JPH04193303A - Refining method for alcohol - Google Patents
Refining method for alcoholInfo
- Publication number
- JPH04193303A JPH04193303A JP2322328A JP32232890A JPH04193303A JP H04193303 A JPH04193303 A JP H04193303A JP 2322328 A JP2322328 A JP 2322328A JP 32232890 A JP32232890 A JP 32232890A JP H04193303 A JPH04193303 A JP H04193303A
- Authority
- JP
- Japan
- Prior art keywords
- solvent
- ethanol
- water
- extraction
- impurity
- 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
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 115
- 238000000034 method Methods 0.000 title claims abstract description 19
- 238000007670 refining Methods 0.000 title 1
- 239000002904 solvent Substances 0.000 claims abstract description 55
- 239000012535 impurity Substances 0.000 claims abstract description 46
- 238000000605 extraction Methods 0.000 claims abstract description 35
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 22
- 239000000203 mixture Substances 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 13
- 239000001294 propane Substances 0.000 claims abstract description 11
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 8
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 8
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 7
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000000855 fermentation Methods 0.000 claims description 4
- 230000004151 fermentation Effects 0.000 claims description 4
- 238000003786 synthesis reaction Methods 0.000 claims description 3
- 239000011877 solvent mixture Substances 0.000 claims description 2
- 239000002994 raw material Substances 0.000 abstract description 11
- 238000000926 separation method Methods 0.000 abstract description 7
- 235000019441 ethanol Nutrition 0.000 description 59
- 239000012071 phase Substances 0.000 description 12
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 5
- 239000001273 butane Substances 0.000 description 5
- 238000004821 distillation Methods 0.000 description 5
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 4
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 3
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 3
- 238000000638 solvent extraction Methods 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 238000005259 measurement Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- QSJXEFYPDANLFS-UHFFFAOYSA-N Diacetyl Chemical group CC(=O)C(C)=O QSJXEFYPDANLFS-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 238000006703 hydration reaction Methods 0.000 description 1
- ZXEKIIBDNHEJCQ-UHFFFAOYSA-N isobutanol Chemical compound CC(C)CO ZXEKIIBDNHEJCQ-UHFFFAOYSA-N 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
- 238000010189 synthetic method Methods 0.000 description 1
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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Landscapes
- Extraction Or Liquid Replacement (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は化学合成アルコール又は発酵アルコール製造プ
ロセスから生じる水／エタノール／不純物の混合物から
不純物を分離する方法に関する。DETAILED DESCRIPTION OF THE INVENTION Field of the Invention The present invention relates to a method for separating impurities from a water/ethanol/impurity mixture resulting from a chemically synthesized alcohol or fermentative alcohol production process.
化学合成アルコールは通常エチレンの水和反応によって
製造され、合成反応後の組成は約２０ｗｔ％のエタノー
ルと約８０ｗｔ％の水を主成分とするが、これ以外にエ
チルエーテル、アセトアルデヒド、メチルエチルケトン
、２−ブタノール、アセトン等の微量の不純物を含んで
おり１、 アルコールの濃縮と独立に又は並行してこれ
らの不純物を分離し、アルコール専売法又はＪＩＳ規格
に適合するように精製する必要がある。Chemically synthesized alcohol is usually produced by a hydration reaction of ethylene, and the composition after the synthesis reaction is mainly composed of about 20 wt% ethanol and about 80 wt% water, but in addition to these, ethyl ether, acetaldehyde, methyl ethyl ketone, 2- It contains trace amounts of impurities such as butanol and acetone1, and these impurities must be separated independently or in parallel with alcohol concentration and purified to comply with the Alcohol Exclusive Law or JIS standards.
一方、発酵アルコールは約１０ｗｔ％のエタノールと約
９０ｗｔ％の水を主成分とするが、これ以外にアセトア
ルデヒド、メタノール、酢酸エチル、ｎ−プロパツール
、ｉ−ブタノール、ｎ−ブタノール、ｊ−アミルアルコ
ール、ジアセチル、酢酸等の微量の不純物を含んでおり
、やはり規格に適用するように精製する必要がある。On the other hand, fermented alcohol has approximately 10 wt% ethanol and approximately 90 wt% water as main components, but in addition to these, it also contains acetaldehyde, methanol, ethyl acetate, n-propanol, i-butanol, n-butanol, and j-amyl alcohol. It contains trace amounts of impurities such as , diacetyl, and acetic acid, and must be purified to meet the standards.
従来、これら不純物の精製は蒸留又は溶剤抽出法により
行なわれている。蒸留法では、不純物のエタノールに対
する揮発度が不純物の種類及びエタノール濃度により複
雑に変化するために、プロセスが複雑となり多くのエネ
ルギーと多大の装置コストが必要である。又、溶剤抽出
法では液体又は超臨界状態の００２を溶剤として用いる
方法が特願昭６０−４１６２７号公報にみられる。Conventionally, purification of these impurities has been carried out by distillation or solvent extraction methods. In the distillation method, the volatility of impurities relative to ethanol varies in a complicated manner depending on the type of impurities and the ethanol concentration, so the process is complicated and requires a lot of energy and equipment cost. Further, in the solvent extraction method, a method using liquid or supercritical 002 as a solvent is found in Japanese Patent Application No. 41627/1983.
本発明は合成法又は発酵法により製造された水／エタノ
ール／不純物からなる混合物から、不純物を選択的に分
離する方法に関し、水／エタノールを無水化できる溶剤
として本発明者らが特願平１−１６０６９６号で提案し
たプロパン、プロピレン、ブタンを該不純物の抽出溶剤
として用いることによって、不純物の分離を行なおうと
するものである。The present invention relates to a method for selectively separating impurities from a mixture of water/ethanol/impurities produced by a synthetic method or a fermentation method. This method attempts to separate impurities by using propane, propylene, and butane proposed in No. 160696 as extraction solvents for the impurities.
本発明者らは、超臨界状態又は擬臨界状態のプロパン、
プロピレン又はブタンを抽出溶剤として用いることによ
りエタノール／水混合物からエタノールを選択的にかつ
経済的に抽出分離できることを既に見いだしている（例
えば、特願平１−ｔｅ０６９６号）。The present inventors have discovered that propane in a supercritical or quasi-critical state,
It has already been found that ethanol can be selectively and economically extracted and separated from an ethanol/water mixture by using propylene or butane as an extraction solvent (for example, see Japanese Patent Application No. 1-TE0696).
本発明者らは、かかる溶剤と同一のものを用いて合成法
又は発酵法により製造された水／アルコール／不純物混
合物から不純物を選択的に分離する方法を鋭意検討した
結果、プロパン、プロピレン、ブタンを液体状態に保持
して抽出溶剤として用いることにより、過度のアルコー
ルを抽出することなく、経済的に大部分の不純物を選択
的に抽出できることを見出した。The present inventors have intensively investigated a method for selectively separating impurities from a water/alcohol/impurity mixture produced by a synthesis method or a fermentation method using the same solvent, and found that propane, propylene, butane It has been found that most impurities can be economically and selectively extracted without extracting excessive amounts of alcohol by keeping it in a liquid state and using it as an extraction solvent.
すなわち、本発明は発酵法又は化学合成法により製造さ
れた水／エタノール／不純物からなる混合物を抽出塔中
部に供給し、液体状態のプロパン、プロピレン、ｎ−１
タン、１−ブタン単独又はそれらの混合物の溶剤を該抽
出塔下部より、又、水を該抽出塔の上部より供給し、該
抽出塔上部より実質的にエタノールを含まない溶剤／不
純物混合物を、該抽出塔下部より実質的に不純物を含ま
ない水／エタノール／溶剤混合物を回収することを特徴
とするアルコールの精製方法である。That is, in the present invention, a mixture of water/ethanol/impurities produced by a fermentation method or a chemical synthesis method is supplied to the middle part of the extraction column, and liquid propane, propylene, n-1
A solvent of ethanol, 1-butane alone or a mixture thereof is supplied from the lower part of the extraction column, water is supplied from the upper part of the extraction column, and a solvent/impurity mixture substantially free of ethanol is supplied from the upper part of the extraction column, This method of purifying alcohol is characterized by recovering a water/ethanol/solvent mixture substantially free of impurities from the lower part of the extraction column.
以下、本発明の一実施態様を第１図に従って詳述する。Hereinafter, one embodiment of the present invention will be described in detail with reference to FIG.
第１図において、■は向流抽出塔（充填塔、多孔板塔、
トレイ型塔など通常化学プラントに用いられているもの
が使用できる。２は原料（水／エタノール／不純物）供
給ライン、３は水供給ライン、４は液体溶剤（プロパン
、プロピレン、ｎ−ブタン又はｉ−ブタン）供給ライン
、５はラフィネート（実質的に不純物の分離された水、
エタノール及び少量の溶解した溶剤からなる）取出しラ
イン、６は溶剤相（溶剤、不純物、少量の水からなる）
取出しライン、７は減圧弁、８は溶剤相供給ライン、９
は溶剤分離塔、１０は不純物取出しライン、１１は溶剤
ガス抜出しライン、１２は溶剤圧縮機、１３は加圧蒸留
ボイラ及び１４は溶剤還流ラインである。In Figure 1, ■ indicates a countercurrent extraction tower (packed tower, perforated plate tower,
Those commonly used in chemical plants, such as tray-type columns, can be used. 2 is a raw material (water/ethanol/impurities) supply line, 3 is a water supply line, 4 is a liquid solvent (propane, propylene, n-butane or i-butane) supply line, and 5 is a raffinate (where impurities are substantially separated). water,
6 is the solvent phase (consisting of solvent, impurities and a small amount of water);
Take-out line, 7 is a pressure reducing valve, 8 is a solvent phase supply line, 9
10 is a solvent separation column, 10 is an impurity removal line, 11 is a solvent gas extraction line, 12 is a solvent compressor, 13 is a pressurized distillation boiler, and 14 is a solvent reflux line.
（発酵アルコールの組成） 発酵アルコールの代表的な組成は下記のとおりである。(Composition of fermented alcohol) A typical composition of fermented alcohol is as follows.
（合成アルコールの組成） 合成アルコールの代表的な組成は下記のとおりである。(Composition of synthetic alcohol) A typical composition of synthetic alcohol is as follows.
原料の水／エタノール／不純物混合物は向流抽出塔１の
中部の原料供給ライン２より、水は該抽出塔１の上部の
水供給ライン３より、一方抽出溶剤は該向流抽出塔１の
下部の液体溶剤供給うイン４より供給し、該抽出溶剤を
液体状態に保持して向流抽出操作を行なうことにより、
該不純物は溶剤に選択的に抽出され、溶剤相取出しライ
ン６より溶剤とともに実質的にエタノールを含まない溶
剤相として抜き出され、塔底のラフィネート取出しライ
ン５からは不純物が実質的に分離された水／エタノール
混合物が抜き出される。この混合物は別途エタノールと
水に分離することができる。The raw material water/ethanol/impurity mixture is supplied from the raw material supply line 2 at the middle of the countercurrent extraction column 1, water is supplied from the water supply line 3 at the upper part of the extraction column 1, and the extraction solvent is supplied from the lower part of the countercurrent extraction column 1. By supplying the liquid solvent from the liquid solvent supply channel 4 and maintaining the extraction solvent in a liquid state to perform a countercurrent extraction operation,
The impurities were selectively extracted by the solvent and extracted together with the solvent from the solvent phase take-off line 6 as a solvent phase substantially free of ethanol, and the impurities were substantially separated from the raffinate take-off line 5 at the bottom of the column. A water/ethanol mixture is drawn off. This mixture can be separately separated into ethanol and water.
原料の水／エタノール／不純物からなる混合物中のエタ
ノール含有量は約５ｗｔ％から約９５ｗｔ％の広範囲に
わたってよいが、本発明は特に４０ｗｔ％以下のエタノ
ール濃度に対して効果的である。これは、エタノール濃
度が低い程、エタノールに対する不純物の分離度（比揮
発度）が１．０より遠ざかり、不純物をより選択的に抽
出できるためである。Although the ethanol content in the raw water/ethanol/impurities mixture can range widely from about 5 wt% to about 95 wt%, the present invention is particularly effective for ethanol concentrations below 40 wt%. This is because the lower the ethanol concentration, the more the degree of separation (specific volatility) of impurities with respect to ethanol becomes further than 1.0, and impurities can be extracted more selectively.
ライン４の溶剤は原料１重１部に対して１〜２０重量部
であるが、好ましくは１〜１０重量部である。The amount of the solvent in line 4 is 1 to 20 parts by weight, preferably 1 to 10 parts by weight, per 1 part by weight of the raw material.
６方ライン３の水は原料１重量部に対して通常０，１〜
５重量部の範囲であるが、好ましくは原料エタノール濃
度に応じて、過剰とならない抽出溶剤の液体状態とは、
溶剤の臨界温度以下で、かつその温度における溶剤の蒸
気圧以上１．に保持した圧力の状態を意味する。The water in the 6-way line 3 is usually 0.1 to 1 part by weight of the raw material.
The liquid state of the extraction solvent is within the range of 5 parts by weight, but preferably does not become excessive depending on the raw material ethanol concentration.
Below the critical temperature of the solvent and above the vapor pressure of the solvent at that temperature 1. means a state of pressure maintained at
しかしながら、抽出溶剤の不純物抽出の選択性は温度に
よって変動し、その選択性を高めるには温度は１０〜６
０℃の範囲、好ましくは１０〜３０℃である。However, the selectivity of impurity extraction of the extraction solvent varies depending on the temperature, and to increase the selectivity, the temperature is 10 to 6
It is in the range of 0°C, preferably 10-30°C.
次に、溶剤相取出しライン６の溶剤相（溶剤、不純物か
らなり実質的にエタノールを含まない）は、溶剤相供給
ライン８より溶剤分離塔９に導入され、溶剤はストリッ
ピング蒸留操作により塔頂の溶剤ガス抜出しライン１１
より、一方不純物は塔底の不純物取出しライン１０より
抜き出される。Next, the solvent phase (consisting of solvent and impurities and substantially free of ethanol) from the solvent phase take-off line 6 is introduced into the solvent separation column 9 from the solvent phase supply line 8, and the solvent is removed from the top of the column by a stripping distillation operation. Solvent gas extraction line 11
On the other hand, impurities are extracted from the impurity removal line 10 at the bottom of the column.
ライン１１の溶剤はガス状態であり、溶剤圧縮機１２で
再圧縮してその圧縮熱を加圧蒸留リボイラ１３で熱回収
し、液体溶剤供給ライン４を経て向流抽出塔１へ、また
一部は溶剤還流ライン１４を経て溶剤分離塔９へ再循環
される。The solvent in the line 11 is in a gaseous state, and is recompressed by the solvent compressor 12, and the heat of compression is recovered by the pressure distillation reboiler 13, and is then partially transferred to the countercurrent extraction column 1 via the liquid solvent supply line 4. is recycled to the solvent separation column 9 via the solvent reflux line 14.
〔実施例１〕
発酵アルコール及び合成アルコールの模擬液を、市販の
試薬を用いて作成し、１１の相平衡測定セルに仕込み、
プロパンをプランジャーポンプで相平衡測定セルに所定
温度にて所定圧力になるまで供給し、約２４時間保持し
、溶剤相と液相を各々微少量サンプリングしてガスクロ
マトグラフィーでその組成を分析し、下記式で定義され
るエタノールに対する各不純物の比揮発度（分離度）を
求め、その結果を第２図及び第３図に示した。[Example 1] A simulated solution of fermented alcohol and synthetic alcohol was prepared using commercially available reagents and charged into 11 phase equilibrium measurement cells.
Propane was supplied to the phase equilibrium measurement cell using a plunger pump at a predetermined temperature and pressure until it reached a predetermined pressure, held for about 24 hours, and a small amount of each of the solvent phase and liquid phase was sampled and their compositions were analyzed using gas chromatography. The specific volatility (degree of separation) of each impurity with respect to ethanol defined by the following formula was determined, and the results are shown in FIGS. 2 and 3.
α：エタノールに対するｉ成分の比揮発度ｉ
ｙｌ ：溶剤−相中のｉ成分のモル
分率
ｘｊ ：液相中の１成分のモル分
率
Ｃ２ＨｓＤｌ’ｌ ： Ｃ２Ｈ５ＯＨ（エタノール）の
平衡定数
■
Ｃ２Ｈ，０１ｌ
Ｃ２ｔｌ、ＯＨ：溶剤相中のエタノー
ルのモル分率
Ｃ２Ｈ５０Ｈ：液相中のエタノール
のモル分率
第２図及び第３図より液相エタノール濃度が低い程不純
物の比揮発度が大きくなる傾向にあり、加水してエタノ
ール濃度を下げると不純物が分離しやすくなることを示
している。α: Specific volatility of component i with respect to ethanol i yl: Molar fraction of component i in the solvent phase xj: Mole fraction of one component in the liquid phase C2HsDl'l: Equilibrium constant of C2H5OH (ethanol)■ C2H, 01l C2tl, OH: molar fraction of ethanol in the solvent phase C2H50H: molar fraction of ethanol in the liquid phase From Figures 2 and 3, the lower the concentration of ethanol in the liquid phase, the greater the specific volatility of impurities tends to be. This indicates that reducing the ethanol concentration by adding water makes it easier to separate impurities.
〔実施例２〕
実施例１に示した発酵アルコール及び合成アルコールの
模擬液を、内径５ｃｍ、高さ７ｍの充填塔の中間より１
ｋｇ／ｈで供給し、下部よりプロパンを４ ｋｇ／ ｈ
で、上部より水を１ｋｇ／ｈで供給して向流抽出操作を
行なった。[Example 2] The simulated fermented alcohol and synthetic alcohol liquid shown in Example 1 was poured into a packed tower with an inner diameter of 5 cm and a height of 7 m.
Propane is supplied from the bottom at a rate of 4 kg/h.
Then, water was supplied from the top at a rate of 1 kg/h to carry out a countercurrent extraction operation.
温度４０℃、圧力４０ ｋｇ／ ｃｍ”Ｇの条件下では
供給したエタノールの全量が塔底より抜き出さき
［ｉ
原料組成と塔底への回収率は下記のようであった。Under the conditions of a temperature of 40° C. and a pressure of 40 kg/cm"G, the entire amount of supplied ethanol was extracted from the bottom of the column [i. The raw material composition and recovery rate to the bottom of the column were as follows.
〔実施例３〕
実施例１で、分離率の悪かったアセトアルデヒド、アセ
トン、ｎ−プロパツールについて、第２図、第３図に示
した比揮発度を用いてプロパン溶媒抽出を第１図に示す
フローに従ってシミュレーションした結果、下記条件に
よりエタノールとアセトアルデヒド、アセトン及びｎ
−プロパツールを完全に分離でき、かつエタノールの回
収率は１００％という好ましい結果が得られた。[Example 3] For acetaldehyde, acetone, and n-propanol, which had poor separation rates in Example 1, propane solvent extraction was shown in Figure 1 using the specific volatility shown in Figures 2 and 3. As a result of simulation according to the flow, ethanol, acetaldehyde, acetone and n
- Favorable results were obtained in which propatool could be completely separated and the recovery rate of ethanol was 100%.
（条件）
温 度 ４０℃
圧 力 ４ ０ ｋｇ／’ｃｍ２Ｇ
段 数 ２０段（理論段数）
原料供給段 塔頂より６段目
溶媒流量 ７ｋｇ／ｈ
原料流量 １ ｋｇ／ ｈ
加水流量 １ ｋｇ／ ｈ
〔発明の効果〕
本発明により、発酵アルコール又は化学合成アルコール
中の不純物を溶剤としてプロパン、プロピレン、ｎ−ブ
タン、１−ブタンを用いて向流抽出をする際に、塔頂よ
り水を加えることにより不純物の比揮発度を増大させて
エタノールと分離しやすくさせ、かつ、エタノールが溶
剤に抽出されて損失となるのを防止できる効果を奏する
。(Conditions) Temperature: 40℃ Pressure: 40 kg/'cm2G
Number of plates: 20 (theoretical plate number) Raw material supply stage: 6th stage from the top of the column Solvent flow rate: 7 kg/h Raw material flow rate: 1 kg/h Water addition flow rate: 1 kg/h [Effects of the invention] According to the present invention, in fermented alcohol or chemically synthesized alcohol When performing countercurrent extraction of impurities using propane, propylene, n-butane, or 1-butane as a solvent, adding water from the top of the column increases the specific volatility of the impurities and makes them easier to separate from ethanol. Moreover, it is possible to prevent ethanol from being extracted into a solvent and resulting in loss.
第１菌は本発明の一実施態様を示すフロー、第２図は発
酵アルコール不純物系における不純物のエタノールに対
する比揮発度を、また第３図は合成アルコール微量不純
物の比揮発度を夫々示す図表である。The first bacterium is a flowchart showing one embodiment of the present invention, FIG. 2 is a chart showing the specific volatility of impurities to ethanol in the fermented alcohol impurity system, and FIG. 3 is a chart showing the specific volatility of trace impurities in synthetic alcohol. be.
Claims (1)
ノール／不純物からなる混合物を抽出塔中部に供給し、
液体状態のプロパン、プロピレン、ｎ−ブタン、ｉ−ブ
タン単独又はそれらの混合物の溶剤を該抽出塔下部より
、又、水を該抽出塔の上部より供給し、該抽出塔上部よ
り実質的にエタノールを含まない溶剤／不純物混合物を
、該抽出塔下部より実質的に不純物を含まない水／エタ
ノール／溶剤混合物を回収することを特徴とするアルコ
ールの精製方法。(1) Supplying a mixture of water/ethanol/impurities produced by a fermentation method or a chemical synthesis method to the middle part of the extraction column,
A liquid solvent of propane, propylene, n-butane, i-butane alone or a mixture thereof is supplied from the lower part of the extraction column, water is supplied from the upper part of the extraction column, and substantially ethanol is supplied from the upper part of the extraction column. A method for purifying alcohol, which comprises recovering a substantially impurity-free water/ethanol/solvent mixture from the lower part of the extraction column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2322328A JPH0651084B2 (en) | 1990-11-28 | 1990-11-28 | How to purify alcohol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2322328A JPH0651084B2 (en) | 1990-11-28 | 1990-11-28 | How to purify alcohol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH04193303A true JPH04193303A (en) | 1992-07-13 |
| JPH0651084B2 JPH0651084B2 (en) | 1994-07-06 |
Family
ID=18142415
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2322328A Expired - Lifetime JPH0651084B2 (en) | 1990-11-28 | 1990-11-28 | How to purify alcohol |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0651084B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007161599A (en) * | 2005-12-09 | 2007-06-28 | Daicel Chem Ind Ltd | Method for producing ethylamines |
| WO2008026446A1 (en) * | 2006-08-29 | 2008-03-06 | Kabushiki Kaisha Kobe Seiko Sho | Method for extracting target substance and apparatus for extracting target substance |
| JP2014171417A (en) * | 2013-03-07 | 2014-09-22 | Mitsui Eng & Shipbuild Co Ltd | Bioethanol recovering method and bioethanol recovering system |
-
1990
- 1990-11-28 JP JP2322328A patent/JPH0651084B2/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2007161599A (en) * | 2005-12-09 | 2007-06-28 | Daicel Chem Ind Ltd | Method for producing ethylamines |
| WO2008026446A1 (en) * | 2006-08-29 | 2008-03-06 | Kabushiki Kaisha Kobe Seiko Sho | Method for extracting target substance and apparatus for extracting target substance |
| JP2014171417A (en) * | 2013-03-07 | 2014-09-22 | Mitsui Eng & Shipbuild Co Ltd | Bioethanol recovering method and bioethanol recovering system |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0651084B2 (en) | 1994-07-06 |
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