JPH04126512A - System for separating and recovering gaseous mixture and its operation - Google Patents
System for separating and recovering gaseous mixture and its operationInfo
- Publication number
- JPH04126512A JPH04126512A JP2246997A JP24699790A JPH04126512A JP H04126512 A JPH04126512 A JP H04126512A JP 2246997 A JP2246997 A JP 2246997A JP 24699790 A JP24699790 A JP 24699790A JP H04126512 A JPH04126512 A JP H04126512A
- Authority
- JP
- Japan
- Prior art keywords
- gas
- mixed gas
- cooled
- adsorbed
- adsorption
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000008246 gaseous mixture Substances 0.000 title abstract 6
- 238000001179 sorption measurement Methods 0.000 claims abstract description 55
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 238000010438 heat treatment Methods 0.000 claims abstract description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 32
- 238000000034 method Methods 0.000 claims description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 17
- 239000001569 carbon dioxide Substances 0.000 claims description 16
- 238000011084 recovery Methods 0.000 claims description 16
- 239000003463 adsorbent Substances 0.000 claims description 15
- 238000000926 separation method Methods 0.000 claims description 10
- 238000010248 power generation Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 89
- 230000008929 regeneration Effects 0.000 abstract description 11
- 238000011069 regeneration method Methods 0.000 abstract description 11
- 239000000567 combustion gas Substances 0.000 abstract 1
- 239000000203 mixture Substances 0.000 abstract 1
- 239000002699 waste material Substances 0.000 abstract 1
- 238000003795 desorption Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000010926 purge Methods 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011017 operating method Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 238000003916 acid precipitation Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- 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
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- 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)
- Carbon And Carbon Compounds (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は混合成分の分離回収システムに係り、特に、火
力発電ボイラ等からの排ガス中の炭酸ガス（ＣＯ２）分
離・回収システム及び運転方法に関する。[Detailed Description of the Invention] [Field of Industrial Application] The present invention relates to a separation and recovery system for mixed components, and in particular to a system and operating method for separating and recovering carbon dioxide (CO2) in exhaust gas from a thermal power boiler, etc. .
酸性雨、オゾン層破壊、地球温暖化は人類の将来にとっ
て、極めて大きな地球的規模の環境問題であり、その対
策が必要とされている。この中で、地球温暖化はＣ○２
濃度の上昇が主原因の一つとされている。主に化石燃料
をボイラで燃焼させ、得られた熱エネルギを電気エネル
ギに変換する火力発電所のボイラ排ガスからのＣＯｚの
排出量が多い。この排出ＣＯｘ量は数百ＫＷの電力量を
賄う場合、−時間当り数百トンにも及び、国内の電力需
要量を考えると膨大なＣＯｚが排出されていることにな
る。Acid rain, ozone layer depletion, and global warming are extremely large global environmental problems for the future of humanity, and countermeasures are required. Among these, global warming is C○2
Increased concentration is said to be one of the main causes. A large amount of COz is emitted from the boiler exhaust gas of thermal power plants, which mainly burn fossil fuels in boilers and convert the resulting thermal energy into electrical energy. The amount of COx emitted reaches several hundred tons per hour when several hundred kilowatts of electricity is supplied, which means that a huge amount of COz is emitted when considering the domestic electricity demand.
この様なことから、近年、火力発電所のボイラ排ガス等
に含まれるＣ Ｏｘを回収し、有効利用及び貯蔵などの
手段によってＣＯｚの大気中への排出を抑制することが
叫ばれている。特に、ＣＯ２の排出抑制技術としてＣＯ
２の分離回収システムが注目されている。For this reason, in recent years, there has been a call for controlling the emission of COz into the atmosphere by recovering COx contained in boiler exhaust gas from thermal power plants, and effectively using and storing it. In particular, CO2 emissions control technology
The second separation and recovery system is attracting attention.
従来、比較的Ｃｏｘの濃度が低い空気中のＣｏ２分離除
去技術としては深冷分離法の前処理装置として圧力差ス
イング吸着法（特願昭４６−４９５４２号。Conventionally, as a technology for separating and removing CO2 from air where the concentration of Cox is relatively low, the pressure difference swing adsorption method (Japanese Patent Application No. 46-49542) is used as a pre-treatment device for the cryogenic separation method.
Ｕ Ｓ −３９６７４６４号、 Ｕ Ｓ−３２１０９５
０号等）が知られている。また、混合ガスからのＣＯｘ
の分離除去に関しては圧力差スイング吸着法（特開昭６
４−２７６１４号、特開昭５２−５９０７３号、特開平
１−１５５９２６号公報）により行うことが知られてい
る。一方、ＣＯｘの分離回収技術に関しては圧力差スイ
ング吸着法により廃ガスからのＣｏｗ回収法（吸着（Ｐ
Ｓ Ａ）による廃ガスからのＣＯｘ回収、化学装置、
８月号、ｐ５４〜５９ （１９８９））がある。US-3967464, US-321095
No. 0 etc.) are known. In addition, COx from mixed gas
Regarding the separation and removal of
4-27614, JP-A-52-59073, and JP-A-1-155926). On the other hand, regarding COx separation and recovery technology, Cow recovery from waste gas (adsorption (P
COx recovery from waste gas by S A), chemical equipment,
August issue, pages 54-59 (1989)).
上記従来技術「吸着（Ｐ Ｓ Ａ）による廃ガスからの
ＣＯｚ回収」には、高炉熱風炉ガス、石油改質ガス、水
素製造ガス等の比較的ＣＯｚ濃度が２０％前後と高い場
合と燃焼排ガス中のＣＯ２濃度が１０％前後と比較的希
薄の場合の圧力差スイング吸着（以下ＰＳＡ法と略す）
によるＣ ０２の分離回収に関して述べられている。こ
の中でも燃焼排ガス中のＣＯ２濃度が希薄な場合には、
製造コスト及びＰＡＳ装置が大型化するなどの観点から
ＣＯｘ分離回収を二段方式で行うことが記載されている
。すなわち、ＣＯｚの分離回収を一段目のＰＳＡ装置で
ＣＯｚを粗濃縮し、二段目のＰＳＡ装置で高濃縮して分
離回収する方式である。The above conventional technology "COz recovery from waste gas by adsorption (PSA)" is applicable to cases where the COz concentration is relatively high at around 20%, such as blast furnace hot stove gas, reformed petroleum gas, hydrogen production gas, etc., and combustion exhaust gas. Pressure difference swing adsorption (hereinafter abbreviated as PSA method) when the CO2 concentration is relatively dilute, around 10%.
The separation and recovery of C 02 is described. Among these, when the CO2 concentration in the combustion exhaust gas is low,
It is described that COx separation and recovery is performed in a two-stage method from the viewpoint of manufacturing costs and increasing the size of the PAS device. That is, this is a method in which COz is separated and recovered using a first-stage PSA device that roughly concentrates COz, and a second-stage PSA device that highly concentrates and separates and recovers COz.
また、ＣＯｘの分離回収に関しては吸着工程を終了した
吸着塔に製品ＣＯｚガスを供給し、すでに共吸着されＮ
Ｚ 、Ｏｘなどをパージし吸着工程終了基にＣＯｘを充
満させたのち、吸着したＣ Ｏ２とパージ用ＣＯｘを真
空ポンプにより回収する方法が記載されている。Regarding the separation and recovery of COx, the product COz gas is supplied to the adsorption tower that has completed the adsorption process, and the COz gas that has already been co-adsorbed is removed.
A method is described in which, after purging Z 2 , Ox, etc. and filling the adsorption step end group with COx, the adsorbed CO 2 and purging COx are recovered using a vacuum pump.
この方法で濃度が希薄な燃焼排ガス等のＣｏｔの分離回
収では回収率の向上を図るため、ＰＳＡ装置の二段にす
る必要があり′、ＰＳＡ装置の大型化、所要消費動力の
増大につながる等の問題が生じる。また、製品Ｃｏｎを
パージし共吸着のＮ２ 。In order to improve the recovery rate when separating and recovering Cot such as combustion exhaust gas with a dilute concentration using this method, it is necessary to use a two-stage PSA device, which leads to an increase in the size of the PSA device and an increase in the required power consumption. The problem arises. In addition, the product Con was purged and co-adsorbed with N2.
ｏ２を除去したのち、吸着ＣＯＺとパージ用ＣＯｚを真
空ポンプにより回収する際に、ＣＯｚは高吸着成分であ
り、吸着剤からのＣｏｎの脱離速度が遅く、かつ、脱離
量が少なくなるため、真空ポンプによる減圧を高真空度
にする必要がある。このため、真空ポンプの動力が大き
くなる問題が生じる。この問題点は、Ｃｏｎの分離回収
コストに大きく影響を及ぼすことになる。After removing o2, when recovering adsorbed COZ and purge COz using a vacuum pump, COz is a highly adsorbed component, and the rate of desorption of Con from the adsorbent is slow, and the amount of desorbed is small. , it is necessary to reduce the pressure by a vacuum pump to a high degree of vacuum. Therefore, a problem arises in that the power of the vacuum pump increases. This problem greatly affects the cost of separating and recovering Con.
本発明の目的は、上記手段によらず濃度が希薄に燃焼排
ガス等からのＣＯｚを効率よく分離・回収することにあ
る。An object of the present invention is to efficiently separate and recover COz from combustion exhaust gas and the like in a diluted manner without using the above-mentioned means.
上記目的を達成するために、圧力スイング吸着法によっ
て混合ガス中の高吸着ガスのＣＯｚを吸着し残りの低吸
着ガスを精′製する方法において、低吸着精製ガスを冷
却あるいは加熱する手段によって冷却あるいは加熱し加
熱低吸着精製ガスにより吸着ＣＯｘを吸着剤から脱離し
、この手段によって分離されたＣ Ｏｘを回収する手段
は前記冷却低吸着精製ガスにより前記加熱低吸着精製ガ
スとＣＯｘを含む混合ガスを冷却しＣＯｚのみを液化し
て回収するようにしたものである。In order to achieve the above objective, in a method of adsorbing COz, which is a highly adsorbed gas in a mixed gas, by pressure swing adsorption and purifying the remaining low adsorbed gas, the low adsorbed purified gas is cooled by means of cooling or heating. Alternatively, the means for desorbing the adsorbed COx from the adsorbent by heating and using the heated low-adsorption purified gas and recovering the COx separated by this means is to use the cooled low-adsorption purified gas to generate a mixed gas containing the heated low-adsorption purified gas and COx. The COz is cooled and only the COz is liquefied and recovered.
混合ガス中のＣＯｚを濃縮する際には精製混合ガス中に
はＣＯｘが存在しない様に吸着工程を実施する。また、
濃縮ＣＯ２を吸着剤から肌着する再生工程でＣＯｚを含
まない精製混合ガスで濃縮ＣＯｚを分離する際には、Ｃ
Ｏｚが完全に分離（共吸着の混合ガスが一部含まれる）
するまで精製混合ガスあるいは加熱した精製混合ガスを
供給する。この操作が終了した時点で、吸着工程時の圧
力で貯留した精製混合ガスにより吸着塔を昇圧する。さ
らに、ＣＯｚを精製混合ガスあるいは加熱精製混合ガス
により分離した後、回収する際には精製混合ガスを冷熱
発生手段により冷却し、冷却精製混合ガスと分離ＣＯｚ
との熱授受を行うことによりＣＯｘを液化回収する。こ
の場合、精製混合ガスは分離ＣＯｚのみが液化する温度
まで冷却する。When concentrating COz in the mixed gas, an adsorption step is carried out so that COx does not exist in the purified mixed gas. Also,
C
Oz is completely separated (some co-adsorption mixed gas is included)
Supply purified mixed gas or heated purified mixed gas until At the end of this operation, the adsorption tower is pressurized with the purified mixed gas stored at the pressure during the adsorption step. Furthermore, after separating COz using purified mixed gas or heated purified mixed gas, when recovering, the purified mixed gas is cooled by a cold heat generating means, and the cooled purified mixed gas and separated COz
The COx is liquefied and recovered by exchanging heat with the COx. In this case, the purified mixed gas is cooled to a temperature at which only the separated COz liquefies.
この構成及び操作によれば、再生工程において濃縮ＣＣ
）ｚを真空ポンプ単独減圧手段による吸着剤からの脱離
操作に比べ、Ｃｏ２を含まない精製混合ガスあるいは加
熱精製混合ガスを供給するため、吸着剤からの脱離促進
が図れ、真空ポンプの動力が低減できる。また、加熱精
製混合ガスをＣＯｚが完全に分離するまで供給するよう
にすれば真空ポンプ減圧操作が不要とすることもできる
。According to this configuration and operation, in the regeneration process, concentrated CC
) Compared to the desorption operation of z from the adsorbent using a vacuum pump alone as a depressurizing means, since a purified mixed gas that does not contain Co2 or heated purified mixed gas is supplied, desorption from the adsorbent can be promoted, and the power of the vacuum pump is reduced. can be reduced. Further, if the heated purified mixed gas is supplied until COz is completely separated, the vacuum pump depressurization operation can be made unnecessary.
さらに、吸着剤の再生度合い及びＣＯ２回収率を向上で
きる。さらには、加圧工程時にはＣＯ２を含まない精製
混合ガスで再生工程後の吸着塔を昇圧することにより吸
着工程時にはＣＯｚの吸着量が増大できるため、吸着塔
のコンパクト化が図れる。また、冷却精製混合ガスによ
り濃縮ＣＯ２のみを液化するため、高純度のＣＯｚが効
率よく回収できる。Furthermore, the degree of regeneration of the adsorbent and the CO2 recovery rate can be improved. Furthermore, during the pressurization step, by pressurizing the adsorption tower after the regeneration step with a purified mixed gas that does not contain CO2, the amount of COz adsorbed during the adsorption step can be increased, so the adsorption tower can be made more compact. Furthermore, since only the concentrated CO2 is liquefied using the cooled purified mixed gas, highly purified COz can be efficiently recovered.
以下、本発明の一実施例を第１図により説明する。 An embodiment of the present invention will be described below with reference to FIG.
先ず本実施例の構成を説明する。水分吸着除去用の二基
の吸着塔ＩＡ、ＩＢをもちそれぞれ原料混合ガス供給用
切替え弁１１Ａ、ＩＩＢ、再生工程時の脱着ガス切替え
弁１３Ａ、１３Ｂ、精製混合ガス取り出し用切替え弁１
２Ａ、１２Ｂ、原料混合ガス圧送用の圧縮機４．吸着剤
再生用の真空ポンプ５．吸着塔ＩＡ、ＩＢからの精製混
合ガス中のＣＯ２濃縮用の吸着塔２Ａ、２Ｂ、吸着塔２
Ａ、２Ｂへの精製混合ガス供給用切替え弁２１Ａ。First, the configuration of this embodiment will be explained. It has two adsorption towers IA and IB for adsorption and removal of water, respectively, switching valves 11A and IIB for supplying raw material mixed gas, switching valves 13A and 13B for desorption gas during the regeneration process, and switching valve 1 for removing purified mixed gas.
2A, 12B, Compressor for pressure-feeding raw material mixed gas4. Vacuum pump for adsorbent regeneration5. Adsorption towers 2A and 2B for concentrating CO2 in purified mixed gas from adsorption towers IA and IB, and adsorption tower 2
Switching valve 21A for supplying purified mixed gas to A and 2B.
２１Ｂ、再生工程時の脱着ガス切替え弁２３Ａ。21B, desorption gas switching valve 23A during the regeneration process;
２３Ｂ、吸着塔２Ａ、２Ｂからの精製混合ガス取り出し
用切替え弁２２Ａ、２２Ｂ、吸着剤再生用真空ポンプ６
、精製混合ガス貯留タンク８．熱交換器２及び７．冷熱
発生用膨張タービン９、混合ガスタンク１０、加熱用熱
交換器５０及び６ｏとから構成され、さらに、吸着塔Ｉ
Ａ、ＩＢ、２Ａ。23B, switching valves 22A, 22B for taking out purified mixed gas from adsorption towers 2A, 2B, vacuum pump 6 for regenerating adsorbent
, purified mixed gas storage tank8. Heat exchangers 2 and 7. It is composed of an expansion turbine 9 for generating cold heat, a mixed gas tank 10, and heat exchangers 50 and 6o for heating, and further includes an adsorption tower I.
A, IB, 2A.
２Ｂとには精製混合ガス供給用切替え弁１５Ａ。2B is a purified mixed gas supply switching valve 15A.
１５Ｂ、２５Ａ、２５１３がそれぞれ設置されている。15B, 25A, and 2513 are installed, respectively.
次に、動作を説明する。ここでは、吸着塔ＩＡ及び２Ａ
が吸着工程を実施し吸着塔ＩＢ、２Ｂが再生及び加圧工
程を実施している動作状態で、以下を説明する。Next, the operation will be explained. Here, adsorption towers IA and 2A
The following will be explained under the operating condition in which the adsorption towers IB and 2B are performing the adsorption process and the regeneration and pressurization processes are being performed.
原料混合ガス１中の水分は予め、熱交換器２において冷
却・凝縮され、凝縮水３は系外に排出される。この後、
混合ガスは圧縮機４によって圧力Ｐａ＝１．６ａｔａま
で昇圧され、切替え弁１１Ａを介して吸着塔ＩＡに供給
される。ここで、熱交換器２の操作温度における蒸気正
分相当の原料混合ガス１中の残りの水分が吸着除去され
、精製混合ガスは吐出端１００Ａから切替え弁１２Ａを
介して吸着塔２Ａに供給される。吸着塔２ＡではＣ０２
が吸着濃縮され、残りの精製混合ガスは吐出端２００Ａ
から切替え弁２２Ａ及び３０ａを介してタンク８に貯蔵
される。タンク８に貯留された精製混合ガスの一部は切
替え弁３０ｄを介して膨張タービン９に供給され冷却さ
れる。冷却された精製混合ガスはタンク１ｏに貯留され
る。Moisture in the raw material mixed gas 1 is previously cooled and condensed in a heat exchanger 2, and condensed water 3 is discharged outside the system. After this,
The mixed gas is pressurized to a pressure Pa=1.6ata by the compressor 4, and is supplied to the adsorption tower IA via the switching valve 11A. Here, the remaining moisture in the raw material mixed gas 1 equivalent to the steam fraction at the operating temperature of the heat exchanger 2 is adsorbed and removed, and the purified mixed gas is supplied from the discharge end 100A to the adsorption tower 2A via the switching valve 12A. Ru. In adsorption tower 2A, C02
is adsorbed and concentrated, and the remaining purified mixed gas is discharged from the discharge end 200A.
The fuel is stored in the tank 8 via the switching valves 22A and 30a. A part of the purified mixed gas stored in the tank 8 is supplied to the expansion turbine 9 via the switching valve 30d and is cooled. The cooled purified mixed gas is stored in tank 1o.
一方、再生工程にある吸着塔ＩＢでは切替え弁１２Ｂ、
１５Ｂ、ＩＩＢ閉、１３Ｂ開の状態で真空ポンプ５によ
り吸着された水分は減圧・脱着され、吐出端４０から系
外に排出される。また、吸着塔２Ｂでは切替え弁２２Ｂ
、２５Ｂ、２１Ｂ閉。On the other hand, in the adsorption tower IB in the regeneration process, the switching valve 12B,
Moisture adsorbed by the vacuum pump 5 when 15B and IIB are closed and 13B is open is depressurized and desorbed, and is discharged from the discharge end 40 to the outside of the system. In addition, in the adsorption tower 2B, the switching valve 22B
, 25B, 21B closed.
２３Ｂ開の状態で吸着された他の混合成分を一部含む濃
縮Ｃ○２は真空ポンプ６により減圧・脱着され配管５０
を経て熱交換器７に供給される。熱交換器７では、混合
成分を一部含む濃縮ＣＯ２は貯留タンク１０からの冷却
された精製混合ガスによって冷却され、ＣＯｚのみが液
化される。液化Ｃ○２は弁９０を介して配管５０を経て
貯蔵される。熱交換器７で液化されたＣ○２以外の混合
ガス成分は、切替え弁３０ｆを介して膨張タービン９に
より冷却され、タンク９に貯留される。冷却された精製
混合ガスは熱交換器２において、原料混合ガス中の水分
を冷却・凝縮する冷熱源としても使用される。さらに、
再生工程にある吸着塔ＩＢ、２Ｂでは真空ポンプ５及び
６による減圧・脱着操作に加え、次の操作が行われる。Concentrated C○2 containing some of the other mixed components adsorbed when 23B is open is depressurized and desorbed by the vacuum pump 6 and transferred to the pipe 50.
It is supplied to the heat exchanger 7 through the. In the heat exchanger 7, the concentrated CO2 partially containing the mixed components is cooled by the cooled purified mixed gas from the storage tank 10, and only COz is liquefied. The liquefied C○2 is stored via the pipe 50 via the valve 90. The mixed gas components other than C○2 liquefied in the heat exchanger 7 are cooled by the expansion turbine 9 via the switching valve 30f, and stored in the tank 9. The cooled purified mixed gas is also used as a cold heat source in the heat exchanger 2 to cool and condense moisture in the raw mixed gas. moreover,
In the adsorption towers IB and 2B in the regeneration process, in addition to the depressurization and desorption operations by the vacuum pumps 5 and 6, the following operations are performed.
先ず、吸着塔ＩＢでは切換弁１２Ｂ、１１が閉、弁１５
Ｂ。First, in adsorption tower IB, switching valves 12B and 11 are closed, and valve 15 is closed.
B.
１３Ｂ開の状態でタンク８からのＣＯｚを含まない精製
混合ガスの一部が切替え弁３０ｂを介し配管５１を経て
吐出端１００Ｂから供給される。この場合、熱交換器６
０において加熱した精製混合ガスを供給してもよい。供
給された精製混合ガスあるいは加熱精製混合ガスにより
吸着された水分が吸着剤から脱離され、真空ポンプ６に
より系・外に排出される。この操作は排出混合ガス中の
水分露点が一４０℃以下になる様に精製混合ガスが順次
供給される。この場合、熱交換器２及び７で水分、ＣＯ
ｘを冷却した後の精製混合ガスを切替え弁３０ｈ、３０
ｅを介して吸着塔ＩＢに供給してもよい、吸着塔２Ｂで
は切替え弁２２Ｂ、２１Ｂ閉、２５Ｂ、２３Ｂ開の状態
でタンク８からの精製混合ガスが切替え弁３０ｃを介し
て配管５２を経て吐出端２００Ｂから供給される。この
場合、熱交換器５０で加熱した精製混合ガスを供給する
ことにより吸着剤からのＣＯｚの脱離を速めてもよい。With 13B open, a portion of the purified mixed gas not containing COz from the tank 8 is supplied from the discharge end 100B via the switching valve 30b and the pipe 51. In this case, the heat exchanger 6
A purified mixed gas heated at 0 may be supplied. Moisture adsorbed by the supplied purified mixed gas or heated purified mixed gas is desorbed from the adsorbent and discharged to the outside of the system by the vacuum pump 6. In this operation, purified mixed gas is sequentially supplied so that the water dew point in the discharged mixed gas becomes 140° C. or less. In this case, heat exchangers 2 and 7 contain water and CO2.
After cooling the purified mixed gas, the switching valves 30h and 30
In the adsorption tower 2B, the purified mixed gas from the tank 8 is passed through the pipe 52 via the switching valve 30c with the switching valves 22B and 21B closed and 25B and 23B open. It is supplied from the discharge end 200B. In this case, the desorption of COz from the adsorbent may be accelerated by supplying purified mixed gas heated by the heat exchanger 50.
供給された精製混合ガスあるいは加熱精製混合ガスによ
り吸着された混合ガス成分が一部含む濃縮Ｃｏｘが吸着
剤から脱離され、真空ポンプ６により熱交換器７に供給
される。吸着塔２Ｂへの精製混合ガスは真空ポンプ６の
吸引側でＣＯ２濃度が１％以下になる様に、順次、供給
される。Concentrated Cox partially containing mixed gas components adsorbed by the supplied purified mixed gas or heated purified mixed gas is desorbed from the adsorbent and supplied to the heat exchanger 7 by the vacuum pump 6 . The purified mixed gas is sequentially supplied to the adsorption tower 2B so that the CO2 concentration becomes 1% or less on the suction side of the vacuum pump 6.
この場合、熱交換器２及び７において水分、ＣＯ２を冷
却した後の精製混合ガスを切替え弁３０ｅ。In this case, the purified mixed gas after cooling moisture and CO2 in the heat exchangers 2 and 7 is transferred to the switching valve 30e.
３０ｇを介して配管５２を経て吐出端２００Ｂから吸着
塔２Ｂに供給してもよい。It may also be supplied to the adsorption tower 2B from the discharge end 200B via the pipe 52 via 30g.
さらに、吸着塔ＩＢ及び２Ｂが真空ポンプ５及び６、あ
るいは精製混合ガスによって水分、 ＣＯ２が吸着剤か
ら前述の条件に脱離れた時点で吸着塔ＩＢ及び２Ｂがタ
ンク８からの精製混合ガスにより昇圧される。この後、
吸着塔ＩＡとＩＢ、２Ａと２Ｂが切替り、吸着塔ＩＡ及
び２Ａが再生工程を、吸着塔ＩＢ及び２Ｂが吸着工程を
実施し、順次、この操作を繰り返犬す。Furthermore, when the adsorption towers IB and 2B are depressurized by the vacuum pumps 5 and 6 or the purified mixed gas or the purified mixed gas from the adsorbent under the above-mentioned conditions, the adsorption towers IB and 2B are pressurized by the purified mixed gas from the tank 8. be done. After this,
The adsorption towers IA and IB, 2A and 2B are switched, the adsorption towers IA and 2A perform the regeneration process, the adsorption towers IB and 2B perform the adsorption process, and this operation is repeated in sequence.
ＣＯｘの回収システム及び運転方法は第２図に示した様
なガスタービン５００．燃焼器５０１゜発電機５０２．
排熱回収熱交換器５０３．蒸気タービン５０４９発電機
５０６及び熱交換器５０５等から構成される複合発電プ
ラントからの排ガス１中のＣＯｚの回収に適しているが
、これに限定゛されるものではない。The COx recovery system and operating method is a gas turbine 500 as shown in FIG. Combustor 501° Generator 502.
Exhaust heat recovery heat exchanger 503. The present invention is suitable for recovering COz in the exhaust gas 1 from a combined power generation plant composed of a steam turbine 5049, a generator 506, a heat exchanger 505, etc., but is not limited thereto.
本発明によれば、濃縮ＣＯｚを真空ポンプ単独減圧手段
により吸着剤から脱離する操作に比べ、ＣＯｚを含まな
い精製混合ガスにより濃縮ＣＯｚを脱離するため、吸着
剤からのＣＯｚの脱離促進を速める効果がある。この操
作で、濃縮ＣＯｚ脱離後の精製混合ガス中のＣＯｚ濃度
が１％以下になるまで精製混合ガスあるいは加熱精製混
合ガスを供給するため、吸着剤の再生促進が図れ、かつ
、ＣＯｚの回収率を向上できる効果がある。この操作で
は、真空ポンプを用いずに、精製混合ガスのみで濃縮Ｃ
Ｏｚを脱離できるため、所要動力の低減を図れる。また
、精製混合ガスを供給する操作により吸着塔を昇圧する
ため、吸着工程時にはＣＯｘの吸着量を増大することが
でき、装置のコンパクト化が図れる効果がある。さらに
、精製混合ガスをＣＯｚのみが液化する温度まで冷却し
、冷却精製混合ガスにより、一部共吸着している他の混
合ガスを含む脱離ガスからＣＯｘのみを液化回収するた
め、高純度のＣＯｚが効率よく回収できる効果がある。According to the present invention, compared to an operation in which concentrated COz is desorbed from an adsorbent using a vacuum pump alone for decompression, since concentrated COz is desorbed using a purified mixed gas that does not contain COz, the desorption of COz from the adsorbent is promoted. It has the effect of accelerating. With this operation, purified mixed gas or heated purified mixed gas is supplied until the COz concentration in the purified mixed gas after desorption of concentrated COz becomes 1% or less, so it is possible to promote the regeneration of the adsorbent and to recover COz. This has the effect of improving the rate. In this operation, concentrated C is used only with purified mixed gas without using a vacuum pump.
Since Oz can be desorbed, the required power can be reduced. Furthermore, since the pressure of the adsorption tower is increased by the operation of supplying the purified mixed gas, the amount of COx adsorbed can be increased during the adsorption step, which has the effect of making the apparatus more compact. Furthermore, the purified mixed gas is cooled to a temperature at which only COz liquefies, and the cooled purified mixed gas is used to liquefy and recover only COx from the desorbed gas containing other mixed gases that are partially co-adsorbed. This has the effect of efficiently recovering COz.
第１図は本発明の一実施例の系統図、第２図は複合発電
プラントの系統図である。
２．７，５０，６０・・・熱交換器、４・・・圧縮機、
５゜６・・・真空ポンプ、ＬＡ、Ｂ、２Ａ、Ｂ・・・吸
着塔、第１図
第２図
８Ｆ−FIG. 1 is a system diagram of an embodiment of the present invention, and FIG. 2 is a system diagram of a combined power generation plant. 2.7,50,60...heat exchanger, 4...compressor,
5゜6...Vacuum pump, LA, B, 2A, B...Adsorption tower, Figure 1, Figure 2, 8F-
Claims (1)
スを吸着・分離し低吸着ガスを精製する方法において、 前記低吸着精製ガスを冷却あるいは加熱する手段と冷却
あるいは加熱低吸着精製ガスにより前記高吸着ガスを除
去あるいは回収することを特徴とする混合ガスの分離回
収システム。 ２、請求項１において、ガスタービン、蒸気タービン、
排熱回収熱交換器等からなる複合発電プラントからの排
ガス中の炭酸ガスの回収を行う排ガス中からの炭酸ガス
の回収法。３、請求項１において、加熱低吸着精製ガス
により高吸着ガスを脱着した後、冷却低吸着精製ガスに
より脱着高吸着ガスを冷却・液化して回収する混合ガス
の分離回収システム。[Claims] 1. A method for adsorbing and separating a highly adsorbed gas in a mixed gas to purify a low adsorbed gas by pressure swing adsorption method, comprising: a means for cooling or heating the purified gas with low adsorption; A mixed gas separation and recovery system, characterized in that the high adsorption gas is removed or recovered using a heated low adsorption purified gas. 2. In claim 1, a gas turbine, a steam turbine,
A method for recovering carbon dioxide from exhaust gas, which recovers carbon dioxide from exhaust gas from a combined power generation plant that consists of an exhaust heat recovery heat exchanger, etc. 3. A mixed gas separation and recovery system according to claim 1, in which the highly adsorbed gas is desorbed by the heated, low-adsorbent purified gas, and then the desorbed, highly adsorbed gas is cooled and liquefied by the cooled, low-adsorbed purified gas, and then recovered.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2246997A JPH04126512A (en) | 1990-09-19 | 1990-09-19 | System for separating and recovering gaseous mixture and its operation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2246997A JPH04126512A (en) | 1990-09-19 | 1990-09-19 | System for separating and recovering gaseous mixture and its operation |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04126512A true JPH04126512A (en) | 1992-04-27 |
Family
ID=17156841
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2246997A Pending JPH04126512A (en) | 1990-09-19 | 1990-09-19 | System for separating and recovering gaseous mixture and its operation |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04126512A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7474090B2 (en) * | 2004-10-22 | 2009-01-06 | Delphi Technologies, Inc. | Position sensor and assembly |
| JP2019141759A (en) * | 2018-02-16 | 2019-08-29 | 大陽日酸株式会社 | Gas refining apparatus, gas refining method, propene producing apparatus and propane producing apparatus |
| JP2019177315A (en) * | 2018-03-30 | 2019-10-17 | 大陽日酸株式会社 | Gas refining apparatus and gas refining method |
-
1990
- 1990-09-19 JP JP2246997A patent/JPH04126512A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7474090B2 (en) * | 2004-10-22 | 2009-01-06 | Delphi Technologies, Inc. | Position sensor and assembly |
| JP2019141759A (en) * | 2018-02-16 | 2019-08-29 | 大陽日酸株式会社 | Gas refining apparatus, gas refining method, propene producing apparatus and propane producing apparatus |
| US11471819B2 (en) | 2018-02-16 | 2022-10-18 | Taiyo Nippon Sanso Corporation | Gas refining apparatus, gas refining method, propene manufacturing apparatus, and propane manufacturing apparatus |
| JP2019177315A (en) * | 2018-03-30 | 2019-10-17 | 大陽日酸株式会社 | Gas refining apparatus and gas refining method |
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