JPH0144755B2 - - Google Patents
Info
- Publication number
- JPH0144755B2 JPH0144755B2 JP55083228A JP8322880A JPH0144755B2 JP H0144755 B2 JPH0144755 B2 JP H0144755B2 JP 55083228 A JP55083228 A JP 55083228A JP 8322880 A JP8322880 A JP 8322880A JP H0144755 B2 JPH0144755 B2 JP H0144755B2
- Authority
- JP
- Japan
- Prior art keywords
- coal
- solvent
- slurry
- decomposition
- product
- 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
- 239000003245 coal Substances 0.000 claims description 112
- 239000002904 solvent Substances 0.000 claims description 83
- 239000002002 slurry Substances 0.000 claims description 66
- 238000000605 extraction Methods 0.000 claims description 23
- 239000000047 product Substances 0.000 claims description 23
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 239000004094 surface-active agent Substances 0.000 claims description 14
- 239000007795 chemical reaction product Substances 0.000 claims description 13
- 238000004519 manufacturing process Methods 0.000 claims description 11
- 238000000354 decomposition reaction Methods 0.000 claims description 10
- 239000002245 particle Substances 0.000 claims description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 238000005984 hydrogenation reaction Methods 0.000 claims description 6
- 239000003921 oil Substances 0.000 description 15
- 238000004821 distillation Methods 0.000 description 10
- 238000000034 method Methods 0.000 description 10
- 238000005292 vacuum distillation Methods 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- 239000000295 fuel oil Substances 0.000 description 6
- 238000002156 mixing Methods 0.000 description 5
- 238000001035 drying Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000011521 glass Substances 0.000 description 4
- 239000003077 lignite Substances 0.000 description 4
- 238000010298 pulverizing process Methods 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 238000000638 solvent extraction Methods 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- 239000002802 bituminous coal Substances 0.000 description 2
- GVGUFUZHNYFZLC-UHFFFAOYSA-N dodecyl benzenesulfonate;sodium Chemical compound [Na].CCCCCCCCCCCCOS(=O)(=O)C1=CC=CC=C1 GVGUFUZHNYFZLC-UHFFFAOYSA-N 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229940080264 sodium dodecylbenzenesulfonate Drugs 0.000 description 2
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 239000003945 anionic surfactant Substances 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000002563 ionic surfactant Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 125000000896 monocarboxylic acid group Chemical group 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 150000003014 phosphoric acid esters Chemical class 0.000 description 1
- 230000002250 progressing effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003476 subbituminous coal Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000003809 water extraction Methods 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Description
〔産業上の利用分野〕
本発明は、石炭液化における石炭・溶剤スラリ
の製造方法、詳しくは瀝青炭、亜瀝青炭、褐炭な
どの水分を含む石炭を乾燥、粉砕することなく加
熱された溶剤とともに湿式ミルに供給して、適正
温度および適正粘度を有する石炭・溶剤スラリと
し、ついでこの石炭・溶剤スラリを水素添加のも
とで予熱して分解抽出反応により生成物を留出せ
しめ、この生成物を前記溶剤の少なくとも一部と
して循環使用するようにした熱経済性に優れ、か
つ工程の簡易化を図ることができる石炭液化にお
ける石炭・溶剤スラリの製造方法に関するもので
ある。
〔従来の技術〕
近年、石炭を有効利用するために、石炭の液化
の技術開発が進められている。石炭を液化する場
合、一般的にはその前処理として石炭・溶剤スラ
リを製造しなければならない。従来は水分を含む
石炭を予め乾燥、粉砕した後、溶剤を加えて攪拌
混合して石炭・溶剤スラリを製造している。
〔発明が解決しようとする課題〕
しかし、この種の従来法においては、石炭の乾
燥は、高温ガスを使用するので酸化されやすく、
かつ乾燥、粉砕した石炭の貯蔵に際して温度上昇
のおそれがあり、また乾燥、粉砕した石炭と溶剤
とを攪拌混合する際には、石炭粒度が微細である
ために、溶剤上に浮上したりして、溶剤中に均一
に分散させることが難しく、さらに攪拌混合して
所定の石炭・溶剤スラリを製造する操作が回分操
作となり、連続操作では困難であり、かつ攪拌混
合に際して乾燥、粉砕した石炭を供給するときに
発じんするなどの不都合があつた。
本発明は上記の諸点に鑑みなされたもので、熱
経済性に優れ、かつ工程に簡易化を図ることがで
きる石炭液化における石炭・溶剤スラリの製造方
法を提供することを目的とするものである。
〔課題を解決するための手段および作用〕
上記の目的を達成するために、本願の第１の発
明の方法は、水分を含む石炭と溶剤とを使用して
石炭を液化するにあたり、水分を含む石炭と加熱
した溶剤とを湿式ミルに供給し石炭の粉砕、石炭
と溶剤との混合および石炭の脱水を行つて所定の
温度を有する石炭・溶剤スラリとし、ついでこの
石炭・溶剤スラリを水素添加のもとで予熱して分
解抽出反応を行わしめ、分解抽出反応生成物を前
記溶剤の少なくとも一部として循環使用すること
を特徴としている。
また、本願の第２の発明の方法は、水分を含む
石炭と溶剤とを使用して石炭を液化するにあた
り、水分を含む石炭、加熱した溶剤および界面活
性剤を湿式ミルに供給し石炭の粉砕、石炭と溶剤
との混合、石炭の脱水および石炭粒子の分散を行
つて所定の温度を有しかつ粒子の沈降し難い石
炭・溶剤スラリとし、ついでこの石炭・溶剤スラ
リを水素添加のもとで予熱して分解抽出反応を行
わしめ、分解抽出反応生成物を前記溶剤の少なく
とも一部として循環使用することを特徴としてい
る。
上記の第１および第２の発明の方法において、
循環使用する分解反応生成物として、分解抽出反
応により生成したスラリ状生成物を蒸留して得た
留出油を用いるのが望ましい。また、循環使用す
る分解反応生成物として、分解抽出反応により生
成したスラリ状生成物およびこのスラリ状生成物
を蒸留して得た留出油を用いることが望ましい。
以下、本発明の構成を図面に基づいて説明す
る。第１図は本発明の方法を実施する装置の一例
を示している。粗破砕された瀝青炭、亜瀝青炭、
褐炭などの水分を含む石炭は乾燥、粉砕されるこ
となく、そのまま石炭搬送装置１によりボールミ
ルなどの湿式ミル２に供給されるとともに、加熱
された溶剤が溶剤循環ライン３から湿式ミル２に
供給され、湿式ミル２内で石炭の粉砕、石炭と溶
剤との混合および石炭の脱水が行われて所定の温
度を有する石炭・溶剤スラリが製造される。この
場合、石炭の粉砕粒度が200メツシユ通過率約50
〜95％、石炭・溶剤スラリの水分が約０〜10重量
％、石炭・溶剤スラリの温度が約100〜250℃とな
るような運転条件を適宜選択する。ついでこの石
炭・溶剤スラリはポンプ４にて予熱器５に送ら
れ、水素供給管６から添加される水素とともに予
熱され、さらに反応塔７に送られて分解抽出反応
が行われる。分解抽出反応により生成したスラリ
状生成物は、気液分離器８に送られてガスが分離
された後、常圧蒸留塔１０に導入されて塔頂の軽
質油留出管１１から軽質油が抜き出され、塔底油
は蒸圧塔底油留出管１２にて減圧蒸留塔１３に送
られる。減圧蒸留塔１３では塔頂の燃料油留出管
１４から燃料油が抜き出され、塔底の減圧塔底油
留出管１５から重質油が抜き出され、通常はガス
化装置に送られる。減圧蒸留塔１３から留出する
燃料油の一部または全部は、前述の溶剤循環ライ
ン３により石炭の溶剤として湿式ミル２に循環さ
れる。循環する溶剤として減圧蒸留塔１３から留
出する燃料油を使用する代りに、減圧蒸留塔１３
の塔底油、常圧蒸留塔１０の塔底油などスラリ状
生成物を蒸留して得た留出油であれば、これを使
用することができる。なお１６はガス精製装置、
１７は精製ガス抜出管、１８は水分離槽、２０は
水抜出管、２１は排ガス排出塔である。
つぎに本発明の他の例について説明する。上記
の例はスラリ状生成物を蒸留して得た留出油を、
溶剤の一部または全部として循環使用するもので
あるが、本例はこのスラリ状生成物を蒸留して得
た留出油を、溶剤循環ライン３で溶剤として湿式
ミル２に循環使用するとともに、分解抽出反応に
より生成したスラリ状生成物を、スラリ状生成物
循環ライン２２により、溶剤として湿式ミル２に
循環使用するものである。なお循環量は、留出油
とスラリ状生成物との合計が、原料石炭の必要溶
剤量の一部または全部となるように適宜調節す
る。
さらに本発明の他の例について説明する。本例
は石炭粒子を溶剤中に均一に分散せしめて石炭粒
子の沈降を防止することを目的とするもので、石
炭、加熱した溶剤および界面活性剤を湿式ミル２
に供給し石炭の粉砕、石炭と溶剤との混合、石炭
の脱水および石炭粒子の分散を行つて、所定の温
度を有し、かつ粒子の沈降し難い石炭・溶剤スラ
リとし、ついでこの石炭・溶剤スラリを、水素添
加のもとで予熱して分解抽出反応を行わしめ、分
解抽出反応生成物を前記溶剤の少なくとも一部と
して循環使用するものである。循環使用する分解
抽出反応生成物として、スラリ状生成物を蒸留し
て得た留出油のみを用いる場合、この留出油とス
ラリ状生成物とを用いる場合があることは、前述
の例の場合と同様である。
本例において用いる界面活性剤としては、イオ
ン性の界面活性剤がよいが、とくに分子中に−
SO3H基もしくは−OSO3H基を有するものまた
はその塩、リン酸エステルまたはその塩、−
COOH基を有するものまたはその塩などのアニ
オン性界面活性剤、あるいはこれらの配合物が好
適である。また界面活性剤の添加量は、石炭・溶
剤スラリの0.01〜５重量％程度とするのが好まし
い。界面活性剤は直接湿式ミル２に投入してもよ
く、または溶剤循環ライン３、スラリ状生成物循
環ライン２２または原料石炭中に予め添加するよ
うにしてもよい。
界面活性剤の効果について、シリンダに高さ
180mmまでスラリを入れ、５mm径、20ｇのガラス
棒の落下沈降時間を計測した。第２図に、界面活
性剤を添加したスラリと、界面活性剤を添加しな
いスラリとの比較を行つた。本例の場合、界面活
性剤として、アニオン系のドデシルベンゼンスル
フオン酸ナトリウムを、スラリ中の褐炭重量に対
し0.5重量％を添加したものである。
本図より、界面活性剤を添加しないスラリは、
シリンダ底部に近づくにつれ、ガラス棒の落下に
長時間を要し、底部に高濃度の褐炭が沈降しつつ
あることがわかる。一方、界面活性剤を添加した
スラリは、底部までほぼ等速にガラス棒が落下
し、スラリ中の褐炭粒子の沈降防止に、添加剤が
有効に作用していることがわかる。
なお第１図は、一例として減圧蒸留を行う場合
の水素化溶剤抽出装置を示しているが、本発明は
他の水素化溶剤抽出装置、たとえば減圧蒸留を行
わない水素化溶剤抽出装置などに適用できること
は勿論である。
〔実施例〕
以下、本発明の実施例について述べる。
実施例 １
第１図に示す装置を用いて実験を行つた。原料
石炭として第１表に示す組成のケンタツキー州産
の瀝青炭を使用した。
[Industrial Field of Application] The present invention relates to a method for producing a coal/solvent slurry in coal liquefaction, and more specifically, a method for producing a coal/solvent slurry in coal liquefaction, in particular, a method for producing a coal/solvent slurry in coal liquefaction. to obtain a coal/solvent slurry having an appropriate temperature and appropriate viscosity, and then preheat this coal/solvent slurry under hydrogenation to distill out the product by decomposition extraction reaction. The present invention relates to a method for producing a coal/solvent slurry in coal liquefaction, which has excellent thermoeconomic efficiency and can simplify the process by recycling at least a part of the solvent. [Prior Art] In recent years, in order to effectively utilize coal, technological development of coal liquefaction has been progressing. When coal is liquefied, it is generally necessary to produce a coal/solvent slurry as a pretreatment. Conventionally, after drying and pulverizing coal containing moisture, a solvent is added and mixed with stirring to produce a coal/solvent slurry. [Problem to be solved by the invention] However, in this type of conventional method, coal is easily oxidized because high-temperature gas is used to dry it.
Furthermore, there is a risk of temperature rise when storing dried and pulverized coal, and when stirring and mixing dried and pulverized coal with a solvent, the coal particles are fine and may float on top of the solvent. It is difficult to disperse the coal uniformly in the solvent, and the operation of stirring and mixing to produce the specified coal/solvent slurry is a batch operation, which is difficult to do continuously. There were some inconveniences such as the generation of dust when cleaning. The present invention has been made in view of the above points, and aims to provide a method for producing coal/solvent slurry in coal liquefaction that has excellent thermoeconomic efficiency and can simplify the process. . [Means and effects for solving the problem] In order to achieve the above object, the method of the first invention of the present application is to liquefy coal using coal containing water and a solvent. Coal and heated solvent are supplied to a wet mill, where the coal is pulverized, the coal and solvent are mixed, and the coal is dehydrated to form a coal/solvent slurry having a predetermined temperature.Then, this coal/solvent slurry is subjected to hydrogenation. The method is characterized in that the decomposition-extraction reaction is carried out by preheating the solvent, and the decomposition-extraction reaction product is recycled as at least a part of the solvent. Further, in the method of the second invention of the present application, when coal is liquefied using coal containing moisture and a solvent, the coal containing moisture, a heated solvent, and a surfactant are supplied to a wet mill, and the coal is pulverized. , by mixing coal and a solvent, dehydrating the coal, and dispersing coal particles to form a coal/solvent slurry that has a predetermined temperature and in which particles do not easily settle, and then this coal/solvent slurry is subjected to hydrogenation. It is characterized in that the decomposition-extraction reaction is carried out by preheating, and the decomposition-extraction reaction product is recycled as at least a part of the solvent. In the methods of the first and second inventions above,
As the decomposition reaction product to be recycled, it is desirable to use distillate oil obtained by distilling a slurry product produced by the decomposition-extraction reaction. Further, as the decomposition reaction products to be recycled, it is desirable to use a slurry-like product produced by the decomposition-extraction reaction and a distillate obtained by distilling this slurry-like product. Hereinafter, the configuration of the present invention will be explained based on the drawings. FIG. 1 shows an example of an apparatus for carrying out the method of the invention. Coarsely crushed bituminous coal, subbituminous coal,
Coal containing moisture such as lignite is supplied as is to a wet mill 2 such as a ball mill by a coal conveying device 1 without being dried or pulverized, and a heated solvent is supplied to the wet mill 2 from a solvent circulation line 3. In the wet mill 2, coal is pulverized, coal and a solvent are mixed, and the coal is dehydrated to produce a coal/solvent slurry having a predetermined temperature. In this case, the crushed grain size of the coal is 200, and the mesh passing rate is about 50.
95%, the moisture content of the coal/solvent slurry is approximately 0 to 10% by weight, and the operating conditions are appropriately selected such that the temperature of the coal/solvent slurry is approximately 100 to 250°C. Next, this coal/solvent slurry is sent to a preheater 5 by a pump 4, where it is preheated together with hydrogen added from a hydrogen supply pipe 6, and further sent to a reaction tower 7, where a decomposition and extraction reaction is performed. The slurry-like product generated by the decomposition-extraction reaction is sent to the gas-liquid separator 8 to separate the gas, and then introduced into the atmospheric distillation column 10 where light oil is extracted from the light oil distillation pipe 11 at the top of the column. The bottom oil is extracted and sent to a vacuum distillation column 13 via a vaporization column bottom oil distillation pipe 12. In the vacuum distillation column 13, fuel oil is extracted from the fuel oil distillation pipe 14 at the top of the column, and heavy oil is extracted from the vacuum distillation column 15 at the bottom of the column, and is usually sent to a gasifier. . A part or all of the fuel oil distilled from the vacuum distillation column 13 is circulated to the wet mill 2 as a solvent for coal through the aforementioned solvent circulation line 3. Instead of using the fuel oil distilled from the vacuum distillation column 13 as the circulating solvent, the vacuum distillation column 13
Any distillate oil obtained by distilling a slurry product, such as the bottom oil of the column 10 or the bottom oil of the atmospheric distillation column 10, can be used. In addition, 16 is a gas purification device,
17 is a purified gas extraction pipe, 18 is a water separation tank, 20 is a water extraction pipe, and 21 is an exhaust gas discharge tower. Next, another example of the present invention will be explained. In the above example, distillate oil obtained by distilling a slurry product is
Although part or all of the solvent is recycled, in this example, the distillate obtained by distilling this slurry product is recycled to the wet mill 2 as a solvent in the solvent circulation line 3, and A slurry-like product produced by the decomposition-extraction reaction is recycled to the wet mill 2 as a solvent through a slurry-like product circulation line 22. Note that the amount of circulation is appropriately adjusted so that the total of the distillate oil and the slurry product becomes part or all of the amount of solvent required for the raw coal. Furthermore, other examples of the present invention will be explained. The purpose of this example is to uniformly disperse coal particles in a solvent to prevent the coal particles from settling.
The coal is pulverized, the coal is mixed with a solvent, the coal is dehydrated, and the coal particles are dispersed to form a coal/solvent slurry that has a predetermined temperature and is difficult for particles to settle. The slurry is preheated under hydrogenation to perform a decomposition-extraction reaction, and the decomposition-extraction reaction product is recycled as at least a portion of the solvent. When only the distillate oil obtained by distilling a slurry product is used as the decomposition/extraction reaction product to be recycled, this distillate oil and the slurry product may be used. Same as in case. The surfactant used in this example is preferably an ionic surfactant, but especially -
Those having SO 3 H group or -OSO 3 H group or their salts, phosphoric acid esters or their salts, -
Anionic surfactants such as those having a COOH group or salts thereof, or mixtures thereof are suitable. Further, the amount of surfactant added is preferably about 0.01 to 5% by weight of the coal/solvent slurry. The surfactant may be introduced directly into the wet mill 2 or may be added in advance to the solvent circulation line 3, the slurry product circulation line 22, or the raw coal. Regarding the effect of surfactants, the height on the cylinder
The slurry was filled to a depth of 180 mm, and the settling time of a 20 g glass rod with a diameter of 5 mm was measured. In FIG. 2, a comparison was made between a slurry to which a surfactant was added and a slurry to which no surfactant was added. In the case of this example, anionic sodium dodecylbenzenesulfonate was added as a surfactant in an amount of 0.5% by weight based on the weight of brown coal in the slurry. From this figure, the slurry without adding surfactant is
As you approach the bottom of the cylinder, you can see that it takes a long time for the glass rod to fall, and that a high concentration of lignite is settling at the bottom. On the other hand, in the slurry to which the surfactant was added, the glass rod fell almost at the same speed to the bottom, indicating that the additive was effective in preventing the lignite particles in the slurry from settling. Although FIG. 1 shows a hydrogenated solvent extraction device for performing vacuum distillation as an example, the present invention can be applied to other hydrogenated solvent extraction devices, such as a hydrogenated solvent extraction device that does not perform vacuum distillation. Of course it can be done. [Examples] Examples of the present invention will be described below. Example 1 An experiment was conducted using the apparatus shown in FIG. As raw material coal, bituminous coal from Kentucky having the composition shown in Table 1 was used.
【表】
石炭1000Kg／Hr、循環溶剤500Kg／Hr、循環
スラリ状生成物1812Kg／Hrを湿式ミルに供給し
（溶剤／石炭比1.18）、粉砕、混合、脱水を行つ
た。循環溶剤の温度49℃、粘度5cp（49℃におけ
る）、スラリ濃度０％、循環スラリ状生成物の温
度371℃、粘度20cp（371℃における）、スラリ濃
度28.8％であつた。
湿式ミルにて調製された石炭・溶剤スラリの性
状は第２表の如くであつた。[Table] Coal 1000Kg/Hr, circulating solvent 500Kg/Hr, and circulating slurry product 1812Kg/Hr were supplied to a wet mill (solvent/coal ratio 1.18), and pulverized, mixed, and dehydrated. The circulating solvent temperature was 49° C., the viscosity was 5 cp (at 49° C.), and the slurry concentration was 0%; the circulating slurry product temperature was 371° C., the viscosity was 20 cp (at 371° C.), and the slurry concentration was 28.8%. The properties of the coal/solvent slurry prepared in the wet mill were as shown in Table 2.
【表】
実施例 ２
界面活性剤として、ドデシルベンゼンスルフオ
ン酸ナトリウムを湿式ミルの入口に直接、供給装
置を用いて供給した。界面活性剤の添加量は３
Kg／Hr（供給石炭量に対し0.3重量％）であつた。
他の条件は実施例１と同様であつた。
得られた石炭・溶剤スラリの性状は第３表の如
くであつた。[Table] Example 2 As a surfactant, sodium dodecylbenzenesulfonate was supplied directly to the inlet of a wet mill using a supply device. The amount of surfactant added is 3
Kg/Hr (0.3% by weight based on the amount of coal supplied).
Other conditions were the same as in Example 1. The properties of the obtained coal/solvent slurry were as shown in Table 3.
以上説明したように、本発明の方法は水分を含
む石炭を乾燥、粉砕することなく、加熱した溶剤
とともに湿式ミルに供給し、溶剤の存在下で石炭
の粉砕、石炭と溶剤との混合、石炭の加熱および
石炭中の水分の蒸発を同時に行つて、所定の温度
の石炭・溶剤スラリを製造するものであるから、
下記のような種々の効果を有している。
(1) 水分を含む石炭の乾燥、粉砕および石炭と溶
剤との混合を同時に行うので、工程を簡易化す
ることができる。
(2) 溶剤として反応生成物を循環使用するので、
その熱量を有効に利用することができ、石炭の
加熱、乾燥の必要熱量を系外から補給すること
なくきわめて熱経済的である。
(3) 石炭・溶剤スラリは所定温度に製造し得るの
で、流動に充分な粘度を得ることが可能であ
る。
(4) 湿式ミル内雰囲気は低酸素状態で、高温度で
ないために、石炭の酸化を防止することができ
る。
(5) 湿式ミルは連続操作であつて石炭および溶剤
の流れに短絡が少なく、溶剤／石炭比の制御が
確実に行われ、予熱、反応器の運転操作を安定
に行うことができる。
(6) 湿式ミルの操作は常圧で行われるので、操作
が安全であり、かつ装置材料として比較的低質
のものを使用することができる。
As explained above, the method of the present invention involves feeding coal containing water to a wet mill together with a heated solvent without drying or pulverizing it, pulverizing the coal in the presence of the solvent, mixing the coal with the solvent, and Coal/solvent slurry at a predetermined temperature is produced by simultaneously heating the coal and evaporating the moisture in the coal.
It has various effects as described below. (1) The drying and pulverization of moist coal and the mixing of coal and solvent are performed at the same time, so the process can be simplified. (2) Since the reaction product is recycled as a solvent,
The amount of heat can be used effectively, and the amount of heat required for heating and drying the coal is not supplied from outside the system, making it extremely thermoeconomical. (3) Since the coal/solvent slurry can be manufactured at a predetermined temperature, it is possible to obtain sufficient viscosity for flow. (4) The atmosphere inside the wet mill is low in oxygen and not at high temperatures, which prevents coal from oxidizing. (5) Wet mills operate continuously, with few short circuits in the flow of coal and solvent, and the solvent/coal ratio is reliably controlled, allowing for stable preheating and reactor operation. (6) Wet mills are operated at normal pressure, so they are safe to operate and can use relatively low-quality equipment materials.
第１図は本発明の方法を実施する装置の一例を
示すフローシート、第２図は界面活性剤を添加し
たスラリおよび界面活性剤を添加しないスラリに
おける、液面からのガラス棒落下時間とスラリ高
さとの関係を示すグラフである。
１……石炭搬送装置、２……湿式ミル、３……
溶剤循環ライン、４……ポンプ、５……予熱器、
６……水素供給管、７……反応塔、８……気液分
離器、１０……常圧蒸留塔、１１……軽質油留出
管、１２……蒸圧塔底油留出管、１３……減圧蒸
留塔、１４……燃料油留出管、１５……減圧塔底
油留出管、１６……ガス精製装置、１７……精製
ガス抜出管、１８……水分離槽、２０……水抜出
管、２１……排ガス排出塔、２２……スラリ状生
成物循環ライン。
Fig. 1 is a flow sheet showing an example of an apparatus for carrying out the method of the present invention, and Fig. 2 shows the drop time of the glass rod from the liquid surface and the slurry in slurry with and without surfactant. It is a graph showing the relationship with height. 1...Coal conveyance device, 2...Wet mill, 3...
Solvent circulation line, 4... pump, 5... preheater,
6... Hydrogen supply pipe, 7... Reaction column, 8... Gas-liquid separator, 10... Atmospheric pressure distillation column, 11... Light oil distillation pipe, 12... Vapor pressure tower bottom oil distillation pipe, 13... Vacuum distillation column, 14... Fuel oil distillation pipe, 15... Vacuum tower bottom oil distillation pipe, 16... Gas purification device, 17... Purified gas extraction pipe, 18... Water separation tank, 20...Water withdrawal pipe, 21...Exhaust gas discharge tower, 22...Slurry product circulation line.
Claims (1)
化するにあたり、水分を含む石炭と加熱した溶剤
とを湿式ミルに供給し石炭の粉砕、石炭と溶剤と
の混合および石炭の脱水を行つて所定の温度を有
する石炭・溶剤スラリとし、ついでこの石炭・溶
剤スラリを水素添加のもとで予熱して分解抽出反
応を行わしめ、分解抽出反応生成物を前記溶剤の
少なくとも一部として循環使用することを特徴と
する石炭液化における石炭・溶剤スラリの製造方
法。 ２ 循環使用する分解反応生成物が、分解抽出反
応により生成したスラリ状生成物を蒸留して得た
留出油である特許請求の範囲第１項記載の石炭液
化における石炭・溶剤スラリの製造方法。 ３ 循環使用する分解反応生成物が、分解抽出反
応により生成したスラリ状生成物およびこのスラ
リ状生成物を蒸留して得た留出油である特許請求
の範囲第１項記載の石炭液化における石炭・溶剤
スラリの製造方法。 ４ 水分を含む石炭と溶剤とを使用して石炭を液
化するにあたり、水分を含む石炭、加熱した溶剤
および界面活性剤を湿式ミルに供給し石炭の粉
砕、石炭と溶剤との混合、石炭の脱水および石炭
粒子の分散を行つて所定の温度を有しかつ粒子の
沈降し難い石炭・溶剤スラリとし、ついでこの石
炭・溶剤スラリを水素添加のもとで予熱して分解
抽出反応を行わしめ、分解抽出反応生成物を前記
溶剤の少なくとも一部として循環使用することを
特徴とする石炭液化における石炭・溶剤スラリの
製造方法。 ５ 循環使用する分解反応生成物が、分解抽出反
応により生成したスラリ状生成物を蒸留して得た
留出油である特許請求の範囲第４項記載の石炭液
化における石炭・溶剤スラリの製造方法。 ６ 循環使用する分解反応生成物が、分解抽出反
応により生成したスラリ状生成物およびこのスラ
リ状生成物を蒸留して得た留出油である特許請求
の範囲第４項記載の石炭液化における石炭・溶剤
スラリの製造方法。[Claims] 1. In liquefying coal using coal containing water and a solvent, the coal containing water and a heated solvent are supplied to a wet mill to crush the coal, mix the coal and the solvent, and The coal is dehydrated to form a coal/solvent slurry having a predetermined temperature, and then this coal/solvent slurry is preheated under hydrogenation to perform a decomposition-extraction reaction, and the decomposition-extraction reaction product is converted into a coal-solvent slurry having a predetermined temperature. A method for producing coal/solvent slurry in coal liquefaction, which is characterized in that it is recycled as a part of the slurry. 2. The method for producing a coal/solvent slurry in coal liquefaction according to claim 1, wherein the decomposition reaction product to be recycled is a distillate obtained by distilling a slurry product generated by the decomposition-extraction reaction. . 3. Coal in coal liquefaction according to claim 1, wherein the decomposition reaction products to be recycled are a slurry product produced by the decomposition-extraction reaction and a distillate oil obtained by distilling this slurry product.・Method for producing solvent slurry. 4. When liquefying coal using coal containing moisture and a solvent, the coal containing moisture, heated solvent, and surfactant are supplied to a wet mill to crush the coal, mix the coal and solvent, and dehydrate the coal. Then, the coal particles are dispersed to form a coal/solvent slurry having a predetermined temperature and in which the particles do not easily settle.Then, this coal/solvent slurry is preheated under hydrogenation to perform a decomposition/extraction reaction, and the coal/solvent slurry is decomposed. A method for producing a coal/solvent slurry in coal liquefaction, characterized in that an extraction reaction product is recycled as at least a part of the solvent. 5. The method for producing a coal/solvent slurry in coal liquefaction according to claim 4, wherein the decomposition reaction product to be recycled is a distillate obtained by distilling a slurry product generated by the decomposition-extraction reaction. . 6. Coal in coal liquefaction according to claim 4, wherein the decomposition reaction products to be recycled are a slurry product produced by the decomposition-extraction reaction and a distillate oil obtained by distilling this slurry product.・Method for producing solvent slurry.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8322880A JPS578284A (en) | 1980-06-18 | 1980-06-18 | Preparation of coal-solvent slurry in coal liquefaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8322880A JPS578284A (en) | 1980-06-18 | 1980-06-18 | Preparation of coal-solvent slurry in coal liquefaction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS578284A JPS578284A (en) | 1982-01-16 |
| JPH0144755B2 true JPH0144755B2 (en) | 1989-09-29 |
Family
ID=13796454
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP8322880A Granted JPS578284A (en) | 1980-06-18 | 1980-06-18 | Preparation of coal-solvent slurry in coal liquefaction |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS578284A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108395900B (en) * | 2018-05-03 | 2020-09-01 | 大连爱为能源有限公司 | Pulping treatment method for oil sand |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52145409A (en) * | 1976-05-28 | 1977-12-03 | Kobe Steel Ltd | Liquefaction of low grade coals |
| JPS5351204A (en) * | 1976-10-22 | 1978-05-10 | Kobe Steel Ltd | Conversion of coals |
| JPS53112902A (en) * | 1977-03-12 | 1978-10-02 | Kobe Steel Ltd | Heat dehydration of brown coal |
| JPS53112905A (en) * | 1977-03-12 | 1978-10-02 | Kobe Steel Ltd | Production of slurry for brown coal liquefaction |
| JPS53125404A (en) * | 1977-04-08 | 1978-11-01 | Kobe Steel Ltd | Production of slurry for brown coal liquefaction |
-
1980
- 1980-06-18 JP JP8322880A patent/JPS578284A/en active Granted
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52145409A (en) * | 1976-05-28 | 1977-12-03 | Kobe Steel Ltd | Liquefaction of low grade coals |
| JPS5351204A (en) * | 1976-10-22 | 1978-05-10 | Kobe Steel Ltd | Conversion of coals |
| JPS53112902A (en) * | 1977-03-12 | 1978-10-02 | Kobe Steel Ltd | Heat dehydration of brown coal |
| JPS53112905A (en) * | 1977-03-12 | 1978-10-02 | Kobe Steel Ltd | Production of slurry for brown coal liquefaction |
| JPS53125404A (en) * | 1977-04-08 | 1978-11-01 | Kobe Steel Ltd | Production of slurry for brown coal liquefaction |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS578284A (en) | 1982-01-16 |
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