【正文】 包括的步驟有：在氮洗滌塔中，從包括有大量一氧化碳和包括氮、氫和甲烷在內(nèi)的殘留氣體中除去第一液體餾分；并且第二個液體摩擦在一個中間位置 洗滌塔的底部和頂部之間 , 該部位含有豐富的氮?dú)夂鸵谎趸迹粚兓?，在氣提塔里通過中壓 膜塑法，通過第一液體摩擦的一氧化碳在頂部分離出剩余的氫，第二步蒸餾，在低溫下在蒸餾塔分離出一氧化碳，并且在頂部有少量氮產(chǎn)生，氮主要來源于第一部分離的氣提塔中基本的混合物。除此之外的任務(wù)便是研究一個能夠執(zhí)行這些工藝的工廠。另一任務(wù)就是研究利用其他生產(chǎn)的工藝生產(chǎn)高純度一氧 化碳。 至今，使用氮洗滌單元的殘留氣體作為原料來生產(chǎn)一氧化碳，用于分離一氧化碳，因此利用這些過去被燒掉的氣體生產(chǎn)一氧化碳都已成為可能了。 之后，一氧化碳被用于第一蒸餾塔和第二蒸餾塔頂部冷凝齊的冷卻液。產(chǎn)生的冷凝物就是在第一蒸餾塔中的蒸餾，目的是從剩余的混合物中分離出甲烷。殘留的氣體作為一氧化碳生產(chǎn)的原料混合物。 在先前的研究中，從 6 中氮洗滌出來的氣體被燃燒掉。 在吸收過程 5 中除去二氧化碳，氣體混合物進(jìn)入低溫洗滌氮階段 6，這一階段產(chǎn)生合成物和氣體殘留物，殘留物包括一氧化碳、氫氣、甲烷和氮?dú)狻?特別是，在用于生產(chǎn)氨氣合成物的準(zhǔn)備階段產(chǎn)生一氧化碳，此時，碳?xì)浠衔锖兔旱牟糠盅趸梢垣@得氫。使用傳統(tǒng)的純化技術(shù)生產(chǎn)高純度的一氧化碳是可行的。 描述 發(fā)明的領(lǐng)域： 現(xiàn)有的發(fā)明來源于氨氣合成物和一氧化碳的聯(lián)合生產(chǎn)，也就是這種聯(lián)合生產(chǎn)的工廠。 12所言的工廠，工廠有完整的設(shè)備用于合成氨氣，也就是第一單元上合成物的生產(chǎn)，用于氮?dú)浠衔锘蛎旱牟糠盅趸?，并且在最后一個單元用于氮的洗滌；工廠不斷的在最后一個單元用于氮的洗滌。 12所言的工廠，更多的使用擁有膨脹物的流水線連接高壓氮蒸汽，以便低壓冷卻循環(huán)。 12所言的工廠，還包括使用一個氮冷卻循環(huán)提供高壓氮用于生產(chǎn)氨氣 合成氣。 1所言的，產(chǎn)生純度為 98%的一氧化碳。 9. 依據(jù)聲明 7 所言的，一氧化碳蒸汽使它的壓力降低，并且在低壓下冷卻蒸餾塔的頂部。 7. 依據(jù)聲明 1 所言，產(chǎn)生的一氧化碳蒸汽被壓縮并且用于分離步驟中冷卻循環(huán)中的冷卻液。 5. 依據(jù)聲明 4 所言的，通過蒸餾塔的頂部壓縮機(jī)，輸送的低壓氮蒸汽被壓縮到合成氨氣合成物所需的壓力，并且在分離步驟中作為循環(huán)液在冷卻循環(huán)中循環(huán)使用。 3. 依據(jù)聲明 2 所言的，高壓下的氮蒸汽中的一部分被冷卻，并且分別用于向氣提塔和蒸餾塔。 需改善的過程包括 :從富含一氧化碳和在殘余的組成部分中去除液體分?jǐn)?shù)，包括有底部的氮?dú)?、氫和甲烷洗滌塔；并且第二液體分?jǐn)?shù)在一個中間位置 洗滌塔的底部和頂部之間 , 該部位含有豐富的氮?dú)夂鸵谎趸?；對純化而言，在氣提塔里通過中壓膜塑法，通過第一液體分?jǐn)?shù)的一氧化碳在頂部分離出剩余的氫，第二步蒸餾，在低壓下在蒸餾塔分離出一 氧化碳，并且在頂部有少量氮產(chǎn)生，氮主要來源于第一步分離的氣提塔中基本的混合物。一氧化碳在低溫下從上述洗滌柱中分餾出一級餾分，在上述的洗滌塔中，在一個中間壓力提餾柱，然后在低下分裂蒸餾塔，二級餾分來源于洗滌塔的底部和頂部之間的位置。 摘要 本發(fā)明涉及的工藝是氨合成氣和一氧化碳。 FIG. 2, which schematically represents a plant for bined production of an ammonia synthesis mixture and carbon dioxide according to the invention。 steam expansion in a turbine 10 to drive the pressor 9。 further processes employed for purification are absorption processes, such as the Tenneco Chemicals COSORB process, or adsorption processes (Pressure Swing Adsorption or PSA). In particular, carbon monoxide is produced during preparation of the synthesis mixture used for the synthesis of ammonia, when the hydrogen is obtained by partial oxidation of hydrocarbons or coal. Such a conventional process of preparing the synthesis mixture is illustrated in the diagram in FIG. 1 and will be described in brief below: After removal of the soot at 1, and removal of the hydrogen sulphide at 2, from the mixture delivered by the step of partially oxidizing hydrocarbon or coal at 3, step 4 of converting the CO changes the majority of the CO present, under the action of steam, into carbon dioxide () while producing hydrogen. After removal of by absorption at 5, the gas mixture is subjected to a cryogenic step 6 of washing with nitrogen, which provides the synthesis mixture ( +) as well as a residual gas containing essentially carbon monoxide, hydrogen, methane and nitrogen. FIG. 1 also represents the other operations in the synthesis of ammonia: air distillation at 7, providing the oxygen needed for the partial oxidation 3 and the nitrogen needed for the washing 6。 and a second liquid fraction at an intermediate position between the base and head of the washing column, which is rich in nitrogen and lean in carbon monoxide。 said plant constituting the last unit for washing with nitrogen. 18. In a plant for bined production of an ammonia synthesis mixture and carbon monoxide, prising the production of an ammonia synthesis mixture ( +) from a) a source of hydrogen under high pressure, purified in a final step by washing with nitrogen in a washing column, and b) a stream of nitrogen at high pressure。 a lowpressure distillation column provided with boiling means and with a head condenser, producing a fraction rich in methane at the base and a fraction rich in carbon monoxide at the head。 cryogenically purifying, the carbon monoxide from the first liquid fraction by a first separation under medium pressure in a stripping column separating the residual hydrogen at the head, and a second distillation under low pressure in a distillation column separating the carbon monoxide and the residual nitrogen at the head from the base mixture resulting from the first separation in the stripping column. 2. The process according to claim 1, wherein a portion of the stream of nitrogen at high pressure is used as the cycle fluid of an open cooling cycle involved in the separation steps. 3. The process according to claim 2, wherein a portion of the stream of nitrogen at high pressure is cooled and used to supply base boilers respectively for the stripping and distillation columns. 4. The process according to claim 2, wherein a portion of the stream of nitrogen at high pressure is cooled, has its pressure reduced, and is used at low pressure to cool the head of the distillation column. 5. The process according to claim 4, wherein the lowpressure nitrogen stream delivered by the head condenser of the distillation column is pressed to the pressure needed for the production of the ammonia synthesis mixture, and is recycled as the cycle fluid of the open cooling cycle involved in the separation steps. 6. The process according to claim 1, wherein a portion of the stream of nitrogen at high pressure has its pressure reduced in a turbine to contribute to the refrigeration needed for the separation steps. 7. The process according to claim 1, wherein the stream of carbon monoxide produced is pressed and used as the cycle fluid of an open cooling cycle involved in the separation steps. 8. The process according to claim 7, wherein the pressed stream of carbon monoxide is used to supply base boilers respectively for the stripping and distillation columns. 9. The process according to claim 7, wherein the stream of carbon monoxide has its pressure reduced and used at low pressure to cool the head of the distillation column. 10. The process according to claim 9, wh