DE102007001614A1 - Energy self-sufficient method for manufacturing bioethanol from lignocellulose, protein, starchy or sugary additional material, involves disintegrating additional material, and obtaining raw slurry from disintegrated additional material - Google Patents

Abstract

The The invention relates to an energy self-sufficient process for the production of bioethanol from lignocellulose, protein and starch and / or sugary feeds by crushing and mashing the starting materials, followed by fermentation under Use of fermentation yeast and distillative separation of bioethanol from the sour mash, in which the crushing of the starting materials (16) to particle sizes smaller than 2.5 mm made from the comminuted feedstocks (16) and essential parts of the Schlempewasers generated in the process (1) the Rohmic (2) is obtained from the obtained in this way Rohmic (2) with the addition of liquefaction and saccharification enzymes (3, 4) Sweet Mash (5) is made out of the sweet mash (5) by adding fermented yeast (6) Sour mashes (7) obtained from a phase separation (8) in Dicksauermaische (9) and Dünnsauermaische (10) is subjected to the Dünnsauermaische (10) by means of distillation apparatus (11) and capacitors (12) in Ethanol (13) and Schlempewasser (1) is separated and the Dicksauermaische (9) is fed to a methanation stage (14).

Description

The The invention relates to an energy self-sufficient process for the production of bioethanol from lignocellulose, protein and starch and / or sugary feeds by crushing and mashing the starting materials, followed by fermentation under Use of fermentation yeast and distillative separation of bioethanol from the sour mash. Such a method is for the extraction of ethanol-based petrol and diesel fuels and ethanol-based heating fuels needed.

method for the self-sufficient production of bioethanol from lignocellulose, Protein and starch and / or sugar-containing ingredients have not been made public so far.

To The prior art has technical solutions published with the help of which substantial portions of the bioethanol production needed process energy from the predominantly dissolved biogenic constituents of the resulting in the distillation process Mud are obtained by means of methane fermentation.

So will in the DE 3007 138 C2 discloses a process for the production of ethanol, which undergoes a special fermentation process, the so-called sweet mash in the presence of yeasts and then dividing the fermentation liquor in a Hefekonzentrat- and yeast-free flow. While the yeast-free flow is evaporated to recover ethanol, the yeast concentrate flow is to be recycled back to the fermentation process. It is assumed here that the yeast-free variety of the fermentation product already has the quality of a target-oriented sour mash and has no unfermented portions of the amounts of starch and / or sugar used.

An advanced technical solution will be available with the DE 103 27 954 A1 made known. The improved process described therein for the production of ethanol from biomass envisages comminuting the biomass used as finely as possible to particle sizes of less than 1 mm, then using the comminuted biomass as the medium for the fermentation and recovering the ethanol from the fermented aqueous solution , The proteins contained in the biomass used and the optionally present bran should be separated either before the fermentation or before the ethanol production. In a special process variant, the ethanol-containing fermentation substrate depleted of bran and proteins is to be distilled and thereby separated into ethanol and into an ethanol-free vinasse. This vinasse should be separated into a solid and a clear phase.

While the recovered solid phase before or after a drying process as Additional feed used for animal nutrition is to be used, the recovered clear phase of methane extraction in one High-performance methane reactor. The recoverable methane can be used for reduction the foreign energy use are used. Despite the complex process technology with a number of over the known prior art additional steps will neither dependency from the feed material utilization of seizure products the Ethanol production eliminates the desired independence achieved by external energy use.

This limits the use of the known methods unchanged on energetically sufficiently developed locations on the one hand and on production sites that provide a logistical link to animal producers if not the additional use of external energy for the basic production of protein-rich Dried fodder is to be accepted.

The The object of the invention is therefore to create a technical Solution, with the help of which the shortcomings of the known State of the art are overcome. In particular, will a technical solution needed that with few and simple process steps the cost-effective and self-sufficient ethanol production. Furthermore should for ethanol production predominantly the largely proven and technically mature apparatus technology continues can be used.

The The object is achieved by the features of claim 1. Advantageous embodiments of inventive technical solution are described in the subclaims.

After that bioethanol is made from lignocellulose in an energy self-sufficient process, protein as well as starch and / or sugar-containing starting materials by crushing and mashing the feedstocks, subsequent Fermenting using fermentation yeasts and distillatives Separating the bioethanol made from the sour mash.

The Comminution of the starting materials is made so that the resulting Particle sizes maximum 2.5 mm.

Out the crushed feedstocks and essential parts of the Process generated Schlempewasers then becomes the Rohmische won.

Out the Rohmic obtained in this way is added with the addition of Liquefaction and saccharification enzymes produced.

In Another step will be the sweetmeat Sour mashes undergo a phase separation, in addition to the filter cake as Dicksauermaische a filtrate as Dünnsauermaische arises.

The resulting Dünnsauermaische is subsequently by means of Distillation apparatus and downstream condensers in ethanol and Schlempewasser separated.

The in the phase separation separated Dicksauermaische becomes the purpose the extraction of biomethane for the production of process energy in a cogeneration unit of a parallel operated methanation stage fed.

advantageously, the comminution of the starting materials by wet hammer mill technology, using twin-screw shredders, peeling mills the type Jäckering, pin mills, air flow roller mills and performed the same.

In a preferred process variant is the crushed feedstocks at least part of the lignocellulosome already before the further treatment deprived of gross parts. This relieves the subsequent process stages in considerable measure.

A preferred embodiment of the method provides to be mashed Parts of the starting materials to suspend 4 to 8 parts by mass the suspending medium from process water and Schlempewasser mixed with one part by mass of the comminuted starting materials become. It is envisaged that between 30 and 100% of the amount of Suspendiermediums be used as Schlempewasser.

In Another variant of the method is called process water The condensate from distilled Schlempewasser used.

Farther is provided, the extracted sour mash by means of hydrocyclones and / or filter screw presses and / or decanters in Dicksauermaische and Dünnsauermaische separate.

In order to It is possible that of cellulosic and high protein Ingredients enriched Dünnsauermaische in an upstream Capacitor for cooling the leaving the distillation apparatus Using mixtures of water and alcohol vapor, being not only Cooling energy by avoiding the use of cooling water for the cooling of the water and alcohol vapor mixture, but also heat energy through the avoided use of thermal energy for preheating the Dünnsauermaische is saved.

It is still possible in the distillation apparatus as Schlempewasser accumulating sump product completely as Suspending agent for the production of Rohmaische in the process to use.

About that In addition, it can be obtained as Schlempewasser Bottom product also at least partially for the recovery of process water use, for the extraction of low-salt process water and high-salt concentrate from the Scjlempewasser a vacuum circulation evaporation plant, a microfiltration, ultrafiltration, nanofiltration and Reverse osmosis and / or membrane techniques are used.

The for example, incurred in the vacuum circulation evaporation sour Concentrate is beneficial for pH regulation to be used in the preparation of the yeast batch.

Intended Finally, it is also that in the methanation stage a wet fermentation of the suspended Dicksauermaische in the presence of a mesophilic bacterial culture becomes. The largely consistent quality of the used Dicksauermaische also makes it possible for the bio-suspension for the methanation process more lignocellulosic Feedstocks, for example grain cleaning residues or chopped straw.

The Advantages of the invention are summarized in that for the plant operation no use of energy from fossil or nuclear sources is needed. At more complete Use of the energy-saving potential of the invention Process design can also be considerable Amounts of excess electrical and thermal Energy to external consumers.

Furthermore become significant through the use of Dünnsauermaische in the distillation process longer travel times for the equipment used between the required technological cleaning processes achieved, which significantly increases plant availability becomes.

Due to the lower protein content in the Dünnsauermaische are found in Schlempewasser reduced protein content, whereby the risk of contamination of the heat exchangers used is reduced. Only in this way is the prerequisite created in many cases to be able to dispense with the direct heating of the still by means of steam injection. A decisive advantage of the process according to the invention results not least from the fact that the recovery of aqueous condensates as a reusable low-salt process water from the ammonium poor Schlempewasser is much easier to realize than obtaining qualitatively similar media from the high-ammonia biofilms of the biomethanization process. As a result, highest recycling rates on the one hand and minimized demands on the provision of drinking water or service water for bioethanol production on the other hand can be achieved.

The Invention will be described below with exemplary embodiments be explained.

In the attached drawing show:

1 : the schematic representation of the process stages of ethanol production from Dünnsauermaische and the direct use of the resulting in the distillation of Dünnsauermaische Schlempewasser in the Süßmaischeherstellung;

2 : the schematic representation of the process stages of ethanol production from Dünnsauermaische and the recycling of incurred in the distillation of Dünnsauermaische Schlempewasser in process water and concentrate;

Embodiment 1

According to the 1 are in a plant for the production of bioethanol 13 every 3 t of starting material 16 in the form of wheat with 13 m ^{3 of} aqueous suspending agent 20 at a temperature between 40 and 55 ° C in a wet hammer mill as a crushing stage 15 crushed to a particle size of less than 2.0 mm.

The generated Rohmic 2 become liquefaction enzymes 3 and a first part of saccharification enzymes 4 added.

The Roemma 2 gets into a mash station 22 with a first retention tank as a heated stirred tank in which the Rohmische 2 is heated to at least 75 ° C. The mean residence time of the mash in the first dwell of the mash station 22 is between 1.5 and 2 hours. The energy input into the first dwell is carried out by the second dessicant sweetened fish 5 with a temperature of about 90 ° C and, if necessary, by hot water with a temperature of 115 ° C from the machine cooling of a cogeneration plant operated in parallel with biomethane.

The partially saccharified Rohmic 2 arrives after leaving the first dwell in the second residence, which is also designed as a heated stirred tank. The mean residence time of the mash in the second residence tank is also between 1.5 and 2 hours. In the second dwell the temperature of the mash is raised to about 90 ° C. The heating medium used for this is the distillation apparatus 11 leaving Schlempewasser 1 with a temperature between 80 and 90 ° C and, if necessary, hot water at a temperature of 115 ° C from the machine cooling of a cogeneration plant operated in parallel with biomethane.

The sweet mash leaving the second mash container 5 is passed through a heater in the first retention tank and enters an unheated pump tank.

From this container is the obtained sweet mash 5 taken at a temperature of about 70 ° C, cooled in a heat exchanger using process and / or cooling water to a temperature of less than 35 ° C and optionally the yeast approach vessel 23 for obtaining the yeast batch for the subsequent fermentation process and the current fermentation process using the previously obtained yeast approach supplied.

Fermentation tanks are used for the fermentation process 24 used with a useful volume of 125 m ³ each. In the fermentation tanks 24 In the course of the fermentation time selected between 36 and 72 hours, the sugar-containing extract of the sweet mash 5 fermented with simultaneous release of carbon dioxide to alcohol. The resulting heat of reaction is dissipated by external wall cooling. The resulting sour mash 7 has after completion of the selected fermentation on average an alcohol content between 6.5 and 8 vol .-% and a pH of about 3.7.

It is fed to the so-called beer tank, from which the sour mash 7 to a continuously operated phase separation station 8th arrives. For phase separation 8th a filter screw press is used. This is called Dicksauermaische 9 obtained a filter cake with dry matter contents between 29 and 31% by mass, directly into the hydrolysis of a parallel operated methanation 14 arrives. The filter cake consists of a lignocellulosic and protein-rich dry matter and an alcoholic filtrate.

That at the phase separation 8th resulting filtrate passes into a settling tank designed as a thickener, in which an average residence time of at least 8 hours is ensured. The resulting sediment is removed from the settling tank and also the phase separation 8th fed. The aqueous supernatant obtained in the settling tank passes as Dünnsauermaische 10 to the distillation apparatus 11 , This is the Dünnsauermaische 10 first one to the distillation apparatus 11 fed directly downstream heat exchanger, whereby the Dünnsauermaische 10 is heated from an average of 28 ° C to over 50 ° C.

Then the Dünnsauermaische arrives 10 in another heat exchanger, with the help of which part of the sensible heat of the distillation apparatus 11 removed Schlempewasers 1 with a temperature of at least 80 ° C on the Dünnsauermaische 10 is transmitted. Then reaches the heated to at least 60 ° C Dünnsauermaische 10 above the struts in the distillation apparatus 11 , which is operated as a vacuum column with a top pressure of about 0.5 bar.

The recovered from the steam / alcohol vapor mixture 19 bioethanol 13 is with an ethanol concentration of more than 93% by volume of the distillation station 11 taken in a volume of between 900 and 1100 liters per hour as energy alcohol.

Thereafter, the alcohol-depleted part of the used Dünnsauermaische passes 10 into the column swamp, from where this part as Schlempewasser 1 the still 11 is removed. First, the Schlempewasser serves 1 however, as a means of transport for the distillation apparatus 11 to be supplied thermal energy by being passed through an external heat exchanger for the indirect supply of heat from the hot water cycle of biomethane-powered cogeneration plant.

On selected bottoms of the still 11 removed fusel oils get like the filter cake of the phase separation station 8th into the hydrolysis station of the parallel operated methanation stage 14 ,

The Schlempewasser arising in the distillation station 1 having a temperature of at least 80 ° C is used as an energy carrier and as a suspending agent 20 for the production of the Rohmic 2 provided.

Embodiment 2:

As in Example 1, according to the 2 using triticale Rohmic 2 , Sweet mash 5 , Sour mashed 7 , Carbon dioxide, Dünnsauermaische 10 , Bioethanol 13 and Schlempewasser 1 produced. For the production of the Rohmic 2 becomes a twin-screw fiberizer in the crushing stage 15 used. The dry fiber with a maximum grain size of 1.5 mm is then mixed with a suspending agent 20 suspended, exclusively from untreated Schlempewasser 1 and consists of condensates consisting of evaporated Schlempewasser 1 were won. In this way, salt concentrations in the suspending agent become 20 avoided, which could significantly affect the yeast fermentation process.

1

Schlempewasser

2

Rohmaische

3

liquefying enzyme

4

Saccharifying

5

Süßmaische

6

lees

7

sour mash

8th

phase separation

9

Dick Auer mash

10

Auer thin mash

11

distillation apparatus

12

capacitor

13

ethanol

14

methanation

15

crushing stage

16

feedstock

17

lignocellulosic coarse particles

18

process water

19

mixture from water and alcohol vapor

20

suspending

21

concentrate

22

mash station

23

Hefeansatzgefäß

24

fermenter

25

ethanol tank

QUOTES INCLUDE IN THE DESCRIPTION

This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Cited patent literature

• - DE 3007138 C2 [0004]
• - DE 10327954 A1 [0005]

Claims (14)

Self-sufficient process for the production of bioethanol from lignocellulosic, protein as well as starch and / or sugar-containing feedstocks by crushing and mashing the feedstocks, subsequent fermentation using fermentation yeast and distillative separation of the bioethanol from the sour mash, characterized in that the comminution of the starting materials ( 16 ) is made to particle sizes smaller than 2.5 mm that from the shredded feedstocks ( 16 ) and essential parts of the Schlempewassers ( 1 ) the Rohmic ( 2 ) obtained from the Rohmic ( 2 ) with the addition of liquefaction and saccharification enzymes ( 3 . 4 ) Sweet mash ( 5 ), that from the sweet mash ( 5 ) by adding fermentation yeast ( 6 ) sourermaische ( 7 ) a phase separation ( 8th ) in Dicksauermaische ( 9 ) and Dünnsauermaische ( 10 ) that the Dünnsauermaische ( 10 ) by means of a distillation apparatus ( 11 ) and capacitors ( 12 ) in ethanol ( 13 ) and Schlempewasser ( 1 ) and that the Dicksauermaische ( 9 ) of a methanation stage ( 14 ) is supplied. Energy-autonomous process for the production of bioethanol according to claim 1, characterized in that the comminution ( 15 ) of the starting materials ( 16 ) is carried out by wet hammer mill technology. Energy-autonomous process for the production of bioethanol according to claim 1, characterized in that the comminution ( 15 ) of the starting materials ( 16 ) by means of twin-screw shredders, peeling mills of the Jäckering type, pin mills, air flow roller mills and the like. Like. Is performed. Energy-autonomous process for producing bioethanol according to one of claims 1 to 3, characterized in that the comminuted feedstocks ( 16 ) before the further treatment lignocellulose-rich coarse particles ( 17 ) are withdrawn. Energy-autonomous process for producing bioethanol according to one of claims 1 to 4, characterized in that the proportions of the feedstocks to be mashed ( 16 ) with 4 to 8 parts by weight of suspending medium from process water ( 18 ) and Schlempewasser ( 1 ) per 1 part by weight of starting materials ( 16 ) are mixed. Energy-autonomous process for the production of bioethanol according to claim 5, characterized in that between 30 and 100% of the amount of the suspending medium as Schlempewasser ( 1 ) are used. Energy-autonomous process for the production of bioethanol according to claim 5, characterized in that as process water ( 18 ) the condensate from distilled Schlempewasser ( 1 ) is used. Energy-autonomous process for the production of bioethanol according to one of claims 1 to 7, characterized in that the recovered sour mash ( 7 ) by means of hydrocyclones and / or filter screw presses and / or decanters in Dicksauermaische ( 9 ) and Dünnsauermaische ( 10 ) is separated. Energy-autonomous process for producing bioethanol according to one of claims 1 to 8, characterized in that the cellulosic and protein-rich constituents depleted Dünnsauermaische ( 10 ) in an upstream capacitor ( 12 ) for cooling the distillation apparatus ( 11 ) leaving the mixture ( 19 ) is used from water and alcohol vapor. Energy-autonomous process for the production of bioethanol according to one of claims 1 to 9, characterized in that in the distillation apparatus ( 11 ) as Schlempewasser ( 1 ) completely obtained as a suspending agent ( 20 ) for the production of the Rohmic ( 2 ) is being used. Energy-autonomous process for the production of bioethanol according to one of claims 1 to 9, characterized in that in the distillation apparatus ( 11 ) as Schlempewasser ( 1 ) at least partially for the recovery of process water ( 18 ) is being used. Energy-autonomous process for the production of bioethanol according to claim 11, characterized in that for the recovery of process water ( 18 ) and concentrate ( 22 ) from the Schlempewasser ( 1 ) a vacuum circulation evaporation plant and / or microfiltration, ultrafiltration, nanofiltration and reverse osmosis and membrane techniques are used. Energy-autonomous process for the production of bioethanol according to claim 12, characterized in that the acidic concentrate obtained during the vacuum evaporation ( 22 ) is used for pH regulation in the preparation of the yeast batch. Energy-autonomous process for the production of bioethanol according to one of claims 1 to 7, characterized in that in the methanisis level ( 14 ) a wet fermentation is carried out in the presence of a mesophilic bacterial culture.