是普朗克常数(6.626×10-34J/s),c是光速(3×108m/s),λ是波长。
表1
表2
光波长(nm) | 波能转换值(KJ/mol) |
121 | ~989 |
124 | ~965 |
130 | ~920 |
220 | ~704 |
225 | ~532 |
249 | ~480 |
如从表1和表2可以确认,波长120至250nm的光的波能大于废合成树脂中存在最多的碳间单键的结合能(347kJ/mol)。因此,可以确认所述陶瓷复合体发出的光具有足够的能量来分解废合成树脂中的碳间单键。
实施例2.热重量分析
为了确认所述陶瓷复合体的废合成树脂分解性能,进行了热重分析(thermogravimetric analysis,TGA)。
将高密度聚乙烯(HDPE)样品单独放入热重分析仪中之后,以2℃/min的升温速率升温,并测量重量。另外,除了将高密度聚乙烯样品与陶瓷复合体一起放入热重分析仪之外,在相同条件下测量重量。上述分析结果如图4所示。图4a是高密度聚乙烯样品单独的热重分析结果,图4b显示了高密度聚乙烯样品和陶瓷复合体的热重分析结果。
如上述图4a和4b所示,当单独投入高密度聚乙烯样品时,从220℃的温度下观察到质量减少,相反,当一起投入陶瓷复合体时,确认到在110℃的温度下质量开始减少。
另外,对高密度聚乙烯样品在250℃恒温下进行300分钟的单独热重量分析,并且对高密度聚乙烯样品和陶瓷复合体一起进行相同的分析以进行比较。上述分析结果如图5所示。
如图5所示,在单独投入高密度聚乙烯样品的情况下,85分钟后开始质量减少,分析完成后,可以确认与初始样品投入重量相比发生了12%的重量减少。
相反,当将陶瓷复合体一同投入时,7分钟后开始分解,分析完成后,可以确认与样品的初始重量相比,重量减少了68%。
因此,从所述热重量分析结果证实,陶瓷复合体可以在较低温度下快速分解大量合成树脂。
实施例3.结果物物性及成分分析
根据上述废合成树脂乳化装置的优选实施例,由废合成树脂生产重质油,并对所生产的重质油和残渣的物理性质和成分进行分析。下表3显示了所生产的重质油的物理性质分析结果,图6显示了所生产的重质油的GC-MS(gas chromatograph-massspectrometer)分析谱。另外,残渣的物理性质和成分分析结果如下表4所示。
表3
表4
如上述表3所示,常温下产出高粘度液态重质油,产出重质油的自燃试验、水反应性试验、氧化试验均未发现问题,证实可以安全生产。另外,如图6的GC-MS测定结果所示,生成的重质油显示出C23~C54的碳数分布,确认含有最多量的C34~C44石蜡成分。
另外,如上述表4显示,重质油生产后剩下的残渣是类似木炭的黑色固体,经证实,其中含有水分、灰分、氯、硫黄成分以及少量的汞、镉、铅、砷等金属成分。特别是,因为它具有5000kcal/kg以上的低位发热量,可以确认残渣本身可以用作固体燃料。
因此,由以上结果可以确认,根据本发明优选实施例的废合成树脂乳化装置能够生产出高质量的重质油,并且残渣可以用作固体燃料。
上述实施例是用于解释本发明的示例,并且本发明不限于此。本发明所属领域的普通技术人员将能够通过各种修改来实施本发明,因此本发明的技术保护范围应由所附加的发明要求保护范围确定。
产业上的可利用性
本发明可以在较低温度下将废合成树脂裂解分解,快速生产混合重质油(C24~C60)。
Claims (6)
1.一种废合成树脂乳化装置,其包括:
分解炉,容纳废合成树脂,对所述废合成树脂加热的同时用紫外线照射生成作为重质油的油蒸汽;
热交换器,与所述分解炉连通地设置,用于冷却从所述分解炉流入的作为重质油的油蒸气,并将其转化为液相的重质油;以及
存储罐,与所述热交换器连通地设置,用于接收并储存在所述热交换器中转化的重质油。
2.根据权利要求1所述的废合成树脂乳化装置,其中,所述分解炉包括:
主体,容纳废合成树脂;
加热单元,设置在所述主体的内部,加热所述废合成树脂;
紫外线发射单元,设置在所述主体的内部,并被所述加热单元加热,以发射紫外线照射所述废合成树脂;以及
油蒸汽排出口,设置在所述主体的上部,将生成的上述作为重质油的油蒸汽排出至所述热交换器中。
3.根据权利要求2所述的废合成树脂乳化装置,其中,
所述加热单元将所述主体的内部温度加热至180℃至270℃,
所述紫外线发射单元被所述加热单元加热并发射波长为120nm至250nm的紫外线以分解废合成树脂中含有的烃链。
4.根据权利要求3所述的废合成树脂乳化装置,其中,
所述紫外线发射单元包括一个以上的容纳多个陶瓷复合体的陶瓷复合体容纳部,
所述陶瓷复合体由选自Al2O3、ZrO2以及MgO中的一种或两种以上的陶瓷粉末和选自LiF、MgF2及CaF2中的一种或两种以上的混合物的氟化物粉末,以及选自铽、铈、铕以及镝中的一种或两种以上的混合物之热荧光稀土类的荧光体材料混合并成型后烧结而制造,
所述陶瓷复合体在180℃至270℃的温度下发射波长120nm至250nm的紫外线。
5.根据权利要求2所述的废合成树脂乳化装置,所述废合成树脂乳化装置进一步包括:
温度传感器,与所述分解炉连接并测量所述分解炉内部的温度;
压力传感器,与所述分解炉连接并测量所述分解炉内部的气压;以及
控制单元,接收所述温度传感器和所述压力传感器测量的温度值和气压值并调节所述加热单元的温度。
6.根据权利要求5所述的废合成树脂乳化装置,
所述废合成树脂乳化装置进一步包括流量计,所述流量计连接到所述热交换器,用于测量从所述热交换器供应到所述存储罐的重质油的流量,并将测量的流量值供应到所述控制单元,
其中,当所述流量值小于设定值时,所述控制单元中断运行加热单元。
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