CN102010082B - 废稀硫酸回收利用处理方法 - Google Patents
废稀硫酸回收利用处理方法 Download PDFInfo
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- CN102010082B CN102010082B CN 201010500297 CN201010500297A CN102010082B CN 102010082 B CN102010082 B CN 102010082B CN 201010500297 CN201010500297 CN 201010500297 CN 201010500297 A CN201010500297 A CN 201010500297A CN 102010082 B CN102010082 B CN 102010082B
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- diluted acid
- acid water
- acid
- dilute acid
- tank
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 33
- 238000004064 recycling Methods 0.000 title claims abstract description 10
- 239000002699 waste materials Substances 0.000 title abstract 3
- 239000002253 acids Substances 0.000 claims abstract description 96
- 229920005989 resins Polymers 0.000 claims abstract description 15
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- 238000001914 filtration Methods 0.000 claims abstract description 13
- 150000002500 ions Chemical class 0.000 claims abstract description 10
- 238000003860 storage Methods 0.000 claims abstract description 8
- 229910001385 heavy metals Inorganic materials 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 22
- 235000011149 sulphuric acid Nutrition 0.000 claims description 15
- 239000001117 sulphuric acid Substances 0.000 claims description 15
- 239000006260 foam Substances 0.000 claims description 13
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- 238000005201 scrubbing Methods 0.000 claims description 4
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound 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N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 3
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 3
- 238000010790 dilution Methods 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 239000003595 mist Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
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- UGFAIRIUMAVXCW-UHFFFAOYSA-N carbon monoxide Chemical compound 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Abstract
本发明涉及一种废稀硫酸回收利用处理方法,包括以下步骤,1)将炉气先经过文氏管,同时通过压力泵将稀酸水槽内的稀酸水压入文氏管进行管内喷洒,出理后的炉气再经过泡沫塔,同时通过压力泵将稀酸水槽内的稀酸水压入泡沫塔进行塔内喷洒;2)通过压力泵将步骤1)处理后稀酸水槽内的稀酸清水压入微孔过滤器中,经过过滤后到达稀酸水储槽;3)将大孔胺基膦酸螯合树脂放入步骤2)中稀酸水储槽在常温下混合振荡30min,充分对稀酸水中的重金属离子进行吸附。本发明的有益效果为:采用微孔过滤器对稀酸水过滤,保证过滤出的稀酸水中不含任何的固体杂质;通过树脂吸附法去除溶液中的杂质离子,提高了硫酸产品的透光率、透明度。
Description
废稀硫酸回收利用处理方法
技术领域
[0001] 本发明涉及化工领域,尤其涉及一种废稀硫酸回收利用处理方法。
背景技术
[0002] 硫酸厂拥有两套制酸系统,设计年生产能力分别为四万吨和六万吨,两套装置的炉气净化均采用内喷文氏管-泡沫塔(循环稀酸用板式换热器冷却)_电除雾器的封闭稀酸洗净化流程。采用酸洗流程,为企业减少了大量的清水消耗和处理稀酸所用的石灰或电石渣,酸洗净化流程使用后,清水消耗减少到20〜40m3/h,但到夏季时清水消耗量仍较高约60m3/h。目前硫酸生产过程中,净化岗位产生的稀硫酸,用电石渣中和后排放。排放的硫酸既浪费了资源,也消耗了电石洛,成本高,污水排放量大,不符合国家节能减排的政策要求,因此充分利用好稀硫酸,具有重大意义。
[0003] 国内硫酸行业曾经有过研究,但在工业上没有应用,国外硫酸企业有的利用废稀硫酸生产磷肥,但利用方法对本处理方法没有借鉴意义。
[0004] 由于目前采用的CN过滤器或斜管沉降器为一级过滤设备,过滤的酸渣为相对较粗颗粒的。经过日常的生产观察,经过一级过滤设备过滤后,稀酸水槽内仍有粒径更细的酸渣在稀酸中,因此用微孔过滤器进行二级过滤,使粒径约为400目(I目=IO-3 μ m)的酸渣全部过滤出稀酸水,这样才能保证过滤出的稀酸水中不含任何的固体杂质。主要流程简述为:通过加压泵将稀酸槽内的水打入微孔过滤器,稀酸水经过过滤后溶液中的固体杂质被除去,后一步再通过树脂吸附法去除溶液中的杂质离子。从而保证过滤后的稀硫酸能直接加入到干吸岗位的循环槽中,不 至于降低硫酸产品的透光率、透明度。
发明内容
[0005] 本发明的目的是提供一种废稀硫酸回收利用处理方法,其实现了低成本处理硫酸废水,同时避免了对环境的二次污染。
[0006] 本发明的目的是通过以下技术方案来实现:
[0007] —种废稀硫酸回收利用处理方法,其包括以下步骤:
[0008] I)酸洗净化:将炉气先经过文氏管,同时通过压力泵将稀酸水槽内的稀酸水压入文氏管进行管内喷洒,除去矿尘以及杂质,出理后的炉气再经过泡沫塔,同时通过压力泵将稀酸水槽内的稀酸水压入泡沫塔进行塔内喷洒,进一步除去矿尘以及杂质,处理后的炉气最后进入电除雾器去掉炉气中所含的酸雾;
[0009] 2)将在文氏管和泡沫塔中反应后的稀酸水汇合自流至脱吸塔,脱吸后的稀酸水自流至原水槽中,再通过压力泵将稀酸水从原水槽压入CN过滤器进行固液分离,分离出的酸渣从底部流入酸渣回收桶内,分离出的稀酸清水自流至稀酸水槽内;
[0010] 3)微孔过滤稀酸:通过压力泵将步骤2)处理后稀酸水槽内的稀酸清水压入微孔过滤器中,经过过滤后送入稀酸水储槽;
[0011] 4)树脂吸附法去除杂质离子:将大孔胺基膦酸螯合树脂放入步骤3)中稀酸水储槽中,在常温下混合振荡30min,充分对稀酸水中的重金属离子进行吸附;
[0012] 5)回收利用:将步骤4)树脂吸附后的稀酸水通过压力泵压入干吸岗位回收利用,或作为原料生产硫酸铵。
[0013] 在步骤I)中的文氏管中喷洒所用稀酸水为质量浓度12〜18%的硫酸,温度为35〜45°C。在步骤I)中的稀酸水在压入泡沫塔的过程中被流量20〜40m3/h的清水稀释为2〜5%的硫酸,温度为30〜40°C。在步骤3)中的微孔过滤器的滤膜孔径为0.2〜lum。在步骤4)中每Iml稀酸水中投放0.4g树脂。
[0014] 本发明的有益效果为:
[0015] 1、采用的CN过滤器或斜管沉降器为一级过滤设备,过滤的酸渣为相对较粗颗粒的,再用微孔过滤 器进行二级过滤,使粒径约为400目的酸渣全部过滤出稀酸水,这样才能保证过滤出的稀酸水中不含任何的固体杂质;
[0016] 2、通过树脂吸附法去除溶液中的杂质离子,从而保证过滤后的稀硫酸能直接加入到干吸岗位的循环槽中,不至于降低硫酸产品的透光率、透明度。
附图说明
[0017] 下面根据附图对本实用新型作进一步详细说明。
[0018] 图1是本发明实施例所述的废稀硫酸回收利用处理方法的工艺流程图;
[0019] 图2是微孔过滤工艺流程图。
具体实施方式
[0020] 如图1〜2所示,本发明实施例所述的一种废稀硫酸回收利用处理方法,其包括以下步骤:
[0021] I)酸洗净化:将炉气先经过文氏管,同时通过压力泵将稀酸水槽内的稀酸水压入文氏管进行管内喷洒,除去矿尘以及杂质,出理后的炉气再经过泡沫塔,同时通过压力泵将稀酸水槽内的稀酸水压入泡沫塔进行塔内喷洒,进一步除去矿尘以及杂质,处理后的炉气最后进入电除雾器去掉炉气中所含的酸雾;
[0022] 2)将在文氏管和泡沫塔中反应后的稀酸水汇合自流至脱吸塔,脱吸后的稀酸水自流至原水槽中,再通过压力泵将稀酸水从原水槽压入CN过滤器进行固液分离,分离出的酸渣从底部流入酸渣回收桶内,分离出的稀酸清水自流至稀酸水槽内;
[0023] 3)微孔过滤稀酸:通过压力泵将步骤2)处理后稀酸水槽内的稀酸清水压入微孔过滤器中,经过过滤后送入稀酸水储槽;
[0024] 4)树脂吸附法去除杂质离子:将大孔胺基膦酸螯合树脂放入步骤3)中稀酸水储槽中,在常温下混合振荡30min,充分对稀酸水中的重金属离子进行吸附;
[0025] 5)回收利用:将步骤4)树脂吸附后的稀酸水通过压力泵压入干吸岗位回收利用,或作为原料生产硫酸铵。
[0026] 在步骤I)中的文氏管中喷洒所用稀酸水为12〜18%的硫酸,温度为35〜45°C。在步骤I)中的稀酸水在压入泡沫塔的过程中被流量20〜40m3/h的清水稀释为2〜5%的硫酸,温度为30〜40°C。在步骤3)中的微孔过滤器的滤膜孔径为0.2〜lum。在步骤4)中每Iml稀酸水中投放0.4g树脂。[0027] 本发明在硫酸厂的废稀酸回收利用中带来以下效益:
[0028] 1、经济效益
[0029] (I)回收 100%硫酸:16200X4%= 648 吨;
[0030] 648 吨 X 300 元 / 吨=19.44 万元。
[0031] (2)减少干吸岗位清水补加水成本:16200吨X 3.1元/吨=5.02万元。
[0032] (3)减少电石渣使用成本:489X 120元/吨=5.87万元。
[0033]则年效益合计为 19.44+5.02+5.87 = 30.33 万元。
[0034] 2、社会效益
[0035] 由于回收了废稀·硫酸,从而减少了污水的排放,符合环保要求。
Claims (1)
1.一种废稀硫酸回收利用处理方法,其特征在于,所述方法包括以下步骤:1)酸洗净化,将炉气先经过文氏管,同时通过压力泵将稀酸水槽内的稀酸水压入文氏管进行管内喷洒,除去矿尘以及杂质,处理后的炉气再经过泡沫塔,同时通过压力泵将稀酸水槽内的稀酸水压入泡沫塔进行塔内喷洒,进一步除去矿尘以及杂质,处理后的炉气最后进入电除雾器去掉炉气中所含的酸雾;所述步骤I)中的文氏管中喷洒所用稀酸水为质量百分比12-18%的硫酸,温度为35-45°C ; 所述的稀酸水压入泡沫塔的过程中被流量20-40m3/h的清水稀释为质量百分比2-5%的硫酸,温度为30-40°C ; 2)将在文氏管和泡沫塔中反应后的稀酸水汇合自流至脱吸塔,脱吸后的稀酸水自流至原水槽中,再通过压力泵将稀酸水从原水槽压入CN过滤器进行固液分离,分离出的酸渣从底部流入酸渣回收桶内,分离出的稀酸清水自流至稀酸水槽内; 3)微孔过滤稀酸:通过压力泵将步骤2)处理后稀酸水槽内的稀酸清水压入微孔过滤器中,经过过滤后送入稀酸水储槽;微孔过滤器的滤膜孔径为0.2-lum ; 4)树脂吸附法除去杂质离子:将大孔胺基膦酸螯合树脂放入步骤3)中稀酸水储槽中,在常温下混合震荡30min,充分对稀酸水中的重金属离子进行吸附,每Iml稀酸水中投放·0.4g树脂; ·5)回收利用;将步骤4)树脂吸收后的稀酸水通过压力泵压入干吸岗位回收利用,或作为原料生产硫酸铵。
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