CN210021208U - Distillation energy-saving system for preparing ethanol from carbon monoxide - Google Patents
Distillation energy-saving system for preparing ethanol from carbon monoxide Download PDFInfo
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- CN210021208U CN210021208U CN201920566259.0U CN201920566259U CN210021208U CN 210021208 U CN210021208 U CN 210021208U CN 201920566259 U CN201920566259 U CN 201920566259U CN 210021208 U CN210021208 U CN 210021208U
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Abstract
The utility model discloses a distillation energy-saving system for preparing ethanol from carbon monoxide, which comprises a crude distillation tower I, a composite tower consisting of a crude distillation tower II/a rectification tower II, a rectification tower I, a reboiler, a condenser, a heat exchanger, a storage tank, a vacuum pump, a delivery pump and the like which are matched with the rectification tower I; heating the rectifying tower I by using steam from a boiler through a reboiler of the rectifying tower I; supplying the alcohol steam at the top of the rectifying tower I to the compound tower for heating; the alcohol steam at the top of the composite tower is supplied to the crude distillation tower I for heating; alcohol steam at the top of the coarse distillation tower I is used as the primary preheating of the thick fermented liquor, and distiller's grains at the bottom of the coarse distillation tower I are used as the secondary preheating of the thick fermented liquor. The distillation energy-saving system adopts a reasonable distillation thermal coupling technology and a three-stage differential pressure distillation technology, can fully utilize available energy coupling in alcohol production, and reduces the distillation energy consumption by about 20 percent compared with the conventional distillation.
Description
Technical Field
The utility model relates to a fuel ethanol preparation field, concretely relates to distillation economizer system of carbon monoxide system ethanol.
Background
The preparation of ethanol from carbon monoxide is a novel technology researched in recent years, and at present, converter gas (main component CO) of a steel mill is used as a raw material, and CO in the gas is converted into clean energy fuel ethanol through a microbial fermentation method. The existing distillation process for preparing ethanol from carbon monoxide has high energy consumption, so that the production cost is high, and the method does not conform to the policy of energy-saving and emission-reducing policy advocated by the state.
SUMMERY OF THE UTILITY MODEL
To the problem that exists among the prior art, the utility model aims at providing a distillation economizer system of carbon monoxide system ethanol, this distillation economizer system adopts reasonable distillation thermal coupling technique and tertiary differential pressure distillation technique, can make full use of the usable energy among the alcohol production make its abundant coupling, make the distillation energy consumption reduce about 20% than conventional distillation, the steam for the distillation reduces by a wide margin, reach energy saving and consumption reduction's effect, product quality reaches national fuel ethanol quality index; the distillation method is simple, ensures that the energy between each tower is fully and effectively utilized, has low energy consumption and obviously reduces the production cost.
In order to achieve the above purpose, the present invention adopts the following technical solution.
The energy-saving distillation system for preparing ethanol from carbon monoxide comprises: clear mash primary preheater, clear mash secondary preheater, clear mash tertiary preheater, thick mash primary preheater, thick mash secondary preheater and first CO2Separator, crude distillation tower I condenser, gas scrubbing tower, crude alcohol tank, crude tower I reboiler and second CO2Separator and composite towerThe system comprises a crude tower II reboiler, a first crude alcohol preheater, a second crude alcohol preheater, a rectifying tower I reboiler, a fusel oil separator, a condensed water distributor, a rectifying tower II reflux pump, a crude alcohol pump, a rectifying tower I reflux pump and a rectifying tower II material passing pump;
a clear mash primary preheater, a clear mash secondary preheater, a clear mash tertiary preheater and a first CO which are connected in series in sequence through tube passes2A separator; wherein, the tube side inlet of the primary preheater is communicated with the fermented clear mash raw material inlet; the first CO2The bottom mash outlet of the separator is communicated with the feed inlet of a composite tower, and the composite tower consists of a rough distillation tower II and a rectification tower II; the first CO2The top gas outlet of the separator is communicated with the gas inlet at the bottom of the side wall of the scrubbing tower;
a shell pass inlet of the clear mash primary preheater is connected to a dehydration section, and a shell pass outlet of the clear mash primary preheater is communicated with an inlet of the cooler; a shell pass inlet of the clear mash secondary preheater is communicated with a bottom outlet of the composite tower, and a shell pass outlet of the clear mash secondary preheater is connected to a fermentation section;
the top outlet of the composite tower is communicated with the shell pass inlet of a reboiler of a crude tower I, and the shell pass outlet of the reboiler of the crude tower I is communicated with a first top inlet of the composite tower through a reflux pump of a fine tower II; the tube pass of the reboiler of the crude tower I and the bottom outlet of the crude distillation tower I form closed cycle through a pump;
the middle outlet of the compound tower is communicated with the first inlet of a second crude alcohol preheater through a material passing pump of a rectifying tower II, and the first outlet of the second crude alcohol preheater is communicated with the first inlet of the middle of a rectifying tower I;
the top outlet of the rectifying tower I is communicated with the shell pass inlet of a reboiler of a crude tower II, the shell pass outlet of the reboiler of the crude tower II is communicated with the reflux pump inlet of the rectifying tower I, and the tube pass of the reboiler of the crude tower II forms closed cycle with the bottom outlet of the composite tower through a pump; the outlet of the reflux pump of the fine tower I is communicated with the second inlet at the top of the composite tower;
an outlet in the middle of the rectifying tower I is communicated with an inlet of a fusel oil separator, and a fusel oil outlet of the fusel oil separator is communicated with a fusel oil storage tank; an outlet at the bottom of the rectifying tower I is communicated with a shell pass inlet of the clear mash three-stage preheater, and a shell pass outlet of the clear mash three-stage preheater is connected to a fermentation working section;
an outlet at the bottom of the rectifying tower I is in closed cycle with a tube pass of a reboiler of the rectifying tower I through a pump, a shell pass inlet of the reboiler of the rectifying tower I is communicated with a steam pipeline, and a shell pass outlet of the reboiler of the rectifying tower I is communicated with a water inlet of a condensed water distributor;
a first outlet of the condensation water distributor is communicated with a second inlet of the first crude alcohol preheater, and a second outlet of the first crude alcohol preheater is communicated to a boiler room through a pipeline; a second outlet of the condensed water distributor is communicated with a second inlet of a second crude alcohol preheater, and a second outlet of the second crude alcohol preheater is communicated to a boiler room through a pipeline;
a thick mash primary preheater, a thick mash secondary preheater and a second CO which are connected in series in sequence through a tube pass2A separator; wherein, the tube side inlet of the thick mash primary preheater is communicated with the thick mash raw material inlet; the second CO2The bottom liquid outlet of the separator is communicated with the upper first inlet of the crude distillation tower I, and the second CO is2The top gas outlet of the separator is communicated with the gas inlet at the bottom of the side wall of the scrubbing tower;
a shell pass inlet of the thick mash secondary preheater is communicated with a vinasse outlet at the bottom of the coarse distillation tower I, and a shell pass outlet of the thick mash secondary preheater is connected to a feed workshop;
the top wine vapor outlet of the coarse distillation tower I is communicated with the shell pass inlet of the thick mash primary preheater, the shell pass outlet of the thick mash primary preheater is communicated with the shell pass inlet of the coarse distillation tower I condenser, and the shell pass outlet of the coarse distillation tower I condenser is communicated with the gas inlet at the bottom of the side wall of the scrubbing tower;
a water inlet at the top of the scrubbing tower is communicated with a water supply device; a gas outlet at the top of the scrubbing tower is communicated with a vacuum pump; a light wine outlet at the bottom of the scrubbing tower is communicated with a condensed crude wine outlet of a condenser of the coarse distillation tower I and a condensed crude wine outlet of a thick mash primary preheater through pipelines and a first inlet of a crude alcohol tank;
the second inlet of the crude alcohol tank is communicated with a dehydrated light wine pipeline, and the third inlet of the crude alcohol tank is communicated with a light wine outlet of the fusel oil separator; an outlet at the bottom of the crude alcohol tank is communicated with an inlet of a crude alcohol pump;
the outlet of the crude alcohol pump is communicated with the first inlet of the first crude alcohol preheater; and a first outlet of the first crude alcohol preheater is communicated with a second inlet in the middle of the rectifying tower I.
Preferably, the top outlet of the composite tower is communicated to the dehydration section through a bypass pipe.
Preferably, the outlet of the crude alcohol pump is communicated with the second inlet at the upper part of the crude distillation column I through a branch pipe.
Preferably, the outlet of the reflux pump of the rectifying tower I is communicated with the feed inlet at the upper part of the rectifying tower I through a bypass pipe.
The distillation method of the distillation energy-saving system for preparing the ethanol from the carbon monoxide comprises the following steps:
step 1, pumping fermented clear mash into a clear mash primary preheater to perform primary heat exchange with wine vapor from a dehydration section, and condensing the wine vapor back to the dehydration section through a cooler after the heat exchange; feeding the clear mash after the primary heating into a clear mash secondary preheater to perform secondary heat exchange with vinasse from the bottom of the composite tower, and feeding the vinasse to a fermentation working section for recycling after the heat exchange; clear mash after the second-stage heating is sent into a clear mash three-stage preheater to carry out third-stage heat exchange with residual distilled water from the bottom of the rectifying tower I, and the residual distilled water is sent to a fermentation working section for recycling after heat exchange; clear mash after three-stage heating enters first CO2A separator;
step 2, first CO2CO separated in a separator2Gas enters a gas inlet at the bottom of the side wall of the scrubbing tower from a gas outlet at the top, the gas is washed after water is added into the scrubbing tower through a water supply device, the washed gas is discharged through a vacuum pump, and the washed light wine enters a crude alcohol tank;
first CO2After gas separation in the separatorThe mash enters a composite tower, wine vapor at the top of the composite tower heats a coarse distillation tower I through a reboiler of the coarse distillation tower I, and heated alcohol condensate is sent to a first inlet at the top of the composite tower for reflux through a reflux pump of a fine tower II;
3, conveying the fusel wine at the middle outlet of the compound tower into a second crude alcohol preheater through a material passing pump of a rectifying tower II, exchanging heat with steam condensed water from a condensed water distributor, and conveying the heated fusel wine into a first middle inlet of a rectifying tower I;
step 4, pumping the fermented thick mash into a thick mash primary heat exchanger to perform primary heat exchange with wine vapor from the top of the coarse distillation tower I, condensing the wine vapor through a condenser of the coarse distillation tower I after the heat exchange of the wine vapor, and then washing and discharging the wine vapor in a scrubbing tower; feeding the thick mash subjected to primary heating into a thick mash secondary preheater to perform secondary heat exchange with distiller's grains at the bottom of the coarse distillation tower I, and feeding the distiller's grains to a feed workshop after heat exchange; the thick mash after the second-stage heating enters second CO2A separator;
step 5, second CO2CO separated by a separator2The gas enters a scrubbing tower to be washed and discharged, and the washed light wine is converged with the condensed crude wine of a condenser of the coarse distillation tower I and the condensed crude wine of a primary thick mash preheater and flows into a first inlet of a crude alcohol tank; second CO2The thick mash after the gas is separated by the separator enters a rough distillation tower I;
step 6, enabling the dehydrated weak liquor in the weak liquor pipeline to enter a second inlet of the crude alcohol tank, sending the crude alcohol in the crude alcohol tank into a first crude alcohol preheater through a crude alcohol pump, enabling the crude alcohol in the first crude alcohol preheater to exchange heat with steam condensate water from the condensate water distributor, enabling the steam condensate water to enter a second inlet in the middle of the rectifying tower I, and enabling the steam condensate water to return to a boiler room after the steam condensate water exchanges heat;
step 7, allowing the top alcohol vapor of the rectifying tower I to enter a reboiler of a crude tower II to heat the composite tower, feeding one path of heated alcohol condensate into a second inlet at the top of the composite tower through a reflux pump of the rectifying tower I, and feeding the other path of heated alcohol condensate into an upper feed inlet of the rectifying tower I through a bypass pipe for reflux;
step 8, enabling fusel oil at the middle outlet of the rectifying tower I to enter a fusel oil separator, sending the fusel oil separated in the fusel oil separator to a storage tank, and enabling light wine of the fusel oil separator to enter a third inlet of the crude alcohol tank;
and 9, steam from the boiler enters a reboiler of a fine tower I through a steam pipeline to heat a rectifying tower I, the heated steam condensate enters a condensate distributor, one path of the steam condensate in the condensate distributor heats crude alcohol in a first crude alcohol preheater, the other path of the steam condensate in the condensate distributor heats fusel wine in a second crude alcohol preheater, and the two paths of the heated steam condensate return to a boiler room.
Preferably, the temperature of the steam from the boiler is 160-180 ℃, and the pressure is 0.5-0.7 MPa; the bottom temperature of the crude distillation tower I is 80-84 ℃, and the top temperature is 65-71 ℃; the bottom temperature of the composite tower is 110-116 ℃, and the top temperature is 85-93 ℃; the bottom temperature of the rectifying tower I is 150-160 ℃, and the top temperature is 115-125 ℃.
Further preferably, the temperature of the steam from the boiler is 168 ℃ and the pressure is 0.66 MPa; the bottom temperature of the coarse distillation tower I is 82 ℃, and the top temperature is 68 ℃; the bottom temperature of the composite tower is 113 ℃, and the top temperature is 89 ℃; the bottom temperature of the rectifying tower I is 155 ℃, and the top temperature is 120 ℃.
Preferably, in step 1, the temperature of the fermentation broth is 25-35 ℃.
Further preferably, in step 1, the temperature of the fermentation broth is 30 ℃.
Preferably, in the step 2, one path of the wine vapor at the top of the composite tower passes through a reboiler of the crude tower I to heat the crude distillation tower I, and the other path of the wine vapor passes through a bypass pipe to enter a dehydration section.
Preferably, in the step 4, the temperature of the fermented thick mash is 25-35 ℃; the temperature of thick mash after the second-stage heating is 55-65 ℃.
Further preferably, in the step 4, the temperature of the fermented thick mash is 30 ℃; the temperature of the thick mash after the second heating is 60 ℃.
Preferably, in step 6, the crude alcohol is pumped by the crude alcohol pump into the first crude alcohol preheater in one path and into the second inlet at the upper part of the crude distillation column I in the other path through the branch pipe.
Compared with the prior art, the beneficial effects of the utility model are that:
the utility model discloses an among the distillation economizer system of carbon monoxide system ethanol, including coarse distillation column I, by the compound tower, rectifying column I that coarse distillation column II/rectifying column II are constituteed, three tower altogether to and supporting reboiler, condenser, heat exchanger, basin, vacuum pump and delivery pump etc. with it. A three-stage differential pressure thermal coupling technology is adopted, namely, steam from a boiler passes through a reboiler of a rectifying tower I to heat the rectifying tower I, and only the rectifying tower I uses primary steam; supplying the alcohol steam at the top of the rectifying tower I to the compound tower for heating; the alcohol steam at the top of the composite tower is supplied to the crude distillation tower I for heating; alcohol steam at the top of the coarse distillation tower I is used as the primary preheating of the thick fermented liquor, and distiller's grains at the bottom of the coarse distillation tower I are used as the secondary preheating of the thick fermented liquor.
Wine vapor in the dehydration section is used for primary preheating of clear mash, distiller's grains at the bottom of the composite tower are used for secondary preheating of the clear mash, and residual distilled water at the bottom of the rectifying tower I is used for tertiary preheating of the clear mash; one path of steam condensate in the condensate distributor heats crude alcohol in the crude alcohol preheater, the other path heats fusel wine in the crude alcohol preheater, and the two paths of heated steam condensate return to the boiler room. The energy between each tower is all by abundant effective utilization, the utility model discloses a distillation energy saving system of carbon monoxide system ethanol's distillation energy consumption reduces about 20% than conventional distillation.
Drawings
The present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
FIG. 1 is a diagram of an energy-saving distillation system for preparing ethanol from carbon monoxide.
In the above figures, 1, a primary pre-heater for clear mash; 2, a clear mash secondary preheater; 3, a clear mash three-stage preheater; 4, a thick mash primary preheater; 5 thick mash secondary preheater; 6 first CO2A separator; 7, a crude distillation tower I; 8, a condenser of the crude distillation tower I; 9 a scrubbing tower; 10 a crude alcohol tank; 11 a reboiler of the crude tower I; 12 second CO2A separator; 13 a composite tower; 14 reboiler of crude column II; 15 a first crude alcohol preheater; 16 a second crude alcohol preheater; 17, a rectifying tower I; 18 a reboiler of a fine column I; 19 fusel oil separator; 20 a condensed water dispenser; reflux pump of 21 fine tower II(ii) a 22 crude alcohol pump; a reflux pump of the fine tower I23; 24 fine tower II material passing pump.
Detailed Description
Embodiments of the present invention will be described in detail below with reference to examples, but those skilled in the art will understand that the following examples are only for illustrating the present invention and should not be construed as limiting the scope of the present invention.
Example 1
The energy-saving distillation system for preparing ethanol from carbon monoxide comprises: a clear mash primary preheater 1, a clear mash secondary preheater 2, a clear mash tertiary preheater 3 and a first CO which are connected in series in sequence through tube passes2A separator 6; wherein, the tube side inlet of the clear mash primary preheater 1 is communicated with the fermented clear mash raw material inlet; first CO2The mash outlet at the bottom of the separator 6 is communicated with the feed inlet of a composite tower 13, and the composite tower 13 consists of a rough distillation tower II and a rectification tower II; first CO2The top gas outlet of the separator 6 is communicated with the gas inlet at the bottom of the side wall of the scrubbing tower 9;
a shell pass inlet of the clear mash primary preheater 1 is connected to a dehydration section, and a shell pass outlet of the clear mash primary preheater 1 is communicated with an inlet of a cooler; a shell pass inlet of the clear mash secondary preheater 2 is communicated with a bottom outlet of the compound tower 13, and a shell pass outlet of the clear mash secondary preheater 2 is connected to a fermentation working section;
the top outlet of the composite tower 13 is communicated with the shell pass inlet of the reboiler 11 of the crude tower I, and the top outlet of the composite tower 13 is communicated to the dehydration working section through a bypass pipe; a shell pass outlet of a reboiler 11 of the crude tower I passes through a reflux pump 21 of the fine tower II and a first inlet at the top of the composite tower 13; the tube pass of the reboiler 11 of the crude tower I and the bottom outlet of the crude distillation tower I7 form closed cycle through a pump;
the middle outlet of the compound tower 13 is communicated with the first inlet of the second crude alcohol preheater 16 through a material passing pump 24 of the rectifying tower II, and the first outlet of the second crude alcohol preheater 16 is communicated with the first inlet of the middle of the rectifying tower I17;
the top outlet of the rectifying tower I17 is communicated with the shell pass inlet of the crude tower II reboiler 14, the shell pass outlet of the crude tower II reboiler 14 is communicated with the inlet of the reflux pump 23 of the fine tower I, and the tube pass of the crude tower II reboiler 14 forms closed cycle with the bottom outlet of the composite tower 13 through a pump; an outlet of a reflux pump 23 of the rectifying tower I is communicated with a second inlet at the top of the composite tower 13, and an outlet of the reflux pump 23 of the rectifying tower I is communicated with a feed inlet at the upper part of a rectifying tower I17 through a bypass pipe;
an outlet in the middle of the rectifying tower I17 is communicated with an inlet of a fusel oil separator 19, and a fusel oil outlet of the fusel oil separator 19 is communicated with a fusel oil storage tank; an outlet at the bottom of the rectifying tower I17 is communicated with a shell pass inlet of the clear mash tertiary preheater 3, and a shell pass outlet of the clear mash tertiary preheater 3 is connected to a fermentation working section;
an outlet at the bottom of the rectifying tower I17 and a tube pass of a reboiler 18 of the rectifying tower I form closed cycle through a pump, an inlet of a shell pass of the reboiler 18 of the rectifying tower I is communicated with a steam pipeline, and an outlet of the shell pass of the reboiler 18 of the rectifying tower I is communicated with a water inlet of a condensed water distributor 20;
a first outlet of the condensation water distributor 20 is communicated with a second inlet of the first crude alcohol preheater 15, and a second outlet of the first crude alcohol preheater 15 is communicated to a boiler room through a pipeline; a second outlet of the condensation water distributor 20 is communicated with a second inlet of the second crude alcohol preheater 16, and a second outlet of the second crude alcohol preheater 16 is communicated to the boiler room through a pipeline;
a thick mash primary preheater 4, a thick mash secondary preheater 5 and a second CO connected in series in turn through a tube pass2A separator 12; wherein, the tube side inlet of the thick mash primary preheater 4 is communicated with the thick mash raw material inlet; second CO2The bottom liquid outlet of the separator 12 is communicated with the upper first inlet of the crude distillation tower I7, and the second CO is2The top gas outlet of the separator 12 is communicated with the gas inlet at the bottom of the side wall of the scrubbing tower 9;
a shell pass inlet of the thick mash secondary preheater 5 is communicated with a vinasse outlet at the bottom of the coarse distillation tower I7, and a shell pass outlet of the thick mash secondary preheater 5 is connected to a feed workshop;
the top wine vapor outlet of the rough distillation tower I7 is communicated with the shell pass inlet of the thick mash primary preheater 4, the shell pass outlet of the thick mash primary preheater 4 is communicated with the shell pass inlet of the condenser 8 of the rough distillation tower I, and the shell pass outlet of the condenser 8 of the rough distillation tower I is communicated with the air inlet at the bottom of the side wall of the scrubbing tower 9;
a water inlet at the top of the scrubbing tower 9 is communicated with a water supply device; a gas outlet at the top of the scrubbing tower 9 is communicated with a vacuum pump; the light wine outlet at the bottom of the scrubbing tower 9 is communicated with the condensed coarse wine outlet of the condenser 8 of the coarse distillation tower I and the condensed coarse wine outlet of the thick mash primary preheater 4 through pipelines and a first inlet of a coarse alcohol tank 10;
the second inlet of the crude alcohol tank 10 is communicated with a dehydrated weak liquor pipeline, and the third inlet of the crude alcohol tank 10 is communicated with a weak liquor outlet of the fusel oil separator 19; the bottom outlet of the crude alcohol tank 10 is communicated with the inlet of a crude alcohol pump 22;
the outlet of the crude alcohol pump 22 is communicated with the first inlet of the first crude alcohol preheater 15, and the outlet of the crude alcohol pump 22 is communicated with the second inlet at the upper part of the crude distillation tower I7 through a branch pipe; the first outlet of the first crude alcohol preheater 15 is communicated with the second inlet in the middle of the rectifying tower I17.
The distillation method of the distillation energy-saving system for preparing ethanol from carbon monoxide is based on a three-tower three-level differential pressure distillation system, fermented mash is pumped into the three-tower three-level differential pressure distillation system for alcohol distillation, and the distillation method comprises the following steps:
step 1, pumping fermented clear mash at 30 ℃ into a clear mash primary preheater to perform primary heat exchange with wine vapor from a dehydration section, and condensing the wine vapor back to the dehydration section through a cooler after the heat exchange; feeding the clear mash after the primary heating into a clear mash secondary preheater to perform secondary heat exchange with vinasse from the bottom of the composite tower, and feeding the vinasse to a fermentation working section for recycling after the heat exchange; clear mash after the second-stage heating is sent into a clear mash three-stage preheater to carry out third-stage heat exchange with residual distilled water from the bottom of the rectifying tower I, and the residual distilled water is sent to a fermentation working section for recycling after heat exchange; clear mash after three-stage heating enters first CO2A separator;
step 2, first CO2CO separated in a separator2Gas enters a gas inlet at the bottom of the side wall of the scrubbing tower from a gas outlet at the top, the gas is washed after water is added into the scrubbing tower through a water supply device, the washed gas is discharged through a vacuum pump, and the washed light wine enters a crude alcohol tank;
first CO2Mash after gas separation in the separator enters a feed inlet of the composite tower from a mash outlet at the bottom, wine vapor at the top of the composite tower is divided into two paths from a top outlet, one path is heated in the crude distillation tower I through a reboiler of the crude distillation tower I, and heated alcohol condensate is fed into a first inlet at the top of the composite tower for reflux through a reflux pump of a rectifying tower II; the other path is sent to a dehydration working section through a bypass pipe;
step 3, a part of fusel wine is collected from the middle outlet of the compound tower and sent into a second crude alcohol preheater through a material passing pump of a rectifying tower II, the fusel wine exchanges heat with steam condensed water from a condensed water distributor, and the heated fusel wine is sent into a first middle inlet of a rectifying tower I;
step 4, pumping the thick mash fermented at the temperature of 30 ℃ into a thick mash primary heat exchanger to perform primary heat exchange with wine vapor from the top of the coarse distillation tower I, condensing the wine vapor through a condenser of the coarse distillation tower I after the heat exchange, and then washing and discharging the wine vapor in a scrubbing tower; feeding the thick mash subjected to primary heating into a thick mash secondary preheater to perform secondary heat exchange with distiller's grains at the bottom of the coarse distillation tower I, and feeding the distiller's grains to a feed workshop after heat exchange; the thick mash after the second-stage heating reaches 60 ℃ and enters second CO2A separator;
step 5, second CO2CO separated by a separator2The gas enters a scrubbing tower to be washed and discharged, and the washed light wine is converged with the condensed crude wine of a condenser of the coarse distillation tower I and the condensed crude wine of a primary thick mash preheater and flows into a first inlet of a crude alcohol tank; second CO2The thick mash after the gas is separated by the separator enters a rough distillation tower I;
step 6, enabling the dehydrated weak liquor in the weak liquor pipeline to enter a second inlet of the crude alcohol tank, enabling the crude alcohol in the crude alcohol tank to enter a crude alcohol pump, enabling the crude alcohol pump to send one path of the crude alcohol to a first crude alcohol preheater, enabling the crude alcohol to enter a second inlet in the middle of the rectifying tower I after heat exchange with steam condensate water from the condensate water distributor in the first crude alcohol preheater, and enabling the steam condensate water to return to a boiler room after heat exchange; the other path is sent to a second inlet at the upper part of the crude distillation tower I through a branch pipe.
Step 7, allowing the top alcohol vapor of the rectifying tower I to enter a reboiler of a crude tower II to heat the composite tower, feeding one path of heated alcohol condensate into a second inlet at the top of the composite tower through a reflux pump of the rectifying tower I, and feeding the other path of heated alcohol condensate into an upper feed inlet of the rectifying tower I through a bypass pipe for reflux;
step 8, collecting part of fusel oil from the middle outlet of the rectifying tower I, feeding the fusel oil into a fusel oil separator, feeding the fusel oil separated in the fusel oil separator to a storage tank, and feeding light wine of the fusel oil separator into a third inlet of the crude alcohol tank;
step 9, steam from a boiler enters a reboiler of a fine tower I through a steam pipeline to heat a rectifying tower I, heated steam condensate enters a condensate distributor, one path of the steam condensate in the condensate distributor heats crude alcohol in a first crude alcohol preheater, the other path of the steam condensate in the condensate distributor heats fusel wine in a second crude alcohol preheater, and two paths of the heated steam condensate return to a boiler room;
wherein the temperature of the steam from the boiler is 168 ℃ and the pressure is 0.66 Mpa; the bottom temperature of the crude distillation tower I is 82 ℃, and the top temperature is 68 ℃; the bottom temperature of the composite tower is 113 ℃, and the top temperature is 89 ℃; the temperature of the bottom of the rectifying tower I is 155 ℃, and the temperature of the top of the rectifying tower I is 120 ℃.
Although the invention has been described in detail in this specification with reference to specific embodiments and illustrative embodiments, it will be apparent to those skilled in the art that certain changes and modifications can be made therein without departing from the scope of the invention. Therefore, such modifications and improvements are intended to be within the scope of the invention as claimed.
Claims (5)
1. Energy-conserving system of distillation of carbon monoxide system ethanol is characterized by, includes: a clear mash primary preheater (1), a clear mash secondary preheater (2), a clear mash tertiary preheater (3), a thick mash primary preheater (4), a thick mash secondary preheater (5), and a first CO2A separator (6), a crude distillation tower I (7), a crude distillation tower I condenser (8), a scrubbing tower (9), a crude alcohol tank (10), a crude tower I reboiler (11), and second CO2Separator (12), composite tower (13), crude tower II reboiler (14), first crude alcohol preheater (15), second crude alcohol preheater (16), rectifying tower I (17), rectifying tower I reboiler (18), fusel oil separator (19), condensingA water-binding distributor (20), a refined tower II reflux pump (21), a crude alcohol pump (22), a refined tower I reflux pump (23) and a refined tower II material passing pump (24);
a clear mash primary preheater (1), a clear mash secondary preheater (2), a clear mash tertiary preheater (3) and a first CO which are connected in series in sequence through tube passes2A separator (6); wherein, the pipe side inlet of the clear mash primary preheater (1) is communicated with the fermented clear mash raw material inlet; the first CO2A mash outlet at the bottom of the separator (6) is communicated with a feed inlet of a composite tower (13), and the composite tower (13) consists of a rough distillation tower II and a rectification tower II; the first CO2The top gas outlet of the separator (6) is communicated with the gas inlet at the bottom of the side wall of the scrubbing tower (9);
a shell pass inlet of the clear mash primary preheater (1) is connected to a dehydration section, and a shell pass outlet of the clear mash primary preheater (1) is communicated with an inlet of a cooler; a shell pass inlet of the clear mash secondary preheater (2) is communicated with a bottom outlet of the composite tower (13), and a shell pass outlet of the clear mash secondary preheater (2) is connected to a fermentation section;
the top outlet of the composite tower (13) is communicated with the shell pass inlet of a reboiler (11) of a crude tower I, and the shell pass outlet of the reboiler (11) of the crude tower I is communicated with the first top inlet of the composite tower (13) through a reflux pump (21) of a fine tower II; the tube side of the reboiler (11) of the crude tower I forms closed cycle with the bottom outlet of the crude distillation tower I (7) through a pump;
the middle outlet of the compound tower (13) is communicated with the first inlet of a second crude alcohol preheater (16) through a material passing pump (24) of a rectifying tower II, and the first outlet of the second crude alcohol preheater (16) is communicated with the first inlet of the middle of a rectifying tower I (17);
the top outlet of the rectifying tower I (17) is communicated with the shell pass inlet of a crude tower II reboiler (14), the shell pass outlet of the crude tower II reboiler (14) is communicated with the inlet of a reflux pump (23) of the refined tower I, and the tube pass of the crude tower II reboiler (14) forms closed cycle with the bottom outlet of the composite tower (13) through a pump; an outlet of the reflux pump (23) of the fine tower I is communicated with a second inlet at the top of the compound tower (13);
an outlet in the middle of the rectifying tower I (17) is communicated with an inlet of a fusel oil separator (19), and a fusel oil outlet of the fusel oil separator (19) is communicated with a fusel oil storage tank; an outlet at the bottom of the rectifying tower I (17) is communicated with a shell pass inlet of the clear mash three-stage preheater (3), and a shell pass outlet of the clear mash three-stage preheater (3) is connected to a fermentation working section;
an outlet at the bottom of the rectifying tower I (17) forms closed cycle with a tube pass of a reboiler (18) of the rectifying tower I through a pump, a shell pass inlet of the reboiler (18) of the rectifying tower I is communicated with a steam pipeline, and a shell pass outlet of the reboiler (18) of the rectifying tower I is communicated with a water inlet of a condensed water distributor (20);
a first outlet of the condensed water distributor (20) is communicated with a second inlet of the first crude alcohol preheater (15), and a second outlet of the first crude alcohol preheater (15) is communicated to a boiler room through a pipeline; a second outlet of the condensed water distributor (20) is communicated with a second inlet of a second crude alcohol preheater (16), and a second outlet of the second crude alcohol preheater (16) is communicated to a boiler room through a pipeline;
a thick mash primary preheater (4), a thick mash secondary preheater (5) and a second CO sequentially connected in series through a tube pass2A separator (12); wherein, the tube side inlet of the thick mash primary preheater (4) is communicated with the raw material inlet of the thick mash to be fermented; the second CO2The bottom liquid outlet of the separator (12) is communicated with the upper first inlet of the crude distillation tower I (7), and the second CO is2The top gas outlet of the separator (12) is communicated with the gas inlet at the bottom of the side wall of the scrubbing tower (9);
a shell pass inlet of the thick mash secondary preheater (5) is communicated with a vinasse outlet at the bottom of the coarse distillation tower I (7), and a shell pass outlet of the thick mash secondary preheater (5) is connected to a feed workshop;
the top wine vapor outlet of the coarse distillation tower I (7) is communicated with the shell pass inlet of the thick mash primary preheater (4), the shell pass outlet of the thick mash primary preheater (4) is communicated with the shell pass inlet of the coarse distillation tower I condenser (8), and the shell pass outlet of the coarse distillation tower I condenser (8) is communicated with the air inlet at the bottom of the side wall of the scrubbing tower (9);
a water inlet at the top of the scrubbing tower (9) is communicated with a water supply device; a gas outlet at the top of the gas scrubbing tower (9) is communicated with a vacuum pump; a light wine outlet at the bottom of the scrubbing tower (9) is communicated with a condensed crude wine outlet of a condenser (8) of the coarse distillation tower I and a condensed crude wine outlet of a thick mash primary preheater (4) through pipelines and a first inlet of a crude alcohol tank (10);
the second inlet of the crude alcohol tank (10) is communicated with a dehydrated light wine pipeline, and the third inlet of the crude alcohol tank (10) is communicated with a light wine outlet of the fusel oil separator (19); the bottom outlet of the crude alcohol tank (10) is communicated with the inlet of a crude alcohol pump (22);
the outlet of the crude alcohol pump (22) is communicated with the first inlet of the first crude alcohol preheater (15); and a first outlet of the first crude alcohol preheater (15) is communicated with a second inlet in the middle of the rectifying tower I (17).
2. The distillation energy-saving system for preparing ethanol from carbon monoxide is characterized in that a top outlet of the composite tower (13) is communicated to a dehydration section through a bypass pipe.
3. The energy-saving system for distillation of carbon monoxide to ethanol as claimed in claim 1, wherein the outlet of the crude alcohol pump (22) is connected to the second inlet at the upper part of the crude distillation column I (7) through a branch pipe.
4. The distillation energy-saving system for preparing ethanol from carbon monoxide according to claim 1, wherein an outlet of the reflux pump (23) of the rectifying tower I is communicated with an upper feed inlet of the rectifying tower I (17) through a bypass pipe.
5. The energy-saving distillation system for preparing ethanol from carbon monoxide as claimed in claim 1, wherein the temperature of the steam from the boiler is 160-180 ℃ and the pressure is 0.5-0.7 Mpa; the bottom temperature of the crude distillation tower I is 80-84 ℃, and the top temperature is 65-71 ℃; the bottom temperature of the composite tower is 110-116 ℃, and the top temperature is 85-93 ℃; the bottom temperature of the rectifying tower I is 150-160 ℃, and the top temperature is 115-125 ℃.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
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