以下，將提供本發明之較佳實施例的實施方式。應指出在實施例之實施方式中，為簡單及簡明起見，本說明書不可能詳細描述實際實施例之所有特徵。應理解在任何實施例之實務實施之過程中，如同在工程項目或設計項目之過程中，為了達成開發者之特定目標及滿足一些系統相關或企業相關之約束條件，通常將作出各種決策，其亦將在一實施例與另一實施例之間變化。此外，亦可理解儘管在此類開發過程中作出之努力可為複雜且耗時的，一些基於揭示於本發明中之技術內容之諸如設計、製造及生產的變化形式僅為與揭示於本發明中之內容相關聯之領域的普通技術人員在此項技術中的慣用技術手段，其不應視為本發明揭示內容不足。 除非另外定義，否則本申請專利範圍及本說明書所使用之所有技術或科學術語應具有與本發明所屬之領域的普通技術人員通常瞭解之相同意義。術語「一(a/an)」及其類似物並不表示數量之限制，但表示存在至少一個。術語「包含(comprises/comprising)」、「包括(includes/ including)」及其類似物意謂在「包含」、「包括」前面的元件或物體涵蓋在「包含」、「包括」之後的元件或物體及其圖示等效物，但並不排除其他元件或物體。 在本發明中，本發明者發現Ar在甲醇中之溶解度大於在其水中之溶解度。由此，在甲醇中降低氬含量對於在經由甲醇裂解器及PSA獲得之最終氫產物中減少氬含量係至關重要的。另一方面，本發明者發現在氮中Ar含量遠小於在空氣中。對於通常由低溫空氣分離方法產生之氮氣，Ar含量小於70 ppm (mol)而在空氣中Ar含量為0.934% (mol)。因此在特定溫度及特定壓力下，氮氣中之Ar分壓小於其在空氣中之0.75%，從而甲醇及水中之Ar溶解度可經由與氮氣接觸而顯著下降。 因此，本發明者出人意料地發現針對甲醇/水混合進料引入使用汽提氮之汽提塔可在甲醇/水混合進料中顯著降低氬至足夠低含量，使得在下游PSA單元中，可產生將符合關於氬之極高純度要求的H2
。 在本發明之一個實施例中，在經由甲醇裂解器及PSA獲得之氫氣中降低氬含量之方法，其中該方法之改進包含：在包含甲醇之進料流引入至甲醇裂解器中之前，使該進料流經歷使用包含氮之汽提氣的汽提塔方法。為了減少氫產物中之Ar含量及O2
含量，經歷汽提塔方法之進料流可包含甲醇與水之混合進料。 在本發明中，包含甲醇之進料流可購自Linde AG或外部供應商且儲存於甲醇槽中以供使用。在較佳實施例中，包含甲醇之進料流在使用之前以氮氣覆蓋。如上所述，處理氣體(PSA入口)中之Ar含量主要歸因於甲醇進料之變化而顯著變化，且污染資源係來自上游儲存及運輸，由此新鮮甲醇進料含有最高Ar含量。在甲醇進料經具有低Ar含量之氮氣覆蓋的情況下儲存若干天之後，用於MC及PSA入口氣體之甲醇進料中之Ar含量低得多，因為在0.3巴及環境溫度下甲醇中之Ar將與氮氣中之70 ppm Ar接近平衡。處理氣體中之Ar含量可下降至接近70 ppb。 在本發明之一個實施例中，本發明之汽提塔方法可在環境溫度下進行。詳言之，本發明之汽提塔方法可在自0℃至50℃之溫度、自5℃至45℃之溫度、自5℃至35℃之溫度、自10℃至45℃之溫度、自10℃至35℃之溫度、自15℃至25℃之溫度、自5℃至環境溫度之溫度或其間所有範圍及子範圍之溫度下進行。 在本發明之一個實施例中，包含水之進料流及包含甲醇之進料流在相同位置饋入汽提塔中。在某一具體實施例中，包含水之進料流可經引入至用於引入包含甲醇之進料流的管道中，隨後包含水之進料流與包含甲醇之進料流共同饋入汽提塔中。 在本發明之一個實施例中，包含水之進料流及包含甲醇之進料流可分開地饋入汽提塔中。在一較佳實施例中，包含水之進料流可自汽提塔頂部饋入汽提塔中。可替代地，包含水之進料流可於在包含甲醇之進料流饋入汽提塔中之位置上方的位置饋入汽提塔中。 在本發明之一個實施例中，在經由甲醇裂解器及PSA獲得之氫氣中降低氬含量之方法可包含：在包含甲醇之進料流引入至甲醇裂解器中之前，使該進料流經歷使用包含氫氣代替氮氣之汽提氣的汽提塔方法。在一較佳實施例中，在氫氣中降低氬含量之方法可進一步包含：在包含甲醇之進料流引入至甲醇裂解器中之前，使該進料流經歷使用包含氫之汽提氣的汽提塔方法。在一更佳實施例中，在氫氣中降低氬含量之方法可進一步包含：將離開PSA之氫氣之至少一部分再循環進入氮氣流中。 在本發明之一實施例中，氮氣流可包含低氬含量，諸如氬含量小於70 ppm mol，在1 ppm mol至50 ppm mol之範圍內，在5 ppm mol至50 ppm mol之範圍內，在10 ppm mol至40 ppm mol之範圍內，在20 ppm mol至35 ppm mol之範圍內，或在其間所有範圍及子範圍內。 與先前技術相比，本發明者出人意料地發現在本發明中，用於甲醇/水混合進料之汽提塔之引入可在甲醇/水混合進料中顯著降低氬至足夠低的含量，使得在下游PSA單元中，可生產將符合關於氬之極高純度要求(氫氣中之氬含量在按體積計小於70 ppb之範圍內)的H2
。 此外，因本發明中之汽提塔方法帶來的增加之成本遠低於使用以甲醇裂解器技術為基礎，且可降低Ar至70 ppb以下的現有技術，例如在MC(甲醇裂解器及PSA)或代替MC之改性水電解槽下游加入低溫TSA。 與使用低溫純化器、鈀膜等以純化H2
之替代方案相比，本發明中之方法顯著地較經濟(具成本效益)。使用改性水電解槽亦導致顯著較高之H2
成本，其由電力與諸如甲醇(或天然氣)之燃料相比相對較高之價格造成。 基於NG(天然氣)之蒸汽重組器(SMR)亦已經歷極大的問題(高營業損失=高成本)，尤其在臺灣及中國，其中天然氣進料亦混雜氬痕量(在ppm範圍內，通常在NG中30-60 ppmv)。在SMR之後的PSA方法在氬方面亦不符合H2
規格，除非方法極低效運行(亦即30-40%產物損失)。由於其極難(與任何已知技術相比在經濟上無競爭性)自NG分離氬，使用SMR技術自混雜氬之NG為電子氣體客戶生產氫氣並非新裝備之替代方案。現有SMR設備可在極低回收及高損失之情況下繼續運行。 此外，若在(不遠的)將來(具有甚至更薄的半導體層)，則H2
中氬之規格變得更嚴格(亦即＜10 ppbv)，則基於NG-SMR(後接PSA之天然氣-蒸汽甲烷重整器)之氫不再是可選方案且在氬痕量包含於NG中之情況下將完全不起作用。在NG中之Ar的問題亦可為全世界LNG設備/終端之數量逐漸增加的結果。NG經銷商可使用氮以調節(汽化)LNG之熱值以符合NG管道規格。但用於熱值調節之N2
通常不是高純度N2
而是亦含有氬。然而，藉由使用描述於本發明中之方法，氫氣中之氬含量可甚至降低至小於70 ppb、小於60 ppb、小於50 ppb、小於40 ppb、小於30 ppb、小於20 ppb、小於10 ppb、小於5 ppb或小於1 ppb之範圍。 在本發明之一個實施例中，氫氣中氬含量為介於自1 ppb至70 ppb、自5 ppb至70 ppb、自10 ppb至70 ppb、自20 ppb至70 ppb、自30 ppb至70 ppb、自40 ppb至70 ppb、自50 ppb至70 ppb、自60 ppb至70 ppb、自1 ppb 至60 ppb、自1 ppb至50 ppb、自1 ppb至40 ppb、自1 ppb至30 ppb、自5 ppb至60 ppb、自5 ppb至50 ppb、自5 ppb至40 ppb、自5 ppb至30 ppb、自10 ppb至60 ppb、自10 ppb至50 ppb、自10 ppb至40 ppb、自10 ppb至30 ppb之範圍及其間所有範圍及子範圍內。 在本發明之一個實施例中，氫氣中之O2
含量介於自1 ppb至70 ppb、自5 ppb至70 ppb、自10 ppb至70 ppb、自20 ppb至70 ppb、自30 ppb至70 ppb、自40 ppb至70 ppb、自50 ppb至70 ppb、自60 ppb至70 ppb、自1 ppb至60 ppb、自1 ppb至50 ppb、自1 ppb至40 ppb、自1 ppb至30 ppb、自5 ppb至60 ppb、自5 ppb至50 ppb、自5 ppb至40 ppb、自5 ppb至30 ppb、自10 ppb至60 ppb、自10 ppb至50 ppb、自10 ppb至40 ppb、自10 ppb至30 ppb之範圍及其間所有範圍及子範圍內。 一般而言，經由甲醇裂解器及PSA生產氫氣之方法可包含：(1)引入包含甲醇之進料至甲醇裂解器以形成主要包含氫氣、CO、CH4
及若干包括諸如二甲醚之副產物之重組分的混合氣體；及(2)引入混合氣體至PSA單元以提供氫產物。在一些實施例(如圖1中所展示)中，來自去礦物質水槽之水(去礦物質水或去離子水)進料與來自甲醇槽之甲醇進料混合以提供甲醇與水之混合進料，隨後將甲醇與水之混合進料引入至槽或脫氣器(例如，再循環桶)中。甲醇進料可由外部供應商及Linde自身提供。脫氣或未脫氣之混合進料隨後引入至甲醇裂解器中以提供包含氫氣之混合氣體。在通過水冷卻器、冷凝器(例如冷凝物桶)之後，將混合氣體引入至PAS單元中，從而提供H2
產物。關於經由甲醇裂解器及PSA通常製備H2
產物的細節在先前技術中已為吾人所知，其可以引用之方式併入本文中。 在本發明之一個實施例中，提供一種在經由甲醇裂解器及PSA獲得之氫氣中移除氬/降低氬含量的方法。在本發明之方法中，包含一種改進，其中在包含甲醇之進料流引入至甲醇裂解器中之前，進料流首先經歷使用包含氮之汽提氣的汽提塔方法。在一些實施例中，汽提氣亦可包含氫。 在一些實施例中，進料流可包含甲醇與水之混合進料。在一些實施例中，甲醇與水可混合且在相同位置饋入汽提塔中。在其他實施例中，甲醇與水可分開地饋入汽提塔中，其中水自汽提塔頂部分開地饋入至汽提塔中，或水在甲醇饋入汽提塔中之位置上方的位置饋入(如圖中3所示)。 如圖2中所示，水(去礦物質水或去離子水)進料與甲醇進料混合以提供甲醇與水之混合進料。隨後，甲醇與水之混合進料引入至汽提塔中。在一些實施例中，汽提塔亦可包含如通常使用之再循環桶，其中汽提塔位於再循環桶上方且與再循環桶流體連通。在汽提塔中，汽提氣(例如，氮氣)在汽提塔塔盤以下位置引入，且甲醇與水之混合進料在汽提塔塔盤上部位置引入。在離開汽提塔之後，甲醇與水之混合進料隨後引入至甲醇裂解器中以提供如圖1中所示之包含氫氣之混合氣體，從而提供高純度之H2
產物。在一些實施例中，氬在氫產物中之含量在按體積計小於70 ppb之範圍內。在一些較佳實施例中，氬在氫氣中之含量在按體積計小於70 ppb之範圍內；且O2
在氫氣中之含量在按體積計小於70 ppb之範圍內。 在一些實施例中，本發明之方法可進一步包含：使離開PSA單元之至少一部分氫再循環進入汽提塔，較佳進入氮氣流。詳言之，氫氣之至少一部分及氮氣流自汽提塔塔盤以下之位置引入，或引入至位於汽提塔下方之再循環桶中。在一些另外實施例中，進料流可包含甲醇與水之混合進料。在一些另外實施例中，甲醇與水可混合且在相同位置饋入汽提塔中。在其他實施例中，甲醇與水可分開地饋入汽提塔中，其中水自汽提塔頂部分開地饋入至汽提塔中，或水在甲醇饋入汽提塔中之位置上方的位置饋入(如圖中3所示)。 如圖3中所示，甲醇進料自汽提塔塔盤上方之位置引入至汽提塔中，且水(去礦物質水或去離子水)進料在汽提塔塔盤及甲醇進料引入至汽提塔中之位置上方之位置引入至汽提塔中。在一些實施例中，汽提塔亦可包含如通常使用之再循環桶，其中汽提塔位於再循環桶上方且與再循環桶流體連通。在汽提塔中，氮氣汽提氣在汽提塔塔盤以下之位置引入。在離開汽提塔之後，甲醇與水之混合進料隨後引入至甲醇裂解器中以提供如圖1中所示之包含氫氣之混合氣體，從而提供高純度H2
產物。在圖3中，氫氣之至少一部分在汽提塔塔盤以下之位置提供至汽提塔，或提供至位於汽提塔下方的再循環桶。 在一些實施例中，氫產物中之氬含量在按體積計小於70 ppb之範圍內。在一些較佳實施例中，氫氣中之氬含量在按體積計小於70 ppb之範圍內；且氫氣中之O2
含量在按體積計小於70 ppb之範圍內。 在本發明中，用於汽提塔之氮氣(N2
)流必須符合特定純度(低氬含量)，使得氬將有效地自位於再循環桶上方之汽提塔汽提。在本發明中，氮氣流可購自可購自LINDE AG或其他合格供應商，其易於保證所需效用(氮)規格。在一些實施例中，氮氣流包含低氬含量，諸如小於70 ppm mol、在1 ppm mol至50 ppm mol之範圍內、在5 ppm mol至50 ppm mol之範圍內、在10 ppm mol至40 ppm mol之範圍內、在20 ppm mol至35 ppm mol之範圍內或其間所有範圍及子範圍內之氬含量。 在一些實施例中，本發明之汽提塔方法可在環境溫度下進行。詳言之，本發明之汽提塔方法可在自0℃至50℃之溫度、自5℃至45℃之溫度、自5℃至35℃之溫度、自10℃至45℃之溫度、自10℃至35℃之溫度、自15℃至25℃之溫度、自5℃至環境溫度之溫度或其間所有範圍及子範圍之溫度下進行。 範圍可在本文中表示為自「約」一個特定值及/或至「約」另一特定值。當表示此類範圍時，實例包括自一個特定值及/或至另一特定值。類似地，當藉由使用前述詞「約」將值表示為近似值時，應瞭解特定值形成另一態樣。進一步應理解範圍中之每一者的端點在相對於另一端點及獨立於另一端點時均為重要的。 除非另有明確陳述，否則絕不希望本文中所闡述之任何方法理解為必需依特定次序執行其步驟。因此，在方法請求項實際上未陳述一個次序待要後繼其步驟或在申請專利範圍或說明書中未另外具體陳述該等步驟限於特定次序的情況下，絕不希望推斷任何特定次序。實例 1
來自外部供應商之甲醇進料自卡車釋放至甲醇槽，其中來自卡車之甲醇進料具有Ar含量為101.0 mol/hr之25500 kmol/hr流。在此甲醇進料中，在15℃及1.01巴下Ar含量為3.9 ppm (mol)。此外，空氣中Ar含量為按體積計0.85%。在甲醇槽中，甲醇進料具有1.07 mol/hr之Ar含量。在此甲醇進料中，在15℃及1.31巴下Ar含量為0.04 ppm (mol)。在甲醇槽中，甲醇進料以具有低Ar含量之氮氣覆蓋，其中氮中之Ar含量為按體積計70 ppm。 水進料自水廠引入至水槽。來自水廠之水具有Ar含量為7.60 mol/hr之23400 kmol/hr流。在此甲醇進料中，在15℃及1.01巴下Ar含量為0.32 ppm (mol)。此外，空氣中之Ar含量為按體積計0.92%。在水槽中，水進料具有7.60 mol/hr之Ar含量。在此水進料中，Ar含量為0.32 ppm (mol)。如在本發明中所陳述，甲醇進料及水進料在15℃之溫度及1.31巴之壓力下引入至氮汽提塔中。混合進料自汽提塔之出口引入至甲醇裂解器中，其具有0.64 mol/hr之Ar含量。最後，在100000 kmol/hr之流中之PSA進料氣體具有極低Ar含量，亦即0.006 ppm (mol)。 在此實例中，發現最終氫產物將具有極低Ar含量，其符合在氫氣中較緊密的Ar雜質小於70 ppb之要求。在此實例中，氫產物將具有小於0.006 ppm (mol)或6 ppb (mol)之Ar含量。 以上描述僅為本發明之實施例且並不意欲限定本發明之範疇。熟習此項技術者可作出本發明所有類型之變化形式及修改。在本發明之精神及原理內作出的任何修改、替代方案及改進將處於隨附申請專利範圍之範疇內。Hereinafter, embodiments of the preferred embodiments of the present invention will be provided. It should be noted that in the embodiments of the embodiments, for the sake of brevity and conciseness, it is not possible to describe all the features of the actual embodiments in detail. It will be appreciated that during the practice of any embodiment, as in the course of an engineering project or design project, various decisions are typically made in order to achieve a developer's specific objectives and to meet certain system-related or business-related constraints. It will also vary between an embodiment and another embodiment. In addition, it is to be understood that while efforts made in such development processes can be complex and time consuming, some variations, such as design, fabrication, and production, based on the technical content disclosed in the present invention, are merely disclosed in the present invention. The conventional technical means in the art of the related art in the related art should not be considered as a deficiency of the present disclosure. Unless otherwise defined, all technical or scientific terms used in the claims and the claims are intended to have the same meaning The term "a/an" and its analogs do not denote a limitation of quantity, but indicate that there is at least one. The terms "comprises/comprising", "includes/including" and the like means that the elements or objects preceding "including" or "including" are included in the "including" or "including" elements or Objects and their equivalents, but do not exclude other components or objects. In the present invention, the inventors have found that the solubility of Ar in methanol is greater than the solubility in water. Thus, reducing the argon content in methanol is critical to reducing the argon content in the final hydrogen product obtained via the methanol cracker and PSA. On the other hand, the inventors have found that the Ar content in nitrogen is much smaller than in air. For nitrogen which is usually produced by a cryogenic air separation process, the Ar content is less than 70 ppm (mol) and the Ar content in air is 0.934% (mol). Therefore, at a specific temperature and a specific pressure, the partial pressure of Ar in nitrogen is less than 0.75% in air, so that the solubility of Ar in methanol and water can be significantly lowered by contact with nitrogen. Accordingly, the inventors have surprisingly discovered that the introduction of a stripping column using stripping nitrogen for a methanol/water mixed feed can significantly reduce argon to a sufficiently low level in the methanol/water mixed feed so that in a downstream PSA unit, it can be produced H 2 will be met for extremely high purity requirements for argon. In one embodiment of the invention, a method of reducing argon content in hydrogen obtained via a methanol cracker and PSA, wherein the improvement of the method comprises: prior to introducing the feed stream comprising methanol into the methanol cracker The feed stream undergoes a stripper process using a stripping gas comprising nitrogen. In order to reduce the Ar content and the O 2 content in the hydrogen product, the feed stream undergoing the stripper process may comprise a mixed feed of methanol and water. In the present invention, a feed stream comprising methanol can be purchased from Linde AG or an external supplier and stored in a methanol tank for use. In a preferred embodiment, the feed stream comprising methanol is blanketed with nitrogen prior to use. As noted above, the Ar content in the process gas (PSA inlet) is significantly altered primarily due to changes in the methanol feed, and the contaminated resources are from upstream storage and transportation, whereby the fresh methanol feed contains the highest Ar content. The Ar content in the methanol feed for the MC and PSA inlet gases is much lower after several days of storage of the methanol feed over a nitrogen blanket with a low Ar content, since it is in methanol at 0.3 bar and ambient temperature. Ar will be nearly equilibrated with 70 ppm Ar in nitrogen. The Ar content in the process gas can be reduced to nearly 70 ppb. In one embodiment of the invention, the stripper process of the present invention can be carried out at ambient temperature. In particular, the stripper method of the present invention can be at a temperature from 0 ° C to 50 ° C, a temperature from 5 ° C to 45 ° C, a temperature from 5 ° C to 35 ° C, a temperature from 10 ° C to 45 ° C, and The temperature is from 10 ° C to 35 ° C, from 15 ° C to 25 ° C, from 5 ° C to ambient temperature or all ranges and sub-ranges between them. In one embodiment of the invention, the feed stream comprising water and the feed stream comprising methanol are fed to the stripper at the same location. In a particular embodiment, a feed stream comprising water can be introduced into a conduit for introducing a feed stream comprising methanol, and then the feed stream comprising water is fed together with the feed stream comprising methanol. In the tower. In one embodiment of the invention, the feed stream comprising water and the feed stream comprising methanol can be fed separately into the stripper. In a preferred embodiment, a feed stream comprising water can be fed to the stripper from the top of the stripper. Alternatively, the feed stream comprising water can be fed to the stripper at a location above the location where the feed stream comprising methanol is fed into the stripper. In one embodiment of the invention, the method of reducing the argon content in hydrogen obtained via a methanol cracker and PSA may comprise subjecting the feed stream to use prior to introduction of the feed stream comprising methanol into the methanol cracker. A stripper process comprising a stripping gas of hydrogen instead of nitrogen. In a preferred embodiment, the method of reducing the argon content in hydrogen may further comprise subjecting the feed stream to steam using a stripping gas comprising hydrogen before the feed stream comprising methanol is introduced into the methanol cracker. Titta method. In a more preferred embodiment, the method of reducing the argon content in hydrogen can further comprise: recycling at least a portion of the hydrogen leaving the PSA into the nitrogen stream. In one embodiment of the invention, the nitrogen stream may comprise a low argon content, such as an argon content of less than 70 ppm mol, in the range of 1 ppm mol to 50 ppm mol, in the range of 5 ppm mol to 50 ppm mol, In the range of 10 ppm mol to 40 ppm mol, in the range of 20 ppm mol to 35 ppm mol, or in all ranges and sub-ranges therebetween. In contrast to the prior art, the inventors have surprisingly found that in the present invention, the introduction of a stripping column for a methanol/water mixed feed can significantly reduce argon to a sufficiently low level in a methanol/water mixed feed, such that In the downstream PSA unit, H 2 which will meet the extremely high purity requirements for argon (the argon content in hydrogen is in the range of less than 70 ppb by volume) can be produced. In addition, the increased cost of the stripper process in the present invention is much lower than the prior art using methanol cracker technology and can reduce Ar to below 70 ppb, such as in MC (methanol cracker and PSA). Or add a low temperature TSA downstream of the modified water electrolysis cell in place of MC. Palladium film compared to using cryogenic purifier to purify the H 2 Alternatively, the method of the present invention to significantly more economical (cost-effective). Use of the modified water electrolysis cell also leads to a higher cost of significant H 2, which is caused by electric power such as a methanol (or natural gas) of the fuel is relatively high compared to the price. The NG (natural gas)-based steam recombiner (SMR) has also experienced significant problems (high operating loss = high cost), especially in Taiwan and China, where natural gas feeds are also mixed with argon traces (in the ppm range, usually 30-60 ppmv in NG. After the PSA process in an argon aspect SMR H 2 nor meet specifications, unless a very inefficient method of operation (i.e., 30-40% loss of product). Because it is extremely difficult (economically uncompetitive compared to any known technology) to separate argon from NG, the use of SMR technology to produce hydrogen from NG in mixed argon for electronic gas customers is not an alternative to new equipment. Existing SMR equipment can continue to operate with extremely low recovery and high losses. Further, if the (near) future (semiconductor layer having even thinner), the H 2 in argon specifications become more stringent (i.e., <10 ppbv), the natural gas NG-SMR (based on the PSA followed by The hydrogen of the -hydrogen methane reformer is no longer an alternative and will not work at all if the argon trace is contained in the NG. The problem of Ar in NG can also be the result of a gradual increase in the number of LNG devices/terminals worldwide. NG dealers can use nitrogen to regulate (vaporize) the calorific value of LNG to meet NG pipe specifications. However, N 2 for calorific value adjustment is generally not high purity N 2 but also contains argon. However, by using the method described in the present invention, the argon content in hydrogen can be even reduced to less than 70 ppb, less than 60 ppb, less than 50 ppb, less than 40 ppb, less than 30 ppb, less than 20 ppb, less than 10 ppb, Less than 5 ppb or less than 1 ppb. In one embodiment of the invention, the argon content in the hydrogen is from 1 ppb to 70 ppb, from 5 ppb to 70 ppb, from 10 ppb to 70 ppb, from 20 ppb to 70 ppb, from 30 ppb to 70 ppb. From 40 ppb to 70 ppb, from 50 ppb to 70 ppb, from 60 ppb to 70 ppb, from 1 ppb to 60 ppb, from 1 ppb to 50 ppb, from 1 ppb to 40 ppb, from 1 ppb to 30 ppb, From 5 ppb to 60 ppb, from 5 ppb to 50 ppb, from 5 ppb to 40 ppb, from 5 ppb to 30 ppb, from 10 ppb to 60 ppb, from 10 ppb to 50 ppb, from 10 ppb to 40 ppb, from Ranges from 10 ppb to 30 ppb and all ranges and sub-ranges between them. In one embodiment of the invention, the O 2 content in the hydrogen ranges from 1 ppb to 70 ppb, from 5 ppb to 70 ppb, from 10 ppb to 70 ppb, from 20 ppb to 70 ppb, from 30 ppb to 70. Ppb, from 40 ppb to 70 ppb, from 50 ppb to 70 ppb, from 60 ppb to 70 ppb, from 1 ppb to 60 ppb, from 1 ppb to 50 ppb, from 1 ppb to 40 ppb, from 1 ppb to 30 ppb From 5 ppb to 60 ppb, from 5 ppb to 50 ppb, from 5 ppb to 40 ppb, from 5 ppb to 30 ppb, from 10 ppb to 60 ppb, from 10 ppb to 50 ppb, from 10 ppb to 40 ppb, From 10 ppb to 30 ppb and all ranges and sub-ranges between them. In general, the methanol cracker through a method of producing hydrogen gas and the PSA may include: (1) introducing the feed comprising methanol to form a methanol cracker to 4 and comprises a plurality of by-products such as dimethyl ether of mainly comprising hydrogen, CO, CH a mixed gas of heavy components; and (2) introducing a mixed gas to the PSA unit to provide a hydrogen product. In some embodiments (as shown in Figure 1), water from a demineralization tank (demineralized water or deionized water) feed is mixed with a methanol feed from a methanol tank to provide a mixture of methanol and water. The feed of methanol and water is then introduced into a tank or degasser (eg, a recycle tank). The methanol feed can be supplied by an external supplier and Linde itself. The degassed or undegassed mixed feed is then introduced to a methanol cracker to provide a mixed gas comprising hydrogen. After passing through the water cooler, a condenser (e.g. condensate tub), the mixed gas is introduced into the PAS unit, thereby providing a H 2 products. Details on products are typically prepared via the H 2 PSA and the methanol cracker as I have been known in the prior art, which may be incorporated herein by way of reference. In one embodiment of the invention, a method of removing argon/reducing argon content in hydrogen obtained via a methanol cracker and PSA is provided. In the process of the present invention, an improvement is included in which the feed stream is first subjected to a stripper process using a stripping gas comprising nitrogen before the feed stream comprising methanol is introduced into the methanol cracker. In some embodiments, the stripping gas can also comprise hydrogen. In some embodiments, the feed stream can comprise a mixed feed of methanol and water. In some embodiments, methanol can be mixed with water and fed into the stripper at the same location. In other embodiments, methanol and water may be fed separately to the stripper, wherein water is fed separately from the top of the stripper to the stripper, or water is above the methanol feed to the stripper. Position feed (as shown in Figure 3). As shown in Figure 2, a water (demineralized water or deionized water) feed is mixed with the methanol feed to provide a mixed feed of methanol and water. Subsequently, a mixed feed of methanol and water is introduced into the stripper. In some embodiments, the stripper can also include a recycle tank as is commonly used, wherein the stripper is located above the recycle tank and in fluid communication with the recycle tank. In the stripper, a stripping gas (e.g., nitrogen) is introduced below the stripper tray and a mixed feed of methanol and water is introduced at the upper portion of the stripper tray. After leaving the stripper, the mixture of methanol and water feed is then introduced into a methanol cracker to provide the shown in FIG. 1 comprises a mixed gas of hydrogen gas, thereby providing a high purity of the H 2 product. In some embodiments, the amount of argon in the hydrogen product is in the range of less than 70 ppb by volume. In some preferred embodiments, the amount of argon in the hydrogen is less than 70 ppb by volume; and the amount of O 2 in the hydrogen is less than 70 ppb by volume. In some embodiments, the method of the present invention can further comprise: recycling at least a portion of the hydrogen leaving the PSA unit to the stripper, preferably to the stream of nitrogen. In particular, at least a portion of the hydrogen and nitrogen stream are introduced from below the stripper tray or introduced into a recycle tank located below the stripper. In some additional embodiments, the feed stream can comprise a mixed feed of methanol and water. In some additional embodiments, methanol and water may be mixed and fed into the stripper at the same location. In other embodiments, methanol and water may be fed separately to the stripper, wherein water is fed separately from the top of the stripper to the stripper, or water is above the methanol feed to the stripper. Position feed (as shown in Figure 3). As shown in Figure 3, the methanol feed is introduced to the stripper from a position above the stripper tray, and water (demineralized or deionized water) is fed to the stripper tray and methanol feed. The position introduced above the position in the stripper is introduced into the stripper. In some embodiments, the stripper can also include a recycle tank as is commonly used, wherein the stripper is located above the recycle tank and in fluid communication with the recycle tank. In the stripper, nitrogen stripping gas is introduced at a location below the stripper tray. After leaving the stripper, the mixture of methanol and water feed is then introduced into a methanol cracker to provide the shown in FIG. 1 comprises a mixed gas of hydrogen gas, thereby providing a high purity H 2 product. In Figure 3, at least a portion of the hydrogen is provided to the stripper at a location below the stripper tray or to a recycle tank located below the stripper. In some embodiments, the argon content of the hydrogen product is in the range of less than 70 ppb by volume. In some preferred embodiments, the argon content in the hydrogen is in the range of less than 70 ppb by volume; and the O 2 content in the hydrogen is in the range of less than 70 ppb by volume. In the present invention, for the nitrogen stripper column (N 2) flow has to meet certain purity (low argon content), such as argon effectively stripped from the stripping column located above the recirculation of the tub. In the present invention, the nitrogen stream can be purchased from LINDE AG or other qualified suppliers, which is easy to assure the required utility (nitrogen) specifications. In some embodiments, the nitrogen stream comprises a low argon content, such as less than 70 ppm mol, in the range of 1 ppm mol to 50 ppm mol, in the range of 5 ppm mol to 50 ppm mol, and in the range of 10 ppm mol to 40 ppm The argon content in the range of 20 ppm mol to 35 ppm mol or all ranges and subranges in the range of mol. In some embodiments, the stripper process of the present invention can be carried out at ambient temperature. In particular, the stripper method of the present invention can be at a temperature from 0 ° C to 50 ° C, a temperature from 5 ° C to 45 ° C, a temperature from 5 ° C to 35 ° C, a temperature from 10 ° C to 45 ° C, and The temperature is from 10 ° C to 35 ° C, from 15 ° C to 25 ° C, from 5 ° C to ambient temperature or all ranges and sub-ranges between them. Ranges may be expressed herein as "about" a particular value and/or to "about" another particular value. When such a range is expressed, the examples include from a particular value and/or to another particular value. Similarly, when values are expressed as approximations by using the above-mentioned word "about," it should be understood that the particular value forms another aspect. It is further understood that the endpoints of each of the ranges are important relative to the other endpoint and independent of the other endpoint. Unless expressly stated otherwise, it is in no way intended that any of the methods set forth herein be construed as being necessarily in a particular order. Thus, in the event that a method request item does not actually recite an order to be followed by a step or in the scope of the patent application or the specification does not specifically state that the steps are limited to a particular order, it is never desirable to infer any particular order. Example 1 A methanol feed from an external supplier was released from the truck to a methanol tank where the methanol feed from the truck had a 25500 kmol/hr flow with an Ar content of 101.0 mol/hr. In this methanol feed, the Ar content was 3.9 ppm (mol) at 15 ° C and 1.01 bar. Further, the Ar content in the air was 0.85% by volume. In the methanol tank, the methanol feed had an Ar content of 1.07 mol/hr. In this methanol feed, the Ar content was 0.04 ppm (mol) at 15 ° C and 1.31 bar. In the methanol tank, the methanol feed was covered with nitrogen having a low Ar content, wherein the Ar content in the nitrogen was 70 ppm by volume. Water feed is introduced from the water plant to the sink. The water from the water plant has a flow of 23400 kmol/hr with an Ar content of 7.60 mol/hr. In this methanol feed, the Ar content was 0.32 ppm (mol) at 15 ° C and 1.01 bar. Further, the Ar content in the air was 0.92% by volume. In the water tank, the water feed has an Ar content of 7.60 mol/hr. In this water feed, the Ar content was 0.32 ppm (mol). As stated in the present invention, the methanol feed and water feed were introduced into the nitrogen stripper at a temperature of 15 ° C and a pressure of 1.31 bar. The mixed feed was introduced from the outlet of the stripping column into a methanol cracker having an Ar content of 0.64 mol/hr. Finally, the PSA feed gas in the 100000 kmol/hr stream has a very low Ar content, ie 0.006 ppm (mol). In this example, it was found that the final hydrogen product would have a very low Ar content consistent with the requirement that the tighter Ar impurities in hydrogen be less than 70 ppb. In this example, the hydrogen product will have an Ar content of less than 0.006 ppm (mol) or 6 ppb (mol). The above description is only an embodiment of the invention and is not intended to limit the scope of the invention. Variations and modifications of all types of the invention may be made by those skilled in the art. Any modifications, alternatives and improvements made within the spirit and scope of the invention will fall within the scope of the appended claims.