CN104671622B - 含c30+的固体污染物的处理系统、含油污泥的处理系统及方法 - Google Patents
含c30+的固体污染物的处理系统、含油污泥的处理系统及方法 Download PDFInfo
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- CN104671622B CN104671622B CN201510053501.0A CN201510053501A CN104671622B CN 104671622 B CN104671622 B CN 104671622B CN 201510053501 A CN201510053501 A CN 201510053501A CN 104671622 B CN104671622 B CN 104671622B
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- 230000005540 biological transmission Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- MWPLVEDNUUSJAV-UHFFFAOYSA-N Anthracene Chemical compound 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- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Natural products 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OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- BBEAQIROQSPTKN-UHFFFAOYSA-N Pyrene Chemical compound 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C1=CC=C2C=CC3=CC=CC4=CC=C1C2=C43 BBEAQIROQSPTKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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Abstract
本发明提供了含C30 +的固体污染物的处理系统、含油污泥的处理系统及方法,与现有技术相比,本发明实施例提供的含油污泥的处理系统先将含油污泥输送至热相分解装置中,在燃烧室加热的条件下进行热相分解,得到的含C30 +的固体污染物依次经过筛分、研磨、悬浮,再输送至燃烧室进行燃烧,实现含C30 +的固体污染物的完全燃尽,解决了其对环境带来的污染问题。实验结果表明,处理后的含C30 +的固体污染物呈红色,固体TPH值小于3000mg/kg。
Description
技术领域
[0001]本发明涉及固体污染物处理技术领域,更具体地说,是涉及含C3Q+的固体污染物的处理系统、含油污泥的处理系统及方法。
背景技术
[0002]含油污泥,又称TOC固体污染物,是油田和炼油厂的原油生产储运系统以及污水处理系统中产生的固体污染物。含油污泥中一般含油率在10%〜50%,此外还含有大量的苯系物、酚类、蒽、芘等有毒物质,若不加以处理,不仅污染环境,而且造成资源浪费。
[0003]目前,国内外对含油污泥的处理主要采用以下两种技术,一是完全焚烧技术(简称TDU技术),二是热相分解技术(简称TPS技术)。其中,TDU技术对设备的要求较高,投资成本较大,不利于大规模推广。而TPS技术通过将含油污泥在绝氧条件下加热,使烃类及有机物解吸,其中一部分解吸后的不可凝燃气被循环燃烧形成高温烟气,从而又可以间接提供热解所需能量,节约能源的同时实现了烃类的回收利用,因此TPS技术在处理含油污泥方面具有广阔应用前景。
[0004]但是,采用TPS技术对含油污泥进行处理,只能将含油污泥中30个碳以下的有机污染物挥发出去进行回收利用,而大于30个碳的有机污染物(以下简称C3q+)无法进行分离,产生难以处理的含C3Q+的固体污染物。含C3Q+的固体污染物处理难度大,采用常规焚烧技术无法实现完全燃尽,并且含C3Q+的固体污染物会对环境造成长期严重的污染,无法达到各国环保标准要求。
发明内容
[0005]有鉴于此,本发明的目的在于提供含C3Q+的固体污染物的处理系统、含油污泥的处理系统及方法,本发明提供的处理系统能够实现C3Q+的固体污染物的完全燃尽。
[0006]本发明提供了 一种含C3Q+的固体污染物的处理系统,包括:
[0007]用于将含C3Q+的固体污染物进行筛分的筛分装置;
[0008]与所述筛分装置依次相连的研磨装置、悬浮装置和输送装置;
[0009]以及与所述输送装置相通的燃烧室,所述燃烧室用于将含C3Q+的固体污染物进行燃烧。
[0010]优选的,所述输送装置包括:
[0011]与所述悬浮装置相连的多个相互并联的悬浮体输送管路,所述悬浮体输送管路设有吹入喷咀;
[0012]所述输送装置通过所述吹入喷咀与所述燃烧室直接相通。
[0013]优选的,所述筛分装置包括:
[0014]与所述研磨装置依次相连的干燥单元和滤除单元。
[0015]本发明还提供了一种含油污泥的处理系统,包括:
[0016]用于将含油污泥进行气固分离的热相分解装置,所述热相分解装置设有进料管路和固相出料管路;所述固相出料管路用于排出含C3Q+的固体污染物;
[0017]用于将含C3Q+的固体污染物进行筛分的筛分装置;所述筛分装置与所述固相出料管路相连;
[0018]与所述筛分装置依次相连的研磨装置、悬浮装置和输送装置;
[0019]以及与所述输送装置相通的燃烧室,所述燃烧室用于将含C3Q+的固体污染物进行燃烧;
[0020]所述燃烧室设置在热相分解装置周围,用于对所述热相分解装置进行加热。
[0021] 优选的,还包括:
[0022]设置在所述热相分解装置上的气相出料管路,所述气相出料管路用于排出热解气体;
[0023]与所述气相出料管路相连的气液分离装置,所述气液分离装置设有气相分离管路和液相分离管路;所述气相分离管路与所述燃烧室相通;
[0024]与所述液相分离管路相连的液液分离装置,所述液液分离装置设有油相分离管路和水相分离管路。
[0025]优选的,所述气相出料管路上设有冷凝器,用于对进入气液分离装置前的热解气体进行冷却。
[0026]本发明还提供了一种含油污泥的处理方法,包括以下步骤:
[0027] a)将含油污泥加热,进行热相分解,得到含C3O+的固体污染物;
[0028] b)将步骤a)得到的含C3O+的固体污染物依次进行筛分、研磨、悬浮、输送、燃烧。
[0029]优选的,步骤a)中所述热相分解的温度为300°C〜600°C。
[0030]优选的,所述步骤b)具体包括以下步骤:
[0031] bl)将含C3O+的固体污染物依次进行滤除、干燥,得到筛分后的含C3O+的固体污染物;
[0032] b2)将筛分后的含C3O+的固体污染物进行研磨,得到含C3O+的固体污染物粉末;
[0033] b3)将含C3Q+的固体污染物粉末与空气混合,得到含C3Q+的固体污染物悬浮体;
[0034] b4)将含C3O+的固体污染物悬浮体输送到燃烧室,进行燃烧。
[0035]优选的,所述步骤a)具体包括:将含油污泥加热,进行热相分解,得到含C3O+的固体污染物和热解气体;
[0036] 所述处理方法还包括:步骤c)对所述热解气体进行后处理;
[0037]所述后处理具体包括以下步骤:
[0038] Cl)将热解气体进行气液分离,分别得到液体油和不可凝燃气;
[0039] c2)将步骤Cl)得到的液体油进行液液分离,分别得到水和可回收碳氢化合物;
[0040] c3)将步骤Cl)得到的不可凝燃气通入燃烧室,进行燃烧;
[0041 ] 所述步骤c2)和步骤c3)没有顺序限制。
[0042]本发明提供了含C3Q+的固体污染物的处理系统、含油污泥的处理系统及方法,所述含油污泥的处理系统包括:用于将含油污泥进行气固分离的热相分解装置,所述热相分解装置设有进料管路和固相出料管路;所述固相出料管路用于排出含C3Q+的固体污染物;用于将含C3O+的固体污染物进行筛分的筛分装置;所述筛分装置与所述固相出料管路相连;与所述筛分装置依次相连的研磨装置、悬浮装置和输送装置;以及与所述输送装置相通的燃烧室,所述燃烧室用于将含C3Q+的固体污染物进行燃烧;所述燃烧室设置在热相分解装置周围,用于对所述热相分解装置进行加热。与现有技术相比,本发明实施例提供的含油污泥的处理系统先将含油污泥输送至热相分解装置中,在燃烧室加热的条件下进行热相分解,得到的含C3O+的固体污染物依次经过筛分、研磨、悬浮,再输送至燃烧室进行燃烧,实现含C30+的固体污染物的完全燃尽,解决了其对环境带来的污染问题。实验结果表明,处理后的含C30+的固体污染物呈红色,固体TPH值小于3000mg/kg。
[0043]此外,本发明实施例提供的含油污泥的处理系统能够对热相分解后的热解气体进行逐步分离,得到的不可凝燃气可循环输送至燃烧室进行燃烧,节约能源;得到的液相碳氢化合物进行回收,从而实现资源的二次利用。
附图说明
[0044]为了更清楚地说明本发明实施例或现有技术中的技术方案,下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍,显而易见地,下面描述中的附图仅仅是本发明的实施例,对于本领域普通技术人员来讲,在不付出创造性劳动的前提下,还可以根据提供的附图获得其他的附图。
[0045]图1为本发明实施例提供的含C3O+的固体污染物的处理系统的结构示意图;
[0046]图2为本发明实施例提供的含油污泥的处理系统的结构示意图。
具体实施方式
[0047]下面将结合本发明实施例,对本发明的技术方案进行清楚、完整地描述,显然,所描述的实施例仅仅是本发明一部分实施例,而不是全部的实施例。基于本发明中的实施例,本领域普通技术人员在没有做出创造性劳动前提下所获得的所有其他实施例,都属于本发明保护的范围。
[0048]本发明提供了 一种含C3Q+的固体污染物的处理系统,包括:
[0049]用于将含C3O+的固体污染物进行筛分的筛分装置;
[0050]与所述筛分装置依次相连的研磨装置、悬浮装置和输送装置;
[0051]以及与所述输送装置相通的燃烧室,所述燃烧室用于将含C3Q+的固体污染物进行燃烧。
[0052]请参阅图1,图1为本发明实施例提供的含C3Q+的固体污染物的处理系统的结构示意图,其中,I为筛分装置,2为研磨装置,3为悬浮装置,4为输送装置,5为燃烧室,6为悬浮体输送管路,7为吹入喷阻。
[0053]在本发明中,所述筛分装置(I)用于将含C3Q+的固体污染物进行筛分,便于进行后续处理。所述筛分装置(I)优选包括:
[0054]与所述研磨装置(2)依次相连的干燥单元和滤除单元。在本发明中,所述滤除单元用于将大粒径的含C3Q+的固体污染物筛出,便于进行进一步研磨;本发明对所述滤除单元所用的具体设备没有特殊限制,如可采用本领域技术人员熟知的振动筛。
[0055]在本发明中,所述干燥单元与所述滤除单元相连,用于将含C3Q+的固体污染物中的水分脱除,防止多余水分吸收热量,在燃烧室(5)内急速蒸发,造成燃烧室(5)压力增大;本发明对所述干燥单元所用的具体设备没有特殊限制,如可采用本领域技术人员熟知的烘箱。
[0056]在本发明中,所述筛分装置(I)依次与研磨装置(2)、悬浮装置(3)和输送装置(4)相连。所述研磨装置(2)与所述筛分装置(I)的干燥单元直接相连,用于将先后进行滤除和干燥后的含C3Q+的固体污染物进行研磨,得到含C3O+的固体污染物粉末。所述研磨装置(2)优选为气流粉碎机;所述气流粉碎机为本领域技术人员熟知的用于研磨的设备,本发明对此没有特殊限制。
[0057]在本发明中,所述悬浮装置(3)与所述研磨装置(2)直接相连,用于将研磨后的含C30+的固体污染物粉末进行悬浮,得到含C3Q+的固体污染物悬浮体。所述悬浮装置(3)优选为悬浮鼓风机;所述悬浮鼓风机为本领域技术人员熟知的设备,本发明对此没有特殊限制。
[0058]在本发明中,所述输送装置(4)与所述悬浮装置(3)直接相连,用于将含C3Q+的固体污染物悬浮体输送至燃烧室(5)。所述输送装置(4)优选包括:
[0059]与所述悬浮装置(3)相连的多个相互并联的悬浮体输送管路(6),所述悬浮体输送管路(6)设有吹入喷咀(7);
[0060]所述输送装置(4)通过所述吹入喷咀(7)与所述燃烧室(5)直接相通。在本发明中,由悬浮装置(3)得到的含C3Q+的固体污染物悬浮体,经过悬浮体输送管路(6),再由吹入喷咀
(7)输送至燃烧室(5)。
[0061]在本发明中,所述燃烧室(5)与所述输送装置(4)通过所述吹入喷咀(7)直接相通,用于将含C3Q+的固体污染物悬浮体进行燃烧,实现含C3Q+的固体污染物的完全燃尽。
[0062]按照上述本发明实施例提供的含C3Q+的固体污染物的处理系统,能够实现对含C30+的固体污染物的完全燃尽。本发明实施例工作过程如下:
[0063]首先,将含C3Q+的固体污染物在筛分装置(I)中,经滤除单元进行滤除,再经干燥单元进行干燥,得到筛分后的含C3O+的固体污染物。
[0064]其次,将筛分后的含C3O+的固体污染物在研磨装置(2)中进行研磨,得到含C3O+的固体污染物粉末。
[0065]再次,将含C3Q+的固体污染物粉末在悬浮装置(3)中与空气混合,得到含C3Q+的固体污染物悬浮体。
[0066]最后,将含C3Q+的固体污染物悬浮体经输送装置(4)的悬浮体输送管路(6),由吹入喷咀(7)进入燃烧室(5)进行燃烧,实现含C3O+的固体污染物的完全燃尽。
[0067]本发明还提供了一种含油污泥的处理系统,包括:
[0068]用于将含油污泥进行气固分离的热相分解装置,所述热相分解装置设有进料管路和固相出料管路;所述固相出料管路用于排出含C3Q+的固体污染物;
[0069]用于将含C3Q+的固体污染物进行筛分的筛分装置;所述筛分装置与所述固相出料管路相连;
[0070]与所述筛分装置依次相连的研磨装置、悬浮装置和输送装置;
[0071]以及与所述输送装置相通的燃烧室,所述燃烧室用于将含C3Q+的固体污染物进行燃烧;
[0072]所述燃烧室设置在热相分解装置周围,用于对所述热相分解装置进行加热。
[0073]请参阅图2,图2为本发明实施例提供的含油污泥的处理系统的结构示意图,其中,I为热相分解装置,2为进料管路,3为固相出料管路,4为筛分装置,5为研磨装置,6为悬浮装置,7为输送装置,8为燃烧室,9为悬浮体输送管路,10为吹入喷咀,11为气相出料管路,12为气液分离装置,13为气相分离管路,14为液相分离管路,15为液液分离装置,16为水相分离管路,17为油相分离管路,18为冷凝器。
[0074]在本发明中,所述热相分解装置(I)用于将含油污泥进行气固分离。所述热相分解装置(I)设有进料管路(2)和固相出料管路(3),其中,所述进料管路(2)用于将含油污泥输送至热相分解装置(I);所述固相出料管路(3)用于排出含C3Q+的固体污染物。在本发明中,所述热相分解装置(I)通过设置在周围的燃烧室(8)提供的热量,进行绝氧加热,含油污泥从进料管路(2)进入热相分解装置(I)后,在热相分解装置(I)中螺旋给进,往复运动,从而在加热过程中实现气固分离,得到含C3Q+的固体污染物后,经固相出料管路(3)排出,进行进一步处理。
[0075]在本发明中,所述固相出料管路(3)与筛分装置(4)相连。所述筛分装置(4)用于将含C3O+的固体污染物进行筛分,便于进行后续处理。所述筛分装置(4)优选包括:
[0076]与所述研磨装置(5)依次相连的干燥单元和滤除单元。在本发明中,所述滤除单元用于将大粒径的含C3Q+的固体污染物筛出,便于进行进一步研磨;本发明对所述滤除单元所用的具体设备没有特殊限制,如可采用本领域技术人员熟知的振动筛。
[0077]在本发明中,所述干燥单元与所述滤除单元相连,用于将含C3Q+的固体污染物中的水分脱除,防止多余水分吸收热量,在燃烧室(8)内急速蒸发,造成燃烧室(8)压力增大;本发明对所述干燥单元所用的具体设备没有特殊限制,如可采用本领域技术人员熟知的烘箱。
[0078]在本发明中,所述筛分装置(4)依次与研磨装置(5)、悬浮装置(6)和输送装置(7)相连。所述研磨装置(5)与所述筛分装置(4)的干燥单元直接相连,用于将先后进行滤除和干燥后的含C3Q+的固体污染物进行研磨,得到含C3O+的固体污染物粉末。所述研磨装置(5)优选为气流粉碎机;所述气流粉碎机为本领域技术人员熟知的用于研磨的设备,本发明对此没有特殊限制。
[0079]在本发明中,所述悬浮装置(6)与所述研磨装置(5)直接相连,用于将研磨后的含C30+的固体污染物粉末进行悬浮,得到含C3Q+的固体污染物悬浮体。所述悬浮装置(6)优选为悬浮鼓风机;所述悬浮鼓风机为本领域技术人员熟知的设备,本发明对此没有特殊限制。
[0080]在本发明中,所述输送装置(7)与所述悬浮装置(6)直接相连,用于将含C3Q+的固体污染物悬浮体输送至燃烧室(8)。所述输送装置(7)优选包括:
[0081]与所述悬浮装置(6)相连的多个相互并联的悬浮体输送管路(9),所述悬浮体输送管路(9)设有吹入喷咀(10);
[0082]所述输送装置(7)通过所述吹入喷咀(10)与所述燃烧室(8)直接相通。在本发明中,由悬浮装置(6)得到的含C3Q+的固体污染物悬浮体,经过悬浮体输送管路(9),再由吹入喷咀(I O)输送至燃烧室(8)。
[0083]在本发明中,所述燃烧室(8)与所述输送装置(7)通过所述吹入喷咀(10)直接相通,用于将含C3Q+的固体污染物悬浮体进行燃烧,实现含C3Q+的固体污染物的完全燃尽。同时,所述燃烧室(8)设置在热相分解装置(I)周围,用于对所述热相分解装置(I)进行加热。
[0084]在本发明中,所述含油污泥的处理系统优选还包括:
[0085]设置在所述热相分解装置(I)上的气相出料管路(11),所述气相出料管路(11)用于排出热解气体;
[0086]与所述气相出料管路(11)相连的气液分离装置(12),所述气液分离装置(12)设有气相分离管路(13)和液相分离管路(14);所述气相分离管路(13)与所述燃烧室(8)相通;
[0087]与所述液相分离管路(14)相连的液液分离装置(15),所述液液分离装置(15)设有油相分离管路(17)和水相分离管路(16)。
[0088]在本发明中,所述热相分解装置(I)上还设有气相出料管路(11),所述气相出料管路(11)用于排出热解气体。在本发明中,所述热相分解装置(I)将含油污泥进行气固分离,得到含C3Q+的固体污染物和热解气体,其中,所述含C3Q+的固体污染物按照上述技术方案提供的装置及方法进行处理;所述热解气体经气相出料管路(11)排出,进行进一步处理。
[0089]在本发明中,所述气相出料管路(11)与所述气液分离装置(12)相连。所述气液分离装置(12)用于将热解气体进行气液分离。在本发明中,所述气液分离装置(12)设有气相分离管路(13)和液相分离管路(14),其中,所述气相分离管路(13)与所述燃烧室(8)相通,用于将气液分离装置(12)中进行气液分离得到的不可凝燃气输送至燃烧室(8)中进行燃烧;所述液相分离管路(14)用于排出气液分离得到的液体油。
[0090]在本发明中,所述液相分离管路(14)与所述液液分离装置(15)相连。所述液液分离装置(15)用于将所述液体油进行液液分离。在本发明中,所述液液分离装置(15)设有油相分离管路(17)和水相分离管路(16),其中,所述油相分离管路(17)用于排出液液分离得到的可回收碳氢化合物,从而实现可回收碳氢化合物的二次利用;所述水相分离管路(16)用于排出液液分离得到的水。
[0091]在本发明中,所述气相出料管路(11)上优选还设有冷凝器(18),用于对进入气液分离装置前的热解气体进行冷却。
[0092]按照上述本发明实施例提供的含油污泥的处理系统,能够实现对含C3Q+的固体污染物的完全燃尽,同时能够对热相分解后的热解气体进行逐步分离,实现资源的二次利用。本发明实施例工作过程如下:
[0093]首先,将含油污泥经经进料管路(2)输送至热相分解装置(I)中,通过设置在所述热相分解装置(I)周围的燃烧室(8)提供热量,进行绝氧加热,所述含油污泥在热相分解装置(I)中螺旋给进,往复运动,从而在加热过程中实现气固分离,得到含C3Q+的固体污染物和热解气体。其中,所述含C3Q+的固体污染物经固相出料管路(3)排出,进行进一步处理;所述热解气体经气相出料管路(11)排出,进行进一步处理。
[0094]其次,将经固相出料管路(3)排出的含C3Q+的固体污染物,在筛分装置(4)中,经滤除单元进行滤除,再经干燥单元进行干燥,得到筛分后的含C3O+的固体污染物。再将筛分后的含C3O+的固体污染物在研磨装置(5)中进行研磨,得到含C3O+的固体污染物粉末。然后,将含C3Q+的固体污染物粉末在悬浮装置(6)中与空气混合,得到含C3Q+的固体污染物悬浮体。最后,将含C3Q+的固体污染物悬浮体经输送装置(7)的悬浮体输送管路(9),由吹入喷咀(10)进入燃烧室(8)进行燃烧,实现含C3O+的固体污染物的完全燃尽。
[0095]同时,将经气相出料管路(11)排出的热解气,经冷凝器(18)进行初步冷凝后,进入气液分离装置(12)进行气液分离,分别得到液体油和不可凝燃气。其中,所述不可凝燃气经气相分离管路(13)输送至燃烧室(8)中,进行燃烧,为热相分解装置(I)提供热量;所述液体油经液液分离装置(15)进行液液分离,分别得到可回收碳氢化合物和水。最后,所述可回收碳氢化合物经油相分离管路(17)排出,进行回收,实现资源的二次利用;得到的水经水相分离管路(16)排出。
[0096]本发明还提供了一种含油污泥的处理方法,包括以下步骤:
[0097] a)将含油污泥加热,进行热相分解,得到含C3O+的固体污染物;
[0098] b)将步骤a)得到的含C3O+的固体污染物依次进行筛分、研磨、悬浮、输送、燃烧。
[0099]在本发明中,将含油污泥加热,进行热相分解。在本发明中,所述含油污泥是油田和炼油厂的原油生产储运系统以及污水处理系统中产生的固体污染物,本发明对所述含油污泥的来源没有特殊限制。在本发明中,所述热相分解为本领域技术人员熟知的技术手段,用于将含油污泥中的30个碳以下的有机污染物热解挥发。在本发明中,所述热相分解的温度优选为300 °C〜600 °C,更优选为500 °C。
[0100]在本发明中,将含油污泥加热,进行热相分解,得到含C3O+的固体污染物。本发明将所述含C3O+的固体污染物依次进行筛分、研磨、悬浮、输送、燃烧。
[0101]所述将含C3O+的固体污染物依次进行筛分、研磨、悬浮、输送、燃烧的过程优选具体包括以下步骤:
[0102] bl)将含C3Q+的固体污染物依次进行滤除、干燥,得到筛分后的含C3Q+的固体污染物;
[0103] b2)将筛分后的含C3O+的固体污染物进行研磨,得到含C3O+的固体污染物粉末;
[0104] b3)将含C3O+的固体污染物粉末与空气混合,得到含C3O+的固体污染物悬浮体;
[0105] b4)将含C3O+的固体污染物悬浮体输送到燃烧室(8),进行燃烧。
[0106]在本发明中,将含C3Q+的固体污染物依次进行滤除、干燥,得到筛分后的含C3Q+的固体污染物。在本发明中,所述滤除的目的是将大粒径的含C3Q+的固体污染物筛出,便于进行进一步研磨;本发明对所述滤除的设备没有特殊限制,如可采用本领域技术人员熟知的振动筛。在本发明中,所述滤除后的含C3Q+的固体污染物的粒径优选为大于O小于8mm,更优选为大于O小于5mm ο
[0107]在本发明中,所述干燥的目的是将含C3Q+的固体污染物中的水分脱除,防止多余水分吸收热量,在燃烧室(8)内急速蒸发,造成燃烧室(8)压力增大;本发明对所述干燥的设备没有特殊限制,如可采用本领域技术人员熟知的烘箱。在本发明中,所述干燥后的含C3Q+的固体污染物的含水量优选为大于O小于1.5wt%,更优选为大于O小于lwt%。
[0108]得到筛分后的含C3Q+的固体污染物后,本发明将筛分后的含C3Q+的固体污染物进行研磨,得到含C3O+的固体污染物粉末。在本发明中,所述研磨的目的是进一步减小含C3O+的固体污染物的粒径,得到能够在空气中悬浮的含C3Q+的固体污染物粉末。在本发明中,所述研磨后的含C3O+的固体污染物粉末的粒径优选为大于O小于等于1.5μπι,更优选为大于O小于等于 Iym ο
[0109]得到含C3Q+的固体污染物粉末后,本发明将含C3Q+的固体污染物粉末与空气混合,得到含C3Q+的固体污染物悬浮体。在本发明中,所述悬浮用空气与燃烧室(8)内用于燃烧的空气质量相同,这样能够使含C3Q+的固体污染物悬浮体保持一定的紊流强度,在输送过程中形成稳定的悬浮体。
[0110]得到含C3Q+的固体污染物悬浮体后,本发明将含C3Q+的固体污染物悬浮体输送到燃烧室(8),进行燃烧。在本发明中,所述输送过程经多个相互并联的悬浮体输送管路(9),再由悬浮体输送管路(9)末端的吹入喷咀(10)吹入燃烧室(8)。在本发明中,所述燃烧的温度优选为300 °C〜600 °C,更优选为500 °C。
[0111]在本发明中,对燃烧后的固体进行TPH值检测,所述TPH值检测的方法为本领域技术人员熟知的石油烃类物质检测的方法,本发明对此没有特殊限制。
[0112]在本发明中,将含油污泥加热,进行热相分解,得到含C3O+的固体污染物和热解气体。其中,所述含C3Q+的固体污染物按照上述技术方案提供的处理方法进行处理;所述热解气体优选还包括进行后处理。
[0113]在本发明中,所述后处理优选具体包括以下步骤:
[0114] Cl)将热解气体进行气液分离,分别得到液体油和不可凝燃气;
[0115] c2)将步骤Cl)得到的液体油进行液液分离,分别得到水和可回收碳氢化合物;
[0116] c3)将步骤Cl)得到的不可凝燃气通入燃烧室,进行燃烧;
[0117] 所述步骤c2)和步骤c3)没有顺序限制。
[0118]在本发明中,将热解气体进行初步冷凝后,进行气液分离,分别得到液体油和不可凝燃气。其中,所述不可凝燃气输送至燃烧室(8)中,进行燃烧,为热相分解装置(I)提供热量;所述液体油再进行液液分离,分别得到可回收碳氢化合物和水。其中,所述可回收碳氢化合物进行回收,实现资源的二次利用;得到的水排出处理系统。
[0119]本发明提供了含C3Q+的固体污染物的处理系统、含油污泥的处理系统及方法,所述含油污泥的处理系统包括:用于将含油污泥进行气固分离的热相分解装置,所述热相分解装置设有进料管路和固相出料管路;所述固相出料管路用于排出含C3Q+的固体污染物;用于将含C3O+的固体污染物进行筛分的筛分装置;所述筛分装置与所述固相出料管路相连;与所述筛分装置依次相连的研磨装置、悬浮装置和输送装置;以及与所述输送装置相通的燃烧室,所述燃烧室用于将含C3O+的固体污染物进行燃烧;所述燃烧室设置在热相分解装置周围,用于对所述热相分解装置进行加热。与现有技术相比,本发明实施例提供的含油污泥的处理系统先将含油污泥输送至热相分解装置中,在燃烧室加热的条件下进行热相分解,得到的含C3O+的固体污染物依次经过筛分、研磨、悬浮,再输送至燃烧室进行燃烧,实现含C30+的固体污染物的完全燃尽,解决了其对环境带来的污染问题。实验结果表明,处理后的含C30+的固体污染物呈红色,固体TPH值小于3000mg/kg。
[0120]此外,本发明实施例提供的含油污泥的处理系统能够对热相分解后的热解气体进行逐步分离,得到的不可凝燃气可循环输送至燃烧室进行燃烧,节约能源;得到的液相碳氢化合物进行回收,从而实现资源的二次利用。
[0121]为了进一步说明本发明,下面通过以下实施例进行详细说明。本发明以下实施例所有的含油污泥取自大庆油田含油污泥堆放场。
[0122]实施例1
[0123]在图2所示的本发明实施例提供的含油污泥处理系统中,对含油污泥进行处理。所述含油污泥处理系统的工作过程具体为:
[0124] (I)将6t含油污泥经进料管路(2)输送至热相分解装置(I)中,通过设置在所述热相分解装置(I)周围的燃烧室(8)提供热量,在300°C条件下进行绝氧加热lh,所述含油污泥在热相分解装置(I)中螺旋给进,往复运动,从而在加热过程中实现气固分离,得到含C30+的固体污染物和热解气体。其中,所述含C3Q+的固体污染物经固相出料管路(3)排出,进行进一步处理;所述热解气体经气相出料管路(11)排出,进行进一步处理。
[0125] (2)将经固相出料管路⑶排出的含C3Q+的固体污染物,在筛分装置(4)中,经振动筛进行滤除,再经烘箱进行干燥,得到粒径小于5mm、含水量小于lwt%的含C3O+的固体污染物。再将筛分后的含C3Q+的固体污染物在研磨装置(5)中进行研磨,得到粒径小于Ιμπι的含C30+的固体污染物粉末。然后,将含C3Q+的固体污染物粉末在悬浮装置(6)中与空气充分混合,得到含C3Q+的固体污染物悬浮体。最后,将含C3Q+的固体污染物悬浮体经输送装置(7)的悬浮体输送管路(9),由吹入喷咀(10)进入燃烧室(8),在300°C条件下进行燃烧,完全燃烧后固体呈黑色。
[0126]对燃烧后的固体进行TPH值检测,实验结果表明,固体TPH值为21000mg/kg。
[0127] (3)将经气相出料管路(11)排出的热解气,经冷凝器(18)进行初步冷凝后,进入气液分离装置(12)进行气液分离,分别得到液体油和不可凝燃气。其中,所述不可凝燃气经气相分离管路(13)输送至燃烧室(8)中,进行燃烧,为热相分解装置(I)提供热量;所述液体油经液液分离装置(15)进行液液分离,分别得到可回收碳氢化合物和水。最后,所述可回收碳氢化合物经油相分离管路(17)排出,进行回收,实现资源的二次利用;得到的水经水相分离管路(16)排出。
[0128] 实施例2
[0129]在本发明实施例提供的含油污泥的处理系统中对含油污泥进行处理。所述含油污泥处理系统的工作过程具体为:
[0130] (I)将6t含油污泥经经进料管路(2)输送至热相分解装置(I)中,通过设置在所述热相分解装置(I)周围的燃烧室(8)提供热量,在400°C条件下进行绝氧加热lh,所述含油污泥在热相分解装置(I)中螺旋给进,往复运动,从而在加热过程中实现气固分离,得到含C30+的固体污染物和热解气体。其中,所述含C3Q+的固体污染物经固相出料管路(3)排出,进行进一步处理;所述热解气体经气相出料管路(11)排出,进行进一步处理。
[0131] (2)将经固相出料管路⑶排出的含C3Q+的固体污染物,在筛分装置(4)中,经振动筛进行滤除,再经烘箱进行干燥,得到粒径小于5mm、含水量小于lwt%的含C3O+的固体污染物。再将筛分后的含C3Q+的固体污染物在研磨装置(5)中进行研磨,得到粒径小于Ιμπι的含C30+的固体污染物粉末。然后,将含C3Q+的固体污染物粉末在悬浮装置(6)中与空气充分混合,得到含C3Q+的固体污染物悬浮体。最后,将含C3Q+的固体污染物悬浮体经输送装置(7)的悬浮体输送管路(9),由吹入喷咀(10)进入燃烧室(8),在400°C条件下进行燃烧,完全燃烧后固体呈褐色。
[0132]对燃烧后的固体进行TPH值检测,实验结果表明,固体TPH值为18000mg/kg。
[0133] (3)将经气相出料管路(11)排出的热解气,经冷凝器(18)进行初步冷凝后,进入气液分离装置(12)进行气液分离,分别得到液体油和不可凝燃气。其中,所述不可凝燃气经气相分离管路(13)输送至燃烧室(8)中,进行燃烧,为热相分解装置(I)提供热量;所述液体油经液液分离装置(15)进行液液分离,分别得到可回收碳氢化合物和水。最后,所述可回收碳氢化合物经油相分离管路(17)排出,进行回收,实现资源的二次利用;得到的水经水相分离管路(16)排出。
[0134] 实施例3
[0135]在本发明实施例提供的含油污泥的处理系统中对含油污泥进行处理。所述含油污泥处理系统的工作过程具体为:
[0136] (I)将6t含油污泥经经进料管路(2)输送至热相分解装置(I)中,通过设置在所述热相分解装置(I)周围的燃烧室(8)提供热量,在500°C条件下进行绝氧加热lh,所述含油污泥在热相分解装置(I)中螺旋给进,往复运动,从而在加热过程中实现气固分离,得到含C30+的固体污染物和热解气体。其中,所述含C3Q+的固体污染物经固相出料管路(3)排出,进行进一步处理;所述热解气体经气相出料管路(11)排出,进行进一步处理。
[0137] (2)将经固相出料管路⑶排出的含C3Q+的固体污染物,在筛分装置(4)中,经振动筛进行滤除,再经烘箱进行干燥,得到粒径小于5mm、含水量小于lwt%的含C3O+的固体污染物。再将筛分后的含C3Q+的固体污染物在研磨装置(5)中进行研磨,得到粒径小于Ιμπι的含C30+的固体污染物粉末。然后,将含C3Q+的固体污染物粉末在悬浮装置(6)中与空气充分混合,得到含C3Q+的固体污染物悬浮体。最后,将含C3Q+的固体污染物悬浮体经输送装置(7)的悬浮体输送管路(9),由吹入喷咀(10)进入燃烧室(8),在500°C条件下进行燃烧,完全燃烧后固体呈红色。
[0138]对燃烧后的固体进行TPH值检测,实验结果表明,固体TPH值为2800mg/kg。
[0139] (3)将经气相出料管路(11)排出的热解气,经冷凝器(18)进行初步冷凝后,进入气液分离装置(12)进行气液分离,分别得到液体油和不可凝燃气。其中,所述不可凝燃气经气相分离管路(13)输送至燃烧室(8)中,进行燃烧,为热相分解装置(I)提供热量;所述液体油经液液分离装置(15)进行液液分离,分别得到可回收碳氢化合物和水。最后,所述可回收碳氢化合物经油相分离管路(17)排出,进行回收,实现资源的二次利用;得到的水经水相分离管路(16)排出。
[0140]所公开的实施例的上述说明,使本领域专业技术人员能够实现或使用本发明。对这些实施例的多种修改对本领域的专业技术人员来说将是显而易见的,本文中所定义的一般原理可以在不脱离本发明的精神或范围的情况下,在其它实施例中实现。因此,本发明将不会被限制于本文所示的这些实施例,而是要符合与本文所公开的原理和新颖特点相一致的最宽的范围。
Claims (7)
1.一种含油污泥的处理系统,其特征在于,包括: 用于将含油污泥进行气固分离的热相分解装置,所述热相分解装置设有进料管路和固相出料管路;所述固相出料管路用于排出含C3Q+的固体污染物; 用于将含C3Q+的固体污染物进行筛分的筛分装置;所述筛分装置与所述固相出料管路相连; 与所述筛分装置依次相连的研磨装置、悬浮装置和输送装置; 以及与所述输送装置相通的燃烧室,所述燃烧室用于将含C3Q+的固体污染物进行燃烧; 所述筛分装置包括: 与所述研磨装置依次相连的干燥单元和滤除单元;所述干燥单元所用的具体设备为烘箱; 所述输送装置包括: 与所述悬浮装置相连的多个相互并联的悬浮体输送管路,所述悬浮体输送管路设有吹入喷咀; 所述输送装置通过所述吹入喷咀与所述燃烧室直接相通; 所述燃烧室设置在热相分解装置周围,用于对所述热相分解装置进行加热。
2.根据权利要求1所述的处理系统,其特征在于,还包括: 设置在所述热相分解装置上的气相出料管路,所述气相出料管路用于排出热解气体;与所述气相出料管路相连的气液分离装置,所述气液分离装置设有气相分离管路和液相分离管路;所述气相分离管路与所述燃烧室相通; 与所述液相分离管路相连的液液分离装置,所述液液分离装置设有油相分离管路和水相分离管路。
3.根据权利要求2所述的处理系统,其特征在于,所述气相出料管路上设有冷凝器,用于对进入气液分离装置前的热解气体进行冷却。
4.一种权利要求1〜3任一项所述的含油污泥的处理系统的处理方法,其特征在于,包括以下步骤: a)将含油污泥加热,进行热相分解,得到含C3O+的固体污染物; b)将步骤a)得到的含C3O+的固体污染物依次进行筛分、研磨、悬浮、输送、燃烧。
5.根据权利要求4所述的处理方法,其特征在于,步骤a)中所述热相分解的温度为300Γ〜600Γο
6.根据权利要求4所述的处理方法,其特征在于,所述步骤b)具体包括以下步骤: bl)将含C3O+的固体污染物依次进行滤除、干燥,得到筛分后的含C3O+的固体污染物; b2)将筛分后的含C3O+的固体污染物进行研磨,得到含C3O+的固体污染物粉末; b3)将含C3Q+的固体污染物粉末与空气混合,得到含C3Q+的固体污染物悬浮体; b4)将含C3O+的固体污染物悬浮体输送到燃烧室,进行燃烧。
7.根据权利要求4所述的处理方法,其特征在于,所述步骤a)具体包括:将含油污泥加热,进行热相分解,得到含C3O+的固体污染物和热解气体; 所述处理方法还包括:步骤c)对所述热解气体进行后处理; 所述后处理具体包括以下步骤: Cl)将热解气体进行气液分离,分别得到液体油和不可凝燃气;c2)将步骤Cl)得到的液体油进行液液分离,分别得到水和可回收碳氢化合物;c3)将步骤c I)得到的不可凝燃气通入燃烧室,进行燃烧;所述步骤c2)和步骤c3)没有顺序限制。
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