JPH0567633B2 - - Google Patents
Info
- Publication number
- JPH0567633B2 JPH0567633B2 JP63259903A JP25990388A JPH0567633B2 JP H0567633 B2 JPH0567633 B2 JP H0567633B2 JP 63259903 A JP63259903 A JP 63259903A JP 25990388 A JP25990388 A JP 25990388A JP H0567633 B2 JPH0567633 B2 JP H0567633B2
- Authority
- JP
- Japan
- Prior art keywords
- furfural
- concentration
- temperature
- column
- pressure
- 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
Links
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 claims description 180
- 238000000034 method Methods 0.000 claims description 26
- 238000006243 chemical reaction Methods 0.000 claims description 23
- 239000012530 fluid Substances 0.000 claims description 19
- 238000004519 manufacturing process Methods 0.000 claims description 14
- 239000000243 solution Substances 0.000 claims description 13
- SRBFZHDQGSBBOR-IOVATXLUSA-N D-xylopyranose Chemical compound O[C@@H]1COC(O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-IOVATXLUSA-N 0.000 claims description 12
- 239000007864 aqueous solution Substances 0.000 claims description 9
- 239000002253 acid Substances 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 229920002488 Hemicellulose Polymers 0.000 claims description 7
- 150000002972 pentoses Chemical class 0.000 claims description 7
- PYMYPHUHKUWMLA-UHFFFAOYSA-N arabinose Natural products OCC(O)C(O)C(O)C=O PYMYPHUHKUWMLA-UHFFFAOYSA-N 0.000 claims description 6
- SRBFZHDQGSBBOR-UHFFFAOYSA-N beta-D-Pyranose-Lyxose Natural products OC1COC(O)C(O)C1O SRBFZHDQGSBBOR-UHFFFAOYSA-N 0.000 claims description 6
- 239000003054 catalyst Substances 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 3
- 230000007423 decrease Effects 0.000 claims 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 description 12
- 239000001569 carbon dioxide Substances 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 11
- 239000000203 mixture Substances 0.000 description 5
- 238000000605 extraction Methods 0.000 description 4
- 238000010533 azeotropic distillation Methods 0.000 description 3
- 238000007664 blowing Methods 0.000 description 3
- 238000004821 distillation Methods 0.000 description 3
- 238000010793 Steam injection (oil industry) Methods 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000007086 side reaction Methods 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000194 supercritical-fluid extraction Methods 0.000 description 1
- 235000013311 vegetables Nutrition 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
- 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
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Landscapes
- Furan Compounds (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、フルフラールの製造工程において、
超臨界流体を使用して効率よくフルフラールを製
造し、濃縮する方法に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention provides a method for producing furfural in the production process of furfural.
The present invention relates to a method for efficiently producing and concentrating furfural using supercritical fluid.
フルフラールをペントースまたは植物質中のヘ
ミセルロースから、酸を触媒として製造する方法
は既に知られている。この工程において、生成し
たフルフラールを反応性が高いため、副反応によ
り分解したり縮合物を生じて消費され、収率が低
下するので、これを防ぐためには反応系に存在す
るフルフラールの濃度を小さくするか反応速度を
高め反応時間を短くする必要がある。その代表的
な方法として、(1)反応器中に大量の水蒸気を吹き
込んで水蒸気と共にフルフラールを回収する方
法。
A method for producing furfural from pentose or hemicellulose in vegetable matter using an acid as a catalyst is already known. In this process, the produced furfural is highly reactive, so it is decomposed by side reactions or consumed by forming condensates, reducing the yield. To prevent this, the concentration of furfural present in the reaction system is reduced. It is necessary to increase the reaction rate and shorten the reaction time. Typical methods include (1) a method in which furfural is recovered together with the steam by injecting a large amount of steam into the reactor;
(2)フルフラールの分配率の高い有機溶剤を用い
てフルフラールを回収する方法。(3)管型反応器な
どを用いて高温で短時間の内に反応させた後、反
応液をフラツシユさせ、水蒸気と共に回収する方
法などがある。 (2) A method of recovering furfural using an organic solvent with a high distribution rate of furfural. (3) There is a method in which the reaction is carried out at high temperature in a short time using a tubular reactor, and then the reaction liquid is flashed and recovered together with water vapor.
しかしながら、(1)の方法においては大量の水蒸
気を必要とすること、また回収される水溶液中の
フルフラール濃度は低く（通常和wt％程度）、か
つフルフラール／水系の気液平衡ではフルフラー
ル約35wt％で共沸点があり、水の沸点との差が
小さいことから、共沸蒸留による濃縮工程におい
て大量の熱エネルギーを要するという欠点もあ
る。 However, method (1) requires a large amount of water vapor, and the concentration of furfural in the recovered aqueous solution is low (usually about 35 wt% total), and the vapor-liquid equilibrium of the furfural/water system is about 35 wt% furfural. Since it has an azeotropic point and the difference from the boiling point of water is small, it also has the disadvantage that a large amount of thermal energy is required in the concentration process by azeotropic distillation.
(2)の方法においては回収時に潜熱は必要となら
ないが、溶剤が高価であること、溶剤とフルフラ
ールを分解するための蒸留工程において大量の熱
エネルギーを要するという問題がある。 Although the method (2) does not require latent heat during recovery, there are problems in that the solvent is expensive and that a large amount of thermal energy is required in the distillation process to decompose the solvent and furfural.
(3)の方法においても(1)とほぼ同様の問題があ
る。 Method (3) also has almost the same problem as (1).
本発明はキシロースなどのペントースを含有す
る水溶液や植物質中のヘミセルロースからフルフ
ラールを製造する工程において、エネルギー消費
量が少なく、かつ収率の高い方法を提供すること
およびフルフラール水溶液を高濃度まで濃縮する
ための工業的に有利な方法を提供することであ
り、超臨界抽出法を応用したフルフラール製造工
程について鋭意研究を重ねた結果、本発明をなす
に至つた。
The present invention provides a method for producing furfural from an aqueous solution containing pentose such as xylose or hemicellulose in plants, with low energy consumption and high yield, and a method for concentrating an aqueous furfural solution to a high concentration. The purpose of this invention is to provide an industrially advantageous method for the production of furfural, and as a result of extensive research into furfural production processes using supercritical extraction, the present invention was developed.
すなわち、本発明によれば、キシロースなどの
ペントースを含有する水溶液や植物質中のヘミセ
ルロースから、酸を触媒としてフルフラールを製
造する工程において、臨界温度、臨界圧力を超え
る温度、圧力の流体（超臨界流体と称する）を、
反応器中のフルフラールを含む反応液と接触させ
流通させることにより、フルフラールを抽出し、
反応系外に回収することを特徴とするフルフラー
ルの製造方法が提供され、またフルフラールを含
有する超臨界流体を、濃縮液の一部を還流させる
構造のフルフラール濃縮塔に流通させてフルフラ
ールの濃度を高めることを特徴とするフルフラー
ルの濃縮方法が提供される。
That is, according to the present invention, in the process of producing furfural from an aqueous solution containing pentose such as xylose or hemicellulose in plants using an acid as a catalyst, a fluid at a temperature and pressure exceeding the critical temperature and pressure (supercritical (referred to as fluid),
Furfural is extracted by contacting and circulating the reaction solution containing furfural in the reactor,
A method for producing furfural is provided, which is characterized in that furfural is recovered outside the reaction system, and a supercritical fluid containing furfural is passed through a furfural concentration column having a structure in which a part of the concentrated liquid is refluxed to reduce the concentration of furfural. A method for enriching furfural is provided.
更に、本発明によれば、キシロースなどのペン
トースを含有する水溶液や植物質中のヘミセルロ
ースから、酸を触媒としてフルフラールを製造す
る工程において、臨界温度、臨界圧力を超える温
度、圧力の流体（超臨界流体と称する）を、反応
器中のフルフラールを含む反応液と接触させ流通
させることにより、フルフラールを抽出し、つい
でフルフラールを含有する超臨界流体を濃縮液の
一部を還流させる構造のフルフラール濃縮塔に流
通させてフルフラールの濃度を高め、フルフラー
ルを反応系外に回収することを特徴とするフルフ
ラールの製造方法が提供される。 Furthermore, according to the present invention, in the process of producing furfural from an aqueous solution containing pentoses such as xylose or hemicellulose in plants using an acid as a catalyst, a fluid at a temperature and pressure exceeding the critical temperature and pressure (supercritical A furfural concentrating column has a structure in which furfural is extracted by bringing a fluid (referred to as a fluid) into contact with a reaction solution containing furfural in a reactor and flowing it, and then a part of the concentrated solution is refluxed to a supercritical fluid containing furfural. Provided is a method for producing furfural, characterized in that the concentration of furfural is increased by distributing the furfural through a reaction system, and the furfural is recovered outside the reaction system.
次に図面によつて、本発明の製造法および濃縮
方法を説明する。 Next, the production method and concentration method of the present invention will be explained with reference to the drawings.
第１図は、圧力200Kg／cm2におけるフルフラー
ル／水／超臨界二酸化炭素３成分系の気液平衡
を、二酸化炭素を除いたフルフラール／水２成分
についてのｘ−ｙ線図で示したものである。 Figure 1 shows the vapor-liquid equilibrium of the furfural/water/supercritical carbon dioxide three-component system at a pressure of 200 kg/cm 2 as an x-y diagram for the two components furfural/water excluding carbon dioxide. be.
反応器にペントース又はヘミセルロースと触媒
としての酸を仕込み、フルフラール生成反応を
140℃で行なわせ、超臨界二酸化炭素を流通させ
てフルフラールを抽出し、反応器中のフルフラー
ル濃度を2wt％に保つた場合、第１図より超臨界
二酸化炭素中に抽出されるフルフラール／水２成
分中のフルフラール濃度は38wt％（この組成は
既にフルフラール／水２成分系の共沸組成を超え
ている）となる。これを塔頂部を80℃まで冷却し
たフルフラール濃縮塔に導入し、適当な還流をか
けて、塔頂部で超臨界二酸化炭素と接触する液相
組成を6wt％以上に保てば、90wt％以上の濃度の
フルフラールを塔頂より得ることができる。濃縮
塔を80℃よりもつと低温で操作すれば、さらに高
濃度のほとんど無水のフルフラールを得ることも
可能である。 A reactor is charged with pentose or hemicellulose and an acid as a catalyst to initiate the furfural production reaction.
When furfural is extracted by flowing supercritical carbon dioxide at 140℃ and the furfural concentration in the reactor is maintained at 2wt%, as shown in Figure 1, the furfural/water extracted into supercritical carbon dioxide2 The concentration of furfural in the component is 38 wt% (this composition already exceeds the azeotropic composition of the two-component furfural/water system). If this is introduced into a furfural condensation tower whose top part is cooled to 80℃, and by applying appropriate reflux to maintain the liquid phase composition in contact with supercritical carbon dioxide at the top part of the tower at 6wt% or more, it is possible to achieve a concentration of 90wt% or more. Concentrated furfural can be obtained from the top of the column. Even higher concentrations of almost anhydrous furfural can be obtained if the concentrator is operated at temperatures below 80°C.
フルフラール生成反応は120〜200℃、好ましく
は140℃以上で行なわれ、圧力は超臨界流体とし
て二酸化炭素を使用する場合は、100Kg／cm2以上
である。超臨界流体としては二酸化炭素以外の流
体を使用することもできる。 The furfural production reaction is carried out at a temperature of 120 to 200°C, preferably 140°C or higher, and the pressure is 100 Kg/cm 2 or higher when carbon dioxide is used as the supercritical fluid. Fluids other than carbon dioxide can also be used as the supercritical fluid.
本発明によれば、フルフラール製造工程におい
て、従来の水蒸気吹き込み法と共沸蒸留の組合せ
のように大量の熱エネルギーを必要とせずに、高
濃度のフルフラールを効率よく回収することがで
きる。
According to the present invention, high-concentration furfural can be efficiently recovered in the furfural production process without requiring a large amount of thermal energy unlike the conventional combination of steam blowing and azeotropic distillation.
すなわち超臨界流体へは水に比べてフルフラー
ルの方がはるかに分配しやすいことから、水蒸気
吹き込み法に比べて高濃度のフルフラールを効率
よく回収することができる。従つて反応液中のフ
ルフラール濃度も低く保たれ、副反応を防いで高
収率を得ることができる。さらに超臨界流体／フ
ルフラール／水系の気液平衡特性を利用して、反
応抽出器に濃縮塔を連結することにより、蒸留法
に比べてはるかに高濃度のフルフラールを回収す
ることができる。従来法では水蒸気吹き込み法に
よる大量の水蒸気使用に加えて、それにより得ら
れた数wt％程度のフルフラール水溶液は、共沸
蒸留により約35wt％共沸組成までしか濃縮でき
ないこと、および蒸留塔の塔底と塔頂の温度差が
数℃しかないことなどから、濃縮工程でも大量の
熱エネルギーを必要とするという欠点があつた
が、本発明ではこれらの欠点が除かれ、高濃度の
フルフラールを効率よく得ることができる。 That is, since furfural is much easier to distribute into the supercritical fluid than water, furfural at a higher concentration can be recovered more efficiently than the steam injection method. Therefore, the concentration of furfural in the reaction solution can be kept low, side reactions can be prevented, and high yields can be obtained. Furthermore, by utilizing the vapor-liquid equilibrium characteristics of the supercritical fluid/furfural/water system and connecting a concentration column to the reaction extractor, furfural can be recovered at a much higher concentration than in the distillation method. In the conventional method, in addition to using a large amount of steam by steam blowing, the resulting aqueous furfural solution of several wt% can only be concentrated to an azeotropic composition of about 35 wt% by azeotropic distillation, and the distillation column Since the temperature difference between the bottom and the top of the tower is only a few degrees Celsius, the concentration process also had the drawback of requiring a large amount of thermal energy. However, the present invention eliminates these drawbacks and makes it possible to efficiently process furfural at high concentrations. You can get a good deal.
次に本発明を実施例により、さらに詳細に説明
する。
Next, the present invention will be explained in more detail with reference to Examples.
実施例 １
温度140℃において、１のオートクレーブに
2.5wt％フルフラール水溶液0.5を仕込み、圧力
100〜200Kg／cm2の超臨界二酸化炭素100Nを流
通させて水溶液を抽出し、大気圧まで減圧し冷却
して得た濃縮物の組成を求めた。その結果を第２
図に示す。圧力が高いほど高濃度のフルフラール
が得られ、200Kg／cm2では約35wt％であつた。こ
れは第１図の気液平衡測定結果とほぼ一致し、水
蒸気吹き込み法の３倍近い濃度である。圧力を増
せばさらに高濃度のフルフラール抽出できること
が明らかである。Example 1 At a temperature of 140°C, in an autoclave of 1.
Prepare 0.5% of 2.5wt% furfural aqueous solution and pressure
The aqueous solution was extracted by passing 100 N of supercritical carbon dioxide at 100 to 200 Kg/cm 2 , and the composition of the concentrate obtained by cooling and reducing the pressure to atmospheric pressure was determined. The second result is
As shown in the figure. The higher the pressure, the higher the concentration of furfural obtained, and at 200Kg/cm 2 it was about 35wt%. This almost coincides with the vapor-liquid equilibrium measurement results shown in Figure 1, and is nearly three times the concentration of the steam blowing method. It is clear that a higher concentration of furfural can be extracted by increasing the pressure.
実施例 ２
0.1規定の希硫酸に50ｇ／のキシロースを溶
解し溶液0.5を内容積１のオートクレーブに
仕込み、温度140℃で４時間反応を行なつたとこ
ろ、反応後のフルフラール濃度は0.86wt％、フル
フラールの収率は49％であつた。Example 2 50g/xylose was dissolved in 0.1N diluted sulfuric acid, 0.5% of the solution was charged into an autoclave with an internal volume of 1, and the reaction was carried out at a temperature of 140°C for 4 hours.The furfural concentration after the reaction was 0.86wt%. The yield of furfural was 49%.
次に同条件で、圧力150Kg／cm2で二酸化炭素を
6.5N／minの流速でオートクレーブ底部より流
通させて４時間反応を行なつたところ、反応溶液
中のフルフラール濃度は0.4wt％に低下し、収率
は58％に向上した。また、抽出液中のフルフラー
ル濃度は6.3wt％であつた。この条件で水蒸気吹
き込みで抽出した場合の回収液濃度は4wt％程度
である。 Next, under the same conditions, carbon dioxide was added at a pressure of 150Kg/ cm2.
When the reaction was carried out for 4 hours by flowing from the bottom of the autoclave at a flow rate of 6.5 N/min, the furfural concentration in the reaction solution decreased to 0.4 wt% and the yield improved to 58%. Further, the furfural concentration in the extract was 6.3 wt%. The concentration of the recovered liquid when extracted by steam injection under these conditions is approximately 4 wt%.
以上の結果から超臨界二酸化炭素を使用して生
成したフルフラールを抽出し、回収することによ
り、反応液中のフルフラール濃度を低く保ち、収
率を向上できるとともに、従来法に比べて高濃度
のフルフラールを回収できることが明らかになつ
た。抽出圧力をあげて抽出速度を高めたり、反応
濃度、反応物濃度、酸濃度、酸種類などを適切に
選ぶことにより、さらに高濃度のフルフラールが
回収でき、収率をさらに高めることが可能であ
る。 From the above results, by extracting and recovering furfural produced using supercritical carbon dioxide, it is possible to maintain a low concentration of furfural in the reaction solution and improve the yield, as well as to increase the concentration of furfural in the reaction solution compared to the conventional method. It became clear that it was possible to recover the By increasing the extraction pressure to increase the extraction rate, and by appropriately selecting the reaction concentration, reactant concentration, acid concentration, acid type, etc., it is possible to recover even higher concentrations of furfural and further increase the yield. .
第１図は、超臨界二酸化炭素／フルフラール／
水３成分系の圧力200Kg／cm2、温度80℃および140
℃における気液平衡関係を、二酸化炭素を除いた
液相と気相のフルフラール濃度の関係で示したも
のであり、第２図は、140℃において超臨界二酸
化炭素を使用してフルフラール水溶液を抽出した
ときの抽出圧力と抽出物中のフルフラール濃度の
関係を示したものである。
Figure 1 shows supercritical carbon dioxide/furfural/
Water three-component system pressure 200Kg/cm 2 , temperature 80℃ and 140℃
The gas-liquid equilibrium relationship at ℃ is shown by the relationship between the furfural concentration in the liquid phase excluding carbon dioxide and the gas phase. Figure 2 shows the extraction of furfural aqueous solution using supercritical carbon dioxide at 140℃. This figure shows the relationship between extraction pressure and furfural concentration in the extract.
Claims (1)
液や植物質中のヘミセルロースから、酸を触媒と
してフルフラールを製造する工程において、臨界
温度、臨界圧力を超える温度、圧力の流体（超臨
界流体と称する）を、反応器中のフルフラールを
含む反応液と接触させ流通させることにより、フ
ルフラールを抽出し、反応系外に回収することを
特徴とするフルフラールの製造方法。 ２ フルフラールを含有する超臨界流体を、濃縮
液の一部を還流させる構造のフルフラール濃縮塔
に流通させてフルフラールの濃度を高めることを
特徴とするフルフラールの濃縮方法。 ３ フルフラール濃縮塔の塔底から塔頂に温度が
下がるような温度勾配を持たせることを特徴とす
る特許請求の範囲第２項記載の方法。 ４ キシロースなどのペントースを含有する水溶
液や植物質中のヘミセルロースから、酸を触媒と
してフルフラールを製造する工程において、臨界
温度、臨界圧力を超える温度、圧力の流体（超臨
界流体と称する）を、反応器中のフルフラールを
含む反応液と接触させ流通させることにより、フ
ルフラールを抽出し、ついでフルフラールを含有
する超臨界流体を濃縮液の一部を還流させる構造
のフルフラール濃縮塔に流通させてフルフラール
の濃度を高め、フルフラールを反応系外に回収す
ることを特徴とするフルフラールの製造方法。 ５ フルフラール濃縮塔の塔底から塔頂に温度が
下がるような温度勾配を持たせることを特徴とす
る特許請求の範囲第４項記載の方法。[Claims] 1. In the process of producing furfural from an aqueous solution containing pentose such as xylose or from hemicellulose in plants using an acid as a catalyst, a fluid at a temperature and pressure exceeding the critical temperature and pressure (supercritical fluid) is used. A method for producing furfural, which comprises extracting furfural by bringing it into contact with a reaction solution containing furfural in a reactor and distributing it, and recovering it outside the reaction system. 2. A method for concentrating furfural, which comprises increasing the concentration of furfural by flowing a supercritical fluid containing furfural through a furfural concentrating column configured to reflux a part of the concentrated liquid. 3. The method according to claim 2, characterized in that the furfural concentration column is provided with a temperature gradient such that the temperature decreases from the bottom to the top of the column. 4. In the process of producing furfural from an aqueous solution containing pentoses such as xylose or from hemicellulose in plants using an acid as a catalyst, a fluid at a temperature and pressure exceeding the critical temperature and pressure (referred to as a supercritical fluid) is reacted. Furfural is extracted by contacting and circulating the furfural-containing reaction solution in the vessel, and then the furfural-containing supercritical fluid is passed through a furfural concentrating column that refluxes a portion of the concentrated solution to reduce the concentration of furfural. A method for producing furfural, which is characterized by increasing the amount of furfural and recovering furfural outside the reaction system. 5. The method according to claim 4, characterized in that the furfural concentration column is provided with a temperature gradient such that the temperature decreases from the bottom to the top of the column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63259903A JPH02108682A (en) | 1988-10-14 | 1988-10-14 | Production and concentration of furfural |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63259903A JPH02108682A (en) | 1988-10-14 | 1988-10-14 | Production and concentration of furfural |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02108682A JPH02108682A (en) | 1990-04-20 |
| JPH0567633B2 true JPH0567633B2 (en) | 1993-09-27 |
Family
ID=17340536
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63259903A Granted JPH02108682A (en) | 1988-10-14 | 1988-10-14 | Production and concentration of furfural |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02108682A (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1319960C (en) * | 2005-09-26 | 2007-06-06 | 天津大学 | Method for preparing furfural by taking xylose mother liquor as raw material |
| UA98002C2 (en) * | 2007-09-07 | 2012-04-10 | Фураникс Технолоджиз Б.В. | Mixture of furfural and 5-(alkoxymethyl)furfural derivatives from sugars and alcohols |
| US9024047B2 (en) | 2010-12-21 | 2015-05-05 | E I Du Pont De Nemours And Company | Methods for furfural production from branched non-fermentable sugars in stillage or syrup |
| CA2859996A1 (en) | 2011-12-28 | 2013-07-04 | Paul Joseph Fagan | Process for the production of furfural |
| US9181211B2 (en) | 2011-12-28 | 2015-11-10 | E I Du Pont De Nemours And Company | Process for the production of furfural |
| WO2013102002A1 (en) | 2011-12-28 | 2013-07-04 | E. I. Du Pont De Nemours And Company | Processes for making furfurals |
| AU2012362300A1 (en) | 2011-12-28 | 2014-06-26 | E. I. Du Pont De Nemours And Company | Process for the production of furfural |
| UA116630C2 (en) | 2012-07-03 | 2018-04-25 | Ксілеко, Інк. | METHOD OF CONVERTING SUGAR TO FURFURYL ALCOHOL |
| JP6648545B2 (en) * | 2016-02-08 | 2020-02-14 | 三菱ケミカル株式会社 | Method for producing sugar liquid for furfural production raw material and method for producing furfural |
-
1988
- 1988-10-14 JP JP63259903A patent/JPH02108682A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPH02108682A (en) | 1990-04-20 |
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