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- JP2012529616A5 JP2012529616A5 JP2012514517A JP2012514517A JP2012529616A5 JP 2012529616 A5 JP2012529616 A5 JP 2012529616A5 JP 2012514517 A JP2012514517 A JP 2012514517A JP 2012514517 A JP2012514517 A JP 2012514517A JP 2012529616 A5 JP2012529616 A5 JP 2012529616A5
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本発明は、低温蒸留による空気分離のための装置及び方法に関する。 The present invention relates to an apparatus and method for air separation by cryogenic distillation.
空気分離のための通常の（「門」型（”double column” type）の）装置は：
・蒸発器によって熱交換が行われる低圧塔を、中圧塔の上に設置し；
・低圧塔および中圧塔を、液体返還（液体酸素を低圧塔から蒸発−凝縮器へ、もしくは液体窒素を蒸発−凝縮器から中圧塔へ）ポンプおよびガスの輸送（蒸発−凝縮器から低圧塔へガス状酸素を返還し、中圧塔から蒸発−凝縮器にガス状窒素を送る）のためのパイプと併設することが知られる。
The usual ("gate" type) device for air separation is:
-A low-pressure column where heat is exchanged by the evaporator is installed above the medium- pressure column ;
• Low pressure and medium pressure towers with liquid return (liquid oxygen from low pressure column to evaporation-condenser, or liquid nitrogen from evaporation-condenser to medium pressure tower ) pump and gas transport (evaporation-condenser to low pressure It is known to be provided with a pipe for returning gaseous oxygen to the tower and sending gaseous nitrogen from the medium pressure tower to the evaporator-condenser.
ガス返還パイプにおける圧力の損失を減じ（優れた効果）、液体返還ポンプからのエネルギーの損失を減ずるため、最初の配置がエネルギー効率の向上を可能にすることが知られる。 It is known that the initial arrangement allows for increased energy efficiency in order to reduce the pressure loss in the gas return pipe (excellent effect) and reduce the loss of energy from the liquid return pump.
低圧塔において二つの蒸発−凝縮器を有する空気分離のための装置は、以下のような設備として知られる：
・配置１：低圧塔（二つの蒸発器を備える）を中圧塔の上に設置する（仏国特許出願公開第２７２４０１１号明細書、図１および４）。
An apparatus for air separation with two evaporation-condensers in a low-pressure column is known as the following equipment:
Arrangement 1: A low-pressure column (with two evaporators) is installed on top of a medium- pressure column (French Patent Application No. 2724011, FIGS. 1 and 4).
・配置２：中圧塔の頭上の蒸発器を直接的に介して熱交換を行うように、低圧塔の底部を床面上に、そして低圧塔の頂部を中圧塔の上に設置する（仏国特許出願公開第２７２４０１１号明細書、図２および３）。 -Arrangement 2: the bottom of the low pressure column is placed on the floor and the top of the low pressure column is placed on the medium pressure column so that heat exchange is performed directly through the evaporator above the medium pressure tower ( French Patent Application No. 2724011, FIGS. 2 and 3).
・配置３：低圧塔（二つの蒸発器を備える）を中圧塔の隣に設置する（米国特許第６１３４９１５号公報、欧州特許出願公開第０１９５０６５号公報）。 Arrangement 3: A low-pressure column (with two evaporators) is installed next to a medium- pressure column (US Pat. No. 6,134,915, European Patent Application Publication No. 0195065).
配置１および２は、同等のエネルギー効率が得られ得ることが知られる。これら二つの場合において、ガスパイプにおける圧力の損失が存在するが、液体返還ポンプはない。 It is known that arrangements 1 and 2 can achieve comparable energy efficiency. In these two cases, there is a pressure loss in the gas pipe, but there is no liquid return pump.
低圧塔の上流部を床面上に、また凝縮−再沸器を含まない低圧塔の上流部についてですら配置することを提案した文献はない。 The upstream portion of the lower pressure column on the floor, also condensation - no documents even proposed to place in the upstream of the low pressure column without the reboiler.
驚くことに、低圧塔において少なくとも二つの蒸発器を持つ二つの塔を用いる非常に低エネルギーの方法のために、エネルギー消費の期間における最良の実行配置は：
− 中圧塔を床面上に配置し、
− 低圧塔の上流部を床板上に配置し、
− 低圧塔の下流部を床板上に配置する、ということになる。
Surprisingly, for a very low energy process using two columns with at least two evaporators in the low pressure column , the best performing arrangement during the period of energy consumption is:
-Place the medium pressure tower on the floor,
-The upstream part of the low pressure column is placed on the floorboard,
-The downstream part of the low-pressure column will be placed on the floorboard.
主な理由は、低圧塔の一部が中圧塔の上に設備された場合に液体を上げるためのポンプの設置を要する、中圧塔および低圧塔の間の圧力差が、一般的に絶対圧力で２バールより少ないためである。 The main reason is that requires installation of a pump for raising the liquid when a part of the lower pressure column is equipment on a medium pressure column, the pressure difference between the medium pressure column and low pressure column is generally absolute This is because the pressure is less than 2 bar.
本発明の趣旨によれば、装置は空気分離のために設けられ、中圧で運転し得る第１の蒸留塔と、低圧で運転し得る第２の蒸留塔と、低圧で、または前記低圧で運転し得る第３の蒸留塔と、第１の凝縮−蒸発器と、前記第２の塔の底部に配置された第２の凝縮−蒸発器と、少なくとも前記第１の塔に空気を供給するパイプと、前記第１の塔の上部から前記第３の塔の上部に窒素豊富な液体を供給するパイプと、前記第３の塔の底部から前記第１の凝縮−蒸発器に液体を供給する少なくとも一つのパイプと、前記第１の塔の底部から前記第３の塔に液体を供給するパイプと、前記第１の凝縮−蒸発器から前記第２の塔に液体を供給するパイプと、前記第２の塔から前記第３の塔の底部に頂部ガス(overhead gas)を供給するパイプと、を具備し、前記第１、第２、および第３の塔は、隣り合って配置され、できれば全て床面の上に配置される。 In accordance with the spirit of the invention, the apparatus is provided for air separation, a first distillation column that can be operated at medium pressure , a second distillation column that can be operated at low pressure, and at low pressure or at said low pressure. supplying an evaporator, the air in at least said first column - the third distillation column may be operated, first condenser - evaporator, the second condensing located at the bottom of the second column A pipe for supplying a nitrogen-rich liquid from the top of the first column to the top of the third column , and a liquid for supplying the liquid to the first condenser-evaporator from the bottom of the third column At least one pipe, a pipe for supplying liquid from the bottom of the first tower to the third tower , a pipe for supplying liquid from the first condenser-evaporator to the second tower , and pipe supplying top gas (overhead gas) from the second column to the bottom of the third column, comprising a said first , Second, and third columns are arranged adjacent, are all arranged on the floor surface if possible.
好ましくは、前記第２の塔は少なくとも、前記第２の凝縮−蒸発器の上に配置された第３の凝縮−蒸発器を含む。 Preferably, the second column includes at least a third condensing-evaporator disposed on the second condensing-evaporator.
極低温で運転し得る装置の要素、例えば液体酸素蒸発器は、一つの前記塔の下に配置されても良く、他の二つの前記塔および当該要素は、前記床面上に直接置かれる。 Elements of the apparatus that can operate at cryogenic temperatures, such as a liquid oxygen evaporator, may be placed under one of the towers , the other two towers and the elements being placed directly on the floor.
加圧手段が前記第２の塔の底および前記液体酸素蒸発器に接続されても良い。 A pressurizing means may be connected to the bottom of the second column and the liquid oxygen evaporator.
前記第１の凝縮−蒸発器は、前記第１の塔から来るガスによって再沸騰できるように、前記第１の塔の上にあって、前記第１の塔の上部に接続されても良い。 It said first condenser - evaporator, so that it can be reboiled by gas coming from the first column, in the top of the first column, may be connected to the upper portion of the first column.
好ましくは、当該装置は二つの前記塔に接続されたただ一つのポンプを備える。 Preferably, the apparatus comprises a single pump connected to the two towers.
前記ポンプは、前記第２の塔の底部から前記第１の凝縮−再沸器に液体を供給する二つの前記パイプに接続されても良い。 The pump may be connected to two pipes that supply liquid from the bottom of the second column to the first condenser-reboiler.
ガスパイプが前記第１の凝縮器を前記第３の塔の底部に接続しても良い。 A gas pipe may connect the first condenser to the bottom of the third column .
前記第２の塔および／または前記第３の塔の上部は、前記第１の凝縮−再沸器より低い高さにあっても良く、好ましくは前記第１の塔の上部よりも低い。 The upper portion of the second column and / or the third column may be at a lower height than the first condenser-reboiler, and is preferably lower than the upper portion of the first column .
前記第１の塔における嵩密度（packing densities）は、前記第２の塔および／または前記第３の塔における嵩密度より低くても良い。 The packing density in the first tower may be lower than the bulk density in the second tower and / or the third tower .
好ましくは、前記第３の塔は凝縮−再沸器を含まない。 Preferably, the third column does not include a condenser-reboiler.
前記第２の塔は、熱交換手段に加えて、第３の凝縮−再沸器および前記第３の凝縮−再沸器の上に配置された物をも含んでも良い。 In addition to the heat exchange means, the second column may also include a third condenser-reboiler and an object disposed on the third condenser-reboiler.
頂部ガスを前記第２の塔から前記第３の塔の底部に供給するための前記パイプは、前記第１の凝縮−再沸器で蒸発したガス用のパイプに接続しても良い。 The pipe for supplying top gas from the second column to the bottom of the third column may be connected to a pipe for gas evaporated in the first condenser-reboiler.
前記第３の塔の下に配置された前記装置の要素は、好ましくは液体酸素蒸発器である。 The element of the device arranged under the third tower is preferably a liquid oxygen evaporator.
前記第１の塔の運転圧力と前記第２および第３の塔のうち少なくとも一つの圧力との間の圧力差は、好ましくは３バールより少なく、好ましくは２．５バールであり、さらに好ましくは２バールである。 The pressure difference between the operating pressure of the first column and the pressure of at least one of the second and third columns is preferably less than 3 bar, preferably 2.5 bar, more preferably 2 bar.
前記第２の塔の上部と前記第３の塔の底部との運転圧力の圧力差は、１バールより少なくても良く、好ましくは０．５バールよりも少なく、さらに好ましくは０．２バールよりも少ない。 Pressure differential operating pressure between the bottom of the upper and the third column of the second column may be less than 1 bar, more preferably less than 0.5 bar, more preferably 0.2 bar There are few.
本発明は、本発明に係る空気分離のための装置を示す図面を参照することでさらに詳細に開示されるだろう。 The invention will be disclosed in more detail with reference to the drawings showing an apparatus for air separation according to the invention.
図１において、装置は中圧で運転する第１の塔１、低圧で運転する第２の塔２、および第２の塔２よりわずかに低い低圧で運転する第３の塔３を備え、当該低圧塔は、好ましくは塔３の底部と塔２の上部との間で測定される圧力差が５００ミリバール（好ましくは２００ミリバール）より少なくなるように運転する。それぞれの塔の中央で測定される中圧塔１および低圧塔２または３の間の圧力差は、３バールより少なく、好ましくは２．５バール、さらに好ましくは２バールである。 In Figure 1, the apparatus includes a first column 1, third column 3 operating at the second column 2, and a second slightly lower lower pressure than column 2 operating at low pressure for operating at medium pressure, the The low pressure column is preferably operated so that the pressure difference measured between the bottom of column 3 and the top of column 2 is less than 500 mbar (preferably 200 mbar). The pressure difference between the pressure column 1 and lower pressure column 2 or 3 in which is measured at the center of each column is less than 3 bar, preferably 2.5 bar, more preferably 2 bar.
三つの塔１，２，３は床面２７に配置されるが、生成物蒸発器１１が前記塔の下に配置されることで第３の塔３は持ち上げられる。蒸発器１１をどこか別の場所に配置し、塔３を直接床面２７の上に置いても当然良い。床面２７はコンクリート基礎または他の平面からなる。 Although three tower 1,2,3 are arranged on the floor 27, the third column 3 by product evaporator 11 is disposed under the tower is lifted. Of course, the evaporator 11 may be placed somewhere else and the tower 3 placed directly on the floor 27. The floor surface 27 consists of a concrete foundation or another plane.
精製されるとともに冷却された圧縮空気流３３は、区分された第１の塔１の底部に入り、酸素豊富な流れ２５および窒素豊富な流れを作る。酸素豊富な流れ２５は、第３の塔３の下層を通る。窒素豊富な流れは、第１の塔の頂部凝縮器９で凝縮する。前記凝縮器９は、第３の塔３の底部から送られ、床面２７に配置されたポンプ１３によって加圧された液体２３の流れによって冷却される。凝縮器９から蒸発した液体１７は、第２の塔２の頂部ガス１５と混合し、第３の塔３の底に供給されるガスの流れ１９を作る。第２の塔２の塔の上部に、凝縮器９から液体２１が供給される。 The purified and cooled compressed air stream 33 enters the bottom of the sectioned first column 1 to produce an oxygen rich stream 25 and a nitrogen rich stream. The oxygen rich stream 25 passes through the lower layer of the third column 3. The nitrogen rich stream condenses in the top condenser 9 of the first column . The condenser 9 is sent from the bottom of the third tower 3 and is cooled by the flow of the liquid 23 pressurized by the pump 13 disposed on the floor surface 27. The liquid 17 evaporated from the condenser 9 is mixed with the top gas 15 of the second column 2 to produce a gas stream 19 fed to the bottom of the third column 3. On top of the second column 2 of the column, the liquid 21 is supplied from the condenser 9.
第２の塔２は、底部再沸器５そしてできれば中間再沸器７を含む一つまたは二つ、またはそれ以上の再沸器を含む。前記再沸器は、冷間圧縮されたまたはされていない空気の流れ、または冷間圧縮されたまたはされていない窒素の流れを含む、何らかの適当な手段によって加熱されても良い。ガスの流れまたは液体酸素２９は、第２の塔２の下層で回収される。前記液体の流れは、ポンプ（図示せず）によって加圧されても良く、加圧されたガスの流れを作るように蒸発器１１に入れられても良い。 The second column 2 contains one or two or more reboilers including a bottom reboiler 5 and possibly an intermediate reboiler 7. The reboiler may be heated by any suitable means, including a cold compressed air stream or not, or a cold compressed air stream or not. A gas stream or liquid oxygen 29 is recovered in the lower layer of the second column 2. The liquid stream may be pressurized by a pump (not shown) or may be placed in the evaporator 11 to create a pressurized gas stream.
液体窒素の流れ３５は、バルブで膨張するとともに第３の塔３の上部に入れられ、そして窒素豊富なガス状の流れ３１は第３の塔３の上部で回収される。好ましくは、第３の塔３の上部を第１の塔１の上部よりも低くされることで、重力流によってこの輸送を容易にする
図２と図１との差異は、図１は槽型蒸発器である凝縮器９を示すのに対し、図２は薄膜型蒸発器９を示す。この場合、凝縮器から回収される流れ２１は二相流であるとともに、図１に示すように第２の塔の上部に入る。流れ１７は発生しない。
The liquid nitrogen stream 35 is expanded by a valve and placed in the upper part of the third column 3, and the nitrogen-rich gaseous stream 31 is recovered in the upper part of the third column 3. Preferably, the top of the third tower 3 is made lower than the top of the first tower 1 to facilitate this transport by gravity flow. The difference between FIG. 2 and FIG. FIG. 2 shows a thin film evaporator 9 while a condenser 9 is shown. In this case, the stream 21 recovered from the condenser is a two-phase flow and enters the top of the second column as shown in FIG. Stream 17 does not occur.
図３および４は、図１および２の変形であり、それぞれ蒸発器１１が欠けた、または一つの塔の下以外のどこか別の場所に配置された場合を示す。この場合、三つの塔は床面２７に直接置かれる。 FIGS. 3 and 4 are variations of FIGS. 1 and 2 and show the case where the evaporator 11 is missing or placed somewhere other than under one column , respectively. In this case, the three towers are placed directly on the floor 27.
図５および６は、第２の塔がただ一つの再沸器である底部再沸器５を収容する図１および２の変形をそれぞれ示す。この場合、第２の塔は当然短くなる。底部再沸器５は、できれば加圧された、またできれば冷間加圧された窒素または空気によって加熱されても良い。 FIGS. 5 and 6 show the variants of FIGS. 1 and 2, respectively, in which the second tower accommodates the bottom reboiler 5, which is a single reboiler. In this case, the second tower is naturally shorter. The bottom reboiler 5 may be heated by nitrogen or air, preferably pressurized and possibly cold pressurized.
本発明によれば、せいぜい一つか二つのポンプが必要であると解される。第１のポンプは、液体を第３の塔の底部から第１の塔の頂部凝縮器に上げるために用いられるポンプ１３である。加圧された形の酸素が必要とされる場合に用いられる第２のポンプは、液体酸素を加圧するために用いられる。液体２５のような他の液体を上げるため、塔の間の圧力差は液体を浮遊させるに足るものであるべきである。 According to the invention, it is understood that at most one or two pumps are required. The first pump is a pump 13 which is used to raise the liquid from the bottom of the third column in the first column of the top condenser. A second pump, used when pressurized form of oxygen is required, is used to pressurize liquid oxygen. In order to raise other liquids, such as liquid 25, the pressure difference between the columns should be sufficient to float the liquid.
第１の塔の上の蒸発器から第２および／または第３の塔へ重力によって流れが生じ得るようなできる限り高い第１の塔１、およびできる限り低い第２および／または第３の塔２，３を得るために、第１の塔１は比較的低い嵩密度（例えば密度が２５０〜５００ｍ２／ｍ３）を含有し、第２および／または第３の塔は比較的高い嵩密度（６００〜１０００ｍ２／ｍ３）を含有する。パイプ２１，３５における液体の移動は、これによって容易となる。
本願の出願当初の請求項の記載を実施の態様として以下に付記する。
［１］
中圧で運転し得る第１の蒸留塔（１）と、低圧で運転し得る第２の蒸留塔（２）と、低圧で、または前記低圧で運転し得る第３の蒸留塔（３）と、第１の凝縮−蒸発器（９，９Ａ）と、前記第２の塔の底部に配置された第２の凝縮−蒸発器（５）と、少なくとも前記第１の塔に空気を供給するパイプ（３３）と、前記第１の塔の上部から前記第３の塔の上部に窒素豊富な液体を供給するパイプ（３５）と、前記第３の塔の底部から前記第１の凝縮−蒸発器に液体を供給する少なくとも一つのパイプ（２３）と、前記第１の塔の底部から前記第３の塔に液体を供給するパイプ（２５）と、前記第１の凝縮−蒸発器から前記第２の塔に液体を供給するパイプ（２１）と、前記第２の塔から前記第３の塔の底部に頂部ガスを供給するパイプ（１５，１９）と、を具備し、前記第１、第２、および第３の塔は、隣り合って配置され、できれば全て床面（２７）の上に配置される空気分離のための装置。
［２］
極低温で運転し得る装置の要素、例えば液体酸素蒸発器（１１）が、一つの前記塔（１，２，３）の下に配置され、他の二つの前記塔および前記要素が前記床面に直接配置された［１］に記載の装置。
［３］
前記第２の塔（２）の底部と前記液体酸素蒸発器（１１）とに接続された加圧手段を具備した［２］に記載の装置。
［４］
前記第１の凝縮−蒸発器（９，９Ａ）は前記第１の塔（１）の上にあり、前記第１の塔からのガスによって再沸騰し得るように前記第１の塔の上部に接続された［１］ないし［３］のいずれか一つに記載の装置。
［５］
二つの前記塔に接続されたただ一つのポンプ（１３）を具備した［１］ないし［４］のいずれか一つに記載の装置。
［６］
前記ポンプ（１３）が前記第２の塔の底部から前記第１の凝縮−再沸器（９，９Ａ）に液体を供給する二つの前記パイプ（２３）に接続された［５］に記載の装置。
［７］
前記第１の凝縮−再沸器（９）を前記第３の塔（３）の底部に接続するガスパイプ（１７，１９）を具備する［１］ないし［６］のいずれか一つに記載の装置。
［８］
前記第２の塔（２）および／または前記第３の塔（３）の上部は、前記第１の凝縮−再沸器（９，９Ａ）より低い高さにあり、好ましくは前記第１の塔（１）の上部よりも低く、前記第１の塔（１）の嵩密度は前記第２の塔（２）および／または前記第３の塔（３）の嵩密度よりも低くなり得る［１］ないし［７］のいずれか一つに記載の装置。
［９］
前記第３の塔は凝縮−再沸器を含まない［１］ないし［８］のいずれか一つに記載の装置。
［１０］
前記第２の塔（２）は、熱交換手段に加えて第３の凝縮−再沸器（７）および前記第３の凝縮−再沸器の上に配置された熱及び物質交換のための手段を含む［１］ないし［９］のいずれか一つに記載の装置。
［１１］
前記第２の塔から前記第３の塔の底部に頂部ガスを供給する前記パイプ（１５，１９）は、前記第１の凝縮−再沸器（９）で蒸発したガス用のパイプ（１７）に接続される［１］ないし［１０］のいずれか一つに記載の装置。
［１２］
前記第３の塔（３）の下に配置された前記装置の要素は、液体酸素蒸発器（１１）である［１］ないし［１１］のいずれか一つに記載の装置。
［１３］
前記第１の塔（１）の運転圧力と前記第２および第３の塔（２，３）のうち少なくとも一つの圧力との間の圧力差は、３バールよりも少なく、好ましくは２．５バールであり、さらに好ましくは２バールである［１］ないし［１２］のいずれか一つに記載の装置を用いる空気分離のための方法。
［１４］
前記第２の塔（２）の上部と前記第３の塔（３）の底部との運転圧力の圧力差は、１バールより少なく、好ましくは０．５バールよりも少なく、さらに好ましくは０．２バールよりも少ない［１］ないし［１２］のいずれか一つに記載の装置を用いる空気分離のための方法。
First as high first capable as the evaporator of the top of the tower can occur flows by gravity into the second and / or third tower tower 1, and as low as possible second and / or third column To obtain a few, the first column 1 contains a relatively low bulk density (eg a density of 250-500 m 2 / m 3 ), and the second and / or third column has a relatively high bulk density. (600 to 1000 m 2 / m 3 ). The movement of the liquid in the pipes 21 and 35 is thereby facilitated.
The description of the claims at the beginning of the application of the present application will be appended as an embodiment.
[1]
A first distillation column (1) which can be operated at medium pressure, a second distillation column (2) which can be operated at low pressure, and a third distillation column (3) which can be operated at low pressure or at said low pressure A first condenser-evaporator (9, 9A), a second condenser-evaporator (5) arranged at the bottom of the second tower, and a pipe for supplying air to at least the first tower (33), a pipe (35) for supplying a nitrogen-rich liquid from the top of the first tower to the top of the third tower, and the first condenser-evaporator from the bottom of the third tower At least one pipe (23) for supplying liquid to the pipe, a pipe (25) for supplying liquid from the bottom of the first tower to the third tower, and the second from the first condenser-evaporator. A pipe (21) for supplying liquid to the tower of the pipe and a pipe (15,) for supplying top gas from the second tower to the bottom of the third tower 9), comprising a first, second, and third columns are arranged adjacent, apparatus for air separation to be arranged all if possible on the floor surface (27).
[2]
Elements of the device that can operate at cryogenic temperatures, for example a liquid oxygen evaporator (11), are arranged under one of the towers (1, 2, 3), the other two towers and the elements are connected to the floor surface. [1] The apparatus according to [1], which is directly disposed on the apparatus.
[3]
The apparatus according to [2], further comprising pressurizing means connected to the bottom of the second column (2) and the liquid oxygen evaporator (11).
[4]
The first condenser-evaporator (9, 9A) is above the first column (1) and is located at the top of the first column so that it can be reboiled by the gas from the first column. The device according to any one of [1] to [3] connected.
[5]
The apparatus according to any one of [1] to [4], comprising a single pump (13) connected to the two towers.
[6]
[5] The pump (13) is connected to two pipes (23) supplying liquid from the bottom of the second column to the first condenser-reboiler (9, 9A). apparatus.
[7]
According to any one of [1] to [6], comprising a gas pipe (17, 19) connecting the first condenser-reboiler (9) to the bottom of the third column (3). apparatus.
[8]
The top of the second column (2) and / or the third column (3) is at a lower height than the first condenser-reboiler (9, 9A), preferably the first column Lower than the top of the tower (1), the bulk density of the first tower (1) may be lower than the bulk density of the second tower (2) and / or the third tower (3) [ The apparatus according to any one of [1] to [7].
[9]
The apparatus according to any one of [1] to [8], wherein the third column does not include a condenser-reboiler.
[10]
Said second column (2) is for heat and mass exchange arranged on top of a third condenser-reboiler (7) and said third condenser-reboiler in addition to heat exchange means. The apparatus according to any one of [1] to [9], including means.
[11]
The pipes (15, 19) for supplying the top gas from the second column to the bottom of the third column are pipes for gas (17) evaporated in the first condenser-reboiler (9). The device according to any one of [1] to [10], which is connected to the device.
[12]
The device according to any one of [1] to [11], wherein the element of the device arranged under the third tower (3) is a liquid oxygen evaporator (11).
[13]
The pressure difference between the operating pressure of the first column (1) and the pressure of at least one of the second and third columns (2, 3) is less than 3 bar, preferably 2.5 A method for air separation using the apparatus according to any one of [1] to [12], which is bar, more preferably 2 bar.
[14]
The difference in operating pressure between the top of the second column (2) and the bottom of the third column (3) is less than 1 bar, preferably less than 0.5 bar, more preferably 0. A method for air separation using an apparatus according to any one of [1] to [12], less than 2 bar.
Claims (18)
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0953935A FR2946735B1 (en) | 2009-06-12 | 2009-06-12 | APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION. |
| FR0953935 | 2009-06-12 | ||
| PCT/FR2010/051101 WO2010142894A2 (en) | 2009-06-12 | 2010-06-04 | Apparatus and method for separating air by cryogenic distillation |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| JP2012529616A JP2012529616A (en) | 2012-11-22 |
| JP2012529616A5 true JP2012529616A5 (en) | 2014-10-09 |
| JP5823385B2 JP5823385B2 (en) | 2015-11-25 |
Family
ID=42028103
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2012514517A Expired - Fee Related JP5823385B2 (en) | 2009-06-12 | 2010-06-04 | Apparatus and method for air separation by cryogenic distillation |
Country Status (9)
| Country | Link |
|---|---|
| US (1) | US20120118013A1 (en) |
| EP (1) | EP2440871A2 (en) |
| JP (1) | JP5823385B2 (en) |
| CN (1) | CN102667383B (en) |
| AU (1) | AU2010258490B2 (en) |
| CA (1) | CA2762315A1 (en) |
| FR (1) | FR2946735B1 (en) |
| WO (1) | WO2010142894A2 (en) |
| ZA (1) | ZA201108764B (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2946735B1 (en) * | 2009-06-12 | 2012-07-13 | Air Liquide | APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION. |
| US20150316317A1 (en) * | 2012-12-27 | 2015-11-05 | Linde Aktiengesellschaft | Method and device for low-temperature air separation |
| CA2900122C (en) * | 2013-03-06 | 2023-10-31 | Linde Aktiengesellschaft | Air separation plant, method for obtaining a product containing argon, and method for creating an air separation plant |
| US10018414B2 (en) * | 2015-07-31 | 2018-07-10 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for the production of low pressure gaseous oxygen |
| US10101084B2 (en) * | 2015-07-31 | 2018-10-16 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus for the production of low pressure gaseous oxygen |
| FR3075064B1 (en) * | 2017-12-19 | 2019-12-27 | IFP Energies Nouvelles | DISTRIBUTOR TRAY WITH GAS COMPARTMENTS AND CHIMNEYS OF THE SAME FORM FOR OFFSHORE GAS / LIQUID CONTACT COLUMN |
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| US4582518A (en) | 1984-09-26 | 1986-04-15 | Erickson Donald C | Nitrogen production by low energy distillation |
| GB9325648D0 (en) * | 1993-12-15 | 1994-02-16 | Boc Group Plc | Air separation |
| FR2724011B1 (en) * | 1994-08-29 | 1996-12-20 | Air Liquide | PROCESS AND PLANT FOR THE PRODUCTION OF OXYGEN BY CRYOGENIC DISTILLATION |
| US5463871A (en) * | 1994-10-04 | 1995-11-07 | Praxair Technology, Inc. | Side column cryogenic rectification system for producing lower purity oxygen |
| DE19524928A1 (en) * | 1995-07-08 | 1997-01-09 | Basf Ag | Process for the rectification of mixtures of high-boiling air and / or temperature sensitive substances, which require a high separation performance, in a fine vacuum, as well as columns suitable for this process |
| DE19537913A1 (en) * | 1995-10-11 | 1997-04-17 | Linde Ag | Triple column process for the low temperature separation of air |
| FR2761897B1 (en) * | 1997-04-11 | 1999-05-14 | Air Liquide | INSTALLATION FOR SEPARATING A GAS MIXTURE BY DISTILLATION |
| EP0908226B1 (en) * | 1997-10-13 | 2006-02-22 | Taiyo Nippon Sanso Corporation | Process and apparatus for separation of stable isotope compound |
| US5966967A (en) * | 1998-01-22 | 1999-10-19 | Air Products And Chemicals, Inc. | Efficient process to produce oxygen |
| FR2774752B1 (en) * | 1998-02-06 | 2000-06-16 | Air Liquide | AIR DISTILLATION SYSTEM AND CORRESPONDING COLD BOX |
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-
2010
- 2010-06-04 US US13/321,993 patent/US20120118013A1/en not_active Abandoned
- 2010-06-04 CA CA2762315A patent/CA2762315A1/en not_active Abandoned
- 2010-06-04 EP EP10734789A patent/EP2440871A2/en not_active Withdrawn
- 2010-06-04 WO PCT/FR2010/051101 patent/WO2010142894A2/en active Application Filing
- 2010-06-04 CN CN201080025932.1A patent/CN102667383B/en not_active Expired - Fee Related
- 2010-06-04 JP JP2012514517A patent/JP5823385B2/en not_active Expired - Fee Related
- 2010-06-04 AU AU2010258490A patent/AU2010258490B2/en not_active Ceased
-
2011
- 2011-11-29 ZA ZA2011/08764A patent/ZA201108764B/en unknown
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