JPH0432125B2 - - Google Patents
Info
- Publication number
- JPH0432125B2 JPH0432125B2 JP12420784A JP12420784A JPH0432125B2 JP H0432125 B2 JPH0432125 B2 JP H0432125B2 JP 12420784 A JP12420784 A JP 12420784A JP 12420784 A JP12420784 A JP 12420784A JP H0432125 B2 JPH0432125 B2 JP H0432125B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- treatment
- hydrogen
- line
- decarboxylation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
- 239000007789 gas Substances 0.000 claims description 54
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 19
- 229910052739 hydrogen Inorganic materials 0.000 claims description 19
- 239000001257 hydrogen Substances 0.000 claims description 19
- 238000011282 treatment Methods 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 14
- 208000005156 Dehydration Diseases 0.000 claims description 12
- 238000006114 decarboxylation reaction Methods 0.000 claims description 12
- 230000018044 dehydration Effects 0.000 claims description 12
- 238000006297 dehydration reaction Methods 0.000 claims description 12
- 238000006477 desulfuration reaction Methods 0.000 claims description 10
- 230000023556 desulfurization Effects 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 9
- 229910052751 metal Inorganic materials 0.000 claims description 8
- 239000002184 metal Substances 0.000 claims description 8
- 238000006243 chemical reaction Methods 0.000 claims description 7
- 238000002309 gasification Methods 0.000 claims description 7
- 229930195733 hydrocarbon Natural products 0.000 claims description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000002994 raw material Substances 0.000 description 10
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 8
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 6
- 239000012535 impurity Substances 0.000 description 5
- 238000002407 reforming Methods 0.000 description 5
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical group [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 239000001569 carbon dioxide Substances 0.000 description 3
- 239000003345 natural gas Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 229910021536 Zeolite Inorganic materials 0.000 description 2
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 239000010457 zeolite Substances 0.000 description 2
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000000137 annealing Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000006057 reforming reaction Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 239000011787 zinc oxide Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21D—MODIFYING THE PHYSICAL STRUCTURE OF FERROUS METALS; GENERAL DEVICES FOR HEAT TREATMENT OF FERROUS OR NON-FERROUS METALS OR ALLOYS; MAKING METAL MALLEABLE, e.g. BY DECARBURISATION OR TEMPERING
- C21D1/00—General methods or devices for heat treatment, e.g. annealing, hardening, quenching or tempering
- C21D1/74—Methods of treatment in inert gas, controlled atmosphere, vacuum or pulverulent material
- C21D1/76—Adjusting the composition of the atmosphere
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Crystallography & Structural Chemistry (AREA)
- Mechanical Engineering (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Description
産業上の利用分野
本発明は、金属処理分野等における雰囲気ガス
等として使用した水素含有ガスを再利用する方法
に関するものである。
従来技術
水素雰囲気ガスとしては、アンモニアを原料と
するAXガスとLPG、天然ガス等の炭化水素ガス
を原料とするHNXガスとを組合せたものが従来
から広く使用されている。このような水素雰囲気
ガスを使用して焼鈍等の金属熱処理を実施した場
合、水素雰囲気ガスは、金属被処理物から炉内に
持ち込まれる油、酸素、水分等に起因する不純物
（例えば、O2、CO、CO2、CH4、C2H4、H2Ｏ等）
により汚染される。このため、通常該水素雰囲気
ガスは、そのまま或いは燃焼後大気中に放出して
おり、ガス中のH2−N2分は、有効に利用できな
い。
このような不純物や油分を除去する方法とし
て、H2−N2系のガスをコンプレツサーにより高
圧（６Kg／cm2・Ｇ以上）に圧縮し、吸着除去剤を
使用して不純物を除去する方法がある。しかし
PSA法と呼ばれるこの方法は、圧縮用の動力費
及び処理のための設備費が高価であり、また油分
を含むガスを使用すると吸着剤の表面が油分によ
り被覆されて、吸着剤の寿命が極端に短くなると
いう欠点がある。
発明の構成
本発明は、小型の装置を使用して、複雑な操作
を要することなく、使用後の水素含有ガスを有効
に再利用することを可能とするものである。
即ち、本発明は、金属熱処理工程で雰囲気ガス
として使用した水素含有ガスを炭化水素ガスに加
え、脱硫処理、水蒸気又は水蒸気と空気とをガス
化剤とするガス化処理、CO変成処理及び脱炭酸
脱水処理に供することを特徴とする水素含有ガス
の再利用方法に係るものである。
以下図面に示す本発明実施態様フローチヤート
を参照しつつ、本発明を更に詳細に説明する。
第１図において、ライン１からの都市ガス、天
然ガス、石油ガス等の原料炭化水素ガスは、脱硫
装置２に供給され、硫黄分を除去される。脱硫方
法としては、公知の方法でよく、例えば水添脱硫
用のNi−MoX触媒及び／又は、吸着脱硫用の酸
化亜鉛触媒を使用し、温度常温〜400℃、圧力常
圧〜9.5Kg／cm2・Ｇ、H2／原料（モル／モル）０
〜0.1の条件下で行なえばよい。原料炭化水素ガ
ス中の硫黄分は、5ppm以下とすることが好まし
い。
脱硫装置２で得られた脱硫ガスは、ライン３を
通り、ライン４及び５を通る水蒸気とともに、或
いは更にライン６からの空気とともに、外熱式改
質反応器７に供給され、ガス化処理される。反応
条件は、所望のガス組成、原料の種類、ガス化剤
としての水蒸気（又は水蒸気と空気）の割合等に
より異なり得るが、通常温度800〜1000℃、圧力
常圧〜9.5Kg／cm2Ｇ、水蒸気／炭素（モル／原子
比）＝2.0〜5.0、空気／炭素（モル／原子比）＝０
〜3.5、SV＝700〜2000Nm3／m3／hr程度である。
ガス化剤として空気を併用しない場合には、最終
的に得られるガスは、実質的にH2のみからなる
ものとなる。改質反応器７には、高活性で耐久性
に優れたNi系又は白金、ルテニウム、パラジウ
ム等の白金族系触媒が充填されている。白金族系
触媒を使用する場合には、触媒層を予熱すること
なく、ガス化剤である水蒸気による加熱のみで改
質反応を開始させることができる。得られた改質
ガスの組成は使用する雰囲気ガス、原料ガス、ガ
ス化剤等によつて一様ではないが、通常は水素と
窒素のほかに不純物としてそれぞれ１％程度の一
酸化炭素、二酸化炭素及び炭化水素が含有されて
いる。
改質反応器７で得られた改質ガスは、ライン８
を通りライン９からの水蒸気とともにCO変成処
理１０に入る。このCO変成処理により前記改質
ガス中に含まれている微量の一酸化炭素がすべて
水素と二酸化炭素に変換される。CO変成装置内
での反応条件は、公知のCO変成方法のそれと特
に異なるところはなく、例えば触媒としてCu−
Zn系触媒等の変成触媒を使用し、圧力常圧〜９
Kg／cm2・Ｇ程度、温度180〜270℃程度、SV700〜
2000Nm3／m3／hr程度の条件を採用する。
CO変成装置１０からの出ガスは、ライン１１
を通つて脱炭酸脱水装置１２に送られる。脱炭酸
脱水装置としては、公知の装置をそのまま使用し
得るが、モレキユラーシーブ5A、13A（商標名）
として知られる合成ゼオライト等を吸着剤とする
吸脱着式脱炭酸脱水装置を使用するのが有利であ
る。吸着時の条件は、例えば温度常温、圧力常圧
〜９Kg／cm2程度、吸着サイクル６〜20分程度であ
り、脱着時の条件は、例えば圧力常圧〜真空
（200〜60トール）、再生サイクル４〜18分、パー
ジガス量として製品ガスの５〜15％程度である。
脱炭酸脱水装置１２の脱着操作により得られる
オフガスは、ライン１３を経てブロワー１４に送
られ。次いでライン１５を経て、ライン１６から
の燃料ガスとともに、外熱式改質反応器７の加熱
に使用するのが有利である。
脱炭酸脱水装置１２において炭酸ガス及び水分
を除去された製品ガスは、ライン１７を経て、金
属熱処理炉１８に供給され、熱処理時の水素雰囲
気ガスとして使用される。
金属熱処理炉１８から放出された使用ガスは、
ライン１９を通つて、クツシヨンタンク２０に送
られる。この使用ガスは、金属表面等に付着した
油分等が分解してできた汚染物質（CH4、C2H6、
C3H6、C4H10、CnHm、CO、CO2、H2Ｏ、O2、
その他）を含有している。
クツシヨンタンク２０中の使用ガスは、ライン
２１を通つて昇圧機２２に送られ、ここで昇圧さ
れライン２３を通つて再び脱硫装置２に送られ
る。昇圧機２２としては、コンプレツサー、ブロ
ア等が使用できる。
脱硫装置２では、ライン２３から供給された使
用ガスは、ライン１から供給された原料ガスと混
合して脱硫処理を行ない、再び上記と同様の工程
により処理して水素含有ガスとして再使用する。
発明の効果
本発明によれば、小型の装置を使用して、複雑
な操作を要することなく、N2／H2（モル比）＝
０／100〜170／30の範囲内で任意の組成を有する
水素含有ガスが得られる。更に、金属熱処理の雰
囲気ガスとして使用された水素含有ガスは、不純
物を除去し、再使用される。従つて本発明方法に
よれば、都市ガス、天然ガス、LPG等の原料ガ
ス、水蒸気、空気等のガス化剤及び改質炉で必要
な燃料等の使用量を極端に低下でき、またそれに
伴なう設備の縮小化が可能となる。即ち、本発明
方法は、非常に高効率であり、かつ低廉な水素含
有ガスの製造方法である。
実施例
次に本発明の実施例を示して本発明の特徴を詳
しく示す。
実施例１及び比較例１，２
本発明方法及び従来法（A.X.及びH.X.）によ
りN2／H2（モル比）＝75／25の水素含有ガスを
25Nm3／hrの割合で製造した場合の、原料ガス使
用量、燃料使用量、電力消費量、給水量及び空気
使用量の比較を第１表に示す。
なお、実施例１でのガス化処理後及び脱炭酸脱
水処理後におけるガス組成（％）は以下の通りで
あつた。
組成 ガス化処理後 脱炭酸脱水処理後
H2 79.0 79.0
CO 1.1 −
CO2 0.7 −
CH4 0.25 0.2
N2 18.95 20.8
INDUSTRIAL APPLICATION FIELD The present invention relates to a method for reusing hydrogen-containing gas used as an atmospheric gas in the metal processing field and the like. Prior Art As a hydrogen atmosphere gas, a combination of AX gas made from ammonia as a raw material and HNX gas made from a hydrocarbon gas such as LPG or natural gas has been widely used. When metal heat treatment such as annealing is performed using such a hydrogen atmosphere gas, the hydrogen atmosphere gas contains impurities (for example, O 2 , CO, CO 2 , CH 4 , C 2 H 4 , H 2 O, etc.)
contaminated by For this reason, the hydrogen atmosphere gas is usually released into the atmosphere as it is or after combustion, and the H 2 -N 2 portion in the gas cannot be used effectively. One way to remove such impurities and oil is to compress H 2 -N 2 gas to high pressure (6 kg/cm 2 G or more) using a compressor, and then use an adsorption remover to remove the impurities. be. but
This method, called the PSA method, requires high power costs for compression and equipment costs for treatment, and if gas containing oil is used, the surface of the adsorbent will be coated with oil, which will significantly shorten the life of the adsorbent. The disadvantage is that it becomes shorter. Structure of the Invention The present invention makes it possible to effectively recycle used hydrogen-containing gas using a small-sized device and without requiring complicated operations. That is, the present invention adds a hydrogen-containing gas used as an atmospheric gas in a metal heat treatment process to a hydrocarbon gas, and performs a desulfurization treatment, a gasification treatment using steam or steam and air as a gasification agent, a CO conversion treatment, and a decarboxylation treatment. The present invention relates to a method for reusing hydrogen-containing gas, which is characterized by subjecting it to dehydration treatment. The present invention will be described in more detail below with reference to the flowchart of embodiments of the present invention shown in the drawings. In FIG. 1, raw material hydrocarbon gas such as city gas, natural gas, petroleum gas, etc. from a line 1 is supplied to a desulfurization device 2, where sulfur content is removed. The desulfurization method may be a known method, for example, using a Ni-MoX catalyst for hydrodesulfurization and/or a zinc oxide catalyst for adsorption desulfurization, at a temperature of normal temperature to 400°C, and a pressure of normal pressure to 9.5 kg/cm. 2・G, H 2 / raw material (mol/mol) 0
This can be done under conditions of ~0.1. The sulfur content in the raw material hydrocarbon gas is preferably 5 ppm or less. The desulfurization gas obtained in the desulfurization device 2 passes through a line 3 and is supplied to an external heat reforming reactor 7 together with steam passing through lines 4 and 5 or further with air from a line 6, where it is gasified. Ru. The reaction conditions may vary depending on the desired gas composition, the type of raw materials, the ratio of steam (or steam and air) as a gasifying agent, etc., but are usually at a temperature of 800 to 1000°C and a pressure of normal pressure to 9.5 Kg/cm 2 G. , water vapor/carbon (mol/atomic ratio) = 2.0 to 5.0, air/carbon (mol/atomic ratio) = 0
~3.5, SV = about 700 to 2000Nm 3 /m 3 /hr.
When air is not used as a gasifying agent, the gas finally obtained consists essentially of H 2 only. The reforming reactor 7 is filled with a highly active and durable Ni-based catalyst or a platinum group-based catalyst such as platinum, ruthenium, palladium, etc. When a platinum group catalyst is used, the reforming reaction can be started only by heating with steam, which is a gasifying agent, without preheating the catalyst layer. The composition of the obtained reformed gas varies depending on the atmospheric gas, raw material gas, gasifying agent, etc. used, but usually contains hydrogen and nitrogen as well as impurities of approximately 1% each of carbon monoxide and carbon dioxide. Contains carbon and hydrocarbons. The reformed gas obtained in the reforming reactor 7 is transferred to the line 8
and enters the CO conversion treatment 10 together with the steam from line 9. Through this CO conversion treatment, all trace amounts of carbon monoxide contained in the reformed gas are converted into hydrogen and carbon dioxide. The reaction conditions in the CO shift converter are not particularly different from those of known CO shift methods; for example, Cu-
Using a shift catalyst such as a Zn-based catalyst, the pressure is from normal pressure to 9.
Kg/ cm2・G degree, temperature 180~270℃, SV700~
A condition of approximately 2000Nm 3 /m 3 /hr is adopted. Output gas from the CO converter 10 is transferred to the line 11
It is sent to the decarboxylation and dehydration device 12 through the. As the decarboxylation and dehydration equipment, known equipment can be used as is, but Molecular Sieve 5A, 13A (trade name)
It is advantageous to use an adsorption/desorption type decarboxylation/dehydration device using synthetic zeolite known as zeolite as an adsorbent. The conditions for adsorption are, for example, normal temperature, normal pressure to about 9 kg/ cm2 , and adsorption cycle of about 6 to 20 minutes, and the conditions for desorption are, for example, normal pressure to vacuum (200 to 60 torr), and regeneration. The cycle is 4 to 18 minutes, and the amount of purge gas is about 5 to 15% of the product gas. The off-gas obtained by the desorption operation of the decarboxylation and dehydration device 12 is sent to the blower 14 via the line 13. It then passes through line 15 and is advantageously used together with the fuel gas from line 16 to heat the external heat reforming reactor 7 . The product gas from which carbon dioxide and moisture have been removed in the decarboxylation and dehydration device 12 is supplied to the metal heat treatment furnace 18 via a line 17, and is used as a hydrogen atmosphere gas during heat treatment. The used gas released from the metal heat treatment furnace 18 is
It is sent to the cushion tank 20 through line 19. This used gas contains pollutants (CH 4 , C 2 H 6 ,
C3H6 , C4H10 , CnHm, CO, CO2 , H2O , O2 ,
(others). The gas used in the cushion tank 20 is sent through a line 21 to a booster 22, where it is pressurized and sent through a line 23 to the desulfurizer 2 again. As the booster 22, a compressor, a blower, etc. can be used. In the desulfurization device 2, the gas supplied from the line 23 is mixed with the raw material gas supplied from the line 1, subjected to a desulfurization treatment, and then processed again through the same steps as described above to be reused as a hydrogen-containing gas. Effects of the Invention According to the present invention, N 2 /H 2 (molar ratio) =
A hydrogen-containing gas having an arbitrary composition within the range of 0/100 to 170/30 can be obtained. Furthermore, the hydrogen-containing gas used as an atmospheric gas for metal heat treatment is reused after removing impurities. Therefore, according to the method of the present invention, the amount of raw material gases such as city gas, natural gas, and LPG, gasifiers such as steam and air, and fuel required for the reformer can be extremely reduced, and the amount of fuel required for the reformer can be extremely reduced. This makes it possible to downsize the equipment. That is, the method of the present invention is a very highly efficient and inexpensive method for producing hydrogen-containing gas. EXAMPLES Next, examples of the present invention will be shown to illustrate the features of the present invention in detail. Example 1 and Comparative Examples 1 and 2 Hydrogen-containing gas with N 2 /H 2 (molar ratio) = 75/25 was produced by the method of the present invention and conventional methods (AX and HX).
Table 1 shows a comparison of raw material gas usage, fuel usage, power consumption, water supply volume, and air usage when produced at a rate of 25Nm 3 /hr. The gas composition (%) after the gasification treatment and after the decarboxylation and dehydration treatment in Example 1 was as follows. Composition After gasification After decarboxylation and dehydration H 2 79.0 79.0 CO 1.1 − CO 2 0.7 − CH 4 0.25 0.2 N 2 18.95 20.8
【表】
実施例２及び比較例３
本発明方法及び従来法（H.X.）により、N2／
H2（モル比）＝85／15の水素含有ガスを25Nm3／
hrの割合で製造した場合の、原料ガス使用量、燃
料使用量、電力消費量、給水量及び空気使用量の
比較を第２表に示す。
なお、実施例２でのガス化処理後及び脱炭酸脱
水処理後におけるガス組成（％）は以下の通りで
あつた。
組成 ガス化処理後 脱炭酸脱水処理後
H2 86.1 88.4
CO 1.2 −
CO2 0.8 −
CH4 0.3 0.3
N2 11.6 11.3[Table] Example 2 and Comparative Example 3 N 2 /
H 2 (molar ratio) = 85/15 hydrogen-containing gas at 25Nm 3 /
Table 2 shows a comparison of raw material gas usage, fuel usage, electricity consumption, water supply volume, and air usage when manufacturing at the rate of hr. The gas composition (%) after the gasification treatment and after the decarboxylation and dehydration treatment in Example 2 was as follows. Composition After gasification After decarboxylation and dehydration H 2 86.1 88.4 CO 1.2 − CO 2 0.8 − CH 4 0.3 0.3 N 2 11.6 11.3
第１図は、本発明方法の一実施態様を示すフロ
ーチヤートである。
１……炭化水素供給ライン、２……脱硫装置、
４，５，９……水蒸気供給ライン、６……空気供
給ライン、７……外熱式改質反応器、１０……
CO変成処理、１２……脱炭酸脱水装置、１８…
…金属熱処理炉、２０……クツシヨンタンク、２
２……昇圧機。
FIG. 1 is a flowchart showing one embodiment of the method of the present invention. 1...Hydrocarbon supply line, 2...Desulfurization equipment,
4, 5, 9...Steam supply line, 6...Air supply line, 7...External heat reforming reactor, 10...
CO conversion treatment, 12...Decarboxylation and dehydration equipment, 18...
...Metal heat treatment furnace, 20...Cushion tank, 2
2... Boost machine.
Claims (1)
水素含有ガスを炭化水素ガスに加え、脱硫処理、
水蒸気又は水蒸気と空気とをガス化剤とするガス
化処理、CO変成処理及び脱炭酸脱水処理に供す
ることを特徴とする水素含有ガスの再利用方法。1 Hydrogen-containing gas used as atmospheric gas in the metal heat treatment process is added to hydrocarbon gas, and desulfurization treatment,
A method for reusing hydrogen-containing gas, characterized by subjecting it to gasification treatment, CO conversion treatment, and decarboxylation and dehydration treatment using water vapor or water vapor and air as gasifying agents.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12420784A JPS613831A (en) | 1984-06-15 | 1984-06-15 | Reutilizing method of hydrogen-containing gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP12420784A JPS613831A (en) | 1984-06-15 | 1984-06-15 | Reutilizing method of hydrogen-containing gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS613831A JPS613831A (en) | 1986-01-09 |
| JPH0432125B2 true JPH0432125B2 (en) | 1992-05-28 |
Family
ID=14879639
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP12420784A Granted JPS613831A (en) | 1984-06-15 | 1984-06-15 | Reutilizing method of hydrogen-containing gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS613831A (en) |
-
1984
- 1984-06-15 JP JP12420784A patent/JPS613831A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS613831A (en) | 1986-01-09 |
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