JPH0763586B2 - Treatment method of waste air in regeneration of coke oven gas desulfurization liquid - Google Patents
Treatment method of waste air in regeneration of coke oven gas desulfurization liquidInfo
- Publication number
- JPH0763586B2 JPH0763586B2 JP63050833A JP5083388A JPH0763586B2 JP H0763586 B2 JPH0763586 B2 JP H0763586B2 JP 63050833 A JP63050833 A JP 63050833A JP 5083388 A JP5083388 A JP 5083388A JP H0763586 B2 JPH0763586 B2 JP H0763586B2
- Authority
- JP
- Japan
- Prior art keywords
- waste air
- coke oven
- oil
- regeneration
- ammonia
- 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 - Fee Related
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Classifications
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- 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
Landscapes
- Treating Waste Gases (AREA)
- Industrial Gases (AREA)
Description
【発明の詳細な説明】 ＜産業上の利用分野＞ 本発明は、コークス炉ガス（以下、COGと称す）の精製
工程において、硫化水素、シアン化水素、芳香族成分お
よびアンモニア等を含んだまま、このCOG中のアンモニ
アをアルカリ源として硫化水素およびシアン化水素を吸
収除去する脱硫装置で循環使用される脱硫液を、空気酸
化して再生したときに発生する廃空気の処理方法に関す
る。DETAILED DESCRIPTION OF THE INVENTION <Industrial field of application> The present invention relates to a coke oven gas (hereinafter, referred to as COG) refining process while containing hydrogen sulfide, hydrogen cyanide, an aromatic component, ammonia and the like. The present invention relates to a method for treating waste air generated when a desulfurization liquid that is circulated and used in a desulfurization device that absorbs and removes hydrogen sulfide and hydrogen cyanide by using ammonia in COG as an alkali source is regenerated by air oxidation.
＜従来の技術＞ 従来、COG中に含有する硫化水素およびシアン化水素の
除去方法としては、COG中のアンモニアをアルカリ源と
して吸収するフマックス・ロダックス法、タカハックス
法等がよく知られている。これらの方法で硫化水素、シ
アン化水素を吸収した脱硫液には、ロダンアンモン、過
硫酸アンモニウム、硫酸アンモニウム、アンモニア水お
よび水硫化アンモニウムを含んでいる。そしてこの脱硫
液は、循環再使用するために空気と触媒（例えば、フマ
ックス・ロダックス法ではピクリン酸が用いられる）を
用いて脱硫液中の水硫化アンモニウムをアンモニア水と
単体硫黄に置換して再生を行っている（例えば、特公昭
52−3404号公報参照）。<Prior Art> Conventionally, as a method for removing hydrogen sulfide and hydrogen cyanide contained in COG, a Humax-Rodax method and a TAKAHAX method, which absorb ammonia in COG as an alkali source, are well known. The desulfurization liquid which has absorbed hydrogen sulfide and hydrogen cyanide by these methods contains rhodan ammonium, ammonium persulfate, ammonium sulfate, aqueous ammonia and ammonium hydrosulfide. This desulfurization solution is then regenerated by replacing the ammonium hydrosulfide in the desulfurization solution with ammonia water and elemental sulfur by using air and a catalyst (for example, picric acid is used in the Humax-Rhodox method) for circulation reuse. Have been conducted (for example,
52-3404).
第２図は、従来のCOGの精製および脱硫液再生における
廃空気の処理のフロー図である。FIG. 2 is a flow chart of conventional waste gas treatment in COG purification and desulfurization liquid regeneration.
COG1は、脱硫装置２、アンモニア吸収装置３およびガス
軽油捕集装置４を経て精製される。脱硫装置２には脱硫
循環液５が循環し、COG1中の硫化水素およびシアン化水
素を吸収した脱硫液６は、再生装置７でピクリン酸を触
媒とし空気８を吹込んで酸化再生され再使用される。脱
硫液６中の前記過硫酸アンモニウムは、この再生装置７
で再生反応が進み過ぎたときに副反応として生成するも
ので、前記ロダンアンモンとともに任意の濃度になるよ
う適宜脱硫液の一部を脱硫廃液９として系外へ抜出すこ
とにより調整されている。COG1 is refined through a desulfurizer 2, an ammonia absorber 3 and a gas light oil collector 4. The desulfurization circulation liquid 5 circulates in the desulfurization device 2, and the desulfurization liquid 6 which has absorbed hydrogen sulfide and hydrogen cyanide in COG1 is oxidized and regenerated by the regeneration device 7 by blowing air 8 using picric acid as a catalyst and reused. The ammonium persulfate contained in the desulfurization liquid 6 is generated by the regeneration device 7
Is generated as a side reaction when the regeneration reaction proceeds too much, and is adjusted by appropriately extracting a part of the desulfurization liquid as a desulfurization waste liquid 9 to the outside of the system so that the desulfurization liquid has an arbitrary concentration together with the above-mentioned rhodammone.
ところで、COG1中に含有されているベンゼン、トルエ
ン、キシレン等の芳香族成分は、アンモニアを含むほか
のCOG成分とともに気液平衡関係において脱硫液６中に
溶解および同伴し、さらに再生装置７において発生する
廃空気10との気液平衡関係から廃空気10側に放散される
ため、前記軽油捕集装置４に用いる吸収油11を廃空気10
の油洗浄装置12へ循環させて該廃空気10中の芳香族成分
を吸収除去し、引続いて前記アンモニア吸収装置３に用
いた硫酸アンモニウムを含む稀硫酸液13をアンモニア回
収装置14へ循環させ、油洗浄された廃空気15中のアンモ
ニアを硫酸アンモニウムとして回収したのち放散廃空気
16として大気放散している。By the way, aromatic components such as benzene, toluene, xylene, etc. contained in COG1 are dissolved and entrained in the desulfurization liquid 6 in a gas-liquid equilibrium relationship with other COG components containing ammonia, and are further generated in the regenerator 7. Because of the gas-liquid equilibrium relationship with the waste air 10 that is discharged to the waste air 10 side, the absorption oil 11 used for the light oil collecting device 4 is
To remove the aromatic components in the waste air 10 and then to circulate the dilute sulfuric acid solution 13 containing ammonium sulfate used in the ammonia absorption device 3 to the ammonia recovery device 14. Ammonia in oil-washed waste air 15 is recovered as ammonium sulphate and then exhausted.
It is released to the atmosphere as 16.
＜発明が解決しようとする課題＞ しかしながら、上記廃空気の処理方法において、芳香族
成分の油洗浄による回収率はその吸収効率から90重量％
程度が限界であり、環境保全上十分な処理とは言い難
い。<Problems to be Solved by the Invention> However, in the above waste air treatment method, the recovery rate of aromatic components by oil cleaning is 90% by weight from the absorption efficiency.
The degree is limited, and it cannot be said that the treatment is sufficient for environmental protection.
また、上記廃空気中のアンモニアを硫酸アンモニウムと
して回収する方法は、硫酸アンモニウム市況の低迷して
いる場合には、市場価格にくらべて製造原価が数倍にな
ることも珍しくなく、一方COG精製の性格上硫酸アンモ
ニウムの回収量を状況に応じて調節できないため廃空気
処理費増大の要因となっている。Further, in the method of recovering ammonia in waste air as ammonium sulfate, it is not uncommon for the production cost to be several times higher than the market price when the market price of ammonium sulfate is sluggish. Since the recovery amount of ammonium sulfate cannot be adjusted according to the situation, it is a factor of increasing the waste air treatment cost.
本発明は、上記の問題点に着目してなされたもので、コ
ークス炉ガス脱硫液の再生における廃空気を、燃焼処理
することにより環境汚染の少ない成分組成にして放散す
るとともに硫酸アンモニウムの生産調整ができ、さらに
蒸気として熱回収することができる廃空気の処理方法を
提供することを目的としている。The present invention has been made in view of the above problems, and waste air in the regeneration of coke oven gas desulfurization liquid is burned to reduce the composition of components with less environmental pollution and to control the production of ammonium sulfate. It is an object of the present invention to provide a method for treating waste air which can be recovered as heat and can be recovered as steam.
＜課題を解決するための手段＞ 上記目的を達成するために、本発明によれば、コークス
炉で発生するコークス炉ガス中の硫化水素およびシアン
化水素を吸収除去する脱硫装置で循環使用される脱硫液
を、空気酸化して再生したときに発生する廃空気の処理
において、前記廃空気を油洗浄して芳香族成分含有量を
調整したのちアンモニアを除去することなくそのまま燃
焼処理することを特徴とするコークス炉ガス脱硫液の再
生における廃空気の処理方法が提供される。<Means for Solving the Problems> In order to achieve the above object, according to the present invention, a desulfurization liquid circulated and used in a desulfurization device for absorbing and removing hydrogen sulfide and hydrogen cyanide in coke oven gas generated in a coke oven. In the treatment of waste air generated when air is oxidized and regenerated, the waste air is washed with oil to adjust the content of aromatic components and then directly burned without removing ammonia. A method for treating waste air in the regeneration of coke oven gas desulfurization liquid is provided.
以下に、本発明を添付の図面に示す好適実施例を参照し
ながら詳細に説明する。Hereinafter, the present invention will be described in detail with reference to the preferred embodiments shown in the accompanying drawings.
第１図において、COG精製工程は従来例と全く同じであ
るので説明を省略する。なお、17は供給硫酸、18は硫酸
アンモニウム分離乾燥装置、19は含芳香族吸収油、20は
ガス軽油回収装置である。In FIG. 1, the COG refining process is exactly the same as that of the conventional example, and therefore its explanation is omitted. In addition, 17 is a supply sulfuric acid, 18 is an ammonium sulfate separating / drying device, 19 is an aromatic absorbing oil, and 20 is a gas light oil recovery device.
COG1中の硫化水素およびシアン化水素を吸収した脱硫液
６を再生装置７でピクリン酸を触媒として空気８を吹込
んで酸化再生したときに発生する廃空気10の組成は、例
えば芳香族成分が0.45〜0.8Vol％、アンモニアが0.5〜
0.95Vol％、酸素が17〜18Vol％、窒素が76.4Vol％、水
分が55g/Nm3、その他のCOG成分が４〜5Vol％である。The composition of the waste air 10 generated when the desulfurization liquid 6 which has absorbed hydrogen sulfide and hydrogen cyanide in COG 1 is oxidatively regenerated by blowing air 8 with picric acid as a catalyst in the regenerator 7, for example, aromatic components are 0.45 to 0.8. Vol%, ammonia 0.5 ~
0.95Vol%, oxygen 17~18Vol%, nitrogen 76.4Vol%, water 55 g / Nm 3, other COG component is 4~5Vol%.
この廃空気10を、まず油洗浄装置12で吸収油11を用いて
洗浄し、後述する焼却炉22内で助燃料と混合された混合
ガス中の芳香族成分が0.37〜0.6Vol％になるよう吸収除
去する。このようにして燃焼発熱量を調整することによ
り、NOxの生成、増加を防止することができる。The waste air 10 is first washed with the absorption oil 11 in the oil washing device 12 so that the aromatic component in the mixed gas mixed with the auxiliary fuel in the incinerator 22 described later becomes 0.37 to 0.6 Vol%. Absorb and remove. By adjusting the combustion calorific value in this way, it is possible to prevent the generation and increase of NO x .
除去方法としては、例えば充填物としてテラレット（日
鉄化工機製）を用いた充填塔で、充填高さが5m、L/Gが
0.5〜1.0/Nm3、温度が30〜40℃、圧力が300mmAqで実
施すればよい。As a removal method, for example, a packing tower using Terralet (manufactured by Nittetsu Kakoki) as a packing, with a packing height of 5 m and L / G
It may be carried out at a temperature of 0.5 to 1.0 / Nm 3 , a temperature of 30 to 40 ° C., and a pressure of 300 mmAq.
油洗浄された廃空気15は、アンモニアを除去することな
く後述する燃焼廃ガス23と熱交換器21で熱交換されたの
ち、焼却炉22に導びかれ、助燃料として例えばCOG1を加
え約1100℃で燃焼する。焼却炉22は、例えば、１次燃焼
室と２次燃焼室を備えた円筒中空横型炉でよい。ここ
で、焼却炉２への油洗浄された廃空気15の供給方法と燃
焼温度の制御との関係で、得られる燃焼排ガス23中のNO
xの生成率が増減する。すなわち、油洗浄された廃空気1
5中のアンモニアは燃焼条件によっては高濃度なほどNOx
の生成を増加させる要因となるが、脱硝反応用のアンモ
ニア源ともなるので、適切な燃焼条件を選択することに
よりNOxの生成を抑制することができる。例えば、上記
の油洗浄された廃空気15では、助燃用と１次燃焼室に全
体の80％、２次室に20％の割合で分配供給し、全体の燃
焼時間は２〜４秒で終了させることが好ましい。The oil-cleaned waste air 15 is heat-exchanged with a combustion waste gas 23 and a heat exchanger 21, which will be described later, without removing ammonia, and then introduced into an incinerator 22, where, for example, COG1 is added as an auxiliary fuel to about 1100. Burns at ℃. The incinerator 22 may be, for example, a cylindrical hollow horizontal furnace having a primary combustion chamber and a secondary combustion chamber. Here, due to the relationship between the method of supplying the oil-cleaned waste air 15 to the incinerator 2 and the control of the combustion temperature, the NO in the exhaust gas 23 obtained is obtained.
The generation rate of x increases or decreases. That is, oil-washed waste air 1
Ammonia in 5 as a high concentration by combustion conditions NO x
However, since it also serves as an ammonia source for the denitration reaction, NO x production can be suppressed by selecting appropriate combustion conditions. For example, in the above-mentioned oil-cleaned waste air 15, 80% of the total is supplied to the auxiliary combustion and primary combustion chambers and is supplied to the secondary chambers at a ratio of 20%, and the overall combustion time is 2 to 4 seconds. Preferably.
温度の制御方法としては、燃焼排ガス中のNOxの増減状
況を見ながら１次室の温度を助燃料で制御すればよい。As a temperature control method, the temperature of the primary chamber may be controlled by the auxiliary fuel while observing the increase / decrease state of NO x in the combustion exhaust gas.
燃焼排ガス23の顕熱は、例えば廃熱ボイラー24を設けて
蒸気25として回収し、さらに熱交換器21を経たのち大気
放散される。26はボイラー用水である。なお、この燃焼
排ガス23中のNOxが排出基準値を越えるような場合は、
公知の触媒を用いた小容量脱硝装置を設置することで対
処することができる。The sensible heat of the combustion exhaust gas 23 is recovered as steam 25 by providing, for example, a waste heat boiler 24, further passes through the heat exchanger 21, and is then released to the atmosphere. 26 is water for boilers. If the NO x in the combustion exhaust gas 23 exceeds the emission standard value,
This can be dealt with by installing a small capacity denitration device using a known catalyst.
＜実施例＞ 以下に本発明を実施例に基づき、具体的に説明する。<Examples> The present invention will be specifically described below based on Examples.
（実施例１〜３） コークス炉ガス中の硫化水素およびシアン化水素をフマ
ックス・ロダックス法で除去した脱硫液を、ピクリン酸
を触媒として空気酸化する再生装置（脱硫液供給量4500
m3/時、空気量17000Dry Nm3/時、容量20000Nm3/時のも
の）で発生した廃空気の組成は、芳香族成分が0.8Vol
％、アンモニアが0.65Vol％、酸素が17.5Vol％、窒素が
76.4Vol％、水分が55g/Nm3、その他のCOG成分が4.3Vol
％であった。(Examples 1 to 3) A regenerator for air-oxidizing a desulfurization liquid obtained by removing hydrogen sulfide and hydrogen cyanide in a coke oven gas by the Humax-Rhodax method using picric acid as a catalyst (desulfurization liquid supply amount 4500).
m 3 / time, when the air amount 17000Dry Nm 3 /, the composition of the waste air generated in the volume 20000 nm 3 / time ones), aromatic components 0.8Vol
%, Ammonia 0.65Vol%, oxygen 17.5Vol%, nitrogen
76.4Vol%, moisture 55g / Nm 3 , other COG components 4.3Vol
%Met.
この廃空気中の芳香族成分がそれぞれ第１表に示す濃度
になるよう油洗浄装置（容量20000Nm3/時）で吸収油を
用いて、L/Gが0.5/Nm3、温度35℃で洗浄したのち、助
燃料として第１表に示す濃度のCOGを用い、第１表に示
す燃焼温度で燃焼した。このときの油洗浄された廃空気
の供給率は92.5〜98Vol％、COGの供給率は7.5〜2Vol％
で、得られた燃焼排ガスの組成は第１表のとおりで比較
的低NOxのものであった。The aromatics in this waste air are washed with the oil washing device (capacity 20000 Nm 3 / hour) at a L / G of 0.5 / Nm 3 and a temperature of 35 ° C so that the aromatic components in the waste air have the concentrations shown in Table 1. After that, COG having the concentration shown in Table 1 was used as the auxiliary fuel, and combustion was performed at the combustion temperature shown in Table 1. At this time, the supply rate of oil-washed waste air is 92.5 to 98 Vol%, and the supply rate of COG is 7.5 to 2 Vol%.
The composition of the obtained combustion exhaust gas was as shown in Table 1 and had a relatively low NO x .
（比較例１） 上記実施例と同じ組成の廃空気を実施例と同じ油洗浄装
置で同じ吸収油を用いてL/Gが2.5/Nm3、温度35℃で廃
空気中の芳香族成分を吸収除去し、引続いてアンモニア
回収装置（L/Gが６、スプレー式吸収塔、能力20000Nm3/
時）で硫酸アンモニウム48wt％を含む3wt％濃度稀硫酸
を用いてアンモニアを除去し放散廃空気とした。上記油
洗浄された廃空気および放散廃空気の組成を第２表に示
す。(Comparative Example 1) Waste air having the same composition as in the above example was used in the same oil cleaning device as in the example to use the same absorbing oil to remove aromatic components in the waste air at L / G of 2.5 / Nm 3 and temperature of 35 ° C. Absorbed and removed, followed by ammonia recovery device (L / G 6, spray absorption tower, capacity 20000 Nm 3 /
At the same time), ammonia was removed using 3 wt% dilute sulfuric acid containing 48 wt% ammonium sulfate to produce waste air. The compositions of the oil-washed waste air and the exhausted waste air are shown in Table 2.
＜発明の効果＞ 本発明は、以上説明したように構成されているので、ア
ンモニアを除去することなく燃焼することにより比較的
低NOxの燃焼排ガスとすることができるから、硫酸アン
モニウムの生産調整に寄与でき、環境汚染の少ない燃焼
排ガスとして放散できる。さらに、燃焼廃熱を蒸気とし
て熱回収できるから経済的である。 <Effects of the Invention> Since the present invention is configured as described above, it is possible to produce a combustion exhaust gas with a relatively low NO x by combusting without removing ammonia. It can contribute and can be emitted as combustion exhaust gas with little environmental pollution. Furthermore, it is economical because the combustion waste heat can be recovered as steam.
第１図はCOGの精製および本発明方法の一例を示すフロ
ー図である。 第２図はCOGの精製および従来の廃空気の処理のフロー
図である。 符号の説明 １……COG、 ２……脱硫装置、 ３……アンモニア吸収装置、 ４……ガス軽油捕集装置、 ５……脱硫循環液、 ６……脱硫液、 ７……再生装置、 ８……空気、 ９……脱硫廃液、 10……廃空気、 11……吸収油、 12……油洗浄装置、 13……硫酸アンモニウムを含む稀硫酸液、 14……アンモニア回収装置、 15……油洗浄された廃空気、 16……放散廃空気、 17……供給硫酸、 18……硫酸アンモニウム分離乾燥装置、 19……含芳香族吸収油、 20……ガス軽油回収装置、 21……熱交換器、 22……焼却炉、 23……燃焼排ガス、 24……廃熱ボイラー、 25……蒸気、 26……ボイラー用水FIG. 1 is a flow chart showing an example of purification of COG and the method of the present invention. FIG. 2 is a flow chart of COG purification and conventional waste air treatment. Explanation of symbols 1 ... COG, 2 ... desulfurization device, 3 ... ammonia absorption device, 4 ... gas light oil collecting device, 5 ... desulfurization circulation liquid, 6 ... desulfurization liquid, 7 ... regeneration device, 8 …… Air, 9 ・ ・ ・ Desulfurization waste liquid, 10 …… Waste air, 11 …… Absorbing oil, 12 …… Oil cleaning device, 13 …… Dilute sulfuric acid solution containing ammonium sulfate, 14 …… Ammonia recovery device, 15 …… Oil Washed waste air, 16 …… Dissipated waste air, 17 …… Supply sulfuric acid, 18 …… Ammonium sulfate separation drying equipment, 19 …… Aromatic absorption oil, 20 …… Gas gas oil recovery equipment, 21 …… Heat exchanger , 22 …… incinerator, 23 …… combustion exhaust gas, 24 …… waste heat boiler, 25 …… steam, 26 …… boiler water
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０１Ｄ 53/58 Ｃ１０Ｋ 1/08 7106−4Ｈ Ｂ０１Ｄ 53/34 ＺＡＢ ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification code Internal reference number FI Technical display location B01D 53/58 C10K 1/08 7106-4H B01D 53/34 ZAB
Claims (1)
硫化水素およびシアン化水素を吸収除去する脱硫装置で
循環使用される脱硫液を、空気酸化して再生したときに
発生する廃空気の処理において、前記廃空気を油洗浄し
て芳香族成分含有量を調整したのちアンモニアを除去す
ることなくそのまま燃焼処理することを特徴とするコー
クス炉ガス脱硫液の再生における廃空気の処理方法。1. Treatment of waste air generated when a desulfurization liquid which is circulated and used in a desulfurization device for absorbing and removing hydrogen sulfide and hydrogen cyanide in a coke oven gas generated in a coke oven is oxidized and regenerated, A method for treating waste air in the regeneration of a coke oven gas desulfurization liquid, characterized in that the waste air is washed with oil to adjust the content of aromatic components and then directly burned without removing ammonia.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63050833A JPH0763586B2 (en) | 1988-03-04 | 1988-03-04 | Treatment method of waste air in regeneration of coke oven gas desulfurization liquid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63050833A JPH0763586B2 (en) | 1988-03-04 | 1988-03-04 | Treatment method of waste air in regeneration of coke oven gas desulfurization liquid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01224032A JPH01224032A (en) | 1989-09-07 |
| JPH0763586B2 true JPH0763586B2 (en) | 1995-07-12 |
Family
ID=12869756
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63050833A Expired - Fee Related JPH0763586B2 (en) | 1988-03-04 | 1988-03-04 | Treatment method of waste air in regeneration of coke oven gas desulfurization liquid |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0763586B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8898036B2 (en) | 2007-08-06 | 2014-11-25 | Rosemount Inc. | Process variable transmitter with acceleration sensor |
| US9052240B2 (en) | 2012-06-29 | 2015-06-09 | Rosemount Inc. | Industrial process temperature transmitter with sensor stress diagnostics |
| US9207670B2 (en) | 2011-03-21 | 2015-12-08 | Rosemount Inc. | Degrading sensor detection implemented within a transmitter |
| US9602122B2 (en) | 2012-09-28 | 2017-03-21 | Rosemount Inc. | Process variable measurement noise diagnostic |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5754048B2 (en) * | 2011-08-30 | 2015-07-22 | 国立大学法人 鹿児島大学 | Coke oven gas desulfurization method |
-
1988
- 1988-03-04 JP JP63050833A patent/JPH0763586B2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8898036B2 (en) | 2007-08-06 | 2014-11-25 | Rosemount Inc. | Process variable transmitter with acceleration sensor |
| US9207670B2 (en) | 2011-03-21 | 2015-12-08 | Rosemount Inc. | Degrading sensor detection implemented within a transmitter |
| US9052240B2 (en) | 2012-06-29 | 2015-06-09 | Rosemount Inc. | Industrial process temperature transmitter with sensor stress diagnostics |
| US9602122B2 (en) | 2012-09-28 | 2017-03-21 | Rosemount Inc. | Process variable measurement noise diagnostic |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH01224032A (en) | 1989-09-07 |
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