JPH0942780A - Method for heat recovery and heat utilization using chemical energy - Google Patents
Method for heat recovery and heat utilization using chemical energyInfo
- Publication number
- JPH0942780A JPH0942780A JP7190825A JP19082595A JPH0942780A JP H0942780 A JPH0942780 A JP H0942780A JP 7190825 A JP7190825 A JP 7190825A JP 19082595 A JP19082595 A JP 19082595A JP H0942780 A JPH0942780 A JP H0942780A
- Authority
- JP
- Japan
- Prior art keywords
- heat
- reaction
- formula
- carried out
- methyl formate
- 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.)
- Pending
Links
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
- Y02P20/50—Improvements relating to the production of bulk chemicals
-
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Liquid Carbonaceous Fuels (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する分野】本発明は、化学エネルギーを用い
て工場廃熱や河川水などの低温熱源の熱利用を行う方法
に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of utilizing heat of a low temperature heat source such as waste heat from a factory or river water by using chemical energy.
【０００２】[0002]
【従来の技術】従来、熱エネルギーの回収、輸送および
利用方法としては、水蒸気又は熱水を用いる方法が一般
的である。しかしこれらの方法は、熱損失および設備コ
ストの面からの制約が大きく、低温排熱の回収には限界
がある。即ち発電所、製鉄所等のエネルギー多消費型の
各種産業設備では近年省エネルギーが進行し、かなりの
部分の排熱回収が行われているが、 200〜300 ℃以下の
低温排熱は自己設備内で適切に利用する手段がないこと
から廃棄され、そのために大きな冷却負荷を要している
ことが多い。2. Description of the Related Art Conventionally, as a method of recovering, transporting and using thermal energy, a method using steam or hot water is generally used. However, these methods are greatly restricted in terms of heat loss and equipment cost, and there is a limit in recovering low-temperature exhaust heat. In other words, energy saving has been progressing in recent years in various energy-intensive industrial facilities such as power plants and steelworks, and a considerable part of waste heat recovery has been performed. Because of the lack of means for proper use, they are often discarded, which requires a large cooling load.
【０００３】近年、低温排熱を有効に回収して都市の地
域冷暖房や給湯等に利用する方法として熱エネルギーを
化学エネルギーに変えて熱回収と熱利用を行うことが検
討されている。この方法では熱回収側と熱利用側で熱エ
ネルギーと化学エネルギーの変換が必要であるが、長距
離の輸送と貯蔵が可能であり、輸送および貯蔵での熱損
失が無く、エネルギー密度が大きいことから設備コスト
面からも有利な方法とされている。In recent years, as a method of effectively recovering low-temperature exhaust heat and using it for district heating / cooling and hot water supply in cities, it has been studied to convert heat energy into chemical energy to perform heat recovery and heat utilization. This method requires the conversion of heat energy and chemical energy on the heat recovery side and heat utilization side, but it can be transported and stored over long distances, has no heat loss during transport and storage, and has a high energy density. Therefore, this method is advantageous in terms of equipment cost.
【０００４】熱エネルギーと化学エネルギーの変換系で
有力なものとしては (i)式のメタノール分解反応と(i')
式のメタノール合成反応を用いる方法が提案されてい
る。 ＣＨ3 ＯＨ ＝ ＣＯ ＋ ２Ｈ2 (i) ＣＯ ＋ ２Ｈ2 ＝ ＣＨ3 ＯＨ (i') この方法は (i)式のメタノール分解反応が吸熱反応であ
ることから (i)式を用いて排熱回収を行い、得られたＣ
Ｏ＋２Ｈ2 を輸送し、熱利用地で(i')式の発熱反応によ
り熱エネルギーの供給が行われる。(i')式により生成し
たメタノールは熱回収地に循環して再利用される。[0004] The most promising thermal and chemical energy conversion systems are the methanol decomposition reaction of formula (i) and (i ')
A method using the formula methanol synthesis reaction has been proposed. CH 3 OH = CO + 2H 2 (i) CO + 2H 2 = CH 3 OH (i ') In this method, since the methanol decomposition reaction of the formula (i) is an endothermic reaction, the exhaust heat is calculated using the formula (i). The collected C
O + 2H 2 is transported, and thermal energy is supplied to the heat utilization site by an exothermic reaction of the formula (i ′). The methanol produced by the formula (i ') is circulated to the heat recovery site and reused.
【０００５】[0005]
【発明が解決しようとする課題】(i)式および(i')式を
用いる変換系は、安価で取扱性の良いメタノールを用い
て、容易に反応を行うことができることから、エネルギ
ー変換系として有力と見られるが、次のような課題を有
している。 1).熱回収は (i)式の反応の下限温度により制約される
ことになるが、反応速度等の実用的見地から熱回収の下
限温度は 200℃前後が限界であり、排熱回収として最も
望ましい領域とされている 200〜100 ℃から常温程度の
低温度域での熱回収を行うことができない。 2).熱回収を有効に行うために (i)式の下限温度を低下
させる必要があるが、(i) 式の平衡関係は反応温度を低
下と共にメタノール分解側に著しく不利となる。 3).熱利用の面からは(i')式の反応を高温で行うことが
有利であるが、(i')式の反応の平衡関係は反応温度の上
昇と共にメタノール合成反応が著しく不利となる。また
平衡関係を改善するためにはメタノール合成反応を高圧
下で行うことになるが、装置コストおよび操業費等の点
から熱利用性が低く、反応温度および圧力特性の改善が
望まれる。 本発明の目的は、熱エネルギーと化学エネルギー変換シ
ステムにおいて、熱回収温度の下限の低下を図り、装置
コストおよび操業費等の点から熱利用性の高い方法を提
供することである。The conversion system using the formulas (i) and (i ') can be easily reacted using methanol which is inexpensive and easy to handle. Although it seems to be influential, it has the following issues. 1) .Heat recovery is limited by the lower limit temperature of the reaction in equation (i), but from a practical point of view such as the reaction rate, the lower limit temperature of heat recovery is around 200 ° C. It is not possible to recover heat in a low temperature range of 200-100 ° C, which is considered to be the most desirable range, to room temperature. 2). It is necessary to lower the lower limit temperature of equation (i) in order to perform heat recovery effectively, but the equilibrium relationship of equation (i) becomes significantly disadvantageous to the methanol decomposition side as the reaction temperature decreases. 3) From the viewpoint of heat utilization, it is advantageous to carry out the reaction of formula (i ') at a high temperature, but the equilibrium relationship of the reaction of formula (i') is such that the methanol synthesis reaction is significantly disadvantageous as the reaction temperature rises. Become. In order to improve the equilibrium relationship, the methanol synthesis reaction is performed under high pressure. However, heat utilization is low from the viewpoint of equipment cost and operation cost, and it is desired to improve the reaction temperature and pressure characteristics. It is an object of the present invention to provide a method for reducing the lower limit of the heat recovery temperature in a heat energy and chemical energy conversion system, and having a high heat utilization efficiency in terms of equipment cost, operating cost and the like.
【０００６】[0006]
【課題を解決するための手段】発明者等は上記の如き課
題を有する熱エネルギーと化学エネルギーの変換システ
ムについて鋭意検討した結果、メタノールに代えて蟻酸
メチルの分解と水素のシステムを用いることにより、排
熱回収とその利用を極めて有利に行うことができること
を見出し、本発明に到達した。Means for Solving the Problems As a result of intensive investigations by the inventors on a conversion system of thermal energy and chemical energy having the above-mentioned problems, by using a system of decomposition of methyl formate and hydrogen instead of methanol, The inventors have found that exhaust heat recovery and its utilization can be carried out extremely advantageously, and arrived at the present invention.
【０００７】即ち本発明は、 (1)式により熱回収を行
い、その逆反応(1')式により熱利用を行うことを特徴と
する化学エネルギーを用いる熱回収と熱利用の方法であ
る。 ２ＣＨ3 ＯＨ → ＨＣＯＯＣＨ3 ＋ Ｈ2 (1) ＨＣＯＯＣＨ3 ＋ Ｈ2 → ２ＣＨ3 ＯＨ (1')That is, the present invention is a method of heat recovery and heat utilization using chemical energy, characterized in that heat recovery is performed by the equation (1) and heat is utilized by the reverse reaction (1 '). 2CH 3 OH → HCOOCH 3 + H 2 (1) HCOOCH 3 + H 2 → 2CH 3 OH (1 ')
【０００８】[0008]
【発明の実施の形態】まず (1)式のメタノールの脱水素
によるギ酸メチルの分解反応は液相で行うことが好まし
く、反応を液相で行い生成Ｈ2 ガスを系外に除去するこ
とにより、平衡反応が促進されるので有利である。該反
応の触媒には、ラネー銅触媒や銅−クロム系触媒などの
銅系触媒や、担持型パラジウム触媒、Cu-Ni-Al-P触媒、
Cu-Zn-Al-P-Li 触媒などの貴金属触媒が用いられる。反
応温度は１５０〜２５０℃である。また反応時間として
は０．１〜２０ｈｒの範囲、特に０．２〜１０ｈｒが一
般的である。BEST MODE FOR CARRYING OUT THE INVENTION First, the decomposition reaction of methyl formate by dehydrogenation of methanol of the formula (1) is preferably carried out in a liquid phase, and the reaction is carried out in a liquid phase to remove generated H 2 gas out of the system. This is advantageous because the equilibrium reaction is promoted. The catalyst for the reaction includes a copper catalyst such as a Raney copper catalyst or a copper-chromium catalyst, a supported palladium catalyst, a Cu-Ni-Al-P catalyst,
Noble metal catalysts such as Cu-Zn-Al-P-Li catalysts are used. The reaction temperature is 150 to 250 ° C. The reaction time is generally in the range of 0.1 to 20 hours, particularly 0.2 to 10 hours.
【０００９】(1)式の反応の圧力は、その分解温度で示
される蒸気圧下で分解を遂行させることもできるが、平
衡的には低圧ほど有利となる。一般に反応圧力としては
常圧〜３０ａｔｍ、実用的には常圧〜２０ａｔｍの範囲
が好ましい。(1)式と(1')式の反応は化学平衡反応であ
り、気相反応では平衡組成の制約を受けるが、液相反応
とすれば生成するＨ2 ガスが直ちに液相から分離される
ことから反応上有利となる。反応方式はメタノールと触
媒とが接触する方法であれば何れの方法でも採用できる
が、一般的な反応方法としては、流動床、或いは固定床
等が挙げられる。なお反応を促進するために、反応蒸留
により水素ガスとギ酸メチルをメタノールから分離する
ようにすれば化学平衡上有利であり、たとえばワンパス
転化率が低い場合でも、反応蒸留を組み込むことにより
系内の反応率を高めることができるので、一般に用いら
れる循環方式に比べて効率の良いシステムとすることが
できる。The pressure of the reaction of the formula (1) can be carried out under the vapor pressure shown by the decomposition temperature, but the lower pressure is more advantageous in equilibrium. Generally, the reaction pressure is preferably in the range of normal pressure to 30 atm, and practically in the range of normal pressure to 20 atm. The reactions of formulas (1) and (1 ') are chemical equilibrium reactions, and the equilibrium composition is restricted in the gas phase reaction, but in the case of the liquid phase reaction, the generated H 2 gas is immediately separated from the liquid phase. This is advantageous in terms of reaction. Although any reaction method can be adopted as long as it is a method in which methanol and a catalyst come into contact with each other, a general reaction method includes a fluidized bed or a fixed bed. In order to accelerate the reaction, it is advantageous in terms of chemical equilibrium that hydrogen gas and methyl formate are separated from methanol by reactive distillation. For example, even if the one-pass conversion is low, by incorporating reactive distillation, Since the reaction rate can be increased, the system can be made more efficient than the generally used circulation system.
【００１０】前述の如く (1)式と(1')式の反応は化学平
衡反応であるので、(1')式の反応においても (1)式と同
様の銅系触媒や貴金属触媒を用いて逆反応を行うことに
より熱利用を行うことができる。熱利用を有効に行うた
めにはできるだけ高温で(1')式のメタノール合成反応を
行うことが望ましい。As described above, since the reactions of the formulas (1) and (1 ') are chemical equilibrium reactions, the same copper-based catalyst or noble metal catalyst as that of the formula (1) is used in the reaction of the formula (1'). By utilizing the reverse reaction, heat can be utilized. In order to effectively utilize heat, it is desirable to carry out the methanol synthesis reaction of the formula (1 ') at a temperature as high as possible.
【００１１】(1')式の反応においてＨＣＯＯＣＨ3 とＨ
2 ガスのモル比は理論的には１：１であるが、Ｈ2 ガス
が過剰な条件が有利であり、該モル比は１：１〜１００
である。未反応Ｈ2 ガスの循環再使用を考えると該モル
比は１：１．２〜５０とすることが好ましい。反応器ま
たは反応管から分離された未反応Ｈ2 ガスは、反応系に
循環することができる。反応圧力は５〜２００ kg/cm2
であり、好ましくは１０〜１００ kg/cm2 である。(1')
式の反応も平衡反応であり、ギ酸メチルは生成するメタ
ノールよりも低沸点であるから、反応蒸留により生成し
たメタノールを蒸留で系外に連続的に抜き出すようにす
れば、高い反応率でメタノールを容易に得ることができ
る。In the reaction of the formula (1 '), HCOOCH 3 and H
The molar ratio of the 2 gases is theoretically 1: 1 but it is advantageous under the condition that the H 2 gas is excessive, and the molar ratio is from 1: 1 to 100.
It is. Considering the recycling and reuse of unreacted H 2 gas, the molar ratio is preferably 1: 1.2 to 50. Unreacted H 2 gas separated from the reactor or reaction tube can be circulated to the reaction system. Reaction pressure is 5-200 kg / cm 2
And preferably 10 to 100 kg / cm 2 . (1 ')
The reaction of the formula is also an equilibrium reaction, and since methyl formate has a lower boiling point than the produced methanol, if the methanol produced by the reactive distillation is continuously withdrawn from the system by distillation, the methanol will be produced at a high reaction rate. Can be easily obtained.
【００１２】(1')式のギ酸メチルと水素ガスの反応の方
法はとくに制限されるものではなく、連続式方法として
触媒を管型反応器に充填し、反応管上部からギ酸メチル
と水素ガスを並流で連続供給するトリクルベッド式、下
部からギ酸メチルを連続供給し、並流もしくは向流で水
素ガスを連続供給する方式、管型反応管で反応管出口反
応液の一部を循環する循環方式等いずれも実施できる。
これらの方法により反応器また反応管からは触媒と分離
されたメタノールとギ酸メチル混合物が得られ、蒸留に
よりによりメタノールを分離し、回収されたギ酸メチル
を原料として循環することができる。The method of reacting methyl formate with hydrogen gas of the formula (1 ') is not particularly limited, and as a continuous method, a catalyst is filled in a tubular reactor, and methyl formate and hydrogen gas are charged from the upper part of the reaction tube. , A trickle bed system that continuously supplies parallel flow, a system that continuously supplies methyl formate from the lower part and continuously supplies hydrogen gas in parallel or countercurrent, and circulates a part of the reaction solution at the reaction tube outlet with a tubular reaction tube. Any circulation method or the like can be implemented.
By these methods, a mixture of methanol and methyl formate separated from the catalyst can be obtained from the reactor or reaction tube, methanol can be separated by distillation, and the recovered methyl formate can be circulated as a raw material.
【００１３】本発明の方法は、従来のメタノールの合成
および分解反応の場合と比較して低圧で反応を行うこと
ができ、メタノールからギ酸メチルを生成する反応がよ
り低温で行われるので低温での熱回収に有利である。ま
た(1')式の反応により１００℃以上の高温でスチームや
熱水を発生させ、工場や都市部の熱需要地での種々の熱
源や冷暖房に有効に用いることができる。The method of the present invention can carry out the reaction at a lower pressure than in the case of the conventional synthesis and decomposition reaction of methanol, and since the reaction for producing methyl formate from methanol is carried out at a lower temperature, it can be carried out at a lower temperature. It is advantageous for heat recovery. Moreover, steam or hot water is generated at a high temperature of 100 ° C. or higher by the reaction of the equation (1 ′), and it can be effectively used for various heat sources and cooling / heating in heat demand areas of factories and urban areas.
【００１４】[0014]
【実施例】次に実施例により本発明を更に詳しく説明す
る。但し本発明はこれらの実施例に限定されるものでは
ない。EXAMPLES The present invention will be described in more detail by way of examples. However, the present invention is not limited to these examples.
【００１５】実施例１（メタノールの脱水素） チタン内張りの内容積３００ｍｌの上下攪拌式オートク
レーブを用い、流通式反応を行った。オートクレーブ内
にラネー銅４０ｇとメタノール２００ｍｌを入れ、上下
攪拌しながらオートクレーブを２００℃に加熱し、メタ
ノールを５．３ｇ／ｈｒ供給した。また、水素ガスをオ
ートクレーブの液中に導入し、反応圧力が５０ kg/cm2
G になるように冷却器を通して抜き出した。抜き出しガ
ス量は７５．３リッター／ｈｒであり、メタノール０．
１ｖｏｌ％、ギ酸メチル１．７２ｖｏｌ％であった。反
応液の分析の結果、メタノールの反応率は８１．１％、
ギ酸メチルの収率は７３．１％であった。Example 1 (Dehydrogenation of Methanol) A flow type reaction was carried out using an up / down stirring type autoclave having an inner volume of 300 ml with a titanium liner. 40 g of Raney copper and 200 ml of methanol were placed in the autoclave, and the autoclave was heated to 200 ° C. while stirring vertically, and methanol was supplied at 5.3 g / hr. Also, hydrogen gas was introduced into the autoclave liquid, and the reaction pressure was 50 kg / cm 2
It was pulled out through a cooler so as to be G. The amount of gas taken out was 75.3 liters / hr, and methanol was 0.
It was 1 vol% and methyl formate 1.72 vol%. As a result of analysis of the reaction solution, the reaction rate of methanol was 81.1%,
The yield of methyl formate was 73.1%.
【００１６】[0016]
【発明の効果】実施例より明らかなように本発明の方法
ではギ酸メチルを媒体とする反応の熱利用を行うことに
より、従来熱利用が困難であった２５０℃以下の低温の
工場廃熱を熱源として、１００℃以上の高温でスチーム
や熱水を発生させ、工場や都市部の熱需要地での種々の
熱源や冷暖房に有効に用いることができる。本発明の方
法は比較的低圧の温和な条件で反応が行われるので装置
コストが少なくて済み、また液相反応として反応蒸留を
用いれば効率良く熱回収と熱利用を行うことができるの
で、省エネルギー対策として極めて優れた方法である。EFFECTS OF THE INVENTION As is clear from the examples, by utilizing the heat of the reaction using methyl formate as a medium in the method of the present invention, the low temperature industrial waste heat of 250 ° C. or lower, which has been difficult to utilize in the conventional heat, can be obtained. As a heat source, steam or hot water is generated at a high temperature of 100 ° C. or higher, and it can be effectively used for various heat sources and cooling and heating in heat demand areas of factories and cities. In the method of the present invention, the reaction is carried out under relatively low pressure and mild conditions, so that the cost of the apparatus can be reduced, and if reactive distillation is used as a liquid phase reaction, heat can be efficiently recovered and used, so that energy can be saved. This is a very good measure.
フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｃ１０Ｌ 1/02 6958−4Ｈ Ｃ１０Ｌ 1/02 Continuation of the front page (51) Int.Cl. 6 Identification number Office reference number FI technical display location C10L 1/02 6958-4H C10L 1/02
Claims (4)
(1)'式により熱利用を行うことを特徴とする化学エネル
ギーを用いる熱回収と熱利用の方法 ２ＣＨ3 ＯＨ → ＨＣＯＯＣＨ3 ＋ Ｈ2 (1) ＨＣＯＯＣＨ3 ＋ Ｈ2 → ２ＣＨ3 ＯＨ (1')1. Heat recovery by the equation (1) and its reverse reaction
Method of heat recovery and heat utilization using chemical energy characterized by utilizing heat according to formula (1) '2CH 3 OH → HCOOCH 3 + H 2 (1) HCOOCH 3 + H 2 → 2CH 3 OH (1' )
触媒または貴金属触媒の存在下で行う請求項１の化学エ
ネルギーの用いる熱回収と熱利用方法2. The heat recovery and heat utilization method using chemical energy according to claim 1, wherein the reaction of the formula (1) and / or the formula (1 ′) is carried out in the presence of a copper catalyst or a noble metal catalyst.
で行う請求項１〜２の化学エネルギーの用いる熱回収と
熱利用方法3. The heat recovery and heat utilization method using chemical energy according to claim 1, wherein the reaction of formula (1) and / or formula (1 ′) is carried out in a liquid phase.
で行い、反応蒸留によりメタノール、Ｈ2 ガスおよびギ
酸メチルを分離する請求項３の化学エネルギーの用いる
熱回収と熱利用方法4. The heat recovery using chemical energy according to claim 3, wherein the reaction of the formula (1) and / or the formula (1 ′) is carried out in a liquid phase, and methanol, H 2 gas and methyl formate are separated by reactive distillation. How to use heat
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7190825A JPH0942780A (en) | 1995-07-26 | 1995-07-26 | Method for heat recovery and heat utilization using chemical energy |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7190825A JPH0942780A (en) | 1995-07-26 | 1995-07-26 | Method for heat recovery and heat utilization using chemical energy |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0942780A true JPH0942780A (en) | 1997-02-14 |
Family
ID=16264395
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7190825A Pending JPH0942780A (en) | 1995-07-26 | 1995-07-26 | Method for heat recovery and heat utilization using chemical energy |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0942780A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103557597A (en) * | 2013-10-18 | 2014-02-05 | 中国寰球工程公司 | MTP (methanol to propylene) reaction mixed gas heat recovery method and system |
-
1995
- 1995-07-26 JP JP7190825A patent/JPH0942780A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103557597A (en) * | 2013-10-18 | 2014-02-05 | 中国寰球工程公司 | MTP (methanol to propylene) reaction mixed gas heat recovery method and system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4590310A (en) | Process for the preparation of 2,2,2-trifluoroethanol | |
| EP0003530B1 (en) | A process for preparing phosgene | |
| EP0994072B1 (en) | Ammonia synthesis process | |
| CN108997085B (en) | Method and system for recovering by-products in dimethyl oxalate synthesis process | |
| JPH04282330A (en) | Process for producing methanol | |
| CA1112670A (en) | Process for manufacture of methanol | |
| US4661624A (en) | Process for the production of methyl formate | |
| CZ280489B6 (en) | Process for preparing methanol | |
| JPH0942780A (en) | Method for heat recovery and heat utilization using chemical energy | |
| EP0625502B1 (en) | Process for producing methyl formate | |
| CN110872226A (en) | Preparation process of trifluoroacetic acid | |
| Tadokoro et al. | Technical evaluation of UT-3 thermochemical hydrogen production process for an industrial scale plant | |
| JP2007204388A (en) | Method of recovering reaction heat | |
| JP2004002336A (en) | Method for producing nitrous acid ester | |
| WO2001007385A1 (en) | Methanol process for natural gas conversion | |
| JPH0942779A (en) | Method for heat recovery and heat utilization using chemical energy | |
| JP4496327B2 (en) | Methods of heat recovery, heat utilization and power generation using chemical energy | |
| JP3322280B2 (en) | Method of heat recovery and utilization using chemical energy | |
| KR100365023B1 (en) | A process for recovering acetic acid from methylacetate | |
| JP2001263828A (en) | Energy converting system using hydrogenating reaction of methyl formate | |
| JPH09268144A (en) | Heat recovery and heat utilization using chemical energy | |
| JPH10204422A (en) | Heat recovery/utilization using chemical energy | |
| JP4691632B2 (en) | Heat recovery, heat utilization and power generation using chemical energy of methanol and methyl formate | |
| US4056607A (en) | Thermochemical process for the production of hydrogen and oxygen from water | |
| JP2003113144A (en) | Method for producing alkylaryl carbonate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20050310 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20050413 |
|
| A02 | Decision of refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A02 Effective date: 20050803 |