JPH04202292A - Method for converting reformed lpg gas into highly calorific gas - Google Patents
Method for converting reformed lpg gas into highly calorific gasInfo
- Publication number
- JPH04202292A JPH04202292A JP33205090A JP33205090A JPH04202292A JP H04202292 A JPH04202292 A JP H04202292A JP 33205090 A JP33205090 A JP 33205090A JP 33205090 A JP33205090 A JP 33205090A JP H04202292 A JPH04202292 A JP H04202292A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- catalyst
- reformed
- lpg
- liquefied petroleum
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims description 11
- 239000007789 gas Substances 0.000 claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 33
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 claims abstract description 25
- 239000003915 liquefied petroleum gas Substances 0.000 claims abstract description 24
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000006243 chemical reaction Methods 0.000 claims abstract description 4
- 150000003464 sulfur compounds Chemical class 0.000 claims abstract description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 3
- 229910052739 hydrogen Inorganic materials 0.000 claims description 3
- 239000001257 hydrogen Substances 0.000 claims description 3
- 229910052593 corundum Inorganic materials 0.000 abstract 1
- 235000013980 iron oxide Nutrition 0.000 abstract 1
- VBMVTYDPPZVILR-UHFFFAOYSA-N iron(2+);oxygen(2-) Chemical class [O-2].[Fe+2] VBMVTYDPPZVILR-UHFFFAOYSA-N 0.000 abstract 1
- 238000011282 treatment Methods 0.000 abstract 1
- 229910001845 yogo sapphire Inorganic materials 0.000 abstract 1
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- QPLDLSVMHZLSFG-UHFFFAOYSA-N Copper oxide Chemical compound [Cu]=O QPLDLSVMHZLSFG-UHFFFAOYSA-N 0.000 description 5
- 150000007514 bases Chemical class 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 239000005751 Copper oxide Substances 0.000 description 3
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- 229910000431 copper oxide Inorganic materials 0.000 description 3
- 239000000843 powder Substances 0.000 description 3
- 238000000629 steam reforming Methods 0.000 description 3
- 239000011787 zinc oxide Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 2
- 239000000654 additive Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 2
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000005554 pickling Methods 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 229910000287 alkaline earth metal oxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000000911 decarboxylating effect Effects 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 238000009377 nuclear transmutation Methods 0.000 description 1
- 125000001741 organic sulfur group Chemical group 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 235000017557 sodium bicarbonate Nutrition 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 150000004763 sulfides Chemical class 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Catalysts (AREA)
- Industrial Gases (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、液化石油ガス（ＬＰＧ）を原料として高カロ
リーの都市ガスを製造する方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION [Industrial Application Field] The present invention relates to a method for producing high-calorie city gas using liquefied petroleum gas (LPG) as a raw material.
ＬＰＧを改質して都市ガスに適する品質にするために従
来はＬＰＧをスチーム改質し、次に銅−亜鉛系触媒でｃ
ｏ変成してＣｏｆＩＡ度を減少させ、更に銅−亜鉛系触
媒でＣＯ濃度を低下させていた（社団法人日本ガス協会
、［第３７回都市シンポジウム講演要旨集、Ｐ１４〜１
５、平成元年」）。Conventionally, in order to reform LPG to a quality suitable for city gas, LPG was reformed with steam, and then treated with a copper-zinc catalyst.
o modification to reduce the CofIA degree, and a copper-zinc catalyst to reduce the CO concentration (Japan Gas Association, [37th Urban Symposium Lecture Abstracts, P14-1
5. 1989).
そのフローシートの概略を第２図に示す。すなわち、Ｌ
ＰＧは図面左方よりスチームとともにスチーム改質基１
に入って改質が行なわれ、次に銅−亜鉛系触媒に脱硫剤
として酸化亜鉛触媒を充填した第１ＣＯ変成塔２でｃｏ
変成が行なわれる。An outline of the flow sheet is shown in Figure 2. That is, L
PG is steam modified group 1 with steam from the left side of the drawing.
Co
Transmutation takes place.
そのオフガスは熱交換器３で熱交換が行なわれる。The off-gas undergoes heat exchange in a heat exchanger 3.
そこで、ＣＯ濃度５％以下にまで低下させて、ＬＰＧを
添加して製品ガスとされていた。この方法におけるガス
の組成等の変化の一例を表１に示す。Therefore, the CO concentration was lowered to 5% or less and LPG was added to produce a product gas. Table 1 shows an example of changes in gas composition, etc. in this method.
表１
［発明が解決しようとする課題］
この方法は１２Ａ、１３Ａ等の高カロリーガスの規格値
に入りにくい問題があった。Table 1 [Problems to be Solved by the Invention] This method has a problem in that it is difficult to meet the standard values of high-calorie gases such as 12A and 13A.
本発明は上記課題を解決した高カロリーガスの製造方法
を提供するものである。The present invention provides a method for producing high-calorie gas that solves the above problems.
すわなち、本発明は液化石油ガスの改質ガスを酸化鉄を
主成分とする触媒に接触させて硫黄化合物を除去し、Ｃ
Ｏ変成後ニッケル−アルミナ系触媒に接触させて該ガス
中の一酸化炭素と水素を反応させてメタンを生成させ、
必要により液化石油ガス添加を行なうことを特徴とする
液化石油ガス改質ガスの高カロリー化方法に関するも′
のである。That is, the present invention removes sulfur compounds by bringing reformed gas of liquefied petroleum gas into contact with a catalyst containing iron oxide as a main component, and
After O modification, contact with a nickel-alumina catalyst to react carbon monoxide and hydrogen in the gas to generate methane,
This invention also relates to a method for increasing the calorie content of liquefied petroleum gas reformed gas, which is characterized by adding liquefied petroleum gas as necessary.
It is.
本発明の方法は、ＬＰＧをスチーム改質等によってクラ
ンキングしたガス、又はこれをさらに改質したガスに適
用するものであり、例えば第２図のプロセスにおいては
※印で示す位置のスチーム改質ガスが好ましい。The method of the present invention is applied to a gas obtained by cranking LPG by steam reforming or the like, or to a gas further reformed. For example, in the process shown in Fig. 2, steam reforming is performed at the positions marked with Gas is preferred.
酸化鉄を主成分とする触媒は担体に酸化鉄（αＦ ｅｘ
Ｏ３）と酸化亜鉛（ＺｎＯ）及び酸化銅（Ｃｕｂ）を
担持し、これに塩基性化合物を添加したものである。担
体はＣａＯ１Ｓｉｎ、、Ａｆ２０３、ＭｇＯ１Ｔｉ○２
等を単独あるいは適宜混合したものである。Catalysts containing iron oxide as the main component contain iron oxide (αF ex
ZnO3), zinc oxide (ZnO), and copper oxide (Cub) are supported, and a basic compound is added thereto. The carrier is CaO1Sin, Af203, MgO1Ti○2
etc. alone or in an appropriate mixture.
酸化鉄は、α−Ｆｅｚ０３を主とするもので粒径６０ｐ
以下の超微粉が好ましい。このような酸化鉄超微粉は鉄
粉を希塩酸等に溶解した溶液を燃料とともに７００〜８
００°Ｃで噴霧して焙焼することにより得ることができ
る。ＺｎＯ及びＣｕＯは市販されている工業用のものを
そのまま使用することができる。Iron oxide is mainly α-Fez03 and has a particle size of 60p.
The following ultrafine powders are preferred. This type of ultrafine iron oxide powder is produced by mixing a solution of iron powder in dilute hydrochloric acid, etc. with a fuel of 700 to 8
It can be obtained by spraying and roasting at 00°C. Commercially available industrial ZnO and CuO can be used as they are.
これに添加される塩基性化合物はアルカリ金属又はアル
カリ土類金属の酸化物及び炭酸塩が適当である。酸化物
の例としてＣａＯｌＭｇＯ等、そして炭酸塩の例として
はＮ ａ ＨＣ０３、Ｎ ａ ｚ ＣＯ：ｌ、ＣａＣＯ
３、Ｋ、ＣＯ２等を挙げることができる。The basic compounds added thereto are suitably alkali metal or alkaline earth metal oxides and carbonates. Examples of oxides include CaOlMgO, and examples of carbonates include Na HC03, Na z CO:l, CaCO
3, K, CO2, etc.
触媒の組成としては酸化鉄３０〜８０重量％程度、酸化
亜鉛２〜１５重量％重量％酸化銅２〜１５重量％程度、
担体１０〜３０重量％程度、そして塩基性化合物の添加
物１〜１０重景％重量が適当である。The composition of the catalyst is approximately 30-80% by weight of iron oxide, 2-15% by weight of zinc oxide, 2-15% by weight of copper oxide,
Appropriate amounts are about 10 to 30% by weight of the carrier and 1 to 10% by weight of the basic compound additive.
この触媒の製造方法としては酸化鉄、酸化亜鉛及び酸化
銅を混合後、担体、塩基性化合物の添加物と水を加えて
混合造粒し、結晶水除去のため１００〜４００″Ｃ程度
゛で軽（焙焼すればよい。担体及び塩基性化合物は酸化
鉄等と一緒に加えてもよい。The method for producing this catalyst is to mix iron oxide, zinc oxide, and copper oxide, then add a carrier, basic compound additives, and water, granulate the mixture, and heat the mixture at about 100 to 400"C to remove crystallization water. Light (roasting may be sufficient.) A carrier and a basic compound may be added together with iron oxide, etc.
粒径は５〜２０閤程度が適当であり、７〜１５圓程度が
好ましい。The particle size is suitably about 5 to 20 g, preferably about 7 to 15 g.
この触媒は１２０〜３００℃、常圧以上の比較的低圧で
有機イオウ、ＮＯｘ及びジエン類を同時に分解すること
ができる。混合ガスの流速は空間速度（ＳＶ）で１００
〜１０００ｈｒ−’程度の範囲で使用でき、６５０ｈｒ
−’以下では極めて良好な除去成績を上げることができ
る。また、触媒の再生は少量の空気と水蒸気を送入する
ことによってＦｅｚＳ＝、ＦｅＳ等の硫化物に変化した
触媒がＦｅ、０３に再生され、長期間の継続使用が可能
である。This catalyst can simultaneously decompose organic sulfur, NOx, and dienes at a temperature of 120 to 300°C and a relatively low pressure above normal pressure. The flow velocity of the mixed gas is 100 in space velocity (SV)
It can be used within the range of ~1000hr-' and 650hr
-' or less, extremely good removal results can be achieved. Further, the catalyst is regenerated by introducing a small amount of air and water vapor, so that the catalyst that has changed to sulfides such as FezS= and FeS is regenerated to Fe and 03, allowing continuous use for a long period of time.
ＬＰＧ又はその改質ガスは、この酸化鉄系触媒塔に１０
０〜２００″Ｃ程度、好ましくは１２０〜２００″Ｃ程
度に加熱して送入する。そうすると、この塔内で硫黄化
合物質等が除去され、その後ＣＯ変成する。LPG or its reformed gas is fed to this iron oxide catalyst tower at a rate of 10
It is heated to about 0 to 200''C, preferably about 120 to 200''C, and then fed. Then, sulfur compounds and the like are removed in this column, and then CO is converted.
このオフガスをニッケル−アルミナ系触媒に接触させて
該混合ガス中の一酸化炭素と二酸化炭素に水素を反応さ
せてメタンを生成させる。This off-gas is brought into contact with a nickel-alumina catalyst to cause carbon monoxide and carbon dioxide in the mixed gas to react with hydrogen to produce methane.
この反応により温度が２００〜３００″Ｃ程度上昇する
ので、この熱を熱交換等で回収してから熱量調節を行な
い、製品ガス化する。This reaction raises the temperature by about 200-300''C, so this heat is recovered by heat exchange or the like, and then the amount of heat is adjusted and the product is gasified.
ＬＰＧ改質ガスに酸化鉄系触媒を作用させることによっ
てＨ２Ｓ、ＣＯ３，Ｃ５２、メルカプタン、ＮＯｘ等を
除去し、ＣＯ変成後ニッケル−アルミナ触媒を作用させ
ることによってガス中のＣＯとＨ２を反応させてＣＨ，
に変え、さらに脱炭酸を必要によりＬＰＧ添加を行なう
ことにより、高カロリー都市ガスとして使用しうるガス
を調製している。H2S, CO3, C52, mercaptan, NOx, etc. are removed by applying an iron oxide catalyst to LPG reformed gas, and after CO conversion, CO and H2 in the gas are reacted by applying a nickel-alumina catalyst. CH,
Gas that can be used as high-calorie city gas is prepared by decarboxylating and adding LPG if necessary.
〔実施例〕
第２図に示す従来のプロセスのスチーム改質基１の出口
に第１図に示す装置を接続した。この装置は、酸化鉄系
触媒を充填した触媒塔４、ＣＯ変成塔５とニッケル−ア
ルミナ系触媒を充填した触媒塔６が直列に接続されてお
り、各触媒塔の出口側には熱交換器７．８が接続されて
いる。そして、熱交換器８の出口にてＬＰＧ熱量調整用
として添加し、その後製品ガスとして取出しうるように
なっている。[Example] The apparatus shown in FIG. 1 was connected to the outlet of the steam reforming group 1 of the conventional process shown in FIG. In this device, a catalyst tower 4 filled with an iron oxide catalyst, a CO shift tower 5, and a catalyst tower 6 filled with a nickel-alumina catalyst are connected in series, and a heat exchanger is installed on the outlet side of each catalyst tower. 7.8 is connected. Then, it is added at the outlet of the heat exchanger 8 to adjust the LPG calorific value, and can then be taken out as a product gas.
このような装置を用いて、ＬＰＧから高カロリーガスの
製造を行なった。第２図のプロセスから抜出したスチー
ム改質ガスの組成は表２に示す通りである。Using such an apparatus, high calorie gas was produced from LPG. The composition of the steam reformed gas extracted from the process shown in FIG. 2 is as shown in Table 2.
触媒塔４に充填した触媒は次のようにして作製した。す
なわち、製鉄業において銅板を塩酸で酸洗するときに発
生する廃酸（ＦｅＣｆｚ２０〜３０％）を７００〜８０
０″Ｃで噴霧焙焼して粒径６〇−以下のα−Ｆｅｚ０３
粉を得た。この酸洗ダスト５０重量％にＺｎＯ１ＣｕＯ
をそれぞれ５重量％を加えて均一に混合し、ボルトラン
ドモメント（ＣａＯ６４％、５ｉ０２２％、ＡｆｚＣｈ
５％等）１５重量％と焼結鉱２３重量％及び重炭酸ソー
ダ２重量％に水を加えて均一に混練した後、７〜１５ｍ
ｍ粒径程度に造粒した。The catalyst packed in the catalyst tower 4 was prepared as follows. In other words, the waste acid (FeCfz 20-30%) generated when pickling copper plates with hydrochloric acid in the steel industry is
α-Fez03 with a particle size of 60- or less by spray roasting at 0″C
Got the powder. ZnO1CuO is added to 50% by weight of this pickling dust.
5% by weight of each were added and mixed uniformly, and Bortland moment (CaO64%, 5i022%, AfzCh
After adding water to 15% by weight of sintered ore, 23% by weight of sintered ore, and 2% by weight of bicarbonate of soda and kneading them uniformly, 7 to 15 m
It was granulated to about m particle size.
触媒塔６のニッケル−アルミナ系触媒には市販品を使用
した。A commercially available product was used as the nickel-alumina catalyst in the catalyst column 6.
触媒塔４のＳＶは６００／ｈｒ、そして触媒塔６のＳＶ
は５０００／ｈｒであり、ガス温度は触媒塔４人口が２
００°Ｃ前後、出口も３００°Ｃ前後、触媒塔６人口も
３００″Ｃ前後、出口が５００°Ｃ前後、そして熱交換
器７出口が２００°Ｃ前後であった。圧力３ ｋｇ／ｄ
のＬＰＧの混合量は４段階に変えた。The SV of catalyst tower 4 is 600/hr, and the SV of catalyst tower 6 is
is 5000/hr, and the gas temperature is 2 when the catalyst tower 4 population is 2.
The temperature was around 00°C, the outlet temperature was around 300°C, the catalyst column 6 population was around 300°C, the outlet temperature was around 500°C, and the heat exchanger 7 outlet temperature was around 200°C. Pressure 3 kg/d.
The amount of LPG mixed was changed in four stages.
運転結果を表２に示す。The operation results are shown in Table 2.
（以下余白）
次に、前記の触媒塔６のオフガスにＬＰＧを各種割合で
添加してＣｐとＷＩの関係を求めた結果を第２図に実線
で示す。一方、改質ガスをｃｏ変成しただけのガスにＬ
ＰＧを添加した場合のＣｐとＷＩの関係を同図に点線で
示す。(Left space below) Next, the relationship between Cp and WI was determined by adding LPG in various proportions to the off-gas of the catalyst tower 6, and the results are shown in FIG. 2 by solid lines. On the other hand, L
The relationship between Cp and WI when PG is added is shown by a dotted line in the figure.
本発明の方法により、容易に１２Ａ、１３Ａ等の規格に
入る高カロリーガスを製造することができる。By the method of the present invention, it is possible to easily produce high-calorie gas that meets standards such as 12A and 13A.
製造プロセスでは各触媒の寿命を大幅に延ばすことがで
き、また製品ガスからは硫黄分等がほぼ完全に診去され
ているところから配管腐食等の問題も全く生じない。In the manufacturing process, the life of each catalyst can be significantly extended, and since sulfur content is almost completely removed from the product gas, problems such as pipe corrosion do not occur at all.
第１図はＬＰＧから高カロリー都市ガスを製造するプロ
セスにおいて、本発明の実施例で使用した改造部分を示
すフローシートであり、第２図は従来例のフローシート
である。第３図は本発明の実施例で得られたガスと比較
例のガスについてＬＰＧの添加量を変えた場合のＣｐと
Ｗｌの関係を示すグラフである。FIG. 1 is a flow sheet showing a modified part used in an embodiment of the present invention in the process of producing high-calorie city gas from LPG, and FIG. 2 is a flow sheet of a conventional example. FIG. 3 is a graph showing the relationship between Cp and Wl when the amount of LPG added is changed for the gas obtained in the example of the present invention and the gas of the comparative example.
Claims (1)
に接触させて硫黄化合物を除去し、ＣＯ変成後ニッケル
−アルミナ系触媒に接触させて該ガス中の一酸化炭素と
水素を反応させてメタンを生成させ、必要により液化石
油ガス添加を行なうことを特徴とする液化石油ガス改質
ガスの高カロリー化方法The reformed gas of liquefied petroleum gas is brought into contact with a catalyst mainly composed of iron oxide to remove sulfur compounds, and after CO conversion, the reformed gas is brought into contact with a nickel-alumina catalyst to react the carbon monoxide and hydrogen in the gas. A method for increasing the calorie content of liquefied petroleum gas reformed gas, characterized by producing methane and adding liquefied petroleum gas as necessary.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2332050A JPH0774349B2 (en) | 1990-11-29 | 1990-11-29 | Method for producing high calorie gas from LPG reformed gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2332050A JPH0774349B2 (en) | 1990-11-29 | 1990-11-29 | Method for producing high calorie gas from LPG reformed gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04202292A true JPH04202292A (en) | 1992-07-23 |
| JPH0774349B2 JPH0774349B2 (en) | 1995-08-09 |
Family
ID=18250581
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2332050A Expired - Lifetime JPH0774349B2 (en) | 1990-11-29 | 1990-11-29 | Method for producing high calorie gas from LPG reformed gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0774349B2 (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58156324A (en) * | 1982-02-26 | 1983-09-17 | ザ・グツドイヤ−・タイヤ・アンド・ラバ−・カンパニ− | Desulfurizing method from gas current |
| JPS594183A (en) * | 1982-06-30 | 1984-01-10 | Fujitsu Ltd | Color detecting system |
| JPS60264304A (en) * | 1984-06-12 | 1985-12-27 | Osaka Gas Co Ltd | Apparatus for producing fuel gas |
-
1990
- 1990-11-29 JP JP2332050A patent/JPH0774349B2/en not_active Expired - Lifetime
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS58156324A (en) * | 1982-02-26 | 1983-09-17 | ザ・グツドイヤ−・タイヤ・アンド・ラバ−・カンパニ− | Desulfurizing method from gas current |
| JPS594183A (en) * | 1982-06-30 | 1984-01-10 | Fujitsu Ltd | Color detecting system |
| JPS60264304A (en) * | 1984-06-12 | 1985-12-27 | Osaka Gas Co Ltd | Apparatus for producing fuel gas |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0774349B2 (en) | 1995-08-09 |
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