JP2000008051A - Hydrocracking of liquid heavy hydrocarbon and apparatus therefor - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide both a method for hydrocracking of a liquid heavy hydrocarbon by which the catalytic reaction of the liquid heavy hydrocarbon with hydrogen gas is accelerated in a compact apparatus and the production cost is low in high yield and the apparatus therefor. SOLUTION: A liquid heavy hydrocarbon or the liquid heavy hydrocarbon containing hydrogen gas mixed therewith is fed to a catalyst fixed bed 6 arranged on the outside of plural hydrogen ventilating tubes 2 and the hydrogen gas is simultaneously infiltrated from the interior of the hydrogen ventilating tubes 2 to carry out a catalytic reaction of the liquid heavy hydrocarbon with the hydrogen gas. The heat of the catalytic reaction is cooled. The liquid heavy hydrocarbon having a long chain molecular structure is reacted with the hydrogen and cracked into a liquid hydrocarbon having a short chain by the catalytic reaction. The hydrogen gas infiltrated into the catalyst fixed bed 6 and flowing therein simultaneously contributes to the cooling of the heat of the catalytic exothermic reaction.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an apparatus and a device for hydrocracking liquid heavy hydrocarbons such as heavy oil, and more particularly to a method and an apparatus for hydrocracking liquid heavy hydrocarbons by a hydrocracking process. It is.

[0002]

2. Description of the Related Art Gasoline, LP gas, kerosene, gas oil and the like are refined by atmospheric distillation or vacuum distillation of crude oil, but at the same time, a large amount of residual oil, which is heavy oil, is generated. Since the amount of investment in the residual oil treatment process is enormous, a more efficient and economical treatment method is required. Decompose heavy oil to gasoline,
Processes for upgrading kerosene, light oil, etc. are roughly classified into three types: a fluid catalytic cracking process using a catalyst, a hydrocracking process using a catalyst in a hydrogen stream, and a high-temperature non-catalytic pyrolysis process.

FIG. 3 shows a conceptual diagram of a conventional liquid heavy hydrocarbon hydrocracking apparatus using a hydrocracking process. As shown in the figure, the liquid heavy hydrocarbon such as heavy oil is usually supplied to the liquid heavy hydrocarbon inlet nozzle 2 at the top of the reaction column together with hydrogen gas.
1 and via the distributor 22
The catalyst flows into the zeolite-based or iron-based catalyst fixed layer 23 having a plurality of stages or multiple stages. The liquid heavy hydrocarbon flows down from the distributor 22 to the lower catalyst fixed bed 23 at a low speed, and in the case of a multistage, flows down to the lower catalyst fixed bed 23 at a low speed, and the purified liquid hydrocarbon after the reaction is completed. (Upgrading oil such as light oil) flows out of a purified liquid hydrocarbon outlet nozzle 25 via a purified oil collector 24 provided at the bottom of the reaction tower.

In the catalyst fixed layer 23, a liquid heavy hydrocarbon having a long chain molecular structure reacts with hydrogen gas supplied together and is decomposed into short chains by a catalytic reaction. The temperature in layer 23 increases. In order to cool the temperature rise, as shown in FIG. 3, the hydrogen gas supplied from the hydrogen gas inlet nozzle 26 is blown from below the catalyst fixed layer 23 through a diffuser such as a nozzle. The injected hydrogen gas is involved in the catalytic reaction together with the cooling of the catalyst fixed layer 23. Therefore, as shown in FIG. 3, the conventional liquid heavy hydrocarbon cracking apparatus requires a space A for supplying hydrogen gas. Note that the catalyst can be extracted from the lower portion of the catalyst fixed layer 23 through the catalyst extraction nozzle 27.

[0005] The temperature and pressure in the conventional liquid heavy hydrocarbon hydrocracker are 350 to 500 ° C, respectively.
It is about 150 to 200 atg.

[0006]

Since the conventional liquid heavy hydrocarbon hydrocracking apparatus is constructed as described above, it has the following problems. (A) In the space A (see FIG. 3) for supplying hydrogen for catalytic reaction heat cooling, as the amount of processing increases and the number of stages increases, the height of the apparatus increases. (B) In the fixed catalyst layer, it is necessary to sufficiently contact the catalyst particles with liquid heavy hydrocarbons (heavy extraction, etc.) and hydrogen gas. However, the supply of liquid heavy hydrocarbons is a flow-down system and the supply speed is slow. This leads to an enormous amount of catalyst and, consequently, an increase in the size of the reaction tower. (C) As described in the above (a) and (b), an increase in the size of the apparatus is inevitable, which increases the manufacturing cost.

Accordingly, the present invention provides a compact catalyst, in which the catalytic reaction between liquid heavy hydrocarbons and hydrogen gas is promoted,
It is an object of the present invention to provide a method and an apparatus for hydrocracking liquid heavy hydrocarbons which are inexpensive to produce and have a high yield.

[0008]

The present invention has solved the above-mentioned problems as follows. That is, a liquid heavy hydrocarbon or a liquid heavy hydrocarbon mixed with hydrogen gas is supplied to the catalyst fixed layer disposed outside the plurality of hydrogen ventilation tubes, and hydrogen gas is infiltrated from inside the hydrogen ventilation tube. The catalytic reaction between the liquid heavy hydrocarbon and the hydrogen gas is performed, and the heat of the catalytic reaction is cooled.

Contrary to the above, a liquid heavy hydrocarbon or a liquid heavy hydrocarbon mixed with hydrogen gas is supplied to a catalyst fixed layer disposed inside a plurality of hydrogen ventilation tubes, The liquid heavy hydrocarbon and the hydrogen gas may be catalyzed by infiltrating the hydrogen gas from the outside.

[0010]

DESCRIPTION OF THE PREFERRED EMBODIMENTS Embodiments of the present invention will be described based on embodiments with reference to the drawings.

FIG. 1 is a conceptual diagram of a device for hydrocracking liquid heavy hydrocarbons such as heavy oil according to the present invention.

As shown in FIG. 1, inside a pressure vessel 1 of a reaction tower, a bundle of a hydrogen permeable tube 2 made of a porous metal material or the like, a tube sheet 3 for supporting both upper and lower ends of the bundle, A catalyst layer support plate 4 for dividing a bundle of tubes 2 into a plurality of stages in the vertical direction, solid-liquid separation plates 5 provided on both sides of the catalyst layer support plate 4, and a catalyst supplied around the bundle. Catalyst fixed layer 6
Is provided.

Each catalyst layer support plate 4 is alternately provided to be shifted left and right, one end of which is in contact with the solid-liquid separation plate 5 and the other end thereof is in contact with the inner wall of the pressure vessel 1. Between the solid-liquid separation plate 5 and the inner wall of the vessel 1 is formed a liquid heavy hydrocarbon channel 7 through which liquid heavy hydrocarbon or liquid heavy hydrocarbon mixed with hydrogen gas flows from upper to lower. A hydrogen gas channel 8 is provided between the upper and lower tube sheets 3 and the top and bottom of the container 1.

A liquid heavy hydrocarbon inlet nozzle 9 is provided on the upper side of the pressure vessel 1, and a purified liquid hydrocarbon outlet nozzle 10 is provided on the lower side. A hydrogen gas outlet nozzle 11 is provided at the top of the reaction tower, and a hydrogen gas inlet nozzle 12 is provided at the bottom.
Is provided. Further, a catalyst supply device 13 for supplying the catalyst to each stage and a catalyst removal nozzle 14 for removing the catalyst from each stage are provided.

A porous metal material or MF (Micro Filtration), UF (Ultra Filtra)
The metal film material having pores of sizes up to
US, tool steel, Inconel, titanium alloy, aluminum alloy, etc. are used.

The above-mentioned MF means a fine size of about several μm to 0.1 μm, and UF means an extra fineness of about 1 μm to 0.01 μm.

As the catalyst layer support plate 4, a flat plate or a punch plate having a number of holes having a size that does not allow passage of spherical catalyst particles or cylindrical (core of a pencil) particles is used.

As the solid-liquid separation plate 5, a punch plate having a large number of holes having a size through which catalyst particles cannot similarly pass is used.

Next, the operation of the above-mentioned liquid heavy hydrocarbon hydrocracking apparatus will be described.

The liquid heavy hydrocarbon supplied from the liquid heavy hydrocarbon inlet nozzle 9 or the liquid heavy hydrocarbon mixed with hydrogen gas passes through the upper catalyst fixed layer 6 and passes through the liquid heavy hydrocarbon channel 7 to the lower heavy hydrocarbon channel 7. , And this is repeated over a plurality of stages to be purified and discharged from the purified liquid hydrocarbon outlet nozzle 10.

The flow velocity of the liquid heavy hydrocarbon in the fixed catalyst layer 6 is higher than that of the above-mentioned conventional flow-down type, and it is possible to form a turbulent state. It can be.

The hydrogen gas penetrates from the inner wall to the outer wall of the hydrogen-permeable tube 2 made of a porous metal material or the like and into the catalyst fixed layer 6 due to the pressure difference between the inner and outer walls. In the catalyst fixed layer 6, the liquid heavy hydrocarbon having a long-chain molecular structure reacts with hydrogen by a catalytic reaction to be decomposed into a short-chain liquid hydrocarbon. At the same time, the hydrogen gas that enters and flows into the catalyst fixed layer 6 contributes to the cooling of the catalyst reaction heat.

As described above, the liquid heavy hydrocarbon hydrocracking device according to the present invention uses the hydrogen gas of the conventional cracking device without using a diffuser such as a nozzle, and a porous gas vertically positioned in the flow of the liquid heavy hydrocarbon. Metal material or MF, UF
Through the contact surface of the metal film material up to the size, it is characterized by having a group of ultra-fine bubbles that do not mediate large bubbles or a hydrogen gas intrusion mechanism at a molecular diffusion level. Furthermore, the flow rate of the liquid heavy hydrocarbons in the fixed catalyst layer is free from problems such as channeling (short-circuit flow flowing in the direction of smaller fluid resistance) in the conventional gas-liquid solid contact.
Since the flow velocity in the fixed catalyst layer becomes more uniform and can be controlled to a turbulent flow region, further diffusion is promoted. Also, a porous metal or UF that plays the role of this hydrogen gas intrusion mechanism
The contact surface of the metal film material up to the size also has the function of heat exchange for extracting reaction heat.

In the above embodiment, the hydrogen gas is infiltrated into the catalyst fixed layer 6 provided outside the tube 2 from the inside of the hydrogen gas-permeable tube 2. On the contrary, as shown in FIG. A catalyst fixed layer 6a is provided in a hydrogen ventilation tube 2a whose upper and lower ends are supported by a tube sheet 3a, and a liquid heavy hydrocarbon mixed with a liquid heavy hydrocarbon or hydrogen gas is flowed into the catalyst fixed layer 6a. Hydrogen gas may be allowed to enter the catalyst fixed layer 6a from outside the tube 2a to cause a catalytic reaction between the liquid heavy hydrocarbon and the hydrogen gas. That is, a plurality of bundles of the hydrogen ventilation tube 2a in which the catalyst fixing layer 6a is disposed inside the pressure vessel 1a and the liquid heavy hydrocarbon is supplied together with the hydrogen gas, and the bundle of the hydrogen ventilation tube 2a are vertically arranged in plural numbers. Support plate 4 divided into steps
a, the support plates 4a are alternately shifted left and right, one end of the support plate 4a is separated from the inner wall of the pressure vessel 1a, and the other end is brought into contact with the inner wall of the pressure vessel 1a to form a hydrogen gas flow path. I have. Note that a liquid heavy hydrocarbon inlet nozzle 9a is provided at the top of the pressure vessel 1a, and a purified liquid hydrocarbon outlet nozzle 10a is provided at the bottom. Further, a hydrogen gas outlet nozzle 11a is provided on the upper side of the pressure vessel 1a, and a hydrogen gas inlet nozzle 12a is provided on the lower side.

[0025]

Since the present invention is configured as described above, the following effects can be obtained. (A) The hydrogen gas supply space A for cooling the catalytic reaction heat provided in the conventional apparatus is unnecessary. (B) Since the flow rate of the liquid heavy hydrocarbon in the catalyst is significantly higher than that of the conventional apparatus, it is possible to form a turbulent state, and the contact between the catalyst particles and the liquid heavy hydrocarbon and hydrogen gas is good. Therefore, the catalytic reaction is promoted and the amount of the catalyst can be reduced. (C) Due to the above (a) and (b), the apparatus becomes extremely compact as compared with the conventional apparatus, and the manufacturing cost can be reduced. (D) The yield is significantly higher than that of a conventional apparatus capable of increasing the supply amount of liquid heavy hydrocarbons.

[Brief description of the drawings]

FIG. 1 is a conceptual diagram of a liquid heavy hydrocarbon hydrocracking apparatus according to an embodiment of the present invention.

FIG. 2 is a conceptual view of a liquid heavy hydrocarbon hydrocracking apparatus according to another embodiment of the present invention.

FIG. 3 is a conceptual diagram of a conventional liquid heavy hydrocarbon hydrocracking apparatus.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1, 1a Pressure vessel 2, 2a Hydrogen ventilation tube 3, 3a Tube sheet 4 Catalyst layer support plate 4a Support plate 5 Solid-liquid separation plate 6, 6a, 23 Catalyst fixed layer 7 Liquid heavy hydrocarbon channel 8 Hydrogen gas channel 9, 9a , 21 Liquid heavy hydrocarbon inlet nozzle 10, 10a, 25 Refined liquid hydrocarbon outlet nozzle 11, 11a Hydrogen gas outlet nozzle 12, 12a, 26 Hydrogen gas inlet nozzle 13 Catalyst supply device 14 Catalyst removal nozzle 22 Distributor 24 Refined oil collector

Continuing on the front page (72) Inventor Shuzo Matsumura 8,4 Aichi Wai, Gloucester Walk, 38 A London, UK (72) Inventor Shoji Yoneda 1-1 Nikko-cho, Fuchu-shi, Tokyo Inside Japan Steel Works, Ltd. (72) Inventor Rokuro Denda 1-1 Nikko-cho, Fuchu-shi, Tokyo Inside Japan Steel Works, Ltd.

Claims (9)

[Claims] 1. A liquid heavy hydrocarbon is supplied to a catalyst fixed layer (6) disposed outside a plurality of hydrogen ventilation tubes (2), and hydrogen gas infiltrates from inside the hydrogen ventilation tubes (2). And causing a catalytic reaction between the liquid heavy hydrocarbon and hydrogen gas and cooling the heat of the catalytic reaction. 2. A liquid heavy hydrocarbon is supplied to a catalyst fixed layer (6a) disposed inside a plurality of hydrogen ventilation tubes (2a), and hydrogen gas is supplied from the outside of the hydrogen ventilation tubes (2a). A method for hydrocracking liquid heavy hydrocarbons, which comprises causing the liquid heavy hydrocarbons to undergo a catalytic reaction with the hydrogen gas by infiltration and cooling the heat of the catalytic reaction. 3. The liquid heavy hydrocarbon hydrocracking method according to claim 1, wherein a liquid heavy hydrocarbon mixed with hydrogen gas is supplied instead of the liquid heavy hydrocarbon. 4. A bundle of a hydrogen ventilation tube (2) in which a catalyst fixed layer (6) is disposed outside and a hydrogen gas is supplied inside, and a hydrogen ventilation tube (2) is provided inside the pressure vessel (1). ), A catalyst layer support plate (4) for vertically dividing the bundle into a plurality of stages, and solid-liquid separation plates (5) provided on both sides of the catalyst layer support plate (4). The layer support plate (4) is alternately shifted left and right, one end of which is in contact with the solid-liquid separation plate (5), and the other end of which is in contact with the inner wall of the pressure vessel (1). A liquid heavy hydrocarbon hydrocracking apparatus characterized in that: 5. The liquid carbonized carbonization according to claim 4, wherein the hydrogen-permeable tube is made of a porous metal material or a metal film material having pores of sizes up to MF and UF. Hydrogen hydrocracker. 6. The catalyst layer support plate (4) is a punch plate having a large number of holes of a size that cannot pass through a flat or spherical catalyst particle or a cylindrical particle. 6. The liquid heavy hydrocarbon hydrocracking apparatus according to 5. 7. The liquid weight according to claim 4, wherein the solid-liquid separation plate (5) is a punch plate having a large number of holes through which catalyst particles cannot pass. Hydrocarbon cracker. 8. A bundle of a hydrogen permeable tube (2a) in which a catalyst fixed layer (6a) is disposed inside and a liquid heavy hydrocarbon is supplied inside the pressure vessel (1a); And a support plate (4a) that vertically divides the bundle into a plurality of stages. The support plates (4a) are alternately shifted left and right, one end of which is separated from the inner wall of the pressure vessel (1a). A liquid heavy hydrocarbon hydrocracking apparatus characterized in that an end is brought into contact with an inner wall of a pressure vessel (1a) to form a hydrogen gas flow path. 9. The liquid heavy hydrocarbon hydrogenation according to claim 1, wherein a liquid heavy hydrocarbon mixed with hydrogen gas is supplied instead of the liquid heavy hydrocarbon. Disassembly device.