JPS6142760B2 - - Google Patents
Info
- Publication number
- JPS6142760B2 JPS6142760B2 JP54070374A JP7037479A JPS6142760B2 JP S6142760 B2 JPS6142760 B2 JP S6142760B2 JP 54070374 A JP54070374 A JP 54070374A JP 7037479 A JP7037479 A JP 7037479A JP S6142760 B2 JPS6142760 B2 JP S6142760B2
- Authority
- JP
- Japan
- Prior art keywords
- coal
- gasification
- gas
- polymer
- section
- 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
Links
- 238000002309 gasification Methods 0.000 claims description 70
- 239000003245 coal Substances 0.000 claims description 55
- 229920000642 polymer Polymers 0.000 claims description 35
- 239000003054 catalyst Substances 0.000 claims description 27
- 238000003763 carbonization Methods 0.000 claims description 24
- 238000000034 method Methods 0.000 claims description 15
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 12
- 239000011591 potassium Substances 0.000 claims description 12
- 229910052700 potassium Inorganic materials 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 239000007789 gas Substances 0.000 description 47
- 239000000428 dust Substances 0.000 description 11
- 239000011269 tar Substances 0.000 description 11
- 239000002956 ash Substances 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 8
- 238000000354 decomposition reaction Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 239000011280 coal tar Substances 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 244000292604 Salvia columbariae Species 0.000 description 3
- 235000012377 Salvia columbariae var. columbariae Nutrition 0.000 description 3
- 235000001498 Salvia hispanica Nutrition 0.000 description 3
- 235000014167 chia Nutrition 0.000 description 3
- 238000007796 conventional method Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000010000 carbonizing Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N Calcium oxide Chemical compound [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000002898 organic sulfur compounds Chemical class 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000011403 purification operation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000004071 soot Substances 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
- Industrial Gases (AREA)
Description
〔産業上の利用分野〕
本発明は、石炭のガス化方法に係り、特に燃料
ガス、還元ガス、化学工業用原料ガスなどを高収
率で得ることを可能にする石炭のガス化方法に関
する。
〔従来の技術〕
従来の石炭ガス化方法は、高温法と低温法に大
別される。高温法は、石炭を1400〜2000℃という
高温で乾留ガス化し、H2やCOに富んだガスを生
成させるものであるが、石炭のガス化を高温で行
なうことから、運転操作に高速の技術を必要と
し、装置材料も耐熱性のある高価なものを使用し
なければならないこと、揮散した灰分がガス化炉
出口及び後続機器に付着し、閉塞等のトラブルを
起すことなどの欠点がある。
これに対し、低温法は、石炭を700〜1000℃と
いう低温で乾留ガス化して燃料用ガスを製造する
方法であつて、高温法と異なり、装置材料に比較
的安価なものを使用できるなどの利点がある。
〔発明が解決しようとする問題点〕
しかしながら、ガス化の際にコールタール等が
石炭の10〜20％程度副生するために石炭のガス化
率が低いこと、生成したコールタール等がガス化
炉以降の配管や装置に付着し、閉塞の危険がある
ことなどの欠点がある。
〔発明の目的〕
本発明の目的は、上記の低温法石炭ガス化方法
の欠点を改良し、石炭のガス化率が高く、運転ト
ラブルのない新規な石炭のガス化方法を提供する
ことにある。
〔発明の概要〕
本発明は、上記の目的を達成するために、石炭
を、石炭乾留ガス化部で700〜1000℃の温度で部
分燃焼させながら水蒸気と接触させて乾留ガス化
し、その際副生し、蒸発したタール等の高分子重
縮合物を含む生成ガスを、上記石炭乾留ガス化部
から分離したのち、その生成ガスをそのまま未反
応水蒸気と共にポリアルミン酸カリウムを主成分
とするハニカム型触媒を充填した高分子重縮合物
ガス化部に導入し、該ガス化部で生成ガス中の高
分子重縮合物を低温で分解ガス化するもので、石
炭を石炭乾留ガス化部で低温（700〜1000℃）で
乾留ガス化し、その生成ガス中の高分子重縮合物
をガス化部で触媒により分解ガス化させること
で、石炭のガス化温度を上げることなく、高分子
重縮合物を分解でき、しかも石炭乾留部ガス化部
で石炭の乾留・水性ガス化反応を行ない、その生
成ガスを石炭から分離してガス化部でポリアルミ
ン酸カリウムを主成分とするハニカム型触媒によ
りガス中の高分子重縮合物を分解することで、石
炭のガス化を連続的にできると共に従来よりガス
化率を10〜20％向上させることができる。
〔実施例〕
以下、本発明の実施例を添付図面に基づいて説
明する。
第１図は、本発明を実施するに好適な、高分子
重縮合物ガス化部を備えた石炭のガス化装置を示
すものである。第１図において、石炭投入部１よ
り石炭乾留ガス化部４に投入された石炭は、水蒸
気導入部２より送られた水蒸気及び燃焼用酸素
（又は酸素含有ガス）導入部３より送られた酸素
（又は空気などの酸素含有ガス）と700〜100℃の
温度条件下に接触し、乾留・部分燃焼及び水性ガ
ス化反応によつてガス化する。上記の如く、石炭
の乾留ガス化に際して生成ガス中には、コールタ
ール等の高分子重縮合物が石炭の10〜20％程度副
生するが、本発明によれば、石炭の乾留ガス化後
の高分子重縮合物含有ガスを未反応水蒸気と共に
高分子重縮合物ガス化部６に導入し、該ガス化部
６に充填された高分子重縮合物を分解する触媒と
接触させる。高分子重縮合物含有ガスが、上記触
媒と接触することにより、コールタールなどの高
分子重縮合物は、石炭の乾留ガス化反応に供され
なかつた未反応水蒸気と下式の如く反応して
H2，CO，CO2などのガスを生成する。
CnHm＋nH2O
→nCO＋（ｍ／２＋ｎ）H2 (1)
CnHm＋2nH2O
→nCO2＋（ｍ／２＋2n）H2 (2)
高分子重縮合物ガス化部６に充填される触媒
は、ポリアルミン酸カリウム（K2O−Al2O3）を用
いる。又、触媒層は、高分子重縮合物含有ガスと
同伴する灰、未反応カーボンなどの粉塵による閉
塞を防止するためにハニカム型触媒による固定床
とする。
石炭乾留ガス化部１で生じる灰や未反応カーボ
ンは、灰排出部５より適宜排出されるので、高分
子重縮合物ガス化部６に送られる灰や未反応カー
ボンの量は、それ程多くないのが通常であるが、
粉塵量が多い場合には、サイクロンなどで除塵後
高分子重縮合物のガス化を行なつても良い。
上式(1)，(2)の如く、高分子重縮合物をH2，
CO，CO2などに分解した後の生成ガスは、生成
ガス排出部７より排出され、後続のプロセスに送
られる。
タール等の高分子重縮合物の分解ガス化触媒と
してのポリアルミン酸カリウムを主成分とする触
媒は、従来用いられている酸化カルシウム
（CaO）より遥かに活性が高く、かつ耐被毒性、
耐高温特性に優れており、石炭中の灰成分、生成
ガス中の硫化水素、有機イオウ化合物などに被毒
されることなく、また1200℃に於いても分解され
ず、かつカリウムの揮散も認められず、活性の低
下がない。このため、タール等の高分子重縮合物
の分解ガス化温度を実用上1000℃以上にする必要
がなく、又500℃においてもガス化でき、実用に
おいても700℃という低温度でガス化が可能であ
る。
またガス化部にタール等の高分子重縮合物を含
む生成ガスをそのまま導入することで略断熱状態
で高分子重縮合物を分解ガス化でき、そのガス化
部出口温度を入口温度より低下させることがで
き、回収した生成ガスの熱回収温度幅を狭め熱回
収装置の容量を大幅に縮小することができる。
通常、石炭のガス化で回収される生成ガスは、
除じん、脱硫、（硫化水素除去）などの精製が必
要となるので、回収したガスの温度を精製操作温
度にまで降下させる必要があり、熱効率上、この
熱を回収することが好ましい。現在のガス精製温
度は、精製方法によつても異なるが、技術的、経
済的に可能性のある最高温度は600℃である。一
方、タール等の高分子重縮合物の分解ガス化反応
は著しい吸熱反応で、生成ガス1Nm3中のタール
等の高分子重縮合物１ｇを分解ガス化させた場合
の吸熱量は、そのガス温度を10℃降下させるのに
見合つた量であるので、石炭ガス化による生成ガ
ス中に含まれる20〜30ｇ／Ｎm3のタール等の高分
子重縮合物を断熱状態で分解ガス化させることに
より、ガス化部での出口温度を、その入口温度よ
り200〜300℃降下させることができ、従つてガス
の精製に、この200〜300℃に相当する熱量を回収
する必要がなくなり、熱回収装置の容量を大幅に
縮小することができる。
すなわち、本発明においては、ポリアルミン酸
カリウムという高性能ガス化触媒を使用すると共
にタール等の高分子重縮合物を含む生成ガスを石
炭乾留ガス化部から分離し、高分子重縮合物のみ
を高分子重縮合物ガス化部において分解ガス化さ
せることで低温度で分解させることができる共に
熱回収を大幅に縮小できることを可能としたもの
である。
また、本発明は、ハニカム型触媒を用いること
により含じん生成ガスを簡単に且つ効果的に分解
ガス化できるものである。
すなわち、石炭ガス化乾留ガスは700〜1000℃
程度の温度を有する灰分などの粉じんを多く含ん
だガスでこのガス中のタール等の高分子重縮合物
を触媒で分解ガス化する場合、触媒層が粉じんで
閉塞する危険性がある。このためには生成ガス中
の粉じんを除じんすればよいが、現状では700〜
1000℃といつた高温度における除じんは技術的、
経済的に難しく、またタール等の高分子重縮合物
は極めて短時間のうちに分解ガス化しないと重縮
合がさらに進行し、カーボン（煤）化してしま
い、これをガス化することは極めて困難になる。
本発明においては、ハニカム型触媒をも用いる
ため、ガス化部でのガス通路面積が大となり、ダ
ストによる閉塞の問題が生ぜず、しかも重縮合物
と触媒との接触面積が小さくても活性の高いポリ
アルミン酸カリウムを用いるため、分解ガス化に
は全く支障のないものとすることができる。
第２図は、本発明を実施するに好適な他の装置
例を示すものであり、この図において、石炭乾留
ガス化部４は、流動床石炭乾留部４ａとその下段
の流動床チヤーガス化部４ｂで構成される。石炭
は、石炭投入部１より流動床石炭乾留部４ａに投
入され、流動床チヤーガス化部４ｂから上昇して
くる高温還元性ガスにより乾留され、生成した高
分子重縮合物含有ガスは、高分子重縮合物ガス化
部６へ送られる。他方、チヤーは、下降管８を経
てチヤーガス化部４ｂに送られ、水蒸気導入部２
及び空気導入部３により導入された水蒸気及び空
気の存在下に部分燃焼及び部分酸化することによ
りガス化し、石炭乾留部４ａ、更には高分子重縮
合物ガス化部６へ送られる。高分子重縮合物含有
ガスは、ポリアルミン酸カリウムのハニカム型触
媒を充填した固定床式反応器である高分子重縮合
物ガス化部６において上記触媒と接触して、高分
子重縮合物は、上式(1)，(2)の如く反応して、
H2，CO，CO2などのガスを生成する。
第１表は、第２図の装置を用いて本発明を実施
した場合のタール生成率、石炭ガス化率及び生成
ガス組成を高分子重縮合物のガス化処理を行なわ
ない従来法と比較したものである。
[Industrial Application Field] The present invention relates to a coal gasification method, and particularly to a coal gasification method that makes it possible to obtain fuel gas, reducing gas, raw material gas for chemical industry, etc. in high yield. [Prior Art] Conventional coal gasification methods are broadly classified into high-temperature methods and low-temperature methods. The high-temperature method involves carbonizing coal at a high temperature of 1,400 to 2,000 degrees Celsius to produce gas rich in H 2 and CO. Because coal is gasified at high temperatures, it requires high-speed technology for operation. There are drawbacks such as the need to use heat-resistant and expensive equipment materials, and the volatilized ash adhering to the gasifier outlet and subsequent equipment, causing problems such as blockages. On the other hand, the low-temperature method is a method of producing fuel gas by carbonizing coal at a low temperature of 700 to 1000°C. There are advantages. [Problems to be solved by the invention] However, the gasification rate of coal is low because about 10 to 20% of coal tar, etc. is produced as a by-product during gasification, and the generated coal tar, etc. is difficult to gasify. There are disadvantages such as the fact that it adheres to piping and equipment after the furnace and poses a risk of blockage. [Object of the Invention] The object of the present invention is to improve the drawbacks of the above-mentioned low-temperature coal gasification method, and to provide a new coal gasification method that has a high coal gasification rate and is free from operational troubles. . [Summary of the Invention] In order to achieve the above object, the present invention carbonizes coal by contacting it with steam while partially burning it at a temperature of 700 to 1000°C in a coal carbonization gasification section, and at the same time carbonizes coal by carbonization. After the generated gas containing raw and evaporated polymer polycondensates such as tar is separated from the coal carbonization gasification section, the generated gas is directly passed along with unreacted steam to a honeycomb type catalyst mainly composed of potassium polyaluminate. The coal is introduced into a polymer polycondensate gasification section filled with coal, and the polymer polycondensate in the produced gas is decomposed and gasified at a low temperature in the gasification section. The polymer polycondensates in the resulting gas are decomposed and gasified by a catalyst in the gasification section, thereby decomposing the polymer polycondensates without raising the coal gasification temperature. In addition, the carbonization and water gasification reactions of coal are carried out in the coal carbonization and gasification sections, and the resulting gas is separated from the coal, and the gasification section uses a honeycomb-type catalyst containing potassium polyaluminate as the main component to reduce the high concentrations in the gas. By decomposing molecular polycondensates, coal can be gasified continuously and the gasification rate can be improved by 10 to 20% compared to conventional methods. [Example] Hereinafter, an example of the present invention will be described based on the accompanying drawings. FIG. 1 shows a coal gasifier equipped with a polymer polycondensate gasifier suitable for carrying out the present invention. In FIG. 1, coal input from coal input section 1 to coal carbonization gasification section 4 contains steam sent from steam introduction section 2 and oxygen sent from combustion oxygen (or oxygen-containing gas) introduction section 3. (or oxygen-containing gas such as air) under a temperature condition of 700 to 100°C, and gasifies through carbonization, partial combustion, and water gasification reaction. As mentioned above, during the carbonization gasification of coal, polymer polycondensates such as coal tar are by-produced in the gas produced by about 10 to 20% of the coal, but according to the present invention, after the carbonization gasification of coal, The polymer polycondensate-containing gas together with unreacted water vapor is introduced into the polymer polycondensate gasification section 6 and brought into contact with a catalyst filled in the gasification section 6 for decomposing the polymer polycondensate. When the polymer polycondensate-containing gas comes into contact with the above catalyst, the polymer polycondensate such as coal tar reacts with unreacted water vapor that was not subjected to the coal carbonization gasification reaction as shown in the following equation.
Generates gases such as H 2 , CO, and CO 2 . CnHm+nH 2 O →nCO+(m/2+n)H 2 (1) CnHm+2nH 2 O →nCO 2 +(m/2+2n)H 2 (2) The catalyst filled in the polymer polycondensate gasification section 6 is polyaluminic acid Potassium (K 2 O−Al 2 O 3 ) is used. Further, the catalyst layer is a fixed bed of a honeycomb type catalyst in order to prevent clogging by dust such as ash and unreacted carbon accompanying the gas containing the polymeric polycondensate. Ash and unreacted carbon generated in the coal carbonization gasification section 1 are appropriately discharged from the ash discharge section 5, so the amount of ash and unreacted carbon sent to the polymer polycondensate gasification section 6 is not so large. Usually,
If the amount of dust is large, the polymer polycondensate may be gasified after dust removal using a cyclone or the like. As shown in the above formulas (1) and (2), the polymer polycondensate is exposed to H 2 ,
The generated gas after being decomposed into CO, CO 2 , etc. is discharged from the generated gas discharge section 7 and sent to the subsequent process. Catalysts whose main component is potassium polyaluminate as a decomposition and gasification catalyst for polymeric polycondensates such as tar are much more active than the conventionally used calcium oxide (CaO), and are highly resistant to poisoning.
It has excellent high-temperature resistance properties, is not poisoned by ash components in coal, hydrogen sulfide in generated gas, organic sulfur compounds, etc., does not decompose even at 1200 degrees Celsius, and is also confirmed to volatilize potassium. There is no decrease in activity. For this reason, the decomposition and gasification temperature of polymeric polycondensates such as tar does not need to be higher than 1000°C in practice, and gasification can be performed even at 500°C, and gasification can be performed at temperatures as low as 700°C in practical use. It is. In addition, by directly introducing the generated gas containing polymeric polycondensates such as tar into the gasification section, the polymeric polycondensates can be decomposed and gasified in an almost adiabatic state, and the temperature at the gasification section outlet is lower than the inlet temperature. This makes it possible to narrow the heat recovery temperature range of the recovered generated gas and significantly reduce the capacity of the heat recovery device. Normally, the produced gas recovered from coal gasification is
Since purification such as dust removal, desulfurization, (removal of hydrogen sulfide), etc. is required, it is necessary to lower the temperature of the recovered gas to the purification operation temperature, and in terms of thermal efficiency, it is preferable to recover this heat. Current gas purification temperatures vary depending on the purification method, but the highest technically and economically possible temperature is 600°C. On the other hand, the decomposition and gasification reaction of polymeric polycondensates such as tar is a remarkable endothermic reaction, and the amount of heat absorbed when 1 g of polymeric polycondensates such as tar is decomposed and gasified in 1 Nm 3 of the generated gas is This amount is sufficient to lower the temperature by 10℃, so by decomposing and gasifying 20 to 30 g/ Nm3 of polymer polycondensates such as tar contained in the gas produced by coal gasification under adiabatic conditions. , the outlet temperature in the gasification section can be lowered by 200 to 300 degrees Celsius from the inlet temperature, and therefore there is no need to recover the amount of heat equivalent to this 200 to 300 degrees Celsius for gas purification, and a heat recovery device is required. capacity can be significantly reduced. That is, in the present invention, a high-performance gasification catalyst called potassium polyaluminate is used, and the produced gas containing polymeric polycondensates such as tar is separated from the coal carbonization gasification section, and only the polymeric polycondensates are polymerized. By decomposing and gasifying the molecular polycondensate in the gasification section, it is possible to decompose at a low temperature and to significantly reduce heat recovery. In addition, the present invention makes it possible to easily and effectively decompose and gasify dust-containing generated gas by using a honeycomb type catalyst. In other words, coal gasification carbonization gas is 700-1000℃
When using a catalyst to decompose and gasify polymeric polycondensates such as tar in a gas containing a large amount of dust such as ash having a temperature of about 100 mL, there is a risk that the catalyst layer may become clogged with dust. For this purpose, it is necessary to remove the dust from the generated gas, but currently the
Dust removal at high temperatures of 1000℃ is technically difficult.
It is economically difficult, and if polymer polycondensates such as tar are not decomposed and gasified within a very short time, the polycondensation will proceed further and turn into carbon (soot), which is extremely difficult to gasify. become. In the present invention, since a honeycomb type catalyst is also used, the gas passage area in the gasification section is large, and the problem of clogging due to dust does not occur, and even if the contact area between the polycondensate and the catalyst is small, the activity can be maintained. Since high potassium polyaluminate is used, decomposition and gasification can be performed without any problem. FIG. 2 shows another example of an apparatus suitable for carrying out the present invention. In this figure, the coal carbonization gasification section 4 includes a fluidized bed coal carbonization section 4a and a fluidized bed carbonization section below it. Consists of 4b. Coal is charged into the fluidized bed coal carbonization section 4a from the coal input section 1, and carbonized by the high temperature reducing gas rising from the fluidized bed coal gasification section 4b, and the generated polymer polycondensate-containing gas is It is sent to the polycondensate gasification section 6. On the other hand, the chia is sent to the chia gasification section 4b via the downcomer pipe 8, and is then sent to the steam introduction section 2.
It is gasified by partial combustion and partial oxidation in the presence of water vapor and air introduced by the air introduction section 3, and is sent to the coal carbonization section 4a and further to the polymer polycondensate gasification section 6. The polymer polycondensate-containing gas is brought into contact with the catalyst in the polymer polycondensate gasification section 6, which is a fixed bed reactor filled with a honeycomb-type catalyst of potassium polyaluminate, and the polymer polycondensate is React as shown in the above formulas (1) and (2),
Generates gases such as H 2 , CO, and CO 2 . Table 1 compares the tar production rate, coal gasification rate, and produced gas composition when the present invention is carried out using the apparatus shown in Figure 2 with a conventional method that does not perform gasification treatment of polymer polycondensates. It is something.
以上要するに本発明によれば次のごとき優れた
効果を発揮する。
(1) 石炭を、石炭乾留ガス化部で乾留ガス化さ
せ、その生成ガスを高分子重縮合物ガス化部に
導入して生成ガス中の高分子重縮合物を、ポリ
アルミン酸カリウムを主成分とするハニカム型
触媒を用いて分解ガス化させることで、従来の
低温法と同様低温（700〜1000℃）で石炭ガス
化が行なえると共にガス化に際して副生するコ
ールタールのごとき高分子重縮合物を分解ガス
化でき、そのガス化率を従来より10〜20％向上
できる。
(2) 石炭乾留ガス化部と高分子重縮合物ガス化部
の２段に分けて反応を行なうことで、石炭灰の
排出操作や触媒操作が容易となりかつ水性ガス
化反応及び触媒による高分子重縮合物の分解反
応を個々に制御できるため、そのガス化率を最
適に行なうことができる。
(3) 高分子重縮合物を分解できるので、配管や装
置を閉塞するような運転トラブルを解消するこ
とができる。
(4) 分解ガス化触媒としてポリアルミン酸カリウ
ムを主成分とした活性の高い触媒を用いるの
で、生成ガス中の高分子重縮合物を低温で分解
ガス化できると共に、その吸熱反応で回収ガス
の温度を低下でき、回収ガスの精製時の熱回収
を大幅に縮小でき熱効率がよい。
(5) ポリアルミン酸カリウムを主成分とするハニ
カム型触媒を用い、その触媒層に高分子重縮合
物を含む生成ガスを通してもダストによる触媒
層の閉塞が生じない。
In summary, the present invention exhibits the following excellent effects. (1) Coal is carbonized into gas in a coal carbonization gasification section, and the resulting gas is introduced into a polymer polycondensate gasification section to convert the polymer polycondensate in the resulting gas into polycondensate containing potassium polyaluminate as its main component. By decomposition and gasification using a honeycomb-type catalyst, coal gasification can be performed at low temperatures (700 to 1000℃) similar to conventional low-temperature methods, and polymer polycondensation such as coal tar, which is a by-product during gasification, can be performed. It can decompose and gasify substances, and the gasification rate can be improved by 10 to 20% compared to conventional methods. (2) By conducting the reaction in two stages: the coal carbonization gasification section and the polymer polycondensate gasification section, the coal ash discharge operation and catalyst operation are facilitated, and the water gasification reaction and polymer polymerization by the catalyst are facilitated. Since the decomposition reaction of the polycondensate can be individually controlled, the gasification rate can be optimized. (3) Since polymer polycondensates can be decomposed, operational problems such as clogging pipes and equipment can be resolved. (4) Since a highly active catalyst containing potassium polyaluminate as the main component is used as the decomposition gasification catalyst, the polymer polycondensate in the generated gas can be decomposed and gasified at low temperatures, and the endothermic reaction can lower the temperature of the recovered gas. The heat recovery during purification of recovered gas can be significantly reduced, resulting in good thermal efficiency. (5) Even if a honeycomb type catalyst containing potassium polyaluminate as a main component is used and a generated gas containing a polymer polycondensate is passed through the catalyst layer, the catalyst layer will not be clogged with dust.
第１図及び第２図は、本発明の方法を実施する
に好適な装置例を示す図である。
図中、１は石炭導入部、２は水蒸気導入部、３
は燃焼用酸素（又は酸素含有ガス）導入部、４は
石炭乾留ガス化部、４ａは石炭乾留部、４ｂはチ
ヤーガス化部、５は灰排出部、６は高分子重縮合
物ガス化部、７は生成ガス排出部、８はチヤー下
降管である。
FIGS. 1 and 2 are diagrams showing examples of apparatus suitable for carrying out the method of the present invention. In the figure, 1 is the coal introduction part, 2 is the steam introduction part, and 3
is a combustion oxygen (or oxygen-containing gas) introduction part, 4 is a coal carbonization gasification part, 4a is a coal carbonization part, 4b is a coal gasification part, 5 is an ash discharge part, 6 is a polymer polycondensate gasification part, 7 is a produced gas discharge section, and 8 is a chia downcomer.
Claims (1)
の温度で部分燃焼させながら水蒸気と接触させて
乾留ガス化し、その際副生し、蒸発したタール等
の高分子重縮合物を含む生成ガスを、上記石炭乾
留ガス化部から分離したのち、その生成ガスを、
そのまま未反応水蒸気と共にポリアルミン酸カリ
ウムを主成分とするハニカム型触媒を充填した高
分子重縮合物ガス化部に導入し、該ガス化部で生
成ガス中の高分子重縮合物を低温で分解ガス化す
ることを特徴とする石炭のガス化方法。1 Coal is heated to 700 to 1000℃ in the coal carbonization gasification section.
Carbonization gasification is carried out by contacting with water vapor while partially burning the coal at a temperature of The generated gas,
The polymer polycondensate gasification section filled with a honeycomb-shaped catalyst mainly composed of potassium polyaluminate is introduced together with unreacted water vapor as it is, and in the gasification section, the polymer polycondensate in the produced gas is decomposed into a gas at a low temperature. A method for gasifying coal, which is characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7037479A JPS55161887A (en) | 1979-06-05 | 1979-06-05 | Gasification of coal |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7037479A JPS55161887A (en) | 1979-06-05 | 1979-06-05 | Gasification of coal |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS55161887A JPS55161887A (en) | 1980-12-16 |
| JPS6142760B2 true JPS6142760B2 (en) | 1986-09-24 |
Family
ID=13429594
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7037479A Granted JPS55161887A (en) | 1979-06-05 | 1979-06-05 | Gasification of coal |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS55161887A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110835554A (en) * | 2019-12-03 | 2020-02-25 | 内蒙古工业大学 | A kind of method of calcium carbide slag catalyzing bituminous coal steam gasification |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59221272A (en) * | 1983-05-21 | 1984-12-12 | 株式会社ハイランド | Container pack |
| KR100395139B1 (en) * | 1999-12-23 | 2003-08-21 | 재단법인 포항산업과학연구원 | Catalyst of coal gasification |
| EP1142981A3 (en) * | 2000-03-23 | 2003-04-02 | Fraunhofer-Gesellschaft Zur Förderung Der Angewandten Forschung E.V. | Apparatus for power generation by gasification of biomass with subsequent catalytic removal of tar compounds from the heating gas |
| US20040244289A1 (en) * | 2001-09-28 | 2004-12-09 | Fumiaki Morozumi | Process for reforming inflammable gas, apparatus for reforming inflammable gas and gasification apparatus |
| JP2006241229A (en) * | 2005-03-01 | 2006-09-14 | Takuma Co Ltd | Gasification system |
| US9364812B2 (en) | 2010-11-17 | 2016-06-14 | Highbury Biofuel Technologies Inc. | Freeboard tar destruction unit |
| JP5646966B2 (en) * | 2010-11-19 | 2014-12-24 | 三菱日立パワーシステムズ株式会社 | Method and apparatus for producing gas mainly containing hydrogen |
| EP2927305A1 (en) * | 2014-04-03 | 2015-10-07 | Ulf Söderlind | A fluidized bed gasifier system with freeboard tar removal |
| JP7225568B2 (en) * | 2018-05-23 | 2023-02-21 | 株式会社Ihi | gasification furnace |
| CN110835555B (en) * | 2019-12-03 | 2021-06-18 | 内蒙古工业大学 | Method for modifying steam gasification performance of lignite with carbide slag |
-
1979
- 1979-06-05 JP JP7037479A patent/JPS55161887A/en active Granted
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110835554A (en) * | 2019-12-03 | 2020-02-25 | 内蒙古工业大学 | A kind of method of calcium carbide slag catalyzing bituminous coal steam gasification |
| CN110835554B (en) * | 2019-12-03 | 2021-06-22 | 内蒙古工业大学 | A kind of method of calcium carbide slag catalyzing bituminous coal steam gasification |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS55161887A (en) | 1980-12-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US3746522A (en) | Gasification of carbonaceous solids | |
| JP2003041268A5 (en) | ||
| WO2008013794A2 (en) | Conversion of carbonaceous materials to synthetic natural gas by pyrolysis, reforming, and methanation | |
| CN1036375A (en) | production of fuel gas | |
| JP2009057497A (en) | Gasification method, gas generator and gasifier | |
| US4155990A (en) | Process for removal and recovery of sulfide from coal gas | |
| JPS6142760B2 (en) | ||
| US2963348A (en) | Hydrocarbon conversion process | |
| US4117100A (en) | Process for reduction of sulfur dioxide to sulfur | |
| US4159201A (en) | Process for producing a carbon monoxide-rich gas | |
| CN101372312A (en) | Method for producing hydrogen from coal gasification | |
| JPS6274993A (en) | Method for producing carbon monoxide and hydrogen-containing gas | |
| JPS5938161B2 (en) | Method for producing synthesis gas for ammonia production | |
| JP3936115B2 (en) | Recycling method of gas, drainage and fine slag in waste gasification | |
| JPH10506951A (en) | Method for removing ammonia from gasification gas | |
| JP7727366B2 (en) | Gasification gas production apparatus and gasification gas production method | |
| JPS63159496A (en) | Method and apparatus for treating raw gas | |
| JP4041880B2 (en) | Method for gasifying organic matter using porous inorganic particles | |
| JP3377546B2 (en) | Gasification method of organic matter | |
| JP4555319B2 (en) | Gasification gas purification method and purification device | |
| JP2007277479A (en) | Method and apparatus for producing hydrogen gas and carbon monoxide gas from combustible waste | |
| JP2008297509A (en) | Tar reforming reactor | |
| JP2008174578A (en) | Coal hydrocracking process | |
| JP4350362B2 (en) | Circulating fluidized bed | |
| KR20200054245A (en) | Method for performing selective catalytic reduction of coke oven flue gas |