CN1120519A - 从稀氨水中脱除nh3-n的方法 - Google Patents
从稀氨水中脱除nh3-n的方法 Download PDFInfo
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- CN1120519A CN1120519A CN 95107950 CN95107950A CN1120519A CN 1120519 A CN1120519 A CN 1120519A CN 95107950 CN95107950 CN 95107950 CN 95107950 A CN95107950 A CN 95107950A CN 1120519 A CN1120519 A CN 1120519A
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- ammonia
- ammonium salt
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- ammonium
- dilute
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- 238000000034 method Methods 0.000 title claims abstract description 22
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 115
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 57
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 20
- 238000003795 desorption Methods 0.000 claims abstract description 13
- 238000010521 absorption reaction Methods 0.000 claims description 11
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 10
- 238000004176 ammonification Methods 0.000 claims description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 4
- 239000003929 acidic solution Substances 0.000 claims description 4
- 238000002425 crystallisation Methods 0.000 claims description 4
- 230000008025 crystallization Effects 0.000 claims description 4
- 238000005201 scrubbing Methods 0.000 claims description 3
- RLLPVAHGXHCWKJ-UHFFFAOYSA-N permethrin Chemical compound CC1(C)C(C=C(Cl)Cl)C1C(=O)OCC1=CC=CC(OC=2C=CC=CC=2)=C1 RLLPVAHGXHCWKJ-UHFFFAOYSA-N 0.000 claims 1
- 238000007781 pre-processing Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 claims 1
- 235000011114 ammonium hydroxide Nutrition 0.000 abstract description 12
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 abstract description 10
- 239000002253 acid Substances 0.000 abstract description 7
- 238000005406 washing Methods 0.000 abstract description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 2
- 229920006395 saturated elastomer Polymers 0.000 abstract 1
- 239000003513 alkali Substances 0.000 description 7
- 239000007787 solid Substances 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- HIVLDXAAFGCOFU-UHFFFAOYSA-N ammonium hydrosulfide Chemical compound [NH4+].[SH-] HIVLDXAAFGCOFU-UHFFFAOYSA-N 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 238000003672 processing method Methods 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000009615 deamination Effects 0.000 description 2
- 238000006481 deamination reaction Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
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- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
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Abstract
本发明为一种从稀氨水中脱除NH3-N的方法,用于富氨水、剩余氨水等稀氨水的处理。本方法利用循环空气与经过预处理的稀氨水在解吸塔中进行接触,使氨解吸到循环空气中,含氨的循环空气经稀酸洗涤,氨被酸化学吸收并生成铵盐的酸性溶液,该酸性溶液达到饱和则有铵盐结晶析出,得到铵盐产品。本方法效率高,无污染,投资小,处理成本低。
Description
本发明涉及一种从稀氨水中脱除NH3-N的工艺方法。属于煤化工系统中的煤制气及炼焦化学工业,用于富氨水、剩余氨水等稀氨水的处理。
此前从稀氨水中脱除氨的方法皆系蒸馏法,即稀氨水经热交换、预热等设备被加热至102~105℃后送入分解器,在此分离H2S、CO2、HCN并与部分氨(相当总氨量的10%)一同放散入大气中。分离出部分(30-40%)H2S、CO2、HCN的稀氨水(含氨6g~8g/L)进入蒸馏塔上部,在塔底部通入直接蒸汽,经提馏氨从稀氨水转入蒸汽(含氨6%左右),氨蒸汽经分缩器部分冷凝作为回流液,未冷凝的氨蒸汽在冷凝冷却器中冷凝冷却遂获得18-20%的浓氨水,塔底废水含氨0.05~0.1%。该工艺也有装备固定铵分解设备的,如此可同时脱除固定铵。实践证明,蒸馏法从稀氨水中脱除氨的工艺具有能耗高(处理一吨稀氨水消耗蒸汽0.25吨);污染环境,且产品浓氨水含酸H2S、HCN及有机油类严重超标,在应用中形成新的污染:在生产过程中设备腐蚀严重,维修费用极高;废水中NH3-N含量达1000~2000PPm以上,给后序的生化处理造成困难。
本发明的目的在于提供一种处理稀氨水的工艺方法,以解决上述传统的工艺方法所存在的能耗高、污染环境、设备腐蚀以及NH3-N脱除效率低等一系列问题,并为蒸氨废水的生化处理创造条件。本发明的工艺流程紧凑,易于控制几乎不消耗或很少消耗蒸汽,效率高,无污染,腐蚀程序也大大降低。
本发明是这样实现的:利用循环空气与经过预处理的稀氨水在解吸塔中进行接触,从而使氨解吸到循环空气中(其浓度远低于爆炸下限),含氨的循环空气经稀酸洗涤,氨遂被酸化学吸收并生成铵盐的酸性溶液,该酸性溶液达过饱和后则有铵盐结晶析出,从而获得铵盐产品(如硫铵等)。本发明方法包括:1.稀氨水的预处理:澄清、过滤除去悬浮物及有机油类(<10PPm);加碱分解其中所含的固定铵盐,降低稀氨水中固定铵盐含量,同时增大氨蒸汽分压,提高解吸效率。2.用循环空气在解吸塔中从预处理后的稀氨水中解吸氨(NH3-N)。3.利用硫酸化学吸收循环空气中的氨,脱氨后的空气重复送入洗涤塔反复应用。
下面结合附图对本发明的方法进行详细描述:
图1是本发明方法的工艺流程图。
图中:1-稀氨水槽; 2-砂石过滤器; 3-压力反应器;
4-沉淀器; 5-中间槽; 6、11-泵;
7-解吸塔; 8-风机; 9-氨化学吸收塔;
10-旋分器; 12-循环母液槽。
稀氨水在45~55℃,含氨6~8g/L)从稀氨水槽1中用泵6,送入砂石过滤器2中,在砂石过滤器2中滤去稀氨水中的悬浮物和焦油等物质;然后在压力反应器3(沿力可为5~6kg)中加入碱,碱为纯碱或苛性碱(火碱),加入的碱与稀氨水中的固定铵盐(氯化按、硫酸铵)作用,使固定铵盐分解,同时增大氨蒸汽分压,于是氨由离子状态转变为分子状态,稀氨水由压力反应器3经沉淀池4到中间槽5,在中间槽5中减压,压力减至1个大气压左右,稀氨水中的氨在减压后从稀氨水中逸出。用泵6引进解吸塔7上部,在解吸塔7内氨进入循环空气中,循环空气一般为惰性气体,并被循环空气载至氨化学吸收塔9,在氨化学吸收塔9中氨被浓度为5~10%的硫酸吸收并生成铵盐(如硫铵等),该酸性溶液达到饱和后则有铵盐析出,即含氨的空气在氨化学吸收塔9中,通过喷洒硫酸溶液,从氨与硫酸的反应中生成硫酸铵(或其它铵盐),该铵盐溶液或单独结晶生产固体铵盐或在焦化厂硫铵系统中结晶均可。为了肪止从氨化学吸收塔9中引出的循环空气挟带致雾,在氨化学吸收塔9出口处没有旋分扑酸器10图中风机8为循环空气动力。脱氨后的空气重复送入洗涤塔反复使用。
本实施例:含NH3-N3000~10000PPm的稀氨水在释氨水槽1中澄清后用泵6抽送至砂石过滤器2,经过滤,油类含量降至10~30mg/L,然后在压力反应器3中加碱分解稀氨水中的固定铵,加碱量随固定铵盐含量而定,为了防止水中沉淀物堵塞解吸塔中的填料,用沉淀器4除去悬浮物,而后到中间槽5用泵6把稀氨水送至解吸塔7的上部,经喷淋均匀地分布在填料表面,空气被用风机8由解吸塔7抽出,分别经氨化学吸收塔9用浓度为5~10%的H2SO4吸收氨后进入旋分器10脱除酸雾,返回解吸塔下部。循环空气出解吸塔的NH3浓度为3000~6000mg/m3,进解吸塔的NH3-N浓度为10~30mg/m3。废水由解吸塔7下部排入生化水处理。
本发明的从稀氨水中脱除NH3-N的方法可以将废水NH3-N含量降至200~300PPm%以下,并可同时获得铵盐产品。本发明方法工艺紧凑,节能,无污染,节约投资处理成本低,尤其适合于中、小型焦化厂,城市煤气厂作为富氨水、剩余氨水待稀氨水的处理方法。
Claims (3)
1.一种从稀氨水中脱除NH3-N的方法,其特征在于利用循环空气与经过预处理的稀氨水在解吸塔中进行接触,使氨解吸到循环空气中,含氨的循环空气经硫酸洗涤,氨被酸化学吸收并生成铵盐的酸性溶液,该酸性溶液达到饱和后则有铵盐结晶析出,从而获得铵盐产品。
2.如权利要求1所述的方法,其特征在于在氨化学吸收塔出口处设有旋分扑酸器(10)。
3.如权利要求1、2所述的方法,其特征在于在稀氨水预处理过程中的压力反应器(3)和沉淀器(4)用来分解固定铵和净化稀铵水。
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CN95107950A CN1039636C (zh) | 1995-08-03 | 1995-08-03 | 从稀氨水中脱除nh3-n的方法 |
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CN95107950A CN1039636C (zh) | 1995-08-03 | 1995-08-03 | 从稀氨水中脱除nh3-n的方法 |
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CN1120519A true CN1120519A (zh) | 1996-04-17 |
CN1039636C CN1039636C (zh) | 1998-09-02 |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001012548A1 (en) * | 1999-08-11 | 2001-02-22 | Hadwaco Ltd Oy | Method for the evaporation of an aqueous solution containing ammonia |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3408157A (en) * | 1966-06-01 | 1968-10-29 | Standard Oil Co | Process for recovery of ammonium salts from process waste streams and disposal thereof |
DE2527985C3 (de) * | 1975-06-24 | 1981-04-16 | Metallgesellschaft Ag, 6000 Frankfurt | Kontinuierliches Verfahren zur Gewinnung von reinem Ammoniak |
CN1036062C (zh) * | 1994-08-03 | 1997-10-08 | 唐山钢铁(集团)公司 | 利用剩余氨水生产硫铵的工艺 |
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1995
- 1995-08-03 CN CN95107950A patent/CN1039636C/zh not_active Expired - Fee Related
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001012548A1 (en) * | 1999-08-11 | 2001-02-22 | Hadwaco Ltd Oy | Method for the evaporation of an aqueous solution containing ammonia |
US6638398B1 (en) | 1999-08-11 | 2003-10-28 | Hadwaco Ltd Oy | Methods for the evaporation of an aqueous solution containing ammonia |
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CN1039636C (zh) | 1998-09-02 |
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