JPH0816229B2 - Device for decomposing tar and ammonia in gas - Google Patents
Device for decomposing tar and ammonia in gasInfo
- Publication number
- JPH0816229B2 JPH0816229B2 JP63260539A JP26053988A JPH0816229B2 JP H0816229 B2 JPH0816229 B2 JP H0816229B2 JP 63260539 A JP63260539 A JP 63260539A JP 26053988 A JP26053988 A JP 26053988A JP H0816229 B2 JPH0816229 B2 JP H0816229B2
- Authority
- JP
- Japan
- Prior art keywords
- gas
- tar
- ammonia
- chamber
- metal catalyst
- 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
Links
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims description 46
- 229910021529 ammonia Inorganic materials 0.000 title claims description 23
- 229910052751 metal Inorganic materials 0.000 claims description 22
- 239000002184 metal Substances 0.000 claims description 22
- 239000003054 catalyst Substances 0.000 claims description 21
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 20
- 239000007800 oxidant agent Substances 0.000 claims description 11
- 229910052759 nickel Inorganic materials 0.000 claims description 10
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 claims description 9
- 229910052804 chromium Inorganic materials 0.000 claims description 9
- 239000011651 chromium Substances 0.000 claims description 9
- 239000011810 insulating material Substances 0.000 claims description 8
- 230000001590 oxidative effect Effects 0.000 claims description 8
- 230000005855 radiation Effects 0.000 claims description 7
- 239000007789 gas Substances 0.000 description 61
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 18
- 239000003245 coal Substances 0.000 description 16
- 238000002309 gasification Methods 0.000 description 16
- 229910052742 iron Inorganic materials 0.000 description 9
- 239000000919 ceramic Substances 0.000 description 8
- 239000000428 dust Substances 0.000 description 8
- 239000003034 coal gas Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 150000003568 thioethers Chemical class 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Working-Up Tar And Pitch (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、石炭ガス化ガス等のガス中に含まれるター
ルおよびアンモニアを分解してガスを精製する装置に関
する。TECHNICAL FIELD The present invention relates to an apparatus for decomposing tar and ammonia contained in a gas such as coal gasification gas to purify the gas.
石炭ガス化ガス中に含まれるタールの石炭ガスからの
分離は、従来次のようにして行なわれていた。即ち、タ
ールの沸点以上の温度にある石炭ガス化ガスを大量の油
または水と接触させ急激に冷却して、タールを油または
水中に溶解および固形物として懸濁させて除去してい
た。また、石炭ガス化ガス中に含まれるアンモニアは、
大量の水と石炭ガス化ガスを接触させてアンモニアを水
中に溶解させることにより除去していた。Separation of tar contained in coal gasification gas from coal gas has been conventionally performed as follows. That is, the coal gasification gas having a temperature not lower than the boiling point of tar is brought into contact with a large amount of oil or water and rapidly cooled, and the tar is dissolved in oil or water and suspended as a solid matter to be removed. Ammonia contained in coal gasification gas is
A large amount of water was brought into contact with coal gasification gas to dissolve ammonia in water to remove it.
石炭ガス化ガス等のガス中のタールは、石炭ガス化ガ
スの温度を低下させていくと、ガス中に気体として存在
するタールが液体から固体に変化する。ガスの熱回収を
熱交換器で行なわせようとすると、熱交換器の伝熱面に
タールが析出し、付着してスケールとなる。伝熱面に付
着したスケールにより熱交換器の熱貫流率の低下や、通
気ガスの抵抗増加のため、短時間でガスの熱回収が不可
能となるという問題点があつた。Tar in gas such as coal gasification gas changes from liquid to solid tar existing as gas in gas as the temperature of coal gasification gas is lowered. When the heat recovery of the gas is attempted to be performed by the heat exchanger, tar is deposited on the heat transfer surface of the heat exchanger and adheres to form a scale. Due to the scale attached to the heat transfer surface, the heat transmission coefficient of the heat exchanger is reduced and the resistance of the ventilation gas is increased, which makes it impossible to recover the heat of the gas in a short time.
また、石炭ガスをそのまま燃料として使用する場合に
は、石炭ガス化ガス中のアンモニアは燃焼時に発生する
NOxの生成原因物質となるという問題点があつた。更に
また、石炭ガスを炭化水素の合成用原料として使用する
場合は、石炭ガス化ガス中のアンモニアは不純物となる
という問題点があつた。Also, when using coal gas as a fuel as it is, ammonia in coal gasification gas is generated during combustion.
There is a problem that it becomes a substance that causes the generation of NOx. Furthermore, when using coal gas as a raw material for hydrocarbon synthesis, there is a problem that ammonia in coal gasification gas becomes an impurity.
本発明は、上記に鑑み、石炭ガス化ガス等のガス中の
タールとアンモニアを効果的に分解させる装置を提供し
ようとするものである。In view of the above, the present invention aims to provide an apparatus for effectively decomposing tar and ammonia in gas such as coal gasification gas.
本発明のガス中のタール及びアンモニアの分解装置
は、耐火断熱材によつて取囲まれた室にガス供給口、ガ
ス排出口、及び酸化剤供給口がそれぞれ開孔し、上記開
孔部と上記室との間には棒状の輻射変換体を設け、かつ
上記室内にニツケル及びクロムの少くとも１種を含んだ
金属触媒を配置した。The apparatus for decomposing tar and ammonia in gas according to the present invention has a gas supply port, a gas discharge port, and an oxidant supply port, each of which is opened in a chamber surrounded by a refractory heat insulating material. A rod-shaped radiation converter was provided between the chamber and the metal catalyst containing at least one of nickel and chromium.
本発明では、ガスはガス供給口から複数の棒状の輻射
変換体の間を通つて室内へ導入されて、同室内に供給さ
れた酸化剤によつてガス中の可燃物が燃焼し、複数の棒
状の輻射変換体の間を通つて排出口から室外に排出され
る。同室とその開孔部との間には、棒状の輻射変換体が
設けられているために、同輻射変換体は熱を室内に閉じ
込め室内を高温に、例えば800℃〜1,300℃に保持する。
この高温の雰囲気中では、ガス中のタールおよびアンモ
ニアはニツケルとクロムの少なくとも１種以上を含む金
属触媒の作用により次のように分解する。In the present invention, the gas is introduced from the gas supply port into the chamber through the plurality of rod-shaped radiation conversion bodies, the combustible substance in the gas is burned by the oxidant supplied to the chamber, and It passes through between the rod-shaped radiation conversion bodies and is discharged to the outside from the discharge port. Since a rod-shaped radiant converter is provided between the chamber and its opening, the radiant converter traps heat in the chamber and keeps the chamber at a high temperature, for example, 800 ° C to 1,300 ° C.
In this high-temperature atmosphere, tar and ammonia in the gas are decomposed as follows by the action of the metal catalyst containing at least one of nickel and chromium.
タールをCmHnの構造をもつとすると、タールとガス中
に含まれるH2Oが金属触媒表面上で反応し、次の反応でC
OとH2に分解される。If tar has a structure of CmHn, tar and H 2 O contained in the gas react on the surface of the metal catalyst, and C
Decomposed into O and H 2 .
CmHn＋mH2O→mCO＋（ｍ＋n/2）H2 また、タールと上記のように発生した水素とが反応し
て、次のようにタール中の不飽和結合に金属触媒表面上
で水素添加反応が起り、タールがH2Oと反応しやすくな
る。CmHn + mH 2 O → mCO + (m + n / 2) H 2 In addition, the tar reacts with the hydrogen generated as described above, and an unsaturated bond in the tar causes a hydrogenation reaction on the metal catalyst surface as follows. , Tar easily reacts with H 2 O.
CmHn＋aH2→CmHn＋2a 一方、アンモニアは金属触媒表面上で次の反応により
水素と窒素に分解される。CmHn + aH 2 → CmHn + 2a On the other hand, ammonia is decomposed into hydrogen and nitrogen by the following reaction on the surface of the metal catalyst.
2NH3→N2＋3H2 このように、本発明では、室の開孔部に設けた複数の
棒状の輻射変換体によつて室内を高温に保ち、同室内で
ニツケルとクロムの少くとも１種を含んだ金属触媒によ
つて、ガス中のタール及びアンモニアが分解された上、
室外に排出される。2NH 3 → N 2 + 3H 2 As described above, according to the present invention, a plurality of rod-shaped radiation converters provided in the opening of the chamber keeps the room at a high temperature, and at least one kind of nickel and chromium is used in the room. With the metal catalyst containing, the tar and ammonia in the gas are decomposed,
It is discharged outdoors.
本発明の一実施例を第１図及び第２図によつて説明す
る。11はガス供給口、13はガス排出口であつて、その間
に室Ａが形成される。室Ａは、Ｖ字形となす上下の鉄板
3,3と同鉄板3,3の両側に設けられた水平の鉄板4,4に取
付けられた耐火断熱材５によつて取囲まれて形成され、
供給口11の下流側に酸化剤供給口12及び室ＡのＶ字形の
部分の最下位にダスト排出口14が開孔している。また、
上記ガス供給口11、ガス排出口13、酸化剤供給口12及び
ダスト排出口14と室Ａとの間には、例えば第２図に示す
ように開孔を横切つて延びる多数の輻射変換体としての
セラミツク棒1a、1c、1b、1dの群がそれぞれ設けられ、
これらは耐火断熱材を貫いて鉄板３、４に取付けられて
いる。また、室Ａ内のＶ字形の部分には、ニツケルとク
ロムの少くとも１種を含む多数の棒状の金属触媒２が設
けられ、同触媒２は耐火断熱材５を貫いて上方の鉄板４
に取付けられている。An embodiment of the present invention will be described with reference to FIGS. 1 and 2. 11 is a gas supply port, 13 is a gas discharge port, and the chamber A is formed between them. Chamber A is a V-shaped upper and lower iron plate
3,3 and the same iron plate 3,3 are formed by being surrounded by the fireproof heat insulating material 5 attached to the horizontal iron plates 4,4 provided on both sides,
An oxidant supply port 12 is provided on the downstream side of the supply port 11 and a dust discharge port 14 is opened at the bottom of the V-shaped portion of the chamber A. Also,
Between the gas supply port 11, the gas discharge port 13, the oxidant supply port 12 and the dust discharge port 14 and the chamber A, for example, as shown in FIG. The ceramic rods 1a, 1c, 1b, 1d are each provided as a group,
These are attached to the iron plates 3 and 4 through the fireproof heat insulating material. Further, in the V-shaped portion in the chamber A, a large number of rod-shaped metal catalysts 2 containing at least one kind of nickel and chromium are provided, and the catalysts 2 penetrate the refractory heat insulating material 5 and the upper iron plate 4 is provided.
Mounted on
本実施例においては、タール、アンモニア及び水蒸気
を含んだ石炭ガス化ガス101は、ガス供給口11からセラ
ミツク棒群1a間を通過して、耐火断熱材５に囲われた室
Ａ内に導入される。また、空気、空気に酸素を富化した
ガス、または純酸素のいずれかである酸化剤102が、酸
化剤供給口12からセラミツク棒群1b間を通過して室Ａ内
に導入させる。室Ａ内において、石炭ガス化ガス101中
の可燃ガスが酸化剤102中の酸素と反応して燃焼し、混
合ガス105の温度が上昇し、800℃〜1,300℃の範囲とな
る。混合ガス105の温度は、ガス中のH2S、タールおよび
NH3濃度により決まるが、その温度は酸化剤102の供給量
により調整される。混合ガス105は、ニツケルまたはク
ロムを少なくとも１種以上含む金属触媒２が設置された
室Ａ内の部分Ｂにおいて同金属触媒２と接触し、タール
はガス中のH2Oと反応してCO、H2に、アンモニアはN2とH
2に分解される。タールとアンモニアが分解したガスは
セラミツク棒群1c間を通過して、ガス排出口13より精製
ガス103として系外へ排出される。石炭ガス化ガス101中
にダストが含まれている場合は、室Ａ内において重力分
級作用により混合ガス105と分離される。金属表面がガ
ス中のH2SやH2と反応して腐食して表面から剥離したも
の、および石炭ガス化ガス101中のダストのうち重力分
級されたものは、セラミツク棒群1d間を通過してダスト
104としてダスト排出口14から排出される。In this embodiment, the coal gasification gas 101 containing tar, ammonia and steam passes from the gas supply port 11 between the ceramic rod groups 1a and is introduced into the chamber A surrounded by the refractory heat insulating material 5. It In addition, the oxidant 102, which is either air, a gas enriched with oxygen in air, or pure oxygen, is introduced into the chamber A from the oxidant supply port 12 through the ceramic rod group 1b. In the chamber A, the combustible gas in the coal gasification gas 101 reacts with the oxygen in the oxidizer 102 and burns, and the temperature of the mixed gas 105 rises to 800 ° C to 1300 ° C. The temperature of the mixed gas 105 is H 2 S, tar and
The temperature is determined by the NH 3 concentration, but the temperature is adjusted by the supply amount of the oxidant 102. The mixed gas 105 comes into contact with the metal catalyst 2 in the portion B in the chamber A in which the metal catalyst 2 containing at least one kind of nickel or chromium is installed, and tar reacts with H 2 O in the gas to generate CO, to H 2, ammonia N 2 and H
It is decomposed into 2 . The gas obtained by decomposing tar and ammonia passes between the ceramic rod groups 1c and is discharged to the outside of the system as a purified gas 103 from the gas discharge port 13. When the coal gasification gas 101 contains dust, it is separated from the mixed gas 105 in the chamber A by the gravitational classification effect. The metal surface reacts with H 2 S or H 2 in the gas to corrode and peel off from the surface, and the dust in the coal gasification gas 101 that has been classified by gravity passes between the ceramic rod groups 1d. Then dust
It is discharged from the dust discharge port 14 as 104.
また、本実施例では、室Ａの開孔部が輻射変換体とし
ての多数のセラミツク棒1a、1b、1c、1dの群によつて構
成されているために、室Ａ内で発生した熱が閉じ込めら
れ、これによつて同室Ａ内を高温に保ち、タール及びア
ンモニアは金属触媒２によつて確実に分解される。Further, in the present embodiment, since the opening portion of the chamber A is constituted by the group of a large number of ceramic rods 1a, 1b, 1c, 1d as the radiation conversion body, the heat generated in the chamber A is generated. It is confined, thereby keeping the inside of the room A at a high temperature, and tar and ammonia are surely decomposed by the metal catalyst 2.
なお、セラミツク棒1a、1b、1c、1dと金属触媒２は、
本実施例では鉄板に取り付けられているが、鉄板３、耐
火断熱材５と共に、金属触媒２を鉄板４よりとり外すこ
とが可能な構造とすれば、保守点検等に便利である。The ceramic rods 1a, 1b, 1c, 1d and the metal catalyst 2 are
Although it is attached to the iron plate in the present embodiment, if the metal catalyst 2 can be removed from the iron plate 4 together with the iron plate 3 and the fireproof heat insulating material 5, it is convenient for maintenance and inspection.
また、石炭ガス中のH2Sは、金属上のニツケルとクロ
ムを硫化し、タールおよびアンモニアの分解能力を低下
させるので、石炭ガス中のH2Sは低い方が望ましい。H2S
によるタールおよびアンモニアの分解能力の低下を防止
するためには、混合ガス105の温度を高くすることが効
果がある。Further, since H 2 S in coal gas sulfides nickel and chromium on the metal and reduces the decomposition ability of tar and ammonia, lower H 2 S in coal gas is desirable. H 2 S
In order to prevent the deterioration of the decomposition ability of tar and ammonia due to, it is effective to raise the temperature of the mixed gas 105.
本発明の他の実施例を第３図に示す。本実施例は、金
属触媒と混合ガス105の接触面積を広くするために、金
属触媒２を板状とし、これに突起をつけることにより強
度を確保して板状に設置したものである。第３図におい
て、混合ガス105は、矢印に示すように、紙面前方から
混合ガス105が供給され紙面後方へ送り出される。Another embodiment of the present invention is shown in FIG. In this embodiment, in order to widen the contact area between the metal catalyst and the mixed gas 105, the metal catalyst 2 is formed in a plate shape, and projections are formed on the metal catalyst 2 to secure the strength and to be installed in the plate shape. In FIG. 3, as shown by the arrow, the mixed gas 105 is supplied from the front side of the paper surface and sent out to the rear side of the paper surface.
上記両実施例においては、金属触媒２と混合ガス105
の接触を良好にすることにより、タール濃度を数mg/Nm3
以下に、アンモニアを10ppm以下まで低減することが可
能となつた。In both of the above examples, the metal catalyst 2 and the mixed gas 105
By making good contact with the tar concentration of several mg / Nm 3
Below, it was possible to reduce ammonia to below 10 ppm.
また、ガス中のタールを分解してその濃度を著しく下
げることによつて、石炭ガス化ガスの熱回収を100℃〜1
50℃の低温域まで容易に行いうるようになつた。Also, by recovering the coal gasification gas heat by decomposing tar in the gas and reducing its concentration significantly,
It has become possible to easily carry out a low temperature range of 50 ° C.
以上説明したように、本発明は、開孔部に設けられた
複数の棒状輻射変換体によつて室内の温度は高温に維持
され、この室内で、ガス中のタール分とアンモニア分を
ニツケル及びクロムの少くとも１種を含んだ触媒によつ
て効果的に分解し、ガス中のタール及びアンモニア濃度
を著しく低減させることができる。As described above, according to the present invention, the temperature in the room is maintained at a high temperature by the plurality of rod-shaped radiation converters provided in the opening, and the tar content and the ammonia content in the gas are kept in the room in the nickel and nickel. It can be effectively decomposed by a catalyst containing at least one kind of chromium, and the tar and ammonia concentrations in the gas can be remarkably reduced.
第１図は、本発明の一実施例としてのタールおよびアン
モニア分解装置の縦断面図、第２図は第１図のＩ−Ｉ断
面図、第３図は本発明の他の実施例としてのタールおよ
びアンモニア分解装置の金属触媒説明図である。 1a、1b、1c、1d……セラミツク棒、 ２……ニツケルおよびクロムを少なくとも１種以上含む
金属触媒、３、４……鉄板、 ５……耐火断熱材、11……ガス供給口、 12……酸化剤供給口、13……ガス排出口、 14……ダスト排出口、 101……石炭ガス化ガス、102……酸化剤、 103……精製ガス、 104……ダストおよび金属片、 105……混合ガス。FIG. 1 is a vertical sectional view of a tar and ammonia decomposing apparatus as one embodiment of the present invention, FIG. 2 is a sectional view taken along the line II of FIG. 1, and FIG. 3 is another embodiment of the present invention. It is a metal catalyst explanatory drawing of a tar and ammonia decomposition apparatus. 1a, 1b, 1c, 1d ... Ceramic rod, 2 ... Metal catalyst containing at least one kind of nickel and chromium, 3 ... 4 Iron plate, 5 ... Fireproof heat insulating material, 11 ... Gas supply port, 12 ... … Oxidizing agent supply port, 13 …… Gas outlet, 14 …… Dust outlet, 101 …… Coal gasification gas, 102 …… Oxidizing agent, 103 …… Refining gas, 104 …… Dust and metal fragments, 105… … Mixed gas.
───────────────────────────────────────────────────── フロントページの続き (72)発明者 坂井 正康 長崎県長崎市飽の浦町１番１号 三菱重工 業株式会社長崎研究所内 (72)発明者 石原 崇夫 東京都千代田区丸の内２丁目５番１号 三 菱重工業株式会社内 ─────────────────────────────────────────────────── ─── Continuation of front page (72) Masayasu Sakai 1-1 1-1 Atsunoura-machi, Nagasaki-shi, Nagasaki Mitsubishi Heavy Industries, Ltd. Nagasaki Research Institute (72) Inventor Takao Ishihara 2-5-1 Marunouchi, Chiyoda-ku, Tokyo Sanryo Heavy Industries Co., Ltd.
Claims (1)
給口、ガス排出口、及び酸化剤供給口がそれぞれ開孔
し、上記開孔部と上記室との間には複数の棒状の輻射変
換体を設け、かつ上記室内にニツケル及びクロムの少く
とも１種を含んだ金属触媒を配置したことを特徴とする
ガス中のタール及びアンモニアの分解装置。1. A gas supply port, a gas discharge port, and an oxidant supply port are opened in a chamber surrounded by a refractory heat insulating material, and a plurality of holes are provided between the opening and the chamber. A device for decomposing tar and ammonia in a gas, wherein a rod-shaped radiation converter is provided, and a metal catalyst containing at least one of nickel and chromium is arranged in the chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63260539A JPH0816229B2 (en) | 1988-10-18 | 1988-10-18 | Device for decomposing tar and ammonia in gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63260539A JPH0816229B2 (en) | 1988-10-18 | 1988-10-18 | Device for decomposing tar and ammonia in gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02107694A JPH02107694A (en) | 1990-04-19 |
| JPH0816229B2 true JPH0816229B2 (en) | 1996-02-21 |
Family
ID=17349369
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63260539A Expired - Fee Related JPH0816229B2 (en) | 1988-10-18 | 1988-10-18 | Device for decomposing tar and ammonia in gas |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0816229B2 (en) |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5610561B2 (en) * | 2008-05-19 | 2014-10-22 | 株式会社タクマ | Tar decomposition method and tar decomposition apparatus |
| JP5047056B2 (en) * | 2008-05-19 | 2012-10-10 | 株式会社タクマ | Method for falling tar decomposition system and tar decomposition system |
| JP2012506483A (en) * | 2008-10-22 | 2012-03-15 | サザン リサーチ インスティチュート | Process for purifying synthesis gas |
| US9028571B2 (en) * | 2011-04-06 | 2015-05-12 | Ineos Bio Sa | Syngas cooler system and method of operation |
| JP5974363B2 (en) * | 2012-06-15 | 2016-08-23 | 株式会社Ihi | Gasification gas generator and tar reformer |
| FI126357B (en) | 2014-11-14 | 2016-10-31 | Teknologian Tutkimuskeskus Vtt Oy | Process and apparatus for gasification of raw material and gaseous product |
-
1988
- 1988-10-18 JP JP63260539A patent/JPH0816229B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH02107694A (en) | 1990-04-19 |
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