JPH03181435A - Production of dimethyl ether - Google Patents
Production of dimethyl etherInfo
- Publication number
- JPH03181435A JPH03181435A JP1317734A JP31773489A JPH03181435A JP H03181435 A JPH03181435 A JP H03181435A JP 1317734 A JP1317734 A JP 1317734A JP 31773489 A JP31773489 A JP 31773489A JP H03181435 A JPH03181435 A JP H03181435A
- Authority
- JP
- Japan
- Prior art keywords
- catalyst
- hydrogen
- carbon dioxide
- mixed gas
- dimethyl ether
- 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
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
-
- 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
- Y02P20/584—Recycling of catalysts
Landscapes
- Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、−酸化炭素と水素の混合ガス、あるいはこれ
にさらに二酸化炭素および／または水蒸気が含まれる混
合ガスからジメチルエーテルを製造する方法に関するも
のである。Detailed Description of the Invention [Field of Industrial Application] The present invention relates to a method for producing dimethyl ether from a mixed gas of carbon oxide and hydrogen, or a mixed gas further containing carbon dioxide and/or water vapor. It is.
一酸化炭素、二酸化炭素および水素の混合ガスからジメ
チルエーテルを製造する方法は、従来いくつか知られて
いる。Several methods for producing dimethyl ether from a mixed gas of carbon monoxide, carbon dioxide, and hydrogen are known.
例えば、特公昭５４−３２７６４号公報には、アルミナ
に銅を担持したメタノール合成触媒と、アルミナに亜鉛
およびクロムを担持したメタノール脱水触媒とを混合し
て反応器に充填し、あるいはこれらの触媒を交互に層状
にして反応器に充填し、これに−酸化炭素、二酸化炭素
および水素の混合ガスを供給して、ジメチルエーテルを
製造する方法が記載されている。For example, Japanese Patent Publication No. 54-32764 discloses that a methanol synthesis catalyst in which copper is supported on alumina and a methanol dehydration catalyst in which zinc and chromium are supported on alumina are mixed and packed into a reactor, or these catalysts are mixed. A method is described for producing dimethyl ether by filling a reactor in alternating layers and feeding a mixed gas of carbon oxide, carbon dioxide and hydrogen thereto.
また、特公昭６１−４３３３２号公報には、銅、亜鉛、
クロムおよびルミニウムの酸化物の混合物を、熱、高温
水蒸気および機械的応力に耐えるように、テトラエチル
オルトシリケート等のケイ素化合物で処理し、その後成
形した触媒を使用するジメチルエーテルの製造方法が記
載されている。In addition, in Japanese Patent Publication No. 61-43332, copper, zinc,
A process for the production of dimethyl ether is described in which a mixture of chromium and aluminum oxides is treated with a silicon compound such as tetraethylorthosilicate to withstand heat, high temperature steam and mechanical stress, and the catalyst is then shaped. .
上述した従来のジメチルエーテルの製造方法は、次のよ
うな問題点があった。The conventional method for producing dimethyl ether described above has the following problems.
銅、亜鉛、クロムおよびアルミニウムの酸化物から成る
触媒は、触媒粒子の機械的強度が十分でなく、触媒層を
高速で流通するガス流体、熱等の作用によって触媒粒子
が徐々に粉化し、触媒層の目詰まりを引き起こすという
問題点があった。In catalysts made of oxides of copper, zinc, chromium, and aluminum, the mechanical strength of the catalyst particles is insufficient, and the catalyst particles gradually become powdered due to the action of gas fluid flowing at high speed through the catalyst layer, heat, etc. There was a problem in that it caused clogging of the layer.
また、メタノールからジメチルエーテルが生成される際
に副生ずる水が、アルミニウムの酸化物と反応し、その
強度を損なうという問題点があった。Another problem was that water, which is produced as a by-product when dimethyl ether is produced from methanol, reacts with aluminum oxide, impairing its strength.
さらに、触媒は、触媒活性が反応時間の経過とともに徐
々に低下するので、触媒活性が低下したときは再生する
必要がある。したがって、触媒を反応器から抜き出して
再生しなければならないが、触媒を抜き出すのが極めて
面倒であった。Furthermore, the catalyst's activity gradually decreases with the passage of reaction time, so it is necessary to regenerate the catalyst when the catalyst activity decreases. Therefore, it is necessary to extract the catalyst from the reactor and regenerate it, but extracting the catalyst is extremely troublesome.
さらにまた、−酸化炭素と水素からジメチルエーテルを
台底する方法は、著しく大きな発熱を伴う反応であるた
め、触媒層に局部加熱が生じやすく、反応温度を均一に
保持、制御することが容易ではないという問題点があっ
た。Furthermore, the method of converting dimethyl ether from carbon oxide and hydrogen is a reaction that generates a large amount of heat, so local heating tends to occur in the catalyst layer, making it difficult to maintain and control the reaction temperature uniformly. There was a problem.
本発明は、上記従来の問題点を解決するためになされた
もので、触媒に機械的強度が要求されず、また反応中、
触媒の抜き出し、再生が容易であり、しかも反応熱の除
去ならびに反応温度の制御が容易なジメチルエーテルの
製造方法を提供することを目的とする。The present invention was made to solve the above-mentioned conventional problems, and the catalyst does not require mechanical strength, and during the reaction,
The object of the present invention is to provide a method for producing dimethyl ether in which the catalyst can be easily extracted and regenerated, and the reaction heat can be easily removed and the reaction temperature can be easily controlled.
本発明は、上記目的を達成するためになされたもので、
−酸化炭素と水素の混合ガス、あるいはこれにさらに二
酸化炭素および／または水蒸気が含まれる混合ガスから
ジメチルエーテルを製造する方法において、触媒を溶媒
に懸濁してスラリー状態で使用することを特徴として構
成されている。The present invention has been made to achieve the above objects,
- A method for producing dimethyl ether from a mixed gas of carbon oxide and hydrogen, or a mixed gas further containing carbon dioxide and/or water vapor, characterized in that the catalyst is suspended in a solvent and used in a slurry state. ing.
本発明で使用される溶媒は、反応条件下において液体状
態を呈するものであれば、そのいずれもが使用可能であ
る。例えば、脂肪族、芳香族および脂環族の炭化水素、
アルコール、エーテル、エステル、ケトンおよびハロゲ
ン化物、これらの化合物の混合物等を使用できる。Any solvent can be used in the present invention as long as it exhibits a liquid state under the reaction conditions. For example, aliphatic, aromatic and alicyclic hydrocarbons,
Alcohols, ethers, esters, ketones and halides, mixtures of these compounds, etc. can be used.
また、硫黄分を除去した軽油、減圧軽油、水素化処理し
たコールタールの高沸点留分等も使用できる。Further, gas oil from which sulfur content has been removed, vacuum gas oil, high-boiling fraction of hydrotreated coal tar, etc. can also be used.
本発明で使用される触媒は、公知のメタノール合成触媒
、メタノール脱水触媒および水性ガスシフト触媒を、単
独または組合わせて使用できる。As the catalyst used in the present invention, known methanol synthesis catalysts, methanol dehydration catalysts, and water gas shift catalysts can be used alone or in combination.
メタノール合成触媒としては、銅−亜鉛、亜鉛−クロム
などがある。メタノール脱水触媒としては、Ｔ−アル旦
す、シリカ・アルごす、ゼオライトなどがある。水性ガ
スシフト触媒としては、銅−亜鉛、鉄−クロムなどがあ
り、メタノール合成触媒も優れた水性ガスシフト触媒で
ある。Examples of methanol synthesis catalysts include copper-zinc and zinc-chromium. Examples of methanol dehydration catalysts include T-aldansu, silica algosu, and zeolite. Water gas shift catalysts include copper-zinc and iron-chromium, and methanol synthesis catalysts are also excellent water gas shift catalysts.
上記触媒は、粒子状または粉末状で溶媒に懸濁してスラ
リー化した状態で使用される。溶媒中に存在させる触媒
量は、溶媒の種類、反応条件などによって適宜選択され
るが、通常は溶媒に対して１〜５０重量％である。The above catalyst is used in the form of a slurry by suspending it in a solvent in the form of particles or powder. The amount of catalyst present in the solvent is appropriately selected depending on the type of solvent, reaction conditions, etc., but is usually 1 to 50% by weight based on the solvent.
このようにして形成された触媒−溶媒スラリー中に一酸
化炭素と水素の混合ガスを流通させることにより、ジメ
チルエーテルが高倍率で得られる。By passing a mixed gas of carbon monoxide and hydrogen through the catalyst-solvent slurry thus formed, dimethyl ether can be obtained at a high magnification.
水素と一酸化炭素の混合割合（Ｈ，／Ｃｏ）は広範囲の
ものが適用可能である。これは、本反応系では、気固接
触反応のように混合ガスが直接触媒に接触することなく
、−度、−酸化炭素と水素が溶媒に溶解した後、触媒と
接触するために、−酸化炭素と水素の溶媒への溶解性を
考慮して溶媒を選択することにより、ガス組成によらず
一定の一酸化炭素と水素の組成を溶媒中で達成させ、さ
らに触媒表面に供給することが可能である。A wide range of mixing ratios (H,/Co) of hydrogen and carbon monoxide can be applied. This is because, in this reaction system, the mixed gas does not come into direct contact with the catalyst as in gas-solid contact reactions, but instead comes into contact with the catalyst after carbon oxide and hydrogen are dissolved in the solvent. By selecting a solvent in consideration of the solubility of carbon and hydrogen in the solvent, it is possible to achieve a constant composition of carbon monoxide and hydrogen in the solvent regardless of the gas composition, and further supply it to the catalyst surface. It is.
一方、水素と一酸化炭素の混合割合（Ｈ，／Ｃ○）が著
しく小さな混合ガス、あるいは水素を含まない一酸化炭
素の場合には、別途スチームを供給して反応器中で一酸
化炭素の一部をスチームにより水素と二酸化炭素に変換
することが必要である。On the other hand, in the case of a mixed gas in which the mixing ratio of hydrogen and carbon monoxide (H, /C○) is extremely small, or in the case of carbon monoxide that does not contain hydrogen, steam is supplied separately to remove carbon monoxide in the reactor. It is necessary to convert some of it into hydrogen and carbon dioxide by steam.
また、原料ガスと触媒の間に溶媒が存在しているため、
ガス組成と触媒表面での組成が必ずしも一致しないこと
から、−酸化炭素と水素の混合ガス、あるいは−酸化炭
素ガス中に比較的高濃度（２０〜５０％）の二酸化炭素
が存在してもよい。In addition, since there is a solvent between the raw material gas and the catalyst,
Since the gas composition and the composition on the catalyst surface do not necessarily match, -a mixed gas of carbon oxide and hydrogen, or -a relatively high concentration (20 to 50%) of carbon dioxide may be present in the carbon oxide gas. .
また、本発明の製造方法は、原料ガス中に硫化水素等の
硫黄化合物、シアン化水素等のシアン化合物、塩化水素
等の塩素化合物など触媒毒となら成分が存在していても
、触媒に対する影響が気固接触法に比べ著しく軽減され
ている。なお、触媒が被毒され、その活性が低下した場
合には、反応器よりスラリーを抜き出し、新たに高活性
触媒を含有するスラリーを反応器へ圧入することにより
、反応器全体の生産性を一定に保持することができる。Furthermore, in the production method of the present invention, even if catalyst poisonous components such as sulfur compounds such as hydrogen sulfide, cyanide compounds such as hydrogen cyanide, and chlorine compounds such as hydrogen chloride are present in the raw material gas, the influence on the catalyst is not a concern. This is significantly reduced compared to the solid contact method. In addition, if the catalyst is poisoned and its activity decreases, the productivity of the entire reactor can be kept constant by extracting the slurry from the reactor and pressurizing a new slurry containing a highly active catalyst into the reactor. can be held.
なお、反応熱は、例えば、反応器内へ冷却コイルを設置
し、それに熱水を通過させることにより中圧蒸気として
回収される。これにより反応温度を自由に制御できる。Note that the reaction heat is recovered as medium-pressure steam by, for example, installing a cooling coil in the reactor and passing hot water through it. This allows the reaction temperature to be freely controlled.
反応条件としては、反応温度１５０〜４００″Ｃ１好ま
しくは２００〜３５０℃であり、また反応圧力は１０〜
３００ｋｇ ／ ｃｔ 、好ましくは２０〜１５０ｋｇ
／Ｃ消である。The reaction conditions include a reaction temperature of 150 to 400"C, preferably 200 to 350"C, and a reaction pressure of 10 to 350"C.
300kg/ct, preferably 20-150kg
/C is off.
本発明のジメチルエーテルの製造方法は、触媒を溶媒に
懸濁してスラリー状態で使用することにより、目詰まり
や機械的強度を問題とせず、また、冷却パイプ等を設け
ることにより反応熱の吸収を簡単に行なえるようにし、
さらに、触媒の抜き出しおよび充填も簡単に行なえるよ
うにしている。In the method for producing dimethyl ether of the present invention, by suspending the catalyst in a solvent and using it in a slurry state, there are no problems with clogging or mechanical strength, and by providing a cooling pipe etc., the reaction heat can be easily absorbed. to be able to do it,
Furthermore, the catalyst can be easily removed and filled.
以下、本発明の実施例について図面を参照して説明する
。Embodiments of the present invention will be described below with reference to the drawings.
第１図は、本発明の一実施例の工程フローを示す説明図
である。FIG. 1 is an explanatory diagram showing a process flow of an embodiment of the present invention.
この図において、符号ｌはジメチルエーテルが製造され
る反応器で、この反応器１の内部には触媒−溶媒スラリ
ーが充填されている。この反応器１の低部と頂部との間
には、反応器１から流出した高温ガスにより、反応器１
に流入する一酸化炭素、二酸化炭素および水素の混合ガ
スを加熱する熱交換器２が連結されるとともに、劣化し
た触媒を再生する触媒再生手段３がポンプ４を介して連
結されている。また、反応器１の低部には、スチームを
導入するためのスチーム発生手段（図示せず）が、圧縮
器５を介して連結されている。なお、符号１４は、反応
熱の回収用のバイブである。In this figure, reference numeral 1 denotes a reactor in which dimethyl ether is produced, and the inside of this reactor 1 is filled with a catalyst-solvent slurry. The high temperature gas flowing out from the reactor 1 creates a gap between the bottom and the top of the reactor 1.
A heat exchanger 2 for heating a mixed gas of carbon monoxide, carbon dioxide, and hydrogen flowing into the reactor is connected to the catalyst, and a catalyst regeneration means 3 for regenerating a deteriorated catalyst is connected via a pump 4. Further, a steam generating means (not shown) for introducing steam is connected to the lower part of the reactor 1 via a compressor 5. Note that the reference numeral 14 is a vibrator for recovering reaction heat.
熱交換器２には、−酸化炭素、二酸化炭素および水素か
ら戒る混合ガスの発生手段（図示せず）が、圧縮器６を
介して連結されるとともに、ジメチルエーテル等と一酸
化炭素等を分離する気−液分離器７が連結されている。A means (not shown) for generating a mixed gas from carbon oxide, carbon dioxide, and hydrogen is connected to the heat exchanger 2 via a compressor 6, and also for separating dimethyl ether, etc., and carbon monoxide, etc. A gas-liquid separator 7 is connected thereto.
そして、混合ガスの発生手段は反応器１の低部側に連通
し、気−液分離器７は反応器１の頂部側に連通している
。The mixed gas generating means communicates with the lower side of the reactor 1, and the gas-liquid separator 7 communicates with the top side of the reactor 1.
気−液分離器７は、ジメチルエーテルと水を分離する液
−液分離器８が低部に連結されるとともに、二酸化炭素
を吸収する二酸化炭素吸収塔９が頂部に連結されている
。In the gas-liquid separator 7, a liquid-liquid separator 8 for separating dimethyl ether and water is connected at the bottom, and a carbon dioxide absorption tower 9 for absorbing carbon dioxide is connected at the top.
二酸化炭素吸収塔９には、二酸化炭素を吸収した吸収液
から二酸化炭素を取り出して吸収液を再生させる吸収液
再生塔１０が連結されており、二酸化炭素吸収塔９の低
部と吸収液再生塔１０の頂部、二酸化炭素吸収塔９の頂
部と吸収液再生塔１０の低部が、それぞれポンプ１１．
１２を介して連通している。The carbon dioxide absorption tower 9 is connected to an absorption liquid regeneration tower 10 that extracts carbon dioxide from the absorption liquid that has absorbed carbon dioxide and regenerates the absorption liquid. 10, the top of the carbon dioxide absorption tower 9, and the bottom of the absorption liquid regeneration tower 10 are respectively connected to the pump 11.
It communicates via 12.
また、二酸化炭素吸収塔９の塔頂は、圧縮器１３を介し
て熱交換器２に連結され、原料ガスである一酸化炭素、
二酸化炭素および水素から戒る混合ガスに、−酸化炭素
および水素からなる混合ガスを合流させるようになって
いる。Further, the top of the carbon dioxide absorption tower 9 is connected to the heat exchanger 2 via the compressor 13, and carbon monoxide, which is the raw material gas,
A mixed gas consisting of carbon dioxide and hydrogen is combined with a mixed gas consisting of carbon oxide and hydrogen.
次に、ジメチルエーテルを製造する工程について説明す
る。Next, the process of producing dimethyl ether will be explained.
まず、混合ガス発生手段で発生した一酸化炭素、二酸化
炭素および水素からなる混合ガスａを、圧縮器６で圧縮
した後熱交換器２に送り込む。熱交換器２に送り込まれ
た混合ガスａは、反応器１から流出した高温の反応ガス
ｂで加熱される。そして、このとき、二酸化炭素吸収塔
９で発生した一酸化炭素および水素からなる循環混合ガ
スＣも、圧縮器１３で圧縮された後混合ガスａと合流し
、熱交換器２で加熱されている。First, a mixed gas a consisting of carbon monoxide, carbon dioxide, and hydrogen generated by a mixed gas generating means is compressed by a compressor 6 and then sent to a heat exchanger 2. The mixed gas a fed into the heat exchanger 2 is heated by the high temperature reaction gas b flowing out from the reactor 1. At this time, the circulating mixed gas C consisting of carbon monoxide and hydrogen generated in the carbon dioxide absorption tower 9 is also compressed in the compressor 13, joins with the mixed gas a, and is heated in the heat exchanger 2. .
熱交換器２で加熱された原料混合ガスａおよび循環混合
ガスＣは、反応器１の低部に導入される。The raw material mixed gas a and the circulating mixed gas C heated in the heat exchanger 2 are introduced into the lower part of the reactor 1.
反応器１内部に導入された原料混合ガスａおよび循環混
合ガスＣは、触媒−溶媒スラリー中を上昇しつつ反応し
、ジメチルエーテルと水とが発生する。このとき、パイ
プ１４に熱水ｄを注入しスチームｅとして取り出すこと
により、内部で発生した反応熱を外部に回収している。The raw material mixed gas a and the circulating mixed gas C introduced into the reactor 1 react while rising in the catalyst-solvent slurry, and dimethyl ether and water are generated. At this time, the reaction heat generated inside is recovered to the outside by injecting hot water d into the pipe 14 and taking it out as steam e.
また、反応器ｌ中の触媒は徐々に劣化するので、この触
媒の劣化に伴い、触媒−溶媒スラリーを適宜頂部より抜
き出し、触媒再生手段３で再生した後、ポンプ４で再び
反応器１の低部に導入する。In addition, since the catalyst in the reactor 1 gradually deteriorates, as the catalyst deteriorates, the catalyst-solvent slurry is appropriately extracted from the top, regenerated by the catalyst regeneration means 3, and then regenerated by the pump 4 into the reactor 1. Department.
さらに、反２器１にスチームが必要な場合は、スチーム
発生手段で発生したスチームｆを、圧縮器５で圧縮して
反応器１の低部から導入する。Further, when steam is required in the reactor 1, the steam f generated by the steam generating means is compressed by the compressor 5 and introduced from the lower part of the reactor 1.
反応器１の頂部からは、反応により発生したジメチルエ
ーテルと水、および未反応の一酸化炭素、二酸化炭素な
らびに水素からなる高温の反応ガスｂが流出し、この反
応ガスｂは、熱交換器２で冷却された後、気−液分離器
７に送られる。そして、この気−液分離器７で、ジメチ
ルエーテルと水の液体混合物ｇと、−酸化炭素、二酸化
炭素および水素の混合ガスｈとに分離される。A high-temperature reaction gas b consisting of dimethyl ether and water generated by the reaction, unreacted carbon monoxide, carbon dioxide, and hydrogen flows out from the top of the reactor 1, and this reaction gas b is transferred to the heat exchanger 2. After being cooled, it is sent to a gas-liquid separator 7. Then, in this gas-liquid separator 7, it is separated into a liquid mixture g of dimethyl ether and water and a mixed gas h of carbon oxide, carbon dioxide and hydrogen.
分離されたジメチルエーテルと水の液体混合物ｇは、液
−液分離器８に送られてジメチルエーテルｉと水ｊにさ
らに分離され、それぞれ回収される。The separated liquid mixture g of dimethyl ether and water is sent to the liquid-liquid separator 8, where it is further separated into dimethyl ether i and water j, and each is recovered.
他方、分離された一酸化炭素、二酸化炭素および水素か
らなる混合ガスｈは、二酸化炭素吸収塔９の低部に導入
されて二酸化炭素が除去され、−酸化炭素と水素からな
る循環混合ガスＣとなる。On the other hand, the separated mixed gas h consisting of carbon monoxide, carbon dioxide and hydrogen is introduced into the lower part of the carbon dioxide absorption tower 9, where carbon dioxide is removed, and - a circulating mixed gas C consisting of carbon oxide and hydrogen is produced. Become.
二の循環混合ガスＣは、上述したように、圧縮器１３で
圧縮されて原料混合ガスａと合流される。As described above, the second circulating mixed gas C is compressed by the compressor 13 and combined with the raw material mixed gas a.
二酸化炭素吸収塔９の二酸化炭素を吸収した吸収液には
、低部より抜き出され、ポンプ１１によって吸収液再生
塔１０の頂部に導入される。この二酸化炭素を吸収した
吸収液には、吸収液再生塔１０で二酸化炭素を除去され
て再生され、再生吸収液ｍとしてポンプ１２によって二
酸化炭素吸収塔９の頂部に戻される。The absorption liquid that has absorbed carbon dioxide from the carbon dioxide absorption tower 9 is extracted from the lower part and introduced into the top of the absorption liquid regeneration tower 10 by a pump 11. The absorption liquid that has absorbed carbon dioxide is regenerated by removing carbon dioxide in an absorption liquid regeneration tower 10, and is returned to the top of the carbon dioxide absorption tower 9 by a pump 12 as a regenerated absorption liquid m.
吸収液再生塔９で発生した二酸化炭素ｎは、塔頂より抜
き出され、回収される。Carbon dioxide n generated in the absorption liquid regeneration tower 9 is extracted from the top of the tower and recovered.
本発明は、ジメチルエーテルの合成反応を触媒−溶媒ス
ラリー中で行うように構成したので、触媒に機械的強度
が要求されず、安価な粉末触媒を使用でき、また反応熱
の除去、反応温度の制御が容易であり、さらに−酸化炭
素と水素の比率の適用範囲が広く、また高濃度の二酸化
炭素の存在化での反応が可能であるとともに、不純物、
触媒毒の影響が少ないなどの効果を有する。In the present invention, the synthesis reaction of dimethyl ether is carried out in a catalyst-solvent slurry, so the catalyst does not require mechanical strength, an inexpensive powder catalyst can be used, and the reaction heat can be removed and the reaction temperature can be controlled. Furthermore, the ratio of carbon oxide and hydrogen can be applied over a wide range, and the reaction can be carried out in the presence of a high concentration of carbon dioxide, and impurities,
It has the effect of being less affected by catalyst poisons.
第１図は、本発明の一実施例の工程フローを示す説明図
である。
１・・・反応器 ３・・・触媒再生手段１４・・
・パイプFIG. 1 is an explanatory diagram showing a process flow of an embodiment of the present invention. 1... Reactor 3... Catalyst regeneration means 14...
·pipe
Claims (1)
酸化炭素および／または水蒸気が含まれる混合ガスから
ジメチルエーテルを製造する方法において、触媒を溶媒
に懸濁してスラリー状態で使用することを特徴とするジ
メチルエーテルの製造方法A method for producing dimethyl ether from a mixed gas of carbon monoxide and hydrogen, or a mixed gas further containing carbon dioxide and/or water vapor, characterized in that the catalyst is suspended in a solvent and used in a slurry state. manufacturing method
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1317734A JPH03181435A (en) | 1989-12-08 | 1989-12-08 | Production of dimethyl ether |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1317734A JPH03181435A (en) | 1989-12-08 | 1989-12-08 | Production of dimethyl ether |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH03181435A true JPH03181435A (en) | 1991-08-07 |
Family
ID=18091448
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1317734A Pending JPH03181435A (en) | 1989-12-08 | 1989-12-08 | Production of dimethyl ether |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH03181435A (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1993010069A1 (en) * | 1991-11-11 | 1993-05-27 | Nkk Corporation | Process for producing dimethyl ether |
| JPH09502792A (en) * | 1993-09-14 | 1997-03-18 | セマテック インコーポレーテッド | Integrated building and transport structures for production under extremely clean conditions |
| US5753716A (en) * | 1997-02-21 | 1998-05-19 | Air Products And Chemicals, Inc. | Use of aluminum phosphate as the dehydration catalyst in single step dimethyl ether process |
| US6069180A (en) * | 1998-12-17 | 2000-05-30 | Air Products And Chemicals, Inc. | Single step synthesis gas-to-dimethyl ether process with methanol introduction |
| US6147125A (en) * | 1996-05-13 | 2000-11-14 | Nkk Corporation | Method and apparatus for producing dimethyl ether |
| US6800665B1 (en) | 1996-05-13 | 2004-10-05 | Jfe Holdings, Inc. | Method for producing dimethyl ether |
| JP2008019176A (en) * | 2006-07-11 | 2008-01-31 | Ihi Corp | Method for synthesizing methanol and dimethyl ether |
| JP2010209038A (en) * | 2009-03-12 | 2010-09-24 | Jx Nippon Oil & Energy Corp | Method for producing oxygen-containing compound |
| JP2017503802A (en) * | 2014-01-07 | 2017-02-02 | リンデ アクチエンゲゼルシャフトＬｉｎｄｅ Ａｋｔｉｅｎｇｅｓｅｌｌｓｃｈａｆｔ | Separation of product stream of dimethyl ether reactor |
| JP2017505224A (en) * | 2014-01-07 | 2017-02-16 | リンデ アクチエンゲゼルシャフトＬｉｎｄｅ Ａｋｔｉｅｎｇｅｓｅｌｌｓｃｈａｆｔ | Processing of gas mixtures formed from the product stream of a dimethyl reactor by separation techniques. |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH029833A (en) * | 1988-01-14 | 1990-01-12 | Air Prod And Chem Inc | Method for direct synthesis and electric production of dimethyl ether and methonol byproducts from a synthetic gas |
| JPH0352835A (en) * | 1989-07-18 | 1991-03-07 | Air Prod And Chem Inc | Direct synthesis of dimethyl ether from synthetic gas and extending of stock fuel by means of cycle plant |
-
1989
- 1989-12-08 JP JP1317734A patent/JPH03181435A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH029833A (en) * | 1988-01-14 | 1990-01-12 | Air Prod And Chem Inc | Method for direct synthesis and electric production of dimethyl ether and methonol byproducts from a synthetic gas |
| JPH0352835A (en) * | 1989-07-18 | 1991-03-07 | Air Prod And Chem Inc | Direct synthesis of dimethyl ether from synthetic gas and extending of stock fuel by means of cycle plant |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1993010069A1 (en) * | 1991-11-11 | 1993-05-27 | Nkk Corporation | Process for producing dimethyl ether |
| JPH09502792A (en) * | 1993-09-14 | 1997-03-18 | セマテック インコーポレーテッド | Integrated building and transport structures for production under extremely clean conditions |
| US6147125A (en) * | 1996-05-13 | 2000-11-14 | Nkk Corporation | Method and apparatus for producing dimethyl ether |
| US6562306B1 (en) | 1996-05-13 | 2003-05-13 | Nkk Corporation | Apparatus for producing dimethyl ether |
| US6800665B1 (en) | 1996-05-13 | 2004-10-05 | Jfe Holdings, Inc. | Method for producing dimethyl ether |
| US7033972B2 (en) | 1996-05-13 | 2006-04-25 | Jfe Holdings, Inc. | Catalyst for producing dimethyl ether, method for producing catalyst and method for producing dimethyl ether |
| US5753716A (en) * | 1997-02-21 | 1998-05-19 | Air Products And Chemicals, Inc. | Use of aluminum phosphate as the dehydration catalyst in single step dimethyl ether process |
| US6069180A (en) * | 1998-12-17 | 2000-05-30 | Air Products And Chemicals, Inc. | Single step synthesis gas-to-dimethyl ether process with methanol introduction |
| JP2008019176A (en) * | 2006-07-11 | 2008-01-31 | Ihi Corp | Method for synthesizing methanol and dimethyl ether |
| JP2010209038A (en) * | 2009-03-12 | 2010-09-24 | Jx Nippon Oil & Energy Corp | Method for producing oxygen-containing compound |
| JP2017503802A (en) * | 2014-01-07 | 2017-02-02 | リンデ アクチエンゲゼルシャフトＬｉｎｄｅ Ａｋｔｉｅｎｇｅｓｅｌｌｓｃｈａｆｔ | Separation of product stream of dimethyl ether reactor |
| JP2017505224A (en) * | 2014-01-07 | 2017-02-16 | リンデ アクチエンゲゼルシャフトＬｉｎｄｅ Ａｋｔｉｅｎｇｅｓｅｌｌｓｃｈａｆｔ | Processing of gas mixtures formed from the product stream of a dimethyl reactor by separation techniques. |
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