JPH0692333B2 - Pressure distillation method of methanol plant - Google Patents
Pressure distillation method of methanol plantInfo
- Publication number
- JPH0692333B2 JPH0692333B2 JP60167410A JP16741085A JPH0692333B2 JP H0692333 B2 JPH0692333 B2 JP H0692333B2 JP 60167410 A JP60167410 A JP 60167410A JP 16741085 A JP16741085 A JP 16741085A JP H0692333 B2 JPH0692333 B2 JP H0692333B2
- Authority
- JP
- Japan
- Prior art keywords
- column
- pressure
- distillation
- reboiler
- reformed gas
- 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 - Lifetime
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Classifications
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
【発明の詳細な説明】 (産業上の利用分野) 本発明はメタノールプラントの加圧蒸留法に関し、特に
プラントのエネルギ原単位を改善すべく、リフオーマ出
口ガスの加圧蒸留プロセスに於いて新規な熱回収技術を
適用した上記蒸留法に関する。Description: FIELD OF THE INVENTION The present invention relates to a pressure distillation method for a methanol plant, and in particular to a novel process in the pressure distillation process of a refumaer outlet gas in order to improve the energy consumption rate of the plant. The present invention relates to the above distillation method to which a heat recovery technique is applied.
(従来の技術) 蒸留プロセスに於けるエネルギ原単位の改善という観点
より、近年加圧蒸留により多重効用を利用した各種のプ
ロセスが検討されている(例えばInd.Eng.Chem.Process
Des.Dev.1983,22,175-179,特開昭53-112803号公報、特
開昭56-123926号公報等)。(Prior Art) Various processes utilizing multiple effects by pressure distillation have been studied in recent years from the viewpoint of improving the energy consumption rate in the distillation process (eg, Ind.Eng.Chem.Process).
Des. Dev. 1983, 22, 175-179, JP-A-53-112803, JP-A-56-123926, etc.).
しかしながら、これらは蒸留系内のエネルギ原単位につ
いてのみの検討であり、改質ガスの熱エネルギ利用を考
慮したプラント全体のエネルギ原単位を改善するという
検討はなされていなかつた。However, these are only studies on the energy intensity of the distillation system, and no study has been made to improve the energy intensity of the entire plant in consideration of the utilization of the heat energy of the reformed gas.
すなわち、加圧蒸留の採用により、加圧精留塔の塔底温
度が高く、改質ガスの廃熱の低温域がプロセスに回収で
きぬ為、その分高温の熱が必要となり、総合的には最高
でない第3図の如きプロセスが利用されることが多かつ
た。なお、第3図中、12は加圧精留塔、13は常圧精留
塔、14は加圧精留塔改質ガスリボイラ、17は加圧精留塔
水蒸気リボイラ、18は加圧精留塔リフラツクスコンデン
サである。That is, by adopting the pressure distillation, the bottom temperature of the pressure rectification column is high, and the low temperature region of the waste heat of the reformed gas cannot be recovered in the process. Often, a process such as Figure 3 that is not the best is used. In FIG. 3, 12 is a pressure rectification column, 13 is an atmospheric rectification column, 14 is a pressure rectification column reforming gas reboiler, 17 is a pressure rectification column steam reboiler, and 18 is a pressure rectification column. It is a tower refractory condenser.
そしてこの大量の余剰廃熱により、冷却水流量あるいは
エアクーラ・フアン動力が増加し、さらにエネルギ原単
位を低下させる原因ともなつていた。This large amount of excess waste heat also increased the flow rate of cooling water or the power of the air cooler / fan, which also caused a reduction in the energy consumption rate.
(発明が解決しようとする問題点) 本発明は、このような低位の余剰廃熱を有効利用し、エ
ネルギ原単位の改善を図るもので、メタノールプラント
の加圧蒸留プロセスに於て、リフオーマ出口ガスの熱エ
ネルギを有効に利用し、低位の廃熱を減少させ、プロセ
スのエネルギ原単位を改善する方法を提案するものであ
る。(Problems to be Solved by the Invention) The present invention is intended to improve the energy consumption rate by effectively utilizing such a low-level surplus waste heat. In the pressure distillation process of a methanol plant, the refiner outlet is used. The present invention proposes a method for effectively utilizing the thermal energy of gas, reducing low-level waste heat, and improving the energy intensity of the process.
(問題点を解決するための手段) 本発明は、脱硫された炭化水素含有ガスを30気圧以上の
圧力に於ける水蒸気及び酸素の2段階の改質工程によ
り、水蒸気含有率が単なる水蒸気改質反応により可能な
水蒸気含有率よりも低いメタノール合成原料ガスに改質
し、かつ合成工程にて生成される8〜30重量%の水を含
む合成粗メタノールが初留塔にてその低沸点副生物が除
去され、続いて常圧塔と加圧塔の2塔から構成された精
留部により蒸留される如き改質、合成及び蒸留工程より
なるメタノールプロセスに於て、 (1) 初留塔の加熱用熱源としては、改質ガスが初留
塔の塔底温度よりも5〜25℃高い温度(すなわち70〜11
5℃)まで熱回収されるリボイラにより賄われ、 (2) 加圧精留塔の加熱用熱源としては、改質ガスが
該精留塔の塔底温度よりも5〜25℃高い温度(すなわち
135〜225℃)まで熱回収されるリボイラ及び水蒸気を熱
源とするリボイラにより賄われ、 (3) 常圧精留塔の加熱用熱源としては、加圧精留塔
の塔頂ガスによる多重効用リボイラ及び改質ガスが該精
留塔の塔底温度よりも5〜25℃高い温度(すなわち、11
0〜150℃)まで熱回収されるリボイラにより賄われる、 上記のうち少くとも2つを組み合わせ、改質ガスは塔底
温度の高い塔から低い塔へ直列に流れるようにしたこと
を特徴とする、改質ガスの熱エネルギを有効に回収しプ
ラント全体のエネルギ消費量を減少させることができる
メタノールプラントの加圧蒸留法に関する。(Means for Solving Problems) The present invention is a steam reforming process in which a desulfurized hydrocarbon-containing gas is subjected to a two-stage reforming process of steam and oxygen at a pressure of 30 atm or higher to simply reform the steam. Synthetic crude methanol containing 8 to 30% by weight of water, which is reformed into a methanol synthesis raw material gas having a lower water vapor content than possible by the reaction and which contains 8 to 30% by weight of water, is a low boiling by-product in the initial distillation column. In a methanol process consisting of reforming, synthesis and distillation steps such that the distillate is removed and subsequently distilled by a rectification section composed of two columns, an atmospheric column and a pressure column, (1) As a heat source for heating, the temperature of the reformed gas is 5 to 25 ° C higher than the bottom temperature of the initial distillation column (that is, 70 to 11 ° C).
(2) As a heat source for heating the pressurized rectification column, the reformed gas is at a temperature 5 to 25 ° C. higher than the bottom temperature of the rectification column (that is, 5 ° C.).
It is covered by a reboiler that recovers heat up to 135 to 225 ° C) and a reboiler that uses steam as a heat source. (3) As a heat source for heating a normal pressure rectification column, a multi-effect reboiler using overhead gas of a pressure rectification column And the temperature of the reformed gas is 5 to 25 ° C. higher than the bottom temperature of the rectification column (that is, 11
It is covered by a reboiler that recovers heat from 0 to 150 ° C), characterized in that at least two of the above are combined so that the reformed gas flows in series from a column with a high bottom temperature to a column with a low bottom temperature. The present invention relates to a pressure distillation method for a methanol plant capable of effectively recovering the thermal energy of the reformed gas and reducing the energy consumption of the entire plant.
単なるスチーム・リフオーマにより改質されたガス中に
は CH4+H2O→CO+3H2の反応により多量のH2が含まれ
る。一方、本発明で採用するスチーム・リフオーマの後
流にオートサーマル・リフオーマを設置する2段改質工
程では、オートサーマル・リフオーマに供給するO2量に
より、メタノール合成に対し余分のH2を水蒸気に変換す
ることができ、かつ高温下でのリフオーミングが可能と
なる為、改質圧力も上げることが可能となる。このH2O
濃度及び圧力の違いにより改質ガス熱回収法が、単なる
スチーム・リフオーマによる方法と、2段改質工程を採
用する本発明とでは変わることになる。A large amount of H 2 is contained in the gas reformed by mere steam reformer due to the reaction of CH 4 + H 2 O → CO + 3H 2 . On the other hand, in the two-stage reforming process in which the autothermal refumer is installed in the downstream of the steam refumer used in the present invention, excess H 2 is vaporized for methanol synthesis depending on the amount of O 2 supplied to the autothermal refumer. The reforming pressure can also be increased because the reforming pressure can be converted to the above and refforming can be performed at a high temperature. This H 2 O
Due to the difference in the concentration and the pressure, the reformed gas heat recovery method is different between the method using a simple steam reformer and the present invention that employs a two-stage reforming process.
そして、本発明によれば、蒸留系外からの熱負荷を最小
とする蒸留プロセスを採用することが、かならずしもプ
ラントのエネルギ原単位を最小とすることにはならぬこ
とがわかる。Further, according to the present invention, it is understood that adopting the distillation process that minimizes the heat load from the outside of the distillation system does not necessarily minimize the energy consumption rate of the plant.
以下、これを具体例に基き説明する。尚、説明はLS/F
(Light-Split/Heat-lntegration-Forward)のプロセス
に基き行うが、本発明はこのLS/Fのみでなく、あらゆる
加圧蒸留プロセスに対し有効である。Hereinafter, this will be described based on a specific example. The explanation is LS / F
(Light-Split / Heat-lntegration-Forward) process, but the present invention is effective not only for this LS / F but also for any pressure distillation process.
なお、LS/Fとは、加圧塔に供給し、塔頂から製品を抜
き、塔底液をその常圧塔に供給し、その塔頂から製品
を、塔底から水を、中間の段から側流を抜出すようなフ
ロー(第1〜3図参照)をいい、1塔目で軽い成分(製
品)の一部を抜き、熱の受授がプロセス全体の流れに対
して順方向である為、LS/Fと呼ぶ。In addition, LS / F is supplied to the pressure tower, the product is removed from the top of the tower, the bottom liquid is supplied to the atmospheric tower, the product is supplied from the top, and the water is supplied from the bottom to the intermediate stage. A side flow is extracted from the above (see Figs. 1 to 3), and in the first tower, a part of the light component (product) is extracted, and the transfer of heat is in the forward direction with respect to the flow of the whole process. Therefore, it is called LS / F.
(1) 比較される2プロセス(従来法と本発明法) 本発明法と従来法における加圧蒸留に於ける改質ガス熱
量の回収フローを第1図と第2図に示す。(1) Two Processes to be Compared (Conventional Method and Present Invention Method) FIG. 1 and FIG. 2 show recovery flows of the reforming gas heat quantity in the pressure distillation in the present invention method and the conventional method.
第2図は、蒸留系外からの熱負荷の最も少ない(すなわ
ち、蒸留のエネルギ原単位の最も小さい)プロセスにお
けるフローである。この熱回収フローは従来の加圧蒸留
に於いてよく用いられるフローであり、以後これを“従
来法”と称する。FIG. 2 is a flow in the process in which the heat load from the outside of the distillation system is the smallest (that is, the energy intensity of distillation is the smallest). This heat recovery flow is a flow often used in conventional pressure distillation, and will be referred to as "conventional method" hereinafter.
従来法では、加圧精留塔12の熱源は、リフオーマー出口
ガスと水蒸気によるリボイラ14,17により賄われ、常圧
精留塔13及び初留塔11の熱源は、多重効用により、加圧
精留塔12のリフラツクスコンデンサ18,18より与えられ
ている。In the conventional method, the heat source of the pressurized rectification column 12 is covered by the reboilers 14 and 17 using the reformer outlet gas and steam, and the heat sources of the atmospheric rectification column 13 and the primary distillation column 11 are pressurized rectified by multiple effects. It is provided by refraction condensers 18 and 18 of the distillation column 12.
第1図は、本発明の一例を示すフローである。本発明法
によれば、精留に必要な熱量は従来法より増えるが、低
位の熱回収が増えるためにプラントのエネルギ消費量は
少くなる。以後これを“本発明法”と称する。FIG. 1 is a flow showing an example of the present invention. According to the method of the present invention, the amount of heat required for rectification is increased as compared with the conventional method, but the energy consumption of the plant is reduced due to the increase in the lower heat recovery. Hereinafter, this is referred to as the “method of the present invention”.
本発明法では、初留塔11の加熱用熱源はリフオーマ出口
ガスの廃熱によりリボイラ16により賄われ、加圧精留塔
12は、リフオーマ出口ガスの廃熱とリボイラ17による水
蒸気をその熱源とし常圧精留塔13は、多重効用による加
圧精留塔12の塔頂ガス及びリフオーマ出口ガスによるリ
ボイラ18,15によりその熱源が賄われている。なお、第
1図中の20は気液分離器を示している。In the method of the present invention, the heat source for heating the first distillation column 11 is covered by the reboiler 16 by the waste heat of the refumeer outlet gas, and the pressure rectification column is used.
12 uses waste heat of the refumeer outlet gas and steam from the reboiler 17 as its heat source, and the normal pressure rectification column 13 uses the reboilers 18 and 15 with the overhead gas of the pressure rectification column 12 and the reformer outlet gas due to multiple effects. The heat source is covered. In addition, 20 in FIG. 1 has shown the gas-liquid separator.
(2) 総合エネルギ原単位 水蒸気及び酸素の2段階改質工程より流出する35気圧の
改質ガスの廃熱を熱源の一部とする2500t/dメタノール
のLS/F蒸留プロセスを具体例とし、以下そのエネルギ原
単位を、従来法(第2図)と本発明法(第1図)に基づ
き比較する。(2) Total energy intensity As a specific example, the LS / F distillation process of 2500 t / d methanol, which uses waste heat of 35 atm reformed gas flowing out of the two-stage reforming process of steam and oxygen as part of the heat source, The energy intensity will be compared below based on the conventional method (Fig. 2) and the method of the present invention (Fig. 1).
各蒸留塔11〜13のリボイラー熱量及び多重効用される加
圧精留塔12のリフラツクスコンデンサ18熱量を示したの
が第1表である。Table 1 shows the calorific value of the reboiler of each of the distillation columns 11 to 13 and the calorific value of the refractory condenser 18 of the pressurized rectification column 12 having multiple effects.
上表より明らかな如く蒸留系外からの熱負荷、すなわち
蒸留のエネルギ消費量だけを比較すると、本発明法より
も従来法の蒸留プロセスの方が10.9MMKcal/hだけ優つて
いる。 As is clear from the above table, when comparing only the heat load from outside the distillation system, that is, the energy consumption of distillation, the conventional distillation process is superior to the method of the present invention by 10.9 MMKcal / h.
しかしながら各蒸留塔の改質ガスリボイラ及び水蒸気リ
ボイラ熱量と改質ガスリボイラ後流に設置される脱気器
給水予熱器19の熱量、そしてプロセスには回収されない
改質ガスの余剰エネルギを示している第2表より明らか
な如く本発明法では改質ガスの低温廃熱が効果的に利用
されたことにより水蒸気リボイラの熱量は逆に17.9MMca
l/hr少くなつている。さらに、本発明法では、従来、余
剰廃熱として回収されなかつた熱量が18.8MMKcal/hrも
少くなり、冷却水所要量の低下、あるいはエアクーラの
フアン動力の低下をもたらす。However, the heat quantity of the reformed gas reboiler and steam reboiler of each distillation column, the heat quantity of the deaerator feedwater preheater 19 installed downstream of the reformed gas reboiler, and the surplus energy of the reformed gas that is not recovered in the process As is clear from the table, in the method of the present invention, the low-temperature waste heat of the reformed gas was effectively used, so that the heat quantity of the steam reboiler was 17.9 MMca
l / hr is decreasing. Furthermore, in the method of the present invention, the amount of heat that has not been recovered as surplus waste heat is reduced by 18.8 MMKcal / hr, and the required amount of cooling water is reduced or the fan power of the air cooler is reduced.
以上のように、本発明法は従来法と比し、蒸留原単位だ
け比べれば劣つているものの総合的には改質ガス熱量を
効果的に回収することができ、省エネルギ型のプロセス
となつていることがわかる。 As described above, the method of the present invention is inferior to the conventional method when compared with the distillation unit, but it is possible to effectively recover the calorific value of the reformed gas as a whole, and it is a process of energy saving type. You can see that
上記の比較は、35気圧の改質ガスより熱回収することを
設定したが、この改質圧力が下がる程、その露点も下が
る為、ますます低温域の余剰熱量が増し、したがつて、
本発明法によるエネルギ原単位の改善度はますます大き
くなる。In the above comparison, it was set to recover heat from the reformed gas of 35 atm, but the lower the reforming pressure, the lower the dew point, so the surplus heat amount in the low temperature region increases, and therefore,
The degree of improvement in the energy consumption rate by the method of the present invention becomes even greater.
尚、第1図のフローは、本発明に基くプロセスの一例で
あり、蒸留系の加圧度、改質系の圧力や熱回収法により
3つの改質ガスリボイラ14〜16のうちの1つを省くこと
も可能である。The flow of FIG. 1 is an example of the process based on the present invention, and one of the three reformed gas reboilers 14 to 16 is selected depending on the pressure of the distillation system, the pressure of the reforming system and the heat recovery method. It is possible to omit it.
第1図は本発明蒸留プロセスの一例を示すフロー図、第
2図及び第3図は多重効用を利用した加圧蒸留に於いて
従来よく使用されるフローの一例を示す図である。FIG. 1 is a flow chart showing an example of the distillation process of the present invention, and FIGS. 2 and 3 are diagrams showing an example of a flow often used conventionally in pressure distillation utilizing multiple effects.
フロントページの続き (72)発明者 守田 和裕 東京都千代田区丸の内2丁目5番1号 三 菱重工業株式会社内 (72)発明者 村山 勝利 新潟県新潟市松浜町3500番地 (72)発明者 橋本 修 新潟県新潟市松浜町3500番地 (56)参考文献 特開 昭53−112803(JP,A) 特開 昭53−79807(JP,A) 特開 昭55−45637(JP,A) 特開 昭56−123926(JP,A) 特公 昭50−16338(JP,B1)Front page continued (72) Inventor Kazuhiro Morita 2-5-1, Marunouchi, Chiyoda-ku, Tokyo Sanryo Heavy Industries Co., Ltd. (72) Inventor Masaru Murayama 3500 Matsuhama-cho, Niigata City, Niigata Prefecture (72) Inventor Osamu Hashimoto Niigata 3500, Matsuhama-cho, Niigata City, Japan (56) Reference JP-A-53-112803 (JP, A) JP-A-53-79807 (JP, A) JP-A-55-45637 (JP, A) JP-A-56-123926 (JP, A) JP-B-50-16338 (JP, B1)
Claims (1)
の圧力に於ける水蒸気及び酸素の2段階の改質工程によ
り、水蒸気含有率が単なる水蒸気改質反応により可能な
水蒸気含有率よりも低いメタノール合成原料ガス(改質
ガス)に改質し、かつ合成工程にて生成される8〜30重
量%の水を含む合成粗メタノールが初留塔にてその低沸
点副生物が除去され、続いて常圧塔と加圧塔の2塔から
構成された精留部により蒸留される如き改質、合成及び
蒸留工程よりなるメタノールプロセスに於て、 (1) 初留塔の加熱用熱源としては、改質ガスが初留
塔の塔底温度よりも5〜25℃高い温度(すなわち、70〜
115℃)まで熱回収されるリボイラにより賄われ、 (2) 加圧精留塔の加熱用熱源としては、改質ガスが
該精留塔の塔底温度よりも5〜25℃高い温度(すなわ
ち、135〜225℃)まで熱回収されるリボイラ及び水蒸気
を熱源とするリボイラにより賄われ、 (3) 常圧精留塔の加熱用熱源としては、加圧精留塔
の塔頂ガスによる多重効用リボイラ及び改質ガスが該精
留塔の塔底温度よりも5〜25℃高い温度(すなわち、11
0〜150℃)まで熱回収されるリボイラ、及び必要ならば
水蒸気を熱源とするリボイラにより賄われる、 上記のうち少くとも2つを組み合わせ、改質ガスは塔底
温度の高い塔から低い塔へ直列に流れるようにしたこと
を特徴とする、改質ガスの熱エネルギを有効に回収しプ
ラント全体のエネルギ消費量を減少させることができる
メタノールプラントの加圧蒸留法。1. A desulfurized hydrocarbon-containing gas is subjected to a two-stage reforming process of steam and oxygen at a pressure of 30 atm or more so that the steam content is higher than that which can be obtained by a simple steam reforming reaction. Low-boiling by-products are removed in a first distillation column from synthetic crude methanol that is reformed to a low methanol synthesis raw material gas (reformed gas) and that contains 8 to 30% by weight of water produced in the synthesis step, Then, in a methanol process consisting of reforming, synthesis and distillation steps such as being distilled by a rectification section composed of two columns of an atmospheric pressure column and a pressure column, (1) As a heat source for heating the first distillation column Is the temperature at which the reformed gas is 5 to 25 ° C. higher than the bottom temperature of the first distillation column (that is, 70 to
(2) As a heat source for heating the pressurized rectification column, the reformed gas is 5 to 25 ° C. higher than the bottom temperature of the rectification column (ie , 135 to 225 ℃) is recovered by a reboiler and steam-based reboiler. (3) As a heat source for heating a normal pressure rectification column, multiple effects by top gas of a pressure rectification column The temperature of the reboiler and the reformed gas is 5 to 25 ° C. higher than the bottom temperature of the rectification column (that is, 11
It is covered by a reboiler that recovers heat up to 0 to 150 ° C) and, if necessary, a reboiler that uses steam as a heat source. At least two of the above are combined and the reformed gas flows from a tower with a high bottom temperature to a tower with a low bottom temperature. A pressure distillation method for a methanol plant capable of effectively recovering the thermal energy of the reformed gas and reducing the energy consumption of the entire plant, which is characterized in that they flow in series.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60167410A JPH0692333B2 (en) | 1985-07-31 | 1985-07-31 | Pressure distillation method of methanol plant |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60167410A JPH0692333B2 (en) | 1985-07-31 | 1985-07-31 | Pressure distillation method of methanol plant |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS6229540A JPS6229540A (en) | 1987-02-07 |
JPH0692333B2 true JPH0692333B2 (en) | 1994-11-16 |
Family
ID=15849176
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP60167410A Expired - Lifetime JPH0692333B2 (en) | 1985-07-31 | 1985-07-31 | Pressure distillation method of methanol plant |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPH0692333B2 (en) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP4773641B2 (en) * | 2001-07-19 | 2011-09-14 | 三菱重工業株式会社 | Method for producing methanol |
CN1317248C (en) * | 2005-10-27 | 2007-05-23 | 天津大学 | Energy saving equipment of double effect rectification for methanol, and method |
CN100378051C (en) * | 2006-06-13 | 2008-04-02 | 天津大学 | Rectifying tech. and equipment of high purity methanol |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5016338A (en) * | 1973-06-18 | 1975-02-20 | ||
GB1592949A (en) * | 1976-12-22 | 1981-07-15 | Ici Ltd | Methanol |
IN148355B (en) * | 1977-03-11 | 1981-01-24 | Ici Ltd | |
JPS5545637A (en) * | 1978-09-28 | 1980-03-31 | Continental Oil Co | Methanol plant |
JPS56123926A (en) * | 1980-03-06 | 1981-09-29 | Toyo Eng Corp | Purification of methanol |
-
1985
- 1985-07-31 JP JP60167410A patent/JPH0692333B2/en not_active Expired - Lifetime
Also Published As
Publication number | Publication date |
---|---|
JPS6229540A (en) | 1987-02-07 |
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