TW202419798A - Method and system for solidifying a gas at atmospheric pressure - Google Patents
Method and system for solidifying a gas at atmospheric pressure Download PDFInfo
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- 238000000034 method Methods 0.000 title claims description 28
- 239000012071 phase Substances 0.000 claims abstract description 114
- 239000007788 liquid Substances 0.000 claims abstract description 29
- 239000007791 liquid phase Substances 0.000 claims abstract description 28
- 239000007790 solid phase Substances 0.000 claims abstract description 17
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 128
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 64
- 239000001569 carbon dioxide Substances 0.000 claims description 58
- 238000001816 cooling Methods 0.000 claims description 37
- 238000007906 compression Methods 0.000 claims description 33
- 230000006835 compression Effects 0.000 claims description 33
- 238000007711 solidification Methods 0.000 claims description 14
- 230000008023 solidification Effects 0.000 claims description 14
- 239000012530 fluid Substances 0.000 claims description 12
- 239000003507 refrigerant Substances 0.000 claims description 12
- 239000007787 solid Substances 0.000 claims description 8
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 6
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000004064 recycling Methods 0.000 claims description 5
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims description 4
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims description 4
- 229910021529 ammonia Inorganic materials 0.000 claims description 3
- 239000001294 propane Substances 0.000 claims description 3
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 3
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 174
- 238000001723 curing Methods 0.000 description 28
- 239000013529 heat transfer fluid Substances 0.000 description 7
- 238000005057 refrigeration Methods 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000011031 large-scale manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 101001121408 Homo sapiens L-amino-acid oxidase Proteins 0.000 description 1
- 102100026388 L-amino-acid oxidase Human genes 0.000 description 1
- 101100012902 Saccharomyces cerevisiae (strain ATCC 204508 / S288c) FIG2 gene Proteins 0.000 description 1
- 101100233916 Saccharomyces cerevisiae (strain ATCC 204508 / S288c) KAR5 gene Proteins 0.000 description 1
- 239000012809 cooling fluid Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Abstract
Description
本發明是關於熱力學領域，且更特別地，是關於一種用於固化諸如二氧化碳或乙炔氣體的氣體的方法。The present invention relates to the field of thermodynamics and, more particularly, to a method for solidifying a gas such as carbon dioxide or acetylene gas.
當前，在大氣壓力下接收的此類氣體的固化使用一或多個壓縮及冷卻步驟，以便使氣體成為液體，且接著使用膨脹步驟，在大氣壓力下及大約零下八十攝氏度的極低溫度下供應固相及氣相。氣相通常在入口處再循環以限制氣體損失，且此再循環氣相的冷有時用於改良氣相與固相的轉換因數。Currently, the solidification of such gases received at atmospheric pressure uses one or more compression and cooling steps in order to make the gas liquid, and then an expansion step to supply solid and gas phases at atmospheric pressure and at very low temperatures of about minus eighty degrees Celsius. The gas phase is usually recirculated at the inlet to limit gas losses, and cooling of this recycled gas phase is sometimes used to improve the conversion factor of the gas phase to the solid phase.
此固化方法適用於工業及農業食品應用，但非常耗能，特別是對於每小時大約一千噸的大規模應用。This curing method is suitable for industrial and agro-food applications, but is very energy intensive, especially for large-scale applications of around one thousand tons per hour.
然而，氣候問題可使此類生產為二氧化碳運輸所需的，目的為在距離捕獲位置非常遠的位置掩埋。實際上，必須特別捕獲來自熱能工廠或工業位置的二氧化碳，以免增加大氣中二氧化碳濃度且因此不增加溫室效應。在收集之後，二氧化碳可重複使用或隔離在合適位置，所述位置通常離捕獲位置非常遠。因此，由氣體管道運輸將是昂貴的或不可想像的。液化二氧化碳的海上運輸需要加壓運輸，且因此需要配置具有顯著厚度的墊片，因此非常昂貴，且使長距離運輸液化二氧化碳非常困難。However, climate problems may make such production necessary for the transport of CO2 for the purpose of landfill at locations very far from the capture site. In practice, CO2 from thermal power plants or industrial locations must be captured specifically so as not to increase the CO2 concentration in the atmosphere and therefore not to increase the greenhouse effect. After collection, the CO2 can be reused or isolated at a suitable location, which is usually very far from the capture site. Transport by gas pipelines would therefore be expensive or unthinkable. The transport of liquefied CO2 by sea requires pressurized transport and therefore requires the provision of gaskets with significant thickness, which is therefore very expensive and makes the transport of liquefied CO2 over long distances very difficult.
因此，可需要大規模產生固態二氧化碳，特別是在大氣壓力下用體積非常大的船運輸二氧化碳，此大規模產生需要在材料及能源資源方面儘可能便宜。Therefore, large-scale production of solid carbon dioxide may be required, especially for transporting the carbon dioxide at atmospheric pressure using very large ships, and this large-scale production needs to be as cheap as possible in terms of material and energy resources.
本發明藉由提供一種用於固化氣體的方法及對應固化系統來至少部分地彌補先前技術的缺點，此使得有可能固化氣體同時使用比習知製程更少的能量及材料資源。根據本發明的方法及系統適用於三相點高於大氣壓力且在正常溫度及壓力條件下（因此，在0攝氏度及一巴下）處於氣態的氣體。因此，此氣體為二氧化碳或乙炔氣體。The present invention at least partially remedies the disadvantages of the prior art by providing a method for solidifying a gas and a corresponding solidification system, which makes it possible to solidify the gas while using less energy and material resources than the known process. The method and system according to the invention are applicable to a gas whose triple point is above atmospheric pressure and which is in the gaseous state under normal temperature and pressure conditions (thus, at 0 degrees Celsius and one bar). Thus, this gas is carbon dioxide or acetylene gas.
為此目的，本發明提出一種用於固化氣體的方法，所述氣體由三相點高於大氣壓力的分子物質形成，所述方法包括以下步驟： -在大氣壓力下接收氣體， -壓縮及冷卻氣體直至氣體完全液化，壓縮使用第一壓縮器及接收來自第一壓縮器的氣體的至少一個第二壓縮器進行，且冷卻使用至少一個熱交換器進行，所述熱交換器實現氣體與製冷劑流體之間的熱交換以便液化氣體， -使由壓縮及冷卻步驟產生的處於液態的氣體膨脹，且在所述膨脹步驟的出口處獲得固體及氣體， 固化方法的特徵在於，膨脹步驟包括： -至少一個第一膨脹子步驟，自由壓縮及冷卻步驟產生的處於液態的氣體產生壓力大於三相點的壓力的液相及氣相，由此獲得的氣相在所述至少一個第二壓縮器的入口處與氣體混合， -以及最終膨脹子步驟，自在所述至少一個第一膨脹子步驟期間獲得的液相在大氣壓力下產生固相及氣相。術語「在大氣壓力下」在本申請案中理解為意指「實質上在大氣壓力下」，換言之，在一巴內且較佳為在0.1巴內。實際上，在最後一個膨脹子步驟的出口處產生的氣相通常略大於大氣壓力。 For this purpose, the present invention proposes a method for solidifying a gas formed by molecular substances with a triple point higher than atmospheric pressure, the method comprising the following steps: - receiving the gas under atmospheric pressure, - compressing and cooling the gas until the gas is completely liquefied, the compression being carried out using a first compressor and at least one second compressor receiving the gas from the first compressor, and the cooling being carried out using at least one heat exchanger, the heat exchanger realizing heat exchange between the gas and a refrigerant fluid in order to liquefy the gas, - expanding the gas in the liquid state produced by the compression and cooling steps, and obtaining a solid and a gas at the outlet of the expansion step, The solidification method is characterized in that the expansion step comprises: - at least one first expansion sub-step, the gas in the liquid state produced by the free compression and cooling step produces a liquid phase and a gas phase at a pressure greater than the pressure of the triple point, the gas phase thus obtained is mixed with the gas at the inlet of the at least one second compressor, - and a final expansion sub-step, producing a solid phase and a gas phase at atmospheric pressure from the liquid phase obtained during the at least one first expansion sub-step. The term "at atmospheric pressure" is understood in this application to mean "substantially at atmospheric pressure", in other words, within one bar and preferably within 0.1 bar. In practice, the gas phase produced at the outlet of the last expansion sub-step is usually slightly greater than atmospheric pressure.
在本發明中，膨脹步驟至少分兩個步驟進行，各第一膨脹子步驟對應於氣體在比三相點的壓力大的壓力下的中間膨脹。In the present invention, the expansion step is performed in at least two steps, and each first expansion sub-step corresponds to an intermediate expansion of the gas under a pressure greater than the pressure at the triple point.
因此，離開各第一膨脹子步驟的氣體不在第一壓縮器的入口（氣體在大氣壓力下的入口）處再循環，而在第一壓縮器的下游的所述至少一個第二壓縮器的入口處再循環，所述至少第二壓縮器的入口處的氣體與在第一膨脹子步驟期間產生的氣體處於相同壓力。當存在若干第二壓縮器時，並非所有第二壓縮器必須接收來自膨脹步驟的再循環氣體，此是因為其入口壓力不允許，或此是因為由第一膨脹子步驟產生的所有氣相不被再循環，儘管僅當其氣相再循環時這些才是感興趣的。在本申請案中，「上游」及「下游」是指二氧化碳自其入口進入第一壓縮器至最後一個膨脹子步驟的流動方向。此外，「相同壓力」在本申請案中理解為意指「實質上在相同壓力下」，換言之，在一巴內。實際上，由於壓力損失，在所述至少一個第二壓縮器的入口處的壓力略低於在第一膨脹子步驟的出口處產生的氣體的壓力。因此，此再循環不需要像先前技術那樣將剛剛在大氣壓力下膨脹的氣體再壓縮至其液化壓力，至少對於由膨脹子步驟產生的氣體的部分。藉助於本發明，由第一膨脹步驟產生的大約8%氣體因此在比三相點的壓力大的壓力下再循環至根據本發明的固化製程中，此在此再循環期間節省能量。此外，第一壓縮器下游的一些膨脹氣體中的此再循環使得有可能減小其大小，此增加能量節省且允許節省硬體資源。Thus, the gas leaving each first expansion sub-step is not recycled at the inlet of the first compressor (inlet of the gas at atmospheric pressure), but at the inlet of said at least one second compressor downstream of the first compressor, the gas at the inlet of said at least second compressor being at the same pressure as the gas produced during the first expansion sub-step. When there are several second compressors, not all of them necessarily receive recycled gas coming from the expansion step, either because their inlet pressure does not allow it or because all the gas phase produced by the first expansion sub-step is not recycled, although these are only of interest when their gas phase is recycled. In the present application, "upstream" and "downstream" refer to the direction of flow of carbon dioxide from its inlet into the first compressor to the last expansion sub-step. Moreover, "same pressure" is understood in the present application to mean "substantially at the same pressure", in other words, within one bar. In practice, due to pressure losses, the pressure at the inlet of the at least one second compressor is slightly lower than the pressure of the gas produced at the outlet of the first expansion sub-step. Therefore, this recycling does not require the recompression of the gas that has just been expanded at atmospheric pressure to its liquefaction pressure, as in the prior art, at least for the part of the gas produced by the expansion sub-step. By means of the invention, about 8% of the gas produced by the first expansion step is thus recycled to the curing process according to the invention at a pressure greater than the pressure of the triple point, which saves energy during this recycling. Moreover, this recycling of some of the expanded gas downstream of the first compressor makes it possible to reduce its size, which increases the energy savings and allows saving hardware resources.
在本發明的一個實施例中，膨脹步驟因此包括若干第一膨脹子步驟，且壓縮及冷卻步驟使用與第一膨脹子步驟一樣多或更多的第二壓縮器，各第一膨脹子步驟產生壓力大於三相點的壓力但低於在先前膨脹子步驟中產生的氣相的壓力的液相及氣相，由此產生的氣相在第二壓縮器中的一者的入口處與氣體混合，所述氣體的壓力與由此產生的氣相的壓力相同。大體而言，歸因於二氧化碳氣體來自的系統的各種分支之間的壓頭損失的差異，接收此類氣相的第二壓縮器的入口處的壓力略小於此氣相的壓力。當然，先前膨脹子步驟是可能的，此是由於整個第一膨脹子步驟之前無此類先前膨脹子步驟。In one embodiment of the invention, the expansion step thus comprises several first expansion sub-steps, and the compression and cooling step uses as many or more second compressors as the first expansion sub-steps, each first expansion sub-step producing a liquid phase and a gas phase at a pressure greater than the pressure of the triple point but lower than the pressure of the gas phase produced in the previous expansion sub-step, the gas phase thus produced being mixed at the inlet of one of the second compressors with a gas having the same pressure as the gas phase thus produced. Generally speaking, the pressure at the inlet of the second compressor receiving such a gas phase is slightly lower than the pressure of this gas phase due to the difference in head loss between the various branches of the system from which the carbon dioxide gas comes. Of course, a previous expansion sub-step is possible since the entire first expansion sub-step is not preceded by such a previous expansion sub-step.
此外，在第一壓縮器的入口處在大氣壓力下較佳地引入在最後一個膨脹子步驟期間獲得的氣相。此氣相通常略大於大氣壓力。此亦使得有可能再循環此氣相。Furthermore, the gas phase obtained during the last expansion substep is preferably introduced at atmospheric pressure at the inlet of the first compressor. This gas phase is usually slightly above atmospheric pressure. This also makes it possible to recycle this gas phase.
在氣體壓縮及冷卻步驟期間，使用的熱交換器實現氣體與例如選自氨、丙烷、丙烯以及二氧化碳的製冷劑流體之間的熱交換。此製冷劑流體在閉合迴路中循環。During the gas compression and cooling steps, a heat exchanger is used to exchange heat between the gas and a refrigerant fluid, for example selected from ammonia, propane, propylene and carbon dioxide, which circulates in a closed loop.
較佳地，壓縮及冷卻步驟進一步使用定位於第一壓縮器後及/或所述至少一個第二壓縮器後的至少一個冷卻器。此冷卻器使用例如來自冷源（例如，環境冷源）的諸如空氣或水的熱傳遞流體。較佳地，此類冷卻器直接連接於第一壓縮器及各第二壓縮器的出口處。Preferably, the compression and cooling steps further use at least one cooler positioned after the first compressor and/or after the at least one second compressor. This cooler uses a heat transfer fluid such as air or water from a cooling source (e.g., an ambient cooling source). Preferably, such a cooler is directly connected to the outlet of the first compressor and each second compressor.
藉由使用冷卻器，除熱交換器之外，本發明亦可減小熱交換器的大小或增加固體/氣體轉換速率。By using a cooler, in addition to a heat exchanger, the present invention can also reduce the size of the heat exchanger or increase the solid/gas conversion rate.
根據本發明的固化方法的有利特徵，壓縮及冷卻步驟進一步使用配置於所述至少一個第二壓縮器中的最後一者與熱交換器之間的熱交換器，所述熱交換器一方面接收來自膨脹步驟的一或多個氣相，且另一方面接收來自所述至少一個第二壓縮器中的最後一者的氣體。換言之，熱交換器接收來自膨脹步驟的冷氣體及剛好在其由熱交換器液化之前不太冷的氣體。因此，此不太冷的氣體在進入熱交換器之前由自膨脹步驟產生的氣體冷卻，此允許連接至熱交換器的冷卻鏈消耗較少能量。According to an advantageous feature of the solidification method of the invention, the compression and cooling step further uses a heat exchanger arranged between the last of the at least one second compressor and a heat exchanger, the heat exchanger receiving on the one hand one or more gas phases from the expansion step and on the other hand gas from the last of the at least one second compressor. In other words, the heat exchanger receives the cold gas from the expansion step and the gas that is not too cold just before it is liquefied by the heat exchanger. Therefore, this not too cold gas is cooled by the gas generated by the expansion step before entering the heat exchanger, which allows the cooling chain connected to the heat exchanger to consume less energy.
根據本發明的固化方法的另一有利特徵，壓縮及冷卻步驟進一步使用配置於所述熱交換器與用於膨脹步驟中的膨脹閥之間的熱交換器，所述熱交換器一方面接收由膨脹步驟產生的一或多個氣相，且另一方面接收來自所述熱交換器的處於液態的氣體。換言之，此其他熱交換器接收來自膨脹步驟的冷氣體及剛好在其由膨脹閥（特別在整個第一膨脹子步驟期間使用的膨脹閥）膨脹之前的不太冷的液體。因此，此不太冷的液體在進入膨脹閥之前由自膨脹步驟產生的氣體冷卻，此允許連接至熱交換器的冷卻鏈消耗更少能量或增加固體/氣體轉換率。According to another advantageous feature of the curing method of the invention, the compression and cooling step further uses a heat exchanger arranged between the heat exchanger and the expansion valve used in the expansion step, the heat exchanger receiving on the one hand one or more gas phases produced by the expansion step and on the other hand gas in liquid form from the heat exchanger. In other words, this further heat exchanger receives the cold gas from the expansion step and the not-so-cold liquid just before it is expanded by the expansion valve, in particular the expansion valve used during the entire first expansion sub-step. Therefore, this not-so-cold liquid is cooled by the gas produced by the self-expansion step before entering the expansion valve, which allows the cooling chain connected to the heat exchanger to consume less energy or to increase the solid/gas conversion rate.
本發明進一步是關於一種用於固化氣體的系統，所述氣體由三相點高於大氣壓力的分子物質形成，所述系統包括： -用於在大氣壓力下接收氣體的構件， -第一壓縮器，能夠自接收構件接收氣體且用於在其輸出處供應壓力大於大氣壓力的氣體， -至少一個第二壓縮器，位於第一壓縮器的出口處，能夠接收壓力大於大氣壓力的氣體且壓縮所述氣體， -至少一個熱交換器，組態以實現製冷劑流體與由所述至少一個第二壓縮器壓縮的氣體之間的熱交換，且能夠供應處於液態的分子物質作為輸出， -用於使在熱交換器的出口處獲得的液體膨脹的構件， 固化系統的特徵在於，膨脹構件包括至少一個能夠供應壓力大於三相點的壓力的液相及氣相的第一膨脹閥，及在所述至少一個第一膨脹閥的出口處的最終膨脹閥，所述最終膨脹閥能夠在大氣壓力下自在所述至少一個第一膨脹閥的出口處獲得的液相供應固相及氣相，且固化系統包括用於在所述至少一個第二壓縮器的入口處再循環壓力大於三相點的壓力的氣相的構件。 The invention further relates to a system for solidifying a gas formed by a molecular substance having a triple point higher than atmospheric pressure, the system comprising: - a member for receiving the gas at atmospheric pressure, - a first compressor capable of receiving the gas from the receiving member and for supplying the gas at a pressure greater than atmospheric pressure at its output, - at least one second compressor, located at the outlet of the first compressor, capable of receiving the gas at a pressure greater than atmospheric pressure and compressing the gas, - at least one heat exchanger, configured to achieve heat exchange between a refrigerant fluid and the gas compressed by the at least one second compressor, and capable of supplying the molecular substance in a liquid state as an output, - means for expanding the liquid obtained at the outlet of the heat exchanger, The curing system is characterized in that the expansion means comprises at least one first expansion valve capable of supplying a liquid phase and a gas phase at a pressure greater than the triple point, and a final expansion valve at the outlet of the at least one first expansion valve, the final expansion valve being capable of supplying a solid phase and a gas phase at atmospheric pressure from the liquid phase obtained at the outlet of the at least one first expansion valve, and the curing system comprises means for recycling a gas phase at a pressure greater than the triple point at the inlet of the at least one second compressor.
較佳地，根據本發明的氣體固化系統包括在其入口處連接至所述至少一個第一膨脹閥的出口的相分離器，相分離器包括連接至最後一個膨脹閥的重相排出口及連接至所述至少一個第二壓縮器的入口的輕相排出口。重相為液相，輕相為氣相。Preferably, the gas solidification system according to the present invention comprises a phase separator connected to the outlet of the at least one first expansion valve at its inlet, the phase separator comprising a heavy phase outlet connected to the last expansion valve and a light phase outlet connected to the inlet of the at least one second compressor. The heavy phase is a liquid phase and the light phase is a gas phase.
再次較佳地，根據本發明的氣體固化系統包括連接於最後一個第一膨脹閥的入口處的相分離器，相分離器包括供應固相的重相排出口及連接至第一壓縮器的入口的輕相排出口。此處，輕相亦為氣相。Preferably again, the gas solidification system according to the present invention comprises a phase separator connected to the inlet of the last first expansion valve, the phase separator comprising a heavy phase discharge port supplying the solid phase and a light phase discharge port connected to the inlet of the first compressor. Here, the light phase is also a gas phase.
在一個實施例中，根據本發明的固化系統包括若干第一膨脹閥及至少一樣多的第二壓縮器，所述第二壓縮器中的各第二壓縮器在其入口處接收由在來自第一壓縮器及第二壓縮器中的第二壓縮器之前的壓縮器壓縮且壓力大於三相點的壓力的氣體，亦接收來自第一膨脹閥中的一者的氣相，所述氣相的壓力與所述第二壓縮器的入口處的壓力相同。實際上，第一膨脹閥中的所述一者經組態以提供氣相，所述氣相的壓力與所述第二壓縮器的入口處的氣相實質上相同。In one embodiment, the curing system according to the present invention comprises a plurality of first expansion valves and at least as many second compressors, each of the second compressors receiving at its inlet a gas compressed by a compressor preceding the first compressor and the second compressor of the second compressor and having a pressure greater than the pressure of the triple point, and also receiving a gas phase from one of the first expansion valves, the pressure of which is the same as the pressure at the inlet of the second compressor. In fact, the one of the first expansion valves is configured to provide a gas phase, the pressure of which is substantially the same as the pressure at the inlet of the second compressor.
有利地，根據本發明的固化系統更包括配置於所述至少一個第二壓縮器中的最後一者與熱交換器之間的熱交換器，熱交換器一方面能夠接收來自所述至少一個第一膨脹閥及/或來自最後一個膨脹閥的一或多個氣相，且另一方面接收來自所述至少一個第二壓縮器中的最後一者的氣體。Advantageously, the curing system according to the present invention further comprises a heat exchanger arranged between the last of the at least one second compressor and the heat exchanger, the heat exchanger being capable of receiving one or more gas phases from the at least one first expansion valve and/or from the last expansion valve on the one hand, and receiving gas from the last of the at least one second compressor on the other hand.
甚至更有利地，根據本發明的固化系統更包括配置於熱交換器與所述至少一個第一膨脹閥之間的熱交換器，熱交換器一方面能夠接收來自所述至少一個第一膨脹閥及/或來自最後一個膨脹閥的一或多個氣相，且另一方面接收來自熱交換器的處於液態的氣體。Even more advantageously, the curing system according to the present invention further comprises a heat exchanger arranged between the heat exchanger and the at least one first expansion valve, the heat exchanger being capable of receiving one or more gas phases from the at least one first expansion valve and/or from the last expansion valve on the one hand, and receiving gas in liquid state from the heat exchanger on the other hand.
較佳地，根據本發明的固化系統更包括定位於第一壓縮器及/或所述至少一個第二壓縮器後的至少一個冷卻器。Preferably, the curing system according to the present invention further comprises at least one cooler positioned after the first compressor and/or the at least one second compressor.
根據本發明的固化系統具有與根據本發明的固化方法的優點類似的優點。The curing system according to the invention has advantages similar to those of the curing method according to the invention.
根據本發明的第一實施例，圖1中所繪示的根據本發明的固化氣體的方法1在圖2所繪示的根據本發明的氣體固化系統2中實施。以根據本發明的此用於固化氣體的方法1固化二氧化碳。然而，固化方法1可轉換為乙炔氣體的固化。According to the first embodiment of the present invention, the method 1 for solidifying gas according to the present invention shown in FIG1 is implemented in the gas solidification system 2 according to the present invention shown in FIG2. Carbon dioxide is solidified by this method 1 for solidifying gas according to the present invention. However, the solidification method 1 can be converted to solidification of acetylene gas.
如圖1所繪示，根據本發明的固化氣體的方法1包括在大氣壓力下接收二氧化碳氣體Cg（參考圖2）的第一步驟12。在本發明的此實施例中，在室溫下，例如在20℃與30℃（攝氏度）之間，在固化系統2的氣體入口管線中接收氣體Cg。As shown in Figure 1, the method 1 of curing gas according to the present invention includes a first step 12 of receiving carbon dioxide gas Cg (refer to Figure 2) under atmospheric pressure. In this embodiment of the present invention, the gas Cg is received in the gas inlet pipeline of the curing system 2 at room temperature, for example between 20°C and 30°C (Celsius).
固化方法1的第二步驟14為壓縮及冷卻氣體Cg直至其完全液化。在此第二壓縮及冷卻步驟14中，使用第一壓縮器22，其中引入在第一步驟12期間接收的氣體Cg，第一壓縮器22使氣體Cg在例如6巴的壓力下離開，第一壓縮器22例如為活塞壓縮器或離心壓縮器。接著藉助於冷卻器24冷卻由第一壓縮器22壓縮的氣體Cg，所述冷卻器一方面接收熱傳遞流體H2O，此處為來自在開放迴路中循環的冷源的水，且另一方面接收由第一壓縮器22壓縮的氣體Cg。The second step 14 of the solidification method 1 is to compress and cool the gas Cg until it is completely liquefied. In this second compression and cooling step 14, a first compressor 22 is used, into which the gas Cg received during the first step 12 is introduced, and the first compressor 22 makes the gas Cg leave at a pressure of, for example, 6 bar, the first compressor 22 being, for example, a piston compressor or a centrifugal compressor. The gas Cg compressed by the first compressor 22 is then cooled by means of a cooler 24 which receives on the one hand a heat transfer fluid H2O, here water from a cold source circulating in an open loop, and on the other hand the gas Cg compressed by the first compressor 22.
壓縮及冷卻氣體Cg的第二步驟14進一步使用第二壓縮器26，將先前壓縮及冷卻的氣體Cg吸入第二壓縮器中，此第二壓縮器26使氣體Cg達到例如15巴的壓力，第二壓縮器26例如為活塞壓縮器或離心壓縮器。此第二壓縮器26亦在其入口處接收由後續膨脹步驟產生的氣體，此將稍後看到。第二壓縮器26的出口處的冷卻器28將氣體Cg冷卻至15巴。為此，冷卻器28使用與冷卻器24相同的冷源。The second step 14 of compressing and cooling the gas Cg further uses a second compressor 26, into which the previously compressed and cooled gas Cg is sucked, and this second compressor 26 brings the gas Cg to a pressure of, for example, 15 bar, and the second compressor 26 is, for example, a piston compressor or a centrifugal compressor. This second compressor 26 also receives at its inlet the gas produced by the subsequent expansion step, which will be seen later. The cooler 28 at the outlet of the second compressor 26 cools the gas Cg to 15 bar. For this purpose, the cooler 28 uses the same cold source as the cooler 24.
作為變體，藉由使用多於兩個壓縮器而使氣體達到此15巴的壓力。因此，在此變體的壓縮鏈中，第一壓縮器後為冷卻器，接著若干「第二」壓縮器，在所述第二壓縮器之間連接有冷卻器，此鏈的最後一個壓縮器亦在其出口處連接至冷卻器。此變體使得可在不同壓力下再循環由後續膨脹步驟產生的氣體，如下文將描述。As a variant, the gas reaches this pressure of 15 bar by using more than two compressors. Thus, in the compression chain of this variant, a first compressor is followed by a cooler, followed by a number of "second" compressors between which coolers are connected, the last compressor of the chain also being connected at its outlet to a cooler. This variant makes it possible to recycle the gas resulting from a subsequent expansion step at a different pressure, as will be described below.
在如同本發明的主要實施例的此替代實施例中，較佳地使二氧化碳氣體Cg在壓縮鏈的出口處達到10巴至20巴的最佳範圍內，15巴僅作為指示在上文提及，且對應於較佳值，由於自能量角度來說其實質上為最佳的。壓縮鏈的出口處的壓力範圍可視情況地在大約幾十巴的範圍內延伸，此取決於所選擇製冷劑流體且不改變根據本發明的方法的性質。In this alternative embodiment like the main embodiment of the present invention, it is preferred to make the carbon dioxide gas Cg reach the optimal range of 10 bar to 20 bar at the outlet of the compression chain, 15 bar is mentioned above only as an indication and corresponds to the preferred value, because it is substantially optimal from an energy point of view. The pressure range at the outlet of the compression chain can be extended in the range of about several tens of bars as appropriate, which depends on the selected refrigerant fluid and does not change the nature of the method according to the present invention.
同樣地，第一壓縮器22使二氧化碳達到可不同於6巴的壓力，例如達到5.3巴，以便保持高於三相點的壓力。實際上，在此第一實施例中，在第二壓縮器26的入口處再循環由第一膨脹子步驟產生的氣相，此氣相在壓力方面高於三相點，如下文所解釋。Likewise, the first compressor 22 brings the carbon dioxide to a pressure which may be different from 6 bar, for example to 5.3 bar, so as to maintain a pressure above the triple point. In practice, in this first embodiment, the gas phase resulting from the first expansion substep is recycled at the inlet of the second compressor 26, this gas phase being at a pressure above the triple point, as explained below.
在此第二壓縮及冷卻步驟14中，在通過第二冷卻器28（或在根據替代實施例中的最後一個第二壓縮器的冷卻器的出口處）之後達到15巴且冷卻至例如20攝氏度與30攝氏度之間的溫度的二氧化碳氣體Cg通過熱交換器30（此處，內部熱交換器）來進一步冷卻。熱交換器30亦由較低溫度的氣體橫穿，此由後續膨脹步驟產生，如下文所解釋。熱交換器30的出口處的二氧化碳氣體Cg處於例如0攝氏度與10攝氏度之間的溫度。In this second compression and cooling step 14, the carbon dioxide gas Cg, which reaches 15 bar and is cooled to a temperature of, for example, between 20 and 30 degrees Celsius after passing through the second cooler 28 (or at the outlet of the cooler of the last second compressor according to an alternative embodiment), is further cooled by passing through a heat exchanger 30 (here, an internal heat exchanger). The heat exchanger 30 is also traversed by gas of lower temperature, which is produced by a subsequent expansion step, as explained below. The carbon dioxide gas Cg at the outlet of the heat exchanger 30 is at a temperature of, for example, between 0 and 10 degrees Celsius.
接著，由熱交換器30冷卻的二氧化碳氣體Cg通過熱交換器32，其中循環製冷劑流體FR，例如氨，且藉由使二氧化碳Cg達到-28℃來使其液化。製冷劑流體FR在與二氧化碳氣體Cg的循環分離的制冷系統34的閉合迴路中循環。作為變體，製冷劑流體FR為丙烷或丙烯。作為變體，制冷系統34使用若干冷卻溫度，使用若干冷卻流體循環迴路，各迴路執行熱力循環。Next, the carbon dioxide gas Cg cooled by the heat exchanger 30 passes through the heat exchanger 32, in which a refrigerant fluid FR, such as ammonia, circulates, and the carbon dioxide Cg is liquefied by bringing it to -28°C. The refrigerant fluid FR circulates in a closed loop of a refrigeration system 34 separated from the circulation of the carbon dioxide gas Cg. As a variant, the refrigerant fluid FR is propane or propylene. As a variant, the refrigeration system 34 uses several cooling temperatures and several cooling fluid circulation circuits, and each circuit performs a thermodynamic cycle.
最終，在此第二壓縮及冷卻步驟14中，將由熱交換器32液化的二氧化碳Cg引入至另一熱交換器36的入口，例如內部熱交換器，所述熱交換器同時接收溫度低於液化二氧化碳Cg的溫度的氣體，所述氣體由後續膨脹步驟產生，如下文所解釋。另一熱交換器36的出口處的液化二氧化碳Cg處於-31攝氏度與-40攝氏度之間的溫度。Finally, in this second compression and cooling step 14, the carbon dioxide Cg liquefied by the heat exchanger 32 is introduced to the inlet of another heat exchanger 36, for example an internal heat exchanger, which simultaneously receives a gas having a temperature lower than that of the liquefied carbon dioxide Cg, which is produced by a subsequent expansion step, as explained below. The liquefied carbon dioxide Cg at the outlet of the other heat exchanger 36 is at a temperature between -31 degrees Celsius and -40 degrees Celsius.
熱交換器30及熱交換器36使得能夠節省用以液化二氧化碳氣體Cg的能量且增加氣體/固體轉換率。替代地，僅使用熱交換器32，且在此情況下，制冷系統34的大小設定為僅確保在由冷卻器24及冷卻器28進行的冷卻二氧化碳Cg之後、在後續膨脹步驟之前的此液化。在另一變體中，除熱交換器32外，亦使用單個熱交換器30或熱交換器36。Heat exchangers 30 and 36 make it possible to save energy for liquefying carbon dioxide gas Cg and to increase the gas/solid conversion rate. Alternatively, only heat exchanger 32 is used and, in this case, the refrigeration system 34 is dimensioned to ensure only this liquefaction after the cooling of carbon dioxide Cg by coolers 24 and 28 and before the subsequent expansion step. In another variant, a single heat exchanger 30 or heat exchanger 36 is used in addition to heat exchanger 32.
由熱交換器36進行的二氧化碳的子冷卻使得有可能增加氣體/固體轉換率且因此減小第一壓縮器24及第二壓縮器26的大小以及其消耗。The sub-cooling of the carbon dioxide by the heat exchanger 36 makes it possible to increase the gas/solid conversion rate and thus reduce the size of the first compressor 24 and the second compressor 26 and their consumption.
在此第二壓縮及冷卻步驟14結束時，二氧化碳Cg因此為處於約15巴、大於5.2巴的壓力的液體，且因此大於三相點的壓力（5.2巴、-56.6℃）。At the end of this second compression and cooling step 14, the carbon dioxide Cg is therefore a liquid at about 15 bar, a pressure greater than 5.2 bar and therefore greater than the pressure of the triple point (5.2 bar, -56.6°C).
下一步驟16為由壓縮及冷卻步驟14產生的處於液態的氣體的膨脹。此氣體膨脹步驟16包括第一膨脹子步驟162，其中將此液態二氧化碳Cg發送至第一膨脹閥38，從而將此液態二氧化碳Cg的壓力降低至小於15巴但大於5.2巴的壓力，例如高達6巴或7巴，以免達到三相點。因此，此第一膨脹在第一膨脹閥38的出口處在相分離器40中產生液相φl及第一氣相φg1，所述液相表示在第一膨脹閥38的入口處的液態二氧化碳Cg的約92%，所述第一氣相表示剩餘8%，這些相的溫度低於第一膨脹閥38的入口但大於-56.6℃。The next step 16 is the expansion of the gas in the liquid state produced by the compression and cooling step 14. The gas expansion step 16 includes a first expansion sub-step 162, in which the liquid carbon dioxide Cg is sent to the first expansion valve 38, thereby reducing the pressure of the liquid carbon dioxide Cg to a pressure less than 15 bar but greater than 5.2 bar, for example, up to 6 bar or 7 bar, so as not to reach the triple point. Therefore, this first expansion produces a liquid phase φl and a first gas phase φg1 in the phase separator 40 at the outlet of the first expansion valve 38, wherein the liquid phase represents about 92% of the liquid carbon dioxide Cg at the inlet of the first expansion valve 38, and the first gas phase represents the remaining 8%, and the temperature of these phases is lower than that at the inlet of the first expansion valve 38 but greater than -56.6°C.
相分離器40的出口處的第一氣相φg1發送至第二壓縮器26的入口，通過熱交換器30及熱交換器36。此第一氣相φg1在第一壓縮器22的出口處與來自冷卻器24的二氧化碳Cg實質上處於相同壓力，且因此可在第二壓縮器26的入口處容易地與此二氧化碳Cg混合。The first gas phase φg1 at the outlet of the phase separator 40 is sent to the inlet of the second compressor 26, passing through the heat exchanger 30 and the heat exchanger 36. This first gas phase φg1 is substantially at the same pressure as the carbon dioxide Cg from the cooler 24 at the outlet of the first compressor 22, and can therefore be easily mixed with this carbon dioxide Cg at the inlet of the second compressor 26.
在使用若干第二壓縮器的本發明的替代實施例中，膨脹步驟16包括例如與接收壓力大於三相點的二氧化碳的第二壓縮器一樣多的第一連續膨脹子步驟，這些第一膨脹子步驟中的最後一者使液態二氧化碳Cg達到仍大於5.2巴的壓力。各第一膨脹子步驟使用單獨膨脹閥，產生對應第一氣相及對應液相。由這些第一膨脹子步驟產生的各第一氣相接著發送至第二壓縮器中的一者的入口，所述第二壓縮器接收來自先前壓縮器的具有與對應氣相的壓力實質上相同的壓力的二氧化碳Cg。較佳地，這些第一氣相全部通過熱交換器30及熱交換器36以冷卻來自第一壓縮器22的二氧化碳Cg。In an alternative embodiment of the invention using several second compressors, the expansion step 16 comprises, for example, as many first consecutive expansion sub-steps as there are second compressors receiving carbon dioxide at a pressure greater than the triple point, the last of these first expansion sub-steps bringing the liquid carbon dioxide Cg to a pressure still greater than 5.2 bar. Each first expansion sub-step uses a separate expansion valve, producing a corresponding first gas phase and a corresponding liquid phase. Each first gas phase produced by these first expansion sub-steps is then sent to the inlet of one of the second compressors, which receives carbon dioxide Cg from the previous compressor at a pressure substantially the same as the pressure of the corresponding gas phase. Preferably, all of the first gas phases pass through the heat exchanger 30 and the heat exchanger 36 to cool the carbon dioxide Cg from the first compressor 22.
參考本發明的主要實施例，膨脹處於液態的氣體的步驟16包括在大氣壓力下自在第一膨脹子步驟162期間獲得的液相φl產生固相φs及第二氣相φg2的最終膨脹子步驟164。固相φs及第二氣相φg2藉由此最後一個膨脹子步驟達到-78℃的溫度。Referring to the main embodiment of the present invention, the step 16 of expanding the gas in the liquid state includes a final expansion sub-step 164 of producing a solid phase φs and a second gas phase φg2 under atmospheric pressure from the liquid phase φ1 obtained during the first expansion sub-step 162. The solid phase φs and the second gas phase φg2 reach a temperature of -78°C by this final expansion sub-step.
為此，將相分離器40中的液相φl發送至第二膨脹閥42的入口，從而將此液相φl的壓力降低至大氣壓力。第二膨脹閥42在其出口處連接至第二相分離器44，使得能夠回收固相φs及第二氣相φg2，所述固相表示在此第二膨脹閥42的入口處的二氧化碳Cg的液相φl的57%，所述第二氣相表示剩餘43%。當第二膨脹閥42的入口處的液相φl的溫度低時，以固相獲得的二氧化碳Cg的百分比更大。For this purpose, the liquid phase φ1 in the phase separator 40 is sent to the inlet of the second expansion valve 42, thereby reducing the pressure of this liquid phase φ1 to atmospheric pressure. The second expansion valve 42 is connected to the second phase separator 44 at its outlet, making it possible to recover a solid phase φs, which represents 57% of the liquid phase φ1 of the carbon dioxide Cg at the inlet of this second expansion valve 42, and a second gas phase φg2, which represents the remaining 43%. When the temperature of the liquid phase φ1 at the inlet of the second expansion valve 42 is low, the percentage of carbon dioxide Cg obtained in the solid phase is greater.
相分離器44的出口處的第二氣相φg2發送至第一壓縮器22的入口，穿過熱交換器30及熱交換器36。因此，此第二氣相φg2冷卻在熱交換器32的出口處及第二壓縮器26的出口處的二氧化碳Cg，並且第一氣相φg1亦冷卻在熱交換器32的出口處及第二壓縮器26的出口處的二氧化碳Cg，亦進入熱交換器30及熱交換器36。The second gas phase φg2 at the outlet of the phase separator 44 is sent to the inlet of the first compressor 22, passing through the heat exchanger 30 and the heat exchanger 36. Therefore, the second gas phase φg2 cools the carbon dioxide Cg at the outlet of the heat exchanger 32 and the outlet of the second compressor 26, and the first gas phase φg1 also cools the carbon dioxide Cg at the outlet of the heat exchanger 32 and the outlet of the second compressor 26, and also enters the heat exchanger 30 and the heat exchanger 36.
類似地，在使用若干第二壓縮器的本發明的替代實施例中，在最後一個膨脹子步驟之後，最終膨脹閥放鬆在最後一個第一膨脹子步驟期間獲得的液相，以便在分離器中獲得固相及氣相，氣相在第一壓縮器22的入口處再循環。Similarly, in an alternative embodiment of the invention using several second compressors, after the last expansion sub-step, the final expansion valve relaxes the liquid phase obtained during the last first expansion sub-step so as to obtain a solid phase and a gas phase in the separator, and the gas phase is recycled at the inlet of the first compressor 22.
由此描述的根據本發明的固化系統2相對於先前技術在能量消耗方面是最佳化的。特別地，藉助於兩個膨脹子步驟中的膨脹步驟16且藉助於熱交換器30及熱交換器36，相對於不包括這些特徵的固化系統實現30%的能源節省。The curing system 2 according to the invention thus described is optimized in terms of energy consumption relative to the prior art. In particular, by means of the expansion step 16 of the two expansion sub-steps and by means of the heat exchanger 30 and the heat exchanger 36, an energy saving of 30% is achieved relative to a curing system that does not include these features.
根據本發明的第二實施例，根據本發明的固化氣體的方法1在如圖3所繪示的根據本發明的氣體固化系統20中實施，以固化二氧化碳氣體。固化系統20包括大量與二氧化碳固化系統2相同的元件，因此以相同方式引用所述元件且不進行詳細說明。According to the second embodiment of the present invention, the method 1 for curing gas according to the present invention is implemented in a gas curing system 20 according to the present invention as shown in FIG3 to cure carbon dioxide gas. The curing system 20 includes a large number of the same elements as the carbon dioxide curing system 2, and thus the elements are referenced in the same manner and are not described in detail.
在本發明的此第二實施例中，在接收氣體的步驟12中，在室溫下，例如在20℃與30℃（攝氏度）之間，在固化系統20的氣體入口管線中接收氣體Cg。In this second embodiment of the invention, in the step 12 of receiving gas, gas Cg is received in the gas inlet line of the curing system 20 at room temperature, for example between 20° C. and 30° C. (degrees Celsius).
在固化方法1的第二步驟14期間，壓縮及冷卻氣體Cg直至其完全液化。在此第二實施例中，使用三個壓縮器： -第一壓縮器52，例如具有低壓縮比的離心壓縮器，使在第一步驟12期間接收的氣體Cg達到例如2.6巴的壓力。由第一壓縮器52壓縮的氣體Cg接著藉助於冷卻器53冷卻，所述冷卻器一方面接收熱傳遞流體H2O，且另一方面接收由第一壓縮器52壓縮的氣體Cg。 -第二壓縮器54，例如具有低壓縮比的離心壓縮器，使先前由第一壓縮器52壓縮及冷卻的氣體Cg達到例如6.6巴的壓力。第二壓縮器54的出口處的冷卻器55用熱傳遞流體H2O使氣體Cg冷卻至6.6巴。 -第三壓縮器56使先前由第二壓縮器54壓縮及冷卻的氣體Cg達到例如14.9巴的壓力。此第三壓縮器56亦在其輸入處接收由第一膨脹子步驟162產生的氣體，此將稍後看到。第三壓縮器56出口處的冷卻器57使用熱傳遞流體H2O使氣體Cg冷卻至14.9巴。舉例而言，第三壓縮器56為活塞壓縮器或離心壓縮器。其亦認為是本發明意義上的另一「第二壓縮器」，儘管第一壓縮器52及第二壓縮器54的作用可視為第一壓縮步驟，使氣體Cg達到足夠高的壓力，以允許後面壓縮器（下游）接收來自第一膨脹子步驟162的氣相。 During the second step 14 of the solidification method 1, the gas Cg is compressed and cooled until it is completely liquefied. In this second embodiment, three compressors are used: - A first compressor 52, for example a centrifugal compressor with a low compression ratio, brings the gas Cg received during the first step 12 to a pressure of, for example, 2.6 bar. The gas Cg compressed by the first compressor 52 is then cooled by means of a cooler 53, which receives, on the one hand, the heat transfer fluid H2O and, on the other hand, the gas Cg compressed by the first compressor 52. - A second compressor 54, for example a centrifugal compressor with a low compression ratio, brings the gas Cg previously compressed and cooled by the first compressor 52 to a pressure of, for example, 6.6 bar. A cooler 55 at the outlet of the second compressor 54 cools the gas Cg to 6.6 bar with a heat transfer fluid H2O. - A third compressor 56 brings the gas Cg previously compressed and cooled by the second compressor 54 to a pressure of, for example, 14.9 bar. This third compressor 56 also receives at its input the gas produced by the first expansion substep 162, as will be seen later. The cooler 57 at the outlet of the third compressor 56 uses the heat transfer fluid H2O to cool the gas Cg to 14.9 bar. For example, the third compressor 56 is a piston compressor or a centrifugal compressor. It is also considered to be another "second compressor" in the sense of the present invention, although the role of the first compressor 52 and the second compressor 54 can be regarded as a first compression step, so that the gas Cg reaches a sufficiently high pressure to allow the subsequent compressor (downstream) to receive the gas phase from the first expansion sub-step 162.
此藉由第一膨脹子步驟162為中間膨脹步驟的事實來解釋，所述中間膨脹步驟僅在比三相點的壓力大的壓力下才實用。至於二氧化碳，三相點處於5.2巴，此壓力為大氣壓力的5倍，藉由若干連續壓縮來壓縮二氧化碳比藉由單個壓縮更有效，從而使得能夠將二氧化碳直接壓縮至高於5.2巴。This is explained by the fact that the first expansion sub-step 162 is an intermediate expansion step, which is only practical at pressures greater than the pressure of the triple point. As for carbon dioxide, the triple point is at 5.2 bar, which is 5 times the atmospheric pressure, and it is more efficient to compress carbon dioxide by several consecutive compressions than by a single compression, thus making it possible to compress carbon dioxide directly to above 5.2 bar.
因此，在第一壓縮器52的出口處，壓力通常將小於三相點的壓力，且將需要等待第二壓縮在壓力方面超過三相點，且能夠在高於此壓力的情況下再循環來自第一膨脹子步驟的氣體。Therefore, at the outlet of the first compressor 52, the pressure will generally be less than the pressure of the triple point, and it will be necessary to wait for the second compressor to exceed the triple point in pressure and be able to recycle the gas from the first expansion sub-step at a pressure higher than this.
已使二氧化碳Cg達到14.9巴且將其冷卻至始終例如20度與30度之間的溫度的壓縮及冷卻的第二步驟14，二氧化碳仍冷卻，在此第二壓縮及冷卻步驟14中，通過熱交換器30，接著通過熱交換器32，接著通過熱交換器36，其在-31攝氏度與40攝氏度之間的溫度下完全液化離開，如同本發明的第一實施例。熱交換器30的出口處的二氧化碳Cg處於例如0攝氏度與10攝氏度之間的溫度，且在熱交換器的出口處處於-28攝氏度。The carbon dioxide Cg has been brought to 14.9 bar and cooled to a temperature of, for example, always between 20 and 30 degrees in the second compression and cooling step 14, the carbon dioxide is still cooled, in this second compression and cooling step 14, passing through the heat exchanger 30, then through the heat exchanger 32, then through the heat exchanger 36, it leaves completely liquefied at a temperature of between -31 degrees Celsius and 40 degrees Celsius, as in the first embodiment of the invention. The carbon dioxide Cg at the outlet of the heat exchanger 30 is at a temperature of, for example, between 0 degrees Celsius and 10 degrees Celsius, and at the outlet of the heat exchanger is at -28 degrees Celsius.
在此第二壓縮及冷卻步驟14結束時，二氧化碳Cg因此為液體且處於14.9巴的壓力。At the end of this second compression and cooling step 14, the carbon dioxide Cg is therefore liquid and is at a pressure of 14.9 bar.
在由壓縮及冷卻步驟14產生的處於液態的二氧化碳Cg的下一膨脹步驟16期間，處於液態的二氧化碳Cg經歷第一膨脹子步驟162，其中此液態二氧化碳Cg發送至第一膨脹閥38，從而將此液態二氧化碳Cg的壓力降低至低於14.9巴但大於5.2巴的壓力，例如高達6巴或7巴，以免達到三相點。因此，此第一膨脹在第一膨脹閥38的出口處在相分離器40中產生液相φl及第一氣相φg1，所述液相表示在第一膨脹閥38的入口處的液態二氧化碳Cg的約92%，所述第一氣相表示剩餘8%，這些相的溫度低於第一膨脹閥38的入口但大於-56.6℃。During the next expansion step 16 of the liquid carbon dioxide Cg produced by the compression and cooling step 14, the liquid carbon dioxide Cg undergoes a first expansion sub-step 162, wherein the liquid carbon dioxide Cg is sent to the first expansion valve 38, thereby reducing the pressure of the liquid carbon dioxide Cg to a pressure lower than 14.9 bar but greater than 5.2 bar, for example, up to 6 bar or 7 bar, so as to avoid reaching the triple point. Therefore, this first expansion produces a liquid phase φl and a first gas phase φg1 in the phase separator 40 at the outlet of the first expansion valve 38, wherein the liquid phase represents about 92% of the liquid carbon dioxide Cg at the inlet of the first expansion valve 38, and the first gas phase represents the remaining 8%, and the temperature of these phases is lower than that at the inlet of the first expansion valve 38 but greater than -56.6°C.
相分離器40的出口處的第一氣相φg1發送至第三壓縮器56的入口，通過熱交換器30及熱交換器36，由此冷卻自第三壓縮器56循環至第一膨脹閥38的二氧化碳。此第一氣相φg1在第二壓縮器54的出口處與來自冷卻器55的二氧化碳Cg實質上處於相同壓力，且因此可在第三壓縮器56的入口處容易地與此二氧化碳Cg混合。The first gas phase φg1 at the outlet of the phase separator 40 is sent to the inlet of the third compressor 56, passes through the heat exchanger 30 and the heat exchanger 36, thereby cooling the carbon dioxide circulated from the third compressor 56 to the first expansion valve 38. This first gas phase φg1 is substantially at the same pressure as the carbon dioxide Cg from the cooler 55 at the outlet of the second compressor 54, and can therefore be easily mixed with this carbon dioxide Cg at the inlet of the third compressor 56.
最終，在最後一個膨脹子步驟164期間，後者在大氣壓力下自在第一膨脹子步驟162期間獲得的液相φl產生固相φs及第二氣相φg2。固相φs及第二氣相φg2藉由此最後一個膨脹子步驟達到-78℃的溫度。Finally, during the last expansion sub-step 164, the latter produces a solid phase φs and a second gas phase φg2 under atmospheric pressure from the liquid phase φl obtained during the first expansion sub-step 162. The solid phase φs and the second gas phase φg2 reach a temperature of -78°C by this last expansion sub-step.
相分離器44的出口處的第二氣相φg2再循環至第一壓縮器52的入口，通過熱交換器30及熱交換器36，此使得有可能冷卻自第三壓縮器56循環至第一膨脹閥38的二氧化碳。當然，本發明不限於剛剛描述的實例，且可在不脫離本發的範疇的情況下對這些實例進行多次修改。The second gas phase φg2 at the outlet of the phase separator 44 is recycled to the inlet of the first compressor 52, passing through the heat exchanger 30 and the heat exchanger 36, which makes it possible to cool the carbon dioxide circulated from the third compressor 56 to the first expansion valve 38. Of course, the present invention is not limited to the examples just described, and these examples can be modified many times without departing from the scope of the present invention.
1:固化方法 2、20:固化系統 12:第一步驟 14:第二步驟/壓縮及冷卻步驟 16:膨脹步驟 22、52:第一壓縮器 24、53、55、57:冷卻器 26、54:第二壓縮器 28:第二冷卻器 30、32、36:熱交換器 34:制冷系統 38:第一膨脹閥 40:相分離器 42:第二膨脹閥 44:第二相分離器 56:第三壓縮器 162:第一膨脹子步驟 164:最後一個膨脹子步驟 Cg:氣體/二氧化碳 H2O:熱傳遞流體 FR:製冷劑流體 φl:液相 φg1:第一氣相 φg2:第二氣相 φs:固相 1: Curing method 2, 20: Curing system 12: First step 14: Second step/Compression and cooling step 16: Expansion step 22, 52: First compressor 24, 53, 55, 57: Cooler 26, 54: Second compressor 28: Second cooler 30, 32, 36: Heat exchanger 34: Refrigeration system 38: First expansion valve 40: Phase separator 42: Second expansion valve 44: Second phase separator 56: Third compressor 162: First expansion sub-step 164: Last expansion sub-step Cg: gas/carbon dioxide H2O: heat transfer fluid FR: refrigerant fluid φl: liquid phase φg1: first gas phase φg2: second gas phase φs: solid phase
本發明的其他特徵及優點將自以下描述及自若干實例實施例兩者呈現，所述實例實施例出於說明的目的而給出且不限於參考隨附示意性圖式，其中： 圖1繪示根據本發明的用於固化氣體的方法的步驟。 圖2示意性地繪示根據本發明的第一實施例實施圖1的固化方法的根據本發明的氣體固化系統。 圖3示意性地繪示根據本發明的第二實施例實施圖1的固化方法的根據本發明的氣體固化系統。 Other features and advantages of the invention will emerge both from the following description and from several example embodiments, which are given for illustrative purposes and are not limited to reference to the accompanying schematic drawings, in which: FIG. 1 shows the steps of a method for curing a gas according to the invention. FIG. 2 schematically shows a gas curing system according to the invention for implementing the curing method of FIG. 1 according to a first embodiment of the invention. FIG. 3 schematically shows a gas curing system according to the invention for implementing the curing method of FIG. 1 according to a second embodiment of the invention.
2:固化系統 2: Curing system
22:第一壓縮器 22: First compressor
24:冷卻器 24: Cooler
26:第二壓縮器 26: Second compressor
28:第二冷卻器 28: Second cooler
30、32、36:熱交換器 30, 32, 36: Heat exchanger
34:制冷系統 34: Refrigeration system
38:第一膨脹閥 38: First expansion valve
40:相分離器 40: Phase separator
42:第二膨脹閥 42: Second expansion valve
44:第二相分離器 44: Second phase separator
Cg:氣體/二氧化碳 Cg: Gas/Carbon Dioxide
H2O:熱傳遞流體 H2O: Heat transfer fluid
FR:製冷劑流體 FR: Refrigerant fluid
φ1:液相 φ1: Liquid phase
φg1:第一氣相 φg1: first gas phase
φg2:第二氣相 φg2: Second gas phase
φs:固相 φs: solid phase
Claims (13)
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR2209747 | 2022-09-26 |
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| Publication Number | Publication Date |
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| TW202419798A true TW202419798A (en) | 2024-05-16 |
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