The present invention describes a process for obtaining lactic acid with a high degree of purity from a fermentative liquor (1) containing sodium lactate, with a view to the production of polylactic acid. The process comprises the unitary operations of centrifugation (101), centrifugal decantation (102), microfiltration (103), ultrafiltration (104), primary filtration in an activated charcoal bed (105), conventional electrodialysis (201), ion exchange columns in a chelating resin bed (202), bipolar electrodialysis (203), ion exchange columns (204), primary evaporation under vacuum (302), secondary filtration in an activated charcoal bed (304), liquid-liquid extraction from the aqueous phase to the organic phase (305), back extraction from the organic phase to the aqueous phase (306), and secondary, atmospheric evaporation (402).
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1. A process for obtaining lactic acid with high purity degree from fermentative liquor containing sodium lactate, vegetable fibers and polysaccharides, characterized by comprising the steps of: a) clarification, comprising the following sub-steps: a1) to centrifuge in (101) fermentative liquor (1), generating a supernatant stream of pre-clarified fermentative liquor (5) and a dense stream of wet mud (2) composed of fibers and cell material containing from 5 to 25% of fermentative liquor, said wet mud (2) being dehumidified in a centrifugal decanter (102), generating a stream of dry pulp (3) with 0.5 to 2.5% residual fermentative liquor; a2) to microfilter by tangential microfiltration in (103) the pre-clarified fermentative liquor (5) of substep a1), generating a stream of microfiltrated liquor (7); a3) to feed the stream (7) of substep a2) to a tangential ultrafiltration operation (104), generating a stream of ultrafiltrated liquor (9); a4) to filter in activated carbon bed (105) the ultrafiltrated liquor (9) of substep a3), generating a clarified and colorless sodium lactate aqueous solution (10); b) regeneration, comprising the following sub-steps: b1) to feed said sodium lactate aqueous solution (10) of substep a4) to a conventional electrodialysis operation (201), generating a sodium lactate concentrated solution (12); b2) to submit said solution (12) of substep b1) to ion exchange with chelating resins (202), generating a stabilized sodium lactate concentrated solution (13) free of bivalent cations; b3) to feed said solution (13) of substep b2) to a bipolar electrodialysis operation (203), promoting the regeneration of lactic acid and generating a stream of pre-regenerated lactic acid (15) with a concentration of 80-200 g/L of lactic acid and 10-20% of sodium lactate; b4) to submit said stream (15) of substep b3) to a bed of strong acid ion-exchange resin operation (204), generating a stream of regenerated lactic acid (16); c) purification, comprising the following sub-steps: c1) to focus said stream (16) of substep b4) by primary vacuum evaporation (302), generating a stream of concentrated regenerated lactic acid with 1-5% of impurities (19); c2) to filter, in a bed of activated carbon (304), said stream (19) of substep c1), generating a stream of colorless lactic acid (22) with 0.1 to 3% of impurities; c3) to submit said stream (22) of substep c2) to a liquid-liquid extractions sequence, the first extraction being from the aqueous phase to the organic phase (305), and the second extraction being from the organic phase to the aqueous phase (306) through contact with a demineralized water stream (24) generating, respectively, a stream of impure lactic acid (23) and a lactic acid diluted solution of with high purity degree (28); and d) concentration, comprising concentrating the lactic acid diluted solution with high purity degree (28) of substep c3) by secondary evaporation in (402), generating a stream (30) of lactic acid with high purity degree and in the concentration of 80-90%.
2. Process, according to claim 1, characterized in that it returns to the centrifugation feed (101) the concentrated streams of microfiltration (6), the concentrated ultrafiltration (8) and the supernatant (4) of the centrifugal decanter (102).
3. Process, according to claim 1, characterized by additionally performing an operation of nanofiltration in membranes between the substeps a3) and a4).
4. Process, according to claim 1, characterized in that the electrodialysis operation (201) generates as a by-product a stream of diluted sodium lactate (11).
5. Process, according to claim 1, characterized in that the operation of bipolar electrodialysis (203) generates as a by-product a concentrated stream of sodium hydroxide (14).
6. Process, according to claim 5, characterized in that said concentrated stream of sodium hydroxide (14) can be used as input to the process.
7. Process, according to claim 1, characterized in that the filtering operations in the activated carbon medium (105, 304) generate intermittently waste flows (21) during the periods of regeneration of activated carbon bed.
8. Process, according to claim 1, characterized in that in the substep c3) the liquid-liquid extraction is employed a moderate molecular weight alcohol selected among alcohol between C4 and C12, a high molecular weight tertiary amine or a mixture in any proportion of C4-C12 alcohol and said amina.
9. Process, according to claim 8, characterized in that the tertiary amine is the trioctylamine.
10. Process, according to claim 8, characterized in that the C4-C12 alcohol is selected from the group comprised of butanol, pentanol, octanol, decanol, dodecanol or similar.
11. Process, according to claim 1, characterized in that the streams of water vapor (31, 37) generated, respectively, by evaporation (302, 402) are used as process utilities.
12. Process, according to claim 1, characterized in that the liquid-liquid extraction operations (305, 306) generate internal recycle streams of an organic phase rich in sodium lactate (26) and an organic phase poor in sodium lactate (27).
13. Process, according to claim 1, characterized in that the operation of secondary evaporation (402) can generate a precipitated sodium lactate stream (33).
14. Process, according to claim 1, characterized by being effected under energetic reuse through the use of heat exchangers (301, 303, 401 and 403) used for preheating streams that feed operations (302, 304, 402).
15. Process, according to claim 14, characterized in that the heat exchanger (303) heats the water stream (24) for the operation of counter-extraction (306).
16. Process, according to claim 1, characterized by further including the operation of batch fermentation (501), a power stream (35) and a stream of caustic soda (36) being added to the fermenter.
17. Process, according to claim 1, characterized by further including the operation of continuous fermentation (501), being added to the fermenter a power stream (35) and a stream of caustic soda (36).
18. Process, according to claim 16, characterized in that the power supply stream (35) consists of a fermentation broth by milk fermenting containing 50 to 80 g/L of sodium lactate, 3 to 5 g/L of cells and fibers, 10 to 50 g/L of polysaccharides, 1 to 5 g/L of protein and vitamins and 100 to 500 ppm of bivalent cations.
19. Process, according to claim 18, characterized in that the concentration of sodium lactate is preferably from 60 to 70 g/L.
20. Process, according to claim 18, characterized in that the concentration of polysaccharides is preferably 10 to 30 g/L.
21. Process, according to claim 1, characterized in that the wet mud stream (2), the waste streams of microfiltration (6) and ultrafiltration (8), the stream of lye (11) generated in conventional electrodialysis, the stream of diluted sodium lactate (14) generated as a by-product of bipolar electrodialysis (203), the stream of dilute lactic acid (23) exhausted from liquid-liquid extraction (305) and stream of sodium lactate precipitate (33) in the secondary evaporation (402) are recycled to the operation of fermentation (501).
The present invention belongs to the field of processes for obtaining lactic acid with high purity degree from a fermentative liquor containing sodium lactate aiming at polylactic acid production.
Lactic acid (2-hydroxypropionic acid) has been increasingly used worldwide in the production of several biodegradable polymers motivated by modern applications in the medical field (as, for example, in artificial prosthesis) and in the pharmaceutical area (as, for example, in medicines with controlled release) and by the strong ecological appeal of using biodegradable polymeric materials based on lactic acid (polylactic acid) from plant substrates in place of plastic of mineral origin. The success of the employment of a green route for the production of polylactic acid requires a complex process that ensures the removal of all of the contaminants in a natural raw material, the isolation of lactic acid and the concentration of the same.
Below are listed the main processes presented in the prior art for the solution of problems of regeneration, purification and concentration of lactic acid produced in fermentation media. As the techniques differ significantly depending on the approach adopted in each invention, subsections are adopted depending on the technology used as base of each patent document.
Generally speaking, it is verified that all of these technologies have as focus the isolated solution of problems of regeneration, purification or concentration which, separately, are ineffective in producing high-purity lactic acid from fermentative liquor with fibers, shells and other hardly removable impurities.
U.S. Pat. No. 4,110,175 patent document refers to a electrodialysis process that uses anionic and cationic membranes with the purpose of removing organic acids including lactic acid, present in fruit juices and other aqueous solutions.
EP 230021 patent document describes a continuous fermentative process coupled to a electrodialysis process for the continuous removal of lactic acid. However, as there are separations and preliminary filtrations, various components of the fermentative liquor are adhered to the surface of polymeric membranes, which implies in a significant increase in the consumption of electrical energy.
Boyaval et al. (Biotechnology Letters, vol. 9, n° 5, pp. 207-212, 1987) presented a process composed of three unit operations: lactate production via fermentation, removal of cells and cell fragments through ultrafiltration and concentration/purification of lactic acid by electrodialysis. However, as prefiltration are not made, ultrafiltration membranes permeability is reduced drastically over time, requiring frequent chemical cleaning of ultrafiltration modules.
U.S. Pat. No. 5,002,881 patent document refers to a fermentation process in which the fermentation product undergoes an operation of ultrafiltration where the retained returns to the fermentation dorna and the permeate corresponding to a solution of ammonium lactate is concentrated through a reverse osmosis operation. Concentrated ammonium lactate is then fed to the electrodialysis operation for recovery and purification of lactic acid. During electrodialysis ammonia hydroxide is formed, which can be returned to the fermentation for pH correction. As disadvantage it can be highlighted the fact that the solution of concentrated ammonium lactate has also unconverted sugars, vitamins, proteins and other contaminants, thus contributing to the electrodialysis efficiency decrease and resulting in a thermally unstable product.
U.S. Pat. No. 5,503,750 patent document refers to a process with a membrane separation operation sequence (ultrafiltration, nanofiltration and reverse osmosis) for the concentration of an ammonium lactate solution and subsequent conversion into lactic acid. As a disadvantage of this process one can highlight the low recovery efficiency (of approximately 54%), other than the fact that the conversion of ammonium lactate into lactic acid uses ion exchange resins (which implies in a large amount of resins, and require subsequent regeneration operations).
U.S. Pat. No. 4,882,277 patent document aims to simplify all the steps used for the purification of lactic acid using only three unit operations: microfiltration, ultrafiltration, and electrodialysis, performed continually throughout the fermentation. The focus of this document is in the arrangement of conventional electrodialysis operation on a laboratory scale.
Complementing the previous document, the U.S. Pat. No. 4,885,247 patent document proposes an arrangement closer to the industrial application, highlighting the possibility of return of residual lactate to the fermenter in order to decrease the alkaline solution demand for controlling the acidity of the medium and reduce process losses.
U.S. Pat. No. 6,319,382 patent document refers to a fermentation (using ammonia to pH correction), purification and regeneration process of lactic acid that consists of a fermentation step, followed by microfiltration and ultrafiltration for withdrawal of cells, cell fragments and macromolecules. The permeate passes through ion exchange resins (chelate resin) for the substitution of bivalent cations by monovalent cations (such as sodium), thus avoiding the formation of insoluble salts that could damage the membranes of the subsequent electrodialysis process. The permeated having no bivalent cations then is submitted to an electrodialysis process for the regeneration of conventional acid and then to the bipolar electrodialysis to acid concentration. One may highlight as a disadvantage of this process the fact of having a high consumption of chemicals for the regeneration of ion-exchange columns, the product loss corresponding to the hold-up (retention) of ion exchange columns in each regeneration, and the requirement for a proper monitoring of the contamination of regenerative solutions. Moreover, these operations do not guarantee the withdrawal of organic contaminants that generate color to the product and lead to thermal instability by the formation of Maillard compounds.
US 2004/033573 A1 American patent document refers to a process that uses membrane separation steps including ultrafiltration, nanofiltration, reverse osmosis and electrodialysis. In this proposal, the fermentative liquor is ultraconcentrated for the retention of high molecular weight substances. Acidification of the permeated is then made to a pH below 3.9. The acidified solution undergoes a step of isolation via nanofiltration and/or reverse osmosis, which promotes the retention of bivalent ions, proteins, other nutrients and organic anions (such as the lactate anion) and permeates molecules free of charge (such as sodium lactate). Afterwards, it may be considered the use of bipolar electrodialysis for the concentration of the lactic acid solution. The use of nanofiltration and/or reverse osmosis constitutes an alternative to conventional electrodialysis process.
EP 0393818 European patent document complements the U.S. Pat. No. 4,885,247 American patent document, including two steps of ion exchange after the electrodialysis step. Strong acidic ion exchange resins are used for the removal of sodium cations that were not removed during conventional electrodialysis and basic ion exchange resins weak to remove sulfate anions.
U.S. Pat. No. 5,571,657 patent document proposes modification of strong acidic ion exchange resins through contact with ammonium and/or amine solutions, so as to increase their selectivity to the Na+ cation, thereby increasing the efficiency of the lactic acid regeneration process of sodium lactate solutions.
U.S. Pat. No. 4,275,234 patent document presents a recovery process of organic acids aqueous solution using an initial organic solvent extraction followed by a second heated water extraction. It is worth noting that this application is restricted to solutions wherein the organic acid is in its free form.
BR8906651 Brazilian patent document proposes a process for purification and recovery of lactic acid from the solutions containing the same, through a sequence of liquid-liquid extractions. Initially, an aqueous solution of lactate and lactic acid is added with a complex forming agent (composed of at least one octol macolytic) generating octol-lactic acid. Afterwards, this aqueous phase passes through a liquid-liquid extraction with an organic solution of saturated halogenated cyclo-alkanes, alkylated and/or halogenated aromatic hydrocarbons and petroleum ether. The organic phase is separated and then passes through a liquid-liquid extraction with water or methanol. As disadvantages, one can highlight the high reaction time for the complex formation (about 8 h), the need of expensive complexing agents and risks associated with the use of aromatic organic solvents that imply a series of operational difficulties.
Works such as those of B. Bar and J. L. Geiner (Biotechnology Progress, vol. 3, n. 109, 1987), Malmary et al (J. Chem. Technol. Biotechnol., n. 75, pp. 1169-1173, 2000), Hartl and Marr (Separation Science and Technology, n. 28, pp. 805-819, 1993) and San-Marín and Cheryan (J. Chem. Technol. Biotechnol., n. 65, pp. 281-285, 1996) attested the separation efficiency of lactic acid extraction in an aqueous solution by means of long-stream trialkylamines and low basicity, which are able to form complexes with carboxylic acids for even low concentrations of solute, keeping a high selectivity.
U.S. Pat. No. 4,444,881 patent document presents a process capable of purifying organic acids of a diluted solution from fermentation. This solution is treated with a tertiary amine carbonate (for example, tributylamine or tricyclohexylmethylamine), resulting in a precipitate of calcium carbonate and organic salt of trialkylammonium. Organic salt solution is isolated, concentrated by extraction with solvent, distilled and heated for the generation of lactic acid and tertiary amine. As a disadvantage it may be highlighted the cost of specific chemical products, such as tertiary amines, and the absence of organic acids post-treatments to ensure the absence of impurities.
U.S. Pat. No. 4,771,001 patent document presents a process for continuous removal of lactate during fermentative liquor of cheese whey. During fermentation the separation and recycling of cells is made via microfiltration and ultrafiltration, wherein the permeate follows the purification steps. The permeate is acidified and then passes through a liquid-liquid extraction with a solution (immiscible in water) of a tertiary trialkylamine of 24 carbons, and an organic solvent. The organic phase is then separated and passes through a liquid-liquid extraction using a suspension of alkali solids and alkali-earth solids in an aqueous solution of ammonium hydroxide, which promote the removal of lactate and lactic acid. In this patent document concentration steps are not addressed or even lactic acid isolation.
U.S. Pat. No. 5,510,526 patent document uses as extracting phase a trialkylamine solution with a strong attraction to lactic acid (for example, tri-n-octylamine and tri-n-dodecylamine) in an extraction with atmosphere of CO2. Sodium bicarbonate crystals are formed and separated from the aqueous phase. Bicarbonate is converted to carbonate and returns to the fermentation process being used for pH neutralization. The alkylamine type used should be chosen so that its power of attraction is high enough to extract the lactic acid from lactate solution and weak enough to deliver the acid to the water. Because they are viscous, these alkylamines should be added from kerosene and/or octanol. The removal of lactic acid from the organic phase is done through contact with water. In the case of kerosene or octanol being used, a step prior to rinsing with water must be made to remove these solvents.
U.S. Pat. No. 6,478,965 patent document presents a route in the use of secondary or tertiary amines (e.g., TEA, or DEMA) in the extraction of water from a stream diluted in lactic acid (about 3%), thus producing a concentrated stream of 15% lactic acid. It is necessary a series of contactors to promote the extraction of water from the organic phase.
U.S. Pat. No. 6,509,179 patent document combines a set of unit operations for purification of lactic acid formed by the steps of acidification, salt removal, activated carbon filtration, primary extraction, secondary extraction, evaporation and vacuum distillation.
U.S. Pat. No. 7,026,145 patent document proposes an improvement in the process of lactic acid extraction using tertiary alkylamines using sulfuric acid along with the amine solution, as well as a preliminary acidification step using this same acid.
US 2004/210088 A1 American document describes several routes of lactic acid production based on liquid-liquid extraction with amines and/or and specific alcohols, the removal of the solvent being made by distillation columns in the top product or in the bottom product (depending on the route considered).
U.S. Pat. No. 7,019,170 patent document describes the recovery of lactic acid from a lactic acid solution and lactate through a sequence of liquid-liquid extraction operations. A first liquid-liquid extraction column promotes the exchange of mass between a stream of lactic acid and lactate and a stream of trialkylamine, generating a stream of primary raffinate and a saturated trialkylamine stream. The saturated trialkylamine stream passes through a column of liquid-liquid extraction with pure water, generating a stream of pure lactic acid and a stream of trialkylamine "alive". A third column of liquid-liquid extraction promotes contact between the primary and raffinate trialkylamine stream "alive", generating a stream of secondary raffinate and a stream of trialkylamine recovered (which can be returned to the first extraction operation).
U.S. Pat. No. 6,489,508 patent document details the process of lactic acid concentration by evaporation highlighting the optimum operating conditions of either pressure (vacuum) and temperature, so as to minimize the change of color of the final product.
The international publication WO 00/56693 A1 describes a vacuum distillation process followed by crystallization, which allows the concentration of a solution of 80% lactic acid up to a concentration of 99%. The high energetic consumption of the evaporation and crystallization operations coupling is a significant disadvantage of this proposal.
U.S. Pat. No. 6,384,276 patent document proposes the acidification of a lactic acid and sodium lactate solution. Then, an evaporative crystallization is made, wherein which sodium lactate is crystallized and the lactic acid is kept in solution. It is observed, however, that the success of this proposal depends on having as load a pure solution (free of sugars, proteins, or vitamins), otherwise there will be contamination of the final product and the generation of a product with color.
U.S. Pat. No. 5,177,008 patent document proposes the use of chromatographic separation operations for the separation of lactic acid for the reuse of that product from the secondary streams of the ethanol industry. However, the high cost of this process, mainly for production of lactic acid on a large scale, significantly restricts the application of this technology.
CN 101234960 patent document proposes a concentration process which promotes initial evaporation of lactic acid followed by rotating distilling (also called molecular distillation), generating a stream of lactic acid with high purity.
It would be helpful if the technique had a process of obtaining lactic acid from fermentation broths that use clarification, regeneration, purification and liquor concentration, the process operating under energetic efficiency regimen by recycling the process streams, the final product being concentrated lactic acid and having high purity degree.
In a broad way, in order to produce a lactic acid with high purity degree from fermentative broths keeping a high global yield, it was developed in the present invention a process consisting of a sequence of unit operations and several recycling streams for by-products reuse and intermediate streams.
e) lactic acid evaporation purified to obtain concentrated lactic acid 80-90% and purified.
Energetic efficiency is ensured through the thermal energy reuse operations of intermediate streams.
Thus, the invention provides a process for obtaining concentrated lactic acid and of high purity degree through the steps for clarification, regeneration, purification, and concentration, the lactic acid being derived from fermentative liquor containing sodium lactate and multiple contaminants present in the fermentation process substrates.
Additionally, in the process of obtaining concentrated lactic acid and of high purity degree of the present invention, the steps proposed are synergistically combined.
FIG. 1 attached is a block diagram that represents in a simplified way the sequence of major unit operations as the process of the present invention, thus showing only the main products streams and intermediate products.
FIG. 2 attached shows a flowchart of the process of the present invention, which describes unit operations and the major streams of the process for producing concentrated lactic acid and with a high purity degree, containing some by-products recycling streams.
FIG. 3 attached shows a flowchart of the process according to the invention, which illustrates the unit operations and major streams of the process for producing concentrated lactic acid and with a high purity degree, by considering energetic integration.
FIG. 4 attached shows a flowchart of the process according to the invention, which illustrates the unit operations and major streams of the process for producing concentrated lactic acid and with a high purity degree by considering energetic integration and mass integration (with by-products recycling streams).
The present invention describes a process for obtaining lactic acid from the steps of clarification, regeneration, purification and concentration of lactic acid derived from a fermentative liquor containing sodium lactate and several contaminants present in the substrates of the fermentation process.
The proposed process is concerned with energetic efficiency. For this reason, several energetic reuse exchangers were considered and not used for crystallization and washing steps, as proposed in prior art documents.
Another concern of the inventors refers to the use of chemical products that are easily accessible in the marketplace and have reduced cost, contrary to what is stated in previous documents that employ specific solvents.
Lactic acid is produced by fermentation, typically fermentation of a growth medium comprising an sugar solution and a protein, for example, milk protein in the form of permeate milk protein obtained from milk protein concentrate. Fermentation is carried out, preferably by adding one or more protease enzymes to the fermenter, to result in a continuous production of hydrolyzed protein simultaneously with fermentation by means of a bacterial culture that produces lactic acid. Bacterial cultures producing lactic acid are cited, for example, in the international publication WO 98/28433.
This invention conjugates several technologies that can be divided into four steps: clarification, regeneration, purification, and concentration.
The process of the present invention is carried out on a continuous basis. In addition, the process of the present invention further admits batch operation.
The process of the present invention allows obtaining a lactic acid aqueous solution at 80-90% and 0.01 to 3% of impurities.
The process of the present invention combines in a synergistic and successive way the steps described, in order to obtain a concentrated product of high purity with energetic efficiency.
The load of the process is derived from a fermentative liquor resulting from a dairy fermentation process and consists of an aqueous solution containing 50 to 80 g/L of sodium lactate (more specifically between 60 and 70 g/L), 3 to 5 g/L of cell mass (derived from microorganisms responsible for fermentation process, such as, for example, Lactobacillus casei) and fibers (derived from the raw material used in the fermentation, such as, for example, manioc fibers—Manihot esculenta), 10 to 50 g/L of polysaccharides (more specifically between 10 g/L and 30 g/L), 1 to 5 g/L of proteins and vitamins and 100 to 500 ppm of bivalent cations (Mg2+, Ca2+ and Sr2+).
The beginning of the process consists of the centrifugation of the fermentative broth, in order to promote the removal of fibers and other suspended solids, thus generating a net stream of pre-clarified fermentative liquor and a wet mud of fibers and cellular material. This operation is essential for the treatment of fermentative liquors that use broths extracted from plants, more specifically of fibrous vegetables.
Practical experience shows that the use of centrifugation upstream other more restrictive filtering operations, such as membranes microfiltration, reduces the frequency of backwash and increases the permeated flow.
The wet mud (containing from 5 to 25% of fermentative liquor) generated in the centrifugation is still impregnated with fermentative liquor, which must be taken out of this pulp, so as to reduce losses of sodium lactate in this clarification step. To achieve this, it is used a centrifugal decanter (decanter) that allows the formation of a dry pulp with 0.5 to 2.5% of residual fermentative liquor. The dry pulp can be sold as a by-product of this process for use in fertilization or as animal feed, to rely on a prior analysis of such viability.
Pre-clarified liquor then passes by a tangential microfiltration through polymeric membranes with pore diameter of 50 μm, preferably 30 μm, which promotes the separation of residual fibers and cells. The stream of liquor held in the microfiltration returns to the entrance of the centrifugation and the microfiltrated liquor stream then passes to the next filtration step.
The microfiltrated liquor feeds the tangential ultrafiltration operation through polymeric membranes with porosity of 30 to 70 kDa, which promotes the separation of macromolecules and cell fragments. The stream of liquor held in the ultrafiltration returns to the entrance of the centrifugation and the ultrafiltrated liquor stream then passes to the next filtration step.
Optionally, the ultrafiltrated liquor stream can be subjected to a nanofiltration step aiming at to reduce the concentration of bivalent cations present in the filtrated medium. Several membranes can be used for this application, such as, for example, polymeric membranes with porosity of 1 to 30 kDa.
The resulting liquor of the ultrafiltration and/or nanofiltration (in case this process is additionally used) feeds the filtration operation in activated carbon bed, which allows for the removal of organic compounds which give color to the aqueous solution. When the load increases considerably in color, one can use powder activated charcoal with 200 rpm shaking and contact time of 10 to 60 minutes prior to bed. As a result, clarified and color-free sodium lactate aqueous solution is obtained.
The sodium lactate stream derived from the activated carbon bed proceeds to the step of electrodialysis (EDC), wherein the sodium lactate is purified and concentrated. The EDC consists of applying a potential difference between pairs of positively (anionic membranes) and negatively (cationic membranes) charged membranes. The sodium lactate aqueous solution (50-80 g/L) is fed between a cationic and an anionic membrane (cell) alternately with a diluted solution of 1 to 10 g/L of sodium lactate. This solution receives the lactate anion that migrates by anionic membrane towards the anode and the sodium cation by negatively charged side. At the end of the process, the sodium lactate aqueous solution is exhausted and the non-ionizable polysaccharides, proteins and vitamins remain in this stream, which returns to the step of centrifugation and/or fermentation. The yield of this step varies from 70 to 90% of recovery, depending on the operating conditions (flow, pressure, stream, DDP, pH, concentration, etc.). The sodium lactate diluted solution can be concentrated in up to 20 times with total residual impurities contents of 1 to 10% and 50 to 200 ppm of bivalent cations (Mg2+, Ca2+ and Sr2+).
Sodium lactate is converted to lactic acid by bipolar electrodialysis. The operating principle of bipolar electrodialysis is similar to EDC, except for the addition of a bipolar membrane (positive and negative charges) in each cell (1 cationic membrane and 1 anionic membrane). Bipolar membranes are sensitive to polyvalent cations that settle on the surface of them, thus reducing the efficiency of regeneration. The polyvalent cations are removed from the lactic acid solution for contents of up to 10 ppm in chelating resins filters before the bipolar electrodialysis. At the end of bipolar electrodialysis, it is obtained a solution with concentrations between 80 and 200 g/L of lactic acid, 1 to 5% of total impurities and 10 to 20% sodium lactate. The final polishing for regeneration of all the sodium lactate in lactic acid is performed on a column with strong ionic exchange resins. The regenerated product is then forwarded to the purification step to remove the remaining impurities.
Lactic acid solution with 1 to 5% of impurities is sent to a evaporation column, which will be concentrated in to 60% by mass. The evaporation step concentrates organic compounds which give color to the product, thus requiring a new activated carbon filtration step for complete removal of coloring. This stream of concentrated lactic acid (400 to 600 g/L) and free of color is admitted in a first column of liquid-liquid extraction, where will contact with an average molecular weight alcohol selected amongst linear and/or branched C4-C12 alcohols (for example: butanol, pentanol, octanol, decanol, dodecanol, etc.), high molecular weight tertiary amines or a mixture of these alcohols with tertiary amines (e.g.: trioctylamine). The alcoholic stream rich in lactic acid follows to a second column, where it will be rinsed with demineralized water and will return in a closed circuit to the first column. At the end of the cycle, it has an aqueous stream with 5 to 20 g/L of lactic acid and an exhausted stream which is disposed of or reused in the fermentation process. The 5 to 20 g/L colorless lactic acid aqueous solution with 0.01 to 3% of total impurities follows to the concentration step.
The concentration of purified and regenerated lactic acid aqueous solution is performed on a simple evaporation step with the temperature of the mass between 100 and 150 degrees Celsius and top temperature of 100 degrees Celsius under atmospheric pressure. Colorless lactic acid at 80-90% in water and with concentration of impurities between 0.01 and 3% is obtained at the end of the evaporation.
Another alternative that makes the evaporation step faster is the vacuum application to the evaporation system.
The passage of the final product in charcoal filters "Carbon Block" can be performed for final polishing.
Figures that illustrate the different modalities of the process of the present invention are described. It should be made clear to the skilled in the art, however, that several modifications and variations are possible for these figures within the scope of the present invention.
The attached figures correspond to process flowcharts wherein unit operations are numbered by the hundreds 100 (clarification step), 200 (regeneration step), 300 (purification step), 400 (concentration step) and 500 (fermentation step) with materials streams represented by the numerals 1 to 38. Full lines are used to describe the liquid or solid state streams and dashed lines are used to describe steam flows.
The basic sequence of unit operations, including major streams, is described in FIG. 1. The unit operations correspond to centrifugation (101), centrifugal decanting (102), microfiltration (103), ultrafiltration (104), primary filtration in activated carbon bed (105), conventional electrodialysis (201), ion-exchange columns in chelating resin bed (202), bipolar electrodialysis (203), ion-exchange columns (204), primary vacuum evaporation (302), secondary filtration in activated carbon bed (304), liquid-liquid extraction of the aqueous phase to the organic phase (305), contra-extraction of organic phase to aqueous phase (306) and secondary atmospheric evaporation (402).
The fermentative liquor (1) is centrifuged in (101), generating a supernatant liquid stream called pre-clarified fermentative liquor (5), and a dense stream called wet mud (2), composed of fibers and cellular material.
The wet mud (2) is then dehumidified in the centrifugal decanter (102), generating a stream of dry pulp (3).
The pre-clarified fermentative liquor (5) passes through a microfiltration operation (103), generating a stream of microfiltrated liquor (7), which is fed to the ultrafiltration operation (104), generating a stream of ultrafiltrated liquor (9). The ultrafiltrated liquor (9) then passes through a filtration process in activated carbon bed (105), generating a clarified and color-free sodium lactate aqueous solution (10). Alternatively, the stream of ultrafiltrated liquor (9) is submitted to a stepe of nanofiltration (not represented) with the aim of reducing the concentration of bivalent cations present in the filtrate.
The aqueous solution of sodium lactate (10) is fed to a conventional electrodialysis operation (201), generating a concentrated sodium lactate solution (12). The concentrated sodium lactate solution (12) then passes by a ion exchange operation with chelating resins (202), generating a stabilized concentrated sodium lactate solution (13) free of bivalent cations.
The stabilized concentrated sodium lactate solution (13) feeds a bipolar electrodialysis operation (203), promoting the regeneration of lactic acid and generating a stream of pre-regenerated lactic acid (15). The stream of pre-regenerated lactic acid (15) then passes through an ion exchange operation in strong acid resin bed (204), generating a stream of regenerated lactic acid (16).
The regenerated lactic acid stream (16) is concentrated through an operation of primary vacuum evaporation (302), generating a stream of concentrated regenerated lactic acid stream (19). The concentrated regenerated lactic acid stream (19) then passes through a filtration process in activated carbon bed (304), generating a stream of colorless lactic acid (22). The colorless lactic acid stream (22) goes through a sequence of liquid-liquid extractions, namely in the aqueous phase to the organic phase (305) and then of the aqueous phase to the organic phase (306) through contact with a stream of demineralized water (24), generating a stream of impure lactic acid (23) and a diluted lactic acid solution with high purity degree (28).
The diluted lactic acid solution with high purity degree (28) is concentrated through an evaporation secondary operation (402), generating a stream of concentrated lactic acid with high purity degree (30).
FIG. 2 further details the process streams, including by-products, intermediate products and inputs.
The streams of microfiltration concentrate (6), of ultrafiltration concentrate (8) and of centrifugal decanter supernatant (4) are returned to the feeding of centrifugation (101).
The electrodialysis operation (201) generates as a by-product as a stream of diluted sodium lactate (11).
The operation of bipolar electrodialysis (203) generates a stream concentrated of sodium hydroxide (14), which can be used as input to the process.
The operations of evaporation (402 and 302) generate streams of water vapor (37 and 31), which may be used as process utilities.
The operations of filtration in activated carbon medium (105 and 304) generate, intermittently, waste flows (21) during the periods of regeneration of activated carbon bed.
The liquid-liquid extraction operations (305 and 306) have internal recycle streams of organic phase rich in sodium lactate (26) and of the organic phase poor in sodium lactate (27).
The operation of secondary evaporation (402) can generate, depending on the contamination, a stream (33) of precipitated sodium lactate, if the latter is not completely regenerated during the process.
FIG. 3 incorporates the possibility of energetic reusing by using heat exchangers (301, 303, 401 and 403) for preheating the streams that feed operations (302, 304 and 402). In addition to the energy saving for water evaporation and concentration of streams (16) and (28), heat exchanger (303) allows the stream heating of demineralized water (24), which guarantees an improvement in the performance of the contra-extraction (306).
FIG. 4 incorporates the possibility of integrating the process of regeneration, purification and concentration of lactic acid by fermentative process.
Said FIG. 4 includes the operation of fermentation (501), which can be carried out in the form of subsequent or continuously batches.
The stream (35) corresponds to the cells feeding, substrate and other nutrients to the fermentation (501).
The stream (36) corresponds to the caustic soda solution added continuously for the control of fermentation pH (501).
The wet mud stream (2) is recycled to the operation of fermentation (501).
The waste streams of microfiltration and ultrafiltration (6 and 8) are also recycled for operation of fermentation (501).
The stream of lye (11) generated in conventional electrodialysis is also recycled for operation of fermentation (501), in order to promote lactic acid neutralization.
The diluted sodium lactate streams (14) generated as a by-product of bipolar electrodialysis (203), of diluted lactic acid (23) exhausted from the liquid-liquid extraction (305) and precipitated sodium lactate (33) in the secondary evaporation (402) are recycled to the operation of fermentation (501).
The invention will be illustrated by the following examples, which should not be considered restrictive.
This example illustrates the scaling, testing and mass balances for the clarification step.
For a process scaled to treat 250 kg/h of sodium lactate (70 g/L) in a fermentative liquor obtained by fermentation of the milky way, it was considered two distinct scenarios depending on the composition of fermentative liquor. The scenario 1 refers to a liqueur composed of 5 g/L of cells of Lactobacillus casei and fibers of cassava (Manihot esculenta), 5 g/L of vitamins and proteins and 30 g/L of polysaccharides not consumed during the fermentation process. The scenario 2 refers to a liqueur composed of 3 g/L of cells of Lactobacillus casei and fibers of cassava (Manihot esculenta), 1 g/L of vitamins and proteins and 10 g/L of polysaccharides not consumed during the fermentation process.
For the clarification of sodium lactate, a centrifuge capable of a feed of 40 m3/h and 4 m3/h of concentrate, a centrifugal decanter with a capacity of 0.5 m3/h and 0.05 m3/h of concentrate, ultrafiltration and microfiltration systems with processing capabilities of 4 m3/h and 3.5 m3/h of microfiltrated and concentrate, respectively, and a filter in activated carbon bed for filtration of 3.5 m3/h are used.
In relation to the microfiltration system, pilot-scale tests indicated that this system must be operated using timed backwash (at a frequency of 15 to 60 minutes) characterized by pumping in reverse microfiltrated liquor itself. Studies indicated the following optimum project parameters of the microfiltration modules: ratio between the permeate flow and feed flow of about 0.15, permeability of 1.0×10−4 L/(h·m2·Pa) (10.0 L/(h·m2·bar)) and transmembrane pressure (difference between power and pressures permeate) equal to 1.0×105 Pa (1.0 bar). The membrane area required for this operation is of about 400 m2, which corresponds to the use of 8 hollow fiber modules with 50 m2 each. The flow rate of the feed pump for this application is 35 m3/h.
In relation to the ultrafiltration system, pilot-scale tests indicated the following optimum project parameters of the ultrafiltration modules: ratio between the permeate flow and feed flow of about 0.50, permeability of 1.5×10−4 L/(h·m2·Pa) (15.0 L/(h·m2·bar)) and transmembrane pressure (difference between the pressures of power and permeated) of 1.5×105 Pa (1.5 bar). The membrane area required for this operation is of about 150 m2, which corresponds to the use of 6 dense flat membrane modules with 25 m2 each. The flow rate of the feed pump for this application is of 8 m3/h.
In relation to the activated carbon bed filter, pilot-scale tests indicated the following optimum project parameters: residence time of the solution in contact with the coal equal to 4 hours and a density of coal packaging of about 800 kg/m3. Thus, for the processing of 3.5 m3/h of sodium lactate aqueous solution a vase of 175 L working volume and a coal mass of 140 kg is used. There was also the need for regeneration of coal every 3-6 hours of system operation using steam at 120-150° C.
Pilot-scale tests made it possible to determine mass balances for the clarification step for the two scenarios proposed, considering purging of 25% of the ultrafiltration waste (attached Tables 1 and 2) and purging of 10% of the ultrafiltration waste (attached Tables 3 and 4). It is important to stress that as this is a continuous operation and which has the concentration of contaminants by the recycling of ultrafiltration wastes, it becomes necessary to purge part of this stream in order to prevent the elevation of the concentration of this waste within the streams that participate in this recycling.
From attached tables 1 to 4 one can determine the mass yielding of the clarification step in relation to sodium lactate as being equal to about 80% for scenarios 1 and 2, considering a purging of 25% and about 90% for scenarios 1 and 2 considering a purging of 10%.
This example illustrates the scaling, testing and mass balances for the concentration step.
For a process scaled without energetic reuse for the concentration of 250 kg/h of sodium lactate sourced from a purified and regenerated lactic acid aqueous solution with lactic acid concentration equal to 15 g/L, it is necessary to use an atmospheric evaporator with heat exchange capacity of about 12 MW for the withdrawal of 16.3 tons/hour of water vapor with a system for the separation of 17 kg/h of insoluble impurities, as described in the attached Table 5 that lists the mass balance of the concentration step. From this table, it is possible to estimate a consumption of about 172 MJ/kg of lactic acid.
On the other hand, a process scale with energetic reuse include a heat exchanger with thermal exchange capacity of about 1.3 MW for preheating the regenerated and purified lactic acid aqueous solution of from 25° C. to 90° C., using hot fluid as the water vapor generated in atmospheric evaporator, as described in the attached Table 6. From this table, it is possible to estimate a consumption of about 153 MJ/kg of lactic acid.
This example illustrates the scaling, testing and mass balances for primary evaporation of the purification step.
For a process scaled without energetic reuse for the concentration of 250 kg/h of sodium lactate sourced from a purified and regenerated lactic acid aqueous solution with lactic acid concentration equal to 125 g/L, it is necessary to use a vacuum evaporator (2.5×104 Pa−250 mbar) with thermal exchange capacity of around 1.0 MW for the withdrawal of 0.6 tons/hour of water vapors, as described in attached Table 7, that lists the primary evaporation mass balance of the purification step. From this table, it is possible to estimate a consumption of about 15.2 MJ/kg of lactic acid.
However, a process scaled with energetic reuse includes a heat exchanger with thermal exchange capacity of about 1.0 MW for pre-heating and evaporation of regenerated diluted lactic acid solution of from 25° C. to 80° C., using hot fluid as water vapor at 120° C. generated in atmospheric evaporator, as described in the attached Table 8.
In this way, it is possible to promote primary evaporation using only the hot fluid generated in the concentration step.
This example illustrates the scaling, testing and mass balances for the liquid-liquid extraction of the purification step.
For a process scaled for the purification of 250 kg/h of lactic acid sourced from a concentrated lactic acid aqueous solution (500 g/L) a conventional first column of liquid-liquid extraction to contact 500 L/h of concentrated lactic acid solution with 1.0 m3/h of octanol and a second column of liquid-liquid contra-extraction to contact 1.0 m3/h of octanol with 1.0 m3/h of demineralized water are used. As a result, it is retrieved an aqueous stream with a flow of 1.0 m3/h of purified lactic acid diluted solution at a concentration of 15 μg/l.
The water streams enter into the lower part of the extractor columns and the alcoholic streams at the top, for the octanol density (0.8 g/mL) is less than that of water (1.0 μg/mL).
The first conventional column has 20 theoretical plates with 1.5 meters in diameter and has a decanter in the output of alcoholic phase to aqueous solution drag retention. The octanol derived from the first column is under pressure and overflows from the decanter to the bottom of the second column.
The second conventional column has the same characteristics as the first and the octanol exhausted from the decanter is recovered in the first column, remaining thus in a closed circuit.
Pilot-scale tests have provided a 70% recovery of lactic acid in the first passage through the system. It is worth noting that the remaining 30% lactic acid can be further concentrated in the evaporation system and resubmitted for new liquid-liquid extraction, resulting in losses to the process.
This example illustrates the scaling, testing and mass balances for the conventional electrodialysis step of regeneration.
For a process scaled for the concentration of 250 kg/h of sodium lactate from a diluted solution of 70 g/L of sodium lactate a module (stack) of conventional electrodialysis (EDC) with capacity for 3.6 m3/h is used. Considering a stream density of 110 A/m2 with stream efficiency of 80% and a 155 V voltage, it is required a 175 m2 membrane area.
This process has a yield of about 80%, from 6.5 m3/h of a solution of 5 g/L sodium lactate, and generates as a by-product 6.5 m3/h of a sodium lactate-poor aqueous solution (14 g/L) containing polysaccharides, proteins and vitamins. The electrolytes consume 3 m3/h of a solution of sulfuric acid at 2%. The product corresponds to a flow rate of 3.5 m3/h of lactic acid solution with a concentration of 125 g/L.
This example illustrates the scaling, testing and mass balances for the bipolar electrodialysis of the regeneration step.
For a process scaled for the regeneration of 200 kg/h of sodium lactate from a 125 g/L of sodium lactate solution a module (stack) of bipolar electrodialysis (EDBM) with a capacity of 3.0 m3/h treatment is used. Considering a stream density of 600 A/m2 with stream efficiency of 70%, a stream average of 2.5 and a 165 V voltage, a 85 m2 membrane area is required.
This process presents a yield of about 90% of lactic acid in relation to the sodium lactate fed. The product corresponds to a flow rate of 3.0 m3/h of lactic acid solution with concentration of 112.5 g/L of lactic acid and 12.5 g/L of sodium lactate.
It should be made clear to the skilled in the art that although the present invention has been described in relation to lactic acid, many other carboxylic acids can also undergo a similar process, such acids including: formic acid, acetic acid, butyric acid, propionic acid, valeric acid, isovaleric acid, capronic acid, acid heptanoic acid, octanic acid, oxalic acid, maloic acid, glutaric acid, adipic acid, glycolic acid, glycinic acid, acrylic acid, tartaric acid, fumaric acid, benzoic acid, maleic acid, phthalic acid or salicylic acid.


'Its still only November' I hear you say. Well, that won't stop them. On twitter yesterday (Tuesday 24th) we predicted that we might expect to see the first few stragglers doing their 12 pubs of Christmas this coming weekend as we're about to head into December. Little did we know, that a few pubs have already had groups in.
We were told about groups going in to the Irishtown House and Brogans on Dame street, but there's surely more than that.
Just as Christmas ads and music get earlier every year, so too do the 12 pubs groups.
As always, for those of you that don't like partaking and don't want to be in a pub that is intermittently mobbed every half hour, we will be putting together our list of pubs that will be banning 12 pubs groups.


What makes the Escalade turn heads in Costa Mesa?
• The Cadillac Escalade is a full-size SUV that combines exceptional performance with a refined design.
• It comes standard with a 420hp V8 engine, as well as a precise 10-speed automatic transmission for the smoothest gear shifting and available all-wheel drive for rough driving conditions.
• A hands-free liftgate simplifies storage and Adaptive Remote Start with keyless access allow you to stow things and enter the vehicle effortlessly.
• With seating for 7 passengers, folding third row seats for additional storage, and a maximum towing capacity of 8,300 lbs., the Escalade is the ideal vehicle for family road trips.
• A suite of safety features like a rear camera mirror and Side Blind Zone Alert will help to prevent collisions as you drive.
Explore our inventory of new Cadillac Escalades and pick the color and options that are right for you. Contact us at (714) 656-4317 about buying or leasing an Escalade in Costa Mesa.
A brilliant look back. Available Rear Camera Mirror streams HD video of what lies behind you to the rearview mirror. While driving down the road, this less obstructed view offers 300% more field of view than a traditional mirror, but can revert back with just a toggle. An integrated washing system keeps the camera lens—and your outlook—incredibly clear.
A higher perspective. Surround Vision provides you a bird's-eye view of the area immediately surrounding your vehicle when in low-speed Drive or Reverse. This view, projected on the Cadillac user experience1 screen, helps reduce blind spots and increase awareness when maneuvering in and out of tight spots.
The Escalade Platinum features 18-way adjustable heated and ventilated front seats with multi-directional massaging. Heated rear seats keep every passenger content on the coldest of journeys, while Tri-Zone Climate Controls allows them to enjoy the environment as they see fit.
The 2018 Escalade arrives with a 6.2L 420 hp V8 paired with a new, intelligent 10-speed automatic transmission that moves between gears in the smoothest, most efficient fashion.
An elevated environment where craftsmanship and comfort are unparalleled. Refinement emanates from every detail. Pleasure pours over every surface. This is where the journey becomes your home.
Sophisticated surfaces guide your eye to crisp, chiseled corners, where iconic light signatures meet arresting chrome accents. It's a look that refuses to be ignored. Or imitated.
Discover the new Cadillac Escalade, available to buy or lease today at Suburban Cadillac of Costa Mesa. On this page, you will find the 2018 Escalade vehicles that are currently available to buy or lease at our Costa Mesa dealership, be able to see the exterior color options, view photos, and more. If you have a question about this new Escalade or any other new or used vehicle at Suburban Cadillac of Costa Mesa, please give us a call at (714) 656-4317, and our friendly staff will be happy to assist you.


text:
Red Oak is an area in the City of South Fulton, Fulton County, Georgia, United States, near College Park and East Point. The ZIP Code is 30272 and 30349  The region is located along U.S. Route 29 and the Georgia State Route 14 Connector to Interstate 85 and 285. The former terminus of SR 14 Connector is in the vicinity of post office destroyed during a civil war battle in 1864.

Through its history the community of Red Oak has never been incorporated as a town, but a post office was built in 1849. Its first postmaster was the Reverend William "Harrison" Walker (1809-1879), a Baptist minister, who came to Fayette County with his father, Levi Loudy Walker (1784-1860), and shows up on the first Fayette County census in 1830. Levi's property adjoined his son's and another son – Redmond – lived close by.

As was the custom the Red Oak post office was established on the property of the postmaster. Rev. Walker's home was in District 9, Land Lot 128 of Fayette County. On one of the early deeds to his property the Atlanta and West Point Railroad can be clearly seen crossing the property.

Local stories state a red oak tree stood at the postal stop giving the community its name – Red Oak.  Today, a Georgia Historical Society marker stands at the intersection of Welcome All Road and U.S. 29/Roosevelt Highway. The marker verifies the existence of the Red Oak post office which was discontinued following the Civil War. Decades later another post office at Red Oak would be re-established and continues to this day.

In 2020, Red Oak was named one of the Historic Main Street Districts in the City of South Fulton.

References
The Newnan Herald, Newnan, Georgia, August 18, 1860, page 3

Reeves, Frances C., A Short History of Fayette County, Georgia 1821-1877, (1977)

White, George, Historical Collections of Georgia: Containing the Most Interesting Facts, Traditions, Biographic Sketches, Etc. Relating to Its History and Antiquities, from Its First Settlement to the Present Time, 1855.

White, George, Statistics of the State of Georgia..., (1849)

Wood, Chris, Clayton County: Reflections of a Crescent Jewell (1993)

Unincorporated communities in Fulton County, Georgia
Unincorporated communities in Georgia (U.S. state)
Unincorporated communities in the Atlanta metropolitan area

redpajama_set_name: RedPajamaWikipedia


Carmel, California (PRWEB) - Hugh Jackman and Tom North were the featured guests on SiriusXM Indie Talk Radio-XL Channel 104, ''Success without Stress'' with host Bob Roth, which aired Friday, June 27. Bob Roth is executive director of the David Lynch Foundation, and in this series he talks to some of the most creative and successful people in the world, as well as leaders from the worlds of military, business, finance, and education, about their experience with Transcendental Meditation, the role it plays in their lives, effects it has on their work and the impact of stress on success.
Award-winning author and inspirational speaker Tom North tells how Transcendental Meditation (TM) was his saving grace. He is the author of True North—The Shocking Truth about ''Yours, Mine and Ours''—an inspirational story of survival and hope. In the book, North reveals how he survived the ordeal of living with an abusive stepfather that drove him to depression and drugs and deprived him of his self-worth—and a mother who protected the perfect ''movie family image'' at all costs. But the book is much more than an inspiring and powerful account of a man who rose to success against all odds. It's also a story of how TM brought peace to Tom North and saved his life.
Click here to listen to Bob Roth's June 27 interview with Tom North on his ''Success without Stress'' show on SiriusXM Indie Radio (audio only).
About Tom North: Tom North, an accomplished writer, inspirational and motivational speaker and financial adviser, is one of TM's most vocal advocates for people who are disaffected or suffering from emotional pain.


text:
2000 WE100 (asteroide 37204) é um asteroide da cintura principal. Possui uma excentricidade de 0.06736590 e uma inclinação de 11.40292º.

Este asteroide foi descoberto no dia 21 de novembro de 2000 por LINEAR em Socorro.

Ver também

 Lista de asteroides
 Asteroide da cintura principal

Referências

Ligações externas

Asteroides da cintura principal
Objetos astronômicos descobertos em 2000


Honored to be named as one of TV One's NewsOne top 15 most share-worthy black blogs or websites for 2014.
NewsOne suggested described A Belle in Brooklyn as "pop culture and relationships from a black, feminist perspective" and suggested folks visit the site because.... "Fans of Bravo's Blood Sweat & Heels will recognize what Lucas's readers have known all along: she knows what she's talking about."
Many of my faves also made the list, including Very Smart Brothas, Colorlines, My Brown Baby, For Harriet, The Crunk Feminist Collective, and Black and Married with Kids.
What sites are most share-worthy to you?


text:
Mugenthirran a/l Ganesan (born 4 April 1993) is a Malaysian footballer who plays for PKNP as a forward.

References

External links

1993 births
Living people
Malaysian footballers
Malaysia Super League players
PKNP FC players
Malaysian people of Tamil descent
Malaysian sportspeople of Indian descent
Association football forwards


text:
McMurray climbs past the cutoff point
October 8, 2017 By [email protected]
By Bob Priddy, Contributing Editor
(NASCAR)—Joplin's Jamie McMurray, bidding to move into the third round of NASCAR's playoffs, has raced past four other drivers and into the top eight in points with a solid fifth-place run at Charlotte. McMurray started the day seeded twelfth, last in the second-round standings. Eight drivers will advance to the third round after next weekend's race at Talladega and the race at Kansas a week later.
McMurray started eighteenth but ran in the top three for most of the first stage, led once for four laps, came home fifth at the end at a track where he often runs well.
Martin Truex Jr., overcame an uncharacteristically bad qualifying run, starting seventeenth, but defended his lead on the last restart and won by almost a full second. Chase Elliott was the runner-up for the second race in a row.
McMurray (show after his Talladega victory in 2009) is one point ahead of Matt Kenseth and two up on Brad Keselowski, both former Cup champions. He's seven behind Jimmy Johnson, the 2016 champion.
Talladega is next up, a restrictor plate race on a track where McMurray has done well but a track that often scrambles standings because of major wrecks resulting from pack racing at 200 mph. He also won at Talladega in 2013, was second in last May's race and has another second-place finish there from 2000.
NASCAR's silly season is well underway with drivers leaving one team and moving to another or speculation about what free agent drivers at the end of the year will find rides and which will be retired. One name not being heard is Carl Edwards, the Columbia driver who announced last January he wasn't racing this year.
(Speaking of Talladega—you might recall this horrific crash in 2009 as Edwards and Brad Keselowski raced for the win)
AUTOWEEK reports there has been no sign that Edwards is interested in coming back. Jack Roush, who fielded the cars and trucks Edwards drove for fourteen years says he's gotten only two texts from Edwards since he made his announcement and, "He didn't express to me any indication that he wants to come back." Some other team leaders say they haven't heard anything from him.
It is getting along toward corn and bean harvesting season in Missouri. And Carl does like to drive those machines, too.
(FORMULA 1)—It's tempting to say that Lewis Hamilton put a lock on his fourth F1 championship with his win in the Japanese Grand Prix on the Suzuka circuit, increasing his lead over Sebastian Vettel to fifty-nine points. It's Hamilton's fourth win the last five races and gives him a fifty-nine point lead over Vettel, who dropped out after four laps.
Hamilton's fourth championship will make him the United Kingdom's most successful Formula 1 driver, giving him one more than Jackie Stewart.
The next Formula 1 race will be within driving distance for many Missourians. It's on the Circuit of the Americas near Austin, Texas next Sunday.
(IndyCar)—Helio Castroneves is done as a full-time driver in IndyCar. Roger Penske will have a car for him in May as Castroneves tries again to win his fourth Indianapolis 500. Otherwise, he'll be racing on Penske's new sports car team in the IMSA series. Castroneves moves to the team's fourth car for the 500, eliminating Juan Pablo Montoya's ride in the race with Penske. He's free to sign with another team although he, too, will be in sports cars this year for Penske.
One-time Indianapolis 500 winner Tony Kanaan will drive for five-time winner A. J. Foyt full time next year. Kanaan won the 500 in 2013. Foyt has four wins as a driver and owned the car that Kenny Brack won the race with in 1999. Kanaan lost his ride with Chip Ganassi Racing at the end of this season.
Stefan Wilson is getting his Indianapolis 500 ride back with Andretti Autosports. He gave up his seat this year so former Grand Prix champion Fernando Alonso could run the race. Wilson would like to use the 500 to attract enough sponsor support to run more races next year. His brother, Justin, was killed in a racing incident at Pocono in 2015.
(Photo credits: NASCAR)
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redpajama_set_name: RedPajamaCommonCrawl


It's sad, but it's true. Scams are something that dominates the binary options trading market. They can be in any form – robot services or scam brokers. You have to be always prepared and cautious against all sorts of binary options scams. For your convenience, we have prepared a scam list along with highlighting the name of scam brokers.
On this page, you can find the list of non-recommended binary options brokers. Anyway, it doesn't mean that all the brokers on this list are fraudulent and steal money. We can just not recommend them for another reason. After a click on the brokers' logo, you can see the detailed information and the review. In the case you see a mistake, do not hesitate and sen dus a comment. We really value your help. Our aim is to be constantly adding new and new brokers, both reliable and on the other hand also the brokers, who have lost our trust.
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From what was said above, the main issue doesn't lie with the concept of binary options trading but with the principles of binary options brokers and other providers. So, what you need to do is chalk out a proper plan and do the needful homework before choosing any respective platform. Go through the reviews, provided they are reliable. Fake brokers reviews are also quite common; therefore you should not entirely make any decision based on the reviews. Testimonials and reviews published on a broker's website are often compromised, so don't form an opinion based on that. In fact, trader forums can also be manipulated by a particular binary broker or his website.
The best way to choose a brokerage firm is by relying up on independent, personal and comparative reviews. Select review sites that only allow real-life users to directly contact and file a problem with a particular broker, thus guaranteeing credibility and transparency to the issue. Have a look at the list of our recommended brokers for example. There's a discussion beneath every single review.
The US recognize binary options instruments as financial instruments. So do European courts. Depending on the locations and the countries, binary trading falls or not falls under any particular regulatory authority. Some of the authorities are CFTC in the US and CySec in Cyprus.
To inspect a broker's reliability quotient, regulatory status can serve as a good indicator for those who want to avoid scams. When a brokerage firm falls under a particular standard or regulatory authority, he is bound to maintain transparency.
The trading on binary options should be done in a straightforward way. For this, the platform of trading should be reliable and quick. The profits can be predicted by carefully analyzing the market and reading the future market conditions while understanding future strategies. However, if a somebody with a binary options strategy comes to you and assures you 95% success rates then that can turn out to be a false assurance. No one can say whether you are going to strike profit or loss, as everything depends on speculation.
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Bonuses are also given from time to time and are widely associated with deposit retention. Though CySec has banned these kinds of deposit match bonuses, non CySec firms are at liberty to use them. However, you should always check the binary broker's terms and conditions thoroughly.
A fair and transparent benchmark should be followed by the brokers to set up prices. This benchmark should be based on real world market situation. If by any chance broker decides to set their own prices then you must assume that those figures have been tampered with. These unscrupulous brokers will try their level best to force you to pay higher prices, hence you must be well-guarded.
For more guidance and information on regulations and features, you can anytime read our independent reviews.
Disputes of varying kinds are reported in several online forums about trading. The complaints can be filed against the brokers directly or through online forums (Such as 24 option forum). The issues can be myriad, from encouraging poor traders to over trade to giving faulty information to price manipulation. Now, if you are dealing with unregulated brokers then little help can be provided. For all these factors, it is always advisable to establish relations with trusted binary options brokers from a country in which you reside.
Though scams have become synonymous with poor services yet you cannot ignore dishonest trading practices committed by some of the unreliable brokers. And if you have any doubts, don't trade with that particular broker. There are many honest brokers, just find one for yourself from here.
Robotic services are mostly either scams or not at all recommended.
How to find out a trading strategy scam?
The Internet is flooded with handsome deals of doubling your money. You will find numerous ads, posts, and articles on how to make you rich overnight. But your conscience and think is that really possible. With such deals, obviously, there might be some hidden factors and issues which need to be considered.
Being good in strategies doesn't mean you have the ability to be a good trader. To become a proficient trader, you need a proper system. When you plan something, you have to devise a plan of how to enter the market as well as exit the market along with managing your money. You also have to consider the present market condition and in accordance to that, you have to do everything. In a case of a strategy, the above said things will hold true except the thing said about market conditions. Binary option strategies may not be right for trading as it includes many missing information.
As marketers are sharp and shrewd, they can easily name a product as a system and give it a complete structure. Hence, you need to watch out for several factors that can make your product a complete waste of money.
Also known as the opaque black box, a boxed system is something that fails to make you understand how a strategy works. Suppose you have bought a product or system that says when you should trade but it doesn't specify any underlying reasons.
If a trader doesn't know the reasons behind some happenings then it is pointless to buy such products. And if such products fail to operate then you have nothing to do. Though you may gain with this product preliminary but in the long run it may sound too effective.
Some ask whether 90% win rates are possible or not. Well, the answer is you can enjoy 90% win rates but at the same time, you can also lose money with 90% win rates. However, stats can easily be manipulated with tampered figures. Some says that you can make $500 per day but in reality, they hardly make any sense.
Before investing in anything, make sure you read between the lines. What is highlighted and what is not. To understand how well you will perform you need to gather few pieces of information, like account size or capital invested, amount of profit per trade, amount at risk on each trade, percentage return, win/loss ratio, biggest loser, biggest winner, average loser, average winner, number of trades and time period during which the strategy was tested.
Apart from all these, there are some other metrics which can help you. Now, if the company from which you ask for these bits of information doesn't help, it is time to be suspicious.
Never choose trading platforms that operates only in one direction. As markets rise and fall, you will obviously want to be a part in both the trends.
A good product or service should not only satisfy you by fulfilling the desired purpose but should also make you understand behind-the-scene modules. By having clear glimpses of the reasons, people can start trading on their own. There is no point in making customers dependent on the product itself throughout.
Don't believe in the statistics that are presented to you. Ask yourself some questions. Use your conscience to make powerful decisions. Never base your judgments on a broker's past performance. Do your necessary homework and research before buying a particular product. Also, don't forget to try out a product or service or system before you purchase it.


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Too busy for creativity – return to normality is affecting our time commitments December is often a funny time, but it feels...
From left: David Orr, National Housing Federation; Emma Maier, Inside Housing; Rachel Johnson, Bright Blue; Shaun Bailey, London Assembly, and Sean Astee, Trafford Council
Trafford leader says safer housing needed in wake of Grenfell
4 Oct 2017, 11:56
Alice Cachia
Cllr Sean Astee, leader of Trafford Council, has said that housing is "becoming the defining issue in our generation" during a fringe event at the Conservative Party conference, and that the Grenfell Tower fire will be a key event for years to come on the need for safer social housing.
A debate called 'The future of social housing in modern Britain' was held in Manchester Town Hall, in which panellists discussed the aftermath of the Grenfell Tower fire and building safer social housing.
Chairing the discussion was non-executive director of Bright Blue think tank and journalist Rachel Johnson, who was joined by David Orr, chief executive of the National Housing Federation; Emma Maier, editor of Inside Housing; Shaun Bailey, London Assembly member and deputy chairman of the regeneration committee, and Cllr Sean Anstee.
Anstee said: "The population is going to rise by 300,000 over the next generation, yet last year we built the lowest number of houses in 24 years which does not make sense.
"Grenfell is systemic of the failure of social housing to provide safe homes for the most vulnerable in society. We have got to build more to accommodate the growing population, and it is in London's interest that the North is successful because we have more space."
Maier said: "There were fires before Grenfell and lessons were not learned. There was one in August 2016 in the Shepherd's Bush tower in the afternoon when luckily nobody died, but it took until the spring of this year for the fire brigade to admit the cladding was why it had spread.
"There is clearly an issue for building standards and safety is a priority. Why did the fire services not make information on the cladding public? It was only through FOIs that we learned the cladding was responsible for the Shepherd's Bush fire.
"In building social housing, safety standards must be paramount."
Orr agreed with Maier, and said: "We need to get a much more systematic way of recording fire safety checks, so that two inspectors don't give two completely opposite results. We have to address this because people in social housing are feeling marginalised and objected, and that comes to a crescendo with a howl of anger from Grenfell."
Bailey criticised how "everyone attacks the Tories but nobody has attacked Labour for failing to address Grenfell." He urged that "We [the Tories] have to show the people of Grenfell that we care. I don't care how you do it – use social media, use whatever, just call Labour into question."
Questions from the floor asked how the Tory Government would produce better, safer social housing.
Bailey added: "We [the Tories] must show we have the will to spend money and prioritise that. We must build on the Green Belt where necessary. If you want people to talk about the Conservatives, we have to talk about Green Belt sites and where we can build and that cannot be ignored.
"There is no magic pot of money, and unlike Labour, the Tories must be prepared to prioritise what money is spent on instead of promising everything. Social housing must be one of those priorities.
He added that: "Architects are building ugly houses with units that face away from each other, and that detracts from the sense of community. Architects have a responsibility to build nicer social houses for people to live in."
The Greater Manchester combined authority last week published an update on high rise buildings which stated that local authority building controls have seen an increase in workloads relating to the need to re-inspect and advise on the suitability and safety of cladding systems. The update also reported that "the current approach to securing fire safety in high rise buildings is not fit for purpose, is open to interpretation, and is inconsistently applied."
Trafford lacks ambition most of the time….
October 05, 2017 at 10:17 am By Schwyz
Typical Schwyz comment….yaaaaaawwwnn. change the record
October 05, 2017 at 1:41 pm By Deh'Traff