CN209721997U

CN209721997U - From the energy saving technique device of low concentration fermentation liquid production alcohol fuel

Info

Publication number: CN209721997U
Application number: CN201920237176.7U
Authority: CN
Inventors: 蓝仁水; 黄贵明
Original assignee: Tianjin New Tianjin Technology And Development Co Ltd
Current assignee: Tianjin New Tianjin Technology And Development Co Ltd
Priority date: 2019-02-25
Filing date: 2019-02-25
Publication date: 2019-12-03
Anticipated expiration: 2029-02-25

Abstract

The utility model relates to a kind of energy saving technique devices more particularly to a kind of energy-saving process method and device for producing alcohol fuel by distillation process from industrial tail gas fermentation liquid from low concentration fermentation liquid production alcohol fuel.Entire ethanol refinery system includes at least four towers and the dewatering units such as first rectifying column, Second distillation column, third distillation column, the 4th rectifying column and other corollary equipments composition.It is thermally integrated between first rectifying column, four tower of Second distillation column, third distillation column and the 4th rectifying column, in addition other heat exchange, the application of power-saving technology significantly reduce operation energy consumption in system.The heat-exchange system of optimization makes dewatering unit organically be unified with distillation system, improves the stability and flexibility of entire distillation system.The utility model overcomes the shortcomings that prior art, and the more currently advanced alcohol fuel rectification technique of operation energy consumption reduces by 30% or more, has significant practicability and economic benefit, have a extensive future.

Description

From the energy saving technique device of low concentration fermentation liquid production alcohol fuel

Technical field

The utility model relates to a kind of energy saving technique devices more particularly to one from low concentration fermentation liquid production alcohol fuel Kind passes through the energy-saving process method and device that distillation process produces alcohol fuel from industrial tail gas fermentation liquid.

Background technique

The problems such as with the in short supply of the energy resources such as petroleum, coal, environmental pollution, greenhouse effects, gets worse, fuel Ethyl alcohol is as a kind of renewable energy, increasingly by the attention of various aspects.Traditional alcohol fuel mainly with cereal crops such as Sorghum, corn, pachyrhizus, cassava etc. are raw material, are obtained by biofermentation approach.It is that alcohol fuel is made in raw material with grain, no It is only expensive, there is also " strive grain with people, with grain strive ground " the phenomenon that.

Using industrial tail gas microbial fermentation technology, alcohol fuel, while the high egg of by-product are converted by steel and iron industry tail gas White feed and compressed natural gas have the characteristics that raw material is sufficient, concentration degree is high, are easy to collect, be produced into traditional fuel ethyl alcohol Originally it compares, overall cost is low, energy utilization rate is high, added value of product is high, it can be achieved that the resource for generating pollution to environment carries out Higher value application, remarkable in economical benefits.

Since industrial tail gas fermentation belongs to gaseous fermentation process, very low (general ethanol content is only for concentration of alcohol in fermentation liquid It is 2~4%.Unless otherwise specified, mass percent is referred both in the application text), it is far below traditional grain crop fermentation liquid second Determining alcohol (10~16%).At present from the process of fermentation liquid production alcohol fuel, three column distillation methods, this method are mostly used There are the higher disadvantages of production energy consumption.If industrial tail gas fermentation preparing fuel ethanol distillation process still uses common process method, must So cause distillation process energy consumption very high, by the serious economy for restricting industrial tail gas producing fuel ethyl alcohol by ferment technique.

Chinese patent CN200410094085.0 discloses a kind of " production of alcohol fuel ", and its essence is using single wine with dregs Tower, Dan Jingta add the original process method of molecular sieve, although process flow is simple, operation energy consumption is very high.

CN200710057523.X discloses a kind of " process of ethyl alcohol rectifying is carried out using three-tower heat integration device ": Entire ethyl alcohol distillation system includes three towers such as topping still, low pressure azeotropy rectification column, high pressure azeotropy rectification column, and topping still, low pressure are total It is thermally integrated between boiling rectifying column, three tower of high pressure azeotropy rectification column, topping still side line gas phase provides part for low pressure azeotropy rectification column Energy, high pressure azeotropy rectification column top gaseous phase provide energy for topping still tower reactor, and alcohol product is by low pressure azeotropy rectification column and height Pressure azeotropy rectification column produces respectively, and essence is still the double-effect rectification technique of single prefractionator, double smart towers, and operation energy consumption is high.

CN200710058736.4 discloses a kind of " fuel ethanol production equipment and method ", and its essence is using double prefractionators The tri-columns rectification process method of (thick tower, rectifying column lower part), double smart towers (rectifier, recovery tower top) plus molecular sieve, slightly It is thermally integrated operation between three tower, rectifying column and recovery tower towers, realizes triple effect technique, operation energy consumption is lower.

CN201010545523.6 disclose " the distillation dehydration device of a kind of alcohol fuel and general grade edible alcohol coproduction and Technique ", the process that similar CN200710058736.4 is provided, topping still, combined column are thermally integrated between three towers of rectifying column Operation, realizes triple effect technique, improvement part is: combined column top gaseous phase is divided into three after the boosting of ethanol vapor gas compressor Stock, one go topping still reboiler, one go methanol tower reboiler, another stock that adsorbing tower with molecular sieve is gone to be dehydrated, dewatered nothing Water-ethanol gas returns to rectification cell and heats to topping still tower reactor reboiler, the technique side that opposite CN200710058736.4 is provided Method further reduced operation energy consumption.The methanol column being arranged in CN201010545523.6 belongs to the general grade edible ethanol of coproduction Required equipment, but redundant equipment is belonged to for fuel alcohol plant.Methanol concentration is well below concentration of alcohol, rectifying in fermentation liquid Resulting azeotropic alcohol can meet GB 18350-2013 " fuel ethanol " standard without methanol removal after being dehydrated.Pressure The setting of contracting machine considerably increases CN201010545523.6 and provides the power consumption of process, and increases the (compression of dynamic equipment Machine) investment and maintenance cost.

CN201710542687.5 discloses " a kind of alcohol fuel energy-saving clean production method ", alcohol fuel rectifying Cheng Shizhi is consistent with CN200710058736.4, is all to use double prefractionators (thick tower, rectifying column lower part), double smart towers (on rectifying column Portion, recovery tower top) add the tri-columns rectification process method of molecular sieve, the difference is that being used for using dewatered dehydrated alcohol gas Fermentation liquid is preheated, this technique is identical as CN201010545523.6.CN201710542687.5 with CN201010545523.6 is the difference lies in that in the process that CN201710542687.5 is provided, " the of rectifying and dewatering unit The heating steam of one smart tower reboiler is live steam, and the steam condensation water of discharge send to the first smart tower tower reactor after collecting and directly heats Tower bottoms ", by this process, the first smart tower tower reactor reboiler can be omitted completely, directly introduce steam into the first smart tower tower Kettle can reach same effect using direct steam heating.The process that CN201710542687.5 is provided is opposite CN201010545523.6 without substantive breakthrough, and steam condensate be directly mixed in the first smart tower tower reactor waste water belong to it is very uneconomical Method.

Summary of the invention

The purpose of this utility model is to provide it is a kind of from low concentration fermentation liquid production alcohol fuel energy saving technique device, The energy-saving process method and device for producing alcohol fuel by distillation process especially from industrial tail gas fermentation liquid, can overcome The shortcomings that prior art.The utility model is adopted breakthroughly on the Process ba- sis of currently used three towers ethanol refinery system It is thermally integrated process with four tower rectifying, quadruple effect, greatly reduces operation energy consumption.Process provided by the utility model has Significant practicability and economic benefit.

It is provided by the utility model from low concentration fermentation liquid production alcohol fuel energy-saving process method include:

1) first rectifying column, Second distillation column, third distillation column and the 4th rectifying column are included at least；

2) first rectifying column described in is combination tower, and first rectifying column top is the first rectifying section, and middle part is to take off light section, under Portion is the first thick tower；

3) Second distillation column described in is stripper, and the following are the second thick towers for charging；

4) third distillation column described in is stripper, and the following are the thick towers of third for charging；

5) the 4th rectifying column described in is combination tower, and the 4th rectifier is the second rectifying section, and middle part is adopted for fusel oil Section out, lower part are dewatering period；

6) first rectifying column, Second distillation column, third distillation column described in and between the 4th rectifying column to be thermally integrated, the 4th Rectifying tower top gaseous phase provides institute's calorific requirement as third distillation column tower reactor heat source, for third distillation column；Third distillation column Top gaseous phase provides institute's calorific requirement as Second distillation column tower reactor heat source, for Second distillation column；Second distillation column tower overhead gas It is mutually used as first rectifying column tower reactor heat source, provides institute's calorific requirement for first rectifying column；

7) it goes dewatering unit gas phase first choice from the 4th rectifying tower top gaseous phase, is also possible to the evaporation of azeotropic alcohol liquid phase Gas phase is also possible to other rectifying tower top gaseous phases in distillation system；

8) the dehydrated alcohol gas phase first choice of dewatering unit output is used as third distillation column tower reactor heat source, it is also possible to do Two tower bottom of rectifying tower heat sources, it is also possible to do first rectifying column tower reactor heat source, it can also be used to fermentation liquid is preheated, it can also For preheating first rectifying column charging, it can also be used to preheat Second distillation column charging, it can also be used to third distillation column charging is preheated, It can also be used for preheating the 4th rectifying column charging；Aforementioned dehydrated alcohol vapor condensation object be process of alcohol products (or alcohol produce Product).

By process provided by the utility model, dewatering unit is molecular sieve water separation tower or infiltrating and vaporizing membrane.Described The light wine first choice of dewatering unit discharge enters first rectifying column, or is fed into the 4th rectifying column, Second distillation column or third essence Evaporate tower.

By process provided by the utility model, when it is not necessary that when producing alcohol fuel, the dewatering unit can stop With by first rectifying column top or side take-off partially azeotropic alcohol, by the 4th the top of the distillation column or upper aqueous phase side take-off Partially azeotropic alcohol；Or the azeotropic alcohol of first rectifying column extraction enters the 4th rectifier column reflux tank or tower top, alcohol product All by the 4th the top of the distillation column or upper aqueous phase side take-off；Or the 4th rectifying column extraction azeotropic alcohol enter first essence Tower return tank or tower top are evaporated, alcohol product is all by first rectifying column tower top or upper aqueous phase side take-off.Realize alcohol fuel Coproduction with azeotropic alcohol product operates.

By process provided by the utility model, fermentation liquid first choice is introduced into the first rectifying column；Second essence The charging for evaporating tower feeds following liquid phase lateral line discharging from first rectifying column；The charging of third distillation column from first rectifying column into Expect following liquid phase lateral line discharging or feeds following liquid phase lateral line discharging from Second distillation column；Fermentation liquid can also be divided into three Stock, goes first rectifying column, Second distillation column and third distillation column respectively；Fermentation liquid can also be introduced into Second distillation column, the The charging of one rectifying column feeds following liquid phase lateral line discharging from Second distillation column, and the charging of third distillation column comes from the first rectifying Tower feeds following liquid phase lateral line discharging or feeds following liquid phase lateral line discharging from Second distillation column；Fermentation liquid can also be advanced Enter third distillation column, the charging of Second distillation column feeds following liquid phase lateral line discharging from third distillation column, first rectifying column Charging feeds following liquid phase lateral line discharging from third distillation column or feeds following liquid phase lateral line discharging from Second distillation column；The The charging of four rectifying columns is that the above liquid phase lateral line discharging, Second distillation column top distillate or its charging are fed from first rectifying column The above liquid phase lateral line discharging, third distillation column overhead or its mixed material for feeding the above liquid phase lateral line discharging.Before pressing Method is stated, it can be by Second distillation column top distillate or its above liquid phase lateral line discharging of charging, third distillation column overhead Or it feeds the above liquid phase lateral line discharging and introduces the above position of first rectifying column charging respectively or all.

By process provided by the utility model, there are three section containing wine with dregs --- the first rectifying in entire rectifier unit system The lower part of tower, the lower part of Second distillation column and third distillation column lower part；First rectifying column, Second distillation column and third distillation column Tower reactor discharges waste water containing wine with dregs respectively；The discharge of 4th tower bottom of rectifying tower is free of wine with dregs waste water；The first rectifying column can be stripping Tower, without top fractionation stage；Second distillation column can be combination tower, and rectifying section is arranged in top；Third distillation column can be combination tower, Rectifying section is arranged in top.

By process provided by the utility model, the third distillation column can be deactivated, the 4th rectifying tower top gaseous It is mutually used as Second distillation column tower reactor heat source, provides institute's calorific requirement for Second distillation column.

By process provided by the utility model, can also increase between the third distillation column and the 4th rectifying column Add the 5th rectifying column, the 5th rectifying column and the first rectifying column, Second distillation column, third distillation column and the 4th rectifying Tower forms five effects and is thermally integrated operation, further decreases operation energy consumption.4th rectifying tower top gaseous phase is as the 5th tower bottom of rectifying tower Heat source provides institute's calorific requirement for the 5th rectifying column；5th rectifying tower top gaseous phase heats heat as third distillation column tower reactor Source provides institute's calorific requirement for third distillation column；Third distillation column top gaseous phase is the as Second distillation column tower reactor heat source Two rectifying columns provide institute's calorific requirement；Second distillation column top gaseous phase is the first rectifying as first rectifying column tower reactor heat source Tower provides institute's calorific requirement.The dehydrated alcohol gas phase first choice of dewatering unit output is used as the 5th tower bottom of rectifying tower heat source, can also It is used as third distillation column tower reactor heat source, it is also possible to do Second distillation column tower reactor heat source, it is also possible to do first rectifying column Tower reactor heat source.It, can be by Second distillation column top distillate or its above liquid phase lateral line discharging of charging, third by preceding method The top of the distillation column distillate or its above liquid phase lateral line discharging of charging, the 5th the top of the distillation column distillate or its charging are with liquid phase Lateral line discharging introduces first rectifying column respectively or all and feeds the above position.

By process provided by the utility model, azeotropic alcohol product first choice is by the top of first rectifying column or upper part side At the top of line and the 4th rectifying column or upper part side line obtains respectively；Fusel oil is by liquid phase side take-off in the middle part of the 4th rectifying column； First rectifying column, Second distillation column, third distillation column, the 5th rectifying column and the 4th rectifying column be all compound tower structure, Rectifying section is all arranged in each tower top.

By process provided by the utility model, (charging above and below) is set near the 4th rectifying column feed entrance point It sets several fusel oil extraction mouths and selects suitable fusel oil to produce mouth according to the operating conditions of input concentration and the 4th rectifying column Fusel oil is discharged.

By process provided by the utility model, the process of alcohol products (or alcohol product or steam condensate) The azeotropic alcohol preheating that can be produced to first rectifying column, the light wine that can be discharged to dewatering unit preheat, can give karusen Liquid preheating, can to first rectifying column feeding preheating, can to Second distillation column feeding preheating, can be fed to third distillation column Preheating can give the 4th rectifying column feeding preheating, recycle wherein heat, reduce cooling-water consumption.

By process provided by the utility model, being thermally integrated between the 4th rectifying column and third distillation column is changed The heat being thermally integrated between heat exchanger, third distillation column and Second distillation column between hot device, the 4th rectifying column and the 5th rectifying column The dehydrated alcohol gas for being thermally integrated heat exchanger, dewatering unit output between integrated heat exchanger, Second distillation column and first rectifying column Phase condenser can using falling-film reboiler, pump forced circulation heat exchanger, the steam generator of indirect heat exchange, plate heat exchanger, Thermosyphon reboiler.By process provided by the utility model, the 4th rectifying column only described in fermentation liquid rectifier unit Tower reactor reboiler need to introduce external heat source heating, other each reboilers, the equal utilisation system internal heat of heat exchanger institute calorific requirement. The heat medium of the 4th tower bottom of rectifying tower reboiler can be steam, conduction oil either heating furnace.It is thermally integrated heat exchange The pattern of device, be only using which kind of heat medium process provided by the utility model implementation detail, do not constitute to this reality It is that can be freely combined completely or changing using other patterns for a person skilled in the art with any restrictions of novel spirit Hot device realizes this technology.

Process provided by the utility model is a kind of energy saving technique side from low concentration fermentation liquid production alcohol fuel Method and device, it is especially a kind of from industrial tail gas fermentation liquid by distillation process produce alcohol fuel energy-saving process method and Device can be also used for the rectifying and dehydration of the aqueous solution that other can form low-boiling azeotrope with water.It is described can be with Water formed the typical substance of low-boiling azeotrope include but is not limited to isopropanol, normal propyl alcohol, sec-butyl alcohol, the tert-butyl alcohol, tetrahydrofuran, Methyl acetate, ethyl acetate, pyridine, acetonitrile etc..

By process provided by the utility model, each tower typical operation conditions are as follows:

First rectifying column tower top operating pressure range is 8~90kpa；

Second distillation column tower top operating pressure range is 20~280kpa；

Third distillation column tower top operating pressure range is 70~500kpa；

4th the top of the distillation column operating pressure range is 100~1280kpa；

Dewatering unit operating pressure range is 100~1280kpa.

Unless otherwise specified, all pressure refer both to absolute pressure in the utility model.

By process provided by the utility model, each tower preferred operations condition are as follows:

First rectifying column tower top operating pressure be 30kpa, 50 DEG C of tower top, 78 DEG C of tower reactor；

Second distillation column tower top operating pressure be 100kpa, 97 DEG C of tower top, 103 DEG C of tower reactor；

Third distillation column tower top operating pressure be 180kpa, 114 DEG C of tower top, 119 DEG C of tower reactor；

4th rectifying tower tower top operating pressure be 590kpa, 130 DEG C of tower top, 159 DEG C of tower reactor；

Dewatering unit (gas-phase dehydration membrane module) operating pressure is 590kpa.

Industrial tail gas fermentation belongs to gaseous fermentation process, and concentration of alcohol is very low in fermentation liquid (being typically only 2~4%), such as The energy consumption control of this low-concentration industrial tail gas fermentation liquid distillation process belongs to typical mash alcohol stripping control separation process. Double prefractionators of CN201710542687.5 offer, double smart towers add the tri-columns rectification process method of molecular sieve to be current cereal crops hair This rectification technique is such as used for industrial tail gas fermentation by the rectification technique that ferment production alcohol fuel industry generallys use Liquid distillation process, operation energy consumption are very high.By taking industrial tail gas fermentation liquid concentration of alcohol 3% as an example, mentioned by CN201710542687.5 The tri-columns rectification process method of confession, the steam consumption of alcohol fuel per ton are up to 3.0 tons of steam.

By process provided by the utility model, the first thick tower, the Second distillation column of the first rectifying column lower part The thick tower of the second of lower part, third distillation column lower part the thick tower of third form the triple effect of low concentration fermentation liquid, be thermally integrated stripping behaviour Make；First thick tower of the first rectifying column lower part, the second thick tower of Second distillation column lower part, third distillation column lower part Three thick towers, the 5th rectifying column lower part the 5th thick tower form the quadruple effect of low concentration fermentation liquid, be thermally integrated stripping operation；Effective gram The defect for having taken the prior art (double prefractionators, mash economic benefits and social benefits stripping operation) significantly reduces the production combustion of industrial tail gas fermentation liquid Expect the operation energy consumption of ethyl alcohol.

Using process provided by the utility model, as shown in 1~attached drawing of attached drawing 6, by conventional double prefractionators (double wine with dregs Tower, mash economic benefits and social benefits stripping operation) three prefractionators are improved to, it realizes the triple effect of mash, be thermally integrated stripping operation, operation energy consumption is only 2.0 tons of steam/ton process of alcohol products, operation energy consumption substantially reduce.

Using process provided by the utility model, as shown in Fig. 8, by conventional double prefractionators, (double prefractionators, mash are double Effect stripping operation) four prefractionators are improved to, it realizes the quadruple effect of mash, be thermally integrated stripping operation, operation energy consumption is only 1.8 tons of steamings Vapour/ton process of alcohol products, operation energy consumption greatly reduce.

The utility model relates to a kind of energy-saving process methods and device from low concentration fermentation liquid production alcohol fuel, especially It is related to a kind of energy-saving process method and device for producing alcohol fuel by distillation process from industrial tail gas fermentation liquid.Entire wine Smart distillation system includes at least four towers and the dewatering units such as first rectifying column, Second distillation column, third distillation column, the 4th rectifying column And other corollary equipments composition.Heat collection between first rectifying column, four tower of Second distillation column, third distillation column and the 4th rectifying column At in addition other heat exchange, the application of power-saving technology significantly reduce operation energy consumption in system.The heat-exchange system of optimization makes to take off Water unit is organically unified with distillation system, improves the stability and flexibility of entire distillation system.This is practical new Type overcomes the shortcomings that prior art, and the more currently advanced alcohol fuel rectification technique of operation energy consumption reduces by 30% or more, With highly significant practicability and economic benefit, have a extensive future.

Detailed description of the invention

Fig. 1 is provided by the utility model a kind of typically from the energy saving technique side of low concentration fermentation liquid production alcohol fuel Method flow chart；Dewatering unit uses gas-phase dehydration membrane module.

Fig. 2 is a kind of differentiation process of Fig. 1, and the 4th the top of the distillation column shown in FIG. 1 does not produce azeotropic alcohol gas phase Remove dewatering unit；The liquid phase azeotropic alcohol of the liquid phase azeotropic alcohol of first rectifying column overhead extraction and the extraction of the 4th the top of the distillation column Together into evaporator E144, the alcohol gas phase after vaporization removes dewatering unit.

Fig. 3 is a kind of differentiation process of Fig. 2, a part of liquid of first rectifying column tower shown in Fig. 2 top side take-off Phase azeotropic alcohol goes to the 4th the top of the distillation column, and final whole azeotropic alcohol is from the 4th rectifier liquid phase side take-off, then Into evaporator E144, the alcohol gas phase after vaporization removes dewatering unit.

Fig. 4 is a kind of differentiation process of Fig. 1, the dehydrated alcohol gas phase of dewatering unit output shown in FIG. 1 be changed to Second distillation column the second reboiler E123 heating；Dewatering unit adsorbs/regenerates handover operation dehydration using molecular sieve.

Fig. 5 is a kind of differentiation process of Fig. 1, when switching produces azeotropic alcohol, deactivates dewatering unit, the first rectifying Column overhead produces liquid phase and the 4th the top of the distillation column extraction liquid phase together as azeotropic alcohol product.

Fig. 6 is a kind of differentiation process of Fig. 5, when switching produces azeotropic alcohol, first rectifying column tower top side line It produces a part of azeotropic alcohol and goes to the 4th the top of the distillation column, final whole azeotropic alcohol is adopted from the 4th rectifier liquid phase side line Out.

Fig. 7 is a kind of differentiation process of Fig. 1, is simplified to the process of Fig. 1, third rectifying is omitted Tower, the 4th rectifying tower top gaseous phase a part are heated to Second distillation column reboiler E122, and another part removes dewatering unit.Through de- The dewatered dehydrated alcohol gas phase of water unit is heated to Second distillation column the second reboiler E123.

Fig. 8 is a kind of differentiation process of Fig. 1, further energy saving optimizing has been carried out to the process of Fig. 1, in third The 5th rectifying column is increased between rectifying column and the 4th rectifying column.4th rectifying tower top gaseous phase a part gives the 5th rectifying column again Device E162 heating is boiled, another part removes dewatering unit；Through the dewatered dehydrated alcohol gas phase of dewatering unit to the 5th rectifying column the Two reboiler E163 heating；5th rectifying tower top gaseous phase is heated to third distillation column reboiler E132.

Specific embodiment

The specific embodiment of the utility model be explained in detail with reference to the accompanying drawings it is as follows, but for illustrative purposes only rather than limit this reality With novel.

Unless otherwise specified, composition, the structure of the process equipments such as specifically used tower part, material are not specified in embodiment (connecting pipeline etc. for being connected between each tower part), reagent etc., are commercially available or the ordinary skill of this field Personnel are obtained with well known method.Related specific experiment method, operating condition, usually according to common process condition and hand Condition described in volume, or according to the normal condition proposed by manufacturer.

As Figure 1-Figure 8, the utility model provides a kind of energy conservation dress from low concentration fermentation liquid production alcohol fuel It sets:

Including at least first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column T140 Four towers and connecting pipeline.

The feeding line is connect with the condenser E111 tube-side inlet of first rectifying column T110, E111 tube side outlet with The feed preheater E113 cold side import of first rectifying column T110 connects, and E113 cold side outlet port is connected to first rectifying column T110's Middle part.The top gaseous phase outlet of first rectifying column T110 and the condenser E111 shell side gas phase entrance of first rectifying column T110 connect It connects, the condenser E111 shell side gaseous phase outlet of first rectifying column T110 and the tail cooler E112 shell side gas phase of first rectifying column T110 Entrance connection, the tail cooler E112 shell side gaseous phase outlet of first rectifying column T110 are connected to vacuum system.First rectifying column T110 Condenser E111 and the condensate outlet pipeline of tail cooler E112 of first rectifying column T110 be divided into two, one is connected to first The overhead reflux mouth of rectifying column T110, another be connected to the 4th rectifying column T140 overhead reflux mouth.E112 condensate outlet pipeline It is additionally coupled to industrial alcohol extraction pipeline.The tower reactor of first rectifying column T110 respectively with the reboiler E114 of first rectifying column T110 Tube-side inlet is connected with the feed preheater E113 hot side import of first rectifying column T110.The feeding preheating of first rectifying column T110 Device E113 hot side outlet is connected with useless wine with dregs discharge pipe.The reboiler tube side outlet of first rectifying column T110 is connected to the first rectifying The tower reactor of tower T110.

First rectifying column T110 feeds the above liquid phase side line outlet and is connected to the 4th the first feed preheater of rectifying column T140 E141 cold side input port, first rectifying column T110 feed following liquid phase side line outlet and are connected to Second distillation column T120 feed preheater E121 cold side input port.

Second distillation column T120 feed preheater cold side outlet port is divided into two, and one is connected to Second distillation column T120 charging Mouthful, another is connected to third distillation column T130 feed preheater E131 cold side input port.Second distillation column T120 top gaseous phase goes out Mouth is connect with first rectifying column T110 reboiler E114 shell side gas phase entrance, first rectifying column T110 reboiler E114 shell side lime set Outlet is connected to the 4th rectifying column T140 the first feed preheater E141 cold side input port.Second distillation column T120 tower reactor is respectively with Two rectifying column T120 reboiler E122 tube-side inlets are connected with Second distillation column T120 feed preheater E121 hot side import.Second Rectifying column T120 feed preheater hot side outlet is connected to first rectifying column T110 feed preheater E113 hot side import.Second essence It evaporates the outlet of tower T120 reboiler tube side and is connected to Second distillation column T120 tower reactor.

Third distillation column T130 feed preheater E131 cold side outlet port is connected to third distillation column T130 feed inlet.Third essence It evaporates the outlet of tower T130 top gaseous phase to connect with Second distillation column T120 reboiler E122 shell side gas phase entrance, Second distillation column T120 Reboiler E122 shell side condensate outlet is connected to the 4th rectifying column T140 the first feed preheater E141 cold side input port.Third rectifying Tower T130 tower reactor respectively with third distillation column T130 the first reboiler E132 tube-side inlet, the second reboiler of third distillation column T130 E133 tube-side inlet is connected with third distillation column T130 feed preheater E131 hot side import.Third distillation column T130 feeding preheating Device hot side outlet is connected to Second distillation column T120 feed preheater E121 hot side import.The first reboiler of third distillation column T130 The outlet of E132 tube side and the outlet of the second reboiler of third distillation column T130 E133 tube side are connected to third distillation column T130 tower reactor.

4th rectifying column T140 the first feed preheater E141 cold side outlet port and the 4th the second feeding preheating of rectifying column T140 Device E142 cold side input port is connected, the 4th rectifying column T140 the second feed preheater E142 cold side outlet port and the 4th rectifying column T140 into Material mouth is connected.4th rectifying column T140 top gaseous phase outlet respectively with third distillation column T130 the first reboiler E132 shell side gas phase Entrance, dewatering unit gas phase import are connected.Third distillation column T130 the first reboiler E132 shell side condensate outlet pipeline is connected to 4th rectifying column T140 overhead reflux mouth.

The dehydrated alcohol vapor delivery line of dewatering unit output is connected to third distillation column T130 the second reboiler E133 shell side Gas phase entrance, the second reboiler of third distillation column T130 E133 shell side condensate outlet are connected with process of alcohol products extraction pipeline. The light wine pipeline of dewatering unit discharge is connected to first rectifying column T110 and feeds the above light wine feed inlet.

Several fusel oil extraction mouths are respectively set in 4th rectifying column T140 feed entrance point above and below, and fusel oil produces mouth It is connect respectively with fusel oil extraction pipeline.

4th rectifying column T140 tower reactor respectively with the 4th rectifying tower reboiler E143 tube-side inlet and the 4th rectifying column T140 First feed preheater E141 hot side import is connected.4th rectifying column T140 the first feed preheater E141 hot side outlet and waste water Discharge pipe connection.The outlet of 4th rectifying column T140 reboiler E143 tube side is connected to the 4th tower bottom of rectifying tower.Heat steam pipe Line is connected to the 4th rectifying column T140 reboiler E143 shell side gas phase entrance, the 4th rectifying column T140 reboiler E143 shell side lime set Outlet is connected to the 4th rectifying column T140 the second feed preheater E142 hot side import.4th the second feeding preheating of rectifying column T140 Device E142 hot side outlet is connected with heating vapour-condensing liquid discharge pipe.

A kind of energy-saving process method from low concentration fermentation liquid production alcohol fuel provided by the utility model includes as follows Step:

1) first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column are included at least T140；

2) the first rectifying column T110 described in is combination tower, and first rectifying column top is the first rectifying section S1101, and middle part is Take off light section S1102), lower part is the first thick tower S1103；

3) the Second distillation column T120 described in is stripper, and the following are the second thick tower S1203 for charging；

4) the third distillation column T130 described in) it is stripper, the following are the thick tower S1303 of third for charging；

5) the 4th rectifying column T140 described in is combination tower, and the 4th rectifier is the second rectifying section S1401, and middle part is Fusel oil produces section S1402, and lower part is dewatering period S1403；

6) first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column T140 described in Between to be thermally integrated, the 4th rectifying column T140 top gaseous phase is used as third distillation column T130 tower reactor heat source, for third rectifying Tower T130 provides institute's calorific requirement；Third distillation column T130 top gaseous phase is the as Second distillation column T120 tower reactor heat source Two rectifying column T120 provide institute's calorific requirement；Second distillation column T120 top gaseous phase heats heat as first rectifying column T110 tower reactor Source provides institute's calorific requirement for first rectifying column T110；

7) there are three sections containing wine with dregs in entire rectifier unit system --- under first rectifying column lower part S1103, Second distillation column Portion S1203 and third distillation column lower part S1303；First rectifying column T110, Second distillation column T120 and third distillation column T130 tower Kettle discharges waste water containing wine with dregs respectively；The discharge of 4th rectifying column T140 tower reactor is free of wine with dregs waste water.

8) azeotropic alcohol product is by the top first rectifying column T110 or upper part side line and the 4th rectifying T140 top of tower Or upper part side line obtains respectively；Fusel oil is by liquid phase side take-off in the middle part of the 4th rectifying column T140；

9) the evaporation gas phase of the 4th rectifying column T140 top gaseous phase or azeotropic alcohol liquid phase removes dewatering unit；

10) the dehydrated alcohol gas phase first choice of dewatering unit output is used as third distillation column T130 tower reactor heat source, can also It is used as Second distillation column T120 tower reactor heat source, it is also possible to do first rectifying column T110 tower reactor heat source, it can also be used to pre- Hot fermentation mash, it can also be used to preheat first rectifying column T110 charging, it can also be used to Second distillation column T120 charging is preheated, it can also For preheating third distillation column T130 charging, it can also be used to preheat the 4th rectifying column T140 charging.

Aforementioned dehydrated alcohol vapor condensation object is process of alcohol products.

By process provided by the utility model, comprise the concrete steps that:

The advanced first rectifying column condenser E111 tube side of industrial tail gas fermentation liquid 101, by first rectifying column T110 tower top Logistics 102 is into first rectifying column T110 feed preheater E113 cold side input port after gas phase 104 preheats, by first rectifying column T110 tower Kettle is discharged the logistics 103 after useless mash 111 preheats and enters the top for taking off light section S1102 in the middle part of first rectifying column T110.First essence It evaporates tower T110 top gaseous phase 104 and enters first rectifying column T110 condenser E111 shell side, E111 does not coagulate gas phase 105 into the first rectifying Tower T110 tail cooler E112 shell side, E112 shell-side outlet fixed gas 106 go vacuum system.First rectifying column T110 condenser E111 It is two strands that shell side lime set and the mixed logistics 108 of first rectifying column T110 tail cooler E112 shell side lime set, which are divided to, one 109 reflux To first rectifying column T110 tower top, another stock 110 enters the 4th rectifying column T140 tower top.First rectifying column T110 tail cooler E112 There are also one 107 conduct industrial alcohol to produce for shell side lime set.Useless mash 111 is discharged through the first rectifying in first rectifying column T110 tower reactor Rectifier unit is discharged in logistics 112 after tower T110 feed preheater E113 and logistics 102 exchange heat.

First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102 Stream 113.First rectifying column T110 charging is following, takes off extraction liquid phase side-stream between the thick tower S1103 of light section S1102 and first 114.Logistics 114 is after the useless heat exchange of mash 205 is discharged in Second distillation column feed preheater E121 and Second distillation column T120 tower reactor Logistics 115 to be divided to be two strands, first burst of logistics 201 enters Second distillation column T120；Second burst of logistics 202 through third distillation column into T130 expects that preheater E131 and third distillation column T130 tower reactor are discharged useless mash 304 and exchange heat, and the logistics 301 after heat exchange enters third Rectifying column T130.

Second distillation column T120 and first rectifying column T110 are thermally integrated operation, Second distillation column T120 top gaseous phase 203 into First rectifying column T110 reboiler E114 shell side provides separation institute's calorific requirement for first rectifying column T110.

Third distillation column T130 and Second distillation column T120 are thermally integrated operation, third distillation column T130 top gaseous phase 302 into Second distillation column reboiler E122 shell side provides separation institute's calorific requirement for Second distillation column T120.

4th rectifying column T140 and third distillation column T130 are thermally integrated operation, the 4th rectifying column T140 tower top one gas phase 404 provide separation required partial heat into third distillation column T130 the first reboiler E132 shell side, to third distillation column T130；The Four another burst of gas phases of rectifying column T140 tower top, 405 air inlet phase dehydration membrane module M150, dewatered dehydrated alcohol gas phase 407 is into Three rectifying column T130 the second reboiler E133 shell sides provide separation required another part heat for third distillation column T130.Heating Steam 430 enters the 4th rectifying column T140 reboiler E143 shell side.

First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102 Stream 113, first rectifying column reboiler E114 shell side lime set 204 and Second distillation column T120 reboiler E122 shell side lime set 303 are mixed It closes, logistics 401 is discharged useless through the 4th rectifying column T140 the first feed preheater E141 and the 4th rectifying column T140 tower reactor after mixing Water 411 exchanges heat, and the logistics 402 after heat exchange is again into the 4th rectifying column T140 the second feed preheater E142, with the 4th rectifying column T140 reboiler E143 shell side steam condensate 431 exchanges heat, and the logistics 403 after heat exchange enters the 4th lower part rectifying column T140 dewatering period The top of S1403.

First rectifying column T110 condenser E111 shell side lime set and first rectifying column T110 tail cooler E112 shell side lime set are mixed One lime set 110 and the mixed logistics 413 of the first reboiler of third distillation column T130 E132 shell side lime set 406 after conjunction enter 4th rectifying column T140 tower top.

Useless mash 304 is discharged after third distillation column T130 feed preheater E131 heat exchange in third distillation column T130 tower reactor Logistics 305 enters Second distillation column T120 feed preheater E121 hot side, Second distillation column T120 feed preheater E121 hot side Outlet streams 206 enter first rectifying column T110 feed preheater E113 hot side.

The light wine 409 that gas-phase dehydration membrane module M150 is generated enters the first rectifying section S1101 of first rectifying column T110

Third distillation column T130 the second reboiler E133 shell side lime set 408 is process of alcohol products.

Fusel oil extraction section S1402 produces fusel oil 410 in the middle part of 4th rectifying column T140.

The discharge of 4th rectifying column T140 the first feed preheater E141 hot side outlet is free of wine with dregs waste water 412.

4th rectifying column T140 the second feed preheater E142 hot side outlet discharges steam condensate 432.

By process provided by the utility model, typical raw material composition are as follows:

Above-mentioned raw materials compositing range does not constitute any limitation to the utility model, and the utility model can be used for various compositions Alcohol fuel fermentation liquid separation.

Embodiment 1:

As shown in Figure 1, the advanced first rectifying column T110 condenser E111 tube side of industrial tail gas fermentation liquid 101, Logistics 102 enters into the cold side first rectifying column T110 feed preheater E113 after being preheated by first rectifying column T110 top gaseous phase 104 Mouthful, the logistics 103 after the preheating of mash 111 of being given up by the discharge of first rectifying column T110 tower reactor, which enters in the middle part of first rectifying column T110, to be taken off gently The top of section S1102.First rectifying column T110 top gaseous phase 104 enters first rectifying column T110 condenser E111 shell side, E111 For not solidifying gas phase 105 into first rectifying column T110 tail cooler E112 shell side, E112 shell-side outlet fixed gas 106 goes vacuum system.The One rectifying column T110 condenser E111 shell side lime set and the mixed logistics of first rectifying column T110 tail cooler E112 shell side lime set 108 points are two strands, one 109 infinite reflux to first rectifying column T110 tower top, another stock 110 enters the 4th rectifying column T140 tower Top.There are also one 107 conduct industrial alcohol to produce for first rectifying column T110 tail cooler E112 shell side lime set.First rectifying column T110 Tower reactor is discharged logistics 112 of the useless mash 111 after first rectifying column T110 feed preheater E113 and logistics 102 exchange heat and essence is discharged Distillation unit.

First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102 Stream 113.First rectifying column T110 charging is following, takes off extraction liquid phase side-stream between the thick tower S1103 of light section S1102 and first 114.Logistics 114 is discharged useless mash 205 with Second distillation column T120 tower reactor through Second distillation column T120 feed preheater E121 and changes It is two strands that logistics 115 after heat, which is divided to, and first burst of logistics 201 enters Second distillation column T120, and second burst of logistics 202 is through third rectifying Tower T130 feed preheater E131 and third distillation column T130 tower reactor are discharged useless mash 304 and exchange heat, and the logistics 301 after heat exchange enters Third distillation column T130.

Third distillation column T130 and Second distillation column T120 are thermally integrated operation, third distillation column T130 top gaseous phase 302 into Second distillation column T120 reboiler E122 shell side provides separation institute's calorific requirement for Second distillation column T12.

First rectifying column T110 feeds above, the first rectifying section S1101 and takes off extraction liquid phase side line object between light section S1102 Stream 113, first rectifying column T110 reboiler E114 shell side lime set 204 and Second distillation column reboiler E122 shell side lime set 303 are mixed It closes, logistics 401 is discharged useless through the 4th rectifying column T140 the first feed preheater E141 and the 4th rectifying column T140 tower reactor after mixing Water 411 exchanges heat, and the logistics 402 after heat exchange is again into the 4th rectifying column T140 the second feed preheater E142, with the 4th rectifying column T140 reboiler E143 shell side steam condensate 431 exchanges heat, and the logistics 403 after heat exchange enters the 4th lower part rectifying column T140 dewatering period The top of S1403.

Following present a kind of typical operation conditions of each tower in embodiment 1, typical operation conditions and operation energy consumption are as follows:

First rectifying column T110 tower top operating pressure be 30kpa, 50 DEG C of tower top, 78 DEG C of tower reactor；

Second distillation column T120 tower top operating pressure be 100kpa, 97 DEG C of tower top, 103 DEG C of tower reactor；

Third distillation column T130 tower top operating pressure be 180kpa, 114 DEG C of tower top, 119 DEG C of tower reactor；

4th rectifying column T140 column overhead operating pressure be 590kpa, 130 DEG C of tower top, 159 DEG C of tower reactor；

By the process that the utility model Fig. 1 is provided, by conventional double prefractionators (double prefractionators, mash economic benefits and social benefits stripping operation) Be improved to three prefractionators --- the thick tower S1103 of the first of the lower part first rectifying column T110, the lower part Second distillation column T120 second Thick tower S1203, the lower part third distillation column T130 the thick tower S1303 of third, realize the triple effect of mash, be thermally integrated stripping operation.It is whole A distillation system first rectifying column T110, Second distillation column T120, third distillation column T130 and the 4th rectifying column T140 form four Effect is thermally integrated operation, and the 4th rectifying T140 column overhead gas phase heats heat as third distillation column T130 tower reactor the first reboiler E132 Source provides a part of heat for third distillation column T130, and the dehydrated alcohol gas phase of dewatering unit output is as third distillation column T130 tower reactor the second reboiler E133 heat source, provides another part heat for third distillation column T130；Third distillation column T130 top gaseous phase provides institute's calorific requirement as Second distillation column T120 tower reactor heat source, for Second distillation column T120；Second Rectifying column T120 top gaseous phase provides required heat as first rectifying column T110 tower reactor heat source for first rectifying column T110 Amount.Only the 4th rectifying column T140 tower bottom reboiler E143 needs middle pressure steam to heat to entire distillation system, and operation energy consumption is only 2.0 Ton steam/ton process of alcohol products, operation energy consumption substantially reduce.

By 200,000 tons/year of fuel alcohol plants, 8000 hour/year of operation hour, middle pressure steam consumption is 50 ton/hours. Other each reboilers, the equal utilisation system internal heat of heat exchanger institute calorific requirement.

Add the tri-columns rectification process side of molecular sieve by double prefractionators of Chinese patent CN201710542687.5 offer, double smart towers Method, distillation system operation energy consumption are 3.0 tons of steam/ton alcohol fuel.By 200,000 tons/year of fuel alcohol plants, operation hours 8000 hours/year, middle pressure steam consumption are 75 ton/hours.

(3.0-2.0)/3.0 ≈ 33%

Double prefractionators of opposite Chinese patent CN201710542687.5 offer, double smart towers add the tri-columns rectification process of molecular sieve Method, the process energy consumption that the utility model Fig. 1 is provided reduce about 33%.

75-50=25 ton/hours of steam can be saved per hour.

25 ton/hours × 8000 hour/year=200000 ton/year of middle pressure steam can be saved every year.

It is calculated by 150 yuan of steam per ton, steam expense can be saved every year:

200000 tons/year × 150 yuan/ton ten thousand yuan/year of ÷ 10000=3000.

A kind of energy-saving process method and device from low concentration fermentation liquid production alcohol fuel provided by the utility model, tool There is highly significant economic benefit.

Embodiment 2:

As shown in Fig. 2, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as Under:

4th rectifying column T140 tower top shown in FIG. 1 does not produce azeotropic alcohol gas phase and removes dewatering unit.First rectifying column After the liquid phase azeotropic alcohol 110 of T110 overhead extraction and the liquid phase azeotropic alcohol 414 of the 4th rectifying column T140 overhead extraction mix Logistics 415 into evaporator E144, the alcohol gas phase 405 after vaporization removes dewatering unit.

Embodiment 3:

As shown in figure 3, it is a kind of differentiation process of Fig. 2, process difference relatively shown in Fig. 2 is such as Under:

The top first rectifying column T110 shown in Fig. 2 a part of liquid phase azeotropic alcohol 110 of side take-off removes the 4th rectifying column T140 tower top, final whole azeotropic alcohol is produced from the 4th rectifying column T140 upper aqueous phase side line 415, then into evaporator E144, the alcohol gas phase 405 after vaporization remove dewatering unit.

Embodiment 4:

As shown in figure 4, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as Under:

Dewatering unit shown in FIG. 1 is changed to be adsorbed/regenerated handover operation dehydration, dewatering unit using molecular sieve T150A/B The dehydrated alcohol gas phase 407 of output is changed to heat to Second distillation column T120 the second reboiler E123.Dewatering unit generates light Wine 409 enters the first rectifying section S1101 of first rectifying column T110.Second distillation column T120 the second reboiler E123 shell side lime set 408 be process of alcohol products.

Embodiment 5:

As shown in figure 5, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as Under:

When switching produces azeotropic alcohol, dewatering unit, first rectifying column T110 overhead extraction liquid phase 110 and the 4th are deactivated Rectifying column T140 overhead extraction liquid phase 414 is together as azeotropic alcohol product 415.

Embodiment 6:

As shown in fig. 6, it is a kind of differentiation process of Fig. 5, process difference relatively shown in fig. 5 is such as Under:

When switching produces azeotropic alcohol, the top first rectifying column T110 a part of azeotropic alcohol 110 of side take-off goes the Four rectifying column T140 tower tops, final whole azeotropic alcohol are produced from the 4th rectifying column T140 upper aqueous phase side line 415.

Embodiment 7:

As shown in fig. 7, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as Under:

The process of Fig. 1 is simplified, third distillation column T130, the 4th rectifying column T140 top gaseous phase is omitted A part 404 is heated to Second distillation column T120 reboiler E122, and another part 405 removes dewatering unit M150.Through dewatering unit Dewatered dehydrated alcohol gas phase 407 is heated to Second distillation column T120 the second reboiler E123.

Following present a kind of typical operation conditions of each tower in embodiment 7, typical operation conditions and operation energy consumption are as follows:

Second distillation column T120 tower top operating pressure be 170kpa, 92 DEG C of tower top, 118 DEG C of tower reactor；

4th rectifying column T140 column overhead operating pressure be 570kpa, 129 DEG C of tower top, 158 DEG C of tower reactor；

Dewatering unit (gas-phase dehydration membrane module) operating pressure is 570kpa.

By the process that the utility model Fig. 7 is provided, entire distillation system only the 4th rectifying column T140 tower bottom reboiler E143 needs middle pressure steam to heat, and distillation system operation energy consumption is 2.7 tons of steam/ton alcohol fuel.

Embodiment 8:

As shown in figure 8, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as Under:

Further energy saving optimizing is carried out to the process of Fig. 1, in third distillation column T130 and the 4th rectifying column T140 Between increase the 5th rectifying column T160.4th rectifying column T140 top gaseous phase a part 404 is boiled again to the 5th rectifying column T160 Device E162 heating, another part 405 remove dewatering unit M150.The 5th is given through the dewatered dehydrated alcohol gas phase 407 of dewatering unit Rectifying column T160 the second reboiler E163 heating.5th rectifying column T160 top gaseous phase 602 gives third distillation column T130 reboiler E132 heating.Second distillation column T120 pushes up distillate that is, first rectifying column T110 reboiler E114 shell side lime set 204 goes first Rectifying column T110 feeds the above position.The charging of 4th rectifying column T140 is to feed the above liquid side from first rectifying column T110 Line discharging 113, third distillation column T130 overhead 303, the 5th rectifying column T160 overhead 603 mixed material.

Following present a kind of typical operation conditions of each tower in embodiment 8, typical operation conditions and operation energy consumption are as follows:

First rectifying column T110 tower top operating pressure be 25kpa, 46 DEG C of tower top, 74 DEG C of tower reactor；

Second distillation column T120 tower top operating pressure be 70kpa, 87 DEG C of tower top, 93 DEG C of tower reactor；

Third distillation column T130 tower top operating pressure be 120kpa, 102 DEG C of tower top, 107 DEG C of tower reactor；

5th rectifying column T160 tower top operating pressure be 195kpa, 116 DEG C of tower top, 121 DEG C of tower reactor；

4th rectifying column T140 tower top operating pressure be 590kpa, 130 DEG C of tower top, 159 DEG C of tower reactor；

By the process that the utility model Fig. 8 is provided, by conventional double prefractionators (double prefractionators, mash economic benefits and social benefits stripping operation) Be improved to four prefractionators --- the thick tower S1103 of the first of the lower part first rectifying column T110, the lower part Second distillation column T120 second Thick tower S1203, the thick tower S1303 of third of the lower part third distillation column T130, the 5th lower part rectifying column T160 the 5th thick tower S1603 It forms the quadruple effect of low concentration fermentation liquid, be thermally integrated stripping operation.Entire distillation system first rectifying column T110, Second distillation column T120, third distillation column T130, the 5th rectifying column T160 and the 4th rectifying column T140 form five effects and are thermally integrated operation, the 4th rectifying Tower T140 top gaseous phase provides one as the 5th tower bottom of rectifying tower the first reboiler E162 heat source for the 5th rectifying column T160 The dehydrated alcohol gas phase of partial heat, dewatering unit output heats heat as the 5th rectifying column T160 tower reactor the second reboiler E163 Source provides another part heat for the 5th rectifying column T160；5th rectifying column T160 top gaseous phase is as third distillation column tower reactor Heat source provides institute's calorific requirement for third distillation column T130；Third distillation column T130 top gaseous phase is as Second distillation column T120 tower reactor heat source provides institute's calorific requirement for Second distillation column T120；Second distillation column T120 top gaseous phase is as first Rectifying column T110 tower reactor heat source provides institute's calorific requirement for first rectifying column T110.Only the 4th rectifying column T140 tower bottom is boiled again Device E143 needs middle pressure steam to heat, and operation energy consumption is only 1.8 tons of steam/ton process of alcohol products, and operation energy consumption substantially reduces.

By 200,000 tons/year of fuel alcohol plants, 8000 hour/year of operation hour, the technique provided by the utility model Fig. 8 Method, middle pressure steam consumption are 45 ton/hours.Other each reboilers, the equal utilisation system internal heat of heat exchanger institute calorific requirement.

Double prefractionators of comparison CN201710542687.5 offer, double smart towers add the tri-columns rectification process method of molecular sieve, Distillation system operation energy consumption is 3.0 tons of steam/ton alcohol fuel, and middle pressure steam consumption is 75 ton/hours:

(3.0-1.8)/3.0=40%

Double prefractionators of opposite CN201710542687.5 offer, double smart towers add the tri-columns rectification process method of molecular sieve, this The process energy consumption that utility model Fig. 8 is provided reduces about 40%.

75-45=30 ton/hours of steam can be saved per hour.

30 ton/hours × 8000 hour/year=240000 ton/year of middle pressure steam can be saved every year.

240000 tons/year × 150 yuan/ton ten thousand yuan/year of ÷ 10000=3600.

It is illustrated in conjunction with the embodiments, the personnel of related fields completely can be according to method provided by the utility model It is suitably changed or changes and combinations, to realize the technology.It should be strongly noted that all these by practical new to this The process flow that type provides carries out similar change or changes and reconfigure, and is aobvious and easy for a person skilled in the art See, is considered as in the spirit, range and content of the utility model.

Claims

1. a kind of energy saving technique device from low concentration fermentation liquid production alcohol fuel, it is characterised in that: include at least the first essence Evaporate tower (T110), Second distillation column (T120), third distillation column (T130) and the 4th rectifying column (T140) and connecting pipeline；

Feeding line is connect with condenser (E111) tube-side inlet of first rectifying column (T110), the outlet of condenser (E111) tube side It is connect with first rectifying column feed preheater (E113) cold side import, feed preheater (E113) cold side outlet port is connected to the first essence It evaporates in the middle part of tower (T110)；The condenser (E111) of the top gaseous phase outlet and first rectifying column (T110) of first rectifying column (T110) The connection of shell side gas phase entrance, condenser (E111) the shell side gaseous phase outlet and first rectifying column (T110) of first rectifying column (T110) Tail cooler (E112) shell side gas phase entrance connection, first rectifying column (T110) tail cooler (E112) shell side gaseous phase outlet connection To vacuum system；The tail cooler (E112) of the condenser (E111) and first rectifying column (T110) of first rectifying column (T110) coagulates Liquid outlet line is divided into two, one be connected to the overhead reflux mouth of first rectifying column (T110), another be connected to the 4th essence Evaporate tower (T140) overhead reflux mouth；Tail cooler (E112) condensate outlet pipeline is additionally coupled to industrial alcohol extraction pipeline；First essence Evaporate the tower reactor of tower (T110) respectively with reboiler (E114) tube-side inlet and first rectifying column of first rectifying column (T110) (T110) feed preheater (E113) hot side import is connected；Feed preheater (E113) hot side of first rectifying column (T110) goes out Mouth is connected with useless wine with dregs discharge pipe；The reboiler tube side outlet of first rectifying column (T110) is connected to first rectifying column (T110) Tower reactor；

The first charging that the above liquid phase side line outlet of the charging of first rectifying column (T110) is connected to the 4th rectifying column (T140) is pre- Hot device (E141) cold side input port, the following liquid phase side line outlet of the charging of first rectifying column (T110) are connected to Second distillation column (T120) feed preheater (E121) cold side input port；

The feed preheater cold side outlet port of Second distillation column (T120) is divided into two, and one is connected to Second distillation column (T120) Feed inlet, another is connected to feed preheater (E131) cold side input port of third distillation column (T130)；Second distillation column (T120) top gaseous phase outlet is connect with first rectifying column reboiler (E114) shell side gas phase entrance, first rectifying column (T110) Reboiler (E114) shell side condensate outlet be connected to the 4th the first feed preheater of rectifying column (E141) cold side input port；Second essence Evaporate the tower reactor of tower (T120) respectively with reboiler (E122) tube-side inlet and Second distillation column of Second distillation column (T120) (T120) feed preheater (E121) hot side import is connected；The feed preheater hot side outlet of Second distillation column (T120) connects To feed preheater (E113) hot side import of first rectifying column (T110)；The reboiler tube side of Second distillation column (T120) exports It is connected to the tower reactor of Second distillation column (T120)；

Feed preheater (E131) cold side outlet port of third distillation column (T130) is connected to the feed inlet of third distillation column (T130)； The top gaseous phase outlet of third distillation column (T130) and reboiler (E122) the shell side gas phase entrance of Second distillation column (T120) connect It connects, reboiler (E122) shell side condensate outlet of Second distillation column (T120) is connected to the first charging of the 4th rectifying column (T140) Preheater (E141) cold side input port；The tower reactor of third distillation column (T130) the first reboiler with third distillation column (T130) respectively (E132) tube-side inlet, the second reboiler (E133) tube-side inlet of third distillation column (T130) and third distillation column (T130) Tower feed preheater (E131) hot side import is connected；The feed preheater hot side outlet of third distillation column (T130) is connected to second Feed preheater (E121) hot side import of rectifying column (T120)；The first reboiler (E132) tube side of third distillation column (T130) The outlet of the second reboiler (E133) tube side of outlet and third distillation column (T130) is connected to the tower reactor of third distillation column (T130)；

The second of the first feed preheater (E141) cold side outlet port of 4th rectifying column (T140) and the 4th rectifying column (T140) into Expect that preheater (E142) cold side input port is connected, the second feed preheater (E142) cold side outlet port of the 4th rectifying column (T140) and the The feed inlet of four rectifying columns (T140) is connected；4th rectifying column (T140) top gaseous phase outlet respectively with third distillation column (T130) the first reboiler (E132) shell side gas phase entrance, dewatering unit gas phase import are connected；Third distillation column (T130) First reboiler (E132) shell side condensate outlet pipeline is connected to the overhead reflux mouth of the 4th rectifying column (T140)；

The dehydrated alcohol vapor delivery line of dewatering unit output is connected to the second reboiler (E133) shell of third distillation column (T130) The second reboiler (E133) shell side condensate outlet and the process of alcohol products extraction of journey gas phase entrance, third distillation column (T130) are managed Line is connected；The light wine pipeline of dewatering unit discharge is connected to the above light wine feed inlet of charging of first rectifying column (T110)；

Several fusel oil extraction mouths are respectively set in the feed entrance point above and below of 4th rectifying column (T140), and fusel oil produces mouth It is connect respectively with fusel oil extraction pipeline；

The tower reactor of 4th rectifying column (T140) reboiler (E143) tube-side inlet and the 4th with the 4th rectifying column (T140) respectively The first feed preheater (E141) hot side import of rectifying column (T140) is connected；First feeding preheating of the 4th rectifying column (T140) Device (E141) hot side outlet is connect with wastewater discharge pipe line；Reboiler (E143) tube side of 4th rectifying column (T140) exports connection To the tower reactor of the 4th rectifying column (T140)；Heating steam pipe line is connected to reboiler (E143) shell side of the 4th rectifying column (T140) Gas phase entrance, reboiler (E143) shell side condensate outlet of the 4th rectifying column (T140) are connected to the of the 4th rectifying column (T140) Two feed preheaters (E142) hot side import；The second feed preheater (E142) hot side outlet of 4th rectifying column (T140) with plus Hot steam drip pipe line is connected.