CN106621796B - Method and device for simultaneously removing carbonyl sulfide and carbon disulfide - Google Patents
Method and device for simultaneously removing carbonyl sulfide and carbon disulfide Download PDFInfo
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- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 47
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 126
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000003054 catalyst Substances 0.000 claims abstract description 55
- 239000007921 spray Substances 0.000 claims abstract description 40
- 238000001816 cooling Methods 0.000 claims abstract description 38
- 238000011069 regeneration method Methods 0.000 claims abstract description 34
- 230000008929 regeneration Effects 0.000 claims abstract description 33
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 27
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 21
- 239000003546 flue gas Substances 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 20
- 229910052717 sulfur Inorganic materials 0.000 claims description 20
- 239000011593 sulfur Substances 0.000 claims description 20
- 239000002826 coolant Substances 0.000 claims description 16
- 230000003197 catalytic effect Effects 0.000 claims description 15
- 238000006460 hydrolysis reaction Methods 0.000 claims description 15
- 239000002918 waste heat Substances 0.000 claims description 12
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 10
- 230000007062 hydrolysis Effects 0.000 claims description 9
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 5
- 238000005406 washing Methods 0.000 claims description 5
- 239000000110 cooling liquid Substances 0.000 claims description 4
- 238000005507 spraying Methods 0.000 claims description 4
- 238000011010 flushing procedure Methods 0.000 claims description 3
- 238000006477 desulfuration reaction Methods 0.000 abstract description 20
- 230000023556 desulfurization Effects 0.000 abstract description 20
- 230000010354 integration Effects 0.000 abstract description 4
- 238000000605 extraction Methods 0.000 abstract description 2
- 238000006555 catalytic reaction Methods 0.000 abstract 2
- 239000007791 liquid phase Substances 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 6
- 239000000428 dust Substances 0.000 description 5
- VCJMYUPGQJHHFU-UHFFFAOYSA-N iron(3+);trinitrate Chemical compound [Fe+3].[O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O VCJMYUPGQJHHFU-UHFFFAOYSA-N 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical class [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- QGJOPFRUJISHPQ-NJFSPNSNSA-N carbon disulfide-14c Chemical compound S=[14C]=S QGJOPFRUJISHPQ-NJFSPNSNSA-N 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 238000009776 industrial production Methods 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- XTVVROIMIGLXTD-UHFFFAOYSA-N copper(II) nitrate Chemical compound [Cu+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O XTVVROIMIGLXTD-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 125000001741 organic sulfur group Chemical group 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- BNGXYYYYKUGPPF-UHFFFAOYSA-M (3-methylphenyl)methyl-triphenylphosphanium;chloride Chemical compound [Cl-].CC1=CC=CC(C[P+](C=2C=CC=CC=2)(C=2C=CC=CC=2)C=2C=CC=CC=2)=C1 BNGXYYYYKUGPPF-UHFFFAOYSA-M 0.000 description 1
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 1
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical class [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- OBSZRRSYVTXPNB-UHFFFAOYSA-N tetraphosphorus Chemical compound P12P3P1P32 OBSZRRSYVTXPNB-UHFFFAOYSA-N 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2255/00—Catalysts
- B01D2255/80—Type of catalytic reaction
- B01D2255/808—Hydrolytic
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/308—Carbonoxysulfide COS
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
本发明公开了一种同时脱除羰基硫、二硫化碳的方法及装置，脱硫装置包括由冷却塔和固定床反应塔组成的换热系统，由汽提塔、喷淋塔和连通管组成的助催化系统，由两个固定床反应塔组成的连续运行系统，由换热系统和再生喷淋系统组成的催化剂再生系统等组成。该方法具有高效的脱硫效率，高温烟气的热量能够得到很好地利用，产物稀硫酸的回用提高了催化反应效率，双反应塔分别处在催化反应和催化剂再生的阶段，通过电磁阀的定时切换能够保证系统的连续运行，同时再生过程能够将失活催化剂表面的单质硫转移到液相中，便于后续过程中单质硫的提取，该装置具有高集成度和自动化程度。
The invention discloses a method and device for simultaneously removing carbonyl sulfide and carbon disulfide. The desulfurization device includes a heat exchange system composed of a cooling tower and a fixed-bed reaction tower, and a catalyst-promoting system composed of a stripping tower, a spray tower and a connecting pipe. The system is a continuous operation system composed of two fixed-bed reaction towers, a catalyst regeneration system composed of a heat exchange system and a regeneration spray system, etc. The method has high desulfurization efficiency, the heat of high-temperature flue gas can be well utilized, and the reuse of the product dilute sulfuric acid improves the efficiency of the catalytic reaction. The double reaction towers are in the stages of catalytic reaction and catalyst regeneration respectively. Timing switching can ensure the continuous operation of the system, and at the same time, the regeneration process can transfer the elemental sulfur on the surface of the deactivated catalyst to the liquid phase, which is convenient for the extraction of elemental sulfur in the subsequent process. The device has a high degree of integration and automation.
Description
技术领域Technical Field
本发明涉及一种同时脱除羰基硫、二硫化碳的方法及装置，属于大气污染控制领域。The invention relates to a method and a device for simultaneously removing carbonyl sulfide and carbon disulfide, belonging to the field of air pollution control.
背景技术Background Art
作为主要的有机硫，COS、CS2广泛存在于工业烟气中，例如黄磷尾气、高炉尾气等。在工业生产和使用过程中排放到大气环境，会对环境和人体造成严重的污染和危害，工业生产中微量的CS2和COS对催化剂有毒害作用，使其催化效果和使用寿命受到严重的影响，CS2和COS还会通过缓慢的水解反应生成H2S，腐蚀生产设备，不仅给工业生产带来了很大的经济损失，而且增加了设备投资和产品成本，同时COS和CS2的排放也是对硫资源的浪费。As the main organic sulfur, COS and CS2 are widely present in industrial flue gas, such as yellow phosphorus tail gas, blast furnace tail gas, etc. They are discharged into the atmosphere during industrial production and use, causing serious pollution and harm to the environment and human body. Trace amounts of CS2 and COS in industrial production are toxic to catalysts, seriously affecting their catalytic effect and service life. CS2 and COS will also generate H2S through slow hydrolysis reaction, corroding production equipment, which not only brings great economic losses to industrial production, but also increases equipment investment and product costs. At the same time, the emission of COS and CS2 is also a waste of sulfur resources.
催化水解法脱除COS和CS2的原理是：COS和CS2在催化剂上与水蒸气反应转化成H2S，然后H2S在后续工段上被脱除，催化水解的反应温度一般低于200℃，并且能耗较低，副反应较少，且大部分原料气中含有水解过程所需的水蒸气。与此同时，低温催化水解COS和CS2的过程可避免原料气裂解、甲烷化等副反应的发生，所以该法成为目前脱除COS和CS2研究领域中的热点之一。The principle of removing COS and CS2 by catalytic hydrolysis is: COS and CS2 react with water vapor on the catalyst to convert into H2S , and then H2S is removed in the subsequent process. The reaction temperature of catalytic hydrolysis is generally lower than 200℃, and the energy consumption is low, the side reactions are few, and most of the raw gas contains water vapor required for the hydrolysis process. At the same time, the low-temperature catalytic hydrolysis of COS and CS2 can avoid the occurrence of side reactions such as cracking and methanation of the raw gas, so this method has become one of the hot spots in the current research field of removing COS and CS2 .
中国专利CN 102886203A公开了“一种烟气脱硫脱汞的方法”的发明。该发明将含氯离子的水喷入循环流化床干法脱硫脱汞除尘装置中，再对烟气进行净化。该方法具有较高的脱硫效率，但是脱除的含硫化合物为SO2，且无催化剂再生工序。中国专利CN103432861A公开了“烧结脱硫除白烟系统及其工艺流程”的发明。该发明按照脱硫、除水、降温的顺序对白烟进行净化。该方法具有较高的脱硫效率和较低的能耗，但是脱除的含硫化合物为SO2，且无催化剂再生工序。中国专利CN 103657368A公开了“一种同时脱硫脱硝脱汞干法烟气净化方法及装置”的发明。该发明采用吸附的方式脱除SO2、还原的方式脱除NOx、氧化的方式脱除Hg。该方法具有较高的脱硫脱硝脱汞效率，但是脱除的含硫化合物为SO2，且无催化剂再生工序。本发明所涉及的同时脱除羰基硫、二硫化碳的方法及装置具有高效的脱硫效率，且自动化程度高、集成度高、可连续运行、热量利用率高、硫回收方便。Chinese patent CN 102886203A discloses the invention of "a method for flue gas desulfurization and demercuration". The invention sprays water containing chloride ions into a circulating fluidized bed dry desulfurization, demercuration and dust removal device, and then purifies the flue gas. The method has a high desulfurization efficiency, but the sulfur-containing compound removed is SO 2 , and there is no catalyst regeneration process. Chinese patent CN103432861A discloses the invention of "a sintering desulfurization and white smoke removal system and its process flow". The invention purifies white smoke in the order of desulfurization, dehydration and cooling. The method has a high desulfurization efficiency and low energy consumption, but the sulfur-containing compound removed is SO 2 , and there is no catalyst regeneration process. Chinese patent CN 103657368A discloses the invention of "a dry flue gas purification method and device for simultaneous desulfurization, denitrification and demercuration". The invention removes SO 2 by adsorption, removes NOx by reduction, and removes Hg by oxidation. The method has high desulfurization, denitrification and mercury removal efficiency, but the sulfur-containing compound removed is SO 2 and there is no catalyst regeneration process. The method and device for simultaneously removing carbonyl sulfide and carbon disulfide of the present invention have high desulfurization efficiency, high automation, high integration, continuous operation, high heat utilization rate and convenient sulfur recovery.
目前，关于用稀硫酸增强同时脱除羰基硫、二硫化碳的方法及装置未见到报道。At present, there is no report on a method and apparatus for enhancing the simultaneous removal of carbonyl sulfide and carbon disulfide using dilute sulfuric acid.
发明内容Summary of the invention
本发明的目的在于提供一种同时脱除羰基硫、二硫化碳的方法，该方法不仅具有高效的脱硫效率，且自动化程度高、集成度高、可连续运行、热量利用率高、硫回收方便，能有效解决有机硫净化的问题，具体步骤如下：The object of the present invention is to provide a method for simultaneously removing carbonyl sulfide and carbon disulfide, which method not only has high desulfurization efficiency, but also has high automation, high integration, continuous operation, high heat utilization rate, and convenient sulfur recovery, and can effectively solve the problem of organic sulfur purification. The specific steps are as follows:
（1）经过预除尘处理后的高温烟气先通过余热锅炉降温至150~200℃，再通过冷却塔进行热交换，使烟气温度降至60~100℃，冷却液升高至60~100℃。(1) After pre-dust removal, the high-temperature flue gas is first cooled to 150~200℃ by the waste heat boiler, and then heat exchanged by the cooling tower to reduce the flue gas temperature to 60~100℃ and raise the coolant temperature to 60~100℃.
（2）经过降温后的气体再通过汽提塔的作用，将汽提塔中的稀硫酸带入固定床反应塔中。(2) The cooled gas then passes through the stripping tower, bringing the dilute sulfuric acid in the stripping tower into the fixed bed reaction tower.
（3）步骤（1）中吸收热量并升温后的冷却液流入固定床反应塔换热夹套中，将反应塔内催化剂的温度提高到60~100℃。(3) The cooling liquid that has absorbed heat and heated up in step (1) flows into the heat exchange jacket of the fixed bed reaction tower, raising the temperature of the catalyst in the reaction tower to 60-100°C.
（4）夹带稀硫酸的气体在固定床反应塔内发生催化水解反应（产生H2S、SO2等产物）。(4) The gas carrying dilute sulfuric acid undergoes a catalytic hydrolysis reaction in the fixed bed reaction tower (producing H2S , SO2 and other products).
（5）产生的SO2随气流进入喷淋塔产生硫酸、亚硫酸，硫酸和亚硫酸经过连通管回流至汽提塔，净化后的气体从出口排出。(5) The generated SO2 enters the spray tower with the air flow to produce sulfuric acid and sulfurous acid. The sulfuric acid and sulfurous acid flow back to the stripping tower through the connecting pipe, and the purified gas is discharged from the outlet.
（6）冷却液在固定床反应塔夹套中放热后重新进入冷却塔循环使用。(6) After releasing heat in the jacket of the fixed bed reactor, the coolant re-enters the cooling tower for recycling.
（7）再生用水流入固定床反应塔冲洗失活催化剂，将催化剂表面的硫酸盐和单质硫带出进入硫磺回收工序，经过水洗后的催化剂在夹套的加热作用下快速烘干，形成再生催化剂。(7) The regeneration water flows into the fixed bed reaction tower to wash the deactivated catalyst, and the sulfate and elemental sulfur on the catalyst surface are taken out and enter the sulfur recovery process. The catalyst after water washing is quickly dried under the heating action of the jacket to form a regenerated catalyst.
本发明所述汽提塔和喷淋塔中稀硫酸摩尔浓度为0.01~0.1mol/L。The molar concentration of dilute sulfuric acid in the stripping tower and the spray tower of the present invention is 0.01-0.1 mol/L.
本发明所述冷却液为乙醇和水的混合液，乙醇与水的摩尔比为0.5~20:1。The coolant of the present invention is a mixture of ethanol and water, and the molar ratio of ethanol to water is 0.5-20:1.
本发明所述固定床反应塔内的催化剂为水解催化剂，例如：改性活性炭催化剂、改性类水滑石催化剂、改性氧化铝催化剂、改性分子筛催化剂、改性金属氧化物催化剂等。The catalyst in the fixed bed reaction tower of the present invention is a hydrolysis catalyst, for example: a modified activated carbon catalyst, a modified hydrotalcite-like catalyst, a modified alumina catalyst, a modified molecular sieve catalyst, a modified metal oxide catalyst, and the like.
本发明的另一目的在于提供一种同时脱除羰基硫、二硫化碳的装置，包括余热锅炉1、冷却塔2、汽提塔3、固定床反应塔Ⅰ4、固定床反应塔Ⅱ5、喷淋塔6、换热泵Ⅰ7、换热泵Ⅱ8、再生泵9、喷淋泵10、连通管11、搅拌器12、换热夹套13；余热锅炉1与冷却塔2连通，冷却塔2与汽提塔3连通；汽提塔3通过三通电磁阀分别与固定床反应塔Ⅰ4和固定床反应塔Ⅱ5连通；固定床反应塔Ⅰ4和固定床反应塔Ⅱ5通过三通电磁阀与喷淋塔6连通；汽提塔3和喷淋塔6的下端通过连通管11连通，喷淋塔6的下端通过喷淋泵10与喷淋塔6的顶端连通；冷却塔2、固定床反应塔Ⅰ4、固定床反应塔Ⅱ5的内壁均设有换热夹套13；再生水箱通过再生泵9与固定床反应塔Ⅰ4和固定床反应塔Ⅱ5的顶端连通，固定床反应塔Ⅰ4和固定床反应塔Ⅱ5底部与硫磺回收装置连通；换热泵Ⅱ8的出口与冷却塔2内部换热夹套的顶部连通，冷却塔2内部换热夹套的底部通过换热泵Ⅰ7分别与固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内部换热夹套的顶部连通，固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内部换热夹套的底部通过三通电磁阀与换热泵Ⅱ8的入口连通。Another object of the present invention is to provide a device for simultaneously removing carbonyl sulfide and carbon disulfide, comprising a waste heat boiler 1, a cooling tower 2, a stripping tower 3, a fixed bed reaction tower I4, a fixed bed reaction tower II5, a spray tower 6, a heat exchange pump I7, a heat exchange pump II8, a regeneration pump 9, a
本发明所述汽提塔3和喷淋塔6的底部均设置搅拌器12。The bottoms of the stripping tower 3 and the spray tower 6 of the present invention are both provided with a stirrer 12 .
本发明所述固定床反应塔Ⅰ4、固定床反应塔Ⅱ5的内部设置再生冲洗装置，底部设置储液槽。The fixed bed reaction tower I4 and the fixed bed reaction tower II5 of the present invention are provided with a regeneration and flushing device inside and a liquid storage tank at the bottom.
本发明的原理为：采用水解催化剂，借助烟气中微量水蒸气和O2，使COS、CS2同时催化水解为H2S，有氧条件下产生的副产物SO2在喷淋工序中继续氧化为硫酸，产生的稀硫酸随气流进入催化工序，从而增强脱硫效率，脱硫反应温度为：60~100℃，COS和CS2脱除效率高于90%，主要反应如下：The principle of the present invention is: using a hydrolysis catalyst, with the help of trace water vapor and O2 in the flue gas, COS and CS2 are simultaneously catalytically hydrolyzed into H2S . The byproduct SO2 produced under aerobic conditions continues to be oxidized into sulfuric acid in the spraying process, and the generated dilute sulfuric acid enters the catalytic process with the air flow, thereby enhancing the desulfurization efficiency. The desulfurization reaction temperature is: 60~100℃, and the COS and CS2 removal efficiency is higher than 90%. The main reactions are as follows:
本发明方法的优点和技术效果：Advantages and technical effects of the method of the present invention:
（1）由冷却塔和固定床反应塔组成的换热系统，高效地利用了烟气自身的温度，不需额外热源即可使催化剂达到适宜反应温度；(1) The heat exchange system consisting of a cooling tower and a fixed bed reaction tower efficiently utilizes the temperature of the flue gas itself, allowing the catalyst to reach a suitable reaction temperature without the need for an additional heat source;
（2）由汽提塔、喷淋塔和连通管组成的助催化系统，能够将副产物SO2再利用，产生的稀硫酸能够对催化水解过程起到增强的作用；(2) The catalyst-promoting system consisting of a stripping tower, a spray tower and a connecting pipe can reuse the by-product SO2 , and the generated dilute sulfuric acid can enhance the catalytic hydrolysis process;
（3）由换热系统和再生喷淋系统组成的催化剂再生系统，能够利用换热系统提供的热量对催化剂进行快速烘干，提高了热量的利用效率，再生过后产生的废液中含有的硫磺能够得到再次利用；(3) The catalyst regeneration system, which consists of a heat exchange system and a regeneration spray system, can use the heat provided by the heat exchange system to quickly dry the catalyst, thereby improving the heat utilization efficiency. The sulfur contained in the waste liquid generated after regeneration can be reused;
（4）喷淋塔和汽提塔底部的搅拌器用于调节储液槽内和储液槽之间的稀硫酸浓度平衡。(4) The agitators at the bottom of the spray tower and the stripping tower are used to adjust the concentration balance of dilute sulfuric acid in and between the storage tanks.
（5）由两个固定床反应塔组成的连续运行系统，能够利用同一套换热装置和再生装置进行催化和再生过程，可定时切换的特性，使反应系统可以连续工作，且自动化程度高、集成度高。(5) The continuously operating system consisting of two fixed-bed reaction towers can use the same set of heat exchange devices and regeneration devices to carry out the catalytic and regeneration processes. The timed switching feature enables the reaction system to work continuously with a high degree of automation and integration.
附图说明BRIEF DESCRIPTION OF THE DRAWINGS
图1为本发明所述装置的结构示意图；FIG1 is a schematic diagram of the structure of the device of the present invention;
图2为本发明工艺流程图。FIG. 2 is a process flow chart of the present invention.
图中：1-余热锅炉；2-冷却塔；3-汽提塔；4-固定床反应塔Ⅰ；5-固定床反应塔Ⅱ；6-喷淋塔；7-换热泵Ⅰ；8-换热泵Ⅱ；9-再生泵；10-喷淋泵；11-连通管；12-搅拌器；13-换热夹套。In the figure: 1-waste heat boiler; 2-cooling tower; 3-stripping tower; 4-fixed bed reaction tower I; 5-fixed bed reaction tower II; 6-spray tower; 7-heat exchange pump I; 8-heat exchange pump II; 9-regeneration pump; 10-spray pump; 11-connecting pipe; 12-agitator; 13-heat exchange jacket.
具体实施方式DETAILED DESCRIPTION
下面结合具体实施例进一步详细描述本发明，但本发明保护范围并不限于如下所述内容。The present invention is further described in detail below in conjunction with specific embodiments, but the protection scope of the present invention is not limited to the contents described below.
本发明实施例所述同时脱除羰基硫、二硫化碳的方法所用装置，包括余热锅炉1、冷却塔2、汽提塔3、固定床反应塔Ⅰ4、固定床反应塔Ⅱ5、喷淋塔6、换热泵Ⅰ7、换热泵Ⅱ8、再生泵9、喷淋泵10、连通管11、搅拌器12、换热夹套13；余热锅炉1与冷却塔2连通，冷却塔2与汽提塔3连通；汽提塔3通过三通电磁阀分别与固定床反应塔Ⅰ4和固定床反应塔Ⅱ5连通；固定床反应塔Ⅰ4和固定床反应塔Ⅱ5通过三通电磁阀与喷淋塔6连通；汽提塔3和喷淋塔6的下端通过连通管11连通，喷淋塔6的下端通过喷淋泵10与喷淋塔6的顶端连通；冷却塔2、固定床反应塔Ⅰ4、固定床反应塔Ⅱ5的内壁均设有换热夹套13；再生水箱通过再生泵9与固定床反应塔Ⅰ4和固定床反应塔Ⅱ5的顶端连通，固定床反应塔Ⅰ4和固定床反应塔Ⅱ5底部与硫磺回收装置连通；换热泵Ⅱ8的出口与冷却塔2内部换热夹套的顶部连通，冷却塔2内部换热夹套的底部通过换热泵Ⅰ7分别与固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内部换热夹套的顶部连通，固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内部换热夹套的底部通过三通电磁阀与换热泵Ⅱ8的入口连通；汽提塔3和喷淋塔6的底部均设置搅拌器12；固定床反应塔Ⅰ4、固定床反应塔Ⅱ5内的设置再生冲洗装置，底部设置储液槽。The device used in the method for simultaneously removing carbonyl sulfide and carbon disulfide described in the embodiment of the present invention includes a waste heat boiler 1, a cooling tower 2, a stripping tower 3, a fixed bed reaction tower I4, a fixed bed reaction tower II5, a spray tower 6, a heat exchange pump I7, a heat exchange pump II8, a regeneration pump 9, a
冷却塔2和固定床反应塔Ⅰ4和固定床反应塔Ⅱ5组成换热系统，冷却塔2吸收烟气的热量并传递到冷却液中，升温后的冷却液流入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5并放热，维持催化剂在一个适宜的反应温度，放热后的冷却液重新返回冷却塔2中再次吸热，从而进行换热循环。Cooling tower 2 and fixed bed reaction towers Ⅰ4 and Ⅱ5 form a heat exchange system. Cooling tower 2 absorbs the heat of the flue gas and transfers it to the coolant. The heated coolant flows into fixed bed reaction towers Ⅰ4 and Ⅱ5 and releases heat to maintain the catalyst at a suitable reaction temperature. The coolant after releasing heat returns to cooling tower 2 to absorb heat again, thereby performing a heat exchange cycle.
汽提塔3、喷淋塔6和连通管11组助催化系统成，从固定床反应塔Ⅰ4和固定床反应塔Ⅱ5产生的副产物SO2在喷淋塔中形成稀硫酸，稀硫酸再经过连通管11回流到汽提塔3中，汽提塔3中的稀硫酸在汽提塔的作用下被带入到固定床反应塔Ⅰ4和固定床反应塔Ⅱ5中增强催化水解作用，从而达到助催化作用。The stripping tower 3, the spray tower 6 and the connecting
换热系统和再生喷淋系统组成再生系统，再生用水进入处于再生过程阶段的固定床反应塔Ⅱ5和固定床反应塔Ⅰ4，催化剂表面的硫酸盐和硫磺在喷淋作用下被冲洗至底部的储液槽，同时催化剂在换热系统的加热下得到烘干，储液槽中的废液用于后续的硫磺提取工序。The heat exchange system and the regeneration spray system constitute the regeneration system. The regeneration water enters the fixed bed reaction tower II5 and the fixed bed reaction tower I4 which are in the regeneration process stage. The sulfate and sulfur on the surface of the catalyst are washed to the liquid storage tank at the bottom by the spraying action. At the same time, the catalyst is dried by the heating of the heat exchange system. The waste liquid in the liquid storage tank is used for the subsequent sulfur extraction process.
固定床反应塔Ⅰ4和固定床反应塔Ⅱ5组成连续运行系统，当一个固定床反应塔Ⅰ4处于反应过程状态时，另一个固定床反应塔Ⅱ5在电磁阀的控制下处于再生过程5状态，每隔一定时间电磁阀会自动切换两塔所处的工作状态，从而达到连续运行的功能。Fixed bed reaction tower Ⅰ4 and fixed bed reaction tower Ⅱ5 constitute a continuous operation system. When one fixed bed reaction tower Ⅰ4 is in the reaction process state, the other fixed bed reaction tower Ⅱ5 is in the regeneration process 5 state under the control of the solenoid valve. The solenoid valve will automatically switch the working state of the two towers at regular intervals, thereby achieving the function of continuous operation.
实施例1Example 1
本实施例所述同时脱除羰基硫、二硫化碳的方法包括以下步骤：The method for simultaneously removing carbonyl sulfide and carbon disulfide described in this embodiment comprises the following steps:
（1）经过预除尘处理后的高温烟气先通过余热锅炉1降温至150℃，再通过冷却塔2进行热交换，使烟气温度降至60℃，冷却液升高至60℃。(1) After pre-dust removal, the high-temperature flue gas is first cooled to 150°C by waste heat boiler 1, and then heat exchanged by cooling tower 2 to reduce the flue gas temperature to 60°C and raise the coolant temperature to 60°C.
（2）经过降温后的气体再通过汽提塔3的作用，将汽提塔3中摩尔浓度为0.01mol/L的稀硫酸带入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5中。(2) The gas after cooling passes through the stripping tower 3, and the dilute sulfuric acid with a molar concentration of 0.01 mol/L in the stripping tower 3 is brought into the fixed bed reaction tower I4 and the fixed bed reaction tower II5.
（3）步骤（1）中吸收热量并升温后的60℃的冷却液流入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5的换热夹套中，将固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内催化剂的温度提高到60℃。(3) The 60°C coolant that has absorbed heat and increased in temperature in step (1) flows into the heat exchange jackets of fixed bed reaction towers I4 and II5, raising the temperature of the catalyst in fixed bed reaction towers I4 and II5 to 60°C.
（4）夹带稀硫酸的气体在固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内发生催化水解反应。(4) The gas carrying dilute sulfuric acid undergoes catalytic hydrolysis reaction in fixed bed reaction tower I4 and fixed bed reaction tower II5.
（5）产生的SO2随气流进入喷淋塔6产生硫酸、亚硫酸，硫酸和亚硫酸经过连通管11回流至汽提塔3，净化后的气体从出口排出。(5) The generated SO2 enters the spray tower 6 along with the air flow to produce sulfuric acid and sulfurous acid. The sulfuric acid and sulfurous acid are refluxed to the stripping tower 3 through the connecting
（6）冷却液在固定床反应塔Ⅰ4和固定床反应塔Ⅱ5夹套中放热后重新进入冷却塔2循环使用。(6) After releasing heat in the jackets of fixed bed reaction tower Ⅰ4 and fixed bed reaction tower Ⅱ5, the coolant re-enters cooling tower 2 for recycling.
（7）再生用水流入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5冲洗失活催化剂，将催化剂表面的硫酸盐和单质硫带出进入硫磺回收工序，经过水洗后的催化剂在夹套的加热作用下快速烘干，形成再生催化剂。(7) The regeneration water flows into the fixed bed reaction tower I4 and the fixed bed reaction tower II5 to wash the deactivated catalyst, and the sulfate and elemental sulfur on the catalyst surface are taken out to enter the sulfur recovery process. The catalyst after water washing is quickly dried under the heating action of the jacket to form a regenerated catalyst.
本实施例所用催化剂为经过硝酸铁改性的活性炭催化剂Fe/AC。The catalyst used in this example is an activated carbon catalyst Fe/AC modified by ferric nitrate.
通过该方法和装置对含硫烟气（CS2浓度40ppm，COS浓度500ppm，O2浓度1%，空速80000h-1）进行脱硫实验，100%的CS2去除率和100%的COS去除率分别达到600min和540min。这表明该方法和装置具有很好的脱硫效果。The method and device were used to conduct a desulfurization experiment on sulfur-containing flue gas (CS 2 concentration 40ppm, COS concentration 500ppm, O 2 concentration 1%, space velocity 80000h -1 ), and 100% CS 2 removal rate and 100% COS removal rate were achieved in 600min and 540min respectively. This shows that the method and device have a good desulfurization effect.
实施例2Example 2
本实施例所述同时脱除羰基硫、二硫化碳的方法包括以下步骤：The method for simultaneously removing carbonyl sulfide and carbon disulfide described in this embodiment comprises the following steps:
（1）经过预除尘处理后的高温烟气先通过余热锅炉1降温至200℃，再通过冷却塔2进行热交换，使烟气温度降至80℃，冷却液升高至80℃。(1) After pre-dust removal, the high-temperature flue gas is first cooled to 200°C by waste heat boiler 1, and then heat exchanged by cooling tower 2 to reduce the flue gas temperature to 80°C and raise the coolant temperature to 80°C.
（2）经过降温后的气体再通过汽提塔3的作用，将汽提塔3中摩尔浓度为0.06mol/L的稀硫酸带入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5中。(2) The gas after cooling passes through the stripping tower 3, and the dilute sulfuric acid with a molar concentration of 0.06 mol/L in the stripping tower 3 is brought into the fixed bed reaction tower I4 and the fixed bed reaction tower II5.
（3）步骤（1）中吸收热量并升温后的80℃的冷却液流入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5的换热夹套中，将固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内催化剂的温度提高到80℃。(3) The 80°C coolant that has absorbed heat and been heated in step (1) flows into the heat exchange jackets of fixed bed reaction towers I4 and II5, raising the temperature of the catalyst in fixed bed reaction towers I4 and II5 to 80°C.
（4）夹带稀硫酸的气体在固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内发生催化水解反应。(4) The gas carrying dilute sulfuric acid undergoes catalytic hydrolysis reaction in fixed bed reaction tower I4 and fixed bed reaction tower II5.
（5）产生的SO2随气流进入喷淋塔6产生硫酸、亚硫酸，硫酸和亚硫酸经过连通管11回流至汽提塔3，净化后的气体从出口排出。(5) The generated SO2 enters the spray tower 6 along with the air flow to produce sulfuric acid and sulfurous acid. The sulfuric acid and sulfurous acid are refluxed to the stripping tower 3 through the connecting
（6）冷却液在固定床反应塔Ⅰ4和固定床反应塔Ⅱ5夹套中放热后重新进入冷却塔2循环使用。(6) After releasing heat in the jackets of fixed bed reaction tower Ⅰ4 and fixed bed reaction tower Ⅱ5, the coolant re-enters cooling tower 2 for recycling.
（7）再生用水流入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5冲洗失活催化剂，将催化剂表面的硫酸盐和单质硫带出进入硫磺回收工序，经过水洗后的催化剂在夹套的加热作用下快速烘干，形成再生催化剂。(7) The regeneration water flows into the fixed bed reaction tower I4 and the fixed bed reaction tower II5 to wash the deactivated catalyst, and the sulfate and elemental sulfur on the catalyst surface are taken out and enter the sulfur recovery process. The catalyst after water washing is quickly dried under the heating action of the jacket to form a regenerated catalyst.
本实施例所用催化剂为由硝酸铁、硝酸铜、硝酸铝制备成的类水滑石催化剂FeCuAlOx。The catalyst used in this example is a hydrotalcite-like catalyst FeCuAlOx prepared from ferric nitrate, copper nitrate and aluminum nitrate.
通过该方法和装置对含硫烟气（CS2浓度40ppm，COS浓度500ppm，O2浓度1%，空速80000h-1）进行脱硫实验，100%的CS2去除率和100%的COS去除率分别达到840min和630min。这表明该方法和装置具有很好的脱硫效果。The method and device were used to conduct a desulfurization experiment on sulfur-containing flue gas (CS 2 concentration 40ppm, COS concentration 500ppm, O 2 concentration 1%, space velocity 80000h -1 ), and the 100% CS 2 removal rate and the 100% COS removal rate were achieved in 840min and 630min respectively. This shows that the method and device have a good desulfurization effect.
实施例3Example 3
本实施例所述同时脱除羰基硫、二硫化碳的方法包括以下步骤：The method for simultaneously removing carbonyl sulfide and carbon disulfide described in this embodiment comprises the following steps:
（1）经过预除尘处理后的高温烟气先通过余热锅炉1降温至180℃，再通过冷却塔2进行热交换，使烟气温度降至95℃，冷却液升高至95℃。(1) After pre-dust removal, the high-temperature flue gas is first cooled to 180°C by waste heat boiler 1, and then heat exchanged by cooling tower 2 to reduce the flue gas temperature to 95°C and raise the coolant temperature to 95°C.
（2）经过降温后的气体再通过汽提塔3的作用，将汽提塔3中摩尔浓度为0.1mol/L的稀硫酸带入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5中。(2) The gas after cooling passes through the stripping tower 3, and the dilute sulfuric acid with a molar concentration of 0.1 mol/L in the stripping tower 3 is brought into the fixed bed reaction tower I4 and the fixed bed reaction tower II5.
（3）步骤（1）中吸收热量并升温后的95℃的冷却液流入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5的换热夹套中，将固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内催化剂的温度提高到95℃。(3) The 95°C coolant that has absorbed heat and heated up in step (1) flows into the heat exchange jackets of fixed bed reaction tower I4 and fixed bed reaction tower II5, raising the temperature of the catalyst in fixed bed reaction tower I4 and fixed bed reaction tower II5 to 95°C.
（4）夹带稀硫酸的气体在固定床反应塔Ⅰ4和固定床反应塔Ⅱ5内发生催化水解反应。(4) The gas carrying dilute sulfuric acid undergoes catalytic hydrolysis reaction in fixed bed reaction tower I4 and fixed bed reaction tower II5.
（5）产生的SO2随气流进入喷淋塔6产生硫酸、亚硫酸，硫酸和亚硫酸经过连通管11回流至汽提塔3，净化后的气体从出口排出。(5) The generated SO2 enters the spray tower 6 along with the air flow to produce sulfuric acid and sulfurous acid. The sulfuric acid and sulfurous acid are refluxed to the stripping tower 3 through the connecting
（6）冷却液在固定床反应塔Ⅰ4和固定床反应塔Ⅱ5夹套中放热后重新进入冷却塔2循环使用。(6) After releasing heat in the jackets of fixed bed reaction tower Ⅰ4 and fixed bed reaction tower Ⅱ5, the coolant re-enters cooling tower 2 for recycling.
（7）再生用水流入固定床反应塔Ⅰ4和固定床反应塔Ⅱ5冲洗失活催化剂，将催化剂表面的硫酸盐和单质硫带出进入硫磺回收工序，经过水洗后的催化剂在夹套的加热作用下快速烘干，形成再生催化剂。(7) The regeneration water flows into the fixed bed reaction tower I4 and the fixed bed reaction tower II5 to wash the deactivated catalyst, and the sulfate and elemental sulfur on the catalyst surface are taken out and enter the sulfur recovery process. The catalyst after water washing is quickly dried under the heating action of the jacket to form a regenerated catalyst.
本实施例所用催化剂为经过硝酸铜改性的活性氧化铝催化剂Fe/Al2O3。The catalyst used in this example is an activated alumina catalyst Fe/Al 2 O 3 modified by copper nitrate.
通过该方法和装置对含硫烟气（CS2浓度40ppm，COS浓度500ppm，O2浓度1%，空速80000h-1）进行脱硫实验，100%的CS2去除率和100%的COS去除率分别达到720min和570min。这表明该方法和装置具有很好的脱硫效果。The method and device were used to conduct a desulfurization experiment on sulfur-containing flue gas (CS 2 concentration 40ppm, COS concentration 500ppm, O 2 concentration 1%, space velocity 80000h -1 ), and 100% CS 2 removal rate and 100% COS removal rate were achieved in 720min and 570min respectively. This shows that the method and device have a good desulfurization effect.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1211033A (en) * | 1968-01-11 | 1970-11-04 | Ontario Research Foundation | Treatment of waste gases |
| US4761395A (en) * | 1987-03-24 | 1988-08-02 | Advanced Technology Materials, Inc. | Process and composition for purifying arsine, phosphine, ammonia, and inert gases to remove Lewis acid and oxidant impurities therefrom |
| EP0424259A1 (en) * | 1989-10-19 | 1991-04-24 | Elf Aquitaine Production | Process for the improvement of the sulphur yield of a sulphur production unit fed with a hydrogen sulphide containing acid gas |
| US5397556A (en) * | 1992-12-16 | 1995-03-14 | The Regents Of The Unviversity Of California | Process for recovery of sulfur from acid gases |
| CN1173854A (en) * | 1995-11-03 | 1998-02-18 | 埃尔夫·阿奎坦生产公司 | Method for removing virtually all the sulphur compounds H2S, SO2, COS and/or CS2 from sulphou plant waste gases, and recovering such compounds as sulphur |
| US6019953A (en) * | 1996-07-26 | 2000-02-01 | Shell Oil Company | Process for gas incineration |
| FR2990360A1 (en) * | 2012-05-10 | 2013-11-15 | Axens | PROCESS FOR TREATING GAS |
| CN103495329A (en) * | 2013-10-18 | 2014-01-08 | 庆华集团新疆和丰能源化工有限公司 | Process for removing hydrogen sulfide and recovering sulphur |
| AT513414A1 (en) * | 2012-10-08 | 2014-04-15 | Kanzler Walter | Process for the two-stage catalytic oxidation of sulfur compounds in exhaust gases |
| CN206240324U (en) * | 2016-10-31 | 2017-06-13 | 昆明理工大学 | It is a kind of to remove cos, carbon disulfide device simultaneously |
-
2016
- 2016-10-31 CN CN201610928220.XA patent/CN106621796B/en active Active
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1211033A (en) * | 1968-01-11 | 1970-11-04 | Ontario Research Foundation | Treatment of waste gases |
| US4761395A (en) * | 1987-03-24 | 1988-08-02 | Advanced Technology Materials, Inc. | Process and composition for purifying arsine, phosphine, ammonia, and inert gases to remove Lewis acid and oxidant impurities therefrom |
| EP0424259A1 (en) * | 1989-10-19 | 1991-04-24 | Elf Aquitaine Production | Process for the improvement of the sulphur yield of a sulphur production unit fed with a hydrogen sulphide containing acid gas |
| US5397556A (en) * | 1992-12-16 | 1995-03-14 | The Regents Of The Unviversity Of California | Process for recovery of sulfur from acid gases |
| CN1173854A (en) * | 1995-11-03 | 1998-02-18 | 埃尔夫·阿奎坦生产公司 | Method for removing virtually all the sulphur compounds H2S, SO2, COS and/or CS2 from sulphou plant waste gases, and recovering such compounds as sulphur |
| US6019953A (en) * | 1996-07-26 | 2000-02-01 | Shell Oil Company | Process for gas incineration |
| FR2990360A1 (en) * | 2012-05-10 | 2013-11-15 | Axens | PROCESS FOR TREATING GAS |
| AT513414A1 (en) * | 2012-10-08 | 2014-04-15 | Kanzler Walter | Process for the two-stage catalytic oxidation of sulfur compounds in exhaust gases |
| CN103495329A (en) * | 2013-10-18 | 2014-01-08 | 庆华集团新疆和丰能源化工有限公司 | Process for removing hydrogen sulfide and recovering sulphur |
| CN206240324U (en) * | 2016-10-31 | 2017-06-13 | 昆明理工大学 | It is a kind of to remove cos, carbon disulfide device simultaneously |
Non-Patent Citations (1)
| Title |
|---|
| 4-甲基-2-羟基硫酚的合成及吸附性能研究;彭青林等;《矿冶工程》;20110415(第02期);全文 * |
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