Extraction and separation technology of aniseed shikimic acid(專利)

Extraction and separation technology of aniseed shikimic acid

Patent Number(s): CN100999461-A
Inventor(s): MIN Y, LIU W, YANG J
Patent Assignee(s) and Codes(s):HONGHE INST (HONG-Non-standard)
Derwent Primary Accession Number: 2008-A50137 [04]
Abstract: NOVELTY - The invention claims an extraction and separation technology of aniseed shikimic acid. Its main steps are to degrease the dry crashed aniseed at 40~45 centigrade, 25~35 MPa through supercritical carbon dioxide to get edible flavor; leaching extract by heating and refluxing at 50~60 centigrade through carbinol after degreasing; extracting at 50~55 centigrade through ethyl acetate and then filtering and separating ethyl acetate to get solid extract; adding carbinol at 50~60 centigrade, heating and churning up until extract dissolves and then filtering, placing the filtered liquid still and cooling to get crystal-the coarse shikimic acid; dissolving the coarse shikimic acid at 45~50 centigrade through mixed solvent of chloroform and carbinol, placing naturally, cooling crystal and then purifying to get purified product, whose purity is larger than 95%. The invention adopts supercritical carbon dioxide to degrease, so that the aniseed oil can be used as flavor and can be eaten directly, it has no harm to human body. This technology improves the use of aniseed, improves degreasing efficiency and reduces the effect of liposoluble ingredients to the later operation so that it improves the recovery rate.
Show Documentation Abstract
International Patent Classification: A61K-036/185; A61K-036/57; A61K-131/00; C07C-051/42; C07C-062/00; C07C-062/04
Derwent Class Code(s): B04 ; B05
Derwent Manual Code(s): B04-A08C2; B04-B01C1; B10-C04A; B11-B03
Patent Details:
Patent Number
Publ. Date
Main IPC
Week
Page Count
Language
CN100999461-A
18 Jul 2007
C07C-051/42
200804


Application Details:
CN100999461-A
CN10065617
13 Jan 2007
Priority Application Information and Date:
CN10065617
13 Jan 2007

膠原蛋白

膠原蛋白是人體的一種非常重要的蛋白質，主要存在於結締組織中。它具有很強的伸張能力，是韌帶和肌鍵的主要成份，膠原蛋白還是細胞外基質的主要組成成分。它使皮膚保持彈性，而膠原蛋白的老化，則使皮膚出現皺紋。膠原蛋白亦是眼睛角膜的主要成份，但以結晶形式組成。
構成膠原的肽鏈，其胺基酸序列非常有特色。首先，它富含甘氨酸和脯氨酸殘基，前者的含量達到總胺基酸殘基的1/3後者則接近1/4；其次，序列中含有不由DNA鹼基三聯密碼子編碼的羥賴氨酸和羥脯氨酸，這兩種胺基酸是在蛋白質一級結構序列形成之後由特定的酶作用於序列中的賴氨酸和脯氨酸形成的；最後，它的序列中只含有很少的酪氨酸殘基;並且不含有色氨酸和半胱氨酸殘基。膠原蛋白一級結構的另一個特點是它的胺基酸的排列。這些胺基酸一般以-甘氨酸-脯氨酸-羥脯氨酸-三聯交替出現的順序排列。只有很少的蛋白質有這樣規則的胺基酸排列。
在空間結構上，膠原蛋白顯示出特殊的三股螺旋纏繞的結構，三條相互獨立的膠原蛋白肽鏈依靠甘氨酸之間形成的氫鍵維繫三股螺旋相互纏繞的結構。膠原蛋白肽鏈的三股螺旋結構不同於普通的α螺旋結構，它的螺距更大，但每一圈螺旋所包含的胺基酸殘基數卻很小，僅為3.3個，因此膠原蛋白的三股螺旋顯得細而長，螺旋中間的空間很小，僅能容納一個氫原子，只有甘氨酸能夠勝任這個位置。另外脯氨酸所特有的肽平面夾角也是形成這種特殊螺旋結構的必須因素。這也是膠原蛋白肽鏈中-甘氨酸-脯氨酸-羥脯氨酸-三聯序列交替出現的原因。膠原蛋白這種特殊的三股螺旋結構保證了它的機械強度。這種三股螺旋被稱為原膠原。
若干個原膠原橫向堆積，序列中所含有的羥賴氨酸和羥脯氨酸側鏈在酶作用下氧化生成醛，相互之前發生羥醛縮合反應形成原膠原之間的共價連結，這種結構被稱為膠原微纖維。許多膠原微纖維橫向堆積，以相同的方式通過共價鍵連結，形成膠原纖維。膠原纖維是膠原蛋白行使生理作用的基本形態，在生物體內膠原纖維交織成富有機械強度合彈性的網狀結構成為結締組織最基本的組成成分。
目前膠原蛋白是非常受到歡迎的保健美容品，使用範圍以整型醫學、營養輔助品、保養品為三大主流，也就是以注射、口服、擦拭為應用。
而其中以注射效果最好但價格昂貴，擦拭則因分子量太大而無法吸收，因此目前較為熱門的是水解過的口服膠原蛋白，不但價格適中且效果好，市面上知名的有台鹽、珍寶三旺、芳珂、金牌、白蘭氏，注射的則有雙美等廠商。
事實上口服的膠原蛋白會受到胃酸破壞，無法吸收，所以口服的膠原蛋白其實對於皮膚的幫助不大，想要皮膚能夠產生膠原蛋白的話，就必須要刺激皮膚表面，讓身體自行生成膠原蛋白，才會有效，目前來說，塗抹左旋Ｃ是副作用最小的方式。
但也有說法指出膠原蛋白是品質較差的蛋白質來源，因為它們沒有全部的必需胺基酸-也就是說它們並不是完全蛋白質(complete protein)。業者聲稱口服膠原蛋白食品能達到改善皮膚、指甲或關節的美容保健功效，但是這個說法並沒有得到任何主流研究結果的支持。通常這些部位有問題的人，比較有可能是因為其他因素造成的，而不是因為飲食中缺乏蛋白質的關係。就算是因為缺乏蛋白質的緣故，蛋白質也能夠由其他較佳的食物來源獲得。
http://zh.wikipedia.org/wiki/%E8%86%A0%E5%8E%9F%E8%9B%8B%E7%99%BD

冷壓油

揭開冷壓油的神秘面紗www.sesameoil.com.tw
揭開冷壓油的神秘面紗元福麻油廠www.sesameoil.com.tw隨著健康概念的興起，近來各種食材也吹起養生風，平日與大家息息相關的食用油也不例外，因此，”冷壓油”成了時髦的火紅商品，然而, 究竟何謂冷壓油？有何益處？有何差別？ 相信這是許多人心中共同的疑問 本文將針對此議題深入探討之。傳統的煉油術不外乎以下五種方式：
一. 南方壓榨法（中國傳統製油法）流程： 篩選清洗→烘焙翻炒→磨碎 →壓榨 → 靜置 → 第一次過濾 → 精密過濾 → 靜置沈澱 → 裝瓶1. 篩選清洗：去除砂土、塵埃、枝葉…等雜質異物。2. 烘焙翻炒：蒸發原料含的水份，以烘焙產生油品特有香味。3. 磨碎：破壞原料細胞膜，以促進提油之製程。4. 壓榨：利用自動化機械壓榨油脂。5. 靜置沈澱：放置於沉澱桶中使雜質沉澱。6. 過濾：去除油中之殘餘雜質，使油品純粹。 7. 7. 裝瓶 : 裝入消毒後之瓶子。二. 北方水洗法（中國傳統製油法）生產方式是原料經過烘培、磨醬、用熱水均勻快速攪拌後，置於鍋中旋動讓油浮出表面，取油靜置，再過濾而成。其原理是利用油和水的不同比重 ，水被原料中的親水物質吸收而取代出油，油浮在表面，相當於油經過了“水洗”過程而去掉了雜質和異味，整個過程稱之為水洗法。三. 溶劑法油是利用溶劑將油萃取出來，再將溶劑蒸發，剩下油的部份，這樣的產率就比傳統用擠壓的方式還高。但是某些維生素可能會因蒸發時的加熱而破壞。四. 連續式螺旋壓榨法使用連續式螺旋壓榨的時期比水壓式晚，典型的連續螺旋壓榨須具備兩個條件，1.需有充足的原料貯量以供應機械持續操作，避免提油中斷。2.需先除去原料中的雜質、砂粒，避免影響油脂品質與油粕成份，並減少機械摩擦損耗。一般螺旋壓榨的原料處理，可分為去皮殼與保留皮殼兩種，螺旋壓榨前須先將油籽原料翻動或捏碎果實，以便打破其均勻而堅實的細胞壁，增加提油效率，更使原料蒸煮均勻以提高油脂品質。五.水壓式壓榨法本法通常應用在批式壓榨，是最古老的提油方式之一，其原理是利用水之壓力搾出原料中之油脂。水壓式壓榨可分為開放式與密閉式兩種，兩種方式之區別在於開放式僅需將含油原料裹固在壓榨布袋內即可，而密閉式則除布袋裹固原料外，還加一成密閉箱。開放式又分板式與箱式兩種，板式壓榨法是將裹有原料之布袋至於板面之間，而在其板面上加上凸起之皺摺紋路或鋪上一層毛墊以便於油之流動與排出。箱式壓榨乃將原料直接放入其長方形的箱式壓榨盒中，免去了濾袋包裹原料的麻煩（其盒子底部之表面是以摺狀多孔之格架形式組成，而上層板面則呈角形，板面由上往下壓，搾出之油流到底部，在排出收集。密閉式壓榨使用具有多孔之鋼製容器，將原料裝載固定在裡面，因此節省許多使用濾布壓榨的麻煩，此外，就使用之壓力而言，密閉式比開放式高，亦即密閉式壓榨可以得到較高的榨油率。
而所謂的冷壓法 即是採取第一種技術-壓榨法，在”烘焙翻炒”這個步驟，有低溫、中溫與高溫三種，一般製油廠會憑藉其經驗，來決定烘炒的溫度與時間。 而所謂的冷壓，是以小火焙炒，經過磨碎，低溫壓榨萃取油、過濾、靜置、再過濾後充填包,過程其實與傳統方式大同小異，只是溫度控制的較低而已，所以，有標榜冷壓的油，就是在強調其富含維生素，而且沒有溶劑殘留的疑慮。
附錄 【麻油相關文獻】 胡麻油，即芝麻油。漢使張騫始自大宛得油麻種來，故名「胡麻」。胡麻自古常用為滋補、補肝腎、補肺、潤五臟，堅筋骨、 添精髓、明耳目、烏髭髮，逐風濕氣。民間世俗最常用於坐月子，產婦滋養， 食補首選「麻油雞」。對於產後諸虛提供熱量來源，驅風（產婦生產時，氣血大量流失，血虛氣虛最易 招風）益肝，養血益精， 益氣力、潤燥、通便、潤腸、堅筋骨。胡麻油熬膏外敷，能滋養、潤滑表皮細胞、涼血、解毒、療瘡、生肌止痛。 【苦茶油相關文獻】 苦茶油含有豐富之蛋白質、 維生素A、E等，其營養價值及對高溫的安定性均優與於黃豆油，甚至可與橄欖油相媲美。苦茶油更是單元不飽和脂肪酸含量最豐富之食用油，不僅對降低血中膽固醇、預防心血管疾病有很大的功效，根據研究顯示，其單元不飽和脂肪酸主要由油酸(Oleic Acid)、亞油酸(Linoleic Acid)組成，加熱時不易產生油煙，具相當的穩定，性質接近橄欖油。另苦茶油含有豐富的山茶柑素，可潤肺、清肝解毒、整腸健胃等營養價值高，為一健康之高級食用油。根據研究顯示，幽門螺旋桿(Helicobacter pylori)會引起胃潰瘍、消化不良及十二指腸潰瘍等消化性疾病，而高達85%~90%之潰瘍疾病都與幽門螺旋桿菌之感染有關。國科會專題研究「苦茶油抗菌因素研究(Study on antimicrobial factors of Camellia oil)*」(86年5月)，結論是苦茶油及苦茶渣之萃取及純化物對幽門螺旋桿菌具有抗菌作用，證實了傳說中苦茶油對胃疾之紓緩。

綠咖啡豆萃取--綠原酸(Chlorogenic Acid)

一項在歐美地區經過長達10年20多萬人數研究統計顯示，每天喝超過七杯咖啡的人比低於二杯的人，罹患第二糖尿病的機會低於50%，且血糖濃度也較低。
綠原酸(chlorlgenic Acid)存在於咖啡豆中，在未經烘培的咖啡豆中含量高達45%以上，而經過烘培的咖啡豆僅存5~10%。
綠原酸的功用
1.阻止小腸吸收 葡萄糖。
2.阻止肝糖酵素釋放葡萄糖進入血液。
3.幫助脂肪燃燒，提供能量給肌肉
4.減少胰島素的需求
以上的功能可以想像，對肥胖者的幫助，能將脂肪組織燃燒掉，因此在調整BMI值有顯著的效果。在臨床試驗中，連續服用六週後，BMI值平均減少6%，肌肉/脂肪比例提升4%。
綠原酸主要存在於綠咖啡豆中，但咖啡所含的咖啡因的成癮性和對身體的危害是不容忽視。經過特殊萃取技術，能使咖啡因的含量低於2%，咖啡豆中所含有毒二萜類(會引發心血管疾病)大幅降低至2PPM以下。
資料來源：http://tw.myblog.yahoo.com/f29801235/article?mid=492&prev=509&next=481

Dibenzothiophene

Dibenzothiophene
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Dibenzothiophene

IUPAC name Dibenzothiophene
Other names Diphenylene sulfide

Identifiers
CAS number 132-65-0
RTECS number HQ3490550

Properties
Molecular formula C12H8S
Molar mass 184.26 g/mol
Appearance Colourless crystals
Density ? g/cm3
Melting point 97-100 °C(lit.)
Boiling point 332-333 °C
Solubility in water insol.
Solubility in other solvents benzene and related

Hazards
Main hazards flammable
R-phrases 22
S-phrases 36

Related compounds
Related compounds Thiopheneanthracenebenzothiophene

Except where noted otherwise, data are given formaterials in their standard state(at 25 °C, 100 kPa)Infobox references


Dibenzothiophene is the organic compound consisting of two benzene rings fused to a central thiophene ring. This tricyclic heterocycle, and especially its alkyl substituted derivatives occur widely in heavier fractions of petroleum.
Dibenzothiophene is prepared by the reaction of biphenyl with sulfur dichloride in the presence of aluminium trichloride.

http://en.wikipedia.org/wiki/Dibenzothiophene

Hydrodesulfurization

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Hydrodesulfurization (HDS) is a catalytic chemical process widely used to remove sulfur (S) from natural gas and from refined petroleum products such as gasoline or petrol, jet fuel, kerosene, diesel fuel, and fuel oils.[1][2] The purpose of removing the sulfur is to reduce the sulfur dioxide (SO2) emissions that result from using those fuels in automotive vehicles, aircraft, railroad locomotives, ships, gas or oil burning power plants, residential and industrial furnaces, and other forms of fuel combustion.
Another important reason for removing sulfur from the naphtha streams within a petroleum refinery is that sulfur, even in extremely low concentrations, poisons the noble metal catalysts (platinum and rhenium) in the catalytic reforming units that are subsequently used to upgrade the octane rating of the naphtha streams.
The industrial hydrodesulfurization processes include facilities for the capture and removal of the resulting hydrogen sulfide (H2S) gas. In petroleum refineries, the hydrogen sulfide gas is then subsequently converted into byproduct elemental sulfur. In fact, the vast majority of the 64,000,000 metric tons of sulfur produced worldwide in 2005 was byproduct sulfur from refineries and other hydrocarbon processing plants.[3][4]
An HDS unit in the petroleum refining industry is also often also referred to as a Hydrotreater.
History
Although reactions involving catalytic hydrogenation of organic substances were known prior to 1897, the property of finely divided nickel to catalyze the fixation of hydrogen on hydrocarbon (ethylene, benzene) double bonds was discovered by the French chemist, Paul Sabatier.[5][6] Thus, he found that unsaturated hydrocarbons in the vapor phase could be converted into saturated hydrocarbons by using hydrogen and a catalytic metal. His work was the foundation of the modern catalytic hydrogenation process.
Soon after Sabatier's work, a German chemist, Wilhelm Normann, found that catalytic hydrogenation could be used to convert unsaturated fatty acids or glycerides in the liquid phase into saturated ones. He was awarded a patent in Germany in 1902[7] and in Britain in 1903,[8] which was the beginning of what is now a worldwide industry.
In the mid-1950's, the first noble metal catalytic reforming process (the Platformer process) was commercialized. At the same time, the catalytic hydrodesulfurization of the naphtha feed to such reformers was also commercialized. In the decades that followed, various proprietary catalytic hydrodesulfurization processes such as the one depicted in the flow diagram below have been commercialized. Currently, virtually all of the petroleum refineries world-wide have one or more HDS units.
By 2006 miniature microfluidic HDS units had been implemented for treating JP-8 jet fuel to produce clean feed stock for a fuel cell hydrogen reformer.[9] By 2007 this had been integrated into an operating 5kW fuel cell generation system.[10]

The process chemistry
Hydrogenation is a class of chemical reactions in which the net result is the addition of hydrogen (H). Hydrogenolysis is a type of hydrogenation and results in the cleavage of the C-X chemical bond, where C is a carbon atom and X is a sulfur, nitrogen (N) or oxygen (O) atom. The net result of a hydrogenolysis reaction is the formation of C-H and H-X chemical bonds. Thus, hydrodesulfurization is a hydrogenolysis reaction. Using ethanethiol (C2H5SH), a sulfur compound present in some petroleum products, as an example, the hydrodesulfurization reaction can be simply expressed as
Ethanethiol + Hydrogen → Ethane + Hydrogen sulfide
C2H5SH + H2 → C2H6 + H2S
For the mechanistic aspects of, and the catalysts used in this reaction see the section catalysts and mechanisms

Process description
In an industrial hydrodesulfurization unit, such as in a refinery, the hydrodesulfurization reaction takes place in a fixed-bed reactor at elevated temperatures ranging from 300 to 400 °C and elevated pressures ranging from 30 to 130 atmospheres of absolute pressure, typically in the presence of a catalyst consisting of an alumina base impregnated with cobalt and molybdenum.
The image below is a schematic depiction of the equipment and the process flow streams in a typical refinery HDS unit.

Schematic diagram of a typical Hydrodesulfurization (HDS) unit in a petroleum refinery
The liquid feed (at the bottom left in the diagram) is pumped up to the required elevated pressure and is joined by a stream of hydrogen-rich recycle gas. The resulting liquid-gas mixture is preheated by flowing through a heat exchanger. The preheated feed then flows through a fired heater where the feed mixture is totally vaporized and heated to the required elevated temperature before entering the reactor and flowing through a fixed-bed of catalyst where the hydrodesulfurization reaction takes place.
The hot reaction products are partially cooled by flowing through the heat exchanger where the reactor feed was preheated and then flows through a water-cooled heat exchanger before it flows through the pressure controller (PC) and undergoes a pressure reduction down to about 3 to 5 atmospheres. The resulting mixture of liquid and gas enters the gas separator vessel at about 35 °C and 3 to 5 atmospheres of absolute pressure.
Most of the hydrogen-rich gas from the gas separator vessel is recycle gas which is routed through an amine contactor for removal of the reaction product H2S that it contains. The H2S-free hydrogen-rich gas is then recycled back for reuse in the reactor section. Any excess gas from the gas separator vessel joins the sour gas from the stripping of the reaction product liquid.
The liquid from the gas separator vessel is routed through a reboiled stripper distillation tower. The bottoms product from the stripper is the final desulfurized liquid product from hydrodesulfurization unit.
The overhead sour gas from the stripper contains hydrogen, methane, ethane, hydrogen sulfide, propane and perhaps some butane and heavier components. That sour gas is sent to the refinery's central gas processing plant for removal of the hydrogen sulfide in the refinery's main amine gas treating unit and through a series of distillation towers for recovery of propane, butane and pentane or heavier components. The residual hydrogen, methane, ethane and some propane is used as refinery fuel gas. The hydrogen sulfide removed and recovered by the amine gas treating unit is subsequently converted to elemental sulfur in a Claus process unit.
Note that the above description assumes that the HDS unit feed contains no olefins. If the feed does contain olefins (for example, the feed is a naphtha derived from a refinery fluid catalytic cracker (FCC) unit), then the overhead gas from the HDS stripper may also contain some ethene, propene, butenes and pentenes or heavier components.
It should also be noted that the amine solution to and from the recycle gas contactor comes from and is returned to the refinery's main amine gas treating unit.

Sulfur compounds in refinery HDS feedstocks
The refinery HDS feedstocks (naphtha, kerosene, diesel oil and heavier oils) contain a wide range of organic sulfur compounds, including thiols, thiophenes, organic sulfides and disulfides, and many others. These organic sulfur compounds are products of the degradation of sulfur containing biological components, present during the natural formation of the fossil fuel, petroleum crude oil.
When the HDS process is used to desulfurize a refinery naphtha, it is necessary to remove the total sulfur down to the parts per million range or lower in order to prevent poisoning the noble metal catalysts in the subsequent catalytic reforming of the naphthas.
When the process is used for desulfurizing diesel oils, the latest environmental regulations in the United States and Europe, requiring what is referred to as ultra-low sulfur diesel (ULSD), in turn requires that very deep hydrodesulfurization is needed. In the very early 2000's, the governmental regulatory limits for highway vehicle diesel was within the range of 300 to 500 ppm by weight of total sulfur. As of 2006, the total sulfur limit for highway diesel is in the range of 15 to 30 ppm by weight.[11]

Thiophenes
A family of substrates that are particularly common in petroleum are the aromatic sulfur-containing heterocycles called thiophenes. Many kinds of thiophenes occur in petroleum ranging from thiophene itself to more condensed derivatives called benzothiophenes and dibenzothiophenes. Thiophene itself and its alkyl derivatives are easier to hydrogenolyse, whereas dibenzothiophene, especially its 4,6-disubstituted derivatives, are considered the most challenging substrates. Benzothiophenes are midway between the simple thiophenes and dibenzothiophenes in their susceptibility to HDS.

Catalysts and mechanisms
The main HDS catalysts are based on MoS2 together with smaller amounts of other metals.[12] The nature of the sites of catalytic activity remains an active area of investigation, but it is generally assumed basal planes of the MoS2 structure are not relevant to catalysis, rather the edges or rims of these sheet.[13] At the edges of the MoS2 crystallites, the molybdenum centre can stabilize a coordinatively unsaturated site (CUS), also known as an anion vacancy. Substrates, such as thiophene, bind to this site and undergo a series a reactions that result in both C-S scission and C=C hydrogenation. Thus, the hydrogen serves multiple roles - generation of anion vacancy by removal of sulfide, hydrogenation, and hydrogenolysis. A simplified diagram for the cycle is shown:

Simplified diagram of a HDS cycle for thiophene

Catalysts
Most metals catalyse HDS, but it is those at the middle of the transition metal series that are most active. Ruthenium disulfide appears to be the single most active catalyst, but binary combinations of cobalt and molybdenum are also highly active.[14] Aside from the basic cobalt-modified MoS2 catalyst, nickel and tungsten are also used, depending on the nature of the feed. For example, Ni-W catalysts are more effective for hydrodenitrification (HDN).

Supports
Metal sulfides are "supported" on materials with high surface areas. A typical support for HDS catalyst is γ-alumina. The support allows the more expensive catalyst to be more widely distributed, giving rise to a larger fraction of the MoS2 that is catalytically active. The interaction between the support and the catalyst is an area of intense interest, since the support is often not fully inert but participates in the catalysis.

Other uses
The basic hydrogenolysis reaction has a number of uses other than hydrodesulfurization.

Hydrodenitrogenation
The hydrogenolysis reaction is also used to reduce the nitrogen content of a petroleum stream and, in that case, is referred to Hydrodenitrogenation (HDN). The process flow scheme is the same as for an HDS unit.
Using pyridine (C5H5N), a nitrogen compound present in some petroleum fractionation products, as an example, the hydrodenitrogenation reaction has been postulated as occurring in three steps:[15][16]
Pyridine + Hydrogen → Piperdine + Hydrogen → Amylamine + Hydrogen → Pentane + Ammonia
C5H5N + 5H2 → C5H11N + 2H2 → C5H11NH2 + H2 → C5H12 + NH3
and the overall reaction may be simply expressed as:
Pyridine + Hydrogen → Pentane + Ammonia
C5H5N + 5H2 → C5H12 + NH3
Many HDS units for desulfurizing naphthas within petroleum refineries are actually simultaneously denitrogenating to some extent as well.

Saturation of olefins
The hydrogenolysis reaction may also be used to saturate or convert olefins (alkenes) into paraffins (alkanes). The process used is the same as for an HDS unit.
As an example, the saturation of the olefin, pentene, can be simply expressed as:
Pentene + Hydrogen → Pentane
C5H10 + H2 → C5H12
Some hydrogenolysis units within a petroleum refinery or a petrochemical plant may be used solely for the saturation of olefins or they may be used for simultaneously desulfurizing as well as denitrogenating and saturating olefins to some extent.

Hydrogenation in the food industry
Further information: Hydrogenation, Wilhelm Normann, and Trans fat
The food industry uses hydrogenation to completely or partially saturate the unsaturated fatty acids in liquid vegetable fats and oils to convert them into solid or semi-solid fats, such as those in margarine and shortening.

Desulfurization technology research
Hundreds of research publications appear annually on HDS technologies. Illustrative of the range of ideas being discussed are reports on ultrasonically assisted desulfurization.[17]

See also
Timeline of hydrogen technologies

References
^ Gary, J.H. and Handwerk, G.E. (1984). Petroleum Refining Technology and Economics (2nd Edition ed.). Marcel Dekker, Inc. ISBN 0-8247-7150-8.
^ Hydrodesulfurization Technologies and Costs Nancy Yamaguchi, Trans Energy Associates, William and Flora Hewlett Foundation Sulfur Workshop, Mexico City, May 29-30, 2003
^ Sulfur production report by the United States Geological Survey
^ Discussion of recovered byproduct sulfur
^ C.R.Acad.Sci. 1897, 132, 210
^ C.R.Acad.Sci. 1901, 132, 210
^ DE Patent DE141029 (Espacenet, record not available)
^ UK Patent GB190301515 GB190301515 (Espacenet)
^ Microchannel HDS (March 2006)
^ Fuel cells help make noisy, hot generators a thing of the past (December 2007) Pacific Northwest National Laboratory
^ Diesel Sulfur published online by the National Petrochemical & Refiners Association (NPRA)
^ Topsøe, H.; Clausen, B. S.; Massoth, F. E., Hydrotreating Catalysis, Science and Technology, Springer-Verlag: Berlin, 1996.
^ Daage, M.; Chianelli, R. R., "Structure-Function Relations in Molybdenum Sulfide Catalysts - the Rim-Edge Model", J. of Catalysis, 1994, 149, 414-427.
^ Chianelli, R. R.; Berhault, G.; Raybaud, P.; Kasztelan, S.; Hafner, J. and Toulhoat, H., "Periodic trends in hydrodesulfurization: in support of the Sabatier principle", Applied Catalysis, A, 2002, volume 227, pages 83-96
^ Kinetics and Interactions of the Simultaneous Catalytic Hydrodenitrogenation of Pyridine andHydrodesulfurization of Thiophene(John Wilkins, PhD Thesis, MIT, 1977)
^ Simultaneous Catalytic Hydrodenitrogenation of Pyridine and Hydrodesulfurization ofThiophene(Satterfield,C.N., Modell, M. and Wilkens, J.A., Ind. Eng. Chem. Process Des. Dev., 1980 Vol. 19, pages 154-160)
^ Deshpande, A., Bassi, A., Prakash, A. (2004) "Ultrasound-Assisted, Base-Catalyzed Oxidation of 4,6-Di­methyl­di­ben­zothio­phene in a Bi­phasic Diesel-Aceto­nitrile System" Energy Fuels, 19 (1), 28 -34, 2005.

External links
Albemarle Catalyst Company (Petrochemical catalysts supplier)
UOP Company (Engineering design and construction of large-scale, industrial HDS plants)
Mustang Engineering Company (Description and flow diagram of an HDS unit, from an article published in the Oil & Gas Journal)
Hydrogenation for Low Trans and High Conjugated Fatty Acids by E.S. Jang, M.Y. Jung, D.B. Min, Comprehensive Reviews in Food Science and Food Safety, Vol.1, 2005
Oxo Alcohols (Engineered and constructed by Aker Kvaerner)
Catalysts and technology for Oxo-Alcohols
http://en.wikipedia.org/wiki/Hydrodesulfurization

Pervaporation

Pervaporation is a method for the separation of mixtures of liquids by partial vaporization through a non-porous or porous membrane.

Contents
1 Theory
2 Applications
3 External links
4 References


Theory
The name of this membrane-based process is derived from the two basic steps of the process, firstly the permeation through the membrane by the permeate, then its evaporation into the vapor phase. This process is used by a number of industries for several different processes, including purification and analysis, due to its simplicity and in-line nature.
The membrane acts as a selective barrier between the two phases, the liquid phase feed and the vapor phase permeate. It allows the desired component(s) of the liquid feed to transfer through it by vaporization. Separation of components is based on a difference in transport rate of individual components through the membrane.
Typically, the upstream side of the membrane is at ambient pressure and the downstream side is under vacuum to allow the evaporation of the selective component after permeation through the membrane. Driving force for the separation is the difference in the partial pressures of the components on the two sides and not the volatility difference of the components in the feed.
The driving force for transport of different components is provided by a chemical potential difference between the liquid feed/retentate and vapor permeate at each side of the membrane. The retentate is the remainder of the feed leaving the membrane feed chamber, which is not permeated through the membrane. The chemical potential can be expressed in terms of fugacity, given by Raoult's law for a liquid and by Dalton's law for (an ideal) gas. It should be noted that during operation, due to removal of the vapor-phase permeate, the actual fugacity of the vapor is lower than anticipated on basis of the collected (condensed) permeate.
Separation of components (e.g. water and ethanol) is based on a difference in transport rate of individual components through the membrane. This transport mechanism can be described using the solution-diffusion model, based on the rate/ degree of dissolution of a component into the membrane and its velocity of transport (expressed in terms of diffusivity) through the membrane, which will be different for each component and membrane type leading to separation.

Applications
Pervaporation is effective for diluting solutions containing trace or minor amounts of the component to be removed. Based on this, hydrophilic membranes are used for dehydration of alcohols containing small amounts of water and hydrophobic membranes are used for removal/recovery of trace amounts of organics from aqueous solutions. Hydrophobic membranes are often PDMS based where the actual separation mechanism is based on the solution-diffusion model described above.
A relatively new membrane in the field of hydrophilic membranes is the ceramic membrane with the actual separation layer being made of amorphous silica. This is in fact a membrane which is porous, with pores ranging around 4 Å, large enough to let water molecules pass through and retain any other solvents that have a larger molecular size such as ethanol. Recent novell hydrophilic ceramic membranes can also be based on titania or zirconia.
Pervaporation is a very mild process and hence very effective for separation of those mixtures which can not survive the harsh conditions of distillation.
Solvent Dehydration: dehydrating the ethanol/water and isopropanol/water azeotropes
Continuous water removal from condensation reactions such as esterifications to enhance conversion and rate of the reaction.
Membrane introduction mass spectrometry
Removing organic solvents from industrial waste waters.
Combination of distillation and pervaporation/vapour permeation
Recently, a number of organophilic Pervaporation membranes have been introduced to the market. Organophilic Pervaporation membranes can be used for the separation of organic-organic mixtures, e.g.:
Reduction of the aromatics content in refinery streams
Breaking of azeotropes
Purification of extraction media
Purification of product stream after extraction
Purification of organic solvents

External links
http://www.membrane-guide.com/membrane_separation/pervaporation/pervaporation_europe.htm suppliers, products, news and facts for engineers involved in the design or the operation of pervaporation systems.
Technology of pervaporation Pervaporation with ceramic membranes
[1] Environmental Importance & as a Green Chemistry solution.

This chemistry article is a stub. You can help Wikipedia by expanding it.

References
Fontalvo Alzate, Javier (2006). Design and performance of two-phase flow pervaporation and hybrid distillation process.. Technische Universiteit Eindhoven, The Netherlands: JWL boekproducties. ISBN 978-90-386-3007-6.
Matuschewski, Heike (2008). MSE — modified membranes in organophilic pervaporation for aromatics/aliphatics separation.. www.desline.com: Desalination.
Retrieved from "http://en.wikipedia.org/wiki/Pervaporation"

http://en.wikipedia.org/wiki/Pervaporation

BASF to present BASIL™ ionic liquid process at technology transfer forum

BASF to present BASIL™ ionic liquid process at technology transfer forum'Smart' process improves yields, economics of chemical operations
MOUNT OLIVE, N.J., May 10, 2004 -- Dr. Uwe Vagt, New Business Development, for BASF's Intermediates Division in Ludwigshafen, Germany, will present BASF's proprietary BASIL technology that utilizes ionic liquids to improve chemical operations on a commercial scale. The presentation will be at 9:30 a.m., on Monday, May 10, 2004, at the 21st Annual International Technology Transfer Forum, hosted by Technology Catalysts, at the Hyatt Regency Reston Town Center in Reston, Va.
BASF's BASIL (Biphasic Acid Scavenging utilizing Ionic Liquids) "smart" process technology economically solves several chemical processing problems associated with acid production during some chemical reactions.
Many organic chemical processes, such as esterifications, produce byproduct acids that must be scavenged in order to prevent decomposition of the primary reaction product, or to prevent unwanted side-reactions. To address this problem, tertiary amines, such as triethylamine, are typically added to the reaction mixture, resulting in the production of a solid ammonium salt. This solid presents a host of problems, including reduction of heat transfer and reaction rates, reduction of yields, and solids separation.
The BASIL process economically avoids the problems resulting from solids generation by making use of ionic liquids to scavenge acids. Instead of using a tertiary amine, a 1-alkylimidazole is used to scavenge acids produced. As the imidazole reacts with the acid, an alkylimidazolium salt is formed which is an ionic liquid at the reaction temperature. As a liquid, the alkylimidazolium salt can be easily removed by a liquid-liquid phase separation. In addition, economic reclamation of the 1-alkylimidazole through deprotonation is possible.
Ionic liquid technology provides the added advantage of having the alkylimidazole act as a nucleophilic catalyst, thereby improving reaction rates, and increasing yields and selectivities.
BASF representatives will be available throughout the technology transfer forum to answer questions and discuss potential licenses for this innovative technology.
Details about the Technology Catalysts 21st Annual International Technology Transfer Forum can be found at http://www.technology-catalysts.com//.
BASF - The Chemical Company. We don't make a lot of the products you buy. We make a lot of the products you buy better.®BASF Corporation, headquartered in New Jersey, is the North American affiliate of BASF AG, Ludwigshafen, Germany. We employ about 11,000 people in North America and had sales of approximately $9 billion in 2003. For more information about BASF's North American operations, or to sign up to receive news releases by e-mail, visit www.basf.com/usa.
BASF is the world's leading chemical company. Our goal is to grow profitably and further increase the value of our company. We help our customers to be more successful through intelligent system solutions and high-quality products. BASF's portfolio ranges from chemicals, plastics, performance products, agricultural products and fine chemicals to crude oil and natural gas. Through new technologies we can tap into additional market opportunities. We conduct our business in accordance with the principles of sustainable development. In 2003, BASF had sales of approximately $42 billion and over 87,000 employees worldwide. Further information on BASF is available on the Internet at http://www.basf.com/.
For more information, contact:Bill PaganoBASFTel: (973)426-2139E-mail: paganow@basf.com