CN105693468A - Post treatment device and post treatment method of ethanol and isopropanol produced by isopropyl acetate hydrogenation method - Google Patents
Post treatment device and post treatment method of ethanol and isopropanol produced by isopropyl acetate hydrogenation method 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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Abstract
The invention relates to a post treatment device and a post treatment method of ethanol and isopropanol which are produced by an isopropyl acetate hydrogenation method. The device comprises a light-component removal tower, an ethanol tower, an isopropanol tower and a heavy-component removal tower, wherein backflows are respectively set up at the tops of all the towers, and a liquid phase is sequentially sent to the middle part of the next tower from a kettle of one tower; a heat pump compression technology is adopted by the backflows at the tops of the ethanol tower and the isopropanol tower, so that not only is the heat energy needed by the backflows of the ethanol tower and the isopropanol tower met, but the ethanol tower is also capable of providing part of heat energy needed by the light-component removal tower. After the whole device and method are used, the consumption of steam in the separation engineering of the ethanol and the isopropanol is greatly reduced; furthermore, condensers arranged at the tops of the ethanol tower and the isopropanol tower are omitted, so that the demand for cooling water is reduced, and effects of saving energy and reducing emission are achieved.
Description
Technical field
The present invention relates to ethanol and isopropanol rectifying device and method that a kind of rectifying device and method, particularly isopropyl acetate hydrogenization method produce。
Background technology
Isopropanol is a kind of important industrial chemicals, is widely used in the fields such as pesticide, medicine, electronics, daily use chemicals, at present, the main method of industrial production isopropanol is propylene hydration method, the method needs the sulphuric acid that working concentration is higher, and equipment corrosion is higher, and technological process is complicated。
Chinese patent CN103980089 reports a kind of technique utilizing isopropyl acetate hydrogenization method to produce ethanol and isopropanol, this technique transformation efficiency is high, flow process is simple, but this explained hereafter is the mixture of ethanol and isopropanol, both ratios are about 2:3, although proposition can both separate this paper by the method for rectification, but the boiling point of ethanol and isopropanol difference only 4 DEG C, therefore adopting conventional rectification, the energy consumption of process will certainly be significantly high。And the purity of the isopropanol frequently resulted in is less than 99.5%, the demand in market can not be met far away。
" the Ethanol Isopropanol separating technology based on MVR heat pump distillation " reports the heat pump distillation method separating alcohol with the simulation of AspenPlus chemical process simulation software and the rectification process of isopropanol, but it adopts single tower distillation, the isopropanol theoretical concentration obtained also is only capable of reaching 99.0%, and when calculating, only account for ethanol and isopropanol mixture, and the hydrogenation of isopropyl acetate there is also the impurity such as 2-amylalcohol, only cannot obtain highly purified ethanol and isopropanol by single tower distillation technique。
Summary of the invention
The invention aims to the equipment for after-treatment and the method that provide a kind of isopropyl acetate hydrogenization method to produce ethanol and isopropanol, it can improve the purity of isopropanol, and reduces required energy consumption, reduces the discharge of waste gas。
Isopropyl acetate hydrogenization method provided by the invention being produced to the equipment for after-treatment of ethanol and isopropanol, its technical scheme is:
Including: include lightness-removing column, ethanol tower, isopropanol tower and weight-removing column；
The middle part of described lightness-removing column is provided with lightness-removing column the first charging aperture, and top is provided with lightness-removing column the second charging aperture, and tower top is provided with lightness-removing column gas phase extraction mouth, is lightness-removing column tower reactor at the bottom of tower；Being respectively arranged with ethanol tower the first charging aperture and ethanol tower the 3rd charging aperture in the middle part of described ethanol tower from low to high, top is provided with ethanol tower the second charging aperture, and tower top is provided with ethanol tower gas phase extraction mouth, is ethanol tower tower reactor at the bottom of tower；Being provided with isopropanol tower the first charging aperture in the middle part of described isopropanol tower, top is provided with isopropanol tower the second charging aperture, and tower top is provided with isopropyl tower gas phase extraction mouth, is isopropanol tower tower reactor at the bottom of tower；Being provided with weight-removing column the first charging aperture in the middle part of described weight-removing column, top is provided with weight-removing column the second charging aperture, and tower top is provided with weight-removing column gas phase extraction mouth, is weight-removing column tower tower reactor at the bottom of tower；
Described lightness-removing column the first charging aperture coupled reaction liquid；Described lightness-removing column gas phase extraction mouth is connected with the arrival end of condenser of light component removal column by pipeline, the port of export of condenser of light component removal column is connected with the arrival end of lightness-removing column return tank by pipeline, and the port of export of lightness-removing column return tank is connected respectively to lightness-removing column the second charging aperture and light component product tank by pipeline；The bottom of described lightness-removing column tower reactor is connected with the refrigerant inlet end of lightness-removing column reboiler and the first recuperation of heat reboiler respectively by pipeline, and the top of lightness-removing column tower reactor is connected with the refrigerant exit end of lightness-removing column reboiler and the first recuperation of heat reboiler respectively by pipeline；
Described ethanol tower the first charging aperture is connected with bottom described lightness-removing column tower reactor by pipeline, described ethanol tower gas phase extraction mouth is connected with the arrival end of ethanol tower heat pump compressor by pipeline, the port of export of ethanol tower heat pump compressor is connected with the heating agent arrival end of the first recuperation of heat reboiler and the second recuperation of heat reboiler respectively by pipeline, the heating agent port of export of the first recuperation of heat reboiler and the second recuperation of heat reboiler is connected to the arrival end of ethanol tower return tank respectively through pipeline, the port of export of ethanol tower return tank is connected respectively to ethanol tower the second charging aperture and alcohol product tank by pipeline；Gone into operation with ethanol tower respectively by the pipeline refrigerant inlet end of reboiler and the second recuperation of heat reboiler of the bottom of described ethanol tower tower reactor is connected, and gone into operation with ethanol tower respectively by the pipeline refrigerant exit end of reboiler and the second recuperation of heat reboiler of the top of ethanol tower tower reactor is connected；
Described isopropanol tower the first charging aperture is connected with bottom described ethanol tower tower reactor by pipeline, described isopropanol tower gas phase extraction mouth is connected with the arrival end of isopropanol tower heat pump compressor by pipeline, the port of export of isopropanol tower heat pump compressor is connected by the heating agent arrival end of pipeline the 3rd recuperation of heat reboiler, the heating agent port of export of the 3rd recuperation of heat reboiler is connected to the arrival end of isopropanol tower return tank by pipeline, and the port of export of isopropanol tower return tank is connected respectively to isopropanol tower the second charging aperture and ethanol tower the 3rd charging aperture by pipeline；Gone into operation with isopropanol tower respectively by the pipeline refrigerant inlet end of reboiler and the 3rd recuperation of heat reboiler of the bottom of described isopropanol tower tower reactor is connected, and gone into operation with isopropanol tower respectively by the pipeline refrigerant exit end of reboiler and the 3rd recuperation of heat reboiler of the top of isopropanol tower tower reactor is connected；
Described weight-removing column the first charging aperture is connected with bottom described isopropanol tower tower reactor by pipeline, described weight-removing column gas phase extraction mouth is connected with the arrival end of weight-removing column condenser by pipeline, the port of export of weight-removing column condenser is connected with the warehouse-in end of weight-removing column return tank by pipeline, the port of export of weight-removing column return tank is connected respectively to weight-removing column the second charging aperture and isopropanol products pot by pipeline, and described weight-removing column return tank is also associated with depressurized system；The bottom of described weight-removing column tower reactor by pipeline and weight-removing column reboiler and refrigerant inlet end be connected, the refrigerant exit end that the top of weight-removing column tower reactor takes off heavily reboiler by pipeline is connected；The bottom of weight-removing column tower reactor is connected to heavy constituent products pot also by pipeline；
Go into operation reboiler, isopropanol tower of described lightness-removing column reboiler, ethanol tower goes into operation reboiler and weight-removing column reboiler is the reboiler of additional heating agent；
Described equipment for after-treatment also includes some being arranged on pipeline for carrying liquid and/or making the pump of liquid supercharging and the valve of the flow velocity and the flow direction for controlling liquid。
Further, it is additionally provided with light component cooler between the remaining light component product tank of described lightness-removing column return tank。
Further, the pipeline connected between the heating agent port of export and the arrival end of ethanol tower return tank of described first recuperation of heat reboiler is provided with the first trim cooler；The pipeline connected between the heating agent port of export and the arrival end of ethanol tower return tank of described second recuperation of heat reboiler is provided with the second trim cooler；The pipeline connected between the heating agent port of export and the arrival end of isopropanol tower return tank of described 3rd recuperation of heat reboiler is provided with the 3rd trim cooler；
Further, connect and the pipeline of ethanol tower the first charging aperture and lightness-removing column tower reactor is additionally provided with water trap。
Further, described water trap adopts molecular sieve adsorption dehydrater and/or inorganic infiltrating and vaporizing membrane dehydrater。
Isopropyl acetate hydrogenization method provided by the invention is produced to the post-processing approach of ethanol and isopropanol, the technical scheme is that
The reactant liquor of isopropyl acetate hydrogenation being carried out lightness-removing column rectification from sending in lightness-removing column in the middle part of lightness-removing column, sets up the backflow of the gas phase portion of lightness-removing column rectification at lightness-removing column tower top, the light composition impurity obtaining reaction is collected in distillate cooling；
The liquid phase part of extraction lightness-removing column rectification bottom lightness-removing column tower reactor, ethanol tower rectification is carried out through sending in ethanol tower in the middle part of ethanol tower, gas phase portion from ethanol tower overhead extraction ethanol tower rectification, after heat pump compresses, obtain ethanol tower heating agent gas, ethanol tower heating agent gas carries out heat exchange respectively through recuperation of heat reboiler and lightness-removing column tower reactor and ethanol tower tower reactor, and sets up the backflow entering ethanol tower, and distillate cooling collection obtains alcohol product；
The liquid phase part of extraction ethanol tower rectification bottom ethanol tower tower reactor, in the middle part of isopropanol tower, send into isopropanol tower carry out isopropanol tower rectification, gas phase portion from the isopropanol rectification of isopropanol column overhead extraction, after heat pump compresses, obtain isopropanol tower heating agent gas, isopropanol tower heating medium liquid carries out heat exchange cooling by recuperation of heat reboiler and isopropanol tower tower reactor, and sets up the backflow entering isopropanol tower, and distillate enters ethanol tower in the middle part of ethanol tower and again carries out ethanol tower rectification；
The liquid phase part of the isopropanol rectification of extraction bottom isopropanol tower tower reactor, sends into weight-removing column in the middle part of weight-removing column and carries out weight-removing column rectification, and from the gas phase portion of weight-removing column overhead extraction weight-removing column rectification and set up backflow, distillate cooling collection obtains isopropanol product；The liquid phase part of the weight-removing column rectification in interim acquisition weight-removing column tower reactor, namely obtains the heavy constituent impurity of reaction；
When post processing just starts, each tower tower reactor absorbs heat respectively through reboiler from the external world；After last handling process is stable, weight-removing column tower reactor absorbs heat still through weight-removing column reboiler；Ethanol tower tower reactor and isopropanol tower tower reactor then change and are carried out heat exchange to absorb heat by respectively through the second recuperation of heat reboiler and the 3rd recuperation of heat reboiler with the heating agent gas after heat pump compresses；Lightness-removing column then both absorbed heat by lightness-removing column reboiler from the external world, carries out heat exchange further through the first recuperation of heat reboiler with the ethanol tower heating agent gas through heat pump compression and absorbs heat。
Further, the liquid phase part of described lightness-removing column rectification, from lightness-removing column tower reactor extraction, to entering between ethanol tower, also have a dehydration。
Further, described dehydration includes, and the liquid phase part of lightness-removing column rectification is first passed through molecular sieve and carries out pressure-variable adsorption dehydration, again passes by molecular sieve dehydration after the material after dehydration is carried out inorganic permeable membrane dehydration。
Further, the number of plates of described lightness-removing column is 95-110, and the reflux ratio of tower top is 30-60；The reacting liquid temperature entering lightness-removing column 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, and pressure is 5-15kPa；The backflow temperature 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；Entering ethanol tower temperature after heating pressurization and be 100-110 DEG C, pressure is 100-200kPa；
The number of plates of described ethanol tower is 140-160, and reflux ratio is 8-10；The gas phase portion temperature of ethanol tower overhead extraction is 73-83 DEG C, and pressure is 0-5kPa；After heat pump compresses, the temperature of the ethanol tower heating agent gas obtained is 132-142 DEG C, and pressure is 150-250kPa；Before ethanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 75-85 DEG C, and pressure is 90-110kPa；The backflow temperature flowing back into ethanol tower is 75-85 DEG C, and pressure is 400-500kPa；Distillate temperature is 40-50 DEG C, and pressure is 500-700kPa；The liquid phase part temperature of ethanol tower tower reactor extraction is 80-90 DEG C, and pressure is 10-30kPa；
The number of plates of described isopropanol tower is 140-160, and reflux ratio is 5-9；The gas phase portion temperature of isopropanol column overhead extraction is 100-110 DEG C, and pressure is 110-210kPa；After heat pump compresses, the temperature of the isopropanol tower heating agent gas obtained is 135-145 DEG C, and pressure is 300-500kPa；Before isopropanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 108-118 DEG C, and pressure is 260-360kPa；The backflow temperature flowing back into isopropanol tower is 108-118 DEG C, and pressure is 700-900kPa；The distillate temperature entering ethanol tower is 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；Entering weight-removing column temperature after heating pressurization and be 105-115 DEG C, pressure is 300-500kPa；
The number of plates of described weight-removing column is 70-85, and overhead reflux is than for 0.5-1；The gas phase portion temperature of weight-removing column overhead extraction is 45-52 DEG C, and pressure is 750-850kPa；The backflow temperature 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 is 80-100 DEG C, and pressure is 750-850kPa。
Technical scheme has following notable beneficial effect:
Take this equipment and method, separate the ethanol and isopropanol purity that obtain all more than 99.9%；Take this equipment and method, take full advantage of the heat of tower top, although add the consumption of electric energy on a small quantity, but save condensed water in a large number and for heating the steam of tower reactor, save the energy generally, and decrease the discharge of waste liquid waste gas。
Accompanying drawing explanation
Fig. 1 is the structural representation of present device
Detailed description of the invention
Embodiment 1
Take the isopropyl acetate hydrogenation liquid of 9 batches of different batches, utilize Moisture Meter to measure water content, by the content of main component than water in gas chromatography determination reactant liquor and major impurity。Concrete content is in Table one:
Each main component and major impurity containing scale (unit: %) in one: nine batch of different batches isopropyl acetate hydrogenation liquid of table
1st batch reaction liquid is heated to 40 DEG C, it is pressurized to 400kPa, the lightness-removing column 100 at the uniform velocity sent into from lightness-removing column the first charging aperture 101 being arranged in the middle part of lightness-removing column 100 carries out lightness-removing column rectification, light component is from lightness-removing column gas phase extraction mouth 104 extraction of the tower top of lightness-removing column 100, lightness-removing column return tank 106 is entered after condenser of light component removal column 108 cools down, the second charging aperture 102 then passing through lightness-removing column 100 top passes back into lightness-removing column 100, distillate, by light component cooler 112, enters light component product tank 107 after cooling；The number of plates of lightness-removing column 100 is 100, and the reflux ratio of overhead reflux is 45；The light component temperature of lightness-removing column gas phase extraction mouth 104 extraction is 66.4 DEG C, and pressure is 10kPa, and the backflow temperature flowing back into lightness-removing column 100 is 55.4 DEG C, and pressure is 600kPa；Distillate temperature is 45 DEG C, and pressure is 650kPa。
The liquid phase part of extraction lightness-removing column rectification bottom lightness-removing column tower reactor 105, after molecular sieve adsorption dehydrater 501 and inorganic infiltrating and vaporizing membrane dehydrater 502 dewater, send into through ethanol tower the first charging aperture 201 and in ethanol tower 200, carry out ethanol tower rectification, gas phase portion from the ethanol tower gas phase extraction mouth 204 extraction ethanol tower rectification of ethanol tower 200 tower top, after ethanol tower heat pump compressor 208 compresses, obtain ethanol tower heating agent gas, ethanol tower heating agent gas carries out heat exchange respectively through the first recuperation of heat reboiler 111 and the second recuperation of heat reboiler 211 with lightness-removing column tower reactor 105 and ethanol tower tower reactor 205, and set up backflow respectively through after the cooling of the first homoiothermic cooling tower 109 and the second homoiothermic cooling tower 209 at ethanol tower return tank 206, backflow enters ethanol tower 200 by ethanol tower the second charging aperture 202, distillate cooling is collected and is entered alcohol product tank 207；The number of plates of ethanol tower 200 is 150, and reflux ratio is 9；The liquid phase part temperature of lightness-removing column tower reactor 105 extraction is 84.8 DEG C, and pressure is 20kPa；Entering temperature during ethanol tower 200 after heating is pressurizeed and dewatered is 106 DEG C, and pressure is 150kPa；The gas phase portion temperature of ethanol tower 200 overhead extraction is 78.3 DEG C, and pressure is 0kPa；After heat pump compresses, the temperature of the ethanol tower heating agent gas obtained is 137.3 DEG C, and pressure is 200kPa；Before ethanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 80 DEG C, and pressure is 100kPa；The backflow temperature flowing back into ethanol tower 200 is 80 DEG C, and pressure is 500kPa；Distillate temperature is 45 DEG C, and pressure is 600kPa。
The liquid phase part of extraction ethanol tower rectification bottom ethanol tower tower reactor 205, send into through isopropanol tower the first charging aperture 301 and in isopropanol tower 300, carry out isopropanol tower rectification, gas phase portion from the isopropanol tower gas phase extraction mouth 304 extraction isopropanol tower rectification of isopropanol tower 300 tower top, after isopropanol tower heat pump compressor 308 compresses, obtain isopropanol tower heating agent gas, isopropanol tower heating medium liquid carries out heat exchange by the 3rd recuperation of heat reboiler 311 with isopropanol tower tower reactor 305, and set up backflow at isopropanol tower return tank 306 after the cooling of the 3rd homoiothermic cooling tower 309, backflow enters isopropanol tower 300 by isopropanol tower the second charging aperture 302, distillate enters ethanol tower 200 through ethanol tower the 3rd charging aperture 203 and again carries out ethanol tower rectification；The number of plates of isopropanol tower 300 is 150, and reflux ratio is 7；The liquid phase part temperature of ethanol tower tower reactor 205 extraction is 85.4 DEG C, and pressure is 22.5kPa；The gas phase portion temperature of isopropanol tower 300 overhead extraction is 104.8 DEG C, and pressure is 160kPa；After heat pump compresses, the temperature of the isopropanol tower heating agent gas obtained is 140.2 DEG C, and pressure is 407kPa；Before isopropanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 113 DEG C, and pressure is 360kPa；The backflow temperature flowing back into isopropanol tower is 113.3 DEG C, and pressure is 800kPa；The distillate temperature entering ethanol tower is 113.3 DEG C, and pressure is 800kPa。
The liquid phase part of the isopropanol rectification of extraction bottom isopropanol tower tower reactor 305, send into weight-removing column 400 through weight-removing column the first charging aperture 401 and carry out weight-removing column rectification, gas phase portion from the weight-removing column gas phase extraction mouth 404 extraction weight-removing column rectification of the tower top of weight-removing column 400, after weight-removing column condenser 408 cools down, enter weight-removing column return tank 406 and set up backflow, backflow flows back into weight-removing column 400 by weight-removing column the second charging aperture 402, and distillate cooling is collected and entered isopropanol products pot 307；The liquid phase part interim acquisition of the weight-removing column rectification in weight-removing column tower reactor 405 enters heavy constituent products pot 407, namely obtains the heavy constituent impurity of reaction；The number of plates of weight-removing column is 80, and overhead reflux ratio is 0.8；The liquid phase part temperature of isopropanol tower tower reactor 305 extraction is 110.6 DEG C, and pressure is 182.5kPa；Entering temperature during weight-removing column 400 after heating pressurization is 110.7 DEG C, and pressure is 400kPa；The gas phase portion temperature of weight-removing column 400 overhead extraction is 47.5 DEG C, and pressure is 800kPa；The backflow temperature flowing back into weight-removing column 400 is 45 DEG C, and pressure is 800kPa；Distillate isopropanol temperature is 45 DEG C, and pressure is 600kPa；The liquid phase part temperature of weight-removing column tower reactor 400 extraction is 90 DEG C, and pressure is 800kPa。
When post processing work just starts, lightness-removing column tower reactor 105 is passed through lightness-removing column reboiler 110 and is absorbed heat from the external world, ethanol tower tower reactor 205 by ethanol tower go into operation reboiler 210 from the external world absorb heat to provide starting impetus, isopropanol tower tower reactor 305 absorbs heat to provide starting impetus by the isopropanol tower reboiler 310 that goes into operation from the external world, weight-removing column tower reactor 405 by weight-removing column reboiler 410 from external world's absorption heat；After last handling process is stable, weight-removing column tower reactor 405 absorbs heat still through weight-removing column reboiler 410；Ethanol tower tower reactor 205 and isopropanol tower tower reactor 305 then change and are carried out heat exchange to absorb heat by respectively through the second recuperation of heat reboiler 211 and the 3rd recuperation of heat reboiler 311 with the heating agent gas after heat pump compresses；Lightness-removing column then both absorbed heat by lightness-removing column reboiler 110 from the external world, carries out heat exchange further through the first recuperation of heat reboiler 111 with the ethanol tower heating agent gas through heat pump compression and absorbs heat。
It is computed, utilizes above-mentioned technique often to process 1 ton of reactant liquor, 5MPa high steam 0.6 ton, 1MPa atmospheric steam 1.67 tons, power consumption 440kWh need to be consumed。Compared with conventional rectification, power consumption adds about 33.3%, and 1MPa atmospheric steam saves about 72.5%。Approximating 0.404kg standard coal with 1kWh electricity, 1 ton of 1MPa atmospheric steam approximates 205kg standard coal, comprehensively often processes 1 ton of reactant liquor, it is possible to 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 the temperature of gas-liquid liquid and force value everywhere, be only one and be preferably worth, 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；The reacting liquid temperature entering lightness-removing column 100 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, and pressure is 5-15kPa；The backflow temperature flowing back into lightness-removing column 100 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 105 extraction 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 ethanol tower 200 overhead extraction is 73-83 DEG C, and pressure is 0-5kPa；After heat pump compresses, the temperature of the ethanol tower heating agent gas obtained is 132-142 DEG C, and pressure is 150-250kPa；Before ethanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 75-85 DEG C, and pressure is 90-110kPa；The backflow temperature flowing back into ethanol tower 200 is 75-85 DEG C, and pressure is 400-500kPa；Distillate temperature is 40-50 DEG C, and pressure is 500-700kPa；The liquid phase part temperature of ethanol tower tower reactor 205 extraction 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 phase portion temperature of isopropanol tower 300 overhead extraction is 100-110 DEG C, and pressure is 110-210kPa；After heat pump compresses, the temperature of the isopropanol tower heating agent gas obtained is 135-145 DEG C, and pressure is 300-500kPa；Before isopropanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 108-118 DEG C, and pressure is 260-460kPa；The backflow temperature flowing back into isopropanol tower 300 is 108-118 DEG C, and pressure is 700-900kPa；The distillate temperature entering ethanol tower 200 is 108-118 DEG C, and pressure is 700-900kPa；The liquid phase part temperature of isopropanol tower tower reactor 305 extraction 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 is than for 0.5-1；The gas phase portion temperature of weight-removing column 400 overhead extraction is 45-52 DEG C, and pressure is 750-850kPa；The backflow temperature flowing back into weight-removing column 400 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 405 extraction is 80-100 DEG C, and pressure is 750-850kPa。
Respectively the isopropyl acetate hydrogenation liquid of residue 8 batches is carried out post processing by the said equipment with method, 9 batches of ethanol obtained and isopropanol product, Moisture Meter is utilized to measure water content, by the content of main component than water in gas chromatography determination reactant liquor and major impurity。Concrete content is 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 only for technology design and the feature of the present invention are described, its object is to allow person skilled in the art will appreciate that present disclosure and to implement according to this, can not limit the scope of the invention with this。All equivalences made according to spirit of the invention change or modify, and all should be encompassed within protection scope of the present invention。
Claims (9)
1. isopropyl acetate hydrogenization method produces the equipment for after-treatment of ethanol and isopropanol, it is characterised in that including: include lightness-removing column (100), ethanol tower (200), isopropanol tower (300) and weight-removing column (400)；
The middle part of described lightness-removing column (100) is provided with lightness-removing column the first charging aperture (101), top is provided with lightness-removing column the second charging aperture (102), tower top is provided with lightness-removing column gas phase extraction mouth (104), is lightness-removing column tower reactor (105) at the bottom of tower；Described ethanol tower (200) middle part is respectively arranged with ethanol tower the first charging aperture (201) and ethanol tower the 3rd charging aperture (203) from low to high, top is provided with ethanol tower the second charging aperture (202), tower top is provided with ethanol tower gas phase extraction mouth (204), is ethanol tower tower reactor (205) at the bottom of tower；Described isopropanol tower (300) middle part is provided with isopropanol tower the first charging aperture (301), top is provided with isopropanol tower the second charging aperture (302), tower top is provided with isopropyl tower gas phase extraction mouth (304), is isopropanol tower tower reactor (305) at the bottom of tower；Described weight-removing column (400) middle part is provided with weight-removing column the first charging aperture (401), top is provided with weight-removing column the second charging aperture (402), tower top is provided with weight-removing column gas phase extraction mouth (404), is weight-removing column tower tower reactor (405) at the bottom of tower；
Described lightness-removing column the first charging aperture (101) coupled reaction liquid；Described lightness-removing column gas phase extraction mouth (104) is connected by the arrival end of pipeline with condenser of light component removal column (108), the port of export of condenser of light component removal column (108) is connected with the arrival end of lightness-removing column return tank (106) by pipeline, and the port of export of lightness-removing column return tank (106) is connected respectively to lightness-removing column the second charging aperture (102) and light component product tank (107) by pipeline；The bottom of described lightness-removing column tower reactor (105) is connected with the refrigerant inlet end of lightness-removing column reboiler (110) and the first recuperation of heat reboiler (111) respectively by pipeline, and the top of lightness-removing column tower reactor (105) is connected with the refrigerant exit end of lightness-removing column reboiler (110) and the first recuperation of heat reboiler (111) respectively by pipeline；
Described ethanol tower the first charging aperture (201) is connected with described lightness-removing column tower reactor (105) bottom by pipeline, described ethanol tower gas phase extraction mouth (204) is connected by the arrival end of pipeline with ethanol tower heat pump compressor (208), the port of export of ethanol tower heat pump compressor (208) is connected with the heating agent arrival end of the first recuperation of heat reboiler (111) and the second recuperation of heat reboiler (211) respectively by pipeline, the heating agent port of export of the first recuperation of heat reboiler (111) and the second recuperation of heat reboiler (211) is connected to the arrival end of ethanol tower return tank (206) respectively through pipeline, the port of export of ethanol tower return tank (206) is connected respectively to ethanol tower the second charging aperture (202) and alcohol product tank (207) by pipeline；Gone into operation with ethanol tower respectively by the pipeline refrigerant inlet end of reboiler (210) and the second recuperation of heat reboiler (211) of the bottom of described ethanol tower tower reactor (205) is connected, and gone into operation with ethanol tower respectively by the pipeline refrigerant exit end of reboiler (210) and the second recuperation of heat reboiler (211) of the top of ethanol tower tower reactor (205) is connected；
Described isopropanol tower the first charging aperture (301) is connected with described ethanol tower tower reactor (205) bottom by pipeline, described isopropanol tower gas phase extraction mouth (304) is connected by the arrival end of pipeline with isopropanol tower heat pump compressor (308), the port of export of isopropanol tower heat pump compressor (308) is connected by the heating agent arrival end of pipeline the 3rd recuperation of heat reboiler (311), the heating agent port of export of the 3rd recuperation of heat reboiler (311) is connected to the arrival end of isopropanol tower return tank (306) by pipeline, the port of export of isopropanol tower return tank (306) is connected respectively to isopropanol tower the second charging aperture (302) and ethanol tower the 3rd charging aperture (203) by pipeline；Gone into operation with isopropanol tower respectively by the pipeline refrigerant inlet end of reboiler (310) and the 3rd recuperation of heat reboiler (311) of the bottom of described isopropanol tower tower reactor (305) is connected, and gone into operation with isopropanol tower respectively by the pipeline refrigerant exit end of reboiler (310) and the 3rd recuperation of heat reboiler (311) of the top of isopropanol tower tower reactor (305) is connected；
Described weight-removing column the first charging aperture (401) is connected with described isopropanol tower tower reactor (305) bottom by pipeline, described weight-removing column gas phase extraction mouth (404) is connected by the arrival end of pipeline with weight-removing column condenser (408), the port of export of weight-removing column condenser (408) is connected with the warehouse-in end of weight-removing column return tank (406) by pipeline, the port of export of weight-removing column return tank (406) is connected respectively to weight-removing column the second charging aperture (402) and isopropanol products pot (307) by pipeline, described weight-removing column return tank (406) is also associated with depressurized system；The bottom of described weight-removing column tower reactor (405) by pipeline and weight-removing column reboiler (410) and refrigerant inlet end be connected, the top of weight-removing column tower reactor (405) is connected by the refrigerant exit end of the de-heavy reboiler (410) of pipeline；The bottom of weight-removing column tower reactor (405) is connected to heavy constituent products pot (407) also by pipeline；
Go into operation reboiler (210), isopropanol tower of described lightness-removing column reboiler (110), ethanol tower goes into operation reboiler (310) and weight-removing column reboiler (410) is the reboiler of additional heating agent；
Described equipment for after-treatment also includes some being arranged on pipeline for carrying liquid and/or making the pump of liquid supercharging and the valve of the flow velocity and the flow direction for controlling liquid。
2. equipment for after-treatment according to claim 1, it is characterised in that be additionally provided with light component cooler (112) between the remaining light component product tank of described lightness-removing column return tank (106)。
3. equipment for after-treatment according to claim 1, it is characterized in that, the pipeline connected between the heating agent port of export and the arrival end of ethanol tower return tank (206) of described first recuperation of heat reboiler (111) is provided with the first trim cooler (109)；The pipeline connected between the heating agent port of export and the arrival end of ethanol tower return tank (206) of described second recuperation of heat reboiler (211) is provided with the second trim cooler (209)；The pipeline connected between the heating agent port of export and the arrival end of isopropanol tower return tank (306) of described 3rd recuperation of heat reboiler (311) is provided with the 3rd trim cooler (309)。
4. according to the equipment for after-treatment one of claim 1-3 Suo Shu, it is characterised in that connect and the pipeline of ethanol tower the first charging aperture (201) and lightness-removing column tower reactor (105) is additionally provided with water trap。
5. equipment for after-treatment according to claim 5, it is characterised in that described water trap adopts molecular sieve adsorption dehydrater (501) and/or inorganic infiltrating and vaporizing membrane dehydrater (502)。
6. 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 in lightness-removing column (100) from lightness-removing column (100) middle part and carries out lightness-removing column rectification, set up the backflow of the gas phase portion of lightness-removing column rectification at lightness-removing column (100) tower top, the light composition impurity obtaining reaction is collected in distillate cooling；
Liquid phase part from lightness-removing column tower reactor (105) bottom extraction lightness-removing column rectification, send in ethanol tower (200) through ethanol tower (200) middle part and carry out ethanol tower rectification, gas phase portion from the ethanol tower rectification of ethanol tower (200) overhead extraction, after heat pump compresses, obtain ethanol tower heating agent gas, ethanol tower heating agent gas carries out heat exchange respectively through recuperation of heat reboiler with lightness-removing column tower reactor (105) and ethanol tower tower reactor (205), and set up the backflow entering ethanol tower, distillate cooling collection obtains alcohol product；
Liquid phase part from ethanol tower tower reactor (205) bottom extraction ethanol tower rectification, send into isopropanol tower (300) through isopropanol tower (300) middle part and carry out isopropanol tower rectification, gas phase portion from the isopropanol rectification of isopropanol tower (300) overhead extraction, after heat pump compresses, obtain isopropanol tower heating agent gas, isopropanol tower heating medium liquid carries out heat exchange cooling by recuperation of heat reboiler and isopropanol tower tower reactor (305), and set up the backflow entering isopropanol tower, distillate enters ethanol tower (200) through ethanol tower (200) middle part and again carries out ethanol tower rectification；
Liquid phase part from the isopropanol rectification of isopropanol tower tower reactor (305) bottom extraction, send into weight-removing column (400) through weight-removing column (400) middle part and carry out weight-removing column rectification, from the gas phase portion of weight-removing column (400) overhead extraction weight-removing column rectification and set up backflow, distillate cooling collection obtains isopropanol product；The liquid phase part of the weight-removing column rectification in interim acquisition weight-removing column tower reactor (405), namely obtains the heavy constituent impurity of reaction；
When post processing just starts, each tower tower reactor (105,205,305,405) respectively through reboiler (110,210,310,410) from the external world absorb heat；After last handling process is stable, weight-removing column tower reactor (405) absorbs heat still through weight-removing column reboiler (410)；Ethanol tower tower reactor (205) and isopropanol tower tower reactor (305) then change and are carried out heat exchange to absorb heat by respectively through the second recuperation of heat reboiler (211) and the 3rd recuperation of heat reboiler (311) with the heating agent gas after heat pump compresses；Lightness-removing column (100) then both absorbed heat by lightness-removing column reboiler (110) from the external world, carries out heat exchange further through the first recuperation of heat reboiler (111) with the ethanol tower heating agent gas through heat pump compression and absorbs heat。
7. post-processing approach according to claim 6, it is characterised in that the liquid phase part of described lightness-removing column rectification, from lightness-removing column tower reactor extraction, to entering between ethanol tower (200), also has a dehydration。
8. post-processing approach according to claim 7, it is characterized in that, described dehydration includes, and the liquid phase part of lightness-removing column rectification is first passed through molecular sieve and carries out pressure-variable adsorption dehydration, again passes by molecular sieve dehydration after the material after dehydration is carried out inorganic permeable membrane dehydration。
9. post-processing approach according to claim 6, it is characterised in that:
The number of plates of described lightness-removing column (100) is 95-110, and the reflux ratio of tower top is 30-60；The reacting liquid temperature entering lightness-removing column (100) 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, and pressure is 5-15kPa；The backflow temperature flowing back into lightness-removing column (100) 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 (105) extraction 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 described ethanol tower (200) is 140-160, and reflux ratio is 8-10；The gas phase portion temperature of ethanol tower (200) overhead extraction is 73-83 DEG C, and pressure is 0-5kPa；After heat pump compresses, the temperature of the ethanol tower heating agent gas obtained is 132-142 DEG C, and pressure is 150-250kPa；Before ethanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 75-85 DEG C, and pressure is 90-110kPa；The backflow temperature flowing back into ethanol tower (200) is 75-85 DEG C, and pressure is 400-500kPa；Distillate temperature is 40-50 DEG C, and pressure is 500-700kPa；The liquid phase part temperature of ethanol tower tower reactor (205) extraction is 80-90 DEG C, and pressure is 10-30kPa；
The number of plates of described isopropanol tower (300) is 140-160, and reflux ratio is 5-9；The gas phase portion temperature of isopropanol tower (300) overhead extraction is 100-110 DEG C, and pressure is 110-210kPa；After heat pump compresses, the temperature of the isopropanol tower heating agent gas obtained is 135-145 DEG C, and pressure is 300-500kPa；Before isopropanol tower heating agent gas starts backflow after recuperation of heat reboiler and cooler cool down, temperature is 108-118 DEG C, and pressure is 260-460kPa；The backflow temperature flowing back into isopropanol tower (300) is 108-118 DEG C, and pressure is 700-900kPa；The distillate temperature entering ethanol tower (200) is 108-118 DEG C, and pressure is 700-900kPa；The liquid phase part temperature of isopropanol tower tower reactor (305) extraction 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 described weight-removing column (400) is 70-85, and overhead reflux is than for 0.5-1；The gas phase portion temperature of weight-removing column (400) overhead extraction is 45-52 DEG C, and pressure is 750-850kPa；The backflow temperature flowing back into weight-removing column (400) 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 (405) extraction is 80-100 DEG C, and pressure is 750-850kPa。
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106955500A (en) * | 2017-04-05 | 2017-07-18 | 青岛科技大学 | A kind of three tower is thermally integrated the method and device of variable-pressure rectification purifying acetic acid isopropyl ester |
| CN107253901A (en) * | 2017-07-26 | 2017-10-17 | 四川天采科技有限责任公司 | A kind of separation of high-purity isopropanol and purification method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104402671A (en) * | 2014-12-11 | 2015-03-11 | 湖南瑞源石化股份有限公司 | Technology producing C3-C5 alkyl alcohol and co-producing alcohol by adding hydrogen in acetic acid C3-C5 alkyl ester |
| 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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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104402671A (en) * | 2014-12-11 | 2015-03-11 | 湖南瑞源石化股份有限公司 | Technology producing C3-C5 alkyl alcohol and co-producing alcohol by adding hydrogen in acetic acid C3-C5 alkyl ester |
| 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 |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106955500A (en) * | 2017-04-05 | 2017-07-18 | 青岛科技大学 | A kind of three tower is thermally integrated the method and device of variable-pressure rectification purifying acetic acid isopropyl ester |
| CN106955500B (en) * | 2017-04-05 | 2019-07-02 | 青岛科技大学 | A kind of three tower is thermally integrated the method and device of variable-pressure rectification purifying acetic acid isopropyl ester |
| CN107253901A (en) * | 2017-07-26 | 2017-10-17 | 四川天采科技有限责任公司 | A kind of separation of high-purity isopropanol and purification method |
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