WO2011108213A1 - キャスタブル中の硫黄化合物の除去方法 - Google Patents
キャスタブル中の硫黄化合物の除去方法 Download PDFInfo
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- WO2011108213A1 WO2011108213A1 PCT/JP2011/000935 JP2011000935W WO2011108213A1 WO 2011108213 A1 WO2011108213 A1 WO 2011108213A1 JP 2011000935 W JP2011000935 W JP 2011000935W WO 2011108213 A1 WO2011108213 A1 WO 2011108213A1
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Definitions
- the present invention relates to a method for removing sulfur compounds contained in castables constructed as heat-resistant members on the inner surfaces of reactors, pipes and the like. More specifically, the sulfur compounds contained in castables constructed as heat-resistant members on the inner surface of the connecting pipe from the reforming catalyst tube outlet of the synthesis gas production device to the waste heat boiler are removed in advance before the operation of the synthesis gas production device. On how to do.
- heat-resistant members are coated on the inner surfaces of the reactors and pipes as necessary. is doing.
- this heat-resistant member castable is often used because it is easy to construct.
- this castable often contains a trace amount of a sulfur compound, and when exposed to high temperatures, the sulfur compound is detached, which may adversely affect subsequent devices and products.
- a synthetic gas mixed gas of carbon monoxide and hydrogen
- a reforming reaction Is done.
- the produced synthesis gas produces liquid hydrocarbons by, for example, a Fischer-Tropsch reaction, and the obtained liquid hydrocarbons are hydrotreated to produce synthetic hydrocarbons such as product fuel oil.
- a series of steps including this Fischer-Tropsch reaction is called a Gas-to-Liquids (GTL) process.
- the synthesis gas can be used for methanol synthesis and oxo synthesis.
- the reforming reaction proceeds at a high temperature of 700 to 900 ° C., for example, in the case of the steam reforming method. Therefore, the high-temperature synthesis gas generated from the reformer outlet is sent to a waste heat boiler through a pipe covered with a castable which is a refractory material, and is heat-exchanged.
- the sulfur compound originally contained in the castable may be desorbed, and the sulfur compound may be mixed in the gas. Furthermore, since the separation and recovery of carbon dioxide from the produced synthesis gas is carried out by chemical absorption using a weakly basic aqueous solution such as an amine solution, the sulfur compound contained in the product gas is also separated and recovered simultaneously with the carbon dioxide. Become. Therefore, the separated and recovered gas is supplied to the reformer for producing synthetic gas in a state containing the sulfur compound desorbed from the castable, and the reforming catalyst used in the reformer is deteriorated by the adsorption poisoning of the sulfur compound. There's a problem.
- the object of the present invention is to avoid the adverse effects on subsequent devices and products due to sulfur compounds desorbed from castables installed as heat-resistant members on the inner surfaces of reactors and pipes. Furthermore, the present invention provides a castable sulfur compound mixed in a product gas produced by a reforming reaction such as natural gas, the mixed sulfur compound is separated and recovered together with carbon dioxide, and the recovered carbon dioxide is used as a raw material gas. By recycling, the sulfur compound is supplied to the reformer, and the reforming catalyst of the reformer is prevented from being poisoned by sulfur and being deteriorated.
- the present invention removes sulfur compounds in castable by circulating steam purged from steam or a gas containing steam to castable constructed as a heat-resistant member on the inner surface of a reactor, piping, etc. It is characterized by doing.
- the present invention removes sulfur compounds contained in the castable in advance by flowing a purge gas made of steam or a steam-containing gas through piping used in the synthesis gas production apparatus before the operation of the synthesis gas production apparatus. It is characterized by doing.
- FIG. 3 is a schematic diagram showing an outline of a sulfur compound removal test from a castable in Example 1.
- 4 is a schematic diagram showing an outline of a reforming reaction test in Example 2.
- FIG. 6 is a schematic diagram showing an outline of a sulfur compound removal test from castables in Comparative Examples 1 to 5.
- FIG. 9 is a schematic diagram showing an outline of a reforming reaction test in Comparative Example 6.
- the method for removing sulfur compounds from castables used in reactors and pipes according to the present invention is to circulate a purge gas consisting of steam or a steam-containing gas in advance in reactors and pipes that use castables as heat-resistant materials.
- the reactor and piping may be used in any apparatus as long as a castable is used as a heat-resistant material.
- unreacted carbon dioxide gas and produced carbon dioxide gas contained in the produced synthesis gas are separated and recovered, recycled to the synthesis gas production process, and reused in the carbon dioxide reforming method.
- the sulfur compound desorbed from the castable is separated and recovered and supplied to the reformer for synthesis gas production, and the reforming catalyst used for the reformer is a sulfur compound.
- the problem of deterioration due to adsorption poisoning can be prevented.
- the synthesis gas production apparatus is an apparatus having at least a reformer that produces synthesis gas from natural gas by a reforming reaction, and a pipe that connects the reformer and other sections, and all or at least the reformer outlet of the pipe This means that castables are used in some parts. Furthermore, in the synthesis gas production apparatus according to the present invention, a decarbonation section for separating and recovering carbon dioxide in the synthesis gas is provided in the steps after the reformer, and a gas containing the separated and collected carbon dioxide (hereinafter referred to as separation and recovery). Gas) is recycled to the reformer and reused in the reforming reaction.
- separation and recovery a gas containing the separated and collected carbon dioxide
- the synthesis gas production apparatus may include a desulfurization section for desulfurizing sulfur compounds contained in natural gas.
- a desulfurization section for desulfurizing sulfur compounds contained in natural gas.
- any process used in a known syngas production apparatus such as a heat recovery section for recovering heat generated by the reforming reaction, an oxygen supply section, or a syngas adjustment section may be provided.
- the heat recovery section is preferably installed in a process after the reformer and before the decarbonation section.
- the reformer is equipped with a catalyst tube filled with a reforming catalyst, and the reforming reaction proceeds by the catalytic action of the reforming catalyst by heating the natural gas mixed with carbon dioxide and steam in the catalyst tube. Syngas is produced.
- the reforming reaction can be performed by a known method such as a steam reforming method using steam or a carbon dioxide reforming method using carbon dioxide.
- the steam reforming method is a method in which steam is added to natural gas and a synthesis gas is generated according to the following reaction formula (1).
- the carbon dioxide reforming method is a method in which carbon dioxide gas is added to natural gas.
- carbon dioxide contained in natural gas is used to produce synthesis gas according to the following reaction formula (2).
- Equation (1) CH 4 + H 2 O ⁇ CO + 3H 2 Equation (2): CH 4 + CO 2 ⁇ 2CO + 2H 2
- the ratio of CO and H 2 to be generated can be adjusted.
- any known reforming catalyst can be used.
- An oxide catalyst or the like is preferably used, and a noble metal-supported basic oxide catalyst or the like is preferably used when the steam reforming method and the carbon dioxide reforming method are performed simultaneously.
- the concentration of the sulfur compound contained in the gas introduced into the synthesis gas production section is preferably less than 10 vol-ppb in terms of sulfur atoms.
- the gas introduced into the synthesis gas production section is steam so that the H 2 O / C molar ratio is greater than 0 and less than or equal to 3.0 and / or the CO 2 / C molar ratio is greater than 0 and less than or equal to 1.0. And / or carbon dioxide is added.
- the natural gas contains organic sulfur compounds such as dimethyl sulfide (DMS: (CH 3 ) 2 S) and carbonyl sulfide (COS). Therefore, it is preferable that natural gas is desulfurized by a desulfurization apparatus installed in a desulfurization section in the synthesis gas production apparatus before being introduced into the reformer.
- DMS dimethyl sulfide
- COS carbonyl sulfide
- the desulfurization For the desulfurization, known methods such as an alkali cleaning method, a solvent desulfurization method, and a catalytic desulfurization method can be used. Among them, it is particularly preferable to desulfurize by a catalytic desulfurization method (hydrodesulfurization method) by hydrotreatment.
- the hydrodesulfurization method includes a first step of hydrotreating a sulfur compound contained in a gas and a second step of absorbing the sulfur compound hydrogenated in the first step with a desulfurization agent. Desulfurization method.
- the synthesis gas produced by the reforming reaction contains carbon dioxide gas generated by the shift reaction accompanying the steam reforming and unreacted carbon dioxide gas in the carbon dioxide reforming.
- these carbon dioxide gases are separated and recovered in the decarbonation section.
- a method for separating and recovering carbon dioxide gas a chemical absorption method, a physical adsorption method, a membrane separation method and the like are known, but in this embodiment, it is preferable to use a chemical absorption method using an amine-based aqueous solution such as monoethanolamine. .
- an amine treater comprising an absorption tower and a regeneration tower is used.
- carbon dioxide contained in the synthesis gas is absorbed in an amine-based aqueous solution such as monoethanolamine in the absorption tower.
- a method of stripping the amine-based aqueous solution that has absorbed the carbon dioxide gas by heating with steam in a regeneration tower to dissipate the carbon dioxide gas and recovering the diffused carbon dioxide gas can be preferably used.
- the carbon dioxide thus separated and recovered is then recycled to the reformer and can be reused for the carbon dioxide reforming reaction.
- the produced synthesis gas has a high temperature of about 900 ° C. at the reformer outlet. For this reason, there exists a possibility that the sulfur compound in the castable used as a coating on the pipe connecting the steps after the reformer outlet may be desorbed in the form of hydrogen sulfide and mixed into the synthesis gas.
- the separated and recovered gas that is separated and recovered in the decarbonation step and then introduced into the reformer includes hydrogen sulfide desorbed from the castable in addition to the carbon dioxide gas. If the sulfur compound concentration in the gas introduced into the reformer exceeds 10 vol-ppb in terms of sulfur atoms due to the hydrogen sulfide, the reforming catalyst may be deteriorated by sulfur poisoning.
- a purge gas composed of steam or a steam-containing gas is circulated in advance in the piping used in the reformed gas production apparatus before the operation of the synthesis gas production apparatus. Remove the sulfur compounds in the castable by drying and rolling.
- Drying is preferably performed before the synthesis gas production apparatus is operated and before the catalyst tube is filled with the reforming catalyst.
- the purge gas it is preferable to use steam or steam-containing gas from the viewpoint of the sulfur compound removal rate.
- the steam content is not particularly limited, but is usually 1 vol-% or more, preferably 10 vol-% or more, and more preferably 50 vol-% or more.
- the heating temperature of the dry firing is 650 to 900 ° C., preferably 750 to 900 ° C., and the sulfur compound is efficiently removed by circulating until the sulfur compound in the discharged purge gas is not detected. be able to.
- the sulfur compound in the castable can be detected at a detection limit value of 1.0 wtppm or less in terms of sulfur atoms, and the removal rate can be 97% or more if it is circulated for 48 hours or more. It is possible to remove.
- deterioration of the reforming catalyst during production of synthesis gas can be suppressed by the synthesis gas production apparatus using the pipe from which the sulfur compound contained in the castable is removed by the above method.
- the synthesis gas thus produced is subjected to, for example, a Fischer-Tropsch reaction, and a gaseous product is separated from the Fischer-Tropsch reaction product to produce Fischer-Tropsch oil.
- the hydrotreated product obtained by hydrotreating can be suitably used in a GTL process in which light hydrocarbon gas and kerosene oil, which is the final product, are separated by distillation.
- hydrogen can be suitably produced from the synthesis gas produced by the synthesis gas production apparatus using the piping embodying the present invention.
- Example 1 In order to show that a sulfur compound in castable is removed by circulating a purge gas through a pipe and drying it, Example 1 below was performed.
- Plycast MIX # 786 (trade name. Concentration of sulfur compound contained is 39.5 wt-ppm in terms of sulfur atom) manufactured by Japan Publico Co., Ltd. was used.
- the castable raw material was kneaded with water, and after it was confirmed that strength was generated, it was crushed into 2 mm-4 mm pieces.
- the chemical composition of the castable before the test is as shown in Table 1.
- the SUS reaction tube 14 filled with the castable fragments 11 between the alumina bead layers 12 and 13 was heated to a predetermined temperature, and steam or a steam / nitrogen mixed gas was allowed to flow from the upper part of the apparatus for 48 hours (FIG. 1).
- the purge gas that has passed through the castable is condensed with water by the cooler 15 and separated into gas and liquid, and the sulfur compound concentration in the condensed water 16 is analyzed by ICP (inductively coupled plasma) analysis.
- the sulfur compound concentration in the nitrogen gas 17 is sulfur chemiluminescence.
- SCD-GC gas chromatograph
- SCD sulfur chemiluminescence detector
- the castable was extracted after the experiment was completed, and the concentration of the sulfur compound remaining in the castable was also measured.
- Table 2 shows the results after circulating the purge gas for 48 hours.
- concentration of the outflow sulfur compound into the gas and liquid after 48 hours was zero. Further, the concentration of residual sulfur compounds in the castable after 48 hours decreased to less than 1.0 wt-ppm (below the detection limit) in terms of sulfur atoms.
- Example 2 In order to confirm that no sulfur compound was mixed in the synthesis gas from the castable through which the purge gas was allowed to flow, the following Example 2 was performed.
- Example 2 After the test of Example 1, the SUS reaction tube 24 in which the castable 21 (7.5 cc) subjected to the steam treatment was installed in the rear stage of the reforming catalyst 28 was prepared, and the synthesis gas having an H 2 / CO ratio of 2.0 was prepared. A reforming reaction test to be manufactured was carried out (FIG. 2), and it was confirmed by SCD-GC analysis whether or not a sulfur compound was contained in the synthesis gas 29 generated from the reactor outlet.
- Example 3 In order to investigate the change in the sulfur compound removal rate depending on the heating temperature when the purge gas is circulated, the same test apparatus as in Example 1 is used, except for the temperature of the packed bed, except for the steam / nitrogen mixed gas of Example 1. The sulfur compound removal test was carried out under the conditions described above. As a result, when the temperature of the packed bed was maintained at 650 ° C. and 750 ° C., and the steam / nitrogen mixed gas was allowed to flow for 48 hours, the sulfur compound removal rates in the castable were 80% and 97%, respectively.
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Abstract
Description
式(1): CH4 + H2O → CO + 3H2
式(2): CH4 + CO2 → 2CO + 2H2
式(4): R-NH2 + H2S → R-NH3 + + HS-
配管にパージガスを流通させ乾燥焚きすることでキャスタブルの硫黄化合物が除去されることを示すため、以下の実施例1を行った。
パージガスを貫流させたキャスタブルからは合成ガス中に硫黄化合物が混入しないことを確認するため、以下の実施例2をおこなった。
パージガスを流通させる際の加熱温度による硫黄化合物除去率の変化を調べるため、実施例1と同様の試験装置を用いて、充填層の温度以外は実施例1のスチーム/窒素混合ガスの場合と同一の条件にして硫黄化合物除去試験を実施した。その結果、充填層の温度を650℃、750℃に維持してスチーム/窒素混合ガスを48時間流したときのキャスタブル中の硫黄化合物除去率は、それぞれ80%、97%であった。
スチームを含まないパージガスでの硫黄化合物除去効率を確認するため、以下の比較例を行った。
実施例1と同様の試験装置を用いて、パージガスの組成を表4中に示すように変えたほかは実施例1と同一の条件にして硫黄化合物除去試験を実施し、キャスタブル31中に残存している硫黄化合物濃度及び硫黄化合物除去率を求めた(図3)。
実施例2と同様に比較例4による硫黄化合物除去試験後のキャスタブル41(15cc)を触媒層後段に設置して改質反応試験を実施し、生成合成ガス49中への硫黄化合物の流出をSCD-GC分析により確認した(図4)。なお、キャスタブルの充填量は15ccとした。表5の結果が示すように、反応開始直後から生成ガス中への硫黄化合物の脱離が確認され、以後連続的に発生した。スチームを用いない加熱前処理では硫黄化合物の除去は不充分であることが確認された。
12 アルミナビーズ層
13 アルミナビーズ層
14 SUS反応管
15 冷却器
16 凝縮水
17 窒素ガス
21 キャスタブル
24 SUS反応管
28 リフォーミング触媒
29 合成ガス
31 キャスタブル
41 キャスタブル
49 合成ガス
Claims (5)
- 反応器及び配管の内表面に耐熱部材として施工されたキャスタブルにスチーム又はスチーム含有ガスからなるパージガスを流通させて乾燥焚きを行うことを特徴とする、キャスタブル中の硫黄化合物の除去方法。
- 前記配管が合成ガス製造装置に使用され、前記乾燥焚きを合成ガス製造装置の稼動前に行うことを特徴とする、請求項1に記載のキャスタブル中の硫黄化合物の除去方法。
- 前記乾燥焚きを合成ガス製造用装置に改質触媒を充填する前に行うことを特徴とする、請求項2に記載のキャスタブル中の硫黄化合物の除去方法。
- 前記乾燥焚きの温度は750~900℃であることを特徴とする、請求項1~3の何れか1項に記載のキャスタブル中の硫黄化合物の除去方法。
- 前記乾燥焚きは48時間以上行うことを特徴とする、請求項4に記載のキャスタブル中の硫黄化合物の除去方法。
Priority Applications (9)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN201180011677.XA CN102781565B (zh) | 2010-03-02 | 2011-02-21 | 浇注料中的硫化物的去除方法 |
EP11750327.6A EP2543431A4 (en) | 2010-03-02 | 2011-02-21 | METHOD FOR REMOVING SULFUR COMPOUNDS FROM A MOLDED MATERIAL |
US13/581,019 US8832967B2 (en) | 2010-03-02 | 2011-02-21 | Method for removing sulfur compounds in castable |
CA2791861A CA2791861C (en) | 2010-03-02 | 2011-02-21 | Method for removing sulfur compounds in castable |
AU2011222348A AU2011222348B2 (en) | 2010-03-02 | 2011-02-21 | Method for removing sulfur compounds in castable |
BR112012021914A BR112012021914B8 (pt) | 2010-03-02 | 2011-02-21 | método para remover compostos de enxofre em fundível |
EA201290736A EA019981B1 (ru) | 2010-03-02 | 2011-02-21 | Способ удаления соединений серы, содержащихся в жаропрочном бетоне |
JP2012502991A JP5591910B2 (ja) | 2010-03-02 | 2011-02-21 | キャスタブル中の硫黄化合物の除去方法 |
ZA2012/06247A ZA201206247B (en) | 2010-03-02 | 2012-08-20 | Method for removing sulfur compounds in castable |
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US (1) | US8832967B2 (ja) |
EP (1) | EP2543431A4 (ja) |
JP (1) | JP5591910B2 (ja) |
CN (1) | CN102781565B (ja) |
AU (1) | AU2011222348B2 (ja) |
BR (1) | BR112012021914B8 (ja) |
CA (1) | CA2791861C (ja) |
EA (1) | EA019981B1 (ja) |
MY (1) | MY160346A (ja) |
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DE102011107669B4 (de) * | 2011-07-12 | 2022-02-10 | Eberspächer Climate Control Systems GmbH & Co. KG | Kraftstoffbehandlungsvorrichtung |
US10046371B2 (en) * | 2013-03-29 | 2018-08-14 | Semes Co., Ltd. | Recycling unit, substrate treating apparatus and recycling method using the recycling unit |
US10131593B2 (en) * | 2013-08-06 | 2018-11-20 | Chiyoda Corporation | Systems and methods for producing hydrogen from a hydrocarbon and using the produced hydrogen in a hydrogenation reaction |
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- 2011-02-21 EA EA201290736A patent/EA019981B1/ru not_active IP Right Cessation
- 2011-02-21 EP EP11750327.6A patent/EP2543431A4/en not_active Withdrawn
- 2011-02-21 JP JP2012502991A patent/JP5591910B2/ja not_active Expired - Fee Related
- 2011-02-21 CN CN201180011677.XA patent/CN102781565B/zh active Active
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JP2003336079A (ja) * | 2002-05-20 | 2003-11-28 | Kyuchiku Ind Co Ltd | 熱分解ガスの改質方法 |
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BR112012021914B8 (pt) | 2019-10-01 |
US20120317833A1 (en) | 2012-12-20 |
JP5591910B2 (ja) | 2014-09-17 |
JPWO2011108213A1 (ja) | 2013-06-20 |
CA2791861A1 (en) | 2011-09-09 |
MY160346A (en) | 2017-02-28 |
BR112012021914A2 (pt) | 2016-05-31 |
ZA201206247B (en) | 2013-05-29 |
CN102781565B (zh) | 2016-04-27 |
CN102781565A (zh) | 2012-11-14 |
EP2543431A1 (en) | 2013-01-09 |
AU2011222348A1 (en) | 2012-09-20 |
AU2011222348B2 (en) | 2013-11-07 |
US8832967B2 (en) | 2014-09-16 |
EA201290736A1 (ru) | 2013-02-28 |
EA019981B1 (ru) | 2014-07-30 |
CA2791861C (en) | 2016-09-06 |
BR112012021914B1 (pt) | 2019-04-02 |
EP2543431A4 (en) | 2014-01-15 |
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