JPH03243691A - Coliquefaction of coal with bituminous material using acid-type iron oxide catalyst - Google Patents
Coliquefaction of coal with bituminous material using acid-type iron oxide catalystInfo
- Publication number
- JPH03243691A JPH03243691A JP4058090A JP4058090A JPH03243691A JP H03243691 A JPH03243691 A JP H03243691A JP 4058090 A JP4058090 A JP 4058090A JP 4058090 A JP4058090 A JP 4058090A JP H03243691 A JPH03243691 A JP H03243691A
- Authority
- JP
- Japan
- Prior art keywords
- coal
- iron oxide
- pref
- oxide catalyst
- type iron
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000003054 catalyst Substances 0.000 title claims abstract description 30
- 239000003245 coal Substances 0.000 title claims abstract description 25
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 239000000463 material Substances 0.000 title claims abstract description 14
- 238000000034 method Methods 0.000 claims abstract description 19
- 239000002253 acid Substances 0.000 claims description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 16
- 239000001257 hydrogen Substances 0.000 abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 11
- 238000009835 boiling Methods 0.000 abstract description 6
- 150000001875 compounds Chemical class 0.000 abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000002244 precipitate Substances 0.000 abstract description 3
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 abstract description 2
- 239000004202 carbamide Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 abstract description 2
- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 abstract description 2
- 229910000360 iron(III) sulfate Inorganic materials 0.000 abstract description 2
- 238000005336 cracking Methods 0.000 abstract 1
- 239000000203 mixture Substances 0.000 abstract 1
- 239000002994 raw material Substances 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 16
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 239000010426 asphalt Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 4
- 239000007795 chemical reaction product Substances 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 238000005979 thermal decomposition reaction Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- MBMLMWLHJBBADN-UHFFFAOYSA-N Ferrous sulfide Chemical compound [Fe]=S MBMLMWLHJBBADN-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 241000269821 Scombridae Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- CCKOTZKIYZRJBN-UHFFFAOYSA-N [O-2].O.S.[Fe+2] Chemical compound [O-2].O.S.[Fe+2] CCKOTZKIYZRJBN-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Natural products N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 125000003118 aryl group Chemical group 0.000 description 1
- NFMAZVUSKIJEIH-UHFFFAOYSA-N bis(sulfanylidene)iron Chemical compound S=[Fe]=S NFMAZVUSKIJEIH-UHFFFAOYSA-N 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 239000008367 deionised water Substances 0.000 description 1
- 229910021641 deionized water Inorganic materials 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910000339 iron disulfide Inorganic materials 0.000 description 1
- VXWSFRMTBJZULV-UHFFFAOYSA-H iron(3+) sulfate hydrate Chemical compound O.[Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O VXWSFRMTBJZULV-UHFFFAOYSA-H 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 235000020640 mackerel Nutrition 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- -1 naphtha Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000003415 peat Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000004525 petroleum distillation Methods 0.000 description 1
- 239000011295 pitch Substances 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000003476 subbituminous coal Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000011275 tar sand Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 229910000859 α-Fe Inorganic materials 0.000 description 1
Abstract
Description
【発明の詳細な説明】
（技術分野）
本発明は、酸型酸化鉄触媒を用いる石炭と歴青物質との
共液化方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION (Technical Field) The present invention relates to a method for co-liquefaction of coal and bituminous material using an acidic iron oxide catalyst.
（従来技術及びその問題点）
石炭の液化は、石炭の複雑な構造を熱分解させてガソリ
ンやナフサ、加えて、ジーゼル油やジェット燃料といっ
た液体燃料を効率よく製造することを主な目的として行
われるものである。石炭の主たる化学構造は芳香族類で
あるため熱分解によってラジカルを生成し易い。反応系
内で熱分解ラジカルをそのまま放置すれば一旦生成した
熱分解ラジカルはラジカル間で再結合して安定化し、原
料石炭より大きな分子量を持つ化合物を生成する、いわ
ゆる、コーキング現象を引き起こすため目的には沿わな
くなる。このコーキング現象を避けて目的を達成するた
めには熱分解ラジカルに水素を添加してラジカルの安定
化を行うことが不可欠である。(Prior art and its problems) The main purpose of coal liquefaction is to thermally decompose the complex structure of coal to efficiently produce liquid fuels such as gasoline, naphtha, diesel oil, and jet fuel. It is something that can be done. Since the main chemical structure of coal is aromatic, it easily generates radicals through thermal decomposition. If the thermal decomposition radicals are left as they are in the reaction system, the thermal decomposition radicals once generated will recombine between the radicals and become stable, producing a compound with a molecular weight larger than that of raw coal, causing the so-called coking phenomenon. will not follow. In order to avoid this coking phenomenon and achieve the objective, it is essential to stabilize the radicals by adding hydrogen to the thermally decomposed radicals.
ラジカルの水素添加には２つの方法がある。その１つは
高圧水素ガス共存下で石炭の熱分解を行ってラジカルを
水素ガスによって水素添加する方法で、他の１つはあら
かじめ水素化処理して水素を富化させた溶媒を用い、こ
の溶媒の水素によってラジカルの水素添加を行う方法で
ある。There are two methods for radical hydrogenation. One method is to thermally decompose coal in the coexistence of high-pressure hydrogen gas and hydrogenate the radicals with hydrogen gas. This is a method of hydrogenating radicals using hydrogen in a solvent.
実際の石炭液化法は高圧水素ガスと水素富化溶媒とが共
存している系で行なわれている。このため、反応後、水
素を放出してしまった溶媒を回収して再び水素化処理を
行ってその水素共与性を高めるための溶媒循環プロセス
が必要になる。The actual coal liquefaction method is carried out in a system where high-pressure hydrogen gas and hydrogen-enriched solvent coexist. Therefore, after the reaction, a solvent circulation process is required to recover the solvent that has released hydrogen and perform the hydrogenation treatment again to improve its hydrogen codonating property.
一方、石炭を歴青物質と共に共液化する方法が知られて
いる。この共液化の目的は石炭液化で行っている溶媒循
環プロセスを省略してプロセスを筒素化することにある
。すなわち、歴青物質は、それ白身、水素／炭素（Ｈ／
Ｃ）原子比が高く、既に、十分に水素富化された化合物
であるため、歴青物質を水素供与性溶媒として用いるな
らば改めてその水素化前処理を必要としないからである
。On the other hand, a method is known in which coal is co-liquefied with bituminous materials. The purpose of this co-liquefaction is to omit the solvent circulation process used in coal liquefaction and streamline the process. That is, the bituminous substance is white, hydrogen/carbon (H/
C) This is because the compound has a high atomic ratio and is already sufficiently hydrogen-enriched, so if a bituminous substance is used as a hydrogen-donating solvent, no further hydrogenation pretreatment is required.
このようなプロセスが有効に機能するにはそのプロセス
に適した触媒の共存が不可欠である。これまで用いられ
てきた触媒といえば、酸化鉄−硫黄系、赤泥−硫黄系並
びに天然硫化鉄や合成硫化鉄系等の硫化物系触媒がその
主なものである。For such a process to function effectively, the coexistence of a catalyst suitable for the process is essential. The main catalysts that have been used so far are iron oxide-sulfur, red mud-sulfur, and sulfide catalysts such as natural iron sulfide and synthetic iron sulfide.
しかしながら、このような硫化物系触媒では未だ満足す
べき結果は得られていない。However, satisfactory results have not yet been obtained with such sulfide catalysts.
（発明の課題）
本発明は、石炭と歴青物質を共液化する方法において、
高活性の触媒を用いることにより、その共液化反応を効
率よく行う方法を提供することをその課題とする。(Problem to be solved by the invention) The present invention provides a method for co-liquefying coal and bituminous material, which includes:
The object of the present invention is to provide a method for efficiently carrying out the co-liquefaction reaction by using a highly active catalyst.
（課題を解決するための手段）
本発明者らは、前記課題を解決すへく鋭意研究を重ねた
結果、酸型酸化鉄触媒を用いることによりその課題を解
決し得ることを見出し、本発明を完成するに至った。(Means for Solving the Problems) As a result of extensive research into solving the above problems, the present inventors discovered that the problems could be solved by using an acid type iron oxide catalyst, and the present invention I was able to complete it.
すなわち、本発明によれば、酸型酸化鉄触媒を用いるこ
とを特徴とする石炭と歴青物質の共成化方法が提供され
る。That is, according to the present invention, there is provided a method for co-synthesizing coal and bituminous material, which is characterized by using an acid type iron oxide catalyst.
本発明で用いる歴青物質としては、石油系及び石炭系の
アスファルトやピッチ、石油の蒸留残渣、負
タールサントビチューメン、真岩油等が挙げられる。歴
青物質は、水素／炭素原子比（）ｌ／Ｃ原子比）の高い
ものが好ましく、一般には、Ｈ／Ｃ原子比が１．５以上
のものが有利に用いられる。石炭としては、従来一般に
用いられている泥炭や、褐炭、亜歴青炭、歴青炭が用い
られる。石炭と歴青物質の使用割合は、石炭１００重量
部に対し、歴青物質１００〜２，０００重量部、好まし
くは１５０〜１，０００重量部の割合である。Examples of the bituminous substance used in the present invention include petroleum-based and coal-based asphalt and pitch, petroleum distillation residue, negative tar sand bitumen, and true rock oil. The bituminous material preferably has a high hydrogen/carbon atomic ratio (l/C atomic ratio), and in general, those with an H/C atomic ratio of 1.5 or more are advantageously used. As the coal, peat, lignite, subbituminous coal, and bituminous coal, which are commonly used in the past, are used. The ratio of coal and bituminous material used is 100 to 2,000 parts by weight, preferably 150 to 1,000 parts by weight, per 100 parts by weight of coal.
本発明で用いる酸型酸化鉄触媒は硫酸第２鉄に鯖を混合
し、これを水に溶解させた後、加熱し、得られた沈殿を
濾過し、水洗し、乾燥及び焼成することによって製造す
るもので、アンモニア水やか性アルカリを用いる従来法
とは異る方法で得ることができる。焼成温度は、３５０
〜７５０℃、好ましくは４００〜５００℃である。The acid type iron oxide catalyst used in the present invention is produced by mixing mackerel with ferric sulfate, dissolving this in water, heating, filtering the resulting precipitate, washing with water, drying and calcining. It can be obtained by a method different from the conventional method using aqueous ammonia or caustic alkali. The firing temperature is 350
-750°C, preferably 400-500°C.
本発明の触媒を用いる石炭及び歴青物質の共液化は、従
来公知の方法に従って実施することができる。この場合
、水素圧力は１０〜３０ＭＰａ、好ましくは１５−３５
−３Ｏであり、反応温度は３５０−５２７℃、好ましく
は４００〜４５０℃である。反応時間は、３０〜９０分
間、好ましくは４０〜６０分間である。Co-liquefaction of coal and bituminous material using the catalyst of the present invention can be carried out according to conventionally known methods. In this case, the hydrogen pressure is 10-30 MPa, preferably 15-35
-3O, and the reaction temperature is 350-527°C, preferably 400-450°C. The reaction time is 30 to 90 minutes, preferably 40 to 60 minutes.
（実施例） 次に本発明を実施例によりさらに詳細に説明する。(Example) Next, the present invention will be explained in more detail with reference to Examples.
実施例１
１００ｇの硫酸第２鉄含水塩と２５０ｇの尿素とを混合
しこれを脱イオン水に溶解して全量を２リツトルにする
。この水溶液を温浴中で９０℃以上に加熱する。望まし
くは、９３−９５℃で２時間以上加熱すると褐色の沈で
んが沈降してくる。これをろ過、水洗し、得られたケー
キを一旦１２０℃で数時間乾燥した後、電気炉で５００
℃、３時間加熱すると約５０５０−７Ｏ／ｇの表面積を
有する赤褐色の酸型酸化鉄触媒が得られる。走査型電子
顕微鏡で観察するとこの触媒は直径約２−３ミクロンの
比較的均一なビーズ型粒子から成っていることが特徴的
である。Example 1 100 g of ferric sulfate hydrate and 250 g of urea are mixed and dissolved in deionized water to a total volume of 2 liters. This aqueous solution is heated to 90° C. or higher in a hot bath. Preferably, when heated at 93-95°C for 2 hours or more, a brown precipitate will settle out. This was filtered, washed with water, and the resulting cake was dried at 120°C for several hours, then heated to 500°C in an electric furnace.
C. for 3 hours, a reddish brown acid type iron oxide catalyst having a surface area of about 5050-7 O/g is obtained. When viewed under a scanning electron microscope, the catalyst is characterized by relatively uniform bead-shaped particles about 2-3 microns in diameter.
次に、前記で得た酸型触媒を用いて以下のように石炭−
ビチューメンの共液化反応を行った。Next, using the acid type catalyst obtained above, coal-
A co-liquefaction reaction of bitumen was carried out.
実験装置として電気炉加熱方式の５００ｍ１振どう式オ
ートクレーブを用い、これに所定量の石炭、ビチューメ
ン、触媒及び水素ガスを充填して一定の昇温速度で反応
温度まで昇温した後、一定時間反応温度に保持して十分
に反応を進行させる。反応終了後、ただちに電気炉の加
熱を停止して放冷する。この場合に用いた反応条件を以
下にまとめた。ただし、触媒（ａ）及び触媒（ｂ）は公
知触媒で、本発明による酸型酸化鉄触媒（ｃ）との比較
のための触媒として用いた。A 500 m1 shaking autoclave with an electric furnace heating method was used as the experimental equipment. After filling the autoclave with a predetermined amount of coal, bitumen, catalyst, and hydrogen gas and raising the temperature at a constant rate to the reaction temperature, the reaction was carried out for a certain period of time. The temperature is maintained to allow the reaction to proceed sufficiently. Immediately after the reaction is completed, the heating of the electric furnace is stopped and the reactor is allowed to cool. The reaction conditions used in this case are summarized below. However, the catalysts (a) and (b) are known catalysts, and were used as catalysts for comparison with the acid type iron oxide catalyst (c) according to the present invention.
反応条件：
石炭：バトルリバー炭（１０ｇ）
歴青物質：コールドレイク産
タールサントビチューメンの
減圧ボトム油（１５ｇ）、沸点域、５２４℃以上
触媒（ａ）：赤泥（２，５ｇ）及び硫黄（０’、２５ｇ
）触媒（ｂ）二二硫化鉄（１，４９ｇ）
触媒（Ｃ） ： ！Ｉｔ型酸型鉄化鉄触媒、７５ｇ）水
素初圧： １００Ｋｇ／ｃｍ
反応圧：最大２２０Ｋｇ／ｃｍ２
昇温速度＝３℃／ｍｉｎ
反応温度＝４５０℃
反応時間＝６０分間
次に、反応生成物の分析方法について以下に示す。Reaction conditions: Coal: Battle River coal (10g) Bituminous material: vacuum bottom oil of cold lake tar sant bitumen (15g), boiling point range, 524°C or higher Catalyst (a): Red mud (2.5g) and sulfur ( 0', 25g
) Catalyst (b) Iron disulfide (1,49g) Catalyst (C): ! It-type acid type iron ferrite catalyst, 75 g) Hydrogen initial pressure: 100 Kg/cm Reaction pressure: Maximum 220 Kg/cm2 Temperature increase rate = 3°C/min Reaction temperature = 450°C Reaction time = 60 minutes Next, the reaction product The analysis method is shown below.
反応生成物を室温でトルエン抽出してトルエン可溶分（
ＴＳ）と不溶分（ＴＩ）とに分別する。The reaction product was extracted with toluene at room temperature to obtain the toluene soluble content (
It is separated into TS) and insoluble matter (TI).
（ＴＩ）分を電気炉で焼成して灰分量を求め、灰分基準
の反応率の計算に資した。(TI) was calcined in an electric furnace to determine the ash content, which contributed to the calculation of the reaction rate based on the ash content.
（ＴＳ）分は室温で正ヘキサン抽出して正ヘキサン可溶
分（ＴＳ−Ｈ５）と不溶分（ＴＳ−ＨＩ）とに分別する
。The (TS) fraction is extracted with regular hexane at room temperature and separated into a regular hexane soluble fraction (TS-H5) and an insoluble fraction (TS-HI).
（ＴＳ−Ｈ５）分は蒸留ガスクロマトグラフィーによっ
て５留分（沸点２００℃以下、２００℃−３２５℃、３
２５℃〜４００℃、４００℃〜５３８℃及び５３８℃以
上）に分割して反応結果を評価した。(TS-H5) was analyzed by distillation gas chromatography into 5 fractions (boiling point below 200℃, 200℃-325℃, 3
The reaction results were evaluated by dividing into 25°C to 400°C, 400°C to 538°C, and 538°C or higher.
前記のように反応を行って得られた反応生成物の分析結
果を使用した触媒との関連で表−１に示す。Table 1 shows the analysis results of the reaction products obtained by carrying out the reaction as described above in relation to the catalysts used.
また、表−２に（ＴＳ−Ｈ５）分の蒸留分割の結果を示
す。Further, Table 2 shows the results of distillation and division for (TS-H5).
表−１
表−２
〔発明の効果〕
以上の実施例に示した実験結果かられかるように、本発
明による酸型酸化鉄触媒を用いることにより、従来の触
媒では達成することが出来なかった石炭及び歴青物質中
のプレアスファルテンのような高沸点化合物を分解して
（ＴＳ−Ｈ５）分に示されるような低沸点化合物を効率
よく得ることが出来る。加えて、分解によるガス量の生
成も少ないため消費した高価な水素ガスの有効利用率も
高めることが出来る。Table-1 Table-2 [Effects of the invention] As can be seen from the experimental results shown in the examples above, by using the acid type iron oxide catalyst of the present invention, the effects that could not be achieved with conventional catalysts were achieved. High boiling point compounds such as pre-asphaltenes in coal and bituminous materials can be decomposed to efficiently obtain low boiling point compounds as shown in (TS-H5). In addition, since the amount of gas produced by decomposition is small, the effective utilization rate of the consumed expensive hydrogen gas can also be increased.
Claims (1)
歴青物質との共液化方法。(1) A method for co-liquefying coal and bituminous material, characterized by using an acid type iron oxide catalyst.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4058090A JPH03243691A (en) | 1990-02-20 | 1990-02-20 | Coliquefaction of coal with bituminous material using acid-type iron oxide catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4058090A JPH03243691A (en) | 1990-02-20 | 1990-02-20 | Coliquefaction of coal with bituminous material using acid-type iron oxide catalyst |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH03243691A true JPH03243691A (en) | 1991-10-30 |
Family
ID=12584430
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4058090A Pending JPH03243691A (en) | 1990-02-20 | 1990-02-20 | Coliquefaction of coal with bituminous material using acid-type iron oxide catalyst |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH03243691A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242871A (en) * | 2013-05-28 | 2013-08-14 | 中国石油大学(华东) | Heavy oil and biomass hydrogenation coliquefaction treatment process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5545703A (en) * | 1978-09-26 | 1980-03-31 | Nippon Steel Chem Co Ltd | Liquefaction of coal |
| JPS58167682A (en) * | 1982-03-29 | 1983-10-03 | Asahi Chem Ind Co Ltd | Thermal cracking of carbonaceous substance |
| JPS60170693A (en) * | 1984-02-14 | 1985-09-04 | Mitsui Sekitan Ekika Kk | Connected process of coal liquefaction process and coke preparation process |
| JPS60203694A (en) * | 1984-03-29 | 1985-10-15 | Agency Of Ind Science & Technol | Liquefaction of coal |
| JPS6487686A (en) * | 1987-09-29 | 1989-03-31 | Agency Ind Science Techn | Coal liquefaction with complex catalyst |
-
1990
- 1990-02-20 JP JP4058090A patent/JPH03243691A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5545703A (en) * | 1978-09-26 | 1980-03-31 | Nippon Steel Chem Co Ltd | Liquefaction of coal |
| JPS58167682A (en) * | 1982-03-29 | 1983-10-03 | Asahi Chem Ind Co Ltd | Thermal cracking of carbonaceous substance |
| JPS60170693A (en) * | 1984-02-14 | 1985-09-04 | Mitsui Sekitan Ekika Kk | Connected process of coal liquefaction process and coke preparation process |
| JPS60203694A (en) * | 1984-03-29 | 1985-10-15 | Agency Of Ind Science & Technol | Liquefaction of coal |
| JPS6487686A (en) * | 1987-09-29 | 1989-03-31 | Agency Ind Science Techn | Coal liquefaction with complex catalyst |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103242871A (en) * | 2013-05-28 | 2013-08-14 | 中国石油大学(华东) | Heavy oil and biomass hydrogenation coliquefaction treatment process |
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