JP2020157173A - Operational method for pretreatment equipment for air liquefaction/separation device - Google Patents
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- 238000000034 method Methods 0.000 title claims abstract description 69
- 238000000926 separation method Methods 0.000 title claims abstract description 27
- 239000002994 raw material Substances 0.000 claims abstract description 62
- 238000001179 sorption measurement Methods 0.000 claims abstract description 46
- 239000007789 gas Substances 0.000 claims description 66
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 62
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 31
- 239000001569 carbon dioxide Substances 0.000 claims description 31
- 230000008929 regeneration Effects 0.000 claims description 19
- 238000011069 regeneration method Methods 0.000 claims description 19
- 239000003463 adsorbent Substances 0.000 claims description 15
- 229930195733 hydrocarbon Natural products 0.000 claims description 11
- 150000002430 hydrocarbons Chemical class 0.000 claims description 11
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 239000004215 Carbon black (E152) Substances 0.000 claims description 7
- 239000001272 nitrous oxide Substances 0.000 claims description 5
- 238000012545 processing Methods 0.000 claims description 3
- OMBRFUXPXNIUCZ-UHFFFAOYSA-N dioxidonitrogen(1+) Chemical compound O=[N+]=O OMBRFUXPXNIUCZ-UHFFFAOYSA-N 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 abstract description 2
- 239000012535 impurity Substances 0.000 description 10
- 238000001816 cooling Methods 0.000 description 9
- 238000010438 heat treatment Methods 0.000 description 8
- 230000007423 decrease Effects 0.000 description 6
- 238000005259 measurement Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- NDGSBJSAXJUQTE-UHFFFAOYSA-N azane;phosphorous acid Chemical compound N.OP(O)O NDGSBJSAXJUQTE-UHFFFAOYSA-N 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 230000004043 responsiveness Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04775—Air purification and pre-cooling
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Description
本発明は、空気液化分離装置の前処理設備の運転方法に関し、詳しくは、空気液化分離装置に供給される原料空気中の水分及び二酸化炭素をはじめとする不純物成分を温度変動吸着法により吸着除去して原料空気を精製する空気液化分離装置の前処理設備の運転方法に関する。 The present invention relates to a method of operating a pretreatment facility of an air liquefaction separation device. Specifically, the present invention adsorbs and removes impurity components such as moisture and carbon dioxide in the raw material air supplied to the air liquefaction separation device by a temperature fluctuation adsorption method. The present invention relates to an operation method of a pretreatment facility of an air liquefaction separation device for purifying raw air.
空気液化分離装置における深冷部の前段には、複数の吸着塔を吸着工程と再生工程とに順次切り換え使用する吸着装置を用いた前処理設備を設置し、吸着塔に充填した吸着剤に原料空気中の水分や二酸化炭素、炭化水素類、窒素酸化物のような不純物成分を吸着除去させて原料空気を精製するようにしている。この前処理設備における吸着装置の運転方法として、吸着工程にある吸着塔に流入する原料空気の温度を測定し、測定した原料空気温度に応じて吸着工程と再生工程との切替時間を変更することが行われている（例えば、特許文献１参照。）。また、吸着塔に導入する原料空気中の二酸化炭素の積算量から切替時間を変更することも行われている（例えば、特許文献２参照。）。 In front of the deep-cooled part of the air liquefaction separation device, a pretreatment facility using an adsorption device that sequentially switches between the adsorption process and the regeneration process is installed, and the adsorbent filled in the adsorption tower is used as a raw material. The raw material air is refined by adsorbing and removing water in the air and impurity components such as carbon dioxide, hydrocarbons, and nitrogen oxides. As an operation method of the adsorption device in this pretreatment facility, the temperature of the raw material air flowing into the adsorption tower in the adsorption process is measured, and the switching time between the adsorption process and the regeneration process is changed according to the measured raw material air temperature. (See, for example, Patent Document 1). Further, the switching time is also changed from the integrated amount of carbon dioxide in the raw material air introduced into the adsorption tower (see, for example, Patent Document 2).
しかし、従来の方法では、一つの吸着工程中の原料空気の温度や二酸化炭素の積算量といった条件に基づいて切替時間を変更しているため、例えば、一つ前の条件に基づいて切替時間を長くし、長時間の再生工程を行っているときに、何らかの外的要因で原料空気の温度上昇や二酸化炭素量の増加が発生した場合、吸着工程中の吸着塔で水分や二酸化炭素を確実に除去するためには、切替時間を短くして吸着工程時間を短縮させる必要があり、再生工程の時間を十分にとれなくなるおそれがある。また、製品ガス使用量の変動によって原料空気量が大きくかつ急激に変動した場合も、対応が困難になるおそれがある。 However, in the conventional method, the switching time is changed based on the conditions such as the temperature of the raw material air and the integrated amount of carbon dioxide in one adsorption process. Therefore, for example, the switching time is changed based on the previous condition. If the temperature of the raw material air rises or the amount of carbon dioxide increases due to some external factor during the long and long regeneration process, the adsorption tower during the adsorption process ensures that moisture and carbon dioxide are removed. In order to remove the carbon dioxide, it is necessary to shorten the switching time to shorten the adsorption process time, and there is a possibility that the regeneration process time cannot be sufficiently taken. In addition, even if the amount of raw material air fluctuates abruptly due to fluctuations in the amount of product gas used, it may be difficult to deal with it.
そこで本発明は、原料空気の条件が変動しても前処理設備の運転を最適化できる空気液化分離装置の前処理設備の運転方法を提供することを目的としている。 Therefore, an object of the present invention is to provide a method of operating a pretreatment facility of an air liquefaction separation device that can optimize the operation of the pretreatment facility even if the conditions of the raw material air fluctuate.
上記目的を達成するため、本発明の空気液化分離装置の前処理設備の運転方法は、第１の構成として、吸着剤を充填した複数の吸着塔を温度変動吸着法により吸着工程と再生工程とに順次切り換え使用する精製器によって、少なくとも、原料空気中の水分及び二酸化炭素を除去して空気液化分離装置に導入する原料空気を精製する空気液化分離装置の前処理設備の運転方法において、前記工程を複数の運転ステップに分割し、一つの運転ステップの長さ及び再生ガスの流量を、前回の運転ステップ中にあらかじめ設定された間隔で測定した前記精製器の入口における原料空気の流量、温度及び圧力のそれぞれから推算した運転ステップの長さ中で最も短い運転ステップの長さを次の運転ステップの長さとし、推算した再生ガスの流量の中で最も多い再生ガスの流量を次のステップの再生ガスの流量とすることを特徴としている。 In order to achieve the above object, the operation method of the pretreatment equipment of the air liquefaction separation device of the present invention has, as the first configuration, a plurality of adsorption towers filled with an adsorbent, and an adsorption step and a regeneration step by a temperature fluctuation adsorption method. In the operation method of the pretreatment equipment of the air liquefaction separation device for purifying the raw material air to be introduced into the air liquefaction separation device by removing at least water and carbon dioxide in the raw material air by the refiner used sequentially. Was divided into a plurality of operation steps, and the length of one operation step and the flow rate of the regenerated gas were measured at preset intervals during the previous operation step, and the flow rate, temperature, and temperature of the raw material air at the inlet of the refiner were measured. The shortest operating step length estimated from each of the pressures is taken as the next operating step length, and the largest regenerated gas flow rate in the estimated regenerated gas flow rate is used for the next step regeneration. It is characterized by the flow rate of gas.
また、本発明の第２の構成は、前記工程を複数の運転ステップに分割し、一つの運転ステップの長さ及び再生ガスの流量を、前回の運転ステップ中にあらかじめ設定された間隔で測定した前記精製器の入口における原料空気の流量、温度、圧力及び二酸化炭素濃度のそれぞれから推算した運転ステップの長さ中で最も短い運転ステップの長さを次の運転ステップの長さとし、推算した再生ガスの流量の中で最も多い再生ガスの流量を次のステップの再生ガスの流量とすることを特徴としている。 Further, in the second configuration of the present invention, the process is divided into a plurality of operation steps, and the length of one operation step and the flow rate of the regenerated gas are measured at intervals set in advance during the previous operation step. The length of the shortest operating step among the lengths of the operating steps estimated from each of the flow rate, temperature, pressure and carbon dioxide concentration of the raw material air at the inlet of the refiner is set as the length of the next operating step, and the regenerated gas is estimated. It is characterized in that the flow rate of the regenerated gas having the largest flow rate in the next step is set as the flow rate of the regenerated gas in the next step.
さらに、本発明の第３の構成は、前記工程を複数の運転ステップに分割し、一つの運転ステップの長さ及び再生ガスの流量を、前回の運転ステップ中にあらかじめ設定された間隔で測定した前記精製器の入口における原料空気の流量、温度、圧力、二酸化炭素濃度、炭化水素濃度及び亜酸化窒素濃度のそれぞれから推算した運転ステップの長さ中で最も短い運転ステップの長さを次の運転ステップの長さとし、推算した再生ガスの流量の中で最も多い再生ガスの流量を次のステップの再生ガスの流量とすることを特徴としている。 Further, in the third configuration of the present invention, the process is divided into a plurality of operation steps, and the length of one operation step and the flow rate of the regenerated gas are measured at preset intervals during the previous operation step. The shortest operation step length estimated from each of the flow rate, temperature, pressure, carbon dioxide concentration, hydrocarbon concentration and nitrous oxide concentration of the raw material air at the inlet of the refiner is set to the next operation. The length of the step is defined as the flow rate of the regenerated gas having the largest estimated flow rate of the regenerated gas, which is the flow rate of the regenerated gas in the next step.
加えて、本発明の第４の構成は、前記工程を複数の運転ステップに分割し、一つの運転ステップの長さ及び再生ガスの流量を、前回の運転ステップ中にあらかじめ設定された間隔で測定した前記精製器の入口における原料空気の流量、温度、圧力、二酸化炭素濃度、炭化水素及び亜酸化窒素の少なくとも一つから推算した運転ステップの長さ中で最も短い運転ステップの長さを次の運転ステップの長さとし、推算した再生ガスの流量の中で最も多い再生ガスの流量を次のステップの再生ガスの流量とすることを特徴としている。 In addition, in the fourth configuration of the present invention, the process is divided into a plurality of operation steps, and the length of one operation step and the flow rate of the regenerated gas are measured at preset intervals during the previous operation step. The shortest operating step length estimated from at least one of the flow rate, temperature, pressure, carbon dioxide concentration, hydrocarbon and nitrogen phosphite of the raw material air at the inlet of the refiner is as follows. It is characterized in that the length of the operation step is defined as the flow rate of the regenerated gas having the largest estimated flow rate of the regenerated gas as the flow rate of the regenerated gas in the next step.
本発明の空気液化分離装置の前処理設備の運転方法によれば、精製器に導入される原料空気の条件に応じて精製器の運転状態を的確に制御できるので、原料空気の精製を確実に行うことができ、運転コストの低減を図ることもできる。 According to the operation method of the pretreatment equipment of the air liquefaction separation device of the present invention, the operating state of the refiner can be accurately controlled according to the conditions of the raw material air introduced into the refiner, so that the raw material air can be reliably purified. This can be done, and the operating cost can be reduced.
図１乃至図４は、本発明における空気液化分離装置の前処理設備の運転方法を説明するためのもので、図１は、本発明方法を適用可能な前処理設備を備えた空気液化分離装置の一例を示す系統図である。図１に示す空気液化分離装置は、原料空気を圧縮、精製するための前処理設備１１と、原料空気を冷却して液化分離する深冷部１２とを備えている。
1 to 4 are for explaining the operation method of the pretreatment equipment of the air liquefaction separation device in the present invention, and FIG. 1 is an air liquefaction separation device provided with the pretreatment equipment to which the method of the present invention can be applied. It is a system diagram which shows an example. The air liquefaction separation device shown in FIG. 1 includes a
前処理設備１１は、空気濾過器１３で塵埃を除去した原料空気を圧縮機１４で所定圧力に圧縮し、予冷設備１５で圧縮熱を除去した後、精製器１６で原料空気中の不純物、例えば、水分、二酸化炭素、炭化水素、亜酸化窒素といった不純物を除去するもので、精製器１６には、前記不純物を除去可能な吸着剤を充填した複数の吸着塔１７を吸着工程と再生工程とに順次切り替えて原料空気の精製を連続して行える温度変動吸着法を採用した吸着装置が用いられている。この吸着装置には、吸着塔１７の一端側及び他端側に複数の切替弁が設けられており、これらの切替弁を所定の順序で切替開閉することにより、各吸着塔が吸着工程と再生工程とに切り替えられる。
In the
また、吸着装置には、再生工程を行っている吸着塔に加熱ガスと冷却ガスとを切替供給するための再生ガス供給部１８が設けられており、再生工程における加熱段階では、深冷部から導出した低温の排ガスを加熱器１８ａで所定温度に加熱して加熱段階を行っている吸着塔に導入し、加熱段階後の冷却段階では、低温の排ガスをバイパス経路１８ｂを通して低温のまま冷却段階を行っている吸着塔に導入するように各弁が切替開閉される。
Further, the adsorption device is provided with a regenerated
図２は、基本的な運転サイクルの一例を示すもので、本例では、吸着工程と再生工程との切替時間を２４０分に設定して１サイクルを形成しており、再生工程は、圧縮空気の導入により加圧された塔内の圧力を大気圧に下げる脱圧段階を１０分、加熱器１８ａで加熱された加熱再生ガスを塔内に流通させて吸着剤を加熱再生する加熱段階を９０分、低温再生ガスを塔内に流通させて吸着剤を吸着工程に適した温度に冷却する冷却段階を１１６分、塔内に精製原料空気の一部を導入して塔内を吸着工程圧力に昇圧する充圧段階を２４分の各段階に区分けされている。
FIG. 2 shows an example of a basic operation cycle. In this example, one cycle is formed by setting the switching time between the adsorption process and the regeneration process to 240 minutes, and the regeneration process is the compressed air. The depressurization step of lowering the pressure in the tower pressurized by the introduction of the above to atmospheric pressure is 10 minutes, and the heating step of heating and regenerating the adsorbent by circulating the heated regeneration gas heated by the
本発明方法では、前記１サイクルを複数の運転ステップ（以下、ステップという。）に区分けし、各ステップごとに得た情報に基づいて制御するようにしている。例えば、流量変更時の応答性を考慮して６０秒を基本的な１ステップの時間とすると、１サイクルは、吸着工程が２４０ステップ、再生工程では、脱圧段階が１０ステップ、加熱段階が９０ステップ、冷却段階が１１６ステップに区分けされる。 In the method of the present invention, the one cycle is divided into a plurality of operation steps (hereinafter, referred to as steps), and control is performed based on the information obtained for each step. For example, if 60 seconds is set as the basic one-step time in consideration of the responsiveness when the flow rate is changed, the adsorption step is 240 steps in one cycle, the decompression step is 10 steps, and the heating step is 90 in the regeneration step. The steps and cooling steps are divided into 116 steps.
また、各ステップで得る情報としては、精製器１６の入口における原料空気の流量、温度、圧力のほか、二酸化炭素濃度、炭化水素濃度、亜酸化窒素濃度といった吸着剤で吸着除去可能な不純物成分であり、原料空気中の水分量は、予冷設備１５から導出した原料空気中に飽和量の水分が含まれているとして、原料空気の流量、温度及び圧力に基づいて容易に算出できる。これらの情報は、精製器１６の入口部に、各情報に対応した流量計、温度計、圧力計、各種分析計を配置することで容易に得ることができる。
The information obtained in each step includes the flow rate, temperature, and pressure of the raw material air at the inlet of the
さらに、各情報の値は、あらかじめ設定された間隔、例えば、１秒間隔、５秒間隔などの間隔で測定した測定値の移動平均で算出するようにしている。例えば、５秒間隔で測定値を採取していて１ステップが６０秒であるときには、６０秒間で測定した１２（６０／５）回の測定値の和を１２で除した移動平均の値を、制御用に使用する値として採用する。そして、各ステップにおける最後の測定値を含めて移動平均を求め、ここから採用した値が、前のステップで採用した値に比較して上昇しているときには、前のステップに対する上昇割合に基づいて次のステップの時間を短縮するとともに、吸着塔の再生ガスを増加させ、逆に前のステップで採用した値に比較して下降しているときには、下降割合に基づいて次のステップの時間を延長するとともに、再生ガスを減少させる。また、一つの移動平均の値が上昇し、他の移動平均の値が下降したときでも、同様に演算処理することにより、次のステップの条件を算出すればよい。 Further, the value of each information is calculated by a moving average of the measured values measured at a preset interval, for example, an interval of 1 second or an interval of 5 seconds. For example, when the measured values are collected at 5-second intervals and one step is 60 seconds, the moving average value obtained by dividing the sum of 12 (60/5) measured values measured in 60 seconds by 12 is used. Adopted as the value used for control. Then, the moving average is calculated including the last measured value in each step, and when the value adopted from this is higher than the value adopted in the previous step, it is based on the rate of increase with respect to the previous step. Shorten the time of the next step and increase the regenerated gas in the adsorption tower, and conversely extend the time of the next step based on the rate of descent when it is descending compared to the value adopted in the previous step. At the same time, reduce the amount of regenerated gas. Further, even when the value of one moving average rises and the value of the other moving average falls, the condition of the next step may be calculated by performing the same calculation processing.
例えば、図３に示すように、１サイクル中のｎ番目のステップ（ステップｎ）におけるステップの時間及び再生ガスの流量は、一つ前のステップ、すなわち、ステップｎ−１での最終の測定結果を含めた移動平均に基づいて決定され、次のステップであるステップｎ＋１におけるステップの時間及び再生ガスの流量は、ステップｎでの最終の測定結果を含めた移動平均によって決定される。 For example, as shown in FIG. 3, the step time and the flow rate of the regenerated gas in the nth step (step n) in one cycle are the final measurement results in the previous step, that is, step n-1. The step time and the flow rate of the regenerated gas in the next step, step n + 1, are determined by the moving average including the final measurement result in step n.
ここで、図４に示すように、工程切替時の原料空気の流量が１００００Ｎｍ３／ｈ、１ステップの時間が６０秒、再生ガス流量が１６００Ｎｍ３／ｈである設計条件で運転しているときに、工程切替後に原料空気の流量が次第に減少して精製器負荷が減少するような場合、５秒間隔で測定した原料空気の流量が次第に変化し、ステップｎ−１の終了直前に測定した流量を含めた１２回分の移動平均が９８７３Ｎｍ３／ｈとなり、流量が１００００Ｎｍ３／ｈから減少、すなわち、原料空気量の減少に伴って精製器負荷が低下していると判断した場合は、再生ガスの流量を１６００Ｎｍ３／ｈから１５８０Ｎｍ３／ｈ（１６００＊（９８７３／１００００））に減少させるとともに、次のステップｎの時間を６０秒から６１秒（（６０／９８７３）＊１００００）に延長する。 Here, as shown in FIG. 4, when operating under the design condition that the flow rate of the raw material air at the time of process switching is 10000 Nm 3 / h, the time of one step is 60 seconds, and the flow rate of the regenerated gas is 1600 Nm 3 / h. In addition, when the flow rate of the raw material air gradually decreases after the process is switched and the load on the refiner decreases, the flow rate of the raw material air measured at 5-second intervals gradually changes, and the flow rate measured immediately before the end of step n-1. If it is judged that the moving average for 12 times including the above is 9873 Nm 3 / h and the flow rate decreases from 10000 Nm 3 / h, that is, the purifier load decreases as the amount of raw material air decreases, the recycled gas The flow rate of the next step n is reduced from 1600 Nm 3 / h to 1580 Nm 3 / h (1600 * (9873/10000)), and the time of the next step n is extended from 60 seconds to 61 seconds ((60/9873) * 10000). ..
同様に、ステップｎ＋１は、ステップｎの終了直前に測定した流量の移動平均に基づいて再生ガスの流量及びステップｎ＋１の時間が設定される。例えば、流量の移動平均が９５５０Ｎｍ３／ｈになったときには、再生ガスの流量を１５８０Ｎｍ３／ｈから１５２８Ｎｍ３／ｈ（１５８０＊（９５５０／９８７３））に減少させるとともに、次のステップｎ＋１の時間を６１秒から６３秒（（６１／９５５０）＊９８７３）に延長する。一方、後半で原料空気の流量が次第に増加して精製器負荷が増大するような場合は、移動平均で求めた値が１より大きくなるので、次のステップにおける再生ガスの流量が増加するとともに、ステップの時間が短縮されることになる。 Similarly, in step n + 1, the flow rate of the regenerated gas and the time of step n + 1 are set based on the moving average of the flow rates measured immediately before the end of step n. For example, when the moving average of the flow rate becomes 9550 Nm 3 / h, the flow rate of the regenerated gas is reduced from 1580 Nm 3 / h to 1528 Nm 3 / h (1580 * (9550/9873)), and the time of the next step n + 1 is reached. Is extended from 61 seconds to 63 seconds ((61/9550) * 9873). On the other hand, when the flow rate of the raw material air gradually increases and the refiner load increases in the latter half, the value obtained by the moving average becomes larger than 1, so that the flow rate of the regenerated gas in the next step increases and the flow rate of the recycled gas increases. The step time will be shortened.
このように、前回のステップで算出した移動平均の変化に応じて今回のステップの長さ及び再生ガスの流量を変化させることにより、精製器１６を負荷に応じた最適な条件で運転することができ、各回の吸着工程において吸着剤で吸着する不純物量を略一定量に制御でき、原料空気中の不純物を確実に除去できるとともに、吸着剤の再生も、略一定の加熱再生ガスによって確実に行うことができる。特に、ステップの長さ及び再生ガスの流量を変化させるための値を移動平均によって算出しているので、測定値をそのまま制御用に用いる場合に比べて、測定値のばらつきや誤差を吸収することができ、例えば、再生ガスの流量を変化させるための弁が頻繁に作動することがなくなる。
In this way, by changing the length of this step and the flow rate of the regenerated gas according to the change in the moving average calculated in the previous step, the
通常の大気条件では、原料空気中の各不純物成分の濃度はほとんど変化せず、原料空気の圧力や温度もほとんど変化しないので、深冷部１２で分離した製品ガスの使用量の変動に伴う原料空気の流量変化を測定するだけでも十分な制御を行うことが可能である。特に、製鉄所向けの空気液化分離装置のように、製品ガスの需要変動が大きいときに極めて有効である。
Under normal atmospheric conditions, the concentration of each impurity component in the raw material air hardly changes, and the pressure and temperature of the raw material air hardly change. Therefore, the raw material due to fluctuations in the amount of product gas used separated by the
また、周辺に工場が多く、二酸化炭素が増減するおそれのあるときには、原料空気中の二酸化炭素濃度を制御用の情報として加えることにより、二酸化炭素の濃度が上昇したときでも、二酸化炭素を吸着剤で確実に除去できるとともに二酸化炭素を吸着した吸着剤の再生も確実に行うことができる。さらに、周囲に化学コンビナートや製鉄所がある場合、あるいは、化学コンビナートや製鉄所の敷地内に配置された空気液化分離装置の場合は、吸着剤で除去可能な炭化水素や亜酸化窒素も制御用の情報に加えることにより、より確実な運転を行うことができる。また、通常の運転では、最大負荷を想定した設計条件に比べて吸着塔の切替間隔が長くなるので、例えば一日あたり６サイクルの切替運転を５サイクル以下にすることができ、吸着塔の再生に要するエネルギーを削減することができる。 In addition, when there are many factories in the vicinity and there is a risk that carbon dioxide will increase or decrease, by adding the carbon dioxide concentration in the raw material air as control information, carbon dioxide will be adsorbed even when the carbon dioxide concentration rises. It can be reliably removed and the adsorbent that has adsorbed carbon dioxide can be reliably regenerated. Furthermore, if there is a chemical complex or steelworks in the surrounding area, or if the air liquefaction separation device is located on the premises of the chemical complex or steelworks, hydrocarbons and nitrogen phosphite that can be removed by the adsorbent are also used for control. By adding to the information of, more reliable operation can be performed. Further, in normal operation, the switching interval of the adsorption tower is longer than the design condition assuming the maximum load. Therefore, for example, the switching operation of 6 cycles per day can be reduced to 5 cycles or less, and the adsorption tower can be regenerated. The energy required for the bicycle can be reduced.
実際の空気液化分離装置の運転では、必要な製品流量の減少によって原料空気の流量が減少し、その結果、次のステップにおける再生ガスの流量を減少させ、ステップの時間を長くすることが必要な場合でも、前記精製器１６の入口における原料空気中の二酸化炭素濃度が一時的に上昇し、その二酸化炭素濃度の上昇からは、次のステップにおける再生ガスの流量の増加と、ステップの時間の短縮が必要となる場合がある。
In the actual operation of the air liquefaction separator, it is necessary to reduce the flow rate of the raw material air by reducing the required product flow rate, and as a result, reduce the flow rate of the regenerated gas in the next step and lengthen the step time. Even in this case, the carbon dioxide concentration in the raw material air at the inlet of the
すなわち、前記精製器の入口における原料空気の流量、温度、圧力、原料空気中の二酸化炭素濃度、炭化水素濃度又は亜酸化窒素濃度といった条件は、基本的に独立してステップの長さ、再生ガスの流量に影響を及ぼす要素である。本発明では、各要素から求められた最も短いステップの長さを採用するとともに、最も多い再生ガスの流量を採用するようにしているので、原料空気の条件に応じた最適なステップの長さ及び再生ガスの流量を設定することができる。したがって、各条件に応じて吸着工程及び再生工程を最適化できるので、各種不純物の除去及び吸着剤の再生を確実に行うことができる。 That is, conditions such as the flow rate, temperature, pressure, carbon dioxide concentration, hydrocarbon concentration, or nitrous oxide concentration of the raw material air at the inlet of the refiner are basically independent of the step length and the regenerated gas. It is a factor that affects the flow rate of. In the present invention, the shortest step length obtained from each element is adopted, and the largest flow rate of the regenerated gas is adopted. Therefore, the optimum step length and the optimum step length according to the conditions of the raw material air are adopted. The flow rate of the regenerated gas can be set. Therefore, since the adsorption step and the regeneration step can be optimized according to each condition, various impurities can be removed and the adsorbent can be reliably regenerated.
また、本発明では、前記精製器の入口における原料空気の流量、温度、圧力、原料空気中の二酸化炭素濃度、炭化水素濃度及び亜酸化窒素濃度といった各種条件の内、任意の要素の一つだけを採用してもよい。しかし、より多くの場合にも前記精製器の適切な運転を担保するためには、前記精製器の入口における原料空気の流量、温度及び圧力を基に単位時間あたりの移動平均を算出する方法、前記精製器の入口における原料空気の流量、温度、圧力及び前記精製器の入口における原料空気中の二酸化炭素濃度を基に単位時間あたりの移動平均を算出する方法、又は、前記精製器の入口における原料空気の流量、温度、圧力及び前記精製器の入口における原料空気中の二酸化炭素濃度、炭化水素又は亜酸化窒素の濃度を基に単位時間あたりの移動平均を算出する方法を採用することが望ましい。 Further, in the present invention, only one of any elements among various conditions such as the flow rate, temperature, pressure, carbon dioxide concentration in the raw material air, hydrocarbon concentration and nitrous oxide concentration at the inlet of the refiner is used. May be adopted. However, in more cases, in order to ensure proper operation of the refiner, a method of calculating a moving average per unit time based on the flow rate, temperature and pressure of the raw material air at the inlet of the refiner, A method of calculating a moving average per unit time based on the flow rate, temperature, pressure of raw material air at the inlet of the refiner and the concentration of carbon dioxide in the raw material air at the inlet of the refiner, or at the inlet of the refiner. It is desirable to adopt a method of calculating the moving average per unit time based on the flow rate, temperature, pressure of the raw material air, the carbon dioxide concentration in the raw material air at the inlet of the refiner, and the concentration of hydrocarbons or nitrous oxide. ..
さらに、本発明では、特定のステップの長さと再生ガスの流量とを対応させることが可能である。つまり、前のステップから求められた次のステップの運転ステップの長さが１０％長くなった場合、単純に再生ガスの流量を１０％減少させることができる。つまり、各ステップにおいて、運転ステップの長さと再生ガスの流量との積の値を一定とすることができる。このような制御方法を採用すると、各制御方法において、各要素からステップの長さのみを演算すればよく、再生ガスの流量は簡単に決めることができる。 Further, in the present invention, it is possible to make a specific step length correspond to the flow rate of the regenerated gas. That is, when the length of the operation step of the next step obtained from the previous step is increased by 10%, the flow rate of the regenerated gas can be simply reduced by 10%. That is, in each step, the value of the product of the length of the operation step and the flow rate of the regenerated gas can be made constant. When such a control method is adopted, in each control method, only the step length needs to be calculated from each element, and the flow rate of the regenerated gas can be easily determined.
なお、１ステップの時間は任意に設定することができ、測定間隔も任意に設定することができる。また、空気液化分離装置の起動時などの特別+な場合は、運転状態が安定するまで制御を行わないように設定することができる。 The time of one step can be arbitrarily set, and the measurement interval can also be arbitrarily set. Further, in a special case such as when the air liquefaction separation device is started, it can be set so that the control is not performed until the operating state becomes stable.
１１…前処理設備、１２…深冷部、１３…空気濾過器、１４…圧縮機、１５…予冷設備、１６…精製器、１７…吸着塔、１８…再生ガス供給部、１８ａ…加熱器、１８ｂ…バイパス経路 11 ... Pretreatment equipment, 12 ... Deep cooling part, 13 ... Air filter, 14 ... Compressor, 15 ... Precooling equipment, 16 ... Purifier, 17 ... Adsorption tower, 18 ... Recycled gas supply part, 18a ... Heater, 18b ... Bypass route
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0842964A (en) * | 1994-07-29 | 1996-02-16 | Nippon Steel Corp | Producing method of adsorption tank in deep freeze separation method |
| JP2006258302A (en) * | 2005-03-15 | 2006-09-28 | Taiyo Nippon Sanso Corp | Purification method for raw material air in air liquefaction separation device |
| JP2009262151A (en) * | 2008-04-21 | 2009-11-12 | Air Products & Chemicals Inc | Cyclical swing adsorption process |
| JP2014113594A (en) * | 2014-03-10 | 2014-06-26 | Shinko Air Water Cryoplant Ltd | Pre-treatment device for air separation apparatus and pre-treatment method therefor |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0842964A (en) * | 1994-07-29 | 1996-02-16 | Nippon Steel Corp | Producing method of adsorption tank in deep freeze separation method |
| JP2006258302A (en) * | 2005-03-15 | 2006-09-28 | Taiyo Nippon Sanso Corp | Purification method for raw material air in air liquefaction separation device |
| JP2009262151A (en) * | 2008-04-21 | 2009-11-12 | Air Products & Chemicals Inc | Cyclical swing adsorption process |
| JP2014113594A (en) * | 2014-03-10 | 2014-06-26 | Shinko Air Water Cryoplant Ltd | Pre-treatment device for air separation apparatus and pre-treatment method therefor |
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