text:
What has been the best method for you to learn a foreign language?
Rosetta Stone, Formal classes, Flash cards, Skype, study groups, books, audio, italki, what's worked best for you?
Flash cards - certainly no, Skype was non-existent in those times, study groups - a good idea, but only if there is a native speaker/qualified tutor in the group, audio - nice, Rosetta Stone - not bad for concrete nouns and basic verbs of motion/action. For me the tools that worked were a monolingual explanatory dictionary and extended immersion in original texts and audio. I noticed that as soon as you cross a threshold of the amount of info you get in a foregin language, the brain switches to the 'language acquisition mode', and you start to memorize things faster. But if you study a language as a set of facts, your capabilities are very limited. But I am sure that some people who like to collect trivia and have 'big' memory, may benefit from simple memorization of rules and facts.
I believe that if you want to make the first contact with the language Roseta is a good choice.
My introduction to Russian was learnrussian.rt.com. It's awesome. 100 free interactive lessons with tons of audio throughout. I don't think I'd be where I am with Russian without it. Let me know what you think.
Good luck,
What helps me to study english most:
1) Cambridge English Grammar
2) Italki
3) Skype-communication with native speakers
Also, I like watching films in english on www.vk.com - you may sign up on this site, it's the greater social web in Russia, you may find out lots of russian movies there and many groups about russian language. But, in general, I perfer to learn foreign language by all these methods. Hope it helps.
i think if you want to learn native language,the best way is go to the native Country,you can learn the language faster.
only two words: Foreign friends.
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Synthesis gases containing carbon monoxide, eg above 40% volume, and hydrogen are methanated to produce substitute natural gas, after CO2 removal, wherein the synthesis gas is simultaneously saturated with water, further heated and divided into first and second feed gas streams. The first feed gas stream is catalytically methanated at a temperature of from 250 to 550° C, and the reaction product mixed with said second feed gas stream. The mixture is methanated over a second catalyst at a temperature of from 250 to 550° C and the product is divided into a second product gas stream and a recycle gas stream and the recycle gas stream is admixed with the first feed gas stream, prior to the first catalytic methanation. The second product gas stream is subjected to a carbon dioxide removal process to produce SNG.
1. A process for producing a methane containing substitute natural gas from a primary synthesis gas containing more than 40 percent by volume of carbon monoxide on a dry basis and hydrogen comprising the steps of:
simultaneously heating and saturating said primary synthesis gas with water;
heating the saturated synthesis gas further and dividing the same into first and second feed gas streams;
admixing a recycle gas stream from the product gas of second concurrent shift and methanation reactions with the first feed gas stream and subjecting the admixture to first concurrent shift and methanation reactions over a catalyst at a temperature of from 250° to 550° C.;
mixing the product of the first reactions with said second feed gas stream and effecting second concurrent shift and methanation reactions on said mixture over a second catalyst at a temperature of from 250° to 550° C.;
dividing the product of the second reactions into a second product gas stream and said recycle gas stream; and
subjecting said second product gas stream to a carbon dioxide removal process.
2. A process as claimed in claim 1, wherein said primary synthesis gas contains greater than 50% by volume (on a dry basis) of carbon monoxide.
3. A process as claimed in claim 1, wherein the saturated primary synthesis gas also contains steam in a ratio of up to 1 part by volume of steam per 1 part by volume of the dry gas.
4. A process as claimed in claim 1, wherein the synthesis gas, after said saturation, has a steam to dry gas ratio (on a volume basis) of 0.1-1.0:1.0.
5. A process as claimed in claim 1, wherein the process is carried out at a pressure of from 50 to 2000 psig.
6. A process as claimed in claim 1, wherein the volumetric ratio of recycle gas stream to second product gas stream is from 1.0-6.0:1.0.
7. A process as claimed in claim 1, wherein the heated synthesis gas is divided into three feed gas streams, said third feed stream being combined with said second product gas and subjected to a third methanation reaction at a temperature of from 250° to 550° C. to produce a third product gas stream.
8. A process as claimed in claim 7, wherein the heated synthesis gas is divided into four feed gas streams, said fourth feed stream being combined with said third product gas stream and subjected to a fourth methanation reaction at a temperature of from 250° to 550° C. to produce a fourth product gas stream.
9. A process as claimed in claim 7, wherein a portion of said third product stream is recycled back to at least one of the inlets of said first, second and third methanation stages.
10. A process as claimed in claim 1, wherein said second product gas stream is subjected to a further catalytic methanation prior to carbon dioxide removal.
11. A process as claimed in claim 10, wherein water vapour is removed from the second product gas stream prior to said further catalytic methanation.
12. A process as claimed in claim 1, wherein the temperature of the water added to saturate the primary synthesis gas is from 150° to 300° C.
13. A process as claimed in claim 12, wherein at least a portion of said water is heated by indirect heat exchange with the product of the first methanation reaction.
14. A process as claimed in claim 13, wherein said water is heated by indirect heat exchange with the product of the first methanation reaction after admixture of said product with said second stream.
This invention relates to the production of fuel gases suitable for use as substitute natural gas (SNG) from a primary synthesis gas produced by the partial oxidation of carbonaceous fuels such as oils or coal.
Processes are known whereby liquid or solid fuels may be gasified to give a product containing minor quantities of methane and much larger amounts of hydrogen and carbon monoxide. These gases are unsuitable for use as SNG but can be upgraded by reaction of the carbon monoxide with steam to give carbon dioxide and hydrogen and thereafter this so called shifted gas can be subjected to methanation reactions. Since the catalysts employed for methanation reactions are usually sensitive to sulphur poisoning it has been common practice to place a desulphurisation train prior to the methanation system. Usually carbon dioxide is also removed from the gas at this stage, so that the final gas, after methanation, is substantially methane.
The present invention now proposes a process for upgrading gases such as those produced by the partial oxidation of carbonaceous fuels which dispenses with the necessity of effecting a shift reaction on the gases prior to methanation and wherein the methanation reaction can be performed under adiabatic conditions, which process offers lower capital and operating costs for gas production than hitherto known.
In accordance with the present invention there is provided a process for methanating primary synthesis gases containing carbon monoxide and hydrogen to produce a substitute natural gas which process comprises simultaneously heating and saturating the primary synthesis gas with water, further heating and dividing the synthesis gas into first and second feed gas streams, subjecting the first feed gas stream to a first methane synthesis reaction over a catalyst at a temperature of from 250° to 550° C., mixing the product of the first reaction with said second feed gas stream and effecting a second methane synthesis reaction on said mixture over a second catalyst at a temperature of from 250° to 550° C., dividing the product of the second reaction into a second product gas stream and a recycle gas stream, admixing the recycle gas stream with the first feed gas stream, prior to effecting said first methane synthesis reaction, and subjecting said second product gas stream to a carbon dioxide removal process.
The process of the invention may be carried out at pressures up to about 2000 psig, and typically the pressure may range from 50 to 1000 psig.
According to a modification of the process of the invention, the heated primary synthesis gas may be divided into more than two feed gas streams and subjected to more than two methane synthesis reactions, the first and second feed gas streams being subjected to methanation reactions as described above and, wherein the third feed gas stream is admixed with the second product gas stream and subjected to a third methane synthesis reaction to produce a third product gas stream. Similarly a fourth feed gas stream may be mixed with the third product gas stream and effecting a fourth methane synthesis reaction to produce a fourth product gas stream. Such third and fourth methane synthesis reactions may also be conducted at a temperature of from 250° to 550° C. Any further feed gas streams may be subjected to methanation by mixing with the product gas from the previous methanation stage and subjecting the mixture to subsequent methanation reactions. It may be desirable to recycle a portion of a subsequent product gas stream back to the inlet of one or more earlier methanation stages by mixing said recycled product gas with the product gas stream from the previous methanation stage. Furthermore, it may be desirable to subject the third and subsequent feed gas streams to separate methane synthesis reactions prior to combination with the respective product gas streams. The carbon dioxide removal process may be effected on the product gas stream from the last methanation reaction.
In order to upgrade the gas further the invention further provides for the addition of at least one further methanation unit taking the whole of the product gas stream immediately prior to the carbon dioxide removal step. The further methane synthesis units may be operated under substantially the same operating temperature and pressure ranges as those for the other units. It may be desired to remove some or all of the water vapour from the gas prior to some or all of the methanation stages after the first two in order to adjust the composition of the final gas.
The primary synthesis gas to be treated in accordance with the invention may be any gas produced by oxidation processes. For example, the gases may be produced by the well known partial oxidation routes for heavy oils or by the gasification of coals with steam and oxygen. The process of the invention is suitable for use with primary synthesis gases having very high contents of carbon monoxide, eg of the order of greater than 40% by volume (dry basis) and preferably greater than 50% by volume and low steam contents of, eg less than, 50% by volume(steam/dry gas), such as those produced by high pressure slagging gasifiers. Such gasifiers are described, for example, in UK Patent Specification No. 977,122. The process of the invention is particularly suitable to those synthesis gases having a volumetric steam to carbon monoxide ratio of from 0-1.0:1.0.
Prior to carrying out the methane synthesis reactions the primary synthesis gases are saturated with water. Typically the temperature of the water is about 180° to 200° C., but the temperature may vary from 150° to 300° C. After saturation the gas may have a steam to dry gas ratio (v/v) of from 0.1-1.0:1.0.
The water used in the saturator is preferably heated by heat exchange with cooling gas streams within the plant. For example, heat may be raised by indirect heat exchange with primary synthesis gas prior to desulphurisation and/or with the final methanated product gas prior to the final carbon dioxide removal stage. However, the heat available from these sources is generally only available at relatively low temperatures and it may be insufficient to raise the temperature of the saturator water to that desired. The desired temperature may be obtained by contacting at least a portion of the saturator water stream with a source from which heat is available at high temperatures. Thus, at least part of the saturator water stream may be subjected to indirect heat exchange with a source of high grade heat within the process, for example, with the first methane synthesis state product, either before or after admixture of said first stage product with the second stream of saturated primary synthesis gas.
Since water is consumed during the methane synthesis reactions and a further part may be lost as a purge stream in the removal of contaminants which build-up in the saturator liquor system, a water make-up stream is necessary. This make-up stream may be heated by indirect heat exchange with cooling gas streams prior to admixture with excess unevaporated water recovered from the saturator for further use.
Most of the remaining heat which needs to be removed from the gas streams within the process is available at relatively high temperatures and this allows high pressure steam to be generated for use in other parts of the gasification process, for example, within the primary synthesis gas producer or for the generation of mechanical power.
The efficiency of the process is maximised by not effecting the methane synthesis in a single stage. Because of the nature of the catalysts it is necessary to control the maximum temperatures obtained in each reactor and this is achieved by recirculating at least part of the methanated gas product, and by by-passing a part of the saturated primary synthesis gas around at least the first stage. Higher steam contents and higher recirculating ratios effect the efficiency of the process, and they are minimised within the constraints of avoiding excessive reactor temperatures and carbon depositions in the catalyst (by mechanisms such as the Boudouard Reaction). A further advantage of dividing the feed gas between the first and second stages is that it readily allows a closer control of reaction temperatures and the use of smaller amounts of recycle gas. The amount of gas recycled is defined by the recycle ratio. The recycle ratio is expressed by the relationship -- ##EQU1## The process of the invention may be carried out using recycle ratios of from 0.2 to 10:1.0 preferably from 1.0 to 6.0:1.0.
According to the various embodiments of the invention gases may be recycled at several positions. We have found that the recycle ratios for each stage may be smaller, the larger the number of stages employed. For methanators operating under substantially similar conditions, there is generally an inverse linear relationship between the recycle ratio (for a given stage) and the number of reactors or stages.
The gas leaving the final methane synthesis stage has a carbon dioxide content which can be above 50% by volume rendering it unsuitable as SNG. It is therefore necessary to treat this gas to lower the carbon dioxide content to less than 10%, eg about 2%. In many cases conventional physical and chemical absorption systems may be employed. However, since the final methane synthesis product gases are likely to have a very high partial pressure of carbon dioxide it has been found especially advantageous to employ cryogenic techniques to remove the bulk of the carbon dioxide. Whatever process is employed for carbon dioxide removal the process of the invention has the advantage that the high partial pressure of carbon dioxide allows more efficient carbon dioxide removal. The conditions under which the methanation stages operate mean that the carbon monoxide and hydrogen content can be controlled more easily than hitherto. If physical absoroption processes such as the Rectisol, Selexol or Sulfinol processes are employed it has been observed that further drying of the gas to pipeline specification is not unually necessary.
The processes employed for carbon dioxide removal may also be employed for the removal of impurities such as hydrogen sulphide and carbonyl sulphide prior to effecting the methane synthesis reactions in accordance with the invention.
It is advantageous to employ the same process to treat the gas streams before and after the methane synthesis stages since such integration leads to lower costs and lower energy requirements for absorbent regeneration purposes.
The removal of sulphur compounds from the primary synthesis gas is easier since the stripped gas from the regenerator of the absorption process will have a much higher hydrogen sulphide content than that obtained if the gas is so treated after being subjected to a conventional shift reaction and this will greatly aid sulphur production.
Chemical absorption processes might be best for the final CO2 removal stage since a physical absorption process, such as the Rectirol Process, would have methane loss problems, but we are unaware of the extent of this problem here, where, presumably, the absorption and stripping stages will not have to operate under conditions as severe as those encountered when both sulphur compounds and CO2 are to be removed.
Since the catalysts used for the methane synthesis reactions are usually extremely sensitive to poisoning by sulphur compounds, if the gas purification stage prior to the saturation stage does not remove sulphur compounds to a sufficiently low level, it is necessary to perform a further fine purification stage. If such a fine purification process is required to operate at high temperatures, eg absorption by zine oxide containing materials, it is best performed after saturation of the primary synthesis gas, eg upon steam-containing gases, provided that the presence of steam in the gas does not adversely effect the operation of the purification process.
The reasons for the higher efficiency for the process of the invention are not believed to be self evident. It can be looked upon as resulting from the reduced number of main stream cooling steps, in that, the cooling of the water laden shifted gas, which in any event would yield mostly heat at low temperature, is eliminated. Equally it can be seen as the liberation of heat, mainly in the methane synthesis stages which is suitable for high pressure steam generation at a useful temperature, whilst high pressure steam has to be added to a conventional shift stage. In a sense, in the methane synthesis stages, the steam for the shift reactions is in part generated internally by the concurrent methanation reactions which also consume the hydrogen produced in the shift reactions.
The obtaining of a high efficiency is dependent on the transfer of low grade heat from the primary synthesis gas, prior to purification, and final methanated gas to the purified synthesis gas to be subjected to the process of the invention The stream to the methane synthesis stages contains much high grade heat because of the relatively high temperature and high steam content. It is advantageous to raise this steam at its partial pressure in this gas as opposed to the full pressure of the system, as would be necessary if this were raised in a boiler and added as high pressure steam. This is achieved by the use of the saturator. Corrosion problems with saturated carbon monoxide containing gases have been evidenced both at low and high temperatures. However, at temperatures in the range of 150° C. to 250° C. no corrosion problems have been experienced, even after considerable use.
Generally since the methane synthesis reactions are accompanied by a significant decrease in gas volume, compared with conventional shift reactions, it is not usually advantageous to cool by direct contact with cold water to obtain the heat exchange from the final methanated gas.
The invention will now be described with reference to the accompanying drawings, in which:
FIG. 1 is a schematic representation of a gas making plant employing the process of this invention; and
FIG. 2 is a schematic representation of part of FIG. 1 showing an alternative arrangement for heating the saturator water stream.
Apparatus common to both figures are designated by the same numeral.
Referring to FIG. 1, a primary synthesis gas is produced in a slagging gasifier 1. The synthesis gas is first treated and cooled to remove tars and oils therefrom in separators exchangers 2, 40 and 3 respectively. The tar and oil free gas is then subjected to desulphurisation in unit 5. In the embodiment shown the sour gas 24 is first subjected to a naphtha pre-washing unit 4 prior to absorption in 5. With some kinds of desulphurisation processes pre-washing is not necessary. The desulphurisation process can be effected at relatively low temperatures and, thus, the sour gas 24 is heat exchanged with the sweet gas 11 in heat exchanger 6 to maximise thermal efficiency. Sweet gas 11 is then saturated with water in saturator 7, water being provided by line 20 and the unevaporated water removed via line 21. Stream 33 is then divided into two streams 34 and 35. Gas stream 34 is then subjected to a first methane synthesis reaction in vessel 8 and the product gas 36 cooled by heat exchange with stream 33 in exchanger 9. Cooled stream 36 is combined with stream 35 to produce a mixed stream 15 which, after temperature adjustment, is subjected to a second methane synthesis reaction in vessel 10 to produce gas stream 16. Stream 16 is divided into two streams, recycle stream 19 which is combined with stream 34 as the feestream for reactor 8 and stream 18 which is reacted in a third methane synthesis reactor 12 to produce gas stream 39. The final product stream 39, after cooling in heat exchanger 14, is treated to remove carbon dioxide in vessel 13 to give an SNG 48.
The water stream 21 recovered from the saturator 7 is recycled via pump 43 for further heating and re-use. In the embodiment shown, stream 21 is divided into streams 22 and 23. Stream 22 is heated by heat exchange with the primary synthesis gas in exchanger 24 and recombined with stream 23 after heat exchanger 25 which is further heated by heat exchange with the final product gas 39 in exchanger 26 to form stream 20 which passes to saturator 7. The water loop formed by streams 21, 22, 23 and 20 is also provided with inlets and take-off points (not shown) for adding make-up water and removing a purge stream respectively.
High pressure steam boilers are provided at 27 and 28 to utilise the high grade heat available in the cooling gas streams 15 and 16 respectively.
Referring to FIG. 2, water stream 21 is divided again to form two streams 22 and 23. Stream 22, as shown in FIG. 1, is heated by synthesis gas in exchanger 24b. Stream 23 is admixed with make-up water 41 heated by stream 39 in exchanger 32 and the combined stream heated by exchanger 25. This stream is divided into streams 29 and 30, stream 29 combining with stream 22 and passing through exchanger 24a, which cools crude primary synthesis gas, before forming stream 31. Water stream 31 is then subjected to heat exchange with a high grade heat source in exchanger 42. Stream 30 is combined with the very hot stream 51 to form stream 20, which passes to saturator 7. Purge liquors may be removed from the water loop via line 38.
The invention will now be illustrated by the following Examples.
Apparatus as shown in FIG. 1 was employed to produce SNG having the characteristics shown in Table 1, stream No. 48. The stream numbers shown in Table 1 report the gas characteristics of the gas at various stages in its production as shown by the same numerals in FIG. 1 of the drawings.
The recycle ratio Volume of Gas 19/Volume of Gas 18 was 2.59.
TABLE 1__________________________________________________________________________STREAM NO. 1 24 11 33 15 37 16 19 34 36 18 39 48__________________________________________________________________________Press. (psia) 465 430 405 390 373 370 355 387 375 373 350 335 1000Temp (° C) 632 32 30 177 418 280 462 280 280 462 280 320 30COMPONENTCo lb mol/h 61.48 61.48 61.48 61.48 35.66 35.66 2.59 1.87 27.94 2.12 0.72 0.03 0.03CO2 lb mol/h 1.34 1.34 1.00 1.00 126.98 126.98 149.12 107.58 0.45 126.43 41.55 41.32 0.33H2 lb mol/h 24.74 24.74 24.74 24.74 24.17 24.17 13.00 9.38 11.24 10.68 3.62 0.63 0.63CH4 lb mol/h 8.49 8.49 8.49 8.49 96.39 96.39 108.06 77.97 3.86 91.75 30.11 31.03 31.03C2 H6 lb mol/h 0.41 0.41 0.41 0.41 0.23 0.23 -- -- 0.19 -- -- -- --C2 H4 lb mol/h 0.27 0.27 0.27 0.27 0.15 0.15 -- -- 0.12 -- -- -- --N2 lb mol/h 0.69 0.69 0.69 0.69 2.49 2.49 2.49 1.80 0.32 2.11 0.69 0.69 0.69H2 S lb mol/h 2.19 2.19 -- -- -- -- -- -- -- -- -- -- --Steam lb mol/h 16.14 0.16 -- 51.79 124.10 124.10 112.89 81.41 23.54 95.85 31.46 32.60 --Tars lb/hr 151.23 -- -- -- -- -- -- -- -- -- -- -- --Oils lb/hr 15.20 -- -- -- -- -- -- -- -- -- -- -- --Naphtha lb/hr 38.30 38.30 -- -- -- -- -- -- -- -- -- -- --NH3 lb/hr 11.0 -- -- -- -- -- -- -- -- -- -- -- --Fatty acids lb/hr 4.48 -- -- -- -- -- -- -- -- -- -- -- --__________________________________________________________________________
The apparatus of FIG. 1 was modified, as shown in FIG. 2, and an SNG prepared under the conditions set out in Table 2. As in Example 1, the stream number reports the gas characteristics at similarly designated points in FIG. 2.
The recycle ratio Volume of Gas 19/Volume of Gas 18 was 2.59.
TABLE 2__________________________________________________________________________STREAM NO. 1 33 15 37 16 19 34 36 18 39__________________________________________________________________________Hydrogen, lb m/h 21988 21988 21484 21484 11556 8335 9993 9489 3220 560Methane, lb m/h 7555 7555 85677 85677 96055 69302 3433 81556 26765 27584Carbon monoxide, lb m/h 54653 54653 31696 31696 2305 1663 24839 1882 642 24Carbon dioxide, lb m/h 889 889 112868 112868 132545 95627 404 112384 36933 36731Nitrogen, lb m/h 617 617 2215 2215 2215 1598 280 1878 617 617Ethane, lb m/h 367 367 200 200 -- -- 167 -- -- --Ethylene, lb m/h 241 241 131 131 -- -- 109 -- -- --Tot. gas dry, lb m/h 86310 86310 254271 254271 244676 176525 39225 207189 68177 65516Steam, lb m/h -- 46034 110312 110312 100348 72361 20922 85199 27961 28982Tot. Gas wet, lb m/h 86310 132344 364583 364583 345024 248886 60147 292388 96138 94498Temperature, ° F 86 351 761 536 864 536 536 863 536 608Press, psig 390 375 360 355 340 372 372 360 335 320__________________________________________________________________________
The final gas had the composition shown in the column headed 39 in Table 2.
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We loved Frank Ocean's Pond O' Serenity and Ezra Miller's bolero business funeral suit, but if there was one bright, shiny, Australian moment that truly made us swoon during tonight's MTV VMAs, it would have to be Rebel Wilson's intro bit for "Best Female Video" with The Wanted. Why was it such a highlight? Well, for one, the Pitch Perfect star wasn't taking herself seriously at all. You can't make Kevin Hart be the only comedic relief in a two-hour show! In case you needed us to break down the reasons Rebel snatched our hearts with her Ruffles-covered hands, they would be…
- That bathing suit shirt.
- The fact that Rebel would publicly proposition The Wanted. "Who wants to be the chip in my dip?," she inquired. Wilson is just saying…what we're all thinking!
- "This one's bisexual," Wilson declared while grabbing Max George. Max merely roles his eyes. Squeeeee!
- Finally, a masturbation joke! "I think I'm just going to go home and finish myself off," Wilson concluded after none of the boys stepped forward to get down. Considering the fact that most attendees were treating the VMAs as solemnly as the Presidential Inauguration, we seriously needed one.
- There are straight-up pubes hanging off that bathing suit shirt. A-mah-zing. Then Kevin had the audacity to declare, "You gotta wax that. That's nasty." Oh, you mean that's perfection? Rebel FTW.
[Photo: Getty Images]
Related: VMAs 10 Worst Dressed? Katy Perry, Ezra Miller, Nicki Minaj And Others We Hate To List Here
5 Reasons Rebel Wilson Was The Best Part Of The VMAs (As If You Needed Us To Tell You)
Miley Cyrus Vs. Pink: Who Rocked The Blond Pompadour Better At The VMAs
Please Tell Us How To Feel About Rita Ora's VMA Red Carpet Outfit: It's A…Racy Pantsuit
2012 Video Music Awards' Best Dressed: From White Hot RiRi To The Fierce Five Cuties


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1. coozin - (noun) a female cousin that will let you fuck her
2. coozin - (verb) the act of fucking one's female cousin
2. coozin - (verb) the act of fucking one's female cousin
That nasty hillbilly is over there tappin' his coozin!
He's one coozin billy goat!
He's one coozin billy goat!
by backwoodscoozinfuckinmuthafuck September 20, 2011
2 more definitions
Top Definition
Fucked up to the perfect level. A state of mind where one is soaring through the sky but still in their senses, as if they're "cruising" through.
"Yo, Niv and I have been coozin alllllll day. We're trying to pick up some more, you good?"
by PikesVillain August 29, 2011
The bestest and most cutest way to say cousin.
My aunt had three kids so now I have three little baby coozins and they are oh so cute!!!
by Face&Butt May 18, 2009


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VPBank posts 40.3 b dong pre-tax profit
In the first nine months this year, total pre-tax profit of VPBank are estimated at 40.3 billion dong, surpassing the plan by 15% set by the shareholder meeting in early year 2004, said a high level VPBank official.
Since the start of 2004, VPBank has put three banking transaction booths in operation in Hanoi and Hai Phong City and completing necessary procedures to open more banking transaction booths and branches nationwide.
According to the plan by VPBank, by the end of 2004, its banking network will have 25 banking transaction booths in Hanoi, HCM City, Hai Phong, Hue, Can Tho and Da Nang.
Category: Finance


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text:
of field."
— Mark Strand
Everyone needs something to hang onto.
It helps us keep the crows away.
You cling to your journey —
A long walk on yellow brick, two taps
From a wizard's wand. I like to think
Of these cornrows as a kind of maze,
Imagine unhitching myself
From this pole I'll never call home
And walking through stalks to an end
Where, like magic, someone touches me.
II. At Picnic
If you stand where I hang
And keep your eyes straight,
You will see a poplar
At the far edge of the field. There,
A body once swayed,
Burning from foot to breast.
The crows cawed
Unmoved, their plucking a parade.
The wind blew the odor of death
In my direction. I had a mind
To cry; I shut my marble eyes
Too afraid to scare a bird.
III. Wants to Know
Who is my father?
Why am I alone?
What must this field
Feel for the plow?
What does the crow love
Other than himself?
IV. On Graduate School
Grass for acres and trees tall,
Then, everywhere there should be
Some harvest to guard, sprouts
A building in which I am mistaken
For a broom, handled as such,
And given to the floor. To dust.
I am here to learn: that which fears me
Must be crow
In this hall of heavy doors
Where my body is a blemish.
V. In the Pulpit
I am a mouthless man of straw.
Fields of wheat wave around me.
Oh, my God, there is so much to sing.
I'm not dumb, but I wish I were.
A fool bothers the Father about a brain.
Hear us, Lord. There is too much to pray.
I am a mouthless man made of straw.
I hang to keep the crows away.
The fruits they pick. The murders they make.
When your Savior asked for water
They gave him vinegar instead.
Sweet Jesus, how long before you come?
I am a mouthless man of straw.
I hang to keep your children fed.
The fruits they pick. The murders they make.
Forgive us, Father, the use of our hands.
Published in Please (Kalamazoo, Michigan: New Issues Poetry & Prose, Western Michigan University, 2009).
© 2010 Jericho Brown and Southern Spaces


text:
Wahl Expands Lithium Ion Line
-- Lithium Ion Beard & Stubble Trimmer Meets Specific Needs of Guys Today --
STERLING, ILL. (March 12, 2013) – The 5 o'clock shadow is sprouting up on jaw lines across the nation and Wahl is making sure guys sporting this look have the tool they need to keep it in check. The company that introduced lithium ion technology to the men's trimmer category is now putting that power where it's needed most—a new specialty trimmer designed for the growing number of guys growing beards and stubble.
According to NPD, the beard and stubble trimmers market grew by 20 percent from 2011 to 2012, representing the fastest growing segment in the category. Through its new Lithium Ion Beard and Stubble Trimmer, Wahl is addressing this growth by adding the same technology that made the Lithium Ion Trimmer a top-seller at retail.
The new addition marks Wahl's first specialty trimmer in its lithium ion grooming lineup. The line includes the Lithium Ion Trimmer, the Lithium Ion + Stainless Steel Trimmer and Lithium Ion Clipper.
"In a recent focus group, 38 percent of guys said they prefer the stubble look when they sport facial hair," said Jeff Bovee, senior product manager for Wahl. "However, while many sport the look, it's important to know that it still needs to be maintained. That's why we are introducing the Beard & Stubble Trimmer as a solution to easily take care of business."
This Lithium Ion Beard & Stubble Trimmer keeps up with the reputation that Wahl's Lithium Ion family is known for, including a sleek body, three times the run time and a one minute quick charge feature for touch ups. It also boasts a longer lasting battery, and with normal use, consumers can wait up to one year between charges.
"The biggest complaint guys have is that their trimmer battery wears out quickly, or dies out mid-use," said Bovee. "Therefore, we knew our Beard & Stubble Trimmer had to be powered by lithium ion. No matter what style guys have, they want their grooming tool to be powerful and hold a charge."
In addition to being powerful and long lasting, this trimmer also has an integrated guide comb system with eight different cutting positions. The new design is about keeping it simple for the job at hand, while also allowing for easy maintenance for guys who live by the motto 'less is more.' It's also sleek and stylish, courtesy of its brushed metal casing.
The Lithium Ion Beard & Stubble Trimmer is available nationwide for a MSRP of $46.99. The product includes the company's signature precision-ground blades for superior performance and a long lasting five- year warranty.
For more information, visit www.wahlhomeproducts.com. Or, to find out tips and tricks for achieving the stubble look, visit Wahl Nation's Encyclopedia of Styles at www.wahlnation.com.
About WAHL
Now in its 94th year, Wahl Clipper Corporation is an international industry leader in the manufacturing of products for the professional beauty and barber salon trade, consumer personal care and animal grooming. Headquartered in Sterling, Ill., Wahl currently employs some 2,000 people worldwide in Argentina, Australia, Brazil, Canada, China, England, Germany, Holland, Hungary, Japan, New Zealand, Russia, South Africa, Spain and the United States. Wahl products are available in 165 countries around the world. For more about Wahl, please visit www.wahl.com.
Media Contact For More Information
Patrick Kopischkie, (414) 225-9522


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Bruce Pinsler from Galaxie Home Remodeling discusses why the economic climate has stimulated the remodeling business, and tell us about some of his company's recent projects. Julia Billen from Warmly Yours Radiant Heating gives insight into floor heating and heating panels for the living room. And in our third segment, Tony Cobb from Underdeck Oasis talks about using the space below your deck ceiling as a living space.
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Video:Balance Exercises for Seniorswith Tricia van der Walde
Learning how to do balance exercises for seniors is important for the elderly. Here, see step-by-step instructions for doing balance exercises for seniors.See Transcript
Transcript:Balance Exercises for Seniors
Hi this is Tricia van der Walde for About.com.
Before Doing Balance Exercises for Seniors
Today I'm going to show you five easy stretches for seniors which can be done in the safety of your own home or also in the gym setting. Before you do any stretches you should be properly hydrated and warmed up for a few minutes so you are more limber to do your stretches. Each stretch should be held for a minimum of 30 seconds to a minute so you are going to breathe 2 or 3 times in each position.
Five Balance Exercises for Seniors
The first stretch I'm going to show you is seated on a chair, good postural alignment and drawing in the belly button. You have your hand placed underneath the chair and with the opposite hand and bring it up, placing it on the side of the head gently drawing the ear towards the shoulder. So now you are drawing the opposite shoulder away from the opposite ear. This is an excellent stretch for the neck and you can repeat this for the opposite side.
The next stretch will be in the standing position so we are going to get up. We are going to do the calf stretch. So you are just going to pivot at the hip, you are going to come forward with your eyes forward, drawing the belly button in, keeping this back nice and straight so you are drawing the toes towards the shin, breathing in and out. Exhaling until you feel the calf muscle releasing and you can stand up and repeat this on the opposite side.
To open up the chest muscle we are going to bring our hands behind us, drawing the shoulders down and the shoulder blades together so that we are relaxing at the shoulders and we are opening up at the level of the chest. Again you hold this for a minimum of 30 seconds, breathing in and out each time.
The next stretch we are going to do sitting down and we are going to take the number four position with our legs, one foot at the level of the opposite knee and we can use a prop for this in the form of a belt or a sash or an elastic band, which is what I have. This helps us keep a nice straight back and here we just pivot forward with both hips well aligned, gazing forward with the eyes, bending down and drawing the belly button in and doing your nice breathing in and out. Hold the stretch until you feel the release on the back all the way from the lower leg to the upper leg. Come up and repeat this on the opposite side.
The last stretch that I want to show is drawing you knees up and letting them fall to the sides, soles of the feet together, sitting back on the palms of your hands, fingers open, shoulders drawing back and just allowing a nice release of the hips. Hold this stretch the same amount of time as the other stretches and that is a great hip opener. Thanks for watching. To learn more just visit us on the web at About.com.


text:
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Select an edition for more focused local news coverage when you visit NOLA.com.
Don't worry. You can change this setting at any time to another local edition.
This is a very sad story and indicative of how our country places more value on taxes and property than life. We are all doomed....pay your taxes or die. What have we become? Very sad indeed. Shame on us all. Vote correctly tomorrow!
Come on TP, if you are going to give out home addresses, please make sure you are using the correct address. Neither of them lived at 4087 Division St. Please get your facts straight.
It is not unheard of for cats to "hide" under car hoods. I have seen kittens "flying" out of a truck on the interstate and sped up to confront the driver. The driver's windows were up and he looked at me as though I were a crazy person while I was trying to mouth to him of the tragedy that was taking place. Obviously, he knew nothing about it. That's when I realized he wasn't "throwing" the cats, but rather, the poor kitties just couldn't hang on going 70 mph with their little paws. Perhaps this is the same thing that happened to this lady? It's tragic that we have so little faith in each other.
I have a feeling those kids were the same kids involved in a shooting in Shrewsbury..
In fact..
"i kinda know it was"
It is your duty to come forward. These criminals should not be allowed to do this again.
I don't understand what you are trying to say. I think the Bacchus organization has done a wonderful job in chosing their celebrity kings. You should start your own krewe and invite who you want to be your king.
That is just perfect.
McCain wins Louisiana...why is this a racial issue? Those who voted for him only voted for him because he was the REPUBLICAN candidate...
Wow. That used to be a pretty safe neighborhood. It looks like JPSO should put a substation there now. I agree with remymcswain, this should be classified as a hate crime.
Bravo NOPD! Now, for the rest of the citizens...follow suit. Snitchers unite and turn in the bad guys and gals. I don't want to live like this anymore. Peace!
First of all, I commend LaBruzzo for his suggestion. It's a good one, however, the monetary amount was an insult (opening bid perhaps?). Considering the amount of $$ the state will pay for the offspring and mother/father for the rest of their lives (and probably the offspring of those offspring), the amount of money offered should have been higher,like $50,000.00. The state would still have come out ahead. However, sterilizing these folks does not automatically mean they are going to be self-sufficient and productive in the workforce. It was just a suggestion people. I think we should all throw ideas on the table, be it good or bad. I will definitely re-elect someone who is not afraid to offend. He's not a robot!! Amen.
Perhaps the shooter was really aiming at the criminals and hit his target. I know it's unheard of, but maybe there is a vigilante amoungst us...or a superhero wannabe.
Wow. Such hatred amongst us. While there are several valid points made, if you all could open your minds to see the objective, you may get a glimpse of how the other side feels.
If one is to belong to a community, then one should abide by the rules of the community. No one is better or more deserving than any of the others. There are no kings or queens in this country. I am not your slave, either. If you can't do for yourself, then do without.
WOW! 20 years seems harsh for spending "his" loan money (he has to pay back) while the guy who shot at the baby in the car is only facing 10 years. AM I on GLUE???
Get him out of here.
That is the mentality we need EVERYONE to have.
An innocent bystander was almost killed (but not) and they caught the perp. That is excellent work NOPD! He is in the system now and won't be getting away with this crime. So, why all the racist comments? I see they are coming from both sides. If you guys hate that much, you really should seek professional help. As a community, we should NOT be against each other. We should be against the criminals...no matter what race they are. Enough is enough!
Amen whtmn:
You are absolutely right. However, it's not a skin color thing, it's a moral mentality. I know some very hard working, honest black folks and I know some very thuggy white folks. It's not the skin color that seperates the good and the bad...it's the way a person respects himself and others around him. We have to force those people to be accountable. We must show them that we won't tolerate it anymore.
Does it really matter? Everyone is entitled to their opinion. It seems that most of us have the same opinion. How can EVERYONE be wrong? Especially when the writing is on the wall, so to speak. How much more do you think the good people will take from these thugs? Be real.
He's been fighting bureaucrats.
Bravo. Let's make sure everyone is honest. Even a small infraction is still an infraction, none the less. If one is inclined to abuse things such as gas usage, what is to keep him/her from abusing other things? This could lead to bigger findings. Don't you question why the mayor's office isn't supporting this?


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Texas Politics
All Texas politics all the time from the San Antonio Express-News and Houston Chronicle
Posts filtered on Tag
'Prime Time' angling for school charter
NFL Hall of Famer Deion Sanders impressed State Board of Education members this week during his presentation involving a charter school application. Sanders founded Prime Time Association, a 501(c)(3) nonprofit organization, three years ago to reach and teach youth through sports and education. The group promotes positive self images and invests in the mental, spiritual, […] [Read More]


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|Towneplace Suites By Marriott Warrensburg hotels are listed below. Search for cheap and discount Towneplace Suites By Marriott hotel rates in Warrensburg, MO for your upcoming individual or group travel. We list the best Towneplace Suites By Marriott Warrensburg hotels + motels so you can review the Warrensburg Towneplace Suites By Marriott hotel list below to find the perfect place.
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Job Seekers, Sign In
South University of Science and Technology, Shenzhen, China Faculty Position in Chemistry « Position Deleted on 5/10/2014 »
|South University of Science & Technology of China
|Shenzhen, China
|03/11/2014 (Reposted Job: Initially posted on 01/09/2014)
|Full Time
|included on Affirmative Action email
This position is no longer an active posting on HigherEdJobsThe Department of Chemistry at the South University of Science and Technology invites applications for full-time faculty positions at the rank of tenure-track Associate or tenured Full professor in the area of Physical Chemistry (preferably molecular spectroscopy), Structural Chemistry (with profound expertise in X-ray crystallography), Chemical Biology (with an education in chemistry), and Analytical Chemistry (preferably NMR or Mass Spectroscopy). Applicants should have a PhD with demonstrated potential in research and a commitment to teaching. Successful candidates are expected to pursue an active research program, to teach both graduate and undergraduate courses, and to supervise graduate students.
South University of Science and Technology, officially established in April 2012, is a research-intensive public institution funded by the municipal of Shenzhen, a growing international metropolitan neighboring Hong Kong. The University is accredited by the Ministry of Education, China and is a pioneer in higher education reform in China. The teaching language at the University is English or Putonghua. The choice is made by the instructor.
The University offers internationally competitive salaries, fringe benefits including medical/dental insurance, retirement and housing subsidies.
The faculty recruitment will continue until the positions are filled. The shortlisted candidates will be invited for an on-site interview.
Please visit our website to apply: http://talent.sustc.edu.cn/en/. All applications should include a CV and a detailed list of publications with Research ID. Those interested in cluster hiring should send CVs and publication lists with Research ID as a group. Evaluations will commence immediately and appointments will be made on a continuous basis. Additional information on SUSTC is available on the University homepage http://sustc.edu.cn/.
Qualified applicants are also encouraged to apply for the Recruitment Program of Global Expert ("Thousand Talents Program") through SUSTC. Successful applicants will get extra research fund and living allowance from the government. Additional information is available through email inquiry or http://talent.sustc.edu.cn/.
If you have any questions, please feel free to contact us at firstname.lastname@example.com.
For the website of Department of Chemistry: http://sustc.edu.cn//cn/faculty/chemistry/
© Copyright 2015 Internet Employment Linkage, Inc.


text:
I am using ruby mechanize to submit form. When I submit form results are opened in new tab.I don't how to get contents of new tab opened. Please anyone help me to get content of new tab opened using mechanize. I also did google but I didn't get much help. Please help me... Thank you
Take the 2-minute tour ×
Stack Overflow is a question and answer site for professional and enthusiast programmers. It's 100% free.
I don't see what's special about submitting a form and being taken to a new page, whether it's in the same tab or not. A concept of a tab is typically defined by web browser (think Firefox or Chrome). If you're using Mechanize, you're not really using a web browser.
The example from Mechanize's guide explains it:
Submitting a form returns a bunch of HTML, whether that is a new "page" or a new "tab"
To view the page you can pretty print:


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January 11: UPCoM-Index Dips another Day on Week Trading
The UPCoM-Index, the measure of 131 unlisted public companies, closed slightly lower for another day – the fourth day in a row – as investors lost interest in equity assets.
The index lost 0.05 points, or 0.15 percent, to settle at 33.37.
Among index members, 9 rallied, 15 tumbled, and 106 closed unmoved. Up to 101 stocks closed untraded.
The market volume totalled 57,000 shares valued at 170 million dong, compared with 6.3 million shares and 314 billion dong from a day earlier.
IN4 was the biggest gainer, climbing nearly 10 percent to finish at 5,600 dong on a trade of 100 shares.
In the downswing, ND2 was the biggest loser, erasing 10 percent to close at 3,600 dong on a trade of 100 units.
NOS was the most active stock on the gauge with 15,000 shares changed hands, which closed flat at 2,000 dong.
Foreigners did not trade any shares today.
Category: Stocks


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One day, I'm gonna get around to trying.....
What is your list of 5 ingredients/ dishes that you just have never gotten aroudn to trying ever? Not necessariy because it's a rarity ingredient or cost/location prohibitve but just simply a "someday I'll get around to it" thing
Mine list (no particular order):
dragon fruit
pad thai
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