soap noodles manufacturing process soap noodles manufacturing process

Soap Noodles Manufacturing Process

He further noted that “apart from the process line, we have fully installed three lines for soap finishing; each has a capacity of 2 tonnes per hour for the production of laundry, multipurpose and toilet soaps respectively”. Nwaorgu added: “The ...

Soap Noodles Manufacturing Process

Photos of Sabmiller Plant Onitsha, Highest Foreign Direct Investment In Nigeria / I Want To Show You How To Produce Soap To Meet International Standard At The Mos / Crazy Government Bans - Soap Noodles (1) (2) (3) (4)

As part of its concept to produce locally the basic raw materials, Orange Drugs Limited is set to produce ‘soap noodles’ at its subsidiary –Orange Drugs Limited Onitsha Plant.

The production at Orange Drugs Limited Onitsha Plant which will be commissioned this month, is for the company’s internal consumption and sale to other companies in the same industry, within and outside Nigeria.

Industry watchers say the diversification has given Orange Drugs Limited a competitive edge in terms of cost advantage and consistency in quality of its basic raw material input.

Orange Drugs Limited is one of the three subsidiaries of Orange Group Limited, the other two are Orange Kalbe Limited and Orange West Africa Limited.

Speaking to journalists in Lagos, Henshaw Nwaorgu, plant manager, (soap), Orange Drugs Limited said “the saponification process plant comprises of the tank farm (with tanks to store over 20,000 metric tonnes of PKO/CPO/Tallow); the bleaching plant; the boiler (steam generation); water treatment plant; caustic dissolving unit; the saponification crusher (two units of 25 tonnes each); the spray dryer; and two storage silos.”

According to him, “Orange Drugs Limited Onitsha Plant was fully installed in April 2011 and test runs were conducted in May 2012 with our technical teams from Germany and Italy and other well tested Nigerian professionals.”

He said the plant currently has the capacity to produce five tonnes per hour equivalent to 80 tonnes in two shifts per day (of eight hours per shift). “This is the phase currently being commissioned. Capacity per annum is estimated at 19,200 metric tonnes. The second phase to be commissioned in October 2013, would eventually bring the factory to its full capacity of 15 tonnes of soap with 12 finishing lines”, Nwaorgu said.

He further noted that “apart from the process line, we have fully installed three lines for soap finishing; each has a capacity of 2 tonnes per hour for the production of laundry, multipurpose and toilet soaps respectively”.

Nwaorgu added: “The company has a vibrant workforce with technical knowhow that are constantly evolving new products to meet the demands for our teaming consumers locally and internationally. The factory has a proposed workforce of 1,200 persons, thereby creating job opportunities as well as establishing Orange Group as a major contributor to the creation of jobs in Nigeria.”

Please moderators move this thread to the front page and help me to display the message and picture in the links that i provided. Thanks. Here is the picture of the giant factory. It is bigger than what is in the picture and it would be commisioned this august. www.naijahottestgist.

Lord Naya: Please moderators move this thread to the front page and help me to display the message and picture in the links that i provided. Thanks. Here is the picture of the giant factory. It is bigger than what is in the picture and it would be commisioned this august. www.naijahottestgist.

The Dubai dreams takes years of financial discipline/investment and less corrupt environment to come through. On that note, not only one person or groups of persons can achieve the Dubai dream, but EVERYONE. Anambra may be at it, but still far from the reality of Dubai dream.

The Dubai dreams takes years of financial discipline/investment and less corrupt environment to come through. On that note, not only one person or groups of persons can achieve the Dubai dream, but EVERYONE. Anambra may be at it, but still far from the reality of Dubai dream.

It is this kind of vision that drove the rulers of Dubai to turn a semi desert to attract the best of talents and capital from all over the world, and today Dubai is everybody’s dream destination. A similar strategy was deployed by Taiwan, harnessing its strategic location and endowments. When they started, their initial plans were dismissed as ‘unrealistic’.

Soludo envisions Anambra, with its peculiar small landmass, as one “Free Trade Zone.” Some of his programmes range from the Sir Louis Odumegwu-Ojukwu airport, metropolitan urban renewal programmes to turn the ‘ONA axis’ (Onitsha, Nnewi, Awka axis) into commercial and industrial hubs; revolution to turn the more than 40,000 four-storey buildings in Onitsha which are now dead assets into viable, collaterable assets that can be used to secure substantial bank loans for business; the commercial agriculture strategy to work with Malaysians and Israelis to turn Omambala and Orumba zones into agricultural and agro-industrial parks to feed Nigeria, the plan for a brand new modern city, industrial parks, plans for community development, erosion control, education and health, as well as security. It is long and indeed ambitious.

I am particularly excited by Soludo’s brand new city idea by which he proposes to extend the current capital city (the Greater Awka into Awka North) or the Greater Onitsha into Nsugbe/Otuocha axis. The proposed six kilometre boulevard adorned with many shopping malls including the Anambra Shopping World which he believes would be Africa’s largest shopping mall with international brands, world class recreational parks, hotels, cinema, restaurants and the likes, would be a dream come through. The world’s most beautiful Avenue is Champs Elysees in Paris and no one goes to Paris without visiting Champs Elysees, which is only 1.9 kilometres long. The Anambra Boulevard promises to be Africa’s ‘must visit’ location, and will be a signature project in the new city. A well planned new city with modern facilities, together with the new airport, and industrial/commercial and agricultural parks will kick-start a dynamic domestic economy to which most of us would proudly want to relocate.

I am also excited about Soludo’s five million hybrid palm seedlings programme to re-engineer the palm revolution and compete with Malaysia and Indonesia as world’s largest palm producers. I understand that 50 - 100 hybrid palms can lift a poor household out of poverty, and this would mean 50,000 households. Imagine the agro-processing industries that would emerge, the revenue to government, and prosperity to all. Malaysia took its palm seedlings from Anambra in early 1960s and created prosperity with them.

The innovative Community Government is a study in comprehensive grassroots development framework that will involve the people in addressing their peculiar local needs. I can go on and on.

Soludo has insisted that Anambra cannot be developed with Federation Account allocation but by private capital. There must be very few people with Soludo’s national and international networks and personal capacity to mobilize private capital to transform Anambra.

He has done it before. When Soludo dreamt of the Africa Finance Corporation (AFC) to do what the African Union could not accomplish in over 25 years, many thought it was a joke but he did it and AFC is now Africa’s number one infrastructure bank. He dreamt of consolidating the banking system and most people said it was ‘impossible.’ Soludo set out to put Nigerian banks on the global map, and announced that he wanted Nigerian banks in the top 100 banks in the world within 10 years. Most people thought this was ‘idealistic.’ In three years, he put two Nigerian banks in the top 300 banks and 12 others within the top 1000 banks. What Soludo brings is his ever restless and cerebral capacity to think big and exceptional execution capacity.

To me, ADT is a clear roadmap to prosperity. It was Oliver Wendell Holmes who once said that, “Once a mind has been stretched by a new idea, it never returns to its original shape.” Soludo has stretched the minds of Ndi Anambra with a new idea. Now, we cannot wait again. Happy birthday to you, my brother!

The picture you saw is the administrative buildings, the main factory is massive. It is located at the Ogbaru industrial layout near Onitsha. The goodnews is that not only will this factory be manufacturing various finished products, it will also be producing the raw materials and semi-finished products that would be bought by various firms within and outside the country. The factory is fitted with the latest technological equipments and manned by professionals. So the main factory which is not on the above picture is big.

Lord Naya: The picture you saw is the administrative buildings, the main factory is massive. It is located at the Ogbaru industrial layout near Onitsha. The goodnews is that not only will this factory be manufacturing various finished products, it will also be producing the raw materials and semi-finished products that would be bought by various firms within and outside the country. The factory is fitted with the latest technological equipments and manned by professionals. So the main factory which is not on the above picture is big.

No doubt he has what's good in mind for the people, however, the discipline is required. If there's no fiscal responsibility and financial discipline, you can have a ton of good stuff which will not worth it.

The Dubai dreams takes years of financial discipline/investment and less corrupt environment to come through. On that note, not only one person or groups of persons can achieve the Dubai dream, but EVERYONE. Anambra may be at it, but still far from the reality of Dubai dream.

Everyone in the world agrees Dubai is a soulless city built with and on slaves from Asia and East Africa. Don't look to Dubai when there are so many better less gaudy options. All the glitters....

Everyone in the world agrees Dubai is a soulless city built with and on slaves from Asia and East Africa. Don't look to Dubai when there are so many better less gaudy options. All the glitters....

i thought they already have varieties of soap in the market? well its a welcome development to the people of anambra.btw i know tony ezenna to be from orlu zone in imo state. i pray he extends his industry to imo too.we are in dire need of industries!

why dont u just move on with the topic instead of igniting a tribal conflict.haters will always be around to condemn or make mockery of anything good.so mechionu and face the topic!

Everyone in the world agrees Dubai is a soulless city built with and on slaves from Asia and East Africa. Don't look to Dubai when there are so many better less gaudy options. All the glitters....

Thank you, my brother. I've always said it on this forum that Dubai is just about the worst analogy one can use for a success story.

berem: why dont u just move on with the topic instead of igniting a tribal conflict.haters will always be around to condemn or make mockery of anything good.so mechionu and face the topic!

berem: why dont u just move on with the topic instead of igniting a tribal conflict.haters will always be around to condemn or make mockery of anything good.so mechionu and face the topic!

berem: why dont u just move on with the topic instead of igniting a tribal conflict.haters will always be around to condemn or make mockery of anything good.so mechionu and face the topic!

berem: why dont u just move on with the topic instead of igniting a tribal conflict.haters will always be around to condemn or make mockery of anything good.so mechionu and face the topic!

Y wuld people behav lite they are fooools on NL. U copy a whole thread 2write little or nothin while we hav all read it. This is stupiiidy.

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insprocess of sugar manufacturing tant tea manufacturing process

Instant Tea Manufacturing Process

In the leaf tea manufacture process, the dryer exhaust containing aroma volatiles can be cooled to obtain an aqueous condensate containing aromavolatile compounds. The evaporator condensate stream in instant tea ...

Instant Tea Manufacturing Process

Patent 8257769 Issued on September 4, 2012. Estimated Expiration Date: December 10, 2028. Estimated Expiration Date is calculated based on simple USPTO term provisions. It does not account for terminal disclaimers, term adjustments, failure to pay maintenance fees, or other factors which might affect the term of a patent.

The invention relates to a process for recovering volatile compounds from an aqueous tea extract. The invention particularly relates to a process for recovering and concentrating tea volatile compounds e.g. aroma compounds from dilute aqueoustea condensate streams and other waste steams.

Tea is one of the most widely consumed beverage in the world. Tea is available in many forms e.g. as green tea, black tea, hot instant tea, iced tea etc.

Green tea is generally prepared by heat treating (e.g. by steaming or pan-frying) freshly picked leaves to arrest enzyme action and then subjecting the leaves to a series of drying and rolling steps.

Black tea is generally prepared by subjecting freshly picked tea leaves to a series of processing conditions including withering and macerating the fresh tea leaves, followed by fermentation which mainly contributes to the characteristic colour,flavour and aroma of black tea. The tea is dried at high temperature after fermentation to arrest the enzyme action and to bring down the moisture to a low level.

Green tea and black tea are products which are brewed in hot water to produce tea infusions in the hot water wherefrom the tea leaf insolubles have to be filtered before the infusions are consumed. Hot instant tea is a product which contains nowater insolubles. This hot instant tea product is fully soluble in hot water and this solubilized product can be consumed as such without any filtration. Iced tea is a product made from tea where the fully water-soluble fractions of tea are dissolvedin water with or without additional flavours and the dissolved tea solution is kept chilled in a refrigerator before it is consumed.

The process for the preparation of hot instant tea and iced tea are described in literature. One such description can be found in the reference book `Tea--Cultivation to Consumption` edited by K. C. Wilson & M. N. Clifford & published byChapman & Hall (1992).

Many tea manufacturing processes produce by-product streams that contain aroma volatile compounds. In the leaf tea manufacture process, the dryer exhaust containing aroma volatiles can be cooled to obtain an aqueous condensate containing aromavolatile compounds. The evaporator condensate stream in instant tea manufacturing processes also contains aroma volatile compounds. However, the aroma in these condensate streams is usually present at very low levels. Typically the concentration ofaroma volatiles in the condensate streams is below 500 mg/l, and often less than 50 mg/l and can be as low as 10 mg/l. This dilute nature of the aroma in the condensate streams restricts their application as a source of aroma for add-back. Thesecondensate steams are often not utilized or are limited in their use due to the extremely low concentrations. In many cases these streams are even discarded, leading to loss of precious aroma bearing compounds. This is because the known processes forrecovery of these compounds are either not technically and/or commercially viable or are very inefficient. Tea aroma is one of the most important factors for determining tea quality. Hence tea with good aroma profile fetches a premium in the market. Recovery of aroma volatile compounds from the condensate streams can provide a source of natural tea aroma that can be used for add-back and improving the aroma of the tea.

Many processes to recover and concentrate volatile compounds from dilute streams have been known and practised. These processes include reverse osmosis, distillation, cryoconcentration, freeze drying, staged/partial condensation and pressureswing adsorption. Distillation has always been one preferred process. GB 1061009 (Salada Foods, 1967) describes a process for recovery of aroma from aqueous tea streams using distillation carried out in an inert atmosphere. The present inventors havedetermined that using the method described in the GB publication, the quality of the tea aroma recaptured improves to a small extent but a large percentage of the aroma present in the tea aqueous extract can not be recovered using this process and thereare high losses.

It is an object of the present invention to provide for a process for the enhanced recovery of volatile compounds from aqueous tea extract streams like condensate streams from hot instant tea and ice tea manufacture.

It is another object of the present invention to provide for a process for the recovery of volatile compounds like aroma compounds in more concentrated forms as compared to known processes of the prior art.

According to the first aspect of the present invention there is provided a process for recovering volatile compounds from an aqueous tea extract by distilling the said extract by fractional distillation comprising condensing of vapours,separating the oil phase condensate from the aqueous phase and refluxing the substantially oil-free aqueous phase.

It is further particularly preferred that the fractional distillation is carried out in a distillation assembly that contains less than 5 volume percent of non-condensable gases prior commencing the distillation operation.

It is even further particularly preferably that the distillation assembly is filled with steam before commencing the distillation operation.

According to a second aspect of the present invention there is provided a process for producing tea with enhanced aroma comprising mixing tea with the volatile compounds recovered by the first aspect of the invention.

"Tea" for the purposes of the present invention means material from Camellia sinensis var. sinensis or Camellia sinensis var. assamica. It also includes rooibos tea obtained from Aspalathus linearis. "Tea" is also intended to include theproduct of blending two or more of any of these materials.

The aqueous tea extract of this invention could be from any of the following tea sources: fermented tea (i.e. black tea), semi-fermented tea (i.e. oolong tea) and/or substantially unfermented tea (i.e. green tea). "Fermentation" refers to theoxidative and hydrolytic process that tea undergoes when certain endogenous enzymes and substrates are brought together, e.g., by mechanical disruption of the cells by maceration of the leaves. During this process colourless catechins in the leaves areconverted to a complex mixture of yellow and orange to dark-brown polyphenolic substances. Alternately and preferably the aqueous tea extract could be spent or waste condensate streams from processes for preparing hot instant tea/iced tea.

Many volatile compounds contribute to the aroma of tea. A list of most of the aroma volatile compounds is reported in `Tea--Cultivation to Consumption` edited by K. C. Wilson & M. N. Clifford & published by Chapman & Hall (1992). Some of theimportant tea aroma compounds from this list are acetaldehyde, benzaldehyde, benzyl alcohol, t,t-2,4-decadienal, b-damascenone, diacetyl, geraniol, c-4-heptenal, t,t-2,4-heptadienal, t-2-heptanal, 2,4-hexadienol, 1-hexanal, 1-hexanol, hexanoic acid,c-3-hexenol, t-2-hexenal, b-ionone, linalool & its oxides, methional, 2-methyl butanal, 3-methyl butanal, 2-methyl propanal, methyl sulphide, methyl salicylate, nerol, t-2,c-6-nonadienal, t,t-2,4-nonadienal, nonanal, octanal, t-2-octenal, 1-octene-3-ol,1-pentanol, t-2-pentenal, 1-penten-3-ol, phenylacetaldehyde, 2-phenylethanol, a-terpenial, and vanillin.

A number of aqueous condensate streams containing aroma volatiles are available or potentially available from tea manufacturing processes. The concentration of aroma volatiles in these aqueous condensate streams range from 10 mg/l to 500 mg/l.Such streams include the one from aroma capture from the dryer exhaust in leaf tea manufacture described in WO 2007/039018. Aroma stripping from tea extraction processes before its concentration has been described in patents GB 855 423, GB 1 490 370 andU.S. Pat. No. 3,717,472. All these processes result in aqueous aroma condensates. Similarly, the condensate collected in the evaporation stage for concentration of soluble solids also has aroma volatiles, though at very low levels.

In the present invention, the volatile compounds can be recovered from waste streams which would otherwise have fetched no value. The invention has the advantage in that the volatile compounds are recovered and concentrated to a low watercontent. The invention also provides for concentrating the aroma compounds to a form of nearly pure oil. The concentration of the volatile compounds by the process of the invention provides for improved economy when they are added back to tea toprepare aroma enriched tea. Since the concentrate has low water content, tea to which it is added requires very little or no subsequent drying to prepare an aroma enriched tea product. Hence the process preferably comprises simply spraying theconcentrate on to tea and packing the sprayed tea.

The first aspect of the present invention provides for a process for recovering volatile compounds from an aqueous tea extract comprising fractional distillation of said extract in a distillation assembly wherein the vapours are substantiallycondensed, the oil phase in the condensate is separated from the aqueous phase and the substantially oil-free aqueous phase is refluxed. The fractional distillation is preferably a multi-stage batch distillation.

The process preferably comprises substantial condensation of the overhead/rectified vapours. This may be achieved using cold traps, cold fingers or any other known condensation methods.

A preferred aspect of the invention provides for a process wherein the assembly contains less than 5 volume percent of non-condensable gases prior to charging the aqueous tea extract to said assembly.

A further preferred aspect provides for the distillation assembly to be substantially free of air or any other non-condensable gases before commencing the distillation operation. Most preferably the distillation assembly is filled with steambefore commencing the distillation operation. By the phrase `non-condensable gas` is meant to include those gases having a vapour pressure greater than 1 bar (absolute) at 0° C. Examples of commonly used non-condensable gases are air, oxygen,nitrogen, carbon dioxide, and helium.

The process of the invention is capable of recovering and concentrating aqueous tea extract which generally has 10 to 500 ppm of volatile compounds. Starting with such a concentration, the distillation process of the invention recovers andconcentrates the aroma compounds to a concentration higher than 20000 ppm. It is also possible to concentrate it to nearly pure oil. The inventors have used all the recovery and concentration equipments known to them and available in the art forconcentrating aqueous tea extracts and found that with known equipments, the extract could be concentrated by a factor of at most 40. Using the process of the invention, a concentration factor of greater than 80, sometimes greater than 100 could beobtained. It has also been found that out of the total amount of the volatile compounds in an aqueous tea extract, nearly 70 to 85 percent of the volatile compounds can be recovered by the process of the invention. Thus the losses are at most 30%.

The distillation assembly used for the process of the invention generally comprises a reboiler, a distillation column, a condenser and a liquid-liquid separator. The process is optimally operated when the volume ratio of the total feed to thereboiler to the total condensate hold up in the condenser and liquid-liquid separator at the conclusion of the distillation operation is higher than 100, preferably in the range of 100 to 2000, more preferably in the range of 100 to 500.

A very important advantage of the present invention is that the process can be carried out at close to ambient conditions of pressure i.e. pressures close to atmospheric. The distillation is generally carried out with reboiler temperatures near100° C., preferably in the temperature range of 80 to 100° C. The reboiler is heated to this temperature using any known heating means e.g. using a electrically heated resistance coils, or the reboiler could be jacketed and hot water orsteam could be passed through the jacket to heat the material being distilled.

A suitable method of ensuring that the distillation assembly does not comprise more than 5% non-condensable gases before commencing the distillation operation, is to fill it up with steam while purging the air out of the assembly. Steam may betapped form an external source e.g. a boiler and piped into the assembly. Alternately, a small amount of water is initially taken in the reboiler and all of the water is boiled off to steam to fill up the distillation assembly while the air is purgedout of the assembly.

A preferred method of ensuring high recovery and minimizing loss of volatiles is by following a practice wherein the aqueous tea extract desired to be concentrated is not added to the reboiler at the start of the process. Initially, water,which comprises a small percentage e.g. 5 to 10 wt % of the total aqueous tea extract feed to be distilled, is added to the reboiler. The distillation operation is started with this feed and a total reflux is established. The operation is carried outtill the air is purged from the column. Thereafter the aqueous tea extract is gradually added to the reboiler while ensuring that a reflux is maintained as the distillation process is carried out. It has been found that in a typical batch of 100 kg ofaqueous tea extract, the distillation operation can generally be completed in a time of 4 to 6 hours.

The distillation assembly has a distillation column which is preferably filled with packings which preferably provides a low hold up in the range of 10 to 20%. To achieve this end, packings are generally chosen from structured packings, wiremesh packings, saddles or Raschig rings. The packed column for the process of the invention is generally kept short and usually does not require more than 10 equilibrium stages, preferably 3 to 5 equilibrium stages. Having such short columns alsoensures lower equipment cost and thereby improves the commercial viability of the process. A preferred condition for carrying out the process of the invention comprises carrying out the distillation at a low boil-up rate, preferably in the range of 30to 40% of flooding. The distillation is preferably carried out under near total reflux conditions.

The distillation assembly preferably has a condenser that is a shell and tube condenser, preferably vertically mounted. The vapors are preferably be fed to the vertical condenser from the top. The vapors are preferably be fed to the tube sideof the condenser.

The distillation assembly is preferably operated at conditions that ensure minimal or substantially no internal reflux. This is ensured, for example, by providing good insulation on all the units and pipelines where flow of vapours occurs. Ensuring minimal or substantially no internal reflux is especially important during the start-up stage to ensure minimal loss and maximum recovery of volatile compounds. This is achieved, for example, by ensuring that the distillation column isexternally heated during start-up. The heating may be by known method e.g. by providing steam in a jacket around the distillation column.

It has also been determined that the pipelines for transporting the vapours in the distillation assembly are preferably of a small diameter. It is especially preferred that the ratio of the diameter of the liquid-liquid separator to thediameter of the pipeline downstream of it is greater than 2, preferably in the range of 2 to 20, more preferably in the range of 10 to 20.

As shown in FIG. 1 the distillation assembly comprises a reboiler (E1) equipped with a jacket (J1) to which aqueous tea extract can be added through valve (V1) and residue can be drained using valve (V2). The assembly is equipped with a packedcolumn (E2) filled with Raschig ring packings. A vertical shell and tube heat exchanger (E3) is provided to condense the volatiles. A valve (V3) is provided on condenser (E3) to drain any condensate. A liquid-liquid separator (E4) is provideddownstream of the condenser to collect the concentrated volatile compounds. Various liquid-liquid separators may be used. Preferred ratio of the volume of the reboiler to that of the liquid-liquid separator is in the range of 50 to 2000, morepreferably in the range of 100 to 500. A valve (V4) is provided at the top of the liquid-liquid separator as an oil overflow valve. A product discharge valve (V6) as shown is provided to collect the concentrated volatile compounds. A reflux valve (V5)is provided to control the reflux ratio at which the distillation is carried out.

When in use, calculated amount of water is first added to the reboiler (E1), the water in the reboiler is heated by passing steam in the jacket (J1). As the water in the reboiler boils to form steam, the steam is allowed to fill up all parts ofthe distillation assembly, and the air is purged from the assembly using the various vent valves. When the distillation assembly is substantially filled up with the condensable gas viz. steam, the aqueous tea extract is added to the reboiler to beginthe distillation. Initially a part of the total amount of tea extract is added to the reboiler. The overhead vapours are condensed in the condenser, the oil phase in the condensate is separated from the aqueous phase and the substantially oil-freeaqueous phase is refluxed. The reflux valve is adjusted to the desired position to get the desired reflux ratio. As the process attains close to steady state operation, the rest of the tea extract is added intermittently to the reboiler. The reboileris usually kept filled to 5 to 70 volume percent filling. As the distillation proceeds, the concentrated volatile compounds collect in the liquid-liquid separator (E4). At the end of the process, the concentrated volatile compounds are drained throughvalve (V6) and collected as desired.

A batch of 20 L of aqueous tea extract having 200 mg/l of volatile aroma compounds was distilled using the process of the invention using the distillation assembly as shown in FIG. 1. In the distillation assembly, the volume of the reboiler was40 liters. A two meter tall glass column filled with Sulzer BX packing was used. The volume of condensate collected was 1000 ml. About 3 liters of water was used initially to purge the air out of the assembly and to saturate it with steam prior toaddition of the tea extract. A two-phase condensate appears almost at the start of distillation--the lighter phase being the oil phase while the heavier phase being the aqueous phase. Care was taken to separate the two phases and only the aqueous phasewas refluxed to the distillation column during the entire operation. The results in terms of (a) percent of volatile compounds lost, (b) the concentration ratio and (c) the % recovery were determined and are summarized in Table-1.

A batch at exactly the same conditions as in Example-1 was carried out except that no water was used to saturate the assembly prior to adding the tea extract . The distillation was started with air filled in the void spaces of the distillationassembly. The corresponding results are summarized in Table-1.

A batch of 144 L of aqueous tea extract having 346 mg/l of volatile aroma compounds was distilled using the process of the invention using the distillation assembly as shown in FIG. 1. About 6 liters of water was used initially to purge the airout of the assembly and to saturate it with steam prior to addition of the tea extract . A two-phase condensate appears almost at the start of distillation--the lighter phase being the oil phase while the heavier phase being the aqueous phase. Care wastaken to separate the two phases and only the aqueous phase was refluxed to the distillation column during the entire operation. The distillation was carried out by gradually adding the tea extract to the reboiler over a period of 8 hours. The totaltime of distillation was 10 hours. In the distillation assembly the volume of the reboiler was 200 liters. About 335 ml of total distillate product rich in aroma was recovered from the liquid-liquid separator of which 30 ml was aroma in pure oil phase. The corresponding results are summarized in Table-1.

A batch of 100 L of aqueous tea extract having 302 mg/l of volatile aroma compounds was distilled using the process of the invention using the distillation assembly and the process similar to Example-3. About 800 ml of condensate rich in aromawas recovered from the liquid-liquid separator. The corresponding results are summarized in Table-1.

A batch distillation run similar to Example-4 was carried out except that the reflux comprised of a mix of oil and aqueous phases. The corresponding results are summarized in Table-1.

Where F is the amount of aroma compound in the feed, P is the amount of aroma compound in the product, B is the amount of aroma compound in the residue and L is the amount of aroma compound lost in the process.

The data in Table-1 indicates that the loss of volatile aroma compounds in the examples as per the invention (Examples 1 to 4) is much less as compared to process of the prior art (Example 5). Also the % recovery in the examples as per theinvention is significantly better then the example of the prior art. Further, with the process of the present invention, product having higher concentration of aroma compounds can be prepared as compared to the prior art.

Experiments were conducted in a distillation assembly similar to that shown in FIG. 1 except that (i) the volume of the reboiler was 10 liters; (ii) the volume of the condenser was 43 ml and (iii) the column was 1 m long packed and had adiameter of 38 mm. It was packed with glass Raschig rings of diameter 12 mm and length 12 mm. Experiments were done to concentrate aqueous solutions of two model aroma compounds present in tea extract solution. The two model compounds used were2-methyl propanal (which is a low boiling compound) and Linalool (which is a relatively high boiling compound). The experiments were conducted similar to Example-1 except that the following conditions were used:

In Experiments 6, 8 and 9 about three liters of feed were fed to the reboiler over the course of distillation. In Experiments 7, 10 and 11, about 5 liters of feed were fed to the reboiler over the course of distillation. In all the experiments30% of the feed was boiled over.

The distillation was conducted after purging the assembly of air and filling with steam prior to the start of distillation. The feed was added gradually over a period of 3 hours and the total time of distillation was 4 hours.

The distillation was conducted starting with air present in the assembly. The reboiler was filled with all of the feed at the beginning of the experiment. The total time of distillation was 4 hours.

The distillation was conducted after purging the assembly of air and filling with nitrogen prior to start of distillation. Nitrogen flow was stopped gradually once the system filled up with the vapours of the feed. The total time ofdistillation was 4 hours.

TABLE-US-00002 TABLE 2 Concentration Model Concentration in product, Concentration % % Example compound in feed, mg/L mg/L ratio recovery losses 6 2-methyl 97 4905 51 54.8 15.0 propanal 8 2-methyl 133 950 7.2 6.6 92.4 propanal 9 2-methyl 96 72

Process of Sugar Manufacturing

Renmatix, manufacturer of cellulosic sugars for biobased chemical and fuel markets, has announced the opening of a new research and development center in Pennsylvania. ... facility is to accelerate the company's exploration of new sustainable feedstock sources, assist downstream customers in their transition to cellulosic sugars, and further enhance the economics of the Plantrose process to produce the lowest cost sugar intermediates for renewable materials.

Process of Sugar Manufacturing

Sustainable Plant - Manufacturing Best Practices for the Energy Efficient Industry Professional. Facebook Twitter LinkedIn RSS Follow Us:

Share on emailEmail Share on printPrint Share on tweetRenmatix, manufacturer of cellulosic sugars for biobased chemical and fuel markets, has announced the opening of a new research and development center in Pennsylvania. The multi-million-dollar facility is to accelerate the company’s exploration of new sustainable feedstock sources, assist downstream customers in their transition to cellulosic sugars, and further enhance the economics of the Plantrose process to produce the lowest cost sugar intermediates for renewable materials.

The proprietary Plantrose process converts cellulosic biomass – from wood waste to agricultural residue – into useful, cost-effective sugars. The supercritical hydrolysis technology deconstructs non-food biomass an order of magnitude faster than other processes and uses no significant consumables. Renmatix operations in Georgia are currently capable of converting three dry tons of cellulosic biomass to Plantro sugar per day.

“With this new facility, Renmatix will apply its deep technical expertise to expand our feedstock processing capabilities and partner with customers, ranging from emerging biochemical players to Fortune 500 corporations, to incorporate our Plantro sugars into their manufacturing processes,” said Manuk Colakyan, CTO, Renmatix. “We’ve already proven Renmatix’s technology is cost-competitive. Now, we’re looking to further reduce costs as we scale to commercial production.”

Last month, Renmatix announced a joint development agreement with Waste Management to explore the viability of using Renmatix's water-based technology to produce industrial sugars from post-consumer urban waste, including food scraps, construction debris, and paper. The new technical center, equipped with an experienced research staff of chemistry, biology, and process experts, will lead the analysis of urban waste streams, and more than 50 types of sustainable biomass that are available around the world, as future feedstocks for the Plantrose process.

Renmatix’s Plantrose process uses supercritical water – a state in which water acts as a solvent – to economically and efficiently deconstruct a wide range of non-food plant material in a continuous reaction to extract cellulosic sugars. Cellulosic sugars, derived from non-food plant material, are the building blocks of plantrochemicals (petrochemicals made from plants) and the emerging bioeconomy.

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The company’s Acme electrical devices meet criteria established by the company for its Eco-Certified designation. Demonstrating its commitment for a better, cleaner environment, a company has developed an eco-certification designation for a variety of its industrial products, including the company’s entire line of Acme electrical devices. The company’s Acme electrical devices meet criteria established by the company for its Eco-Certified designation:

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The data in Table-2 indicates that superior recovery can be obtained using a preferred aspect of the invention (Examples 6 and 7). Further, the losses using the preferred process of the invention are much lower.

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Siripurapu et al., “Adaptogenic and anti-amnesic properties of Evolvulus alsinoides in rodents” Pharmacology, Biochemistry and Behavior, (2005), vol. 81, pp. 424-432.

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