JPS6355497B2 - - Google Patents
Info
- Publication number
- JPS6355497B2 JPS6355497B2 JP59116846A JP11684684A JPS6355497B2 JP S6355497 B2 JPS6355497 B2 JP S6355497B2 JP 59116846 A JP59116846 A JP 59116846A JP 11684684 A JP11684684 A JP 11684684A JP S6355497 B2 JPS6355497 B2 JP S6355497B2
- Authority
- JP
- Japan
- Prior art keywords
- distillation column
- ethanol
- heat pump
- condensate
- vapor
- 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
Links
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 48
- 238000004821 distillation Methods 0.000 claims description 31
- 238000010521 absorption reaction Methods 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 9
- 239000012535 impurity Substances 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 6
- 238000000746 purification Methods 0.000 description 8
- 238000010586 diagram Methods 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000007796 conventional method Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000006096 absorbing agent Substances 0.000 description 3
- 239000011550 stock solution Substances 0.000 description 3
- 239000007864 aqueous solution Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000203 mixture Substances 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
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
【発明の詳細な説明】
産業上の利用分野
本発明はエタノール水溶液の分離方法に関する
ものである。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to a method for separating an aqueous ethanol solution.
従来例の構成とその問題点
第１図に精製塔における実施例を示す。従来の
エタノール水溶液の分離方法として、蒸留塔１と
第一〜第三の分縮器２，３，４を用いる方法があ
る。これは、エタノール水溶液５を蒸留塔１に導
いて蒸留し、蒸留塔１で発生した大部分がエタノ
ールの蒸気６すなわち水蒸気や不純物を含む塔頂
気体を第一〜第三の分縮器２，３，４に直列に通
すもので、エタノール純度の最も高い第一分縮器
２の凝縮液７は分離して精製塔８へ供給し第二分
縮器３の凝縮液９は蒸留塔１へ、不純物を多く含
む第三分縮器４の凝縮液１０は不純物処理塔１１
へ、それぞれ導かれる。このように、三段もの分
縮器が用いられるのは水とエタノールの蒸気圧が
近いこと、原液に不純物が含まれていること等の
理由に基づく。Configuration of conventional example and its problems Figure 1 shows an example of a purification column. As a conventional method for separating an aqueous ethanol solution, there is a method using a distillation column 1 and first to third dephlegmators 2, 3, and 4. In this system, an aqueous ethanol solution 5 is introduced into a distillation column 1 to be distilled, and the vapor 6 generated in the distillation column 1, which is mostly ethanol, i.e., the top gas containing water vapor and impurities, is transferred to the first to third dephlegmators 2, 3 and 4 in series, the condensate 7 of the first fractionator 2 with the highest ethanol purity is separated and supplied to the purification column 8, and the condensate 9 of the second fractionator 3 is sent to the distillation column 1. , the condensate 10 of the third condenser 4 containing many impurities is sent to the impurity treatment tower 11
Each will be guided to As described above, the reason why a three-stage dephlegmator is used is because the vapor pressures of water and ethanol are similar, and the raw solution contains impurities.
なお、第２図に示すように、原液の濃度はX1
＝10Wt％〜30Wt％、還流比は、蒸発量の60％〜
85％程度で、精製エタノール当り必要な分離のた
めのエネルギーは700kcal／Kg〜1600kcal／Kgで
ある。 As shown in Figure 2, the concentration of the stock solution is
= 10Wt% ~ 30Wt%, reflux ratio is 60% ~ evaporation amount
At about 85%, the energy required for separation per purified ethanol is 700 kcal/Kg to 1600 kcal/Kg.
一方、第５図に示すように、蒸留塔１と吸収ヒ
ートポンプ１２を用いる方法もある。これは、エ
タノール水溶液５を蒸留塔１に導いて蒸留し、蒸
留塔１で発生した蒸気６を吸収ヒートポンプ１２
の再生器Ｒおよび蒸発器Ｅに熱源として導き、そ
の凝縮液１３の一部を精製塔８へ、残りを蒸留塔
１へ還流するものである。すなわち、蒸留塔１の
蒸気６が有する熱エネルギーの吸収ヒートポンプ
１２の熱源として利用したものと言える。なお、
第５図中Ｃは凝縮器Ａは吸収器である。 On the other hand, as shown in FIG. 5, there is also a method using a distillation column 1 and an absorption heat pump 12. In this system, an aqueous ethanol solution 5 is introduced into a distillation column 1 to be distilled, and the vapor 6 generated in the distillation column 1 is absorbed by a heat pump 12.
A portion of the condensate 13 is refluxed to the purification column 8 and the remainder to the distillation column 1. In other words, it can be said that the thermal energy contained in the steam 6 of the distillation column 1 is utilized as a heat source for the absorption heat pump 12 . In addition,
In FIG. 5, the condenser A is an absorber.
しかしながら、これら従来の方法によると、蒸
留分離に多大なエネルギーを要し、後者の方法に
あつては、第１、第２分縮機能が無くなるため精
製塔８に導くエタノールの純度が落ち、精製塔８
では必要熱が増えるという欠点があつた。 However, according to these conventional methods, a large amount of energy is required for distillation separation, and in the case of the latter method, the first and second partial condensation functions are lost, so the purity of the ethanol led to the purification column 8 decreases, and the purification tower 8
However, the disadvantage was that the required heat increased.
発明の目的
本発明は上記従来の欠点を解消するエタノール
の分離方法を提供することを目的とする。OBJECTS OF THE INVENTION It is an object of the present invention to provide a method for separating ethanol that eliminates the above-mentioned conventional drawbacks.
発明の構成
上記目的を達成するため、本発明のエタノール
の分離方法は、不純物を含むエタノールを蒸留塔
に導いて蒸留し、前記蒸留塔で発生した大部分が
エタノールの蒸気を吸収ヒートポンプの蒸発器に
熱源として導き、その凝縮液を留出液として分離
する一方、残りの該蒸気を前記吸収ヒートポンプ
の再生器に熱源として導き、その凝縮液を前記蒸
留塔に還流し、残りの該蒸気を分縮器に導く構成
としたものであり、これにより、エタノールの純
度を落とすことなく、蒸留分離に必要なエネルギ
ーを低減することができるものである。Composition of the Invention In order to achieve the above object, the ethanol separation method of the present invention involves introducing ethanol containing impurities into a distillation column, distilling it, and absorbing the vapor, which is mostly ethanol, generated in the distillation column into an evaporator of a heat pump. The remaining vapor is introduced as a heat source to the regenerator of the absorption heat pump, the condensate is refluxed to the distillation column, and the remaining vapor is separated. The structure is such that the ethanol is led to a condenser, thereby making it possible to reduce the energy required for distillation separation without reducing the purity of ethanol.
実施例と作用
以下、本発明の一実施例を図面に基づいて説明
するが、その前に先ず一般的説明を行う。Embodiment and Operation An embodiment of the present invention will be described below with reference to the drawings, but first a general explanation will be given first.
吸収ヒートポンプの蒸発器Ｅと再生器Ｒで必要
とする熱量の比は回収器の大きさによつて異な
り、回収器での回収率により第４図に示すよう
に、QR／QEは0.7〜0.98程度となる。 The ratio of the amount of heat required by the evaporator E and the regenerator R of an absorption heat pump varies depending on the size of the recovery device, and as shown in Figure 4, Q R /Q E is 0.7 depending on the recovery rate in the recovery device. ~0.98.
したがつて、第３図に示すようにQ2：Q1＋QB
か0.7〜1/0.7となる範囲は還流比が77％以下のと
ころでほとんど可能となる。また、この範囲内で
蒸留塔から排出される排熱のうち利用可能と思わ
れる75℃以上の熱量は、加熱蒸気の熱量に比して
第３図のようになつている。すなわち、
廃熱の総和（Q1＋Q2＋QB）は加熱に必要な
量よりも多い（原液が約99℃で供給されるた
め）。 Therefore, as shown in Figure 3, Q 2 :Q 1 +Q B
The range of 0.7 to 1/0.7 is almost possible when the reflux ratio is 77% or less. Furthermore, within this range, the amount of heat above 75°C that is considered usable among the waste heat discharged from the distillation column is compared to the amount of heat of the heated steam, as shown in Figure 3. That is, the total amount of waste heat (Q 1 +Q 2 +Q B ) is greater than the amount required for heating (because the stock solution is supplied at approximately 99°C).
Q1＋QB＝Q2となるところの還流比が60％〜
70％の範囲にある。 The reflux ratio where Q 1 + Q B = Q 2 is 60% ~
In the 70% range.
温度的には加熱する塔底温度が約107℃、塔
頂ガス（蒸気）の凝縮温度が77℃〜78℃であ
る。 In terms of temperature, the bottom temperature of the heated column is approximately 107°C, and the condensation temperature of the tower top gas (steam) is 77°C to 78°C.
そこで、このような特性を考慮して、本発明は
蒸留塔と吸収ヒートポンプを分縮機能を失わせる
ことなく組合わせて用いるようにした。 Therefore, in consideration of such characteristics, the present invention uses a distillation column and an absorption heat pump in combination without losing the partial condensation function.
第６図において、１は蒸留塔１２は吸収ヒート
ポンプ、Ｒはその再生器、Ｃは凝縮器、Ａは吸収
器、Ｅは蒸発器で、この蒸発器Ｅは第一分縮器と
して、前記再生器Ｒは第二分縮器として用いられ
る。４は第三分縮器、８は精製塔、１８は流量調
節器を示す。なお、蒸発器Ｅは２分割され、一方
の部屋は前述のように第１分縮器として用いら
れ、他方の部屋は塔底液１４を熱源とする熱交換
室として用いられる。 In FIG. 6, 1 is a distillation column 12 which is an absorption heat pump, R is its regenerator, C is a condenser, A is an absorber, and E is an evaporator. Container R is used as a second condenser. 4 is a third dephlegmator, 8 is a purification column, and 18 is a flow rate regulator. The evaporator E is divided into two parts, one of which is used as a first dephlegmator as described above, and the other part is used as a heat exchange room using the bottom liquid 14 as a heat source.
このような構成で先ず、エタノール水溶液５を
蒸留塔１に導き蒸留する。次に、蒸留塔１で発生
した蒸気６を吸収ヒートポンプ１２の蒸発器Ｅに
熱源として導き、その凝縮液１６を精製塔８へ導
く一方、残りの蒸気１５を再生器Ｒに熱源として
導く、このとき、蒸発器Ｅの他方の部屋には塔底
液１４を導き熱回収を行う。次に、再生器Ｒの凝
縮液１７は蒸留塔１に還流し、残りの蒸気１５は
第三分縮器４に導いて冷却水に完全に凝縮させ
る。なお、還流比が60％〜77％の範囲で各機器の
熱量およびヒートポンプの回収器（図示せず）の
熱量大きさを決定する。また、第３図において
Q2＜Q1＋QBの範囲では、再生器Ｒと蒸発器Ｅで
互いに交換したフローとする。 With such a configuration, first, the ethanol aqueous solution 5 is introduced into the distillation column 1 and distilled. Next, the steam 6 generated in the distillation column 1 is guided to the evaporator E of the absorption heat pump 12 as a heat source, the condensate 16 thereof is guided to the purification column 8, and the remaining vapor 15 is guided to the regenerator R as a heat source. At this time, the bottom liquid 14 is introduced into the other chamber of the evaporator E for heat recovery. Next, the condensate 17 from the regenerator R is returned to the distillation column 1, and the remaining vapor 15 is led to the third demultiplexer 4 and completely condensed into cooling water. Note that the heat amount of each device and the heat amount size of the heat pump recovery device (not shown) are determined within the range of the reflux ratio from 60% to 77%. Also, in Figure 3
In the range Q 2 <Q 1 +Q B , the regenerator R and evaporator E exchange flows.
第７図は還流比が小さくて良い原液の場合に用
いる流れを示し、この場合は蒸留塔１の底液１４
を蒸発器Ｅに通さない。なお吸収器Ａに直接底液
を受熱流体として循環させてもよい。またこれら
実施例において、吸収ヒートポンプ１２より発生
する低圧蒸気を該蒸溜塔１又は他の蒸留塔へ直接
戻すように構成してもよい。 Figure 7 shows the flow used in the case of a good stock solution with a small reflux ratio; in this case, the bottom liquid 14 of the distillation column 1
Do not pass through evaporator E. Note that the bottom liquid may be directly circulated in the absorber A as a heat-receiving fluid. Further, in these embodiments, the low-pressure steam generated by the absorption heat pump 12 may be directly returned to the distillation column 1 or another distillation column.
このような方法によると、第一〜第三の分縮器
を用いる第１図の方法より、蒸気消費量が40％〜
70％減少できる。 According to this method, the steam consumption is reduced by 40% compared to the method shown in Fig. 1 using the first to third dephlegmators.
It can be reduced by 70%.
発明の効果
以上本発明によれば分縮機能を有するためエタ
ノールの純度を落とすことなく、蒸留分離に必要
なエネルギーを低減することができる。Effects of the Invention As described above, according to the present invention, since it has a partial condensation function, the energy required for distillation separation can be reduced without reducing the purity of ethanol.
第１図は分縮器を用いた従来方法によるフロー
図、第２図はエタノール蒸留塔の蒸気加熱量をあ
らわす図、第３図はエタノール蒸留塔排熱量割合
をあらわす図、第４図は回収器の効率と加熱量割
合の関係をあらわす図、第５図は吸収ヒートポン
プを用いた従来方法によるフロー図、第６図およ
び第７図はそれぞれ吸収ヒートポンプを用いた本
発明方法によるフロー図である。
１…蒸留塔、４…第三分縮器、５…エタノール
水溶液、８…精製塔、１２…吸収ヒートポンプ、
１６，１７…凝縮液。
Figure 1 is a flow diagram of the conventional method using a dephlegmator, Figure 2 is a diagram showing the amount of steam heating in the ethanol distillation column, Figure 3 is a diagram showing the ratio of the amount of heat released from the ethanol distillation column, and Figure 4 is a diagram showing the amount of heat recovered from the ethanol distillation column. Figure 5 is a flow diagram of the conventional method using an absorption heat pump, and Figures 6 and 7 are flow diagrams of the method of the present invention using an absorption heat pump, respectively. . 1... Distillation column, 4... Third condenser, 5... Ethanol aqueous solution, 8... Purification column, 12... Absorption heat pump,
16, 17... Condensate.
Claims (1)
留し、前記蒸留塔で発生した大部分がエタノール
の蒸気を吸収ヒートポンプの蒸発器に熱源として
導き、その凝縮液を留出液として分留する一方、
残りの該蒸気を前記吸収ヒートポンプの再生器に
熱源として導き、その凝縮液を前記蒸留塔に還流
し、残りの該蒸気を分縮器に導くことを特徴とす
るエタノールの分離方法。1. Ethanol containing impurities is led to a distillation column to be distilled, the vapor of mostly ethanol generated in the distillation column is led to an evaporator of an absorption heat pump as a heat source, and the condensate is fractionated as a distillate, while
A method for separating ethanol, which comprises guiding the remaining vapor to the regenerator of the absorption heat pump as a heat source, refluxing the condensate thereof to the distillation column, and guiding the remaining vapor to a partial condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59116846A JPS60260529A (en) | 1984-06-06 | 1984-06-06 | Method of separation of ethanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP59116846A JPS60260529A (en) | 1984-06-06 | 1984-06-06 | Method of separation of ethanol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60260529A JPS60260529A (en) | 1985-12-23 |
| JPS6355497B2 true JPS6355497B2 (en) | 1988-11-02 |
Family
ID=14697074
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP59116846A Granted JPS60260529A (en) | 1984-06-06 | 1984-06-06 | Method of separation of ethanol |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60260529A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009066519A (en) * | 2007-09-13 | 2009-04-02 | Kiriyama Seisakusho:Kk | Separator employing distillation and membrane separation in combination |
| CN108144320A (en) * | 2017-12-23 | 2018-06-12 | 天津市鹏翔科技有限公司 | Special extract rectification self-balancing split-phase is without blowback method of flow control |
| CN114470830A (en) * | 2021-12-07 | 2022-05-13 | 安徽世华化工有限公司 | Ethanol recovery and purification device |
-
1984
- 1984-06-06 JP JP59116846A patent/JPS60260529A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60260529A (en) | 1985-12-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2396242C2 (en) | Method of methanol recuperation | |
| US6417411B2 (en) | Method for production of ethylene glycol | |
| US20220288504A1 (en) | Process for distilling a crude composition in a rectification plant including an indirect heat pump | |
| US4334965A (en) | Process for recovery of olefinic nitriles | |
| US3186795A (en) | Method of recovering ammonia | |
| WO2003035222A1 (en) | Water-soluble organic material condensation apparatus | |
| US4645569A (en) | Process for producing anhydrous ethanol | |
| US4362601A (en) | Method for distilling ethyl alcohol by adding salt or salts | |
| JP6571228B2 (en) | MVR type aqueous ammonia distillation equipment | |
| US3694322A (en) | Method for separating acrylonitrile and acetonitrile by extractive distillation with coolant vapor generation | |
| JPS6355497B2 (en) | ||
| KR890009905A (en) | Method for Separation of Ethylene Oxide from Aldehyde Impurities | |
| US4983260A (en) | Process for concentrating aqueous ethylene oxide solutions | |
| JP2019122953A (en) | Distillation apparatus of ammonia aqueous solution | |
| JPS62103072A (en) | Method of purifying ethylene oxide | |
| EP1636178B1 (en) | Method for making caprolactam | |
| JPS6337622B2 (en) | ||
| US2974750A (en) | Distillation and absorption process | |
| EP1636179B1 (en) | Method for making caprolactam from impure 6-amino-capronitrile containing tetrahydroazepine | |
| JPS6141497B2 (en) | ||
| CN217472758U (en) | Recovery unit of allyl chloride tail gas | |
| JPS6133017B2 (en) | ||
| EP3604278B1 (en) | Process for the purification of acrolein | |
| JPH05237302A (en) | Distillation plant | |
| JPS61158774A (en) | Device for purifying ethanol |