• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    Procedure for obtaining pure butanol. The present invention relates to a process for obtaining pure butanol in the lower part of a first distillation column from a fermentation broth comprising butanol, water, ethanol and acetone. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2681121A2
    申请号:ES201730303
    申请日:2017-03-08
    公开日:2018-09-11
    发明作者:Carlos BLÁZQUEZ ESCUDERO；Concepción HIDALGO CANDAU；Patricia BLÁZQUEZ ELENA；Emilia SASTRE GARCÍA；Elena CACHAZA GIANZO；Juan Luis RAMOS MARTÍN
    申请人:Abengoa Research SL；
    IPC主号:
    专利说明:

    5
    10
    fifteen
    twenty
    25
    30
    35
    PROCEDURE FOR OBTAINING PURE BUTANOL DESCRIPTION
    The present invention relates to a process for obtaining pure butanol in the lower part of a first distillation column from a fermentation broth comprising butanol, water, ethanol and acetone.
    Therefore, the invention could be framed in the field of industrial use of by-products and their recovery.
    STATE OF THE TECHNIQUE
    The concentration of butanol in fermentation broths is less than 2%, so its recovery by classical techniques is very expensive energy. Different distillation schemes have been proposed for the separation of butanol, however, their energy consumption is high.
    In the documents ["Synthesis and design of new hybrid configurations for biobutanol purification” Massimiliano Errico et al., Computers and Chemical Engineering 84 (2016) 482-493] and ["Extractive Fermentation of Acetone and Butanol: Process Design and Economic Evaluation” Steven Roffler et al., Biotechnology progress, Volume 3, Issue 3 (1987) 131-140] describe different configurations consisting of 5 distillation columns and a decanter at the end of the process for the purification of biobutanol obtained from the acetone-butanol process. ethanol (ABE) with an energy expenditure of more than 22 MJ / kg of recovered butanol.
    One of the embodiments described in the document "Evaluation of Different Process Designs for Biobutanol Production from Sugarcane Molasses" Abraham Blignault van der Merwe, Thesis (2010), University of Stellenboschse] describes a configuration comprising 4 distillation columns and with which a 99.9% purity butanol is obtained and 95.6% of the total butanol is recovered.In this configuration the ethanol is not recovered, it is treated as a waste.
    The use of decanters in intermediate steps of biobutanol recovery processes has already been described previously in the literature as an improvement in
    2
    5
    10
    fifteen
    twenty
    25
    30
    35
    Pure butanol recovery procedure by distillation. However, it focuses on the purification of butanol only.
    For example, in the document ["Process Alternatives for Biobutanol Purification: Design and Optimization" Eduardo Sánchez-Ramírez et al., Ind. Eng. Chem. Res., 54 (2015) 351,358], specifically in one of its embodiments, it is described a configuration with four distillation columns and a decanter but in which only butanol can be purified, a similar configuration is described in WO2009013160.
    Therefore, it is necessary to continue developing pure butanol recovery processes from more efficient fermentation broths and whose by-products can be recovered.
    DESCRIPTION OF THE INVENTION
    The method of recovery of butanol from a fermentation broth object of the present invention consists of a train of separation columns (distillation) integrated with a liquid-liquid separation stage (decantation). The main advantage of the invention lies in the location of the liquid-liquid separation (decantation) stage. In the present invention, the liquid-liquid separation step, whose main object is the breakage of the butanol-water azeotrope, is located integrated in the second distillation column called feed distillation column or Feed Stripping Column (FSC) in English. The main advantage of the present invention is the simplification of the distillation train, the decrease in the size of the associated equipment, as well as the decrease in energy consumption.
    Therefore, in a first aspect, the present invention relates to a process for obtaining pure butanol in the lower part of a first distillation column from a fermentation broth comprising butanol, water, ethanol and acetone, wherein said Procedure comprises the following stages:
    to. separating a stream of fermentation broth into a stream comprising a first initial stream formed by the azeotrope formed by butanol and water and a second initial stream comprising ethanol and acetone, said separation is carried out by distillation at a pressure of 0 , 5 bar at 1 bar and a temperature of 40 ° C to 135 ° C in a first distillation column;
    5
    10
    fifteen
    twenty
    25
    30
    35
    b. decanting the first initial stream comprising the azeotrope formed by butanol and the water obtained in step (a) at a pressure of 0.5 bar at 1 bar and a temperature of 40 ° C to 135 ° C in a two stream decanter Decanting: the first settling stream rich in butanol and a second settling stream rich in water and poor in butanol
    C. reintroduce, in the lower part of the distillation column of step (a), the first liquid stream of decanting rich in butanol obtained in step (b).
    d. separating the second stream rich in water and poor in butanol obtained in step (b) in two liquid streams a first distillation stream rich in butanol and poor in water, and a second distillation stream rich in water and poor in butanol , said separation is carried out by distillation at a pressure of 0.5 bar at 1 bar and a temperature of 40 ° C to 135 ° Cen a second distillation column and introducing a stream of steam into said column;
    and. reintroduce at the top of the first distillation column the first liquid stream of distillation rich in butanol and poor in water obtained in step (d) and
    F. extract the pure butanol stream from the bottom of the first distillation column.
    In the present invention the "fermentation broth" is obtained by fermentation of sugars. It is possible to use broths obtained from different sugars and fermentation processes provided that the final broth contains acetone, ethanol and butanol. Generally, acetone, ethanol and butanol is in the concentrations indicated below:
    • Acetone 0.1% w / w - 15% w / w
    • Ethanol 0.1% w / w - 5% w / w
    • Butanol 0.1% w / w - 22% w / w
    In the present invention, "azeotrope" is understood as that liquid consisting of two or more miscible liquids whose boiling point is constant and which behaves as if it were a single component. In this case, butanol and water form a azeotrope that has a boiling point range between 100 ° C and 118 ° C.
    5
    10
    fifteen
    twenty
    25
    30
    35
    Step (a) of the process of the present invention serves to separate the mixture of butanol, water, acetone and ethanol present in the free solid fermentation broth stream separated at a previous stage into two initial streams, a first initial stream of butanol and water forming an azeotrope and a second initial stream of ethanol and acetone. In that same distillation column, specifically in the lower part of the first distillation column, more pure and water-free butanol is accumulating.
    In the decantation stage (b) of the process of the present invention, a decanter is incorporated into the first distillation column described in (a), specifically at the height in which there is a distillation plate where the concentration of acetone and ethanol is so low. that can be separated into two liquid phases by breaking the heterogeneous azeotrope between butanol and water. The concentration of acetone should not exceed a value between 0.05% - 0.5%, the concentration of ethanol a value between 1% - 4%. Two settling streams are obtained: the first settling stream rich in butanol and a second settling stream rich in water and poor in butanol.
    In step (c) of the process of the present invention, the first butane-rich liquid decantation stream obtained from the stage (b) decanter is reintroduced into the lower part of the first column (also called the depletion section) obtaining high purity butanol.
    In step (d) of the process of the present invention, the second water stream rich in water and poor in butanol, obtained in step (b), is taken to a second distillation column to thereby separate two liquid streams a first stream of distillation rich in butanol and poor in water, and a second distillation stream rich in water and poor in butanol.
    In step (e) of the process of the present invention, the first liquid distillation stream rich in butanol is redirected to the top of the first distillation column.
    The last stage of the process, step (f), refers to the extraction of the pure butanol stream from the bottom of the first distillation column.
    5
    5
    10
    fifteen
    twenty
    25
    30
    35
    In a preferred embodiment, the process of the present invention comprises the following steps prior to step (a):
    to'. Separate dissolved solids in a fermentation stream comprising butanol, solids and water by distillation at a pressure of 0.5 bar at 1 bar and a temperature of 40 ° C to 135 ° C b ’. introduce the stream comprising butanol, acetone, ethanol and water obtained in step (a ’) in the first distillation column.
    In said embodiment, the solids contained in the fermentation broth are separated from it by evaporation, providing the heat required to evaporate the fermentation broth in the boiler and obtaining the solids from the bottom of the column (step (a ')). In said preferred embodiment a stream is obtained comprising butanol, acetone, ethanol and water which is introduced into the first distillation column.
    In another preferred embodiment, the process of the present invention comprises the following additional steps of separation of acetone and ethanol from the second initial stream comprising the following steps:
    to''. separating the second initial stream of acetone and ethanol obtained in the distillation column of step (a) in two streams: a first stream, rich in acetone, and a second stream, rich in ethanol, said separation is carried out by distillation at a pressure of 0.5 bar at 1 bar and a temperature of 40 ° C to 135 ° C in a third distillation column;
    b ’’. extract the first stream of pure acetone from the top of the third distillation column,
    C''. optionally purify the second stream, rich in ethanol obtained in step (a ’) using molecular sieves, and
    d ''. extract the ethanol stream obtained in stage b '' or in stage c ''.
    Throughout the description and the claims the word "comprises" and its variants are not intended to exclude other technical characteristics, additives, components or steps. For those skilled in the art, other objects, advantages and features of the invention will be derived partly from the description and partly from the practice of the invention. The following examples and figures are provided by way of illustration, and are not intended to be limiting of the present invention.
    6
    5
    10
    fifteen
    twenty
    25
    30
    35
    BRIEF DESCRIPTION OF THE FIGURES
    FIG. 1 Obtaining Butanol with a decantation integrated in the distillation train.
    FIG. 2 Ternary diagram for feeding the decanter of example 1.
    FIG. 3. Distillation scheme with particular example of the concentrations in each of the streams for obtaining butanol of the present invention.
    FIG. 4 Distillation scheme for obtaining butanol with a classic configuration of five distillation columns.
    Fig. 5 Distillation scheme for obtaining butanol with another configuration of five distillation columns, with separation of acetone and butanol in the same column.
    EXAMPLES
    The invention will now be illustrated by tests carried out by the inventors, which show the effectiveness of the product of the invention.
    Example 1: Obtaining Butanol with a decantation integrated in the distillation train.
    A mixed stream of fermentation outlet (1) with 0.61% (by weight) of butanol and another mixture of ABE-water solvents (2) containing 23.76% w / w butanol (table 1). Stream 1 is introduced into the first distillation column, column A or stripper A in English, where the solvents are separated from the solids with a separation efficiency of 100%. Solvent recovery per head of column A is 100%. Column A, consists of 30 stages and operates at 0.6 bar and a temperature of 92 ° C in the boiler. The energy consumption of said column is 6.24 MJ / kg of butanol (table 2).
    Table 1 collects the composition data of the feed streams to the process:
     Feeding
     Current 1 Current 2 Current 3
     Temperature, ° C  32.00 32.00 170.00
     Pressure, bar  1.01 1.01 1.01
     Glucose  1559.95 0.00 0.00
     Acetone  437.13 4549.63 0.00
     Butanol  1302.82 8395.13 0.00
     Ethanol  569.98 1078.11 0.00
     Butyric  214.28 0.00 0.00
     Acetic  214.28 0.00 0.00
     Lactic  214.28 0.00 0.00
     Solids no  18248.00 0.00 0.00
     fermentable
     Water  191357.58 21309.48 3000.00
     Total flow, kg / h  214118.30 35332.35 30000.00
    By funds obtained in this first column A 87.10% of the water from the process is recovered, with a purity of 90.2%. This is what we call vinasse since it must be separated from unfermented solids before being reused.
    The stream of heads with 22.40% in butanol, 7.50% in acetone and 9.80% in ethanol, together with the mixed current output of the extraction system (2) with 23.8% 10 of butanol ( Table 1), are introduced in the second distillation column called the feed distillation column, or in English "Feed Stripping Column" and its acronym FSC. This feed distillation column consists of 30 stages and operates at 0.5 bar in heads and a temperature of 132 ° C in the boiler (table 2).
    fifteen
    As mentioned above, the formation of two immiscible phases in stream 2 is expected, but the difference in the composition of water and butanol between the organic phase and the aqueous phase is not large enough to break the azeotrope (Figure 2). The reason for this behavior is the high concentration of acetone 20 in said stream.
    5
    10
    fifteen
    twenty
    25
    30
    35
    When the acetone content is reduced sufficiently, then it is possible to break the heterogeneous butanol-water azeotrope with the phase separation produced by decantation (Figure 3.b). The butanol-rich phase has a 65% (weight) content thereof, while the water-rich phase has a butanol concentration of 10%. The organic phase rich in butanol is returned to the feed distillation column, while the water-rich phase is introduced into a new distillation column (column B or Stripper B in English).
    The extraction stage is that which has such an ethanol-acetone composition, which allows the separation of the current into two phases and breaks the heterogeneous azeotrope between water and butanol. The extraction is carried out in step 20. The operating conditions of the decanter are at 0.6 bar pressure and 79.2 ° C.
    The water-rich stream is introduced in column B where 87.2% of the system water is recovered by funds with a purity of 90.18%. Said column B consists of 40 stages and operates at 0.6 bar in heads and a temperature of 60 ° C in the boiler (table 2). In said column a recovery of 100% (mass) of butanol, and 99.6% (mass) of ethanol is achieved. The azeotropic concentration of butanol at 0.6 bar (46.1% w / w) is obtained per head, which is recirculated to the feed distillation column.
    From the bottoms of the feed distillation column, 99.90% butanol purities (mass) are obtained, the energy consumption in the boiler being 2.72 MJ / Kg of butanol.
    The current obtained by Feed Strip Column heads contains 73.3% (w / w) of acetone and 24.2% (w / w) of ethanol. This current is introduced into a fourth separation column (column C or Stripper C in English) where 99.63% (w / w) of the acetone entering the system is recovered. The column consists of 40 separation stages and operates at 0.5 bar, reaching a temperature of 92 ° C in the boiler.
    Table 2 shows the main operating conditions of each of the columns of the system for example 1.
     Column  Column A Feed distillation column Column B Column C
     No. plates  30.00 30.00 40.00 20.00
     Estimated diameter  3.50 2.90 2.00 0.09
     Condenser temperature, ° C  82.00 31.00 36.00 81.00
     Condenser pressure, bar  0.60 1.00 0.50 0.60
     Boiler temperature, ° C  92.00 132.00 65.00 92.00
     Boiler energy, kJ / kg butanol  6.24 2.72 0.00 0.00
     Total steam flow, kg / h  0.00 0.00 0.00 3000.00
    Table 3 shows the main recoveries obtained in the system for example 1.
     Product streams  % Purity% Recovery
     Acetone  99.93 99.36
     Ethanol  91.58 99.94
     Butanol  98.31 100
     Water  99.99 12.75
     Vinasse  90.19 87.1
    5
    Compared to the traditional separation processes of acetone, butanol, ethanol solutions, this configuration has as its main advantage the simplification of the distillation train, the decrease in the size of the associated equipment, as well as the decrease in energy consumption.
    10 • The equivalent energy requirements for this new configuration
    they are 9.66 MJ / Kg of butanol. As can be seen, this consumption is lower than those reported in previous studies 24.4 MJ / Kg of butanol (Scheme I) or 22.4 MJ / kg of butanol (Scheme II) [Van der Merwe, A.B. et al., Fuel (2013) 105: 451-8].
    • Likewise, this method offers a simplification of the distillation train by reducing the number of columns required to 4 instead of 5.
    5
    10
    fifteen
    twenty
    25
    30
    35
    In a particular example (simulated) the concentrations in each of the streams would be represented by Figure 3.
    Example 2: Obtaining Butanol with a decantation at the end of the distillation train.
    The typical scheme of separation by distillation using 5 towers, is represented in Figure 4. With a configuration where the vinasses are obtained in the bottoms of the first column, while by heads butanol is obtained at a concentration around 40% ( p / p).
    High purity acetone can be obtained from the heads of the second column.
    The bottoms of the second column are fed to a third column for the purification of ethanol.
    The decantation stage is integrated at the end of the butanol purification process, after separating the acetone and / or ethanol from the fermentation broth.
    The aqueous phase of the decanter is fed to a butanol recovery tower, and the organic phase to a final purification tower to obtain butanol.
    The number of plates of towers 1, 2, 3, 4 and 5 are 40, 30, 40, 10 and 10, respectively. The equivalent energy requirements are 24.4 MJ / Kg of butanol.
    Example 3: Obtaining Butanol with a decantation at the end of the distillation train with another typical configuration.
    In the second typical configuration of 5 columns (Figure 5), the vinasses are obtained in the bottoms of the first column, while by heads butanol is obtained at a concentration around 40% (w / w).
    Acetone and ethanol can be obtained from the heads of the second column (Figure 5) and this stream will go to a third column for purification of both.
    eleven
    The bottoms of the second tower are fed directly to the decanter where the aqueous phase of the decanter is fed to a butanol recovery tower, and the organic phase to a final purification tower to obtain butanol.
    The number of plates of towers 1, 2, 3, 4 and 5 are 40, 30, 40, 10 and 10, respectively. The equivalent energy requirements of the configuration scheme shown in Figure 5 are 22.4 MJ / Kg of butanol.
    10 Table 4 shows the main results obtained by this new invention compared to the typical results [Van der Merwe, A.B. et al., Fuel (2013) 105: 451-8].
    Table 4: Comparative data 15
     Results  Invention Example 2 Example 3
     Energy consumption (MJ / kh ButOH)  9.66 24.40 22.40
     Number of columns  4 5 5
    Note that in this calculation of energy consumption in the invention integration and examples 2 and 3 have been taken into account. Therefore, the difference in energy consumption between the invention and examples 2 and 3 is not due solely to the 20 differences In the configuration.
    权利要求:
    Claims (3)
    [1]
    5
    10
    fifteen
    twenty
    25
    30
    35
    1. A process for obtaining pure butanol in the lower part of a first distillation column from a fermentation broth comprising butanol, water, ethanol and acetone, wherein said process comprises the following steps:
    to. separating a stream of fermentation broth into a stream comprising a first initial stream formed by the azeotrope formed by butanol and water and a second initial stream comprising ethanol and acetone, said separation is carried out by distillation at a pressure of 0 , 5 bar at 1 bar and a temperature of 40 ° C to 135 ° C in a first distillation column;
    b. decanting the first initial stream comprising the azeotrope formed by butanol and the water obtained in step (a) at a pressure of 0.5 bar at 1 bar and a temperature of 40 ° C to 135 ° C in a two stream decanter Decanting: the first settling stream rich in butanol and a second settling stream rich in water and poor in butanol;
    C. reintroduce in the lower part of the distillation column of step (a), the first liquid stream of butanol-rich decantation obtained in step (b).
    d. separating the second stream rich in water and poor in butanol obtained in step (b) in two liquid streams a first distillation stream rich in butanol and poor in water, and a second distillation stream rich in water and poor in butanol , said separation is carried out by distillation at a pressure of 0.5 bar at 1 bar and a temperature of 40 ° C to 135 ° C in a second distillation column and introducing a stream of steam into said column; Y
    and. reintroduce at the top of the first distillation column of step (a) the first liquid distillation stream rich in butanol and poor in water obtained in step (d) and
    F. extract the pure butanol stream from the bottom of the first distillation column.
    5
    10
    fifteen
    twenty
    25
    [2]
    2. The method according to claim 1, wherein said method further comprises the following steps prior to step (a):
    to'. separating dissolved solids in a fermentation stream comprising butanol, solids and water by distillation at a pressure of 0.5 bar to 1 bar; and a temperature of 40 ° C to 135 ° C b ’. introduce the stream comprising butanol, acetone, ethanol and water obtained in step (a ’) in the first distillation column.
    [3]
    3. The process according to any of claims 1 or 2, comprising the following additional steps of separation of acetone and ethanol from the second initial stream comprising the following steps;
    to''. separating the second initial stream of acetone and ethanol obtained in the distillation column of step (a) in two streams: a first stream, rich in acetone, and a second stream, rich in ethanol, said separation is carried out by distillation at a pressure of 0.5 bar at 1 bar and a temperature of 40 ° C to 135 ° C in a third distillation column;
    b ’’. extract the first stream of pure acetone from the top of the third distillation column,
    c ". optionally purifying the second stream, rich in ethanol obtained in step (a’ ’) by molecular sieves, and
    d ". extract the ethanol stream obtained in stage b" or in stage c ".
    类似技术:
    公开号 | 公开日 | 专利标题
    US9169186B2|2015-10-27|System and method for continuously producing polyoxymethylene dimethyl ethers
    FI80218C|1990-05-10|Process and plant for purification of a two-component liquid mixture by distillation
    KR20120051695A|2012-05-22|Recovery of butanol from a mixture of butanol, water and an organic extractant
    KR20120039017A|2012-04-24|Recovery of butanol from a mixture of butanol, water and an organic extractant
    AR044617A1|2005-09-21|EXTRACTION METHOD FOR REMOVING IMPURITIES FROM MOTHER SOLUTION IN CARBOXYL ACID SYNTHESIS
    CA2466999A1|2004-12-05|Extraction process for removal of impurities from mother liquor in the synthesis of carboxylic acid
    RU2007144082A|2009-06-10|METHOD FOR PRODUCING ACETIC ACID
    CN106458827B|2021-07-09|Process for purifying benzoic acid
    KR20100125408A|2010-11-30|Purification of acetic acid from wood acetylation process using extraction
    ES2829500T3|2021-06-01|Dividing wall in the ethanol purification process
    CN101074258B|2010-04-21|Method for separating and extracting phytosterin and Vitamin E from soyabean deodorization distillate
    JP6207503B2|2017-10-04|Acetic acid recovery method
    CN203923057U|2014-11-05|Improved Butanol Recycling device
    ES2681121B1|2019-09-16|PROCEDURE FOR OBTAINING PURE BUTANOL
    CN1970530A|2007-05-30|Method for separating and purifying capsaicin compound using membrane separation technology
    BR112018011104B1|2021-03-23|PROCESS TO PURIFY METHYL METHACRYLATE
    JP2009256294A|2009-11-05|Economical process for producing anhydrous alcohol or gasohol using ether solvent
    ES2543441T3|2015-08-19|Crystallization procedure of a water soluble compound
    WO2016080531A1|2016-05-26|Method for concentrating and dehydrating butanol
    CN101987861B|2012-08-22|Method for purifying 7-dehydrocholesterol leftovers
    BR102014032357B1|2021-05-18|system and process for recovering isoamyl alcohol, ethanol and butanol and products thus obtained
    US9828317B2|2017-11-28|Method for purification of alcohols
    AR086134A1|2013-11-20|SEPARATION PROCESS OF REDUCED ENERGY ALCOHOL WITH WATER REMOVAL
    US9403751B2|2016-08-02|Liquid-liquid extraction process for the production of acrylic esters
    CN112707794A|2021-04-27|Method for separating propanol from aqueous phase byproduct of Fischer-Tropsch synthesis
    同族专利:
    公开号 | 公开日
    ES2681121R1|2018-11-13|
    ES2681121B1|2019-09-16|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US20080015395A1|2006-06-16|2008-01-17|D Amore Michael B|Process for making butenes from aqueous 1-butanol|
    US20140142352A1|2012-11-20|2014-05-22|Butamax Advanced Biofuels Llc|Butanol purification|
    法律状态:
    2018-09-11| BA2A| Patent application published|Ref document number: 2681121 Country of ref document: ES Kind code of ref document: A2 Effective date: 20180911 |
    2018-11-13| EC2A| Search report published|Ref document number: 2681121 Country of ref document: ES Kind code of ref document: R1 Effective date: 20181105 |
    2019-09-16| FG2A| Definitive protection|Ref document number: 2681121 Country of ref document: ES Kind code of ref document: B1 Effective date: 20190916 |
    2020-02-24| FA2A| Application withdrawn|Effective date: 20200218 |
    优先权:
    申请号 | 申请日 | 专利标题
    ES201730303A|ES2681121B1|2017-03-08|2017-03-08|PROCEDURE FOR OBTAINING PURE BUTANOL|ES201730303A| ES2681121B1|2017-03-08|2017-03-08|PROCEDURE FOR OBTAINING PURE BUTANOL|
    [返回顶部]