JPS62153387A - Manufacture of methane-rich gas - Google Patents
Manufacture of methane-rich gasInfo
- Publication number
- JPS62153387A JPS62153387A JP29533885A JP29533885A JPS62153387A JP S62153387 A JPS62153387 A JP S62153387A JP 29533885 A JP29533885 A JP 29533885A JP 29533885 A JP29533885 A JP 29533885A JP S62153387 A JPS62153387 A JP S62153387A
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- JP
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- Prior art keywords
- steam
- gas
- reactor
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- supplied
- 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.)
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- Hydrogen, Water And Hydrids (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Industrial Gases (AREA)
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は炭化水素又はメタノールを水蒸気改質して、都
市ガス等に使用されるメタンリッチガスを製造する方法
に関するものであって、特に、中小規模でメタンリッチ
ガスを製造する場合に好適な炭化水素又はメタノールの
水蒸気改質方法に係る。Detailed Description of the Invention [Field of Industrial Application] The present invention relates to a method of steam reforming hydrocarbons or methanol to produce methane-rich gas used as city gas, etc. The present invention relates to a method for steam reforming hydrocarbons or methanol suitable for producing methane-rich gas on a large scale.
［従来の技術］
ＬＰＧ、ナフサ等の炭化水素又はメタノールを断熱的に
水蒸気改質してメタンリッチガスを製造する場合、従来
は通常のボイラーで発生させた水蒸気を、炭化水素又は
メタノールに混合し、この混合物をのヒーターで予熱し
てから改質反応器に供給する方法が一般に採用されてい
る。つまり、従来法では改質反応に必要な水蒸気を発生
させるためのボイラーと、炭化水素又はメタノールの混
合物を改質反応温度に予熱するためのヒーターに、それ
ぞれ加熱炉を必要とするのが通常である。そして、原料
として含硫黄炭化水素を用いる場合には、これを水蒸気
改質するに先立ち水素化脱硫しなければならない関係で
、上記の二つの加熱炉に加えて、原料炭化水素と水添用
水素を脱硫温度に昇温するための加熱炉が必要とされる
。[Prior Art] When producing methane-rich gas by adiabatically steam reforming hydrocarbons such as LPG, naphtha, or methanol, conventionally, steam generated in a normal boiler is mixed with the hydrocarbon or methanol, A method generally employed is to preheat this mixture with a heater before supplying it to the reforming reactor. In other words, conventional methods usually require a heating furnace for the boiler to generate the steam necessary for the reforming reaction and the heater for preheating the hydrocarbon or methanol mixture to the reforming reaction temperature. be. When sulfur-containing hydrocarbons are used as raw materials, they must be hydrodesulfurized before steam reforming, so in addition to the two heating furnaces mentioned above, the raw material hydrocarbons and hydrogen for hydrogenation must be A heating furnace is required to raise the temperature to the desulfurization temperature.
［発明が解決しようとする問題点コ
つまり、従来の水蒸気改質法では、脱硫の要のない原料
を使用する場合でさえ、最低二つの加熱炉が必要で、こ
れに伴う付帯設備も別途膜けなければならないので、装
置全体が複雑にならざるを得ない。そして、装置が複雑
であることは、装置のスタートアップに時間を要する不
都合もある。従って、中小規模でメタンリッチガスを製
造せんとする場合には、従来の水蒸気改質法を必ずしも
好適な方法とすることができない。[Problems to be solved by the invention] In other words, in the conventional steam reforming method, even when using raw materials that do not require desulfurization, at least two heating furnaces are required, and the accompanying equipment is also separate. As a result, the entire device inevitably becomes complicated. Moreover, the complexity of the device also has the disadvantage that it takes time to start up the device. Therefore, when it is desired to produce methane-rich gas on a small to medium scale, the conventional steam reforming method is not necessarily a suitable method.
［問題点を解決するための手段］
本発明は改質反応帯域に供給される水蒸気を過熱水蒸気
に置き換えることによって、換言すれば、通常のボイラ
ーを過熱水蒸気発生器に置き換えることによって、水蒸
気改質反応に必要な水蒸気と熱量を過熱水蒸気で賄える
ようにした。従って、中小規模でメタンリッチガスを製
造する場合に適した新しい水蒸気改質法を提案する。[Means for Solving the Problems] The present invention achieves steam reforming by replacing the steam supplied to the reforming reaction zone with superheated steam, in other words, by replacing a normal boiler with a superheated steam generator. The steam and heat required for the reaction can be covered by superheated steam. Therefore, we propose a new steam reforming method suitable for producing methane-rich gas on a small to medium scale.
すなわち、本発明に係るメタンリッチガスの製造法は、
炭化水素又はメタノールに水蒸気を混合し、これを断熱
型水蒸気改質反応帯域に供給してメタンリッチガスを製
造する方法において、炭化水素又はメタノールと混合す
る水蒸気に、過熱水蒸気を使用して反応に要する熱を過
熱水蒸気で賄う事を特徴とする。That is, the method for producing methane-rich gas according to the present invention is as follows:
In a method for producing methane-rich gas by mixing steam with hydrocarbons or methanol and supplying it to an adiabatic steam reforming reaction zone, superheated steam is used to add steam to the steam to be mixed with hydrocarbons or methanol to reduce the amount required for the reaction. The feature is that the heat is provided by superheated steam.
〔作 用］
本発明において、供給原料としてはＬＰＧ、ナフサ等の
炭化水素が使用できる外、メタノールも使用可能である
。また、改質触媒には炭化水素またはメタノールの低温
水蒸気改質反応に、従来から広く使用されて来た当業界
で周知の触媒が１本発明でも使用することができる。そ
して、原料炭化水素を水蒸気改質に先立って、脱硫しな
ければならない場合には、当業界で周知の水素化脱硫触
媒を使用することができる。[Function] In the present invention, hydrocarbons such as LPG and naphtha can be used as the feedstock, and methanol can also be used. Further, as the reforming catalyst, any catalyst well known in the art that has been widely used in the low-temperature steam reforming reaction of hydrocarbons or methanol can be used in the present invention. If the feedstock hydrocarbon must be desulfurized prior to steam reforming, hydrodesulfurization catalysts well known in the art can be used.
以下第１図にそって本発明を説明すると、供給原料はラ
イン１から、また過熱水蒸気発生用の水はライン２から
それぞれ系内に導入される。The present invention will be described below with reference to FIG. 1. Feedstock is introduced into the system through line 1, and water for generating superheated steam is introduced into the system through line 2.
ライン２の水は熱交換器７で予熱されて過熱水蒸気発生
器５に送られる。ライン１の供給原料は、ライン１１か
ら供給される生成ガスの一部と混合され、熱交換器６で
水素化脱硫温度に加温された後、水素化脱硫反応器３に
導入される。Water in line 2 is preheated by heat exchanger 7 and sent to superheated steam generator 5. The feedstock in line 1 is mixed with a portion of the product gas supplied from line 11, heated to the hydrodesulfurization temperature in heat exchanger 6, and then introduced into hydrodesulfurization reactor 3.
反応器３で脱硫された供給原料は、次いで過熱水蒸気発
生器５から得られる過熱水蒸気と共に。The feedstock desulfurized in reactor 3 is then together with superheated steam obtained from superheated steam generator 5.
断熱型の水蒸気改質反応器４に導入されて水蒸気改質さ
れる。It is introduced into an adiabatic steam reforming reactor 4 and subjected to steam reforming.
ライン１を流れる供給原料が既に脱硫されているか、あ
るいは脱硫の要のない原料の場合には、当然のことなが
ら水素化脱硫反応器３が不要で、そうした原料はそのま
ま過熱水蒸気発生器５からの過熱水蒸気と共に、断熱型
水蒸気改質反応器４に導入することができる。If the feedstock flowing through the line 1 has already been desulfurized or does not require desulfurization, the hydrodesulfurization reactor 3 is of course unnecessary, and such raw material can be directly fed from the superheated steam generator 5. It can be introduced into the adiabatic steam reforming reactor 4 together with superheated steam.
断熱型水蒸気改質反応器４の出口ガスは、熱交換器６及
び７を経て冷却器８に供給されるが、この間に出口ガス
はライン１の供給原料を脱硫温度まで加熱し、ライン２
から過熱水蒸気発生器５に供給される水を予熱する。冷
却器８からの流出物は、常法通り気液分離器９に供給す
ることにより、目的生成物たるメタンリッチガスをライ
ンｌＯに得ることができる。そして、メタンリッチガス
の一部は、供給原料を水素化脱硫する場合の水素含有ガ
スとして、ライン１１に送られる。The outlet gas of the adiabatic steam reforming reactor 4 is supplied to the cooler 8 via heat exchangers 6 and 7, during which time the outlet gas heats the feedstock in line 1 to the desulfurization temperature and passes through the line 2.
The water supplied to the superheated steam generator 5 is preheated. By supplying the effluent from the cooler 8 to the gas-liquid separator 9 in a conventional manner, a methane-rich gas, which is the target product, can be obtained in the line IO. A portion of the methane-rich gas is then sent to line 11 as a hydrogen-containing gas when the feedstock is hydrodesulfurized.
本発明においては、供給原料の断熱的水蒸気改質に要す
る熱量が過熱水蒸気で賄われるが。In the present invention, the amount of heat required for adiabatic steam reforming of the feedstock is covered by superheated steam.
第２図を用いてこの点をさらに具体的に説明すると１次
の通りである。This point will be explained more specifically using FIG. 2 as follows.
すなねち、第２図は脱硫ＬＰＧと過熱水蒸気を、スチー
ム比（Ｈ２０モル／Ｃグラム原子）＝１．０で混合して
断熱型水蒸気改質反応器に供給する場合において、反応
器入口温度を４００℃又は３５０℃に維持するためには
、何度の過熱水蒸気が必要であるかを示したグラフであ
るが、例えば、断熱型水蒸気改質反応器に供給される脱
硫ＬＰＧの温度が３００℃である場合、温度約５１２℃
の過熱水蒸気を脱硫ＬＰＧに混合すれば、断熱型水蒸気
改質反応器の入口温度が４００ ’Ｃに保持されること
を第２図は示している。従って、本発明によれば、反応
器に送られる供給原料の温度に応じて、これに混合され
る過熱水蒸気の温度を調節することにより、所望の断熱
的水蒸気改質反応を進行させることができるのである。In other words, Figure 2 shows the reactor inlet when desulfurized LPG and superheated steam are mixed at a steam ratio (H20 mol/C gram atom) and supplied to an adiabatic steam reforming reactor. This is a graph showing how many times superheated steam is required to maintain the temperature at 400°C or 350°C. When it is 300℃, the temperature is about 512℃
FIG. 2 shows that the inlet temperature of the adiabatic steam reforming reactor can be maintained at 400'C by mixing superheated steam of 20% with the desulfurized LPG. Therefore, according to the present invention, the desired adiabatic steam reforming reaction can proceed by adjusting the temperature of the superheated steam mixed with the feedstock fed to the reactor according to the temperature of the feedstock fed to the reactor. It is.
尚、本発明方法を実施するに際し、そのスタートアッ′
プ時の断熱型水蒸気改質反応器４の昇温は、過熱水蒸気
発生器５からの過熱水蒸気をバイパスライン（鎖線参照
）に送り、熱交換器６．７、冷却器８、気液分離器９及
びリサイクルコンプレッサ１２を経由させて反応器３，
４を供給させることにより、これら反応器を水蒸気の露
点以上に昇温させ、しかる後、バイパスラインを閉じて
過熱水蒸気発生器５からの過熱水蒸気を反応器４に供給
することで行なうことができる。この場合、反応器内に
ドレンが発生したならば、これを反応器底部から抜き出
すことができる。In addition, when carrying out the method of the present invention, the starting point is
To raise the temperature of the adiabatic steam reforming reactor 4 at the time of pumping, the superheated steam from the superheated steam generator 5 is sent to the bypass line (see the chain line), and the heat exchanger 6.7, the cooler 8, and the gas-liquid separator 9 and a recycle compressor 12 to reactor 3,
4 to raise the temperature of these reactors above the dew point of the steam, and then close the bypass line and supply superheated steam from the superheated steam generator 5 to the reactor 4. . In this case, if condensate is generated in the reactor, it can be extracted from the bottom of the reactor.
［実 施 例］
第１図に示すフローに従って、ＬＰＧを水蒸気改質した
。[Example] LPG was steam reformed according to the flow shown in FIG.
Ｌ Ｐ Ｇ １００ｋｇ／ｈｒを６ ｋｇ／ａＪＧで蒸
発させ、これをライン１に供給し、ライン１１がらの水
素含有ガスとの混合物を、熱交換器６にて３００℃まで
昇温しで水素化脱硫反応器３に導入し、ＬＰＧの脱硫を
行なった。脱硫反応器３から流出するガスに、過熱水蒸
気発生器５から得られる温度５１５℃の過熱水蒸気１２
４ｋｇ／ｈｒを混合し、入口温度４００℃で断熱型水蒸
気改質反応器４に供給して圧力５ ｋｇ／ａＪＧで反応
させたところ、出口温度４６０℃の改質ガスが得られた
。LPG 100kg/hr is evaporated at 6 kg/aJG, this is supplied to line 1, and the mixture with hydrogen-containing gas from line 11 is heated to 300°C in heat exchanger 6 to hydrogenate. The LPG was introduced into the desulfurization reactor 3 to desulfurize LPG. Superheated steam 12 at a temperature of 515°C obtained from the superheated steam generator 5 is added to the gas flowing out from the desulfurization reactor 3.
When the mixture was mixed at 4 kg/hr and supplied to the adiabatic steam reforming reactor 4 at an inlet temperature of 400°C and reacted at a pressure of 5 kg/aJG, a reformed gas with an outlet temperature of 460°C was obtained.
この改質ガスは熱交換器６にて被加熱流体を３００℃ま
で加熱するに充分な熱量を有しており。This reformed gas has enough heat to heat the fluid to be heated to 300° C. in the heat exchanger 6.
当゛該熱交換器での熱交換によって、改質ガス自体は３
５０℃に降温した。このガスを熱交換器７に通して、冷
却器８に送り、未反応水蒸気を凝縮した後、気液分離器
９でこれを除去して次の組成のメタンリッチガスを得た
。Through heat exchange in the heat exchanger, the reformed gas itself
The temperature was lowered to 50°C. This gas was passed through a heat exchanger 7 and sent to a cooler 8 to condense unreacted water vapor, and then removed by a gas-liquid separator 9 to obtain a methane-rich gas having the following composition.
ＣＨ４６５，３容量％
Ｈ，１４，８容量％
Ｇｏ ０．９容量％
ＣＯ□ １９．０容量％
［発明の効果］
本発明の方法によれば、ＬＰＧ、ナフサ等の炭化水素又
はメタノールの水蒸気改質に必要なスチームと熱量を、
過熱水蒸気で賄うことができるので、メタンリッチガス
製造プロセスを簡略化することができ、従って、軽便な
装置と操作でメタンリッチガスを製造することができる
。CH465, 3% by volume H, 14,8% by volume Go 0.9% by volume CO□ 19.0% by volume [Effects of the invention] According to the method of the present invention, steam reforming of hydrocarbons such as LPG, naphtha, or methanol is possible. Steam and heat necessary for quality,
Since it can be supplied with superheated steam, the methane-rich gas production process can be simplified, and therefore, methane-rich gas can be produced with simple equipment and operations.
第１図は本発明方法の一実施例を示すフローシートであ
り、第２図は断熱型水蒸気改質反応器に送られるＬＰＧ
及び過熱水蒸気の温度と、反応器入口温度との関係を示
すグラフである。
３：水素化脱硫反応器 ４：断熱型水蒸気改質反応器
５：過熱水蒸気発生機 ６，７：熱交換器８：冷却器
９：気液分離器１２：リサイクルコンプレ
ッサFIG. 1 is a flow sheet showing an example of the method of the present invention, and FIG. 2 is a flow sheet showing an example of the method of the present invention, and FIG.
and is a graph showing the relationship between the temperature of superheated steam and the reactor inlet temperature. 3: Hydrodesulfurization reactor 4: Adiabatic steam reforming reactor 5: Superheated steam generator 6, 7: Heat exchanger 8: Cooler
9: Gas-liquid separator 12: Recycling compressor
Claims (1)
断熱型水蒸気改質反応帯域に供給してメタンリッチガス
を製造する方法において、炭化水素又はメタノールと混
合する水蒸気に、過熱水蒸気を使用して反応に要する熱
を過熱水蒸気で賄う事を特徴とするメタンリッチガスの
製造法。1. In a method for producing methane-rich gas by mixing steam with hydrocarbons or methanol and supplying the same to an adiabatic steam reforming reaction zone, superheated steam is used to react with the steam to be mixed with hydrocarbons or methanol. A method for producing methane-rich gas that uses superheated steam to cover the heat required for methane-rich gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60295338A JPH0613720B2 (en) | 1985-12-27 | 1985-12-27 | Method for producing methane gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60295338A JPH0613720B2 (en) | 1985-12-27 | 1985-12-27 | Method for producing methane gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62153387A true JPS62153387A (en) | 1987-07-08 |
| JPH0613720B2 JPH0613720B2 (en) | 1994-02-23 |
Family
ID=17819320
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60295338A Expired - Lifetime JPH0613720B2 (en) | 1985-12-27 | 1985-12-27 | Method for producing methane gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0613720B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002179402A (en) * | 2000-12-11 | 2002-06-26 | Toyota Motor Corp | Reforming device |
| CN106946637A (en) * | 2017-03-22 | 2017-07-14 | 中国石油大学(北京) | The device and technique of a kind of skid-mounted type lower carbon number hydrocarbons production methane |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5244802A (en) * | 1975-10-06 | 1977-04-08 | Osaka Gas Co Ltd | Preparation of high calorific value fuel gas |
| JPS5335702A (en) * | 1976-09-13 | 1978-04-03 | Metallgesellschaft Ag | Method of producing methane containing gas |
| JPS5394303A (en) * | 1977-01-31 | 1978-08-18 | Chiyoda Chem Eng & Constr Co Ltd | Preparation of methane-rich gas |
| JPS54124003A (en) * | 1978-03-04 | 1979-09-26 | Metallgesellschaft Ag | Production of fuel gas |
-
1985
- 1985-12-27 JP JP60295338A patent/JPH0613720B2/en not_active Expired - Lifetime
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5244802A (en) * | 1975-10-06 | 1977-04-08 | Osaka Gas Co Ltd | Preparation of high calorific value fuel gas |
| JPS5335702A (en) * | 1976-09-13 | 1978-04-03 | Metallgesellschaft Ag | Method of producing methane containing gas |
| JPS5394303A (en) * | 1977-01-31 | 1978-08-18 | Chiyoda Chem Eng & Constr Co Ltd | Preparation of methane-rich gas |
| JPS54124003A (en) * | 1978-03-04 | 1979-09-26 | Metallgesellschaft Ag | Production of fuel gas |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002179402A (en) * | 2000-12-11 | 2002-06-26 | Toyota Motor Corp | Reforming device |
| CN106946637A (en) * | 2017-03-22 | 2017-07-14 | 中国石油大学(北京) | The device and technique of a kind of skid-mounted type lower carbon number hydrocarbons production methane |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0613720B2 (en) | 1994-02-23 |
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