JPS59197490A - Coke producing equipment - Google Patents
Coke producing equipmentInfo
- Publication number
- JPS59197490A JPS59197490A JP7356383A JP7356383A JPS59197490A JP S59197490 A JPS59197490 A JP S59197490A JP 7356383 A JP7356383 A JP 7356383A JP 7356383 A JP7356383 A JP 7356383A JP S59197490 A JPS59197490 A JP S59197490A
- Authority
- JP
- Japan
- Prior art keywords
- coking
- tank
- heavy oil
- coke
- oil
- 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.)
- Granted
Links
- 239000000571 coke Substances 0.000 title abstract description 29
- 238000004939 coking Methods 0.000 claims abstract description 61
- 238000010438 heat treatment Methods 0.000 claims abstract description 27
- 230000003111 delayed effect Effects 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 2
- 239000003921 oil Substances 0.000 abstract description 28
- 239000000295 fuel oil Substances 0.000 abstract description 25
- 239000002994 raw material Substances 0.000 abstract description 20
- 238000004227 thermal cracking Methods 0.000 abstract description 5
- 238000011282 treatment Methods 0.000 abstract description 5
- 239000003208 petroleum Substances 0.000 abstract description 4
- 239000011280 coal tar Substances 0.000 abstract description 2
- 238000004821 distillation Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 13
- 238000000197 pyrolysis Methods 0.000 description 10
- 238000001816 cooling Methods 0.000 description 7
- 238000005979 thermal decomposition reaction Methods 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Landscapes
- Coke Industry (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、多様な性状の原料重質油から、良好な品質の
製品コークスを製造し得るコークス化装置に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a coking apparatus capable of producing product coke of good quality from raw material heavy oil of various properties.
石油系または石炭系の重質油からコークスを得るために
ディレードコークス化装置が広く用いられている。この
ディレードコークス化装置は、一般に、基本的には原料
重質油の加熱炉と互いに並列に設けられた2基以上のコ
ークス化槽とをこの順序で直列に接続してなるものであ
り、原料重質油をポンプにより加熱して、450〜50
0℃の熱分解温度に達したものをコークス化槽に送り込
んで比較的長時間滞留させ、当該コークス化槽の内部に
重質油の分解によって生成したコークスを蓄積せしめる
とともに、その頂部より分解生成油を留出させることに
よりディレートコ−キング法が実施される。Delayed coking equipment is widely used to obtain coke from petroleum-based or coal-based heavy oil. Generally, this delayed coking equipment basically consists of a heating furnace for raw material heavy oil and two or more coking tanks installed in parallel with each other, connected in series in this order. Heavy oil is heated by a pump to a temperature of 450 to 50
The coke that has reached a thermal decomposition temperature of 0°C is sent to a coking tank where it stays for a relatively long time, and the coke produced by decomposition of heavy oil is accumulated inside the coking tank, and the coke is decomposed from the top. A dilate coking process is carried out by distilling off the oil.
しかしながら、このディレーrコーキング法の一つの問
題点として、限られた性状の原料重質油以外からは高品
質のコークスが得られないことがある。このため、多様
な原料重質油から良質なコークスを製造するための技術
がいくつか提案されている。このような技術としては、
例えば、石油系重質油をあらかじめ、熱分解装置によっ
て適度の熱分解を行なわせ、得られるタールを原料゛と
しであるいは原料の一部として用いる調合油をコークス
化槽に供給する方法(特公昭49−33901号公報な
ど)、接融分解装置からのクラリファイド油を配合原料
油として用いる方法(特公昭あ−18176号公報など
)、直列二段のコークス化槽を使用し、第1段の槽内に
は原料油中の早期コーキング成分から生ずる劣質コーク
スを生成せしめ、第2段の構内において残りの油分から
高品質のコークスを製造する方法(背開昭48−899
02号公報)などがある。前2者は、ディレートコ−キ
ング法における原料油の選択もしくは前処理の範囲に模
する方法であり、後者は原料油中の劣質成分の除去乞主
眼とするものであり、いずれにしても広くは原料油の組
成調整7特徴とする技術といえよう。However, one problem with this delayed coking method is that high-quality coke cannot be obtained from sources other than heavy oil with limited properties. For this reason, several techniques have been proposed for producing high-quality coke from a variety of raw material heavy oils. As such technology,
For example, there is a method in which petroleum-based heavy oil is subjected to appropriate thermal decomposition in advance in a pyrolysis device, and the resulting tar is used as a raw material or as part of the raw material to supply a blended oil to a coking tank (Tokuko Showa). 49-33901, etc.), a method using clarified oil from a fused cracker as a blending stock oil (Japanese Patent Publication No. 18176, etc.), a method using two coking tanks in series, and A method of producing inferior coke from the early coking components in the feedstock oil in the tank, and producing high quality coke from the remaining oil in the second stage premises (Sekai 1989-899).
Publication No. 02). The former two methods are similar to the range of selection or pretreatment of raw material oil in the dilate coking method, and the latter aims at removing inferior components in the raw material oil, and in any case, it is not widely used. It can be said that this technology has seven characteristics: adjusting the composition of raw oil.
本発明は、広い意味では原料油の調整技術に関するとい
えようが比較的簡単な装置の改造によって、反応条件の
操作域を拡大し、多椋な品質の原料油から高品質のコー
クスを生産する技術を提供せんとするものである。In a broad sense, the present invention relates to a technology for adjusting feedstock oil, but by relatively simple modification of equipment, the operating range of reaction conditions can be expanded, and high quality coke can be produced from a wide range of quality feedstock oils. The aim is to provide technology.
従来から使用されている通常のディレーPコークス化装
置においては、加熱炉によって所定の温度に加熱された
流体は、保温されたコークス化槽に単に移送されるに過
ぎない。しかも、コークス化槽は所望の熱分解およびコ
ークス化を進めるために巨大な容積を必要とし、このよ
うな巨大なコークス化槽を加熱して温度調節することは
事実上不可能である。したがって、コークス化槽、の温
度は、加熱炉で加熱された流体が持込む熱量とバランス
する自然の温度に維持されるに過ぎない。jなわち、コ
ークス化槽の温度は加熱炉出口温度にのみ依存する。も
ちろん、この他にも運転変数として原料油の流量や圧力
があるが、実際の工業的製造では設計上の制約によって
その操作$1囲が極く狭い範囲に限られ、製品コークス
の品質改善に有効な程自由ではない。In conventional delay P coking equipment, a fluid heated to a predetermined temperature by a heating furnace is simply transferred to a coking tank where the temperature is maintained. Moreover, the coking tank requires a huge volume in order to proceed with the desired thermal decomposition and coking, and it is virtually impossible to heat and control the temperature of such a huge coking tank. Therefore, the temperature of the coking bath is only maintained at a natural temperature that balances the amount of heat introduced by the fluid heated in the furnace. j That is, the temperature of the coking bath depends only on the temperature at the outlet of the heating furnace. Of course, there are other operating variables such as the flow rate and pressure of feedstock oil, but in actual industrial manufacturing, the operating range is limited to an extremely narrow range due to design constraints, and it is difficult to improve the quality of product coke. Not free enough to be effective.
一力、本発明者らは多年コークスの生産に従事するとと
もに研究を重ねた結果、製品コークス品質にはコークス
化槽での温度条件のみなら゛ず、原料油の初期コークス
化ないしは熱分解条件、特に加熱炉からコークス化槽に
至るまでの熱分解条件が非常に重大な影響を及ぼすこと
を発見した。すなわち、ttiU御の困21’東なコー
クス化槽における反応条件を制御するのでなく、その予
備的な熱分解条件を制御することにより、コークス品質
の制御が可能であることを見出したのである。しかも、
予備的な熱分解工程は、比較的短時間のうちに達成され
るので、その制御は、巨大なコークス化槽におけるそれ
に比べて著しく簡単である。The inventors of the present invention have been engaged in coke production for many years and have conducted extensive research. As a result, the quality of the coke product depends not only on the temperature conditions in the coking tank, but also on the initial coking or thermal decomposition conditions of the feedstock oil. In particular, we discovered that the pyrolysis conditions from the heating furnace to the coking tank have a very important influence. In other words, it has been found that coke quality can be controlled not by controlling the reaction conditions in the coking tank, but by controlling the preliminary thermal decomposition conditions. Moreover,
Since the preliminary pyrolysis step is accomplished in a relatively short time, its control is significantly simpler than in huge coking tanks.
本発明のコークス化装置は、このような知見に基づくも
のであり、より詳しくは加熱炉とコークス化槽とをこの
順序で配管により結合してなるディレーrコークス化装
置において、上記コークス化幅に比べて小容量で独立の
圧力および温度制御手段を備える中間槽を設け、該中間
槽での処理物の実質的に全量をコークス化槽に供給づ−
るようたしたことを時機とするものである。The coking apparatus of the present invention is based on such knowledge, and more specifically, in a delayed coking apparatus in which a heating furnace and a coking tank are connected in this order by piping, the coking width is An intermediate tank having a relatively small capacity and having independent pressure and temperature control means is provided, and substantially the entire amount of the material to be processed in the intermediate tank is supplied to the coking tank.
This is an opportunity to do something like this.
以下、本発明を図面に基いて更に詳細に説明する。Hereinafter, the present invention will be explained in more detail based on the drawings.
図面は、本発明のコークス化装置の各部の配置図である
。この装置は、加熱炉l、中間槽2、並列に配置された
一対のコークス化(曹3a 、 3b 、分留塔4を、
この順序で配管12 、23 ; 34によりゃ士+1
直列に結合してなる。また加熱炉lへやま原料重質油タ
ンク(図示せずはり原料供給配管5カを結合され、この
配管5には分留塔4の底部力\らのイ盾環配管41が結
合されている。また中間槽2の下部にハ過熱スチーム導
入配管6が、上部には冷却油導入配管7が、それぞれ結
合され、更に中間槽2の出口配管には圧力制御弁8が設
けら1−1.て(・る。中間槽2の容積は、コークス化
槽3aまたは3bの容積の1〜5%程度が適当である。The drawing is a layout diagram of each part of the coking apparatus of the present invention. This device consists of a heating furnace 1, an intermediate tank 2, a pair of coking units (coke 3a, 3b, and a fractionating column 4) arranged in parallel.
In this order, pipes 12, 23; 34 +1
They are connected in series. In addition, 5 raw material supply pipes (not shown) are connected to the heating furnace 1 and a raw material heavy oil tank (not shown), and a shield ring pipe 41 for the bottom part of the fractionating column 4 is connected to this pipe 5. Further, a superheated steam introduction pipe 6 is connected to the lower part of the intermediate tank 2, and a cooling oil introduction pipe 7 is connected to the upper part, and a pressure control valve 8 is provided at the outlet pipe of the intermediate tank 2.1-1. The volume of the intermediate tank 2 is suitably about 1 to 5% of the volume of the coking tank 3a or 3b.
上記装置の代表的な運転態様につ(・て説明する。A typical operating mode of the above device will be explained.
まず配管5からは、石油系の常圧な(・し減王直留残渣
油、熱分解残渣油あるいはコールタール等力)らなる原
料重質油を供給し、加熱炉1を経て450〜500℃に
加熱したのち、中間槽2に導入し、こてで100〜30
0秒程度の滞留時間で予備的な加熱分解を行う。この際
、加熱炉1の出口温度が使用した原料油種に対しては低
過ぎる場合に髪ま配管6より過熱スチーム等を導入して
内容物の加熱を行い、また高過ぎる場合には、配管7よ
り低目の温度に加熱した冷却油乞導入して内容物の冷却
を行う。このように、加熱炉lの出口温度でなく、中間
槽2において再度温度制御を行うのは、一旦標準的な油
種に対して設定された加熱炉lの容置、加熱・ぞターン
等のファクターは、原料油種が変化しても追随して変化
させることができず、加熱炉1のみによっては理想的な
予備熱分解条件が採用できない場合があるからである。First, from the pipe 5, raw material heavy oil consisting of petroleum-based normal pressure (reduced straight-run residual oil, pyrolysis residual oil, coal tar, etc.) is supplied, and it passes through the heating furnace 1 to a temperature of 450 to 500 After heating it to ℃, it was introduced into the intermediate tank 2 and heated to
Preliminary thermal decomposition is performed with a residence time of approximately 0 seconds. At this time, if the outlet temperature of the heating furnace 1 is too low for the type of raw material oil used, superheated steam or the like is introduced from the steam pipe 6 to heat the contents; Cooling oil heated to a temperature lower than 7 is introduced to cool the contents. In this way, the reason for controlling the temperature again in the intermediate tank 2, rather than the outlet temperature of the heating furnace 1, is to control the temperature of the heating furnace 1 once set for the standard oil type, heating, turning, etc. This is because the factor cannot be changed accordingly even if the raw material oil type changes, and ideal preliminary pyrolysis conditions may not be adopted depending only on the heating furnace 1.
更に、中間槽2内の圧力は、制御弁8の開閉により、コ
ークス化m3a、3b内の圧力と同等ないしはこれより
高い5−30 Ky/crn” Gに制御される。Furthermore, the pressure in the intermediate tank 2 is controlled to 5-30 Ky/crn''G, which is equal to or higher than the pressure in the coking m3a, 3b, by opening and closing the control valve 8.
後記実施例に示すように予備的熱分解の圧力をある制限
内で高くすることは製品コークスの品質改善のために有
利であることを見出℃た(後記実赫例参照〕が、この中
間槽2における圧力の制御は予備熱分解反応条件として
の圧力を調節するのみでなく、中間槽2内での滞留時間
を調節する作用も有する。また、中間槽2の容積はコー
クス化槽3a 、 3bに比べて著しく小容積であるの
で、同じ初期熱分解の加圧を、コークス比倫3a 、
3bでなく中間槽2で行うことは、加圧容器としての装
置経済上もはるかに有利である。As shown in the example below, we found that increasing the pressure for preliminary pyrolysis within a certain limit is advantageous for improving the quality of coke product (see practical example below); Control of the pressure in the tank 2 not only adjusts the pressure as a pre-pyrolysis reaction condition, but also has the effect of adjusting the residence time in the intermediate tank 2.The volume of the intermediate tank 2 is the same as that of the coking tank 3a, Since the volume is significantly smaller than that of coke 3b, the same initial pyrolysis pressure can be applied to coke 3a,
Carrying out the process in the intermediate tank 2 instead of in the intermediate tank 3b is far more advantageous in terms of the economics of the device as a pressurized container.
上記中間槽2で初期熱分解処理した重質油は、通常のデ
ィレートコ−キング法と同様にコークス化’t43a
、 3bにおいて更にコークス化処理される。The heavy oil subjected to the initial thermal decomposition treatment in the intermediate tank 2 is converted into coke 't43a in the same way as in the normal dilate coking method.
, 3b, further coking treatment is carried out.
すなわち、中間槽2からの重質油は配管ハを経てコーク
ス化Wi 3a 、 3bの一方、たとえば3a にそ
の底部々)ら装入され、槽3a 内で次第に増量しつつ
計24〜48時間保持される過程で更に熱分解ならびに
コークス化処理を受ける。槽3aがほぼ満量となった時
点で、今度は重質油を槽3b・に導入する。一方、槽3
a においては、更にしばらくの間熱分解ならびにコー
クス化を進め、分解油は配管あから分留塔4に導入し、
その塔頂ならびに中間段から配管9a 、 9b 、
9c等を経て分解ガスないし製品軽質油を回収するとと
も□に、その塔底からは配管41を経て、重質油を加熱
器1上流へ循環する。That is, the heavy oil from the intermediate tank 2 is charged into one of the coking Wis 3a and 3b (for example, the bottom part of the coke Wi 3a) through the pipe C, and is held in the tank 3a for a total of 24 to 48 hours while gradually increasing the amount. During the process, it is further subjected to thermal cracking and coking treatment. When tank 3a is almost full, heavy oil is introduced into tank 3b. On the other hand, tank 3
In a, thermal cracking and coking are continued for a while, and the cracked oil is introduced into the fractionating column 4 through the piping.
Pipes 9a, 9b,
The cracked gas or product light oil is recovered through 9c, etc., and the heavy oil is circulated from the bottom of the tower to the upstream side of the heater 1 through a pipe 41.
槽3a において、所要時間保持したのち、槽3aを開
放し、生成した製品コークスを回収する。After holding the coke in the tank 3a for a required period of time, the tank 3a is opened and the product coke produced is recovered.
上記においては、本発明装置の好ましい態様について説
明したが、本発明の’jii)、凹円で各種の改変が可
能である。たとえば上記の例においては、中間槽2にお
いて相加的な加熱および冷却手段を設けているが、これ
は加熱または冷却手段のいずれか一方でもよく、また加
熱および冷却は、直接熱交換でなく間接熱交換によって
もよい。また、中間槽2は前記の目的が達成される限り
どのような形状ないし構造のものであってもよい。従っ
て、前記のような槽壁のものの外に、管状のものあるい
は管をコイル状に配設したものがありうる。In the above, preferred embodiments of the device of the present invention have been described, but various modifications can be made to the concave circle of the present invention. For example, in the above example, additional heating and cooling means are provided in the intermediate tank 2, but this may be either heating or cooling means, and the heating and cooling may be indirect rather than direct heat exchange. It may also be done by heat exchange. Further, the intermediate tank 2 may have any shape or structure as long as the above objective is achieved. Therefore, in addition to the tank wall type described above, there may be a tubular type or a type in which a tube is arranged in a coiled manner.
上述したように、本発明によれば通常のディレードコー
クス化装置において、独立の圧力およ、び温度1j制御
手段乞備えた中間槽を設けるというfThl革な改変に
より、多様な原料重質油の変化に追随して最適な初期熱
分解処理の設定が可能になり、同一の原料重質油から得
られる製品コークスの品質を改善することが可能になる
。As described above, according to the present invention, a conventional delayed coking apparatus is modified to provide an intermediate tank equipped with independent pressure and temperature control means, thereby making it possible to handle a variety of feedstock heavy oils. It becomes possible to set the optimal initial pyrolysis treatment according to changes, and it becomes possible to improve the quality of product coke obtained from the same raw material heavy oil.
以下、実施例、比較例により本発明装置の使用効果につ
いてより具体的に説明する。Hereinafter, the effects of using the device of the present invention will be explained in more detail with reference to Examples and Comparative Examples.
男−」
内径3關、長さ9mの加熱管を備えた加熱炉2基と、こ
の加熱炉に連設された内容積2tの中間槽と、この中間
槽に連設された内容積80tのコークス化槽とからなる
ノξイロットプラント規模のコークス化装置を建設した
。この中間槽は、加熱手段として高温スチーム供給装置
を有し冷却手段としてクエンチングオイル供給装置を有
し、圧力制御手段としてコントロールノ々ルブを有して
いた。Two heating furnaces equipped with heating pipes with an inner diameter of 3 mm and a length of 9 m, an intermediate tank with an internal volume of 2 tons connected to the heating furnaces, and a tank with an internal volume of 80 tons connected to the intermediate tanks. A plant-scale coking unit consisting of a coking tank and a coking tank was constructed. This intermediate tank had a high temperature steam supply device as a heating means, a quenching oil supply device as a cooling means, and a control knob as a pressure control means.
使用した原料重質油の性状を表1に示す。なお、以下の
例2、比較例1および2においても表1に示す原料重質
油を用いた。Table 1 shows the properties of the raw material heavy oil used. Note that the raw material heavy oil shown in Table 1 was also used in Example 2 and Comparative Examples 1 and 2 below.
表 1
このような性状を有する原料重質油を200.9 /分
の速度で加熱炉に供給し、表2に示す条件でデイレード
コーキング乞行なった結果な辰3に示す。Table 1 The raw material heavy oil having the above properties was supplied to the heating furnace at a rate of 200.9/min, and delayed coking was performed under the conditions shown in Table 2. The results are shown in Table 3.
例2
中間槽における中間分解槽圧力を変化させた以外は、例
1と同様にして表2に示す条件下で原料重質油のディレ
ードコーキングを行ない、結果を表3に示す。Example 2 Delayed coking of feedstock heavy oil was carried out under the conditions shown in Table 2 in the same manner as in Example 1 except that the intermediate cracking tank pressure in the intermediate tank was changed, and the results are shown in Table 3.
比較例1
中間ta暑設けなかった以外は例1と同様の・ξイロッ
トプラントを建設し、例1と同様にして表2に示す条件
下で、原料重質油のディレートコ−キングを行ない、結
果を表3に示す。Comparative Example 1 A ξ pilot plant similar to that of Example 1 was constructed except that no intermediate heat was provided, and dirate coking of feedstock heavy oil was carried out under the conditions shown in Table 2 in the same manner as in Example 1. are shown in Table 3.
表 2
表 3
*30〜Zoo℃の間の熱膨張係数値(ダレイン方向)
表3の結果を見ると、中間槽2において加圧下で初期熱
分解を実施した実施例1.2は、それ自体は使用原料油
に対して通常のディレードコーキング法として最適の条
件で実施された比較例と比べて、原料油の分解が進み、
軽質弁(ガス、ガンリン、軽油)の収率が向上している
だけでなく、製品コークスとしても見かけ比重が向上し
、熱膨張係数の小さい良質なコークスが得られているこ
とがわかる。Table 2 Table 3 *Thermal expansion coefficient values between 30 and Zoo℃ (drain direction)
Looking at the results in Table 3, it can be seen that Example 1.2, in which initial pyrolysis was carried out under pressure in intermediate tank 2, was carried out under optimal conditions as a normal delayed coking method for the raw material used. Compared to the comparative example, the decomposition of the feedstock oil has progressed,
It can be seen that not only the yield of light valves (gas, gas oil, diesel oil) has improved, but also the apparent specific gravity of the product coke has improved, resulting in high-quality coke with a small coefficient of thermal expansion.
比較例2
中間槽を設けない比較例1の・ぐイロットプラントによ
り、加熱炉温度乞490℃、コークス化温度y46o−
cとして原料重質油のディレーPコーキングを行なった
が、その際コークス化槽ヲ5に2/cfn2Gから7
K9/CITL2Gにまで加圧した。得られたコークス
は、1.25の見かげ比重(,9/Cm3)および2.
00C,T、E、を有していた。Comparative Example 2 The heating furnace temperature was 490°C and the coking temperature was 46o-
Delay P coking of the raw material heavy oil was carried out as c, but at that time, the coking tank was heated from 2/cfn2G to 7.
The pressure was increased to K9/CITL2G. The obtained coke had an apparent specific gravity of 1.25 (,9/Cm3) and 2.
It had 00C, T, E.
このことから、中間槽を設けずに単にコークス化槽の圧
力を上昇させても、良好な性状を有するコークスは得ら
れないことがわかる。This shows that coke with good properties cannot be obtained simply by increasing the pressure in the coking tank without providing an intermediate tank.
図面は、本発明の一実施例てかかるコークス化装置の谷
部の配置図である。
1・・・加熱炉、2・・・中間や、1.3a 、 3b
・・・コークス化槽、4・・・分留塔、6・・・過熱ス
チーム配管、7・・・冷却油配管、8・・・圧力制御弁
。The drawing is a layout diagram of a trough of a coking apparatus according to an embodiment of the present invention. 1... Heating furnace, 2... Intermediate, 1.3a, 3b
. . . Coking tank, 4. Fractionation tower, 6. Superheated steam piping, 7. Cooling oil piping, 8. Pressure control valve.
Claims (1)
てなるディレードコークス化装置において、上記コーク
ス化槽に比べて小容量で独立の圧力および温度制御手段
を備える中間槽を設け、該中間槽での処理物の実質的に
全量をコークス化槽に供給するようにしたことを特徴と
するコークス化装置。In a delayed coking apparatus in which a heating furnace and a coking tank are connected in this order by piping, an intermediate tank having a smaller capacity than the coking tank and equipped with independent pressure and temperature control means is provided, and the intermediate tank is equipped with an independent pressure and temperature control means. A coking apparatus characterized in that substantially the entire amount of the processed material is supplied to a coking tank.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP7356383A JPS59197490A (en) | 1983-04-26 | 1983-04-26 | Coke producing equipment |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP7356383A JPS59197490A (en) | 1983-04-26 | 1983-04-26 | Coke producing equipment |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS59197490A true JPS59197490A (en) | 1984-11-09 |
JPS6246594B2 JPS6246594B2 (en) | 1987-10-02 |
Family
ID=13521853
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP7356383A Granted JPS59197490A (en) | 1983-04-26 | 1983-04-26 | Coke producing equipment |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS59197490A (en) |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5269906A (en) * | 1975-12-10 | 1977-06-10 | Toa Nenryo Kogyo Kk | Coking process |
-
1983
- 1983-04-26 JP JP7356383A patent/JPS59197490A/en active Granted
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5269906A (en) * | 1975-12-10 | 1977-06-10 | Toa Nenryo Kogyo Kk | Coking process |
Also Published As
Publication number | Publication date |
---|---|
JPS6246594B2 (en) | 1987-10-02 |
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