JP3364103B2 - Control method of absorption liquid in decarbonation equipment - Google Patents
Control method of absorption liquid in decarbonation equipmentInfo
- Publication number
- JP3364103B2 JP3364103B2 JP02724097A JP2724097A JP3364103B2 JP 3364103 B2 JP3364103 B2 JP 3364103B2 JP 02724097 A JP02724097 A JP 02724097A JP 2724097 A JP2724097 A JP 2724097A JP 3364103 B2 JP3364103 B2 JP 3364103B2
- Authority
- JP
- Japan
- Prior art keywords
- carbon dioxide
- liquid
- absorption
- water
- tower
- 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.)
- Expired - Lifetime
Links
Classifications
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、二酸化炭素を含む
ガスをアミン化合物を含む吸収液により吸収する脱炭酸
プロセスにおける吸収液の液量及び濃度制御方法に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for controlling the amount and concentration of an absorbing liquid in a decarboxylation process in which a gas containing carbon dioxide is absorbed by an absorbing liquid containing an amine compound.
【０００２】[0002]
【従来の技術】近年、火力発電設備やボイラー設備で
は、多量の石炭、重油あるいは超重質油を燃料に用いて
おり、大気汚染防止及び地球環境の清浄化の見地から、
二酸化硫黄を主とする硫黄酸化物、窒素酸化物、二酸化
炭素等の放出に関する量的、濃度的抑制が問題になって
いる。最近、二酸化炭素については、フロンガスやメタ
ンガスと共に地球の温暖化の見地から、排出の抑制が検
討されている。そのため、例えば、ＰＳＡ（圧力スウィ
ング）法、膜分離濃縮法および塩基性化合物による反応
吸収する方法等が検討されている。2. Description of the Related Art In recent years, a large amount of coal, heavy oil or super heavy oil has been used as fuel in thermal power generation equipment and boiler equipment. From the standpoint of preventing air pollution and cleaning the global environment,
There has been a problem in quantitative and concentration control of the release of sulfur oxides, nitrogen oxides, carbon dioxide, etc., which mainly contain sulfur dioxide. Recently, with respect to carbon dioxide, suppression of emission has been studied from the viewpoint of global warming together with CFC gas and methane gas. Therefore, for example, a PSA (pressure swing) method, a membrane separation concentration method, a reaction absorption method using a basic compound, and the like have been studied.
【０００３】米国特許５，３１８，７５８号には、塩基
性アミン化合物を吸収液として脱炭酸を行う方法が提案
されている。この方法では、燃焼排ガス中の水分が脱炭
酸設備に流入する量と、吸収液中の水分がガスに同伴し
て脱炭酸設備から流出する量とのバランスが崩れた場合
に、吸収液中のアミン濃度が変動しやすい。アミン濃度
が変動すると、吸収液の二酸化炭素吸収率や再生塔にお
ける負荷吸収液（二酸化炭素吸収後の吸収液）を再生す
るために要する蒸気消費量が変動する。従来、吸収液の
濃度を一定に保つために工程の各部分の分析測定、例え
ば二酸化炭素吸収部へ吸収液を供給するライン等の吸収
液中のアミン濃度の手作業による分析が行われ、これら
の情報を元に水や吸収液の増減が行われていた。このた
め、吸収液量や、アミン濃度の経時変化が大きく、二酸
化炭素の吸収効率が変動し、操作の安定性や、エネルギ
ー消費の点で問題があった。US Pat. No. 5,318,758 proposes a method for decarboxylation using a basic amine compound as an absorbing liquid. In this method, when the balance between the amount of water in the combustion exhaust gas flowing into the decarbonation facility and the amount of water in the absorbing liquid flowing out of the decarbonating facility accompanied with the gas is lost, The amine concentration is likely to fluctuate. When the amine concentration fluctuates, the carbon dioxide absorption rate of the absorption liquid and the vapor consumption required to regenerate the load absorption liquid (absorption liquid after carbon dioxide absorption) in the regeneration tower also fluctuate. Conventionally, in order to keep the concentration of the absorption liquid constant, analytical measurement of each part of the process, for example, manual analysis of the amine concentration in the absorption liquid such as a line for supplying the absorption liquid to the carbon dioxide absorption part is performed, and The amount of water and absorbing liquid was increased or decreased based on the information on. Therefore, the amount of absorbing liquid and the concentration of amine change with time, and the absorption efficiency of carbon dioxide fluctuates, causing problems in stability of operation and energy consumption.
【０００４】[0004]
【発明が解決しようとする課題】本発明は、二酸化炭素
を含むガスをアミンを含む吸収液と気液接触して二酸化
炭素を吸収する脱炭酸プロセスにおいて、吸収液量や吸
収液中のアミン濃度が一定に保たれ、二酸化炭素吸収率
の変動が少なく、安定な操作が可能で、エネルギー消費
の軽減された吸収液の制御方法を提供するものである。DISCLOSURE OF THE INVENTION The present invention relates to a decarboxylation process in which a gas containing carbon dioxide is brought into liquid-liquid contact with an absorption liquid containing amine to absorb carbon dioxide, and the amount of the absorption liquid and the amine concentration in the absorption liquid. It is intended to provide a method of controlling an absorbing solution in which the absorption rate is kept constant, the fluctuation of carbon dioxide absorption rate is small, stable operation is possible, and energy consumption is reduced.
【０００５】[0005]
【課題を解決するための手段】本発明者らは、前記課題
に付き鋭意検討した結果、本発明を完成するに至った。The inventors of the present invention have completed the present invention as a result of extensive studies on the above problems.
【０００６】すなわち、本発明は、下部に二酸化炭素吸
収部と上部にアミン回収部を有する二酸化炭素吸収塔
と、塔頂より二酸化炭素と水分を放出し塔底より再生さ
れた吸収液を排出する再生塔と、アミン回収部から抜き
出されたアミン含有水を貯蔵する水貯槽とからなる脱炭
酸設備において、吸収液の液面測定可能部に液面計を設
けて、該液面が一定になるように水貯槽から二酸化炭素
吸収部に供給される水の流量を調節することにより、脱
炭酸設備内の吸収液量を一定に保ち、且つ、二酸化炭素
吸収部に供給する吸収液の濃度を一定に保つことを特徴
とする吸収液の制御方法に関するものであり、液面測定
可能部が二酸化炭素吸収塔の塔底液滞留部、再生塔の塔
底液滞留部、または吸収液再生塔から二酸化炭素吸収塔
へ吸収液を供給するラインに設けられた吸収液サージタ
ンクであり、二酸化炭素吸収塔へ吸収液を供給するライ
ンに流量計を設け、水貯槽から二酸化炭素吸収部に水を
供給するラインに流量計と流量調節弁を設ける吸収液の
制御方法である。本発明は、さらに、流量計及び液面計
による測定値に基づいて、再生された吸収液が二酸化炭
素吸収部に供給される流量と水貯槽から二酸化炭素吸収
部に供給される水の流量が下記式により定められる吸収
液の制御方法に関するものである。That is, according to the present invention, a carbon dioxide absorption column having a carbon dioxide absorption part in the lower part and an amine recovery part in the upper part, carbon dioxide and water are released from the top of the column, and the regenerated absorption liquid is discharged from the bottom of the column. In a decarbonation facility consisting of a regeneration tower and a water storage tank that stores the amine-containing water extracted from the amine recovery unit, a liquid level gauge is provided in the liquid level measurable unit of the absorbing liquid to keep the liquid level constant. By adjusting the flow rate of water supplied from the water storage tank to the carbon dioxide absorption unit so that the amount of the absorption liquid in the decarbonation equipment is kept constant, and the concentration of the absorption liquid supplied to the carbon dioxide absorption unit is adjusted. The present invention relates to a method for controlling an absorption liquid, which is characterized in that the liquid level measurable part is a bottom liquid retention part of a carbon dioxide absorption tower, a bottom liquid retention part of a regeneration tower, or an absorption liquid regeneration tower. Supply absorption liquid to carbon dioxide absorption tower It is an absorbing liquid surge tank installed in the inn.A flow meter is installed in the line that supplies the absorbing liquid to the carbon dioxide absorption tower, and a flow meter and a flow control valve are installed in the line that supplies water from the water storage tank to the carbon dioxide absorbing unit. This is a method of controlling the absorbing liquid to be provided. The present invention is further based on the flow rate of the regenerated absorption liquid supplied to the carbon dioxide absorption part and the flow rate of water supplied from the water storage tank to the carbon dioxide absorption part, based on the measurement values by the flow meter and the liquid level gauge. The present invention relates to a method of controlling the absorbing liquid defined by the following formula.
【０００７】[0007]
【数２】 [Equation 2]
【０００８】[0008]
【発明の実施の形態】本発明において、二酸化炭素を含
むガスとは、燃料用のガスであっても、燃料の燃焼排ガ
スであっても、その他様々なガスであってもよい。対象
となるガスは水分や硫黄酸化物、窒素酸化物、酸素ある
いはその他の酸性ガスを含んでいてもよい。ガスの圧力
は加圧であっても、減圧であってもよく、温度は低温で
あっても、高温であってもよく、特に制限はない。好ま
しくは、常圧の燃焼排ガスである。BEST MODE FOR CARRYING OUT THE INVENTION In the present invention, the gas containing carbon dioxide may be a gas for fuel, a combustion exhaust gas of fuel, or various other gases. The target gas may contain water, sulfur oxides, nitrogen oxides, oxygen, or other acidic gas. The pressure of the gas may be increased or decreased, the temperature may be low or high, and there is no particular limitation. The combustion exhaust gas at normal pressure is preferable.
【０００９】本発明において使用するアミンは、モノエ
タノールアミン、２−アミノ−２−メチル−１−プロパ
ノールのようなアルコール性水酸基含有１級アミン類、
ジエタノールアミン、２−メチルアミノエタノールのよ
うなアルコール性水酸基含有２級アミン類、トリエタノ
ールアミン、Ｎ−メチルジエタノールアミンのようなア
ルコール性水酸基含有３級アミン類、エチレンジアミ
ン、トリエチレンジアミン、ジエチレントリアミンのよ
うなポリエチレンポリアミン類、ピペラジン、２−メチ
ルピペラジン、ジメチルピペラジン、１−（２−ヒドロ
キシエチル）ピペラジン、２−ピペリジンエタノール、
ピペリジン類、ピロリジン類、２−ピリジンメタノール
のような環状アミン類、キシリレンジアミン、１，３−
ジアミノ−２−プロパノール、２−（２−アミノエチル
アミノ）エタノールのようなポリアミン類、メチルアミ
ノカルボン酸のようなアミノ酸類等及びこれらの混合物
が挙げられる。これらのアミン類は通常１０〜７０重量
％の水溶液として使用される。また吸収液には、二酸化
炭素吸収促進剤、あるいは塩基性炭酸銅のような腐食防
止剤を、さらには、その他の媒体としてメタノール、ポ
リエチレングリコール、スルフォラン等を加えることが
できる。The amine used in the present invention is an alcoholic hydroxyl group-containing primary amine such as monoethanolamine or 2-amino-2-methyl-1-propanol,
Diethanolamine, alcoholic hydroxyl group-containing secondary amines such as 2-methylaminoethanol, triethanolamine, alcoholic hydroxyl group-containing tertiary amines such as N-methyldiethanolamine, polyethylene polyamines such as ethylenediamine, triethylenediamine and diethylenetriamine , Piperazine, 2-methylpiperazine, dimethylpiperazine, 1- (2-hydroxyethyl) piperazine, 2-piperidine ethanol,
Piperidines, pyrrolidines, cyclic amines such as 2-pyridinemethanol, xylylenediamine, 1,3-
Examples include polyamines such as diamino-2-propanol, 2- (2-aminoethylamino) ethanol, amino acids such as methylaminocarboxylic acid, and mixtures thereof. These amines are usually used as an aqueous solution of 10 to 70% by weight. Further, a carbon dioxide absorption promoter or a corrosion inhibitor such as basic copper carbonate can be added to the absorbing solution, and further methanol, polyethylene glycol, sulfolane or the like can be added as another medium.
【００１０】二酸化炭素吸収部とアミン吸収部は、充填
塔であっても、棚段塔であってもよい。The carbon dioxide absorption section and the amine absorption section may be packed columns or plate columns.
【００１１】アミンを含む吸収液は、二酸化炭素と反応
して、例えば、カーバメートのようなアミンの炭酸塩錯
体を生成するが、加熱により分解し、二酸化炭素を放出
してアミンが再生される。再生された吸収液はそのまま
二酸化炭素吸収部にリサイクルして使用することができ
る。The absorption liquid containing amine reacts with carbon dioxide to form a carbonate complex of amine such as carbamate, which is decomposed by heating and releases carbon dioxide to regenerate the amine. The regenerated absorption liquid can be recycled and used as it is in the carbon dioxide absorption unit.
【００１２】再生塔上部から放出された二酸化炭素は水
分を伴うので、コンデンサーにより冷却され、分離器に
導かれて二酸化炭素と凝縮水に分離され、凝縮水の一部
は排ガス中のアミンを回収するために前記二酸化炭素吸
収塔のアミン回収部に供給される。アミン回収部ではそ
の底部からアミンを含む水が抜き出され、水貯槽に貯蔵
される。水貯槽に貯蔵された水の一部は二酸化炭素吸収
部へ供給され、残りの一部はアミン回収部の頂部に循環
供給される。Since carbon dioxide released from the upper part of the regeneration tower is accompanied by water, it is cooled by a condenser, guided to a separator and separated into carbon dioxide and condensed water, and a part of the condensed water recovers amine in exhaust gas. In order to do so, it is supplied to the amine recovery section of the carbon dioxide absorption tower. In the amine recovery section, water containing amine is extracted from the bottom and stored in a water storage tank. A part of the water stored in the water storage tank is supplied to the carbon dioxide absorption section, and the remaining part is circulated and supplied to the top of the amine recovery section.
【００１３】本発明で液の流量を測定する方法として
は、オリフィス、抵抗体式、流体振動式、浮き子式、翼
車式、電磁式、超音波式等従来のものが使用できる。As a method for measuring the flow rate of the liquid in the present invention, conventional methods such as an orifice, a resistor type, a fluid vibration type, a float type, an impeller type, an electromagnetic type and an ultrasonic type can be used.
【００１４】吸収液の液面測定可能部とは、負荷吸収液
または再生後の吸収液が滞留し、液深を持ち、気液界面
を有する所であり、サージタンク、二酸化炭素吸収塔底
部の液滞留部、再生塔底部の液滞留部等が挙げられる。The liquid level measurable part of the absorption liquid is a place where the load absorption liquid or the absorption liquid after regeneration is retained, has a liquid depth, and has a gas-liquid interface, and is located at the bottom of the surge tank and the carbon dioxide absorption tower. Examples include a liquid retention section and a liquid retention section at the bottom of the regeneration tower.
【００１５】本発明で液面を測定する方法としては、差
圧式、浮力式、静電容量式、超音波式等従来のものが使
用できる。As the method of measuring the liquid level in the present invention, a conventional method such as a differential pressure type, a buoyancy type, a capacitance type, an ultrasonic type can be used.
【００１６】本発明で制御信号に応じて流量を調節する
調節弁としては、ボール弁、玉型弁、ベンチュリー弁、
複座弁等従来のものが使用できる。In the present invention, the control valve for adjusting the flow rate according to the control signal includes a ball valve, a lens valve, a Venturi valve,
Conventional valves such as double seat valves can be used.
【００１７】本発明で各種計器から得られる流量及び液
量の値を処理する演算器としては、従来のものが使用で
きる。また、プロセスコンピューター、マイクロコンピ
ューター、パーソナルコンピューター等も利用可能であ
り、さらに、直接ディジタルコントロール又はディスパ
ーストコントロールシステムにより流量及び液量の測定
結果に基づきプロセス全体をシステム的に管理すること
も可能である。計測器のサンプリング間隔は１時間以
下、好ましくは１０分以下、更に好ましくは１分以下で
ある。前記計器からのコンピューターへの入力値を使用
して、例えば、次式のような演算を行い制御値を求める
ことができる。In the present invention, a conventional arithmetic unit can be used as the arithmetic unit for processing the values of the flow rate and the liquid amount obtained from various instruments. Further, a process computer, a microcomputer, a personal computer or the like can be used, and further, the entire process can be systematically controlled based on the measurement results of the flow rate and the liquid amount by the digital control or the disperse control system. . The sampling interval of the measuring instrument is 1 hour or less, preferably 10 minutes or less, and more preferably 1 minute or less. Using the input value from the instrument to the computer, for example, the control value can be obtained by performing the following calculation.
【００１８】[0018]
【数３】 [Equation 3]
【００１９】なお、上記数式は流量計及び流量調節弁を
水貯槽の出口側に設置した場合のものであり、それらを
変形して、他の位置に流量計及び流量調節弁を設置した
場合には、数式を変形して上記に相当する流量を求めて
同じ考え方により液量及び流量調節する方法も本発明に
含まれる。上記の水流量はコンピューターから出力さ
れ、直接又は制御器を経由して各調節弁等を作動させ
る。この関係を図２及び図３に示す。The above formula is for the case where the flow meter and the flow control valve are installed on the outlet side of the water storage tank, and when these are modified and the flow meter and the flow control valve are installed at other positions. In the present invention, a method of modifying the mathematical expression to obtain the flow rate corresponding to the above and adjusting the liquid amount and the flow rate by the same idea is also included in the present invention. The above water flow rate is output from a computer, and each control valve or the like is operated directly or via a controller. This relationship is shown in FIGS.
【００２０】以下、本発明を図により説明する。図１は
本発明のプロセスフローシートである。図で点線は計器
から演算器への出力又は制御器から調節弁への入力を示
す。二酸化炭素を含む燃焼排ガス１を、ガス冷却塔２の
上部に供給し適切な温度まで冷却した後、二酸化炭素吸
収塔３の下部に設けられた二酸化炭素吸収部４に供給
し、吸収液２１を二酸化炭素吸収部４の頂部より流下さ
せ、気液接触により排ガス中の二酸化炭素を吸収する。
二酸化炭素除去後の排ガスはアミン回収部５を上昇し、
アミン回収部５の頂部から供給されるアミン回収用水２
２と気液接触させて、同伴するアミンを水相に回収した
後、二酸化炭素吸収塔３の頂部から排ガス２３として排
出される。二酸化炭素を吸収した負荷吸収液２４は吸収
塔３の底部から排出され、熱交換器８により加熱されて
再生塔９に供給される。再生塔９に供給された負荷吸収
液２４は８０〜１５０℃に加熱されて二酸化炭素を放出
し再生される。再生された吸収液２５は再生塔９の底部
から排出され、前記熱交換器８により冷却されて、サー
ジタンク７に供給される。サージタンク７から流出した
吸収液２１は流量計１４により流量が測定され、二酸化
炭素吸収部４の頂部に吸収液２１として供給される。吸
収液サージタンク７には適切な位置に液面計１５が設置
されている。液面計１５による測定値は系内の吸収液量
を示すものであり、系内の吸収液量が設定レベルより上
か下かが判定される。再生塔９の頂部から放出された二
酸化炭素２６は、水分を含み、コンデンサー１０により
冷却され、分離器１１により凝縮水２７が分離され、乾
燥二酸化炭素２８は系外に排出される。凝縮水２７の一
部は再生塔９に還流され、残りはアミン回収用水２２と
してアミン回収部５の頂部に供給され、二酸化炭素吸収
後の排ガスに同伴するアミンを吸収する。アミン回収部
５の底部からは、アミン含有水２９が抜き出され、水貯
槽６に貯蔵される。水貯槽６に貯蔵された水の一部は流
量計１６により流量を測定し、調節弁１７により所定量
の水３０が二酸化炭素吸収部４へ供給され、残りの水は
アミン回収部５の頂部へ循環供給される。この際、二酸
化炭素吸収部４へ供給される水３０の流量FWは所定流量
FWSETとなるように、流量計１４により測定された吸収
液流量FL、液面計１５により測定された吸収液レベル、
及び流量計１６により測定された水流量を、演算器１２
に入力し、吸収液レベル偏差値εL及び水流量偏差値εF
から制御器１３を経て、弁１７の開度が決定され、操作
される。水貯槽６には、図示していないが、水を補給ま
たは排出できるラインが設けられていてもよい。この結
果、設備内の吸収液流量及びアミン濃度が適切化され、
排ガス中の二酸化炭素を効率よく吸収し、設備の運転が
容易に且つ安定に行われる。The present invention will be described below with reference to the drawings. FIG. 1 is a process flow sheet of the present invention. In the figure, the dotted line indicates the output from the meter to the calculator or the input from the controller to the control valve. The combustion exhaust gas 1 containing carbon dioxide is supplied to the upper part of the gas cooling tower 2 and cooled to an appropriate temperature, and then supplied to the carbon dioxide absorption part 4 provided in the lower part of the carbon dioxide absorption tower 3 to absorb the absorption liquid 21. It is made to flow down from the top of the carbon dioxide absorption part 4, and the carbon dioxide in the exhaust gas is absorbed by gas-liquid contact.
The exhaust gas after removal of carbon dioxide rises in the amine recovery section 5,
Amine recovery water 2 supplied from the top of the amine recovery section 5
After the gas and liquid are brought into contact with 2 to collect the accompanying amine in the aqueous phase, the exhaust gas 23 is discharged from the top of the carbon dioxide absorption tower 3. The load absorption liquid 24 that has absorbed carbon dioxide is discharged from the bottom of the absorption tower 3, heated by the heat exchanger 8 and supplied to the regeneration tower 9. The load absorbing liquid 24 supplied to the regeneration tower 9 is heated to 80 to 150 ° C. to release carbon dioxide and is regenerated. The regenerated absorption liquid 25 is discharged from the bottom of the regeneration tower 9, cooled by the heat exchanger 8 and supplied to the surge tank 7. The flow rate of the absorption liquid 21 flowing out from the surge tank 7 is measured by the flow meter 14, and the absorption liquid 21 is supplied to the top of the carbon dioxide absorption unit 4 as the absorption liquid 21. A liquid level gauge 15 is installed at an appropriate position in the absorbing liquid surge tank 7. The value measured by the liquid level gauge 15 indicates the amount of the absorbing liquid in the system, and it is determined whether the amount of the absorbing liquid in the system is above or below the set level. The carbon dioxide 26 discharged from the top of the regeneration tower 9 contains water, is cooled by the condenser 10, the condensed water 27 is separated by the separator 11, and the dry carbon dioxide 28 is discharged out of the system. Part of the condensed water 27 is refluxed to the regeneration tower 9, and the rest is supplied as amine recovery water 22 to the top of the amine recovery section 5 to absorb the amine that accompanies the exhaust gas after carbon dioxide absorption. The amine-containing water 29 is extracted from the bottom of the amine recovery unit 5 and stored in the water storage tank 6. The flow rate of a part of the water stored in the water storage tank 6 is measured by a flow meter 16, a predetermined amount of water 30 is supplied to the carbon dioxide absorption unit 4 by a control valve 17, and the remaining water is the top of the amine recovery unit 5. It is circulated and supplied to. At this time, the flow rate F W of the water 30 supplied to the carbon dioxide absorption unit 4 is a predetermined flow rate.
As the F WSET, the absorption liquid was measured by the flow meter 14 flow F L, the absorption liquid level measured by the level gauge 15,
And the water flow rate measured by the flow meter 16
To the absorption liquid level deviation value ε L and water flow rate deviation value ε F
To the controller 13, the opening of the valve 17 is determined and operated. Although not shown, the water storage tank 6 may be provided with a line capable of supplying or discharging water. As a result, the absorption liquid flow rate and amine concentration in the equipment are optimized,
Carbon dioxide in the exhaust gas is efficiently absorbed, and the equipment can be operated easily and stably.
【００２１】[0021]
【実施例】以下、実施例により本発明を具体的に説明す
るが、本発明はこれらに限定されるものではない。EXAMPLES The present invention will now be described in detail with reference to examples, but the present invention is not limited thereto.
【００２２】（実施例１）下部に二酸化炭素吸収部と上
部にアミン回収部を有する二酸化炭素吸収塔と、塔頂よ
り二酸化炭素と水分を放出し塔底より再生された吸収液
を排出する再生塔と、アミン回収部からの水を貯蔵する
水貯槽と、吸収液サージタンクとからなる吸収再生設備
において、二酸化炭素吸収部に再生された吸収液を供給
するラインに電磁式流量計と流量調節用複座弁を設置
し、吸収液サージタンクに差圧式液面計を設置し、水貯
槽の出口側の二酸化炭素吸収部への水供給ラインに電磁
式流量計と流量調節用複座弁を設置し、分離器からアミ
ン回収部への水流量の設定を行った後、前記液面計及び
流量計による測定値を計算機に入力した。入力値に基づ
いて、水貯槽から二酸化炭素吸収部に供給される水の流
量を計算し、制御器を経て、流量調節用弁の開度を調節
できるようにした。二酸化炭素１０％を含む脱硫後燃焼
排ガス５００Ｎｍ3／Ｈｒを、吸収塔の二酸化炭素吸収
部に供給し、モノエタノールアミン３０重量％の水溶液
とガス／液比２で６０℃で向流接触させ、二酸化炭素を
吸収した。二酸化炭素吸収後の排ガスは、アミン回収部
で、凝縮水の一部と気液接触させ、アミンを水相に回収
し、大気に放出された。負荷吸収液は、再生塔において
液温１３０℃に加熱され二酸化炭素と水分を放出した。
水貯槽から二酸化炭素吸収部へ供給される水流量は計算
結果にしたがって、不足分を送液した。この結果、設備
内の吸収液保有量が８６０〜８８０ｋｇ、アミン濃度が
２９７〜３０４ｇ／ｋｇと安定して運転することができ
るようになり、排ガス中の二酸化炭素を効率よく吸収す
ることができるようになった。結果を図４及び図５に示
す。(Example 1) A carbon dioxide absorption column having a carbon dioxide absorption section in the lower part and an amine recovery section in the upper part, carbon dioxide and water are discharged from the top of the tower, and the regenerated absorption liquid is discharged from the bottom of the tower. In an absorption / regeneration facility consisting of a tower, a water storage tank that stores water from the amine recovery unit, and an absorption liquid surge tank, an electromagnetic flow meter and flow rate adjustment are provided in the line that supplies the regenerated absorption liquid to the carbon dioxide absorption unit. Installed a double-seat valve for water absorption, installed a differential pressure type liquid level gauge in the absorbing liquid surge tank, and installed an electromagnetic flow meter and a double-seat valve for flow control in the water supply line to the carbon dioxide absorption part on the outlet side of the water storage tank. After installing and setting the water flow rate from the separator to the amine recovery part, the measured values by the liquid level meter and the flow meter were input to the computer. Based on the input value, the flow rate of the water supplied from the water storage tank to the carbon dioxide absorption unit was calculated, and the opening of the flow rate control valve could be adjusted via the controller. Desulfurized combustion exhaust gas 500 Nm 3 / Hr containing 10% carbon dioxide was supplied to the carbon dioxide absorption section of the absorption tower, and was brought into countercurrent contact with an aqueous solution of 30 wt% monoethanolamine at a gas / liquid ratio of 2 at 60 ° C. Absorbed carbon dioxide. The exhaust gas after carbon dioxide absorption was brought into gas-liquid contact with a part of the condensed water in the amine recovery section to recover the amine in the water phase and released into the atmosphere. The load absorption liquid was heated to a liquid temperature of 130 ° C. in the regeneration tower to release carbon dioxide and water.
As for the flow rate of water supplied from the water storage tank to the carbon dioxide absorption unit, the shortage was sent according to the calculation result. As a result, it becomes possible to operate stably with the amount of absorption liquid held in the equipment being 860 to 880 kg and the amine concentration being 297 to 304 g / kg, so that carbon dioxide in exhaust gas can be efficiently absorbed. Became. The results are shown in FIGS. 4 and 5.
【００２３】（比較例１）従来法として、実施例１にお
いて、吸収液を１日に１回サンプリングし、化学分析に
よりアミン濃度を求め、それに基づいて設備の各部分の
液量及び流量を調節弁により調整した。この結果、設備
内の吸収液保有量が８４０〜９２０ｋｇ、アミン濃度が
２８４〜３１１ｇ／ｋｇと変動が著しく大きかった。結
果を図６及び図７に示す。(Comparative Example 1) As a conventional method, in Example 1, the absorption liquid was sampled once a day, the amine concentration was determined by chemical analysis, and the liquid amount and flow rate of each part of the equipment were adjusted based on the amine concentration. Adjusted by valve. As a result, the amount of absorption liquid held in the equipment was 840 to 920 kg, and the amine concentration was 284 to 311 g / kg, which were significantly large fluctuations. The results are shown in FIGS. 6 and 7.
【００２４】[0024]
【発明の効果】本発明によれば、濃度計を用いずに、一
定の期間、アミン回収部の水貯槽から二酸化炭素吸収部
は供給する水の流量を調節することにより、吸収液量及
び濃度を一定に保つ度合いが大幅に改善され、二酸化炭
素の吸収効率、運転操作、エネルギー及びコストが改善
された。According to the present invention, by adjusting the flow rate of water supplied from the water storage tank of the amine recovery unit to the carbon dioxide absorption unit for a certain period of time without using a concentration meter, the absorption liquid amount and concentration can be adjusted. The degree of keeping the temperature constant was greatly improved, and the carbon dioxide absorption efficiency, operation, energy and cost were improved.
【図１】本発明のプロセスフロー図である。FIG. 1 is a process flow diagram of the present invention.
【図２】二酸化炭素吸収部、アミン回収部、再生塔及び
水貯槽との間の流量の関係を示す図である。FIG. 2 is a diagram showing a flow rate relationship among a carbon dioxide absorption section, an amine recovery section, a regeneration tower and a water storage tank.
【図３】各計器、コンピューター、制御器及び調節弁の
関係を示す図である。FIG. 3 is a diagram showing a relationship between each instrument, a computer, a controller, and a control valve.
【図４】本発明による、吸収液の保有量の経時変化を示
す図である。FIG. 4 is a diagram showing a change with time of an amount of an absorbent retained according to the present invention.
【図５】本発明による、吸収液中のアミン濃度の経時変
化を示す図である。FIG. 5 is a diagram showing the time-dependent change of the amine concentration in the absorbing liquid according to the present invention.
【図６】従来の方法による、吸収液の保有量の経時変化
を示す図である。FIG. 6 is a diagram showing a change over time in the amount of the absorption liquid retained by a conventional method.
【図７】従来の方法による、吸収液中のアミン濃度の経
時変化を示す図である。FIG. 7 is a diagram showing a time-dependent change in the amine concentration in an absorbing solution by a conventional method.
１ 脱硫後燃焼排ガス ２ 冷却塔 ３ 吸収塔 ４ 二酸化炭素吸収部 ５ アミン回収部 ６ 水貯槽 ７ サージタンク ８ 熱交換器 ９ 再生塔 １０ コンデンサー １１ 分離器 １２ 演算器 １３ 制御器 １４ 流量計１ １５ 液面計 １６ 流量計２ １７ 流量調節弁 ２１ 吸収液 ２２ アミン回収用水 ２３ 排ガス ２４ 負荷吸収液 ２５ 再生吸収液 ２６ 二酸化炭素 ２７ 凝縮水 ２８ 乾燥二酸化炭素 ２９ アミン含有水 ３０ 水 1 Combustion exhaust gas after desulfurization 2 cooling tower 3 absorption tower 4 Carbon dioxide absorber 5 Amine Recovery Department 6 water storage tank 7 surge tank 8 heat exchanger 9 regeneration tower 10 condenser 11 separator 12 arithmetic unit 13 Controller 14 Flowmeter 1 15 Level gauge 16 Flowmeter 2 17 Flow control valve 21 Absorbing liquid 22 Water for amine recovery 23 Exhaust gas 24 load absorption liquid 25 Regenerated absorbent 26 carbon dioxide 27 Condensed water 28 dry carbon dioxide 29 Amine-containing water 30 water
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平６−154554（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) B01D 53/34 ─────────────────────────────────────────────────── ─── Continuation of the front page (56) Reference JP-A-6-154554 (JP, A) (58) Fields investigated (Int.Cl. 7 , DB name) B01D 53/34
Claims (5)
酸化炭素吸収部と上部にアミン回収部を有する二酸化炭
素吸収塔と、塔頂より二酸化炭素と水分を放出し塔底よ
り再生された吸収液を排出する再生塔と、アミン回収部
から抜き出されたアミン含有水を貯蔵する水貯槽とから
なる脱炭酸設備において、吸収液の液面測定可能部に液
面計を設けて、該液面が一定になるように水貯槽から二
酸化炭素吸収部に供給される水の流量を調節することに
より、脱炭酸設備内の吸収液量を一定に保ち、且つ、二
酸化炭素吸収部に供給する吸収液の濃度を一定に保つこ
とを特徴とする吸収液の制御方法。1. A carbon dioxide absorption tower using an absorption liquid containing amine, having a carbon dioxide absorption section in the lower part and an amine recovery section in the upper part, and carbon dioxide and water released from the top of the tower and regenerated from the bottom of the tower. In a decarbonation equipment consisting of a regeneration tower for discharging the absorbing liquid and a water storage tank for storing the amine-containing water extracted from the amine collecting part, a liquid level gauge is provided in the liquid level measuring part of the absorbing liquid, By adjusting the flow rate of the water supplied from the water storage tank to the carbon dioxide absorption unit so that the liquid level is constant, the amount of absorption liquid in the decarbonation equipment is kept constant and is supplied to the carbon dioxide absorption unit. A method for controlling an absorption liquid, characterized in that the concentration of the absorption liquid is kept constant.
底液滞留部、再生塔の塔底液滞留部、または吸収液再生
塔から二酸化炭素吸収塔へ吸収液を供給するラインに設
けられた吸収液サージタンクである請求項１記載の吸収
液の制御方法。2. The liquid level measurable part is provided in the bottom liquid retention part of the carbon dioxide absorption tower, the bottom liquid retention part of the regeneration tower, or a line for supplying the absorption liquid from the absorption liquid regeneration tower to the carbon dioxide absorption tower. The method for controlling an absorbing solution according to claim 1, wherein the absorbing solution surge tank is provided.
インに流量計を設け、水貯槽から二酸化炭素吸収部に水
を供給するラインに流量計と流量調節弁を設けて流量調
節する請求項１または２記載の吸収液の制御方法。3. A flow meter is provided in a line for supplying an absorption liquid to a carbon dioxide absorption tower, and a flow meter and a flow rate adjusting valve are provided in a line for supplying water from a water storage tank to a carbon dioxide absorption section to adjust the flow rate. The method for controlling the absorbent according to 1 or 2.
部へ吸収液を供給するラインに流量計を設け、水貯槽か
ら二酸化炭素吸収部に水を供給するラインに流量計と流
量調節弁を設けて流量調節する請求項２記載の吸収液の
制御方法。4. A flow meter is provided on a line for supplying the absorption liquid from the absorption liquid surge tank to the carbon dioxide absorption unit, and a flow meter and a flow control valve are provided on a line for supplying water from the water storage tank to the carbon dioxide absorption unit. The method for controlling the absorbing liquid according to claim 2, wherein the flow rate is adjusted.
て、再生された吸収液が二酸化炭素吸収部に供給される
流量と水貯槽から二酸化炭素吸収部に供給される水の流
量が下記式により定められる請求項３または４記載の吸
収液の制御方法。 【数１】 5. The flow rate at which the regenerated absorption liquid is supplied to the carbon dioxide absorption section and the flow rate of water supplied from the water storage tank to the carbon dioxide absorption section are as follows based on the values measured by the flow meter and the liquid level gauge. The method for controlling the absorbing liquid according to claim 3 or 4, which is defined by a formula. [Equation 1]
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02724097A JP3364103B2 (en) | 1997-01-27 | 1997-01-27 | Control method of absorption liquid in decarbonation equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP02724097A JP3364103B2 (en) | 1997-01-27 | 1997-01-27 | Control method of absorption liquid in decarbonation equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH10202054A JPH10202054A (en) | 1998-08-04 |
| JP3364103B2 true JP3364103B2 (en) | 2003-01-08 |
Family
ID=12215563
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP02724097A Expired - Lifetime JP3364103B2 (en) | 1997-01-27 | 1997-01-27 | Control method of absorption liquid in decarbonation equipment |
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| Country | Link |
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| JP (1) | JP3364103B2 (en) |
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| CA2779621C (en) * | 2009-06-17 | 2014-11-25 | Mitsubishi Heavy Industries, Ltd. | Co2 recovering apparatus and method |
| US8309047B2 (en) | 2009-09-15 | 2012-11-13 | Alstom Technology Ltd | Method and system for removal of carbon dioxide from a process gas |
| EP2322265A1 (en) | 2009-11-12 | 2011-05-18 | Alstom Technology Ltd | Flue gas treatment system |
| US20110146489A1 (en) * | 2009-12-17 | 2011-06-23 | Alstom Technology Ltd | Ammonia removal, following removal of co2, from a gas stream |
| US8728209B2 (en) | 2010-09-13 | 2014-05-20 | Alstom Technology Ltd | Method and system for reducing energy requirements of a CO2 capture system |
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| US8529857B2 (en) * | 2011-03-31 | 2013-09-10 | Basf Se | Retention of amines in the removal of acid gases by means of amine absorption media |
| WO2013008914A1 (en) | 2011-07-13 | 2013-01-17 | 株式会社Ihi | Method and device for recovering carbon dioxide |
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| US8986640B1 (en) | 2014-01-07 | 2015-03-24 | Alstom Technology Ltd | System and method for recovering ammonia from a chilled ammonia process |
| JP2016215174A (en) * | 2015-05-26 | 2016-12-22 | 株式会社東芝 | Carbon dioxide recovery system and method of operating carbon dioxide recovery system |
| JP6871720B2 (en) * | 2016-11-14 | 2021-05-12 | 三菱パワー株式会社 | Carbon dioxide absorber |
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-
1997
- 1997-01-27 JP JP02724097A patent/JP3364103B2/en not_active Expired - Lifetime
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| Publication number | Publication date |
|---|---|
| JPH10202054A (en) | 1998-08-04 |
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