WO2022122027A1 - 麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法 - Google Patents

麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法 Download PDF

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WO2022122027A1
WO2022122027A1 PCT/CN2021/137214 CN2021137214W WO2022122027A1 WO 2022122027 A1 WO2022122027 A1 WO 2022122027A1 CN 2021137214 W CN2021137214 W CN 2021137214W WO 2022122027 A1 WO2022122027 A1 WO 2022122027A1
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alkaline hydrolysis
tower
condenser
reflux
rectification tower
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PCT/CN2021/137214
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English (en)
French (fr)
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陈月安
詹见
张其军
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安徽金禾实业股份有限公司
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Priority to EP21902732.3A priority Critical patent/EP4234526A4/en
Priority to CN202180065866.9A priority patent/CN116323532A/zh
Publication of WO2022122027A1 publication Critical patent/WO2022122027A1/zh
Priority to US18/207,734 priority patent/US20230312445A1/en

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    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/80Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
    • C07C29/84Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation by extractive distillation
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74Separation; Purification; Use of additives, e.g. for stabilisation
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/80Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D3/00Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/009Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in combination with chemical reactions
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D3/00Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14Fractional distillation or use of a fractionation or rectification column
    • B01D3/143Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D3/00Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14Fractional distillation or use of a fractionation or rectification column
    • B01D3/32Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322Reboiler specifications
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D3/00Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/40Extractive distillation
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D5/00Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • B01D5/0063Reflux condensation
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24Stationary reactors without moving elements inside
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00Feed or outlet devices; Feed or outlet control devices
    • B01J4/001Feed or outlet devices as such, e.g. feeding tubes
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/88Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/02Monohydroxylic acyclic alcohols
    • C07C31/08Ethanol
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07DHETEROCYCLIC COMPOUNDS
    • C07D309/00Heterocyclic compounds containing six-membered rings having one oxygen atom as the only ring hetero atom, not condensed with other rings
    • C07D309/34Heterocyclic compounds containing six-membered rings having one oxygen atom as the only ring hetero atom, not condensed with other rings having three or more double bonds between ring members or between ring members and non-ring members
    • C07D309/36Heterocyclic compounds containing six-membered rings having one oxygen atom as the only ring hetero atom, not condensed with other rings having three or more double bonds between ring members or between ring members and non-ring members with oxygen atoms directly attached to ring carbon atoms
    • C07D309/40Oxygen atoms attached in positions 3 and 4, e.g. maltol
    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01JCHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2204/00Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
    • B01J2204/005Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the outlet side being of particular interest
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/10Process efficiency

Definitions

  • the invention relates to an alcohol distillation decolorization and impurity removal device and an impurity removal method in the production of maltol.
  • the production process of maltol is divided into Grignard section, chlorination section, sublimation section, crystallization section and drying section.
  • the crystallization section mainly uses alcohol to recrystallize the material to remove impurities and odors in the material and improve product quality.
  • the alcohol is replaced and then distilled in a still.
  • the quality of the distilled alcohol is not good, which affects the quality of the product, and increases the replacement intensity and increases the cost.
  • Chinese patent document CN103570497B discloses an inorganic membrane recycling alcohol treatment method, comprising the following steps: (a) preliminary distillation to obtain the acid alcohol to be processed; (b) after the acid alcohol is pumped into the second reactor, alkali is added to neutralize to The pH value reaches 9 to obtain neutral alcohol; (c) the neutral alcohol is pumped into the evaporator, and the neutral gaseous water-containing alcohol is produced; (d) the gaseous water-containing alcohol is dehydrated by the inorganic membrane dehydration device, and the produced anhydrous alcohol is obtained.
  • the moisture content of ethanol is below 0.01% and enters the alcohol product receiving tank.
  • Chinese patent document CN205182700U discloses an alcohol recovery and reuse system, which recovers the ethanol solvent used in the processes of alkalization, acidification, purification and drying and drying at one time. Ethanol is recovered.
  • the above-mentioned technology still has the problem of high cost in the use process.
  • the first technical problem to be solved by the present invention is to provide a device for alcohol distillation, decolorization and impurity removal in the production of maltol, which is simple in structure, convenient in use and low in cost.
  • the second technical problem to be solved by the present invention is to provide the impurity removal method of the alcohol distillation decolorization and impurity removal device in the above-mentioned maltol production, and the obtained alcohol has high purity and few impurities.
  • the present invention provides an alcohol distillation decolorization and impurity removal device in the production of maltol, comprising a first feed pump, a rectifying tower, a first condenser, a reflux tank, a first reflux pump, a first Reboiler, first extraction pump, alkaline hydrolysis kettle, second condenser, alkaline hydrolysis receiving tank, second feed pump, alkaline hydrolysis distillation column, third condenser, finished product tank, second reflux pump, second
  • the reboiler, the second draw pump, the first feed pump are connected to the inlet end of the rectification tower, the first condenser is connected to the upper outlet of the rectification tower, the other end of the first condenser is connected to the inlet of the reflux tank, the reflux tank
  • the outlet is connected to the rectification tower through the first reflux pump, the lower part of the rectification tower is connected to the first reboiler through a circulation pipeline, the bottom of the bottom of the
  • the inlet end is connected, the alkaline hydrolysis kettle is connected to the second condenser through the circulation pipeline, the outlet end of the alkaline hydrolysis kettle is connected with the inlet end of the alkaline hydrolysis receiving tank, and the outlet end of the alkaline hydrolysis receiving tank is connected with the inlet end of the alkaline hydrolysis rectification tower through the second feed pump , the upper outlet of the alkaline hydrolysis rectification tower is connected with the third condenser, the other end of the third condenser is connected with the inlet end of the finished product tank, the outlet end of the finished product tank is connected with the alkaline hydrolysis rectification tower through the second reflux pump, and the alkaline hydrolysis rectification tower is connected with the The lower part of the tower is connected to the second reboiler through a circulation pipeline, and the bottom of the alkaline hydrolysis rectification tower is connected to the second draw pump.
  • the alcohol distillation decolorization and impurity removal device in the maltol production of the present invention is referred to as the device below.
  • the device has the advantages of simple structure, convenient use and low use cost.
  • the invention provides a kind of impurity removal method utilizing the alcohol distillation decolorization and impurity removal device in the above-mentioned maltol production, comprising the following steps:
  • the crude alcohol is pushed into the rectifying tower according to the speed of 1.5m 3 /h, and the rectifying tower utilizes the first reboiler to heat the crude alcohol, and the temperature at the bottom of the rectifying tower is 85-87 °C, the temperature at the top of the tower is 76-78 °C, the distillate material of the rectification tower is condensed by the first condenser and enters the reflux tank, a part of the material in the reflux tank is refluxed, and the other part is extracted into the alkaline hydrolysis kettle, and the reflux ratio is 0.6, The waste at the bottom of the rectification tower is extracted by the first extraction pump;
  • the material in the alkaline hydrolysis receiving tank enters the alkaline hydrolysis rectification tower at a speed of 1 m 3 /h through the second feeding pump, the alkaline hydrolysis rectification tower heats the material through the thinking reboiler, and the alkaline hydrolysis rectification tower tower
  • the bottom temperature is 80-82 °C
  • the top temperature is 77-78 °C.
  • the distillate of the alkaline hydrolysis distillation column is condensed into the finished product tank through the second condenser, and a part of the finished product tank is refluxed with a reflux ratio of 1.5.
  • the alcohol in the finished product tank is sampled It is extracted after passing the test, and the waste at the bottom of the alkaline hydrolysis distillation column is extracted by the second extraction pump.
  • the method for removing impurities of the alcohol distillation decolorizing and removing device in the production of maltol of the present invention is abbreviated as this method below.
  • the advantages of this method 1.
  • the alcohol content after treatment by this method can reach more than 95%, and the impurity content is low;
  • the alcohol obtained by rectification has good transparency and no peculiar smell and can be used for crystallization, which improves the odor quality of the finished maltol;
  • the rectified alcohol can be taken out, which reduces the cost compared with the previous discharge into wastewater.
  • Figure 1 is a schematic flow diagram of the invention.
  • the alcohol distillation decolorization and impurity removal device in the production of maltol includes a first feed pump 1, a rectification column 2, a first condenser 21, a reflux tank 22, a first reflux pump 221, and a first reboiler 23 , the first extraction pump 24, the alkaline hydrolysis kettle 3, the second condenser 31, the alkaline hydrolysis receiving tank 32, the second feed pump 33, the alkaline hydrolysis distillation column 4, the third condenser 41, the finished product tank 5, the second The reflux pump 51, the second reboiler 42, the second draw pump 43, the first feed pump 1 is connected to the inlet end of the rectification tower 2, the first condenser 21 is connected to the upper outlet of the rectification tower 2, the first The other end of the condenser 21 is connected with the inlet of the reflux tank 22, the outlet of the reflux tank 22 is connected with the rectification column 2 through the first reflux pump 221, and the lower part of the rectification column 2 is connected with the first
  • the inlet end of the solution receiving tank 32 is connected, the outlet end of the alkaline hydrolysis receiving tank 32 is connected with the inlet end of the alkaline hydrolysis rectifying tower 4 through the second feed pump 33, the upper outlet of the alkaline hydrolysis rectifying tower 4 is connected with the third condenser 41, and the third The other end of the condenser 41 is connected with the inlet end of the finished product tank 5, the outlet end of the finished product tank 5 is connected with the alkaline hydrolysis rectification tower 4 through the second reflux pump 51, and the lower part of the alkaline hydrolysis rectification tower 4 is connected with the second reboiler through the circulation pipeline 42.
  • the bottom of the alkaline hydrolysis distillation column 4 is connected to the second extraction pump 43.
  • Embodiment 2 is a diagrammatic representation of Embodiment 1:
  • a method for removing impurities using alcohol distillation decolorizing and removing device in the production of above-mentioned maltol comprising the following steps:
  • the crude alcohol is pushed into the rectifying tower according to the speed of 1.5m 3 /h, and the rectifying tower utilizes the first reboiler to heat the crude alcohol, and the temperature at the bottom of the rectifying tower is 85 °C, The temperature at the top of the tower is 76°C, the distillate material of the rectification tower is condensed by the first condenser and enters the reflux tank. A part of the material in the reflux tank is refluxed, and the other part is extracted into the alkaline hydrolysis kettle. The reflux ratio is 0.6, and the bottom of the rectification tower is The waste is extracted by the first extraction pump;
  • caustic soda in the alkaline hydrolysis kettle, add caustic soda, the caustic soda addition amount is every 4m 3 materials add 25kg caustic soda, then be warming up to 77 °C, insulation 1h alkali hydrolysis finishes, discharge material to alkali hydrolysis receiving tank;
  • the material in the alkaline hydrolysis receiving tank enters the alkaline hydrolysis rectification tower at a speed of 1 m 3 /h through the second feeding pump, the alkaline hydrolysis rectification tower heats the material through the thinking reboiler, and the alkaline hydrolysis rectification tower tower
  • the bottom temperature is 80°C
  • the top temperature is 77°C.
  • the distillate of the alkaline hydrolysis distillation column is condensed into the finished product tank through the second condenser, and a part of the finished product tank is refluxed, and the reflux ratio is 1.5. out, and the waste at the bottom of the alkaline hydrolysis distillation column is extracted by the second extraction pump.
  • the obtained ethanol has a water content of 0.6% and an impurity content of 3.2%.
  • a method for removing impurities using alcohol distillation decolorizing and removing device in the production of above-mentioned maltol comprising the following steps:
  • the crude alcohol is pushed into the rectifying tower according to the speed of 1.5m 3 /h, and the rectifying tower utilizes the first reboiler to heat the crude alcohol, and the temperature at the bottom of the rectifying tower is 86 °C, The temperature at the top of the tower is 77°C, the distillate material of the rectification tower is condensed by the first condenser and enters the reflux tank. A part of the material in the reflux tank is refluxed, and the other part is extracted into the alkaline hydrolysis kettle. The reflux ratio is 0.6, and the bottom of the rectification tower is The waste is extracted by the first extraction pump;
  • the material in the alkaline hydrolysis receiving tank enters the alkaline hydrolysis rectification tower at a speed of 1 m 3 /h through the second feeding pump, the alkaline hydrolysis rectification tower heats the material through the thinking reboiler, and the alkaline hydrolysis rectification tower tower
  • the bottom temperature is 81°C and the top temperature is 77.5°C.
  • the distillate of the alkaline hydrolysis distillation column is condensed into the finished product tank through the second condenser, and a part of the finished product tank is refluxed, and the reflux ratio is 1.5. out, and the waste at the bottom of the alkaline hydrolysis distillation column is extracted by the second extraction pump.
  • the obtained ethanol has a water content of 0.8% and an impurity content of 3.1%.
  • Embodiment 4 is a diagrammatic representation of Embodiment 4:
  • a method for removing impurities using alcohol distillation decolorizing and removing device in the production of above-mentioned maltol comprising the following steps:
  • the crude alcohol is pushed into the rectifying tower according to the speed of 1.5m 3 /h, and the rectifying tower utilizes the first reboiler to heat the crude alcohol, and the temperature at the bottom of the rectifying tower is 87° C., The temperature at the top of the tower is 78°C, the distillate material of the rectification tower is condensed by the first condenser and enters the reflux tank. A part of the material in the reflux tank is refluxed, and the other part is extracted into the alkaline hydrolysis kettle. The reflux ratio is 0.6, and the bottom of the rectification tower is The waste is extracted by the first extraction pump;
  • caustic soda in the alkaline hydrolysis kettle, add caustic soda, the caustic soda addition amount is every 4m 3 materials add 25kg caustic soda, then be warming up to 78 °C, insulation 1h alkali hydrolysis finishes, discharging to the alkali hydrolysis receiving tank;
  • the material in the alkaline hydrolysis receiving tank enters the alkaline hydrolysis rectification tower at a speed of 1 m 3 /h through the second feeding pump, the alkaline hydrolysis rectification tower heats the material through the thinking reboiler, and the alkaline hydrolysis rectification tower tower
  • the bottom temperature is 82°C
  • the top temperature is 78°C.
  • the distillate of the alkaline hydrolysis distillation column is condensed into the finished product tank through the second condenser, and a part of the finished product tank is refluxed, and the reflux ratio is 1.5. out, and the waste at the bottom of the alkaline hydrolysis distillation column is extracted by the second extraction pump.
  • the obtained ethanol has a water content of 1.0% and an impurity content of 3.0%.

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Abstract

本申请公开了一种麦芽酚生产中酒精蒸馏脱色除杂装置,其特征在于:包括精馏塔、碱解釜、碱解精馏塔;精馏塔上侧出口与碱解釜入口相连通,碱解釜出口端与碱解精馏塔入口端相连通,碱解精馏塔上侧出口与成品槽入口端相连通。还公开了一种麦芽酚生产中酒精蒸馏脱色除杂方法。本申请方案处理的产物纯度高。

Description

麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法
本申请要求申请日为2020年12月11日,申请号为202011451866.6,发明名称为麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法的中国专利申请的优先权。
技术领域
本发明涉及麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法。
背景技术
麦芽酚的生产过程分为格氏工段、氯化工段、升华工段、结晶工段、烘干工段。结晶工段主要采用酒精进行对物料进行重结晶,去除物料内的杂质异味,改善产品品质。酒精采用置换后用蒸馏釜蒸馏后套用,蒸馏出来的酒精品质不好,影响产品品质,加大置换力度又造成成本升高。
中国专利文献CN103570497B公开了一种无机膜回收酒精处理方法,包括以下步骤:(a)初步蒸馏得到需处理的酸性酒精;(b)将酸性酒精泵入第二反应釜后,加碱中和至PH值达到9,得到中性酒精;(c)将中性酒精泵入蒸发器,采出中性的气态含水酒精;(d)气态含水酒精通过无机膜脱水装置进行脱水,采出的无水乙醇的水分含量在0.01%以下进入酒精产品受槽。中国专利文献CN205182700U公开了一种酒精回收再利用系统,对碱化、酸化、精制提纯和烘干过程中所用的乙醇溶剂进行了一次性的回收,采用精馏塔设备,同时对气、液态的乙醇进行回收。但是上述技术在使用过程中还是存在成本高的问题。
发明内容
本发明所要解决的第一个技术问题是提供麦芽酚生产中酒精蒸馏脱色除杂装置,该装置结构简单,使用方便,使用成本低。
本发明所要解决的第二个技术问题是提供上述麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,其得到的酒精纯度高、杂质少。
为解决上述第一个技术问题,本发明提供了麦芽酚生产中酒精蒸馏脱色除杂装置,包括第一进料泵、精馏塔、第一冷凝器、回流罐、第一回流泵、第一再沸器、第一采出泵、碱解釜、第二冷凝器、碱解受槽、第二进料泵、碱解精馏塔、第三冷凝器、成品槽、第二回流泵、第二再沸器、第二采出泵,第一进料泵与精馏塔进口端相连,第一冷凝器与精馏塔上侧出口相连,第一冷凝器另一端与回流罐入口相连,回流罐出口通过第一回流泵与精馏塔相连,精馏塔下部通过循环管路连接第一再沸器,精馏塔底部连接第一采出泵,回流罐出口通过另一管路与碱解釜入口端相连,碱解釜通过循环管路连接第二冷凝器,碱解釜出口端与碱解受槽入口端相连,碱解受槽出口端通过第二进料泵与碱解精馏塔入口端相连,碱解精馏塔上侧出口与第三冷凝器相连,第三冷凝器另一端与成品槽入口端相连,成品槽出口端通过第二回流泵与碱解精馏塔相连,碱解精馏塔下部通过循环管路连接第二再沸器,碱解精馏塔底部连接第二采出泵。
为简单说明问题起见,以下对本发明所述的麦芽酚生产中酒精蒸馏脱色除杂装置均简称为本装置。
本装置结构简单,使用方便,使用成本低。
为解决上述第二个技术问题,本发明提供了一种利用上述麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,包括以下步骤:
(1)通过第一进料泵将粗品酒精按照1.5m 3/h的速度打入精馏塔,精馏塔利用第一再沸器对粗品酒精加热,精馏塔塔底温度为85-87℃、塔顶温度为76-78℃,精馏塔馏出物料通过第一冷凝器冷凝并进入回流罐,回流罐中物料一部分回流,另一部分采出至碱解釜中,回流比为0.6,精馏塔底部废料经第一采出泵采出;
(2)向碱解釜内加入片碱,片碱加入量为每4m 3物料加入25kg片碱,然后升温至77-78℃,保温1h碱解结束,放料至碱解受槽;
(3)碱解受槽内的物料通过第二送料泵以1m 3/h的速度进入碱解精馏塔,碱解精馏塔通过思维再沸器对物料进行加热,碱解精馏塔塔底温度为80-82℃、塔顶温度为77-78℃,碱解精馏塔馏出物通过第二冷凝器冷凝进入成品槽,成品槽一部分回流,回流比为1.5,成品槽内酒精取样检测合格后采出,碱解精馏塔底部废料经第二采出泵采出。
为简单说明问题起见,以下对本发明所述的麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法均简称为本方法。
本方法的优点:1.通过本方法处理后的酒精含量能达到95%以上,同时杂质含量低;2.精馏得到的酒精透明度好无异味回结晶套用,改善了麦芽酚成品的气味品质;3.精馏后的酒精可以外卖,较之前排入废水降低了成本。
附图说明
图1是发明的流程示意图。
具体实施方式
实施例一:
参见图1,麦芽酚生产中酒精蒸馏脱色除杂装置,包括第一进料泵1、精馏塔2、第一冷凝器21、回流罐22、第一回流泵221、第一再沸器23、第一采出泵24、碱解釜3、第二冷凝器31、碱解受槽32、第二进料泵33、碱解精馏塔4、第三冷凝器41、成品槽5、第二回流泵51、第二再沸器42、第二采出泵43,第一进料泵1与精馏塔2进口端相连,第一冷凝器21与精馏塔2上侧出口相连,第一冷凝器21另一端与回流罐22入口相连,回流罐22出口通过第一回流泵221与精馏塔2相连,精馏塔2下部通过循环管路连接第一再沸器23,精馏塔2底部连接第一采出泵24,回流罐22出口通过另一管路与碱解釜3入口端相连,碱解釜3通过循环管路连接第二冷凝器31,碱解釜3出口端与碱解受槽32入口端相连,碱解受槽32出口端通过第二进料泵33与碱解精馏塔4入口端相连,碱解精馏塔4上侧出口与第三冷凝器41 相连,第三冷凝器41另一端与成品槽5入口端相连,成品槽5出口端通过第二回流泵51与碱解精馏塔4相连,碱解精馏塔4下部通过循环管路连接第二再沸器42,碱解精馏塔4底部连接第二采出泵43。
实施例二:
一种利用上述麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,包括以下步骤:
(1)通过第一进料泵将粗品酒精按照1.5m 3/h的速度打入精馏塔,精馏塔利用第一再沸器对粗品酒精加热,精馏塔塔底温度为85℃、塔顶温度为76℃,精馏塔馏出物料通过第一冷凝器冷凝并进入回流罐,回流罐中物料一部分回流,另一部分采出至碱解釜中,回流比为0.6,精馏塔底部废料经第一采出泵采出;
(2)向碱解釜内加入片碱,片碱加入量为每4m 3物料加入25kg片碱,然后升温至77℃,保温1h碱解结束,放料至碱解受槽;
(3)碱解受槽内的物料通过第二送料泵以1m 3/h的速度进入碱解精馏塔,碱解精馏塔通过思维再沸器对物料进行加热,碱解精馏塔塔底温度为80℃、塔顶温度为77℃,碱解精馏塔馏出物通过第二冷凝器冷凝进入成品槽,成品槽一部分回流,回流比为1.5,成品槽内酒精取样检测合格后采出,碱解精馏塔底部废料经第二采出泵采出。
经过检测,获得的乙醇含水量为0.6%,杂质含量为3.2%。
实施例三:
一种利用上述麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,包括以下步骤:
(1)通过第一进料泵将粗品酒精按照1.5m 3/h的速度打入精馏塔,精馏塔利用第一再沸器对粗品酒精加热,精馏塔塔底温度为86℃、塔顶温度为77℃,精馏塔馏出物料通过第一冷凝器冷凝并进入回流罐,回流罐中物料一部分回流,另一部分采出至碱解釜中,回流比为0.6,精馏塔底部废料经第一采出泵采出;
(2)向碱解釜内加入片碱,片碱加入量为每4m 3物料加入25kg片碱,然后升温至77.5℃,保温1h碱解结束,放料至碱解受槽;
(3)碱解受槽内的物料通过第二送料泵以1m 3/h的速度进入碱解精馏塔,碱解精馏塔通过思维再沸器对物料进行加热,碱解精馏塔塔底温度为81℃、塔顶温度为77.5℃,碱解精馏塔馏出物通过第二冷凝器冷凝进入成品槽,成品槽一部分回流,回流比为1.5,成品槽内酒精取样检测合格后采出,碱解精馏塔底部废料经第二采出泵采出。
经过检测,获得的乙醇含水量为0.8%,杂质含量为3.1%。
实施例四:
一种利用上述麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,包括以下步骤:
(1)通过第一进料泵将粗品酒精按照1.5m 3/h的速度打入精馏塔,精馏塔利用第一再沸器对粗品酒精加热,精馏塔塔底温度为87℃、塔顶温度为78℃,精馏塔馏出物料通过第一冷凝器冷凝并进入回流罐,回流罐中物料一部分回流,另一部分采出至碱解釜中,回流比为0.6,精馏塔底部废料经第一采出泵采出;
(2)向碱解釜内加入片碱,片碱加入量为每4m 3物料加入25kg片碱,然后升温至78℃,保温1h碱解结束,放料至碱解受槽;
(3)碱解受槽内的物料通过第二送料泵以1m 3/h的速度进入碱解精馏塔,碱解精馏塔通过思维再沸器对物料进行加热,碱解精馏塔塔底温度为82℃、塔顶温度为78℃,碱解精馏塔馏出物通过第二冷凝器冷凝进入成品槽,成品槽一部分回流,回流比为1.5,成品槽内酒精取样检测合格后采出,碱解精馏塔底部废料经第二采出泵采出。
经过检测,获得的乙醇含水量为1.0%,杂质含量为3.0%。
以上所述,仅为本申请的具体实施方式,在本申请的上述教导下,本领域技术人员可以在上述实施例的基础上进行其他的改进或变形。本领域技术人员应该明白,上述的具体描述只是更好的解释本申请的目的,本申请的保护范围应以权利要求的保护范围为准。
此外,本领域的技术人员能够理解,尽管在此所述的一些实施例包括其它实施例中所包括的某些特征而不是其它特征,但是不同实施例的特征的组合意味着处于本申请的范围之内并且形成不同的实施例。例如,在下面的权 利要求书中,所要求保护的实施例的任意之一都可以以任意的组合方式来使用。

Claims (9)

  1. 麦芽酚生产中酒精蒸馏脱色除杂装置,其特征在于:包括精馏塔、碱解釜、碱解精馏塔;精馏塔上侧出口与碱解釜入口相连通,碱解釜出口端与碱解精馏塔入口端相连通,碱解精馏塔上侧出口与成品槽入口端相连通。
  2. 如权利要求1麦芽酚生产中酒精蒸馏脱色除杂装置,其特征在于:还包括第一冷凝器,第二冷凝器,第三冷凝器,第一冷凝器与精馏塔上侧出口相连,碱解釜通过循环管路连接第二冷凝器,碱解精馏塔上侧出口与第三冷凝器相连。
  3. 如权利要求2麦芽酚生产中酒精蒸馏脱色除杂装置,其特征在于:第一冷凝器另一端与回流罐入口相连,回流罐出口通过第一回流泵与精馏塔相连,精馏塔下部通过循环管路连接第一再沸器。
  4. 如权利要求2麦芽酚生产中酒精蒸馏脱色除杂装置,其特征在于:第三冷凝器另一端与成品槽入口端相连,成品槽出口端通过第二回流泵与碱解精馏塔相连,碱解精馏塔下部通过循环管路连接第二再沸器,碱解精馏塔底部连接第二采出泵。
  5. 如权利要求1麦芽酚生产中酒精蒸馏脱色除杂装置,其特征在于:还包括第一进料泵、第一冷凝器、回流罐、第一回流泵、第一再沸器、第一采出泵、第二冷凝器、碱解受槽、第二进料泵、第三冷凝器、成品槽、第二回流泵、第二再沸器、第二采出泵,第一进料泵与精馏塔进口端相连,第一冷凝器与精馏塔上侧出口相连,第一冷凝器另一端与回流罐入口相连,回流罐出口通过第一回流泵与精馏塔相连,精馏塔下部通过循环管路连接第一再沸器,精馏塔底部连接第一采出泵,回流罐出口通过另一管路与碱解釜入口端相连,碱解釜通过循环管路连接第二冷凝器,碱解釜出口端与碱解受槽入口端相连,碱解受槽出口端通过第二进料泵与碱解精馏塔入口端相连,碱解精馏塔上侧出口与第三冷凝器相连,第三冷凝器另一端与成品槽入口端相连,成品槽出口端通过第二回流泵与碱解精馏塔相连,碱解精馏塔下部通过循环管路连接第二再沸器,碱解精馏塔底部连接第二采出泵。
  6. 根据权利要求1-5任一项所述的麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,其特征在于,包括以下步骤:
    (1)通过第一进料泵将粗品酒精按照1.5m 3/h的速度打入精馏塔,精馏 塔利用第一再沸器对粗品酒精加热,精馏塔塔底温度为85-87℃、塔顶温度为76-78℃,精馏塔馏出物料通过第一冷凝器冷凝并进入回流罐,回流罐中物料一部分回流,另一部分采出至碱解釜中,回流比为0.6,精馏塔底部废料经第一采出泵采出;
    (2)向碱解釜内加入片碱,片碱加入量为每4m 3物料加入25kg片碱,然后升温至77-78℃,保温1h碱解结束,放料至碱解受槽;
    (3)碱解受槽内的物料通过第二送料泵以1m 3/h的速度进入碱解精馏塔,碱解精馏塔通过思维再沸器对物料进行加热,碱解精馏塔塔底温度为80-82℃、塔顶温度为77-78℃,碱解精馏塔馏出物通过第二冷凝器冷凝进入成品槽,成品槽一部分回流,回流比为1.5,成品槽内酒精取样检测合格后采出,碱解精馏塔底部废料经第二采出泵采出。
  7. 一种麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,其特征在于,包括以下步骤:
    步骤1:将粗品酒精打入精馏塔,精馏塔塔底温度为85-87℃、塔顶温度为76-78℃,精馏塔馏出物一部分回流,另一部分采出至碱解釜中,回流比为0.6;
    步骤2:向碱解釜内加入片碱,然后升温至77-78℃,保温碱解;
    步骤3:将步骤2保温碱解产物送入碱解精馏塔,碱解精馏塔塔底温度为80-82℃、塔顶温度为77-78℃,碱解精馏塔馏出物一部分回流,回流比为1.5。
  8. 根据权利要求7的麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,其特征在于,包括以下步骤:
    其中步骤1回流比为0.6。
  9. 根据权利要求7的麦芽酚生产中酒精蒸馏脱色除杂装置的除杂方法,其特征在于,包括以下步骤:
    其中步骤3回流比为1.5。
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115845421A (zh) * 2022-12-19 2023-03-28 滨州黄海科学技术研究院有限公司 一种连续化分离全氟己酮的系统及方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112409133A (zh) * 2020-12-11 2021-02-26 安徽金禾实业股份有限公司 麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS52122312A (en) * 1976-04-05 1977-10-14 Kyowa Hakko Kogyo Co Ltd Recovery of ethanol
RU2081650C1 (ru) * 1993-06-24 1997-06-20 Голден Дропс Способ получения спирта-ректификата
CN101747146A (zh) * 2009-12-21 2010-06-23 林海 无味酒精生产工艺及其设备
CN103570497A (zh) 2013-11-01 2014-02-12 安徽金禾实业股份有限公司 一种无机膜回收酒精处理方法及装置
CN205182700U (zh) 2015-11-12 2016-04-27 呼图壁县美嘉生物科技有限公司 一种酒精回收再利用系统
CN106986745A (zh) * 2017-05-24 2017-07-28 武汉金中石化工程有限公司 一种乙醇精制工艺
CN112409133A (zh) * 2020-12-11 2021-02-26 安徽金禾实业股份有限公司 麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB675995A (en) * 1947-11-04 1952-07-23 Bataafsche Petroleum Purifying aqueous solutions of alcohols containing aldehydic impurities by distillation
JP4812059B2 (ja) * 2001-05-25 2011-11-09 宝ホールディングス株式会社 エタノールの精製方法
CN101550063A (zh) * 2008-04-03 2009-10-07 天津市风船化学试剂科技有限公司 一种超纯度无水乙醇的提纯方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS52122312A (en) * 1976-04-05 1977-10-14 Kyowa Hakko Kogyo Co Ltd Recovery of ethanol
RU2081650C1 (ru) * 1993-06-24 1997-06-20 Голден Дропс Способ получения спирта-ректификата
CN101747146A (zh) * 2009-12-21 2010-06-23 林海 无味酒精生产工艺及其设备
CN103570497A (zh) 2013-11-01 2014-02-12 安徽金禾实业股份有限公司 一种无机膜回收酒精处理方法及装置
CN205182700U (zh) 2015-11-12 2016-04-27 呼图壁县美嘉生物科技有限公司 一种酒精回收再利用系统
CN106986745A (zh) * 2017-05-24 2017-07-28 武汉金中石化工程有限公司 一种乙醇精制工艺
CN112409133A (zh) * 2020-12-11 2021-02-26 安徽金禾实业股份有限公司 麦芽酚生产中酒精蒸馏脱色除杂装置和除杂方法

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
"Comprehensive Utilization of Cane Sugar Factory", 31 October 1998, ISBN: 7-5019-2208-X, article LI, XILIU : "Theoretical Basis of Distillation and Impurity-Removal of Alcohol", pages: 29 - 34, XP009538152 *
See also references of EP4234526A4
ZHU HUIYUN, HUANG BAOLI: "Improvement of Several Solvent Recovery Processes in Maltol Production", AN HUI HUA GONG = ANHUI CHEMICAL INDUSTRY, CN, 31 December 2001 (2001-12-31), CN , pages 22 - 23, XP055940852, ISSN: 1008-553X *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN115845421A (zh) * 2022-12-19 2023-03-28 滨州黄海科学技术研究院有限公司 一种连续化分离全氟己酮的系统及方法
CN115845421B (zh) * 2022-12-19 2023-06-30 滨州黄海科学技术研究院有限公司 一种连续化分离全氟己酮的系统及方法

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