JPS5851980B2 - Method for producing light oil and cracked gas from coal and heavy oil - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention provides an improved fluidized bed and spouted bed in a fluidization vessel to process heavy liquid hydrocarbons such as coal and heavy liquid hydrocarbons, such as heavy oil, residual oil, and crude oil. The present invention relates to a method for producing light liquid hydrocarbons (light oil) and cracked gas from oil.

More specifically, this invention uses a fluidization vessel in which solid particles are fluidized, the upper part of which is a coking chamber and the lower part of which is a gasification chamber, and a spouted bed is formed in the coking chamber and a fluidized bed is formed in the gasification chamber. The mixture of coal and heavy oil and steam are supplied to the upper coking chamber, and the mixture of coal and heavy oil is ejected from the lower gasification chamber. Utilizing the sensible heat of Oil and cracked gas are obtained, coke is supplied to the lower gasification chamber together with solid particles, and water vapor, oxygen and liquid hydrocarbons are further supplied to the gasification chamber to exceed the softening point of the ash of 1050 to 1400°C. The resulting high-temperature cracked gas is effectively used to thermally reform the mixture of coal and heavy oil to convert light oil and cracked gas from coal and heavy oil. It relates to a manufacturing method.

Conventionally, methods for producing fuel gas or light oil from coal or a mixture of coal and heavy oil using a fluidization vessel in which solid particles are fluidized are known.

For example, in Japanese Patent Application Laid-Open No. 51-5303, pulverized coal is blown into a high-temperature air stream at the upper part of a fluidized bed reactor together with a gasifying agent of air and steam, and the pulverized coal is suspended in the air stream. A method of gasification at a high temperature of 1100° C. is described.

However, since this method blows pulverized coal into the airflow, it is necessary to complete the gasification in a short time, and it requires high temperatures.Also, since gasification is performed at high temperatures, clinker problems are likely to occur due to the ash produced. Furthermore, since air is used as a gasification agent, nitrogen is contained in the generated gas, which leads to a decrease in calories as a fuel gas.

For example, in Japanese Patent Application Laid-open No. 51-20903, coal and heavy oil are mixed to form a slurry, and this is
After heat treatment at a temperature of 50 ° C., fed into a fluidized bed reactor,
The reactor is heated from the outside to 480-600°C to decompose and convert the mixture of coal and heavy oil, and the solid particles in the bed (60
A method is described in which impurities are fixed in a mesh size of ~100 mesh) and a liquid product is obtained from the gaseous product produced.

However, since this method uses a fluidized bed reactor with a flat perforated plate, the movement of the solid particles is slow, which not only causes the solid particles to stagnate or agglomerate on the walls. Pretreatment is required to reduce the caking properties of coal, and pretreatment equipment for a mixture of coal and heavy oil is required.

In addition, in this method, the heat required for cracking and conversion is supplied by external heating, which not only has poor thermal efficiency, but also has disadvantages such as the fact that the coke, carbon, etc. produced in the fluidized bed reactor are not effectively used. be.

The present invention relates to a method for producing light oil and cracked gas useful as fuel gas, synthesis gas, etc. from coal and heavy oil, which have improved the above-mentioned drawbacks.

This invention has a solid particle inlet and a solid particle outlet, a gas outlet at the top, an inverted conical perforated plate at the bottom, and a perforated plate approximately at the center of the lower part of the perforated plate. The gasification chamber, which has a gas jet nozzle and a liquid hydrocarbon spray nozzle approximately in the center of the gas jet nozzle, is filled with solid particles and porous particles with coke attached to them, which will be described later, from the solid particle supply port. Water vapor and oxygen are supplied through the plate, and liquid hydrocarbon is supplied from the liquid hydrocarbon spray nozzle, and the water vapor is spouted from the gas jet flow nozzle at a flow rate faster than the gas flow velocity of the water vapor and oxygen supplied through the perforated plate to form solid particles. In addition to fluidizing 105
At a temperature of 0 to 1400°C, which does not exceed the softening point of the ash, the liquid hydrocarbons and the coke attached to the solid particles are combusted and gasified and decomposed, and the generated ash is discharged from the system through the solid particle outlet along with the solid particles. The generated high-temperature decomposition gas, together with accompanying solid particles, is discharged from the gas outlet through the gas outlet, which has a solid particle supply pipe, a solid particle discharge pipe, a raw material supply pipe with a nozzle, and a gas discharge pipe. A perforated plate in the shape of an inverted cone is installed in the coking chamber, and a connecting pipe is provided in the center of the perforated plate that communicates vertically with the gas outlet at the top of the gasification chamber. A mixture of coal and heavy liquid hydrocarbons (heavy oil) is supplied to the coking chamber from steam and raw material supply pipes through the plates, forming a spouted bed of solid particles in the coking chamber. The mixture with hydrocarbons is reformed at a temperature of 400 to 700°C using the sensible heat of the high temperature cracked gas and solid particles ejected through the connecting pipe,
Gaseous substances are generated and coke is attached to solid particles, and the solid particles with coke attached are supplied to the gasification chamber from the solid particle supply port of the gasification chamber through the solid particle discharge pipe, and the gaseous substances are relates to a method for producing light oil and cracked gas from coal and heavy oil, which is characterized by discharging this from a gas discharge pipe and separating it into cracked gas and light liquid hydrocarbon (light oil). be.

According to the method of the present invention, a spouted bed and a fluidized bed suitable for thermal reforming of coal and heavy liquid hydrocarbons and combustion gasification of coke can be formed in a fluidization vessel. From quality liquid hydrocarbons, mainly hydrogen,
It is possible to efficiently produce cracked gas containing methane, carbon monoxide, etc., and lightened liquid hydrocarbons having a boiling point of about 400° C. or less and containing no heavy metals or residual carbon.

Examples of heavy liquid hydrocarbons (hereinafter abbreviated as heavy oil) used as raw materials in this invention include crude oil, heavy oil,
Examples include residual oil and by-product oil resulting from thermal decomposition of residual oil.

Further, any type of coal such as lignite, copper coal, bituminous coal, etc. can be used, but it is preferable to use coal that has been pulverized as finely as possible.

The ratio of coal and heavy oil used is not particularly limited, but a ratio of about 2 parts by weight of heavy oil to 1 part by weight of coal is suitable, and the coal and heavy oil are mixed and used in the coking room. It is best to spray with water vapor from the bottom.

The mixture of coal and heavy oil may be supplied to the coking chamber after being heat-treated in advance, or may be supplied without being heat-treated.

In the method of this invention, even if caking coal is used and supplied without heat treatment, solid particles will agglomerate together in the coking chamber, in other words, in the spouted bed, and coke will be deposited on the coking chamber walls and perforated plates. No problems will occur due to adhesion.

The first feature of this invention is that it is suitable for producing light liquid hydrocarbons (in this specification, liquid hydrocarbons with a boiling point of about 400°C or less, hereinafter abbreviated as light oil) and cracked gas from coal and heavy oil. , a fluidization vessel consisting of a coking chamber in the upper part and a gasification chamber in the lower part, the middle part of which is connected by a vertical connecting pipe, is used to form an improved spouted bed in the coking chamber, and the coal in the spouted bed is and thermal reforming, such as vaporization of volatile components in heavy oil, decomposition of vaporized residue to produce light oil, and carbonization, mainly on the surface of solid particles, and generation of coke on the surface of solid particles. This is to fix carbon, heavy metals, sulfur, etc. together with coke using solid particles.

In addition, in this specification, coke is mainly included, and carbon, heavy metals,
Cokes that contain sulfur and other substances are called cokes.

A second feature of the present invention is that an improved fluidized bed is formed in the gasification chamber at the bottom of the coking chamber, and liquid hydrocarbons and coke generated in the spouted bed are transferred to the ash softening point. The combustion gasification and decomposition are carried out at a temperature not exceeding 100 mL, and the generated heat is directly used for thermal reforming of coal and heavy oil in the coking chamber.

Next, other features of the present invention will be explained with reference to the schematic sectional view of the fluidization vessel shown in FIG. 1, which is suitable for carrying out the method of the present invention.

In FIG. 1, the fluidization container 1 consists of a cylindrical coking chamber 1a and a gasification chamber 1b.The coking chamber 1a and the gasification chamber 1b are connected through a short vertical connecting pipe 1c and are integral It becomes.

The caulking chamber 1a has an enlarged part with a large cross-sectional area at the top, and a gas discharge port 2 and a gas discharge pipe 3 are provided at the top, and an inverted conical perforated plate 4 and an auxiliary gas supply pipe 20 are provided at the bottom. A connecting pipe 1c is provided in the center of the plate 4 and communicates vertically with the gas outlet 9 at the top of the gasification chamber 1b.
A raw material supply pipe 6 having a nozzle 5 is provided on the inclined part of the perforated plate 4.
is provided.

Further, the coking chamber 1a has a solid particle discharge pipe 7 and a solid particle supply pipe 8, and the solid particle discharge pipe 7 is connected via a valve 19 to a solid particle supply port 11 of the gasification chamber 1b.

The inner diameter t of the connecting pipe 1c is preferably 1/2 to 1/10, preferably 1/3 to 1/6, of the inner diameter t2 of the caulking chamber 1a.

The gasification chamber 1b has a gas discharge port 9 at the top, an inverted conical perforated plate 10 at the bottom, and a solid particle supply port 11 at the wall.
A gas jet flow outlet 12 is provided in the lower central part of the perforated plate 10 through the perforated plate 10, and a solid particle outlet 13 is provided in the inclined part of the perforated plate 10. A liquid hydrocarbon spray port 14 is provided approximately at the center of the outlet 12 .

Further, in the lower part of the gasification chamber 1b, a fluidizing gas supply pipe 15,
gas jet flow supply pipe 16, liquid hydrocarbon supply pipe 17,
A solid particle extraction pipe 18 and the like are provided.

The fluidization vessel 1 is filled with solid particles, and the solid particles are supplied into the fluidization vessel 1 from a hopper (not shown) through a solid particle supply pipe 8.

In this invention, when high-temperature decomposition gas and solid particles entrained in the decomposition gas, which will be described later, are ejected from the connecting pipe 1c in the center of the perforated plate 4 into the coking chamber 1a, the coking chamber 1a
A spouted bed is formed in the coking chamber a, and when a small amount of water vapor guided from the auxiliary gas supply pipe 20 is supplied through the perforated plate 4, the immobile part of the solid particles at the bottom of the spouted bed in the coking chamber a is eliminated, and the solid particles are separated from each other. Coal and heavy oil supplied from the raw material supply pipe 6 and nozzle 5 can be dispersed well, and adhesion and precipitation of coke on the wall of the coking chamber 1a can be prevented.

Furthermore, when a small amount of steam is supplied through the perforated plate 4 to the coking chamber 1a in which the spouted layer is formed, the coking chamber 1a
A columnar jet is formed in the center of a where solid particles are blown up at a higher speed than the surrounding area, the surrounding solid particles are engulfed by the jet, and the solid particles are scattered radially upward, forming a moving layer. While descending, solid particles near the interface between the jet and the moving layer flow into the jet, and other solid particles gradually flow along the inverted conical perforated plate 4. The solid particles move close to the connecting pipe 1c and are blown upward again, forming an improved spouted bed S accompanied by a circulating flow of solid particles in the coking chamber a.

The raw material supply pipe 6 having the nozzle 5 for supplying coal and heavy oil to the coking chamber 1a may be provided on the wall of the coking chamber 1a, but it is preferable to provide it through the inclined part of the perforated plate 4. Good.

At that time, a steam supply pipe (not shown) having a spout is provided in the inclined part of the perforated plate 4 so that steam can be spouted from around the nozzle 5 into the caulking chamber a. A raw material supply pipe 6 having a nozzle 5 is preferably provided.

Coal and heavy oil are passed through the nozzle 5 of the raw material supply pipe 6 together with steam to the improved spouted bed S in the coking chamber 1a.
In this case, it is preferable to spray toward the spout part of the spouted bed S.

The coal and heavy oil sprayed into the spouted bed S are sprayed onto solid particles, the heavy oil acts as a binder and mostly adheres to the solid particles, and is then spouted from the connecting pipe 1c for high-temperature decomposition. The sensible heat of the solid particles entrained in the gas and cracked gas is used to thermally reform at temperatures of 400 to 700°C.

Thermal modification mainly takes place on the surface of solid particles.

The solid particles adhering to coal and heavy oil are drawn into the jet section and rise as described above, and are scattered radially upward, forming a circulating flow that descends while forming a moving layer.

In the jet section, volatile acids in coal and heavy oil are mainly vaporized and the vaporized residue is thermally decomposed to become light oil, while in the moving bed section, carbonization proceeds.

Gaseous substances and coke are generated by thermally reforming coal and heavy oil in the coking chamber 1a.

The gaseous substances mainly include the above-mentioned volatile acids, liquid hydrocarbons resulting from light oil conversion, and cracked gas ejected from the connecting pipe 1c, and also contain minute amounts of carbon, coke, heavy oil, etc. ing.

Most of the coke is attached to solid particles.

The gaseous substances are led from the gas outlet 2 to the gas exhaust pipe 3, and if necessary, they are passed through a cyclone (not shown) to collect carbon, coke, etc. entrained in the gaseous substances, and are cooled and turned into light substances. Separates into liquid hydrocarbon and cracked gas.

On the other hand, the solid particles with coke attached are removed from the solid particle discharge pipe 7.
The solid particles are then guided to the solid particle supply port 11 of the gasification chamber 1b by controlling the supply amount with the valve 19, and are supplied to the gasification chamber 1b.

In addition, water vapor and oxygen are introduced as fluidizing gas from the fluidizing gas supply pipe 15 of the gasification chamber 1b, and are fed to the porous plate 1.
0 to the gasification chamber 1b, and a mixture of liquid hydrocarbons or carbon and coke separated and recovered from the gaseous matter generated in the coking chamber 1a is introduced from the liquid hydrocarbon supply pipe 17, When the liquid hydrocarbon is sprayed into the gasification chamber 1b from the spray port 14 and water vapor is ejected from the gas jet flow port 12 at a linear flow velocity higher than that of the fluidizing gas supplied from the perforated plate 10, the gasification chamber 1
In b, an improved fluidized bed F of solid particles is formed in which the solid particles are forced to circulate by convection.

In the gasification chamber 1b, the liquid hydrocarbons from the liquid hydrocarbon spray nozzle 14 are partially combusted at a temperature of 1,050 to 1,400°C, which does not exceed the softening point of the ash, and are mixed with the coke and liquid hydrocarbons that have adhered to solid particles. The carbon, coke, etc. that are produced are combusted and gasified to decompose them.

When the fluidized bed F in the gasification chamber 1b is maintained at a temperature of 1050 to 1400°C, which does not exceed the softening point of ash, the coke becomes ash and remains attached to the surface of the solid particles.

The solid particles to which the ash has adhered are removed from the solid particle outlet 1 using a known method.
3 to the outside of the system through the solid particle extraction pipe 18.

The solid particle outlet 13 may be attached to the wall of the gasification chamber 1b, or may be attached to the inclined portion of the perforated plate 10 as shown in FIG.

The softening point of ash is generally 1,100 to 1,500°C, but it varies depending on the type of raw material coal used and cannot be determined generally, so for example, if the softening point of ash is 13
In the case of coal at 00°C, it is better to keep the fluidized bed at a temperature lower than 1300°C.

When the temperature of the fluidized bed F is lower than 1050'C, combustion gasification of carbon, coke, etc. will not be sufficient.

The heat generated in the fluidized bed F of the gasification chamber 1b turns into high-temperature cracked gas, which is ejected and supplied from the gas outlet 9 through the connecting pipe 1c to the coking chamber 1a, where it is used for thermal reformation of coal and heavy oil. It is effectively used for quality.

The cracked gas entrains some solid particles, and the sensible heat of the entrained solid particles is also effectively utilized in the coking chamber 1a.

The cracked gas generated in the gasification chamber 1b mainly contains hydrogen,
Contains carbon dioxide gas, carbon monoxide, etc.

The solid particles used in the method of this invention may be of any kind as long as they are fire resistant and have excellent mechanical strength.
Generally, inorganic oxides are preferred, especially alumina.
Silica-based mullite particles are preferred.

The particle size of the solid particles is preferably 1.4 to 5 mm, and it is preferable to use particles that are as uniform in size as possible.

In carrying out the method of the present invention, oxygen supplied to the gasification chamber 1b through the perforated plate 10 is a mixture of liquid hydrocarbons supplied from the liquid hydrocarbon spray port 14, or a mixture of liquid hydrocarbons and carbon and coke. The amount may be sufficient to burn and gasify and decompose the coke on the surface of the solid particles at a temperature of 1050 to 1400°C, which does not exceed the softening point of ash, and the amount depends on the nature of the liquid hydrocarbon to be supplied, the decomposition temperature, Although it cannot be determined unconditionally as it varies depending on the adhesion ratio and amount of coke on solid particles from the coking chamber 1a and various other conditions, it is generally 3 to 8 parts by weight per 1 part by weight of liquid hydrocarbon. The proportion of

The liquid hydrocarbon supplied from the liquid hydrocarbon spray port 14 may be heavy liquid hydrocarbon such as crude oil, heavy oil, residual oil, etc.
It may be a lightened liquid hydrocarbon obtained by the method of the present invention, and there is no particular restriction on the type of liquid hydrocarbon.

Steam is supplied to the gasification chamber 1b from the perforated plate 10, the gas jet flow outlet 12, and the liquid hydrocarbon spray nozzle 14, but the total amount of water vapor supplied is sufficient to fluidize the solid particles in the gasification chamber 1b. It is acceptable as long as the amount is sufficient to carry out the water gas reaction, and the amount cannot be determined unconditionally because it varies depending on the type and amount of solid particles used, the type and amount of liquid hydrocarbon, the amount of coke, etc. I can't, but
Generally, it is appropriate to supply it at a ratio of 2 to 6 parts by weight per 1 part by weight of the liquid hydrocarbon.

However, if the fluidization start speed of solid particles is Umf-1 (m/sec), the gasification chamber 1b
The superficial column equivalent flow rate of all the gases (calculated based on the temperature and pressure of the gasification chamber 1b) Uo 1 (77Z/sec)
It is preferable that Umf-1 be in the range of 1.3 to 6 times.

Linear flow velocity U J −t (m/se
c) (Calculated based on the pressure and temperature at the time of jet supply) should be faster than the linear flow velocity of the gas at the outlet of the perforated plate 10 for water vapor and oxygen supplied through the perforated plate 10, and generally the above Uo 1. It is appropriate to set the amount in the range of ~10 times as much, and the supply amount is preferably in the range of 10 to 30 Vo/% of the total gas supplied to the gasification chamber 1b.

Further, the spread angle of the perforated plate 10 is suitably 60 to 130 degrees.

When the gasification chamber 1b is maintained under the above conditions, the gasification chamber 1b
A good fluidized bed F in which solid particles are forced to circulate is formed, and the coke is transferred to the combustion gas along with liquid hydrocarbons without causing stagnation of solid particles or agglomeration due to adhesion and agglomeration of solid particles. can be made into

High temperature decomposition gas (approximately 1050 ~
14,000G) mainly contains hydrogen, carbon monoxide, carbon dioxide, etc., and this high-temperature decomposed gas, along with some solid particles, passes from the gas outlet 9 through the connecting pipe 1C and is sent to the coking chamber. It erupts into 1a.

The linear flow velocity Uj -2 (m/sec) of this jet stream at the outlet of the connecting pipe 1c (calculated based on the temperature and pressure at the time of jetting) is determined by the amount of decomposed gas from the gasification chamber 1b and the flow rate of the connecting pipe 1c. It varies depending on the pipe diameter, etc., but if the terminal velocity of solid particles is Ut (=/sec), it is 1.4~
It is best to adjust to a range of 4 times.

The water vapor supplied to the coking chamber 1a through the perforated plate 4 is important for forming an improved spouted layer S in the coking chamber 1a, and its supply amount (Ntr?/se
c) is preferably set to 0.05 to 0.3 times the amount of high temperature decomposed gas (Ntl/sec) ejected from the connecting pipe 1c.

In addition, the superficial column equivalent flow rate U of all gases in the coking chamber 1a
o 2 (m/see) (calculated based on the temperature and pressure of the coking chamber 1a) is the minimum spouting velocity of solid particles that can form a spouted bed, as Um s (m/5ec
), the fluidization start speed of solid particles in the coking chamber 1a is U
If m f-2 (m/sec), then 1. I
It is appropriate to maintain the range of X Ums<Uo-2<4×Umf-2 in order to form a good spouted bed.

The spread angle of the perforated plate 4 in the caulking chamber 1a is 60 to 1
30° is good.

The temperature of the coking chamber 1a is preferably maintained within the temperature range of 400 to 700°C; if it is lower than 400°C, the thermal reformation of coal and heavy oil will not be sufficient, and the carbonization of heavy oil will occur. The above temperature range is suitable because the process does not proceed sufficiently and agglomeration of solid particles tends to occur, and when the temperature is higher than 700°C, the amount of light liquid hydrocarbons in the gaseous substance decreases.

In the coking chamber 1a, the heat generated in the gasification chamber 1b is not only effectively used for thermal reforming, but also the carbon, fine ash, and other impurities that were not combusted and gasified in the gasification chamber 1b are used to remove heavy oil. is attached to solid particles as a binder, so they can be collected.

In addition, the coke produced in the coking chamber 1a by carbonization of coal and heavy oil, in other words by thermal reforming, is porous, which is suitable for combustion or water gasification reaction in the gasification chamber 1b. ing.

Next, examples will be shown.

Example 1 The height from the gas jet flow outlet 12 to the gas outlet 9 of the gasification chamber 1b is 25001W7fi, the inner diameter of the gasification chamber 1b is 150111111, the spread angle of the perforated plate 10 of the gasification chamber 1b is 90', and the coking chamber 1a The length of the connecting pipe 1c is ioomm and the inner diameter of the pipe is 48 mm, the height from the connecting pipe 1c to the gas outlet 2 of the caulking chamber 1a is 2500 mm,
Inner diameter of caulking chamber 1a 180 mm and caulking chamber 1
Australian coal (volatile content 31.1%, fixed carbon 50 ．．
7%, ash content 14.3%) and pyrolysis by-product oil of Minas residue oil [viscosity 11 centibois (at 100°C), specific gravity d
'45:1.12) and produced light oil and cracked gas.

A 300°C mixture of the coal and pyrolysis by-product oil (
The ratio of 2 parts by weight of pyrolysis by-product oil to 1 part by weight of coal) is 53.4! 9/h, 5.3 kg/hr of 300°C water vapor from around the nozzle 5, 300°C from the perforated plate 4.
4.8 kg/hr of water vapor at 300°C passes through the perforated plate 10 of the gasification chamber 1b, and 13.5 kg/hr of water vapor at 300°C and 15.54 Ni/hr of oxygen pass through the perforated plate 10 of the gasification chamber 1b.2. 9 kg/hr and 0.5 kg/hr of water vapor at 300°C from the liquid hydrocarbon spray nozzle.
4.8 liquid hydrocarbons separated and recovered from the gaseous matter from the gas outlet 2 and the gas outlet pipe 3 along with hr
kg/hr to the fluidization container 1, and the coking chamber 1
186. Solid particles to which coke has adhered are discharged from the solid particle discharge pipe 7 of a. Take out Oky/hr and move it to gasification chamber 1b
The solid particles in the fluidization container 1 are circulated from the solid particle supply port 11 to the gasification chamber 1b, and the solid particles in the fluidization container 1 are fluidized and the coking chamber is
00°C and the gasification chamber at 1200°C, gaseous matter is taken out from the gas discharge pipe 3 of the coking chamber 1a, and the gaseous matter is cooled to produce light liquid hydrocarbons 32. OK
/hr and cracked gas 49.4 N1f/hr were obtained.

The composition of the resulting cracked gas is H2: 34.6 vo 1
%, CH4: 4.9vo1%, CO: 40.7v
o1%, CO2: 19.1 vo1%, other 0.7
At vo1%, the calorific value was 2634 Kcal/Nrr7'.

The calorific value of the obtained light liquid hydrocarbon was 9300
Kcal/g.

Note that 4.0 kg/h of ash, garbon, and other impurities adhering to the solid particles produced in the gasification chamber 1b were taken out of the system from the solid particle outlet 13 together with the solid particles.

In addition, new solid particles were supplied from the solid particle supply pipe 8 and adjusted so that 13 kg of solid particles were held in the coking chamber 1a and 11.5 ky of solid particles were held in the gasification chamber 1b.

The solid particles used had an average particle size of 3. It is a spherical mullite particle of Q my.

In addition, the linear flow velocity U J −2 (TL/se
c) is 46.6, the superficial column equivalent gas flow rate Uo-2 (m/sec) in the coking chamber 1a is 2.5, the superficial column equivalent gas flow rate Uo-1 (m/5ee) in the gasification chamber 1b
) is 5.1, and the linear flow velocity Uj-1 (rn/sec) of water vapor at the outlet of the gas jet flow outlet 12 is 12.
0, the fluidization start speed Umf-1 (m/sec) of solid particles in the gasification chamber 1c is 1.6, and the fluidization start speed Umf-2 (m/sec) of solid particles in the coking chamber 1a is
v'sec) is 1.7, the minimum jetting velocity U of solid particles
ms (m/sec) is 18 and Ut (m/sec
) was 31.0.

[Brief explanation of the drawing]

FIG. 1 is a schematic cross-sectional view of a fluidization vessel suitable for carrying out the method of the invention. 1...Fluidization container, 1a...Coking chamber, 1b...Gasification chamber, 1c...Connecting pipe, 2...Gas Discharge port, 3... Gas discharge pipe, 4... Perforated plate, 5... Nozzle, 6... Raw material supply pipe, 7...・Solid particle discharge pipe, 8...Solid particle supply pipe, 9...
・Gas outlet, 10...Perforated plate, 11...
...Solid particle supply port, 12...Gas jet flow outlet, 13...Solid particle outlet, 14...
... Liquid hydrocarbon spray port, 15 ... Fluidization gas supply pipe, 16 ... Gas jet flow supply pipe,
17...Liquid hydrocarbon supply pipe, 18...
・Solid particle extraction pipe, 19... Valve, 20...
...Auxiliary gas supply pipe.

Claims (1)

[Claims] 1. It has a solid particle supply port and a solid particle outlet, a gas discharge port is provided at the top, an inverted cone-shaped perforated plate is provided at the bottom, and a hole is inserted through the perforated plate approximately in the center of the lower part of the perforated plate. The solid particles with coke adhered to them are passed through the porous plate from the solid particle supply port into the gasification chamber, which is equipped with a gas jet nozzle and a liquid hydrocarbon spray nozzle approximately in the center of the gas jet nozzle. supplying water vapor and oxygen, and liquid hydrocarbons from a liquid hydrocarbon spray nozzle, respectively;
The solid particles are fluidized by ejecting water vapor at a linear flow velocity higher than the gas flow velocity of water vapor and oxygen supplied through the perforated plate from the gas jet flow outlet, and
At a temperature of 1400°C, which does not exceed the softening point of the ash, the liquid hydrocarbon and the coke attached to the solid particles are combusted and gasified and decomposed, and the generated ash is taken out of the system from the solid particle outlet along with the solid particles, The generated high-temperature decomposition gas, together with accompanying solid particles, is transported from the gas outlet to the bottom via a solid particle supply pipe, a solid particle discharge pipe, a raw material supply pipe with a nozzle, and a gas discharge pipe. A conical perforated plate is provided, and a connecting pipe is provided in the center of the perforated plate that communicates vertically with the gas outlet at the top of the gasification chamber. A mixture of coal and heavy liquid hydrocarbons is supplied to the coking chamber through the steam plate and the nozzle of the raw material supply pipe, respectively, to form a spouted bed of solid particles in the coking chamber, and the mixture of coal and heavy liquid hydrocarbons is The mixture is thermally reformed at a temperature of 400 to 700°C using the high-temperature decomposed gas and the sensible heat of the solid particles ejected through the connecting pipe to generate a gaseous substance and turn the coke into a solid. The solid particles that are generated and attached to the particles are supplied to the gasification chamber from the solid particle supply port of the gasification chamber through the solid particle discharge pipe, and the gaseous substances are discharged from the gas discharge pipe. A method for producing light oil and cracked gas from coal and heavy oil, which comprises separating cracked gas and light liquid hydrocarbon.