CN105693468B - Isopropyl acetate hydrogenization method production ethanol and the post-processing approach of isopropanol - Google Patents
Isopropyl acetate hydrogenization method production ethanol and the post-processing approach of isopropanol Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
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- 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
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- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
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- 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
Abstract
Isopropyl acetate hydrogenization method production ethanol and the post-processing approach of isopropanol, the method includes to carry out rectifying by lightness-removing column, ethanol tower, isopropanol tower and weight-removing column, the tower top of each tower sets up backflow, and the middle part liquor charging phase from tower reactor to next tower successively respectively；The overhead reflux of wherein ethanol tower and isopropanol tower adopts heat pump compression process, not only solves the heat energy needed for two towers itself backflow, and ethanol tower can also partly provide the heat energy needed for lightness-removing column；Whole equipment and method greatly reduce the consumption of the steam in the separation engineering of ethanol and isopropanol；While the tower top of ethanol tower and isopropanol tower eliminates condenser, the demand of cooling water is reduced, have functions that energy-conservation, reduce discharging.
Description
Technical field
The present invention relates to a kind of ethanol of rectificating method, particularly isopropyl acetate hydrogenization method production and isopropanol rectifying side
Method.
Background technology
Isopropanol is a kind of important industrial chemicals, is widely used in the fields such as agricultural chemicals, medicine, electronics, daily use chemicals, at present,
The main method of industrial production isopropanol is propylene hydration method, and the method needs the higher sulfuric acid of concentration, rotten to equipment
Corrosion is higher, and technological process is complicated.
Chinese patent CN103980089 reports the work of a kind of utilization isopropyl acetate hydrogenization method production ethanol and isopropanol
Skill, the technique transformation efficiency are high, and flow process is simple, but the technique productions be ethanol and isopropanol mixture, both ratios
Example about 2:3, although paper proposition can both separate with for the method for rectifying, but the boiling point phase of ethanol and isopropanol
Only 4 DEG C of difference, therefore adopts conventional rectification, and the energy consumption of process will certainly be very high.And the purity of the isopropanol for frequently resulting in is low
In 99.5%, the demand in market far can not be met.
《Ethanol Isopropanol separating technology based on MVR heat pump distillation》Report soft with Aspen Plus chemical process simulation
The heat pump distillation method separating alcohol of part simulation and the rectification process of isopropanol, but which adopts single tower distillation, the isopropanol for obtaining
Theoretical concentration is also only capable of reaching 99.0%, and when calculating, and only accounts for ethanol and isopropanol mixture, and isopropyl acetate
Hydrogenation in also there is the impurity such as 2- amylalcohol, only cannot obtain highly purified ethanol and isopropanol by single tower distillation technique.
Content of the invention
The invention aims to provide a kind of post processing of the production of isopropyl acetate hydrogenization method ethanol and isopropanol setting
Standby and method, its can improve the purity of isopropanol, and the energy consumption needed for reducing, and reduce the discharge of waste gas.
The isopropyl acetate hydrogenization method that the present invention is provided produces the post-processing approach of ethanol and isopropanol, and technical scheme is：
The reactant liquor of isopropyl acetate hydrogenation is sent in lightness-removing column from the middle part of lightness-removing column carries out lightness-removing column rectifying,
Lightness-removing column tower top sets up the backflow of the gas phase portion of lightness-removing column rectifying, and the light component impurity for obtaining reacting is collected in distillate cooling；
The liquid phase part of lightness-removing column rectifying is produced from lightness-removing column tower reactor bottom, is carried out through sending in ethanol tower in the middle part of ethanol tower
Ethanol tower rectifying, from the gas phase portion of ethanol tower overhead extraction ethanol tower rectifying, after heat pump compression, obtains ethanol tower heating agent gas
Body, ethanol tower heating agent gas carry out heat exchange by recuperation of heat reboiler with lightness-removing column tower reactor and ethanol tower tower reactor respectively, and
The backflow for entering ethanol tower is set up, distillate cooling collection obtains alcohol product；
The liquid phase part of ethanol tower rectifying is produced from ethanol tower tower reactor bottom, is entered through sending into isopropanol tower in the middle part of isopropanol tower
Row isopropanol tower rectifying, from the gas phase portion of the isopropanol rectifying of isopropanol column overhead extraction, after heat pump compression, obtains isopropyl
Alcohol tower heating agent gas, isopropanol tower heating medium liquid carry out heat exchange cooling by recuperation of heat reboiler and isopropanol tower tower reactor, and
The backflow for entering isopropanol tower is set up, and distillate carries out ethanol tower rectifying again through ethanol tower is entered in the middle part of ethanol tower；
From the liquid phase part of the isopropanol rectifying of isopropanol tower tower reactor bottom extraction, enter through sending into weight-removing column in the middle part of weight-removing column
Row weight-removing column rectifying, from the gas phase portion of weight-removing column overhead extraction weight-removing column rectifying and sets up backflow, and distillate cooling is collected
To isopropanol product；The liquid phase part of the weight-removing column rectifying in interim acquisition weight-removing column tower reactor, that is, the heavy constituent for obtaining reacting are miscellaneous
Matter；
When post processing just starts, each tower tower reactor absorbs heat by reboiler from extraneous respectively；Last handling process is steady
After fixed, weight-removing column tower reactor absorbs heat still through weight-removing column reboiler；Ethanol tower tower reactor and isopropanol tower tower reactor then change by
Respectively hot friendship is carried out with the heating agent gas after heat pump compression by the second recuperation of heat reboiler and the 3rd recuperation of heat reboiler
Bring absorption heat；Lightness-removing column then both absorbed heat by lightness-removing column reboiler from extraneous, further through the first recuperation of heat reboiler
Heat exchange is carried out with the ethanol tower heating agent gas compressed through heat pump and absorb heat.
Further, the liquid phase part of the lightness-removing column rectifying, from lightness-removing column tower reactor produce, to enter ethanol tower between,
Also one dehydration.
Further, the dehydration includes, the liquid phase part of lightness-removing column rectifying is first passed through molecular sieve carries out transformation
Adsorption dewatering, again passes by molecular sieve dehydration after the material after dehydration to be carried out inorganic permeable membrane dehydration.
Further, the number of plates of the lightness-removing column is 95-110, and the reflux ratio of tower top is 30-60；Enter lightness-removing column
Reacting liquid temperature is 35-45 DEG C, and pressure is 300-500kPa；The gas phase portion temperature of lightness-removing column overhead extraction is 61.5-71.5
DEG C, pressure is 5-15kPa；The backflow liquid temp for flowing back into lightness-removing column is 50-60 DEG C, and pressure is 500-700kPa；Distillate
Temperature is 40-50 DEG C, and pressure is 550-750kPa；The liquid phase part temperature of lightness-removing column tower reactor extraction is 80-90 DEG C, and pressure is
10-20kPa；When entering ethanol tower after heating pressurization, temperature is 100-110 DEG C, and pressure is 100-200kPa；
The number of plates of the ethanol tower is 140-160, and reflux ratio is 8-10；The gas phase portion temperature of ethanol tower overhead extraction
For 73-83 DEG C, pressure is 0-5kPa；After heat pump compression, the temperature of the ethanol tower heating agent gas for obtaining is 132-142 DEG C,
Pressure is 150-250kPa；Before ethanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cooling, temperature
Spend for 75-85 DEG C, pressure is 90-110kPa；The backflow liquid temp for flowing back into ethanol tower is 75-85 DEG C, and pressure is 400-
500kPa；Liquid temp is distillated for 40-50 DEG C, pressure is 500-700kPa；The liquid phase part temperature of ethanol tower tower reactor extraction is 80-
90 DEG C, pressure is 10-30kPa；
The number of plates of the isopropanol tower is 140-160, and reflux ratio is 5-9；The gas phase portion of isopropanol column overhead extraction
Temperature is 100-110 DEG C, and pressure is 110-210kPa；After heat pump compression, the temperature of the isopropanol tower heating agent gas for obtaining
For 135-145 DEG C, pressure is 300-500kPa；Isopropanol tower heating agent gas is after recuperation of heat reboiler and cooler cooling
Before starting backflow, temperature is 108-118 DEG C, and pressure is 260-360kPa；The backflow liquid temp for flowing back into isopropanol tower is
108-118 DEG C, pressure is 700-900kPa；Enter ethanol tower distillates liquid temp for 108-118 DEG C, and pressure is 700-
900kPa；The liquid phase part temperature of isopropanol tower tower reactor extraction is 105-115 DEG C, and pressure is 130-230kPa；Add through heating
When entering weight-removing column after pressure, temperature is 105-115 DEG C, and pressure is 300-500kPa；
The number of plates of the weight-removing column is 70-85, and overhead reflux ratio is 0.5-1；The gas phase portion of weight-removing column overhead extraction
Temperature is 45-52 DEG C, and pressure is 750-850kPa；The backflow liquid temp for flowing back into weight-removing column is 40-50 DEG C, and pressure is 750-
850kPa；Distillate isopropanol temperature is 40-50 DEG C, and pressure is 500-700kPa；The liquid phase part temperature of weight-removing column tower reactor extraction
Spend for 80-100 DEG C, pressure is 750-850kPa.
Technical scheme has following notable beneficial effect：
This apparatus and method, isolated ethanol and isopropanol purity are taken all more than 99.9%；Take this equipment
And method, take full advantage of the heat of tower top, although increased the consumption of electric energy on a small quantity, but save in a large number condensed water and
For the steam of heat tower reactor, the energy is generally saved, and reduces the discharge of waste liquid waste gas.
Description of the drawings
Fig. 1 is the structural representation of present device
Specific embodiment
Embodiment 1
The isopropyl acetate hydrogenation liquid of 9 batches of different batches is taken, and water content is determined using Moisture Meter, by gas-chromatography
Method determines the content of the main component in reactant liquor than water and major impurity.Concrete content is shown in Table one：
Table one：The content table of each main component and major impurity in nine batches of different batches isopropyl acetate hydrogenation liquid
(unit：%)
1st batch reaction liquid is heated to 40 DEG C, 400kPa is pressurized to, from the lightness-removing column for being arranged at the middle part of lightness-removing column 100
The lightness-removing column 100 that at the uniform velocity sends in one charging aperture 101 carries out lightness-removing column rectifying, and light component is from the de- light of the tower top of lightness-removing column 100
Tower gas phase extraction mouth 104 is produced, and enters lightness-removing column return tank 106 after condenser of light component removal column 108 is cooled down, then by de- light
The second charging aperture 102 on 100 top of tower passes back into lightness-removing column 100, and distillate passes through light component cooler 112, enters after cooling
Light component products pot 107；The number of plates of lightness-removing column 100 is 100, and the reflux ratio of overhead reflux is 45；Lightness-removing column gas phase produces mouth
The light component temperature of 104 extraction is 66.4 DEG C, and pressure is 10kPa, and the backflow liquid temp for flowing back into lightness-removing column 100 is 55.4
DEG C, pressure is 600kPa；Liquid temp is distillated for 45 DEG C, pressure is 650kPa.
The liquid phase part of lightness-removing column rectifying is produced from 105 bottom of lightness-removing column tower reactor, through 501 He of molecular sieve adsorption dehydrater
After inorganic 502 eliminating water of infiltrating and vaporizing membrane dehydrater, sending in ethanol tower 200 through ethanol tower first charging aperture 201 carries out ethanol tower
Rectifying, produces the gas phase portion of ethanol tower rectifying from the ethanol tower gas phase extraction mouth 204 of 200 tower top of ethanol tower, through ethanol tower heat
After pump compressor 208 compresses, ethanol tower heating agent gas is obtained, ethanol tower heating agent gas passes through the first recuperation of heat reboiler respectively
111 and second recuperation of heat reboiler 211 and lightness-removing column tower reactor 105 and ethanol tower tower reactor 205 carry out heat exchange, and respectively
Backflow is set up in ethanol tower return tank 206 after the cooling of the first temperature adjustment cooling tower 109 and the second temperature adjustment cooling tower 209,
Phegma enters ethanol tower 200 by ethanol tower second charging aperture 202, and distillate cooling is collected and enters alcohol product tank 207；Second
The number of plates of alcohol tower 200 is 150, and reflux ratio is 9；The liquid phase part temperature that lightness-removing column tower reactor 105 is produced is 84.8 DEG C, and pressure is
20kPa；When entering ethanol tower 200 after heating pressurization and eliminating water, temperature is 106 DEG C, and pressure is 150kPa；Ethanol tower 200
The gas phase portion temperature of overhead extraction is 78.3 DEG C, and pressure is 0kPa；After heat pump compression, the ethanol tower heating agent gas that obtains
Temperature be 137.3 DEG C, pressure be 200kPa；Ethanol tower heating agent gas is opened after recuperation of heat reboiler and cooler cooling
Begin before backflow, temperature is 80 DEG C, pressure is 100kPa；The backflow liquid temp for flowing back into ethanol tower 200 is 80 DEG C, and pressure is
500kPa；Liquid temp is distillated for 45 DEG C, pressure is 600kPa.
The liquid phase part of ethanol tower rectifying is produced from 205 bottom of ethanol tower tower reactor, is sent through isopropanol tower first charging aperture 301
Entering in isopropanol tower 300 carries out isopropanol tower rectifying, produces from the isopropanol tower gas phase extraction mouth 304 of 300 tower top of isopropanol tower
The gas phase portion of isopropanol tower rectifying, after compressing through isopropanol tower heat pump compressor 308, obtains isopropanol tower heating agent gas, different
Propyl alcohol tower heating medium liquid carries out heat exchange by the 3rd recuperation of heat reboiler 311 and isopropanol tower tower reactor 305, and adjusts through the 3rd
Backflow is set up in isopropanol tower return tank 306 after the cooling of warm cooling tower 309, phegma passes through isopropanol tower second charging aperture
302 enter isopropanol tower 300, and distillate enters ethanol tower 200 through the 3rd charging aperture of ethanol tower 203 and carries out ethanol tower essence again
Evaporate；The number of plates of isopropanol tower 300 is 150, and reflux ratio is 7；The liquid phase part temperature that ethanol tower tower reactor 205 is produced is 85.4
DEG C, pressure is 22.5kPa；The gas phase portion temperature of 300 overhead extraction of isopropanol tower is 104.8 DEG C, and pressure is 160kPa；Through
After heat pump compression, the temperature of the isopropanol tower heating agent gas for obtaining is 140.2 DEG C, and pressure is 407kPa；Isopropanol tower heating agent gas
Before body starts backflow after recuperation of heat reboiler and cooler cooling, temperature is 113 DEG C, and pressure is 360kPa；Flow back into
The backflow liquid temp for entering isopropanol tower is 113.3 DEG C, and pressure is 800kPa；Enter ethanol tower distillates liquid temp for 113.3 DEG C,
Pressure is 800kPa.
From the liquid phase part of the isopropanol rectifying of 305 bottom of isopropanol tower tower reactor extraction, through weight-removing column first charging aperture 401
Sending into weight-removing column 400 carries out weight-removing column rectifying, produces weight-removing column from the weight-removing column gas phase extraction mouth 404 of the tower top of weight-removing column 400
The gas phase portion of rectifying, after weight-removing column condenser 408 is cooled down, enters weight-removing column return tank 406 and sets up backflow, and phegma leads to
Cross weight-removing column second charging aperture 402 and weight-removing column 400 is flowed back into, distillate cooling is collected and enters isopropanol products pot 307；De- weight
The liquid phase part interim acquisition of the weight-removing column rectifying in tower tower reactor 405 enters heavy constituent products pot 407, that is, obtain the restructuring that reacts
Divide impurity；The number of plates of weight-removing column is 80, and overhead reflux ratio is 0.8；Isopropanol tower tower reactor 305 produce liquid phase part temperature be
110.6 DEG C, pressure is 182.5kPa；When entering weight-removing column 400 after heating pressurization, temperature is 110.7 DEG C, and pressure is
400kPa；The gas phase portion temperature of 400 overhead extraction of weight-removing column is 47.5 DEG C, and pressure is 800kPa；Flow back into weight-removing column 400
Backflow liquid temp be 45 DEG C, pressure be 800kPa；Distillate isopropanol temperature is 45 DEG C, and pressure is 600kPa；Weight-removing column tower
The liquid phase part temperature that kettle 400 is produced is 90 DEG C, and pressure is 800kPa.
When post processing work just starts, lightness-removing column tower reactor 105 absorbs heat, second by lightness-removing column reboiler 110 from extraneous
Alcohol tower tower reactor 205 goes into operation reboiler 210 from the extraneous heat that absorbs to provide starting impetus, isopropanol tower tower reactor by ethanol tower
305 go into operation reboiler 310 from the extraneous heat that absorbs to provide starting impetus by isopropanol tower, and weight-removing column tower reactor 405 is by de-
Weight tower reboiler 410 absorbs heat from extraneous；After last handling process is stable, weight-removing column tower reactor 405 is boiled again still through weight-removing column
Device 410 absorbs heat；Ethanol tower tower reactor 205 and isopropanol tower tower reactor 305 then change by respectively by the second recuperation of heat reboiler
211 and the 3rd recuperation of heat reboiler 311 carry out heat exchange with the heating agent gas after heat pump compression to absorb heat；Lightness-removing column
Then both heat is absorbed from extraneous by lightness-removing column reboiler 110, compress further through the first recuperation of heat reboiler 111 and through heat pump
Ethanol tower heating agent gas carry out heat exchange absorb heat.
Being computed, 1 ton of reactant liquor often being processed using above-mentioned technique, need to consume 0.6 ton of 5MPa high steam, 1MPa normal pressure steams
1.67 tons of vapour, power consumption 440kWh.Compared with conventional rectification, power consumption increased about 33.3%, 1MPa atmospheric steam and save about
72.5%.0.404kg standard coal is approximately equal to 1kWh electricity, 1 ton of 1MPa atmospheric steam is approximately equal to 205kg standard coal, comprehensively often locates
1 ton of reactant liquor of reason, can economize on coal about 0.8 ton.
It is pointed out that the number of plates of each tower in embodiment 1, overhead reflux ratio and everywhere the temperature of gas-liquid liquid with
Pressure value, only one is preferably worth, and these values can be floated in following scope：
The number of plates of lightness-removing column 100 is 95-110, and the reflux ratio of tower top is 30-60；Enter the reaction liquid temperature of lightness-removing column 100
Spend for 35-45 DEG C, pressure is 300-500kPa；The gas phase portion temperature of 100 overhead extraction of lightness-removing column is 61.5-71.5 DEG C, pressure
Power is 5-15kPa；The backflow liquid temp for flowing back into lightness-removing column 100 is 50-60 DEG C, and pressure is 500-700kPa；Distillate liquid temperature
Spend for 40-50 DEG C, pressure is 550-750kPa；The liquid phase part temperature that lightness-removing column tower reactor 105 is produced is 80-90 DEG C, and pressure is
10-20kPa；When entering ethanol tower 200 after heating pressurization, temperature is 100-110 DEG C, and pressure is 100-200kPa；
The number of plates of ethanol tower 200 is 140-160, and reflux ratio is 8-10；The gas phase portion temperature of 200 overhead extraction of ethanol tower
Spend for 73-83 DEG C, pressure is 0-5kPa；After heat pump compression, the temperature of the ethanol tower heating agent gas for obtaining is 132-142
DEG C, pressure is 150-250kPa；Before ethanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cooling,
Temperature is 75-85 DEG C, and pressure is 90-110kPa；The backflow liquid temp for flowing back into ethanol tower 200 is 75-85 DEG C, and pressure is
400-500kPa；Liquid temp is distillated for 40-50 DEG C, pressure is 500-700kPa；The liquid phase part temperature that ethanol tower tower reactor 205 is produced
Spend for 80-90 DEG C, pressure is 10-30kPa；
The number of plates of isopropanol tower 300 is 140-160, and reflux ratio is 5-9；The gas phase portion of 300 overhead extraction of isopropanol tower
It is 100-110 DEG C to divide temperature, and pressure is 110-210kPa；After heat pump compression, the temperature of the isopropanol tower heating agent gas for obtaining
Spend for 135-145 DEG C, pressure is 300-500kPa；Isopropanol tower heating agent gas is cooled down through recuperation of heat reboiler and cooler
After start backflow before, temperature be 108-118 DEG C, pressure be 260-460kPa；Flow back into the backflow liquid temp of isopropanol tower 300
For 108-118 DEG C, pressure is 700-900kPa；Enter ethanol tower 200 distillates liquid temp for 108-118 DEG C, and pressure is 700-
900kPa；The liquid phase part temperature that isopropanol tower tower reactor 305 is produced is 105-115 DEG C, and pressure is 130-230kPa；Through heating
When entering weight-removing column 400 after pressurization, temperature is 105-115 DEG C, and pressure is 300-500kPa；
The number of plates of weight-removing column 400 is 70-85, and overhead reflux ratio is 0.5-1；The gas phase portion of 400 overhead extraction of weight-removing column
It is 45-52 DEG C to divide temperature, and pressure is 750-850kPa；The backflow liquid temp for flowing back into weight-removing column 400 is 40-50 DEG C, pressure
For 750-850kPa；Distillate isopropanol temperature is 40-50 DEG C, and pressure is 500-700kPa；The liquid that weight-removing column tower reactor 405 is produced
Phase portion temperature is 80-100 DEG C, and pressure is 750-850kPa.
Isopropyl acetate hydrogenation liquid by the said equipment with method respectively to remaining 8 batches is post-processed, and 9
Ethanol and isopropanol product that individual batch is obtained, determine water content using Moisture Meter, are determined in reactant liquor by gas chromatography
Main component than water and the content of major impurity.Concrete content is shown in Table two and table three：
Table two：Alcohol product purity and major impurity content (unit：%)
| Batch | Ethanol | Water | Isopropanol | Isopropyl acetate |
| 1st batch | 99.93 | 0.046 | 0.001 | 0.022 |
| 2nd batch | 99.96 | 0.021 | 0.002 | 0.022 |
| 3rd batch | 99.94 | 0.042 | 0.005 | 0.022 |
| 4th batch | 99.92 | 0.037 | 0.014 | 0.023 |
| 5th batch | 99.92 | 0.034 | 0.027 | 0.023 |
| 6th batch | 99.93 | 0.044 | 0.010 | 0.022 |
| 7th batch | 99.93 | 0.044 | 0.006 | 0.023 |
| 8th batch | 99.92 | 0.052 | 0.006 | 0.021 |
| 9th batch | 99.92 | 0.046 | 0.007 | 0.021 |
Table three：Isopropanol product purity and major impurity content (unit：%)
| Batch | Isopropanol | Water | Ethanol | 4-methyl-2 pentanone (MIBK) |
| 1st batch | 99.96 | 0.006 | 0.030 | 0.0040 |
| 2nd batch | 99.95 | 0.007 | 0.031 | 0.0042 |
| 3rd batch | 99.96 | 0.011 | 0.028 | 0.0044 |
| 4th batch | 99.95 | 0.011 | 0.031 | 0.0046 |
| 5th batch | 99.96 | 0.005 | 0.025 | 0.0025 |
| 6th batch | 99.96 | 0.010 | 0.023 | 0.0035 |
| 7th batch | 99.97 | 0.011 | 0.021 | 0.0015 |
| 8th batch | 99.97 | 0.011 | 0.021 | 0.0036 |
| 9th batch | 99.97 | 0.012 | 0.020 | 0.0017 |
Above-described embodiment technology design only to illustrate the invention and feature, its object is to allow person skilled in the art
Scholar will appreciate that present disclosure and implement according to this, can not be limited the scope of the invention with this.All according to the present invention
Equivalence changes or modification that Spirit Essence is made, should all be included within the scope of the present invention.
Claims (3)
1. isopropyl acetate hydrogenization method produces the post-processing approach of ethanol and isopropanol, it is characterised in that：
The reactant liquor of isopropyl acetate hydrogenation is sent into from the middle part of lightness-removing column (100) in lightness-removing column (100) carries out lightness-removing column
Rectifying, sets up the backflow of the gas phase portion of lightness-removing column rectifying in lightness-removing column (100) tower top, and distillate cooling is collected and obtains reaction
Light component impurity；
The liquid phase part of lightness-removing column rectifying is produced from lightness-removing column tower reactor (105) bottom, through sending into ethanol tower in the middle part of ethanol tower (200)
(200) in, ethanol tower rectifying is carried out, from the gas phase portion of ethanol tower (200) overhead extraction ethanol tower rectifying, after heat pump compression,
Ethanol tower heating agent gas is obtained, ethanol tower heating agent gas is respectively by recuperation of heat reboiler and lightness-removing column tower reactor (105) and second
Alcohol tower tower reactor (205) carries out heat exchange, and sets up the backflow for entering ethanol tower, and distillate cooling collection obtains alcohol product；
The liquid phase part of ethanol tower rectifying is produced from ethanol tower tower reactor (205) bottom, through sending into isopropyl in the middle part of isopropanol tower (300)
Alcohol tower (300) carries out isopropanol tower rectifying, from the gas phase portion of the isopropanol rectifying of isopropanol tower (300) overhead extraction, through heat
After pump pressure contracting, isopropanol tower heating agent gas is obtained, isopropanol tower heating medium liquid is by recuperation of heat reboiler and isopropanol tower tower reactor
(305) heat exchange cooling is carried out, and the backflow for entering isopropanol tower is set up, distillate is through entering ethanol in the middle part of ethanol tower (200)
Tower (200) carries out ethanol tower rectifying again；
From the liquid phase part of the isopropanol rectifying of isopropanol tower tower reactor (305) bottom extraction, de- through sending in the middle part of weight-removing column (400)
Weight tower (400) carries out weight-removing column rectifying, from the gas phase portion of weight-removing column (400) overhead extraction weight-removing column rectifying and sets up backflow,
Distillate cooling collection obtains isopropanol product；The liquid phase part of the weight-removing column rectifying in interim acquisition weight-removing column tower reactor (405),
The heavy constituent impurity that reacts is obtained；
Post processing just start when, each tower tower reactor (105,205,305,405) respectively by reboiler (110,210,310,
410) heat is absorbed from extraneous；After last handling process is stable, weight-removing column tower reactor (405) is still through weight-removing column reboiler (410)
Absorb heat；Ethanol tower tower reactor (205) and isopropanol tower tower reactor (305) then change by respectively by the second recuperation of heat reboiler
And the 3rd recuperation of heat reboiler (311) carries out heat exchange absorbing heat with the heating agent gas after heat pump compression (211)；De-
Light tower (100) then both absorbed heat by lightness-removing column reboiler (110) from extraneous, further through the first recuperation of heat reboiler (111)
Heat exchange is carried out with the ethanol tower heating agent gas compressed through heat pump and absorb heat；
The number of plates of lightness-removing column (100) is 95-110, and the reflux ratio of tower top is 30-60；Enter the reaction of lightness-removing column (100)
Liquid temp is 35-45 DEG C, and pressure is 300-500kPa；The gas phase portion temperature of lightness-removing column (100) overhead extraction is 61.5-71.5
DEG C, pressure is 5-15kPa；The backflow liquid temp for flowing back into lightness-removing column (100) is 50-60 DEG C, and pressure is 500-700kPa；Evaporate
Go out liquid temp for 40-50 DEG C, pressure is 550-750kPa；The liquid phase part temperature that lightness-removing column tower reactor (105) is produced is 80-90
DEG C, pressure is 10-20kPa；When entering ethanol tower (200) after heating pressurization, temperature is 100-110 DEG C, and pressure is 100-
200kPa；
The number of plates of ethanol tower (200) is 140-160, and reflux ratio is 8-10；The gas phase portion of ethanol tower (200) overhead extraction
It is 73-83 DEG C to divide temperature, and pressure is 0-5kPa；After heat pump compression, the temperature of the ethanol tower heating agent gas for obtaining is 132-
142 DEG C, pressure is 150-250kPa；Ethanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cooling
Before, temperature is 75-85 DEG C, and pressure is 90-110kPa；The backflow liquid temp for flowing back into ethanol tower (200) is 75-85 DEG C, pressure
Power is 400-500kPa；Liquid temp is distillated for 40-50 DEG C, pressure is 500-700kPa；The liquid phase that ethanol tower tower reactor (205) is produced
Portion temperature is 80-90 DEG C, and pressure is 10-30kPa；
The number of plates of isopropanol tower (300) is 140-160, and reflux ratio is 5-9；The gas of isopropanol tower (300) overhead extraction
Phase portion temperature is 100-110 DEG C, and pressure is 110-210kPa；After heat pump compression, the isopropanol tower heating agent gas that obtains
Temperature be 135-145 DEG C, pressure be 300-500kPa；Isopropanol tower heating agent gas is through recuperation of heat reboiler and cooler
Before starting backflow after cooling, temperature is 108-118 DEG C, and pressure is 260-460kPa；Flow back into the backflow of isopropanol tower (300)
Liquid temp is 108-118 DEG C, and pressure is 700-900kPa；Enter ethanol tower (200) distillates liquid temp for 108-118 DEG C, pressure
Power is 700-900kPa；The liquid phase part temperature that isopropanol tower tower reactor (305) is produced is 105-115 DEG C, and pressure is 130-
230kPa；When entering weight-removing column (400) after heating pressurization, temperature is 105-115 DEG C, and pressure is 300-500kPa；
The number of plates of weight-removing column (400) is 70-85, and overhead reflux ratio is 0.5-1；The gas of weight-removing column (400) overhead extraction
Phase portion temperature is 45-52 DEG C, and pressure is 750-850kPa；The backflow liquid temp for flowing back into weight-removing column (400) is 40-50
DEG C, pressure is 750-850kPa；Distillate isopropanol temperature is 40-50 DEG C, and pressure is 500-700kPa；Weight-removing column tower reactor
(405) the liquid phase part temperature for producing is 80-100 DEG C, and pressure is 750-850kPa.
2. post-processing approach according to claim 1, it is characterised in that the liquid phase part of the lightness-removing column rectifying, from de-
Light tower tower reactor extraction, to entering between ethanol tower (200), also one dehydration.
3. post-processing approach according to claim 2, it is characterised in that the dehydration includes, by lightness-removing column rectifying
Liquid phase part first pass through molecular sieve and carry out pressure-variable adsorption dehydration, after the material after dehydration to be carried out inorganic permeable membrane dehydration again
Secondary through molecular sieve dehydration.
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| CN105037094A (en) * | 2015-08-05 | 2015-11-11 | 安徽皖维高新材料股份有限公司 | Energy coupling distillation method for preparing ethyl alcohol by means of acetic acid ester hydrogenation |
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| CN105037094A (en) * | 2015-08-05 | 2015-11-11 | 安徽皖维高新材料股份有限公司 | Energy coupling distillation method for preparing ethyl alcohol by means of acetic acid ester hydrogenation |
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