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Hello In4Luck,
I don't know the exact reason except that it is pretty normal for a company to dilute to cover business expense but we are still way tight on the public float. Anyway, there are too many great things coming to sweat this. It is probably money to promote and entertain during the Olympics and cover operating expense. Once the streams of revenue come in, it will be a totally different story.
Call in and share your perspective if you would.
Regards,
-Greener
Hello In4Luck,
I don't know the exact reason except that it is pretty normal for a company to dilute to cover business expense but we are still way tight on the public float. Anyway, there are too many great things coming to sweat this. It is probably money to promote and entertain during the Olympics and cover operating expense. Once the streams of revenue come in, it will be a totally different story.
Call in and share your perspective if you would.
Regards,
-Greener
I could not have said it better.
Here is a link to what it means to short sell:
Short Sell on You-tube
So these guys cashed there stocks in before doing anything contractual which negated the deal, so Larry gets the stock back and they are left with the broker holding his hand out. So right away they are screwed because if you notice the range they sold in was completely ignorant....like .13 to .11 or even .10
Heres the current ticker with no help:
MVTG
I am confident this is above .13 and anywhere in that range is going to hurt for them.
JMHO
-Greener
Take a deep breath, OK, now......
You don't have to put yourself thru this..... If you don't understand the situation or are uncomfortable.... you know what you need to do. The ball is in your court.
The majority of companies who dilute, go with numbers to the tune of 70 mil are more unstable IMO.
You know what type of things are coming if you are following the PRs.....
Right now, my friend, I honestly don't believe you have been listening to the situation and have a handle on it.
Call in or do whatever it takes to get some peace of mind..... don't air out negativity on this public board, please, we are trying to maintain an atmosphere of research balanced with reason.... maybe a little emotion from time to time... so I understand you are frustrated.... Larry can't be happy with the price either, but guess what, they caught the guy who sold short.
Thats good news, in all likelihood, his funds are still with the broker and he will have to pay the difference, This should turn out good for the pps.
All the Best,
-Greener
Too much drama for me.... where do you get 5 mil from??
I'm sure you call Larry... ask him about it.
-Greener
I don't think that is the point. Larry dealt with these guys, they turned out to be crooked, Larry put the kabosh on the deal so now they will have to buy back the shares they sold because they sold something that was renigged on. Its like selling a car to someone without having the title... you would have to produce and give up the legal title or give back the money. The difference is that stock prices are a moving target.... we all want it to move up before they have to buy back.....then the pps will be up there and their buying will push it up that much more. Thats how I understand it....
I can't do much myself anyway...... funds are low right now. I wish I could help out monetarily and boost my position, put for right now....I can just spread the word.
-Greener
Yeah , let'em go, if they can't hold on to them.... who cares, maybe the next guy will. All I know is, this stock has stability because of management and the decent shareholders we now have.....as few as there are.
Today was a money hemorrhage for many investors, we are only a few trades away from the .15-.17 average. So, I look forward to the Winter Olympics and am trying to post as much DD as possible on message boards to get some fresh action..... every little bit helps.
-Greener
BTW I am sure Larry will extend himself to make this hurt...... unless it is illegal for him to do it.......I can't see why it would be wrong but it may be up to everyday investor to hit the ask so to speak.
Anyone who wants to know more call headquarters for clarification.
MANTRA VENTURE GROUP
Dominion Building
Suite 1205, 207 West Hastings Street
Vancouver
BC
Canada
V6B 1H7
1-(877) 609-2898 (Toll Free)
1-(604) 609-2878
-Greener
Well, if "investor consortium" is the latin verb for turdburger, then I believe they have a period of time to buy back and may not fully be aware until it all hits the fan. They know what they did, but may not be too quick to make their move..... maybe hoping for the price to drop again.
ie: if we can hit the ask a few times it will make it sting more whilst increasing our position. At least thats the idea. Obviously, its not required...... it is just cool to know that we could possibly stick it to one of these clowns for a change.
-Greener
If I understand correctly, some turdburger(s) violated a deal with Mantra and sold shares they didn't own (for next to nothing) and will now have to buy them back(for whatever the going rate is...hopefully .17-.21 or more). So I am sure Larry is going to buy up shares to bump the price up PRIOR to their buy back, This will mean they will get skrewed and the price will go up that much more because they will be buying back. If they are smart, they will hold'em and sell for a decent price.... if they are dumb, they will try to sell cheap to kill the pps for a few days. I doubt they would do that if they had to buy them back at .17 or above.
So it really is in our best interest to get the pps up before the buy back.JMHO
-Greener
This should be pretty substantial.We have seen what this does when 2000 get sold. Low float should provide a great situation. Call Larry or Kol for detials.
-Greener
Short Selling alert
64000 call Larry for details. buy'em up because you know they will have to soon.
-Greener
Mantras site is now tricked out with translator buttons for English, Korean and German. They look like flags from the different countries.... we are going global and not looking back. Lets see, we will probably see Chinese, Spanish, French, and who knows what else in the near future JMHO.
- Greener
Hello,
Great idea, except you don't want to violate the reminders located at the right of the posting box. If you can work within those guidelines it will keep you from being banned. I just paid for my account for this year so I can post on some of the private boards this evening..... every little bit helps.
-Greener
From TD Ameritrade:
Mantra Venture Group announces strategy for 2010
5:10p ET January 13, 2010 (PR NewsWire)
Mantra Venture Group Ltd. ('Mantra', OTCBB:MVTG, FSE,5MV) is please to provide a brief summary of progress made in 2009, and an outline of the corporate strategy for 2010.
The past twelve months have been marked by a prolonged economic recovery - leaving many industries well below the previous highs. Fortunately for Mantra, the global effort of achieving a sustainable recovery has led to new-found stimulus packages that have placed a real emphasis on advancements in environmental sustainability. This has provided oxygen to "fuel the fire" for Mantra's carbon recycling ERC technology.
The following is a summary of Mantra's achievements in 2009.
Technical Advancements - The carbon recycling ERC technology now has a new cathode catalyst structure that has increased the reactor's efficiency to 90% from the previous 46%, and has enhanced cathode stability. The latter, using new IP, is currently being reviewed for patenting. Also achieved was improved conductivity and regeneration of the catalyst. A carbon balance report was completed which indicates a negative carbon balance in making formic acid, yet another ERC advantage.
Business Development - Mantra has expanded its North American network. The company signed an ERC research project agreement with 3M in October. A recognized leader in research and development, 3M has annual sales in excess of $25 billion and employs 75,000 people through operations spanning more than 60 countries. This project is expected to start later this month. Mantra has received extensive interest from international players and now has contacts in Canada, the U.S., Korea, Japan, China, Western Europe and the Middle East.
Mantra was invited to ENTECH 2009 held in Busan, Korea - Korea's largest trade show focused on energy and the environment. Here it met with business and government representatives and several strategic relationships and financing opportunities have since emerged.
Mantra signed a Letter of Intent (LOI) with KC Cottrell Co., Ltd. of Korea - a world leader in environmental technology for over 35 years (http://www.kc-cottrell.com). This will allow the parties to carry out engineering, construction, testing and deployment of a 100 kg per day ERC reactor. The final agreements are pending.
Mantra also signed a collaboration agreement with Ecole Polytechnique Federale de Lausanne's (EPFL) Laboratory of Organometallic and Medicinal Chemistry (LCOM) and Granit Green Networlds, Ltd. (GGN) of Switzerland to engage in a project to convert CO2 to hydrogen fuel using formic acid as the carrier. Various demonstration projects are currently under consideration.
Government Grants - The National Research Council of Canada's Industrial Research Assistance Program (NRC-IRAP) has supported Mantra in two projects: the first, aimed to enhance the ERC technology. Management was very pleased with the outcome. The second is underway. Kemetco Research Inc. carries out the work under the direction of Mantra.
Media Coverage - Mantra's carbon recycling ERC is being recognized:
On December 10th, Larry Kristof, CEO, was featured on Business News Network's "Squeeze Play" with Kim Parlee and Andrew Bell. (http://watch.bnn.ca/squeexeplay/december.2009/squeezeplay-december-10-2009/#clip244949).
On December 5th, the Financial Post published "CO2 captures doubts and the old standbys" including a segment on CCS and Mantra's ERC: (http://www.financialpost.com/story.html?id-2305703 )
District Energy Magazine, November, published "Carbon Recycling: an alternative to carbon capture and storage". (http://districtenergy-digital.org.districtenergy/2009Q4#pg27).
Exploration and Processing, winter edition 2009, gave the cover to Mantra and included article: "Mantra Venture Group explores new ways to reduce carbon emissions". (http://www.nxtbook.com/nxtbooks/shofield/ep_2009winter/index.php#/0)
New Technology Acquisition - In September, Mantra acquired the worldwide exclusive license for the Mixed Reactant Fuel Cell technology (MRFC). MRFC is based on an innovative technology that mixes the fuel with the oxidant and eliminates the need for the expensive yet fragile membrane. MRFC was designed by Professor Emeritus Colin Oloman in the Clean Energy Research Center (CERC) at the University of British Columbia, Canada.
Forecast for the Coming Year (2010) - Mantra has two key projects in development today. Firstly, the ERC technology will be installed as a demonstration in either of two locations. This major project is expected to be implemented mid-year.
The second key initiative is the development of the Mixed Reactant Fuel Cell technology (MRFC). This technology, licensed last year, could replace many of the existing standard fuel cells that are dependent on a proton exchange membrane (PEM). MRFC's main attribute is that it is simpler than the standard fuel cell and will therefore be considerably less expensive to manufacture. In the next few months, Mantra will organize and fund a development process which will take up to two years. Several potential partners have expressed interest.
Mantra has generated a number of prosperous business relationships as of late, and the company looks to further develop those relationships and add to their number throughout the coming year.
Mantra looks to see income growth resulting from sale of licenses for its ERC technology, while the other technologies progress in the development stage. Various demonstration projects and government grants will also contribute to income.
In the coming year, Mantra will also continue to develop the corporate structure of the company. Such efforts will include: creation of optimized business systems and the addition of new Directors resulting from collaborative partnerships and major financings. The management structure will be enhanced.
Mantra will showcase its technology thru the Metro Vancouver 2010 Partnership Investment Program. It will be hosting demonstrations also at the lab.
Larry Kristof, President and CEO of Mantra, comments: "Despite the slow economic recovery, 2009 was a very successful year for Mantra. We made significant progress in the development of our ERC technology, added new management, received government support and built new relationships with corporations on an international scale." He added: "While the company will be focused primarily on the leading ERC technology, Mantra also plans to start an MRFC feasibility study and commence a development project to build an advanced prototype. Further details and updates on both projects will be disclosed as they become available.
Stay up to date with Mantra on Twitter: twitter.com/mantraenergy
About ERC: The Electroreduction of Carbon Dioxide (ERC) is an innovative carbon recycling technology that combines CO2 with water to produce highly sought-after materials such as formic acid, formate salts, oxalic acid and methanol - valuable chemicals used in a variety of industrial applications.
It is the goal of ERC to serve as a safe and more economical alternative to carbon capture sequestration (CCS) - the process of capturing carbon dioxide and storing it in deep geological formations, in the ocean or as mineral carbonates.
About Mantra: Mantra Venture Group Ltd. is a diversified Green Tech company seeking to become a world-leader in the development of commercially viable sustainable technologies. By acquiring the most promising technologies from universities, laboratories and companies and bringing them through to commercialization, Mantra will create significant shareholder value through subsequent acquisitions, spinouts and licensing fees. Current areas of interest for Mantra include: the reduction/recycling of carbon dioxide and alternative energy.
Mantra is a public company quoted on the OTC BB under the symbol MVTG and on the Frankfurt Stock Exchange under the symbol 5MV.
Forward-Looking Statements:
Except for the historical information contained herein, the matters discussed in this press release are forward-looking statements. Actual results may differ materially from those described in forward-looking statements and are subject to risks
Investor Relations
Kol Henrikson
1-877-609-2898
khenrikson@mantraenergy.com
www.mantraenergy.com
SOURCE Mantra Venture Group Ltd.
Sorry, that was old news....... they have had that for a while now.
-Greener
Looks like our boys got a Line of Credit... that seems good:
LOC MVTG Agreement
Well, thanks for sharing, I am too much of a long term holder to know what kind of reaction we are getting from the day trades. My plan is simple, hold , hold'em strong and then hold some more till we see some significant reason to take some profits, emphasis on some. There are no guarantees but, I think this one is sure to please in the near future. They already have 2 major technologies in the queue after ERC starts doing its thing. Also, they will have experience and connections in their corner when they go to develop the next tech. Great time to load up on MVTG
-Greener
I can't help but think that we are due for a big shift in the PPS when you look at how low the volume has been, how low the public float is, and how great the technology is. If the volume heads up it seems to me that we will see some more reasonable PPS..... that should be a nice start to better times for Mantra and shareholders. Also, some of the current LOIs and no doubt the agreements mentioned in news releases for collaboration projects must be close to due...... which means actual funding and could possibly make Mantra's financials look more respectable....that leads to actual completed projects for display and demonstrations...........that in turn will get us more attention from bigger investors. We are all looking forward to the WinterOlympics to see what kind of PR Mantra get. I doubt we get thru Jan and feb without some brilliant news or at least prospects. JMO
-Greener
Yes Indeed,
Also, 3M has a name and reputation that is global, so if you had to choose between joining up with a major industry power in Korea like K.C. Cotrell for instance (Primarily Korea, I'm sure they have a broader scope of activities) and a Global Giant with a household name word-wide with multi- industry dominance plus a colony of scientists and developers at your fingertips............(phew)
....even if it takes a while to get the ball rolling with them, and is a pain in the rear to have to qualify each decision......it is still a tremendous boon to Mantra that I could not imagine being bigger.
Here is the real problem with the way investors now view Mantra IMO.
For example : compare 3M to the former Billy Maize who was a product promoter. People who invest in his company (Pitch Men Inc. or whatever) are going to pay more per share and see more action then if they bought stock in the guy who invented "Magic Putty" for instance. That stock may go nowhere, ever. Right now i think people cannot see Mantra for what it is, just like you can't see who invented the "Magic Putty" or any other of the 1000's of great inventions that Billy Maize sold. It seems like Mantra is a small fish in a big pond, kind of overwhelming to have 3M be their big brother. They seem like one of a million other small businesses 3M works with.
However, Mantra is in the business of developing, promoting and licensing intellectual property...... Huge difference. To me it's more like owning the rights to the Beatles music.... you get a cut whenever someone uses it and you get to sue people who steal it...... in this case globally. So, like an amplifier, 3M helps in developing, promoting, and who knows how the licensing part will work.... heck, maybe 3M will find a way to retro fit it to customers themselves or develop a "plug and play" version so to speak. Or maybe the companies will just store it and wait for a mobile unit to come and zap the CO2 into formate or maybe they will load it and ship it to a central hub ERC recycle center. Maybe combinations of all of these and more will occur, so it is hard to grasp licensing perimeters at this point....one thing for sure, Plenty of ways to help the environment and make loads of dinero. Those with vision can see Mantra as more than a pretty face with a great idea.
In my opinion they are surrounding themselves wisely, with the most influential players, so in the end they can control and profit from the use and promotion of their invention, while not being tied down directly with the day to day problems involved in construction, retro fit, manufacturing etc., while still pulling a profit from these. I also see new companies and jobs springing up with the new industry of Carbon Recycling with Mantra front and center.
Perception of investors needs time to change ..... to me thats the big weight they carry now.
No shortage of opportunity here JMHO
-Greener
We remain stable on low volume.
.18
This float is so low and we are right at the point where the people looking aren't the quality high volume investors we need for this to really get interesting. So many pulling out of the market and into bonds lately that it is no surprise there isn't a lot of action.
Keep on keep'n on
-Greener
47 Boardmarks.... Welcome aboard.
-Greener
Korea is an eventuality however, they don't have the spare land for CCS or the land acreage for Algae. Mantra is the only shoe that fits for their CO2 goals, and the furthest developed option..... So weather its a matter of Mantra licensing it directly or with 3M ......Win Win. Unless they get another option..... unlikely but possible.
-Greener
Very true, and
They mentioned that they already have the demo version ready for the games to do some jaw dropping ERC demonstrations for the spectators. People with deep pocket attend those games.... they are not for reg joe income like me.
-Greener
Notice the issue in price for a THINK brand vehicle is the battery
Buy -a-THINK
And on Mantra's site you see the solution to high price is losing the expensive membrane:
MRFC Overview
Perfect fit !! JMHO
-Greener
Good news for the MRFC (Mixed Reactant Fuel Cell)
Another Mantra technology...... Now that electric cars are becoming popular and more available, its time for the FULL ELECTRIC CAR to be unleashed in good old Indiana USA
Now Mantra needs to enlighten them on the MRFC which would be an easy conversion, and you would have cars on the road using the formate created from ERC.......of course not so easy....it takes time to evolve into something phenominal, but it is a good read in the meantime. JMHO
-Greener
Governor Daniels And Local Leaders Welcome Electric Car Maker To Elkhart
By John Paul (jpaul@wsbt.com)
Tribune Photo/BARBARA ALLISON Indiana Governor Mitch Daniels, left, and Think USA CEO Richard Canney put a "Made In Indiana" sticker on a Think City electric car Tuesday following a press conference in Elkhart Tuesday to announce the manufacturing of the car in Elkhart.
Story Created: Jan 5, 2010 at 3:30 PM EST
Story Updated: Jan 6, 2010 at 10:44 AM EST
ELKHART — The crowd inside the former Phillips Products plant was brought to its feet as electric car manufacturer Think unveiled its model City to public.
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City will be assembled inside the plant once modifications are completed beginning in early 2011.
Governor Mitch Daniels believes the new venture is the future of the automotive industry.
"They are here in the comeback county of Indiana," said Daniels. "They are in an area that has the potential for explosive growth that could redefine transportation in the new century."
"We're determined for Indiana to be the capital of the revolution," Daniels continued.
Elkhart City Council voted unanimously to approve incentives including tax abatements.
The company also received more than $3 million dollars in tax credits and grants.
THINK Chief Executive Officer Richard Canny said his company looked at more two dozen states and counties before selecting Elkhart for its North American production plant.
"We wanted to be somewhere to make a difference," said Canny. "We feel welcomed in Elkhart."
The company already has about 1,500 vehicles on the road in Europe.
Mayor Dick Moore is confident there is real momentum behind THINK and its City vehicle, which were a spin-off from Ford Motor Company.
"It's proven," said Moore. "It's already got thousands and thousand of miles in Europe. It's not a dream or concept or an idea or invention, it's proven."
Canny said there's a market for these vehicles and he believes the company will be competitive among established automakers in the U.S.
"We're the ones out there with the car on the road that you can buy today in Europe, well ahead of others," said Canny. "Other companies have looked at electric vehicles but they're not making them."
Governor Daniels, Congressman Joe Donnelly and Mayor Moore test drove the vehicle outside the plant.
Daniels said the ride was "smooth and accelerated in an instant."
Daniels said the company has the potential to increase the number of green jobs in the state.
"It's a huge positive and huge moment for our state and for Elkhart County," said Daniels. "It's an economic rebirth and you can keep this city or county down for long."
Representative Joe Donnelly said 70 percent of the content will be made locally.
"Elkhart County will be the center of electric vehicle production and technology," said Donnelly.
The Think City has a $30,000 price tag. Canny said he hopes government incentives will lower the price to the $20,000 range.
Hello techlover,
I agree that the PPS is less then stellar, but you have to agree, there is no reward without the risk..... and this company is very slim on the risk side.(JMHO)
2010 is bound to be an awesome year. Just recap all the people Mantra is negotiating with and also the varieties of technology, and the level of the players involved: 3M, Koreans, Swiss, Arabs (Prince Fahd U) Even European countries and more are showing interest .... just in pure Green interest stocks this one rules.
To me being on the ground floor means cheap price when you get in; for a new company in this case.... unfortunately we don't have any control over when it goes up because we don't run the business, we just have the vision to support it. I am sure we will see some positive action in 2010.
have a great night,
-Greener
World Intellectual Property Organization
Read'em and weep: Mantra is King of the intellectual property via WIPO
WIPO # for ERC Link:
www.wipo.int/pctdb/ja/ia.jsp?ia=CA2006%2F001743&IA=CA2006001743&DISPLAY=DESC
(WO/2007/041872) CONTINUOUS CO-CURRENT ELECTROCHEMICAL REDUCTION OF CARBON DIOXIDE
WO 2007041872 20070419
CONTINUOUS CO-CURRENT ELECTRO-CHEMICAL REDUCTION OF CARBON
DIOXIDE RELD OF THE INVENTION
[0001] The invention is in the field of electrochemistry, encompassing processes for the electro-reduction of carbon dioxide in aqueous systems, and apparatus therefor.
BACKGROUND OF THE INVENTION
[0002] The formate salts MHCO2 (where M is typically Na1 K or NH4) and formic acid HCO2H are commercial chemicals that may be produced by industrial thermochemical processes (Kirk-Othmßr • Encyclopedia of Chemical Technology, 1991). For example, sodium formate and subsequently formic acid may be obtained by reaction of sodium hydroxide with carbon monoxide, followed by acidolysis with sulphuric acid.
NaOH + CO -» NaHCO2
2NaHCO2 + H2SO4 ¦> 2HCO2H + Na2SO4
[0003] Formic acid may also be produced as a co-product in the oxidation of hydrocarbons and by the hydrolysis of methyl formate from the carbonylation of methanol. Processes for the synthesis of formate salts (e.g. KHCO2) by the electro- reduction of carbon dioxide are also known (Chaplin and Wragg, 2003; Sanchez et at., 2001; Akahori et al., 2004; Hui and Oloman, 2005).
[0004] Carbon dioxide is considered the main anthropogenic cause of climate change. Methods to sequester CO2 and/or convert it to useful products are therefore needed.
[0005] Oloman and Watkinson in U.S. Pat. Nos. 3,969,201 and 4,118,305 (incorporated herein by reference) describe a trickle bed reactor for ?lectroreduction of oxygen to alkaline peroxide. In various aspects, that electrochemical cell comprises a pair of spaced apart electrodes, at least one of the electrodes being in the form of a fluid permeable conductive mass separated from the counter electrode by a barrier wall. The electrode mass may be in the form of a
bed of particles or a fixed porous matrix. It is composed of an electronically conducting material the surface which is a good electrocatalyst for the reaction to be carried out. Inlets are provided for feeding liquid electrolyte and gas into the electrode mass such that the electrolyte and gas move co-currently through the electrode mass, for example in a direction generally perpendicular to the direction of the current between the electrodes. An outlet is provided for removing solutions containing reaction products from the fluid permeable conductive mass.
SUMMARY OF THE INVENTION
[0006] In various embodiments, the invention provides electro-chemical processes for reduction of carbon dioxide, for example converting carbon dioxide to formate salts or formic acid. In selected embodiments, operation of a continuous reactor with a three dimensional cathode and a two-phase (gas/liquid) catholyt? flow provides advantageous conditions for electro-reduction of carbon dioxide. In these embodiments, the continuous two-phase flow of catholyte solvent and carbon dioxide gas, in selected gas/liquid phase volume ratios, provides dynamic conditions that favour the electro-reduction of CO2 at relatively high effective superficial current densities. In some embodiments, relatively high internal gas hold-up in the cathode chamber {evident in a gas to liquid phase volume ratio > 1 in the feed stream, or > 0.1 within the porous electrode) may provide greater than equilibrium CO2 concentrations in the liquid phase, facilitating relatively high effective superficial current densities. In some embodiments, these characteristics may for example be achieved at catholyte pH > 7 and relatively low CO2 partial pressures (< 10 bar).
[0007] In alternative aspects, the invention involves continuously passing a catholyte mixture through a cathode chamber of an electrochemical reactor. The catholyt? mixture may include carbon dioxide gas and a liquid catholyt? solvent containing dissolved carbon dioxide. The catholyte solvent may for example be an aqueous solvent, it may include a dissolved alkali metal or ammonium bicarbonate, and may be maintained at a desired pH, such as in the range of from about 6 to about 9. A catholyte gas to liquid (G/L) volumetric ratio may be maintained, being the ratio of the volume of carbon dioxide gas to the volume of the liquid catholyte
solvent. The G/L ratio may be maintained in the cathode chamber, for example in the feed stream or in a porous cathode within the chamber. For example, the process may be operated so that the G/L ratio is greater than a threshold value, such as greater than 1 in the feed, or greater than 0.1 within the porous (3D) cathode.
[0008] One aspect of the invention involves passing an electric current between a cathode in the cathode chamber and an anode, to reduce dissolved carbon dioxide to form a desired product. In some embodiments, the process may be operated so that the effective superficial current density at the cathode is greater than a threshold value, such as 1 kA/m2 (or 1.5, 2, 2.5, 3, 3.5, 4, 4.5 or 5 kA/m2). The electric current in the system may for example be a direct current, driven by an electrochemical cell voltage, and in some embodiments the process may be capable of operating at relatively low electrochemical cell voltages, for example less than 10 Volts.
[0009] Various aspects of the invention work in concert to facilitate the adoption, in some embodiments, of process parameters that may improve the economics of processes of the invention. In some embodiments, the processes of the invention may be used with relatively dilute input gas streams, for example the carbon dioxide gas concentration in the feed gas may be from 1 to 100%, or any numeric value within this range (in some embodiments yielding a carbon dioxide partial pressure in the cathode chamber less than a threshold value, such as 3, 5 or 10 Bar). Similarly, relatively low system pressures may be used, for example the cathode chamber may be maintained at a cathode pressure in the range of a minimum value such as 1 , 2, 3, 4 or 5 Bar (1 Bar = 100 kPa(abs)) up to a higher maximum value such as 6, 7, 8, 9 or 10 Bar. In some embodiments, it may be effective to run processes of the invention at elevated temperatures, which may avoid the necessity for cooling, for example at cathode temperatures above a desired threshold such as 20, 25, 30, 35, 40, 45 or 5O0C. In this context, it will be understood that cathode chamber pressures and temperatures may vary along the cathode height. For example, the inlet pressure may be greater than outlet pressure (in some embodiments, the pressure drop may for example range from a
minimum of about 10, 20, 30, 40, or 50 kPa, up to a maximum of about 500, 600, 700, 800 or 900 kPa). Similarly, the outlet temperature may be greater than inlet temperature, with a temperature rise from the inlet to the outlet of from about 1 to 1000C, or any numeric value within this range. It will be understood that the gas composition (particularly CO2 concentration) and the total pressure, fix the CO2 partial pressure, i.e. PpCO2 = (CO2 fraction) x (Total pressure)
[0010] Cathodes for use in the invention may have an effective thickness in the dimension of current flow, such as a porous cathode. These may be referred to as three dimensional (3D) electrodes. Such electrodes may have a selected thickness, such as less than 6, 5, 4, 3, 2, 1 or 0.5mm, and they may have a selected porosity, or range of porosities, such as 5 to 95% or any numeric value within this range, such as 30, 40, 50, 60 or 70%. Cathodes of the invention may be made from a wide variety of selectively electro-active materials, such as tin, lead, pewter, mercury, indium, zinc, cadmium, or other materials such as electronically conductive or non- conductive substrates coated with selectively electro-active materials (e.g. tinned copper, mercury amalgamated copper, tinned graphite or tinned glass).
[0011] The anode may be in an anode chamber, and the anode chamber may be separated from the cathode chamber by an electrochemical cell membrane. The anolyte in the anode chamber may be an aqueous anolyte, and may for example include a dissolved alkali metal hydroxide, a salt (including an ammonium salt) or an acid, and may have a pH range of from about 0 to about 14, or any pH value or range within this range.
[0012] The electrochemical cell membrane may be a cation permeable membrane, for example a membrane that permits selected ions to cross the membrane to balance process stoichiometry.
[0013] The desired products of the process include formate salts, such as ammonium, potassium and sodium formate, or formic acid. The desired product may be separated from the catholyte solvent in a variety of ways. For example, a portion of the catholyte solvent, the recycling catholyte solvent, may be recycled from a cathode chamber outlet to a cathode chamber inlet, and the desired product
may be separated from the recycling catholyte solvent. Similarly, at least a portion of the anolyte may be recycled from an anolyte chamber outlet to an anolyte chamber inlet, and an anode co-product may be separated from the recycling anolyte.
[0014] In selected embodiments, Joule heating of the anolyte may be used to provide heated anolyte, and the heated anolyte may be used to heat the recycling catholyte solvent to separate the desired product from the recycling catholyte solvent, for example by evaporation with fractional crystallization or vacuum distillation. In some embodiments, recycling catholyte, that includes formate, may be reacted with the anolyte, to obtain the desired product by an acidolysis reaction.
BRIEF DESCRIPTION OF THE DRAWINGS
[0015] Figure 1 : is a process flow sheet illustrating aspects of the process of Example 1 , in which A = ammeter, P = pressure gauge, T = thermometer, V = voltmeter, W = wet gas flow meter, PC = pressure control.
[0016] Figure 2: is a schematic illustration of electrochemical cells of the invention, as described in Example 1 , in which the reference numerals denote the following components: 1 and 2: cell bodies; 2, 7 and 9: gaskets; 3: anode feeder, 4: anode spacer; 5: membrane; 6: 3-D cathode (tin-coated copper mesh, tin shot/granules and Pb shot/granules); 8: cathode feeder.
[0017] Figure 3 shows a sectioned elevation view of the single-cell reactor of the invention, Reactor A, as described in more detail in Example 1.
[0018] Figure 4: shows a sectioned elevation view of the single-cell reactor of the invention, Reactor B, as described in more detail in Example 1.
[0019] Figure 5: is a process flow sheet illustrating various aspects of a continuous process for conversion of CO2 to formate salts or formic acid, involving recycling of catholyte and anolyte.
[0020] Figure 6: is a process flowsheet (Flowsheet "A"), illustrating an embodiment of the process for converting CO2 gas to NaHCO2 (sodium formate) and NaHCO3 (sodium bicarbonate) with a byproduct of H2 (hydrogen) and co- product of O2 (oxygen).
[0021 ] Figure 7: is a formalized version of process Flowsheet A, forming the basis for a steady-state material balance stream table for a process of converting approximately 600 tonnes per day of carbon dioxide gas to sodium formate.
[0022] Figure 8: illustrates Process Flowsheet B, for which there is a corresponding material and energy balance stream table in the examples.
[0023] Figure 9: illustrates Process Flowsheet C of the Examples.
DETAILED DESCRIPTION OF THE INVENTION
[0024] In various aspects, the invention provides a continuous reactor for electrored?ction of CO2, which may for example be used in a process that converts a feed of carbon dioxide plus water to formate ion (Reaction 1) and consequently produces formate salts or formic acid.
CO2 + H2O + 2e' -» HCO2" + OH" Reaction 1
[0025] In some embodiments, the invention may utilize an electrochemical reactor analogous to the trickle bed reactor described by Oloman and Watkinson in U.S. Pat. Nos. 3,969,201 and 4,118,305. In such embodiments, the invention may utilize an apparatus for carrying out electrochemical reactions involving gaseous reactants comprising an electrochemical cell having a pair of spaced apart electrodes, at least one of the electrodes, such as the cathode, being in the form of a fluid permeable conductive mass and being separated from the counter electrode by an ionically conductive but electronically insulating layer (such as a membrane or porous diaphragm). The reactor may be operated in a "trickle-bed" mode, with co-current flow of reactant gas and catholyte liquid through a flow-by 3-D cathode. As illustrated in the Examples, the process parameters of the invention may be adjusted so that this reactor achieves advantageous reactant supply (evident for
example as a high gas space velocity, a ratio of the volumetric gas feed flow rate over reactor volume) and mass transfer characteristics. The co-current fluid flow in the cathode may be at any orientation relative to gravity, such as upward or downward.
[0026] In reactors of the invention, an inlet may be provided for feeding a liquid electrolyte and a gas into the fluid permeable conductive mass, and an outlet may be provided for removing solutions containing reaction products from the conductive mass. The inlet and outlet may be arranged so that the electrolyte and gas move co-currently through the conductive mass, for example in a direction generally normal to the flow of electric current between the electrodes. The reactor may for example be provided with a cation membrane separator (as described for example in Hui and Oloman, 2005). In alternative embodiments, other types of reactor may be used.
[0027] Depending on the desired products and overall material balance, the process feed may also include: metal hydroxides and/or metal salts such as MOH, MCI1 M2CO3, M2SO4 and M3PO4 where M is typically an alkali metal (Na, K, etc.) or NH4; acids such as H2SO4, H3PO4, or HCl; or ammonia (NH3).
[0028] Flow sheets in various degrees of detail are provided for alternative processes in Figures 1 , 5, 6, 7, 8 and 9, illustrating the range of embodiments encompassed by the invention. In selected embodiments, the feed CO2 stream to the process may be concentrated, for example to above 80 %vol CO2. Alternatively, a relatively dilute gas stream may be used, such as the product gas from combustion of a fossil fuel (typically containing about 10 %vol CO2). Other potentially reactive components of the feed CO2 stream include oxygen, sulphur oxides, nitrogen oxides and hydrogen sulphide- These may be handled in the process in a variety of ways, for example they may be removed in one or more initial scrubbing steps, so that they are absent or at low concentrations (such as below about 1 %vol) in the feed stream entering the reactor. The total pressure and temperature of the feed CO2 stream may vary over relatively wide ranges, for example from, respectively, about 100 to 1000 kPa(abs), and about 250 to 550 K.
The conversion of CO2 per pass through the electrochemical reactor may be less
than 100%, so that the invention may include provision for recycling the unconverted CO2 gas as welf as recycling the catholyte liquid.
[0029] Process steps 1 to 5 in Figure 5 may be included in some embodiments of the invention, briefly characterized as follows with reference to the annotations on the Figure.
[0030] Step 1. MIX: Continuously mixes the feed water (plus any make-up reagents) with the recycling catholyte, which is then delivered continuously to the reactor cathode chamber.
[0031] Step 2. REACT: [C] Cathode. Continuously drives reaction 1 , along with the side-reaction, Reaction 2, that gives hydrogen by the electro-reduction of water.
2H2O + 2e' -> H2 + 2OH' Reaction 2
[0032] [A] Anode. Continuously drives the complimentary anode reaction(s) whose nature depends on the desired products from the process. For example, if the desired main product is a formate salt and the co-product is oxygen then the anode reaction may be Reaction 3.
2OH' -> 1/2O2 + H2O + 2e' Reaction 3
[0033] If the desired main product is formic acid and the co-product is oxygen or chlorine then the anode reaction may be respectively Reaction 4 or 5. Other anode reactions may include the generation of peroxy-salts of peroxy-acids, such as peroxy-disulphate (2SO4" -> S2O82' + 2e").
2H2O -» O2 + 2H+ + 2e' Reaction 4 2Cr -» Cl2 + 2e' Reaction 5
[0034] The electrode chambers in the reactor may be separated by a membrane that selectively allows the transport of cations from anode to cathode in amounts that balance the desired process stoichiomßtry. If the desired main product is a formate salt then these cations may be alkali metal ions (e.g. Na+, K+ or NH4+) fed to the anolyte as hydroxides, salts or NH3 gas, whereas if the desired main product
is formic acid the transported cations may include protons (H+) generated in Reaction 4 and/or fed to the anolyte as an acid.
[0035] Step 3. SEPARATE: Continuously separates the main product (formate salt or formic acid) and byproduct (hydrogen) from the recycling catholyte.
[0036] Step 4. MIX: Continuously mixes required anode reagents and water with the recycling anolyte.
[0037] Step 5. SEPARATE: Continuously separates the anode co-product(s) from the recycling anolyte.
[0038] In various steps of the process, carbon dioxide and water may be consumed and/or generated in other reactions, such as Reactions 6, 7 and 8 that occur in the reactor or elsewhere in the process.
CO= + OH* -» HCO3' Reaction 6
HCO3' + H+ ^ H2O + CO2 Reaction 7
H+ + OH' -» H2O Reaction 8
[0039] In some embodiments, the process may involve driving the reactor at a relatively high superficial current density (e.g. above 0.5 kA/m2) and current efficiency, for example for formate production (e.g. above 50 %). Processes of the invention may also involve balancing the material and energy requirements of the various process steps to match the required process stoichismetry, while maintaining a low specific energy consumption. For example, processes of the invention have demonstrated 75% current efficiency for formate at 1.3 kA/m2 with a reactor voltage of 3 V at CO2 pressure of 200 kPa(abs) and temperature of 300 K. The management of water may be important to the material balance and require that water be fed to the cathode and/or anode circuits to match its rate of reaction, electro-osmotic transport and evaporation. The consumption of energy in electrochemical reaction, heating, cooling and pumping may be a contributor to the process cost, and may be kept relatively low by appropriate reactor design and by rationalizing the thermal loads in the process. In some embodiments, non-metallic catalysts may be used. For example, U.S. Patent Nos. 5284563 and US 5382332
disclose nickel alkyl cyclam catalysts that may be used for carbon dioxide reduction.
[0040] In some embodiments, a relatively high gas/liquid (G/L) phase feed volumetric flow ratio may be used in the electrochemical reactor (e.g.. G/L flow = 1 to 1000 or 10 to 200), as well as a high gas space velocity (e.g. > 100 h'1). In selected reactors of the invention, increasing G/L from about 5to 100 increases the voltage by less than 10 %. The optimum G/L phase volume (denoted as the "G/L hold-up") ratio depends, in general, on the balance between the effective cathofyte conductivity (usually decreasing with increasing G/L hold-up), the CO2 mass transfer capacity (usually increasing with increasing G/L hold-up) and the intrinsic temperature and pH dependent kinetics of CO2 conversion to the un-reactive bicarbonate/carbonate species in the bulk cathofyte liquid phase.
[0041] In various embodiments, there are two separate gas/liquid (G/L) ratios that may be of importance:
(i) The volumetric G/L ratio in the reactor feed stream(s), with the gas volume flow corrected to STP, this may for example have a range of about 1 to 1000, 1 to 500, 10 to 200, or 10 to 100 or any numeric value within these ranges. For example, gas flow may be 1000 ml/min (corrected to STP), with liquid flow of 20 ml/min to give a G/L [flow] = 1000/20 = 50.
(ii) The volumetric G/L ratio within the porous cathode, i.e. the ratio of gas hold-up to liquid hold-up in the cathode, which may for example have a range = about 0.1 to 10, or about 0.2 to 2, or 0.2 to 4, or any numeric value or range within these ranges. For example, gas hold up may be = 0.6, with liquid hold-up = (1 - 0.6), to give G/L [hold-up] = 0.6 / 0.4 = 1.5. Where, "Hold-up" = fraction of pore space (in 3D cathode) occupied by the specified phase at a given moment. Assumed to be constant in steady-state operation of the reactor. G/L[flow] is not equal to G/L[hold-up] because the gas has a shorter residence time in the cathode than the liquid (i.e. gas "slips" past the liquid). The feed stream and internal hold-up values of (i) and (ii) are of course related, since the value of (ii) depends on the value of (i) together with the cathode characteristics, such as porosity (or vokjage), shape factor, and particle size. Similarly, the value of (i) affects the value of (ii), and
is also related to the CO2 mass transfer capacity in the cathode and the gas space velocity of the reactor.
[0042] The above conditions may be modulated to allow (where CD=current density):
Effective CD > 1.5 kA/m2 at CO2 pressure < 3 Bar.
Effective CD = [superficial CD] x [current efficiency for desired product (e.g. formate)]
Format product concentration > 0.5 M in a single pass. Total reactor voltage at 3 kA/m2 < 5 Volt
[0043] The "superficial current density" is the current passing through the cell divided by the projected surface area of the relevant element, such as the cathode. The "projected surface area" of an element, such as the cathode, is surface area of a projection of the element on a plane parallel to the element. For flat plate elements, the projected surface area is equal to the area of the side of that element facing the other conductive element, for example the projected surface area of the cathode facing the anode. For an element in the form of a planar mesh, the projected surface area is the area within the outline of the mesh as projected onto a continuous planar surface.
[0044] The "current efficiency" (CE) is the ratio, generally expressed as a percentage, of the actual reaction rate to the rate that would be achieved if all of the current passing through the cell were consumed by relevant reaction, such as the reduction of carbon dioxide.
[0045] In some embodiments, the invention may operate at or near adiabatic conditions (T out, up to about 900C). In some embodiments, while reducing the solubility of CO2 in the catholyte, an increasing temperature actually favours the intrinsic kinetics of the electroreduction of carbon dioxide (ERC)1 and good CE can be obtained at higher temperatures by manipulating the factors that promote CO2 mass transfer in a continuous reactor. In some embodiments, the ability to operate at high temperature may be important, because the effects of Joule heating at high
CD under near adiabatic conditions in the continuous reactor may automatically increase the reaction temperature by up to about 800C.
Example 1
[0046] Figure 1 shows a process flow diagram reflecting this example of the electro-reduction of carbon dioxide (ERC). Pure COz or the mixture of CO2 (gas) and N2 (gas) was combined with the catholyte (liquid) at a T junction (mixer), from which the gas and liquid proceeded in slug flow to enter the cathode chamber from the bottom. Thus, the electro-chemical reactor was operated with co-current upward multi-phase (G/L) flow on the cathode side. The anolyte, which was an aqueous KOH solution, also flowed upward through the anode chamber and was recycled to the anolyte storage tank. All gases and liquids passed through individual rotameters. Liquid flow was controlled at the pumps, while gas flows were controlled by manual valves to assure the appropriate gas and liquid loads in the reactor. The reactor inlet and outlet pressures and temperatures were measured by visual gauges at the points indicated in the flowsheet. In runs during which the catholyte product temperatures were controlled, pre-cooling or pre-heating of both anolyte and catholyte was employed to keep the temperature at a desired level. Liquid product was withdrawn from the sampling point and analyzed for formate concentration. Gas product from the gas/liquid separator (a packed bed of graphite felt) was controlled by a 3-way valve either to an Orsat gas analyzer for CO2 and CO analysis, to a wet gas flow meter for flow rate measurement, or to a Tedlar sampling bag for subsequent hydrocarbon analysis with gas chromatograph.
[0047] Galvanostatic electrolysis of CO2 was carried out with a DC power supply connecting across the anode and cathode. A voltmeter was also connected to the unit to measure the reactor voltage. All voltages included anode potential, cathode potential and IR drop. The individual electrode potentials were not measured.
[0048] An automatic pressure control valve was used in the anolyte product line to balance the pressure in the anode chamber against that in the cathode chamber. Such a pressure balance is required to prevent catholyte by-passing the 3-D
cathode and/or the bursting of the membrane that can occur when the cathode pressure exceeds the anode pressure.
[0049] Most runs were conducted with the cathode outlet at the atmospheric pressure. For some runs in Reactor B a manual back pressure control valve and pressure gauge were installed in the catholyte product fine to maintain superatmospheric pressure in the catholyte outlet.
[0050] Processes of the invention were performed first in Reactor A (small reactor) and then in a seven-fold big Reactor B (big reactor) to evidence the effects of scale up. Both reactors have the configuration shown in Figure 2. The reactors consist of a cathode feeder plate and a 3-D cathode, a Nafion cation exchange membrane separator, anode spacer/membrane support, an anode feeder plate and gaskets. The cathode mesh, anode mesh and the anode spacer are sealed on their margins by silicone glue, and then the cell assembly is sandwiched between insulated mild steel plates and uniformly compressed with SS bolts to give a balanced fluid distribution.
[0051] Figure 3 shows a sectioned elevation view of the single-cell Reactor A. The "flow-by" cathode of this reactor had dimensions of 30 mm width and 150 mm height (geometric surface). The thickness of the cathode depended on which 3-D cathode material was used. For tin-coated copper mesh cathode, single or multiple layers of mesh were placed between the membrane and cathode feeder so the thickness of the cathode was the total thickness of these all layers, which ranged from 0.38 to 1.83 mm; for graphite felts and metal granules or shot, the cathode materials were embedded in two layers of Neoprene gasket with the back of the cathode in contact with the cathode feeder, therefore the thickness of the cathode was that of the gasket, i.e. 3.2 mm. The geometric (a.k.a. superficial) cathode area perpendicular to the electric current was 30 mm by 150 mm - 4.5X10"3 m2. In Reactor A the applied current ranged from 1 to 14 A with corresponding superficial current density from 0.22 to 3.11 kA rrf2.
[0052] In Reactor B, tin-coated copper mesh cathodes or tin granule cathodes were used. Figure 4 presents the dimensioned front view and corresponding dimensions of Reactor B with a tin granule fixed-bed cathode. To minimize the bypass of the catholyte at the edges of the cathode bed, the gasket was purposely made with five triangles on each side to direct the flow toward the centre of the cathode. Subtracting the areas taken by those triangles, the superficial cathode area was 3.22x10'2 m2, which was about seven times that of Reactor A (4.5X10"3 m2). The applied current in Reactor B ranged from 20 to 101 A with corresponding superficial current density 0.62 to 3.20 kA m'2.
[0053] Reactor B was assembled with a tin granule fixed-bed cathode, according to the following procedures: (1) A sanded tin plate (99.99 wt% Sn, 3mm thick) cathode feeder was put onto the neoprene gasket; (2) The pretreated tin granules were spread uniformly into a Durabla gasket (3.2 mm thick) on the tin plate, and layers of Netion screen were inserted into the entrance and exit regions of the catholyte flow to distribute the fluid and support the membrane; (3) The wet Nafion 117 membrane was put on top of the tin granule bed, and then, the PVC screen spacer, anode SS mesh, and anode feeder (SS plate) were placed on top of one another in that sequence; (4) Lastly, a cell body was put into place, and 243/8 inch bolts were employed to compress the sandwiched cell uniformly.
[0054] A variety of cathode materials are available for use in alternative aspects of the invention. Carbon dioxide can be electro-chemically reduced on almost all groups of metals in the periodic table to give a variety of products with different levels of selectivity. The following cathode materials, among others, may be adapted to particular embodiments: Nano-stuctured Cu deposited on graphite felt; Cu/Sn alloy deposited on graphite felt; nano-structured Sn on Sn mesh, Sn coated plastic mash, Cu mesh; Sn deposited graphite felt; Sn coated copper mesh; Pb plate, shot, granules, grid and Pb-C reticulate; Sn shot and granules. The last five of the foregoing materials were used in alternative embodiements for the present Example. In some embodiments, a high (specific) surface area micro or nano- structured deposit on a 3D substrate is desirable. Other potential cathodes are.
nano-structured Cu on Cu mesh, nano-structured Sn on Sn mesh, or Sn coated plastic mesh, alternatively with Pb, In or Hg as the electro-active surface.
[0055] Reactor A, using granulated tin cathodes (99.9 wt% Sn) and a feed gas of 100% CO2 showed slightly better performance than that of the tinned-copper mesh cathodes. The seven fold scaled-up Reactor B used a feed gas of 100% CO2 with the aqueous catholyte and anolyte respectively [0.5 M KHCO3 + 2 M KC1] and 2 M KOH1 at inlet pressure from 350 to 600 kPa(abs) and outlet temperature 295 to 325 K. For a superficial current density of 0.6 to 3.1 kA m"2 Reactor B achieved corresponding formate current efficiencies of 91 to 63%, with the same range of reactor voltage as that in Reactor A (2.7 to 4.3 V). Up to 1 M formate was obtained in the catholyte product from a single pass in Reactor B.
Example 2 [recovery of cathode activity].
[0056] An electrochemical reactor as described in Example 1 was constructed and operated as follows:
• Anode feeder = 316 stainless steel plate
• Anode = 304 stainless steel number 10 mesh (10 mesh/inch) • Anode spacer = PVC "fly screen" 10 mesh.
• Separator = Nafion 117 cation membrane.
• Cathode = ca. 50 mesh tin granules. 150 mm high by 32 mm wide by 3 mm thick
• Cathode superficial area = 45E-4 m2 • Cathode feeder = tin foil supported on a copper plate
Operating conditions:
• current = 6 A (i.e. 1.3 kA/m2),
• catholyte = 0.45 M KHCO3 + 2 M KCI, anolyte = 1 M KOH, anolyte flow = 40 ml/min
• CO2 gas flow = 364 ml (STP)/min, catholyte flow = 20 ml/min,
• temperature = 300 K, pressure = 140-170 kPa(abs).
[0057] With a cathode of fresh tin granules the formate current efficiency (CE) dropped from about 60 % at 30 minutes to 50 % at 250 minutes operating time. Recovery of the current efficiency was achieved by:
[0058] (i). Chemical treatment and recycle of the cathode: The used cathode tin granules were treated in 11 wt % nitric acid at room temperature for 2 minutes, washed in deionized water and re-used in the reactor. Table 1 shows that this treatment regained the cathode activity at 30 minutes operating time.
Table 1.
[0059] Similar results for cathode recovery were obtained by treating the used tin granules with hydrochloric acid and/or potassium hydroxide.
[0060] (ii). Polarity reversal: Under similar conditions to those above, with fresh tin granules the formate current efficiency dropped from 65 % at 30 minutes to 48 % at 360 minutes operating time. Polarity reversal was applied to the reactor for 5 minutes at 1 A. The formate current efficiency subsequently increased and was back to 65 % at 400 minutes operating time.
Example 3 [scaJe-up].
[0061] An electrochemical reactor as described in Example 1 was constructed and operated as follows:
• Anode feeder = 316 stainless steel plate
• Anode = 304 stainless steel, number 10 mesh (10 mesh/inch)
• Anode spacer = PVC "fly screen", 10 mesh.
• Separator = Nation 117 cation membrane.
• Cathode = ca. 50 mesh tin granules. 680 mm high by 50 mm wide by 3 mm thick
Cathode superficial area = 340E-4 m2 Cathode feeder = 2 mm thick tin plate.
Operating conditions: • catholyte = 0.45 M KHCO3 + 2 M KCI1 anolyte = 2 M KOH, anolyte flow = 60 ml/min
• CO2 gas flow = 1600-2200 ml (STP)/min, catholyte flow = 20 ml/min,
• temperature in-out = 300-314 K1 pressure in-o?t = 600-100 kPa(abs).
[0062] Table 2 shows the performance of this reactor.
Table 2. Reactor erformance.
Example 4 [acid anolyte]
[0063] A reactor was constructed as in Example 1 , operation was as in Example 2, except the anolyte was replaced by an acid sodium sulphate solution as follows:
Operating conditions: • catholyte = 0.45 M KHCO3 + 2 M KCI,
• anolyte = 0.5 to 2 M Na2SO4 + 0.5 to 4 M H2SO4, anolyte flow = 40 ml/min
• CO2 gas flow = 500 ml (STP)/min, catholyte flow = 20 ml/min,
• temperature = 300 K, pressure s 140-170 kPa(abs).
[0064] The reactor was operated over a current range from 1 to 14 A (0.2 to 3.1 kA/m2) with corresponding formate CE from 80 to 30 % and reactor voltage from 3.5 to 8.0 V.
[0065] This result shows that the process can be operated with an acid anolyte. The various ratios of NaVH+ in the anolyte gave different formate current
efficiencies, thus indicating that the formate CE could be improved by manipulating the anolyte composition.
(Example 5 [ammonium cations].
[0066] In some embodiments, the invention may utilize ammonium cations, to produce ammonium formate. A reactor was constructed as in Example 1 , operation was as in Example 4, except the catholyte potassium cations were replaced by ammonium and the anolyte was replaced by an acid ammonium sulphate solution, as follows:
Operating conditions:
• current = 4 A (i.e. 0.89 kA/m2)
• catholyte = 0.45 M NH4HCO3 + 2 M NH4CI,
• anolyte = 0.93 M (NH4)2SO4 + 0.75 4 M H2SO4, anolyte flow = 40 ml/min
• CO2 gas flow = 500 ml (STP)/mip, catholyte flow = 20 ml/min,
• temperature = 300 K, pressure = 140-170 kPa(abs).
[0067] The reactor was operated over 2 hours with formate CE ranging from 35 to 70 % and reactor voltage from 4.6 to 5.2 V.
[0068] This result demonstrates that the process can use exclusively ammonium cations in the catholyte. The ability to use ammonium cations is illustrated in Process Flowsheets B and C, for the production of formic acid/or ammonium formate.
Example 6 [Lead cathode].
[0069] An electrochemical reactor as described in Example 1 was constructed and operated as follows:
• Anode feeder = 316 stainless steel plate
• Anode = 304 stainless steel number 10 mesh (10 mesh/inch)
• Anode spacer = PVC "fly screen" 10 mesh.
• Separator = Nation 117 cation membrane.
• Cathode = 0.5 mm diameter lead shot. 150 mm high by 32 mm wide by 3 mm thick.
• Cathode superficial area = 45E-4 m2
• Cathode feeder - lead plate.
Operating conditions:
• current = 6 A (i.e. 1.3 kA/m2),
• catholyte = 0.45 M KHCO3 + 2 M KCI, anolyte = 1 M KOH1 anolyte flow = 40 ml/mi n • CO2 gas flow = 364 ml (STP)/min, catholyte flow = 20 ml/min,
• temperature = 300 K1 pressure = 140-180 kPa(abs).
[0070] Operation of this reactor over a period from 2 to 6 hours showed a constant formate current efficiency of 31 +/- 1 %.
Example 7 [Process Flowsheet A]
[0071] The process of this Example is illustrated in Figure 6, showing electro- synthesis of sodium formate from carbon dioxide, water and sodium hydroxide.
[0072] Based on the concept of Figure 5 this process (Figure 6) converts CO2 to
NaHCO2 (sodium formate) and NaHCO3 (sodium bicarbonate) with a byproduct of H2 (hydrogen) and co-product of O2 (oxygen). The feed plus recycle CO2 is compressed to about 300 kPa(abs) and delivered to the cathode of the electrochemical reactor along with the recycling catholyte, an aqueous solution of NaHCO2 and NaHCO3. The cathode outlet goes to a gas/liquid separator from which the liquid is divided into a direct recycle and a stream from which NaHCO2 and NaHCO3 are separated by evaporation and fractional crystallization to give the main cathode products (NaHCO2 and NaHCO3). The cathode outlet gas goes to a gas separation system (e.g. pressure swing adsorption) that recovers H2 and delivers th? unconverted CO2 to recycle. The anode side of this process involves a feed of NaOH (sodium hydroxide) whose sodium content (Na+) is transported across the cation membrane while the hydroxide is converted to oxygen that is recovered as the co-product from a gas/liquid separator. The recycle streams in
this process include the necessary compressors and pumps along with heat exchangers (e.g. C1 , C2, C3) to control the reactor temperature in the range of about 300 to 350 K.
[0073] Figure 7 illustrates Process Flowsheet A, and the steady-state material balance stream table is set out below, based on 600 tonne/day CO2. Formate current efficiency = 77 %. CO2 conversion/pass = 72%.
Example 8 [Process Flowsheet B]
[0074] Figure 8 illustrates the electrosynthesis of formic acid from carbon dioxide and water. The exemplified process converts CO2 to HCO2H (formic acid) with a byproduct of H2 (hydrogen) and co-product of O2 (oxygen). The feed plus recycle CO2 is compressed to about 300 kPa(abs) and delivered to the cathode of the electrochemical reactor (U 1) along with the recycling catholytß, an aqueous
solution of NH4HCO2 and NH4HCO3 plus (if required) a supporting electrolyte such as NH4CI or (NH4J2SO4. The cathode outlet stream goes to a gas/liquid separator (U3) from which the liquid is divided (U5) into a direct recycle and a stream that is passed to a thermochemical acidolysis reactor/separator (U6.U7) where formic acid is obtained by reaction 9 with sulphuric acid (generated in the anolyte) and distilled under partial vacuum to give an overhead product of aqueous formic acid and a bottoms solution of (NH4J2SO4 that is recycled to the anode via the mixer U8. The gas stream from U3 passes to a separator (U4) where H2 is recovered and CO2 is recycled to the reactor feed via mixer U2, along with CO2 generated by the side- reaction 7 in the acidolyis reactor.
[0075] An aqueous solution of (NH4J2SO4 and H2SO4 recycles through the anode circuit, supplying NH4+ and H+ cations for transport to the catholyte via the cation membrane. The co-product O2 gas is generated with protons (H+) at the anode by reaction 4 and recovered from a gas/lquid separator (U9). The recycling acid anolyte is then divided (U10) to supply H2SO4 for the acidolysis reaction (U6) from which the spent reactant is re-combined with the anolyte (U8).
2NaHCO2 + H2SO4 ¦» 2HCO2H + Na2SO4 Reaction 9
[0076] A material and energy (M&E) balance for Flowsheet B operating at steady-state is shown in the stream table below. This M&E balance is based on the assumption of a formate current efficiency of 80% and 80% conversion of CO2 per pass through the electrochemical reactor.
[0077] The primary and secondary net reactions in Flowsheet B are respectively reactions 10 and 11.
CO2 + H2O -» HCO2H + tt O2 Reaction 10 H2O -» H2+ Vz O2 Reaction 11
[0078] The conditions of this process may be chosen to promote the main net reaction 10. The characteristics of the process of this example, to promote reaction 10 may be selected as follows:
i. Appropriate electrode materials, current density, fluid compositions, fluid loads, pressure and temperature in the electrochemical reactor, ii. Maintaining the anolyte composition with respect to acid and salt to provide cation transport across the membrane in the correct ratio (e.g. HTNH4+) that balances the rates of cathode reactions 1 and 2 and holds the catholyt? pH in the desired range. iii. A bulk catholyte pH in the range about 4 to 10, preferably 6 to 8. iv. Maintaining the anolyte composition and flow to provide protons for the acidotysis reaction that produces HCO2H in U6 and allow recovery of the aqueous formic acid by vaporization in U7. v. A concentration of acid (e.g. HzSO4) in the anolyte of greater than about
1 M. vi. Maintaining the formate concentration of the catholyte sufficiently high to allow formation and separation of HCO2H in U6. vii. A concentration of formate (HCO2') in the recycle catholyte of greater than about 1 M, preferably about 5 M. viii. Feeding water to the cathode and/or anode circuits at the appropriate rat?(s) to maintain the water balance and the electrolyte concentrations that facilitate both the electrochemical and thermochemical processes in U1,U6 and U7. ix. Maintaining the flow and temperature of the recycle anolyte sufficiently high to utilize the Joule heating of the electrochemical reactor for evaporation of formic acid in U6. x. A recycle anolyte temperature of greater than about 320 K, with an anolyte flow determined by the energy balance to reduce the need for heating utilities in the process.
[0079] Operation of the process will typically depend on interactions among the conditions i to x listed above. Modeling of this embodiment provided a steady-state material and energy balance, on the basis of 105 tonne/day CO2, giving a current efficiency of 80% and CO2 conversion/pass of 80%. The material and energy balance stream table corresponding to Process flowsheet B is set out below, with the Table continued across the three sub-tables.
Example 9 [Process Flowsheet C]
[0080] Figure 9 illustrates electro-synthesis of ammonium formate from carbon dioxide, ammonia and water. This process converts CO2 and NH3 to NH4HCO2 (ammonium formate) with a byproduct of H2 (hydrogen) and co-product of O2 (oxygen).
[0081] The feed plus recycle CO2 is compressed and delivered to the cathode of the electrochemical reactor along with the recycling catholyte, an aqueous solution of NH4HCO2 (e.g. > 1 M) with minor amounts of NH4HCO2 (ammonium bicarbonate - e.g. 0.1 M). The cathode outlet stream goes to separation system that recovers a solution of NH4HCO2 plus the byproduct hydrogen and recycles the spent catholyte.
[0082] Ammonia (NH3 gas or aqueous solution) is fed to the anolyte circuit where it combines to form (NH4)SSO4 (ammonium sulphate). An aqueous solution of (NH4J2SO4 and H2SO4 then recycles through the anode circuit, supplying NH4+ and H+ cations for transport to the catholyte via the cation membrane. The co- product O2 gas is generated with protons (H+) at the anode by reaction 4 and recovered from a gas/liquid separator. The ratio [NH4+] / [H+] is maintained in the
anolyte to supply these species to the catholyte at rates that balance the stoichiometry of reactions 1 and 2 and produce a catholyte solution of predominantly ammonium formate at pH in the range about 4 to 8.
[0083] The primary and secondary net reactions in flowsheet C are respectively reactions 12 and 13.
CO2 + H2O + NH3 ¦» NH4HCO2 + 1/£ O2 Reaction 12
H2O -» H2+ % O2 Reaction 13
[0084] Variations of this scheme may include for example replacement of
(NH-O2SO4 and H2SO4 in the anolyte by (NH4)3PO4 and H3PO4Or by NH4CI and HCI. In the later case the anode co-product may be Cl2 by reaction 5. Anode co-products may also include peroxy-compoupds such as ammonium persulphate (NH4J2S2O8 or persulphuric acid H2S2Os, etc. by reaction 14.
2SO4" -> S2O8" + 2e" Reaction 14
References
[0085] Kirk-Othmer • Encyclopedia of Chemical Technology. John Wiley, New
York, 1991.
[0086] R. Chaplin and A.Wragg. "Effects of process conditions and electrode material on reaction pathways tor carbon dioxide electrored?ction with particular reference to formate formation". J.Appl.Electrochem. 33:1107-1123 (2003).
[0087] C.M.Sanchez et al. "Electrochemical approaches to alleviation of the problem of carbon dioxide accumulation". Pure AppJ.Chem. 73(12), 1917-1927, 2001.
[0088] Y.Akahori et al. "New electrochemical process for CO2 reduction to formic acid from combustion flue gases" .Denki Kagaku (Electrochemistry) 72(4) 266-270 (2004).
[0089] Li Hui and C.OIoman. "The electro-reduction of carbon dioxide in a continuous reactor". J.Appl. Electrochem. 35, 955-965, (2005).
[0090] K.Hara and T.Sakata. ?lßctrocatlytic formation of CH4 from COz on a Pt gas diffusion electrode". J.EIectrochßm. Soc. 144(2),539-545 (1997)..
[0091] M.N. Mahmood, D.Masheder and C.J.Harty. "Use of gas-diffusion electrodes for high rate electrochemical reduction of carbon dioxide". J. Appl. Electrochem. 17:1159-1170 (1987).
[0092] K.S. Udupa, G.S. Subramamian and H.V.K. Ud?pa. Electrochim Acta 16, 1593, 1976.
[0093] Although various embodiments of the invention are disclosed herein, many adaptations and modifications may be made within the scope of the invention in accordance with the common general knowledge of those skilled in this art. Such modifications include the substitution of known equivalents for any aspect of the invention in order to achieve the same result in substantially the same way. Numeric ranges are inclusive of the numbers defining the range. The word "comprising" is used herein as an open-ended term, substantially equivalent to the phrase "including, but not limited to", and the word "comprises" has a corresponding meaning. As used herein, the singular forms "a", "an" and "the" include plural referents unless the context clearly dictates otherwise. Thus, for example, reference to "a thing" includes more than one such thing. Citation of references herein is not an admission that such references are prior art to the present invention. Any priority document(s) and all publications, including but not limited to patents and patent applications, cited in this specification are incorporated herein by reference as if each individual publication were specifically and individually indicated to be incorporated by reference herein and as though fully set forth herein. The invention includes all embodiments and variations substantially as hereinbefore described and with reference to the examples and drawings.
See the New 3M Pocket Projector at CES 2010
Laptop? Check. MP3 Player? Check. Portable speakers? Check. Pocket projector? Check. The amount of gear business travelers haul around is enough to weigh anyone down. Today, however, that load will get a little lighter with the introduction of the 3M MPro150, the ultimate personal electronics device for the business professional. The latest tool in 3M’s award-winning MPro family of pico projectors, the MPro150 boasts one of the most robust feature sets of any pocket projector currently on the market, combining several applications into one compact, efficient device optimized for the on-the-go businessperson. No more sifting through a small electronics store when checking in for flights, or needing to bring multiple totes to presentations. Visit 3M at the Consumer Electronics Show 2010, booth 20723, South Hall, Level 1 at the Las Vegas Convention Center. Designed with professionals in mind, the MPro150 includes 1 GB internal memory, a micro SD card slot and a USB input for transferring files from a laptop or netbook, eliminating the necessity of a pass-through device and allowing entire presentations to be pre-loaded onto the projector itself. The MPro150 supports Microsoft® Office applications (Word, Power Point® and Excel®), as well as Adobe® PDF, photos and video, allowing the user to project images up to 50-inches at 15 lumens brightness in either the boardroom or break room
En route to that important presentation, business professionals can relax with their favorite tunes, courtesy the MPro150’s integrated MP3 player and headphone jack. And, when it’s time to share with colleagues, a pair of integrated stereo speakers turn the MPro150 into a theater-on-the-go
Additional features include an integrated flip stand, tripod and a variety of input cables, which make the MPro150 ready to use “out-of-the-box” with a wide range of today’s most popular video output gadgets. Available optional accessories include an adapter cable for Apple® products, component video cable and car charger
“The 3M MPro150 puts an entire suite of presentation tools into the business professional’s pocket,” said Mark Colin, vice president, 3M Mobile Interactive Solutions Division. “With no need to pack a separate laptop or projector, business professionals can travel a bit lighter. It’s great for use at home and on-the-go, as well.” The lightweight MPro150 is just over 5 inches long and weighs a mere 5.6 ounces. It is now available for pre-order from shop3M.com and amazon.com, at an estimated price of $395. Orders will begin shipping in early February. For those who are looking for a casual consumer electronics accessory for watching movies, sharing photos or projecting video games up to 50 inches,3M also offers the MPro120 projector, which has an estimated price of $325. Optional accessories for both the MPro150 and MPro120 are sold separately
About 3M A recognized leader in research and development, 3M produces thousands of innovative products for dozens of diverse markets. 3M’s core strength is applying its more than 40 distinct technology platforms – often in combination – to a wide array of customer needs. With $25 billion in sales, 3M employs 75,000 people worldwide and has operations in more than 60 countries. For more information, visit www.3M.com
3M is a trademark of 3M
Microsoft Office is a registered trademark of the Microsoft Company in the United States
Other trademarks are property of their respective owners
Photos/Multimedia Gallery Available: http://www.businesswire.com/cgi-bin/mmg.cgi?eid=6133169<=en
Bid :15 Ask: 18
Holding firm. Whoever gave their position up yesterday (14.5) sold way below any reasonable price. Try buying these shares at 14.5 IMPOSSIBLE
Hopefully stronger hands grab up these shares..... the float is too low for this kind of stuff to continue. JMHO
-Greener
MVTG Investor Highlights Include:
[url]www.newswiretoday.com/news/55732/[tag][/tag]
[/url][tag]Article from PR Newswire Today [/tag]
Has diversified technologies within Green Environment currently Carbon Diuoxide reduction (ERC) and water treatment/purification.
MVTG's technologies are applicable to multiple industries: steel plants (steel pickling), coal plants, mining, fuel cell development, carbon credits and more.
Mantras Electroreduction of Carbon Dioxide technology combines captured CO2 with water to produce high value materials, including: formic acid, formate salts, oxalic acid, and methanol.
In addition, companies adopting ERC stand to make significant profit from its by-products. Formic acid, for example, currently sells for approx. $1,200/ton.
Mantra signed an exclusive Option Agreement to acquire the license of the Biometals Recovery System (BRS)- a revolutionary mine wastewater technology, on February 27th, 2009
Intellectual property worldwide with patents pending.
Mantra successfully completed a prototype capable of processing 1 Kg of CO2 per day in Oct. 2008, and its first commercial scale reactor is schedule for launch in early 2010.
Announced that it has observed an increase in current efficiency in its Electroreduction of Carbon Dioxide (ERC) technology through the use of a new proprietary electrode catalyst structure.
This is just the first of a series of improvements expected by Mantra as they progress through a series of development trials.
Announced it is evaluating partnership opportunities with U.S.-based industry plants to facilitate the pilot scale demonstration project in the U.S. DOE Research Program.
Announced the appointment of Mr. Shawn Kim as the Vice President of International Business Development. Mr. Kim has nine years experience in the financial industry where he started as a business analyst. After dedicating 3 years to Mackenzie Financial Corporation in Toronto, he moved to AIG in Korea where he successfully implemented a worldwide marketing model and secured new business alliances.
Features available at SmallCapReview.com include in-depth profiles of select Small-Cap/Penny Stocks as well as the most comprehensive and up to date news available on the small-cap market.
No investor should assume that reliance on the views, opinions or recommendations contained herein will produce profitable results. Nothing within our site should be construed as an offer or solicitation to buy or sell products or securities. The companies we profile may lack an active trading market for their securities, investing in such securities is highly speculative and carries a high degree of risk. SmallCapReview.com has not been compensated for its services with regards to Mantra Venture Group.
Paul Waide Instructional .PDF on Carbon waste management
Power Point .PDF on CO2 Management
This is an interesting link to and educational Power point (same as above)
http://www.google.com/url?sa=X&q=http://interenerstat.org/work/2008/asean_training/Waide.pdf&ct=ga&cd=cxYyzG-Ribk&usg=AFQjCNG1HuUvy83_AzNgTfPd0M2ZsWiS9w
Seems to link good management of CO2 with using coal for fuel....... There is no cost effective way to clean up coal CO2 except ERC. 100% vital that Mantra gets to move ahead quickly. I am thinking that a wave, or better yet tsunami, of interest is coming and Mantra will need to be ready to ride on that wave. I would not be surprised if some dead end loser companies get picked up as well, but I am confident in Mantra's ability to surf this one out. JMHO
-Greener
Why Cap-and-Trade Ain’t Dead Yet
Where To Store All That Captured CO2
The world's first carbon border tax is on the way—and, surprisingly, it doesn't involve imports from China:
THE VINE
Carbon Tariffs Show Up In Unlikely Places
Bradford PlumerJanuary 4, 2010 | 4:19 pm
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[url]www.breathinglowerbloodpressure.info/news/Carbon-dioxide.html
[/url][tag]Link to this Article[/tag]
To encourage the switch to clean renewable energy, Minnesota plans to add a carbon fee of between $4 and $34 per ton of carbon dioxide emissions to the cost of coal-fired electricity, to begin in 2012, to discourage the use of coal power, the greatest source of greenhouse gas emissions. ...
Most of North Dakota’s electricity exports is generated by coal-fired power plants. North Dakota officials argue that the move would place an unfair tax on electricity exports from the state and discourage its use by Minnesota utilities.
And that means… the world's very first green trade war. Officials in North Dakota have vowed to fight the move in court, arguing that the fee would "discourage coal-powered electricity sales in favor of renewably powered electricity." That's true, but it's not clear this is unfair to North Dakota, which, after all, has more wind resources than any state in the country.
MORE ARTICLES ON: China, Minnesota, North Dakota
ERC vs. CCS
(Not very well put together commentary... but the thoughts are solid...- Greener)
ERC vs CCS Commentary
12/30/2009 1:03:49 AM | | 23 reads | Post #27770186
I must admit –it´s from these “Bullzano” paper,but it´s a better read, than I´ve originally thought. In my, nonexpert, view in these area, this company looks really exciting(but very speculative, too), becausethey´ve got –from what I can see- an approach, which should be at theforefront at all types of CO2conversion/processing/sequestration/storage etc.(&these market inpriciple is gigantic). CCS should be any, any years away from becomeeconomical feasible(beside big environmental skepticism/concerns&any more) &McKinsey speak about, that “adding CCS to the nextgeneration of European power plants could increase their capital costby up to US$1.3 billion each.” Further, they stated: “Their thoroughanalysis suggests that the typical cost of a demonstration project islikely to be in the range of US$80-$120 per tonne of CO2 sequestered.”.Arguably that´s the reason, why “only one full-scale CCS project thatcaptures and sequesters carbon dioxide from a coal-fired power plantexists today, and it is mired in legal challenges.”. But especially,adverse other approaches, they can create a value added process, withwhich they maybe can announce(?) even make money with, instead of burna lot, lot through it. But, how nearly ever, the devil plunge in thedetail &they must develop it further now. It´s for me mainly“virgin soil”, but if i should find some interesting aspects, I´ll addthem from time to time -some advantages of ERC:
“Advantages of ERC technology: MVTG management asserts the following potential advantages relative to alternative methods of CO2 capture and conversion:
+ Process is driven by electric energy that can be taken from anelectric power grid supplied by hydro, wind, solar, tidal or nuclearenergy (all renewable).
+ Medium reaction rate allows for commercial viable CO2 processing times
+ Medium CO2 space velocity gives the ability to treat comparatively large volumes of CO2.
+ High product selectivity for formate and formic acid (up to 90%)
+ Low operating temperature (20° to 80° Celsius) and pressure (below 1 MPa or magnitude of pressure)
+ Hydrogen is not required as a feed reactant, but is present in water used in the process
+ ERC products are useful, and financially profitable sources of income
+ ERC pilot projects can be executed on any scale, whereassequestration(CCS) can only be performed on a very large scale, leadingto exorbitant research and development expenditures ”
CO2 Christmas Tree
( I suggest you get the full report which quotes from Mantra's CleanTech Brief)
Go to :
WV Coal .pdf
Posted by: char in Untagged on Dec 25, 2009
Significant Property Improvement of Plastic Made From Carbon Dioxide, Materials, AIST - NanoTechWire.com - The online resourc.
The several of us here have been at work on this Christmas present for some time now, ever since our exchange of love notes with the contingent from Texas, who would rather all of us in Coal Country bowed down and accepted the fact that Coal isn't King, that he has even higher powers he must be compelled to serve.
We Three Stooges of Christmas say nuts to that, and attempt herein to bring you, everyone in Coal Country, some useful gifts.
Just as the Nobel Committee affirmed, by awarding their Prize in Chemistry to Paul Sabatier, the better part of a century ago, Carbon Dioxide, as arises in a small way from our use of coal, relative to natural sources of CO2, such as volcanism and seasonal vegetative rot, can be reclaimed and recycled into materials of utility and value.
In the multiple ornaments, the several following links and excerpts, hung from this Christmas Day dispatch, we affirm Carbon Dioxide to be a by-product of significant potential worth.
First up, via the report linked above, Japanese researchers inform us that valuable plastic can, indeed, be made with CO2.
As, follows:
"Significant Property Improvement of Plastic Made From Carbon Dioxide
Points
Development of high-performance material by using a composite of plastic made from carbon dioxide
Potential alternative to fossil resource derived plastics such as polyethylene and polypropylene
Expected to contribute to global warming prevention as a technology for fixing and utilizing carbon dioxide massively emitted in and outside Japan
Summary
Hiroshi Shimizu and Li Yongjin (Research Scientist), the Nanostructured Materials Group, the Nanotechnology Research Institute, et. al., succeeded in greatly improving the mechanical properties, including elastic modulus and strength, of plastic (aliphatic polycarbonate) made from carbon dioxide. Plastic with excellent mechanical properties ... has been developed by using a composite of poly(propylene carbonate) (PPC), a kind of aliphatic polycarbonate made from CO2 and propylene oxide, and other plastics. The PPC composite is a high-performance material demonstrating not only improved mechanical properties but also increased heat resistance, and it is expected to be a viable alternative to petroleum-based general-purpose plastics, such as polyethylene, polypropylene, and polystyrene."
Note: "polycarbonate made from CO2 ... is expected to be a viable alternative to petroleum-based general-purpose plastics".
"In PPC made from CO2, fixed CO2 accounts for 43% by weight. Although the ratio of fixed CO2 decreases to about 30% by weight by blending with other plastics to enhance its performance, this PPC composite has an advantage over general-purpose plastics in terms of reduced CO2 emission. In Japan, the amount of CO2 emitted from power plants and ironworks has reached a level of 500 million tons per year, calling for the urgent establishment of technologies for separation and fixation of CO2. Wide use of the newly developed PPC (CO2- based) composite as an alternative to general-purpose plastics is expected to contribute to global warming prevention and lead to reduced dependence on petroleum resources.
Social Background for Research
A synthetic scheme in which plastics are produced from CO2, which was discovered 40 years ago by Prof. Shohei Inoue (currently Professor of Tokyo University of Science), is receiving renewed attention as a technology for fixing and utilizing CO2, which is one of the measures to prevent global warming. While technological development of aliphatic polycarbonate has been at the basic research level in Japan, pilot plants for PPC production were built by the national budget and commercial mass production of PPC has already started in China. However, the mechanical properties of the produced PPC is still far from practical use and its appearance is similar to soft, sticky rubber rather than plastic, and, therefore, extensive improvement is required.
This time, we searched for effective ways to improve the mechanical properties of PPC. Taking into consideration the basic concept of improved material, we aimed at keeping the ratio of CO2 in the PPC composite at about 30 wt%. We hoped to greatly improve the mechanical properties by adding aliphatic polyesters as second and third ingredients, thus controlling the microstructure of the PPC composite."
-------
After an exposition of technical details, the authors conclude with:
"Future Schedule
We continue to pursue further improvement of the properties of PPC composite and also plan to apply the PPC composite to not only general structural materials but also film and packaging materials by making the most of its transparency and gas-barrier property, and to evaluate its performance as a practical material."
So, by productively recycling CO2, we can obtain "a practical material."
In addition to polycarbonate plastic, Japan has discovered that CO2 can also be used in the synthesis of polyurethane, a very versatile material employed in foams, coatings and myriad other applications, as revealed in:
Science Links Japan | Direct Synthesis of Urethane from Carbon Dioxide via Halogen-Free Process.
The following was cut and pasted from the Linked-In website
Linked-In Larry Kristoff
Larry Kristof
President & CEO, Mantra Venture Group Ltd.
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Larry Kristof’s Summary
The goal of Mantra is to bridge the gap between innovation and investment by aggressively seeking out and incubating clean tech innovations and renewable energy solutions. Mantra’s competitive advantage lies in its ability to flexibly pair together investment and scientific expertise to guide promising new technologies through development and into the market.
Based in the Pacific Northwest, a hot-bed of Green Tech innovation, Management has already been successful in acquiring the rights to two revolutionary sustainable technologies: the Electroreduction of Carbon Dioxide (ERC) technology, and the Biometals Recovery System (BRS) (Soon to be announced).
In collaboration with Kemetco Research Inc., Mantra established a research facility in Vancouver, British Columbia for development of its technologies in May 2008. Staffed by dedicated research team, this plant has capabilities in chemical analysis, chemical, metallurgical and mining engineering, as well as a fully equipped scientific laboratory and pilot plant.
Larry Kristof’s Specialties:
Electro-Reduction of CO2, Bio-Metal Recovery System
Larry Kristof’s Experience
President & CEO
Mantra Venture Group Ltd.
(Renewables & Environment industry)
January 2007 — Present (3 years )
At Mantra, we are committed to developing and commercializing technologies that support a greener economy: meeting the needs of the present without compromising the future. Subsequently, our Corporate Mission is to provide businesses and people with the means to achieve significant, sustainable reductions in their ecological footprint, and in doing so, ensure that our investors benefit both morally and financially from their investment. Our current efforts are focused on two pressing markets: the reduction of carbon dioxide and the treatment of mine wastewater. Subsequently, Mantra has positioned itself to become the leader in each of these niche markets through the acquisition of two key technologies: the Electro-reduction of Carbon Dioxide (ERC) and the Biometals Recovery System (BRS).
Mantra Venture bucks its Industry’s Revenue Decline of -3.23% with an Increase of 186.45%
12/25/2009
New York, NY, December 25, 2009,T12-NEWS says that trailing twelve month (TTM) Revenue for Mantra Venture (OTC:MVTG) for its twelve months ended August 31, 2009 increased by 186.45% to $22,916. This compares to Revenue of $8,000 for Mantra Venture over the previous comparable twelve months ended August 31, 2008. The 186.45% increase over the latest twelve months compares with a Revenue increase of 72.47% for its first quarter ended August 31, 2009 as compared to the previous comparable first quarter.
The industry, Venture Capital, in which Mantra Venture is a member generated a Revenue decrease of -3.23% over its most recent twelve months which compared to an increase of 186.45% in Revenue for the company over the earlier or comparable twelve months. The industry's Revenue statistics compared to a decrease in aggregate Revenue of -12.35% for the S&P 500's non-financial companies and an aggregate decrease in Revenue of -16.59% for the Dow Jones Industrial's non-financial companies.
Currently, the Venture Capital industry is ranked at 84 out of 229 industries based on the Revenue growth rates for all industries over the latest 12 months according to T12-NEWS.
T12-NEWS is a financial news publisher, which is dedicated to reporting on the previous or TRAILING 12 month and fourth quarter financial information and data, which is filed by publicly traded companies with the United States Securities Exchange Commission (SEC). T12-NEWS publishes news on revenue and earnings or Net Income on thousands of public companies, which trade on U.S. Securities Exchanges. The reporting of trailing 12 month and Q4 news for public companies is essential because public companies are not required by the U.S. Securities & Exchange Commission (SEC) to report trailing 12 month or fourth quarter financial data when they make their quarterly filings. The reporting and publishing of Trailing 12 month data is necessary because a constant look back at the previous 12 months of comparative data will give investors a more stable reading on the true health of a public company. T12-NEWS also covers and reports on fourth quarter revenue for all publicly traded companies. Fourth quarter comparisons of financial information over prior fourth quarters can also give investors better readings on the financial health of a publicly traded company. The quarterly, semi-annual and nine months comparative data points which are currently required to be filed by public companies can be skewed because they cover shorter time horizons.
Current and archived trailing twelve month and fourth quarter news, reports and archives from T12-NEWS are available at www.StockTrendNews.com.
Copyright 2009 StockTrendNews.com
Hello everyone,
As we move ahead, i would like to have the goal of posting more DD on the actual players Mantra is getting involved with. So far, the discussions seem to be just mentioning the names of the companies.... but these are big time players and from what I gather... the global market is opening up nicely for Mantra and we will be discussing new prospects and deal makers, regularly for some time.
In my mind, if Mantra was not legit, they would be behind bars already for these press releases. This is the most transparent company i have seen. Even though they are still small, i don't think we need to discuss their legitimacy so frequently. We have bigger fish to fry here and people who come to this board need to know what kind of deals are in the works around here.
I sincerely hope everyone has a safe and enjoyable holiday....well deserved of course. And we should be golden in 2010.......enjoy the Winter Games in Vancouver!!
-Greener
That is an awesome thought. Capturing it is no problem, and by the time they figure out how to contain it cheaply, Mantra can utilize it.
Did everyone get to see Larry's interview? I like the point about sequestering CO2 in plastic production. Great interview because they were not easy on him and raised some great questions. Of course, Larry had great responses. JMHO
-Greener