JPH08209155A - Process for gasifying hardly slurriable solid carbonaceous material by simultaneous gasification by dry-and wet-feed systems - Google Patents

Abstract

PURPOSE: To enhance cool gas efficiency to thereby improve gasification performance and safely perform gasification operation by gasifying a hardly slurriable solid carbonaceous material by wet feed system and simultaneously gasifying an easily slurriable solid carbonaceous material by wet-feed system in a process for gasifying a soild carbonaceous material by partially oxidizing it in the presence of oxygen. CONSTITUTION: A hardly slurriable solid carbonaceous material is fed to a dry grinder 1 to be ground therewith into fine particles and then fed through a lock hoppper feeder 2 to a gasification burner 12a. An easily slurriable solid carbonaceous material is fed to a wet grinder 4 to be ground therewith in the presence of water and fed to a gasification burner 12b. Simultaneously, pressurized oxygen as the gasification agent is fed through an oxygen feed line 8 to a gasification oven 9. The conditions of partial oxidation in the reaction chamber 10 are at a temp. of 1400-1450 deg.C, a pressure of 30-100kg/cm<2> , and for a dwelling time of 2-10sec. The resultant gas 13 is taken out through a take-out port 17.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gasification treatment method by partially oxidizing a solid carbonaceous raw material which is difficult to make into a slurry. More specifically, the present invention relates to a method for gasifying a solid carbonaceous raw material which is difficult to slurry, such as brown coal, plastic, and sludge, by simultaneous gasification of a dry feed method and a wet feed method.

[0002]

2. Description of the Related Art Conventionally, fixed bed, fluidized bed and jet bed processes have been used as a method for gasifying a solid carbonaceous raw material such as coal or petroleum coke using a gasifying agent such as an oxygen-containing gas. In either case, a slurry method, that is, a wet feed method, or a pressure lock hopper method, that is, a dry feed method is adopted as the method for supplying the solid carbonaceous material.

For example, as a gasification process by a wet feed system, a solid carbonaceous raw material such as coal or petroleum coke is wet pulverized to form a slurry, which is then supplied into a gasification furnace, and this is supplied as oxygen as a gasifying agent. Is a process in which a flammable gas containing carbon monoxide and hydrogen as main components is generated by partial oxidation by. The so-called Texaco method is widely used (Japanese Patent Laid-Open Nos. 54-15903 and 55-55).
65296, JP-A-56-16592, JP-A-58-80382, and JP-A-58-20838.
No. 6, JP-A-59-49415, etc.).
In the gasification treatment process by the wet feed method, the solid carbonaceous raw material is mixed with water to form a slurry state, and the raw material can be stably fed in that it can be easily fed into the gasification furnace by a pump. In addition, the gasification plant has significant advantages in terms of safety and the like.

By the way, as a method for effectively solving both the problem of the generation of harmful gas and the problem of generation of ash containing heavy metals, the method of gasification treatment of plastic wastes utilizing the above-mentioned Texaco method is the present inventor. Have already been proposed (see Japanese Patent Laid-Open No. 5-208183). In this method, a plastic waste / coal / water slurry containing 100 parts by weight of plastic waste pulverized into fine particles and 5 parts by weight or more of fine particle coal is introduced into a gasification furnace under pressure, The waste and the coal are heated to a temperature (preferably 1200 to 1) higher than the melting temperature of the ash in the coal.
Gasification of plastic waste, characterized in that it partially oxidizes at 500 ° C) to produce a flammable gas, and the metal components contained in the plastic waste are dissolved in the ash content of the coal and collected. It is a processing method.

However, solid carbonaceous raw materials such as this plastic, lignite, and sludge are difficult to be made into a high-concentration slurry with, for example, water, and in the general slurrying technique, the solid content concentration is at most 40% by weight or less. Only concentrated slurry. Therefore, when such a low-concentration slurry is gasified with a gasifying agent such as an oxygen-containing gas, the rate of oxidation reaction is high because the calorific value is low,
There is a problem that the required amount of the gasifying agent increases, and as a result, the cold gas efficiency (that is, the ratio of the total amount of carbon monoxide gas and hydrogen gas to the solid carbonaceous raw material) decreases.

Therefore, in the gasification treatment process of solid carbonaceous raw materials, such as brown coal, plastics, sludge, etc., which are difficult to be slurried, a dry feed method is desired as a method of supplying the solid carbonaceous raw materials. ing. According to the dry feed method, while the cold gas efficiency is high, in order to handle the solid raw material, it is necessary to use a pressure lock hopper method or an air lock feeder method,
There is a drawback that the raw material supply method lacks stability. Further, when a trouble of stopping the supply of raw material occurs, it is difficult to accurately catch it, so that a time delay occurs until the supply of oxygen as a gasifying agent is stopped,
There is still a problem in terms of safety, such as a very dangerous state in the gasification furnace in which oxygen is temporarily sent into the gasification furnace.

[0007]

SUMMARY OF THE INVENTION The present invention is directed to a problem of a decrease in cold gas efficiency due to the supply of a slurry of a solid carbonaceous raw material and water into a gasification furnace in a wet feed system, and a dry feed system. Of supplying solid carbonaceous raw material into the gasification furnace in Japan and problems such as lack of safety in the gasification furnace due to temporary introduction of gasifying agents such as oxygen when the supply of raw material is stopped It is an object of the present invention to provide a gasification treatment method for a difficult-to-slurry solid carbonaceous raw material by simultaneous gasification of a dry feed system and a wet feed system, which solves the above problem.

[0008]

Means for Solving the Problems In order to solve the above problems, the present inventors have conducted extensive studies on a gasification treatment method by partial oxidation of a solid carbonaceous raw material using the Texaco method, and as a result, gasification When supplying solid carbonaceous raw materials into the furnace, dry feed of difficult-to-slurry solid carbonaceous raw materials such as lignite, plastics and sludge and wet feed of easily slurried solid carbonaceous raw materials such as coal and petroleum coke are simultaneously performed. By doing so, it is possible to prevent a decrease in cold gas efficiency caused by the slurry supply of the solid carbonaceous raw material and water, which is a disadvantage of the wet feed system, and to eliminate the risk of lack of supply stability, which is a disadvantage of the dry feed system. Gas with high cold gas efficiency is obtained by dry feed gasification of solid slurry carbonaceous materials such as brown coal, plastic, sludge, etc. In addition to being able to effectively utilize brown coal, plastics, sludge, etc., the dry feed side that is continuously fed into the gasification furnace even when the feed of the solid carbonaceous raw material to be dry fed is stopped. Since the gasifying agent such as oxygen is consumed in the combustion of the solid carbonaceous raw material that is wet-fed, it is found that the gasifying agent such as oxygen does not remain in the generated gas and is safe, and the present invention is completed. Came to.

That is, according to the present invention, a solid carbonaceous raw material is simultaneously introduced into a gasification furnace by using both a dry feed system and a wet feed system, and the melting temperature of ash in the solid carbonaceous raw material is measured under a pressurized condition. It is characterized in that a combustible gas containing carbon monoxide and hydrogen is generated by partial oxidation at a high temperature, and it is difficult to form a slurry slurry solid carbon by simultaneous gasification of a dry feed system and a wet feed system. This can be achieved by providing a method for gasifying a raw material.

The method of the present invention will be described in detail below. In the method of the present invention, the solid carbonaceous raw material supplied into the gasification furnace together with the gasifying agent by the dry feed system is
After pulverization, when mixed with, for example, water to form a slurry, it is a solid carbonaceous raw material that is difficult to form a high-concentration slurry,
This is a low-concentration slurry having a solid content concentration of at most about 40% by weight. Examples of such an object to be treated include low-quality coal such as peat, lignite, and brown coal, plastics, and sludge. Examples of the above-mentioned plastics include a waste product of a plastic product that has been used for its original purpose and has been used up, or a plastic product that has been manufactured for the purpose of use but has become a defective product. Here, the plastic product is a thermoplastic resin or thermosetting resin described later, injection molding, extrusion molding, blow molding, transfer molding, various molding methods such as press molding, automobile interior and exterior parts, parts for railway vehicles, Ship and aircraft parts, electrical and electronic parts, civil engineering and construction materials, packaging containers, lighting equipment parts,
Precision and optical equipment parts, medical equipment parts, sports / leisure goods, daily sundries, other general equipment parts, etc. Therefore, there is no particular limitation on the plastic waste or the defective plastic product to be treated by the dry feed, and the waste or defective product containing any of the thermoplastic resin and the thermosetting resin as a main component, or those It may be a mixture of.

Specific examples of the molded article made of the above-mentioned thermoplastic resin are not particularly limited, and polyolefins such as polyethylene, polypropylene and modified polypropylene, vinyl chloride resins, and thermoplastic polyesters such as polyethylene terephthalate and polybutylene terephthalate. General-purpose engineering resin such as resin, polyamide, polycarbonate, polyoxymethylene, polyphenylene oxide, modified polyphenylene oxide, high-performance engineering resin such as polyphenylene sulfide, polysulfone, polyether sulfone, polystyrene, acrylonitrile-styrene copolymer, acrylonitrile-butadiene・ Styrene resin such as styrene copolymer, acrylic resin, methacrylic resin, polytetrafluoroethylene Fluorine resin such as emissions or, may include those obtained by molding by using a composite material of each of these resins (alloy containing). In addition, specific examples of the molded product made of the thermosetting resin are not particularly limited, and include phenol resin, melamine resin, urea resin, unsaturated polyester resin, urea resin, silicone resin, epoxy resin,
Examples include those molded using an alkyd resin or a composite material (including alloy) of each of these resins. Among these, waste or defective products of plastic products whose main chain is a hydrocarbon chain such as polyolefin, vinyl chloride resin, thermoplastic polyester resin, styrene resin, acrylic resin and methacrylic resin, or
A mixture of these plastic wastes or plastic wastes composed mainly of defective products is desirable.

The sludge, which is the object to be treated by the dry feed in the present invention, includes various industrial wastes and
Examples thereof include organic and inorganic sludge generated from wastewater, purified water, sewage, human waste, waste oil treatment, and the like, and sludge containing harmful substances. In particular, surplus sludge in the activated sludge treatment process can be preferably mentioned.

Next, in the method of the present invention, the solid carbonaceous raw material supplied into the gasification furnace together with the gasifying agent by the wet feed system is pulverized into fine particles,
For example, it is a solid carbonaceous raw material that is easily slurried by mixing with water or the like. Such solid carbonaceous raw materials include relatively high quality coal such as subbituminous coal, bituminous coal, anthracite, coal coke, carbonized coal, charcoal, petroleum coke, granular carbon medium, oil shale, tar sand and Preferable examples are solid carbonaceous raw materials such as pitch and mixtures thereof. Further, in the method of the present invention, as the solid carbon raw material, a semi-solid carbonaceous fuel such as asphalt, rubber and rubber tires of automobiles can be included. The coal coke is a strong, porous residue composed of carbon and mineral ash produced when the coal is heated in the coke oven in the absence of air. Carbonized coal is obtained by pyrolyzing coal in the presence or absence of air, hydrogen or syngas.
The granular carbon medium is obtained as a by-product during the production of the synthetic gas by the partial oxidation method of the solid carbonaceous raw material, and is contained in the flow of the outflow gas from the gasification furnace at about 0 to 20% by weight.
(Based on the weight of carbon in the solid carbon fuel). Pitch is also a black amorphous solid or semi-solid residue obtained from the distillation of tar and tar products.

In the wet feed in the method of the present invention, first, the above-mentioned slurryable solid carbonaceous raw material is pulverized to an appropriate size, then mixed with a liquid solvent as a slurrying agent, and pumped. It produces a deliverable slurry. As the liquid solvent, in addition to the above-mentioned water, liquefied petroleum gas, crude oil, atmospheric distillation residual oil, vacuum distillation residual oil, heavy distillate from crude oil, naphtha, kerosene, light oil, tar sand oil, shale oil, Extracted oil from coal, coal liquefied oil, aromatic hydrocarbons such as benzene, toluene and xylene fractions, liquid hydrocarbons such as hexane, heptane, cyclohexane, tetralin, decalin, coal tar and mixtures thereof, and liquid CO ₂ etc. Among these, in addition to the role as the above-mentioned transport medium, the role as a temperature relaxation agent in the production of a synthesis gas containing carbon monoxide and hydrogen by partial oxidation of the solid carbonaceous raw material and the water gas reaction Water can be most preferably used in consideration of its role as a hydrogen / carbon monoxide ratio adjusting agent in the synthesis gas, and its low price and availability.

By the way, in the method of the present invention, gasification which is fed into the gasification furnace together with the easily fed slurry-like solid carbonaceous raw material which is wet-fed or the hardly-slurried solid carbonaceous raw material which is dry-fed, respectively. Examples of the agent include oxygen-containing gas. This oxygen-containing gas is
It contains free oxygen gas, and partially oxidizes the easily slurried solid carbonaceous raw material and the hardly slurried solid carbonaceous raw material introduced into the gasification furnace together with the oxygen-containing gas, and mainly monoxide It functions as an oxidant for producing a combustible gas containing carbon and hydrogen, that is, a synthesis gas. Specifically, air, oxygen-enriched air, that is, air containing 21 mol% or more oxygen, and substantially pure oxygen gas, that is, oxygen gas having a concentration of 95 mol% or more (the rest is nitrogen gas). And a noble gas). Of these, substantially pure oxygen gas is preferred to reduce the amount of nitrogen and other gaseous impurities in the gas evolved from the gasifier.

Further, in the method of the present invention, the easily slurried solid carbonaceous raw material is introduced into the gasification furnace together with the gasifying agent, and at the same time, the hardly slurried solid carbonaceous raw material is gasified together with the gasifying agent. It is introduced into a furnace, and is partially oxidized at high temperature under pressure to be gasified to generate a synthesis gas mainly containing carbon monoxide and hydrogen. The temperature of combustion for the partial oxidation, that is, the gasification temperature should be at least higher than the melting temperature of the ash in the easily slurried solid carbonaceous raw material supplied into the gasification furnace, Although it varies depending on the type of the easily slurried solid carbonaceous raw material, coal such as subbituminous coal, bituminous coal and anthracite is preferably 1200 to 1500.
C., more preferably in the range of 1350 to 1450.degree. If the gasification temperature is lower than 1200 ° C., the ratio of carbon contained in the coal to be gasified decreases, and the ratio of unburned carbon in the gas generated from the gasification furnace increases. Since the melting of the ash contained in the coal is not sufficient, the metal components such as heavy metals contained in the dry-fed lignite, plastics, sludge and other difficult-to-slurry solid carbonaceous raw materials cannot be taken out from the gasifier, etc. Not preferable. Also, the gasification temperature is 1
Above 500 ° C, the gasification burner tip,
The life of the refractory bricks lined along the inner wall of the reaction chamber in the gasification furnace is shortened, and long-term stable operation of the gasification furnace cannot be performed, which is not preferable. The gasification temperature should be within the above-mentioned more preferable range in order to reliably suppress the occurrence of the above-mentioned unfavorable phenomena and maintain long-term stable operation of the gasification furnace.

On the other hand, the pressure of the reaction chamber in the gasification furnace, that is, the gasification pressure has little relation to the gasification reactivity of the solid carbonaceous raw material and is not particularly limited, but the economical efficiency of the equipment. Considering the above, usually 3 to 250 kg / cm
^It is desirable to be kept under a pressure of ² G, preferably 30 to 100 kg / cm ² G. That is, the gasification pressure is 3
If it is lower than kg / cm ² G, the gas volume becomes large, the apparatus becomes large, and the equipment cost becomes high, which is not preferable. Also, if the gasification pressure exceeds 250 kg / cm ² G, it will be difficult to seal the lock hopper feeder or air lock feeder installed in the dry feed line, and the gasification furnace and other incidental equipment will have high pressure resistance. Is required, and the thickness of these facilities becomes large, which results in high cost, which is not preferable.

Next, the gasification treatment method of the difficult-to-slurry solid carbonaceous raw material by the simultaneous gasification of the dry feed method and the wet feed method of the present invention (hereinafter, simply referred to as the “method of the present invention”) will be described. This will be described in detail with reference to the apparatus flow diagram shown in the accompanying drawing (FIG. 1) which is an embodiment. In the method of the present invention, the solidified carbonaceous raw material which is difficult to slurry is first supplied to the dry crushing apparatus 1 and subjected to dry crushing treatment to form fine particles. The degree of pulverization varies depending on the kind of the non-slurrying solid carbonaceous raw material, but at least the maximum particle size is 3 mm or less, and the average particle size is usually 10 to 5
The thickness is preferably 00 μm, preferably 20 to 100 μm. The maximum particle size exceeds 3 mm and the average particle size is 5
If it exceeds 00 μm, the lock hopper feeder 2 to be described later may be clogged at the discharge port or the gasification burner 12 may be clogged, and the solidified carbonaceous material difficult to slurry in the reaction chamber 10 of the gasification furnace 9 may be generated. The combustion of the raw material does not proceed to a desired degree, and the metal components such as heavy metals contained in the hardly-slurried solid carbonaceous raw material are not sufficiently scattered, which is not preferable. On the other hand, if the average particle size is less than 10 μm,
Not only the improvement of the crushing effect cannot be expected, but also the time required for the crushing process in the dry crushing apparatus 1 is too long, which is not preferable.
As the dry pulverizer, a ball mill, a rod mill, a roller mill, a stamp mill, a jet mill, a vibration mill, a cutter, a crusher, etc. are preferably used. When the above-mentioned plastics are used as the raw material for solidified carbonaceous slurry, it is particularly preferable to use a cutter, a crusher or the like as the dry crushing device.

The finely powdered solid carbonaceous raw material which is hardly slurried is then sent to the lock hopper feeder 2. Although not shown in FIG. 1, the transfer to the lock hopper feeder 2 is performed by a known method such as gravity transfer by a rotary feeder or transfer by a blower.
The lock hopper feeder 2 is composed of an upper hopper 21, an intermediate hopper 22, and a lower hopper 23, a connecting pipe connecting these hoppers, and lock hopper valves 24, 25 and 26 provided in the connecting pipe. There is. And at least two lock hopper feeders 2
A plurality of series or more are installed, and the plurality of series of lock hopper feeders 2 are appropriately switched and used, whereby the difficult-to-slurry solid carbonaceous raw material is introduced into the gasification furnace 9 through the gasification burner 12a. It is dry fed.

For example, in the lock hopper feeder 2, in the series in which the difficult-to-slurry solid carbonaceous raw material is not supplied to the gasification burner 12a, the upper hopper 21 and the intermediate hopper 22 are empty, and The lock hopper valves 24, 25 and 26 are all in the fully closed state. In addition, the lower hopper 23 may or may not be filled with the pulverized material of the solidified carbonaceous raw material that is difficult to slurry. In such a state, the fine pulverized non-slurrying solid carbonaceous raw material sent from the dry crushing device 1 is first filled in the upper hopper 21. After the completion of the filling of the predetermined amount, the supply line to the lock hopper feeder 2 is switched to a series different from the above one in which the difficult-to-slurry solid carbonaceous raw material is not supplied to the gasification burner 12a. The solidified carbonaceous raw material in the form of fine particles is filled in the upper hopper 21 of the same series. At the same time, the lock hopper valve 24 is fully opened, and the difficult-to-slurry solid carbonaceous raw material with which the upper hopper 21 is filled is transferred to the intermediate hopper 22. After the transfer is completed,
The lock hopper valve 24 is fully closed again and the pressurized gas such as nitrogen gas is introduced so that the intermediate hopper 22 is pressurized to almost the same pressure as the lower hopper 23.
Next, the lock hopper valve 25 is fully opened, and the fine particle-like non-slurry solid carbonaceous raw material in the intermediate hopper 22 is discharged to the lower hopper 23.
Then, after this payout is completed, the lock hopper valve 25 is fully closed again, the pressurized gas in the intermediate hopper 22 is released, and the intermediate hopper 22 becomes normal pressure. If the lower particulate hopper 23 has already been filled with the fine particulate difficult-to-slurry solid carbonaceous raw material, the fine-particle difficult-to-slurry solid carbonaceous raw material is gasified by the gasification burner 12a.
Is supplied to the lower hopper 23 and waits until the filling amount of the fine particulate difficult-to-slurry solid carbonaceous raw material in the lower hopper 23 becomes a predetermined level or less, from the intermediate hopper 22 of the fine-grain difficult-to-slurry solid carbonaceous raw material. The payout to the lower hopper 23 may be performed.

Meanwhile, during this period, the lock hopper feeder 2
In another series, the supply of the difficult-to-slurry solid carbonaceous raw material to the gasification burner 12a is performed as follows. That is, in this series, at least the lower hopper 2
No. 3 is filled with a particulate solidified non-slurry solid carbonaceous raw material and is pressurized to a predetermined pressure, and the lock hopper valves 25 and 26 are fully closed. In this state, the lock hopper valve 26 is fully opened,
The fine-particle-like difficult-to-slurry solid carbonaceous raw material is continuously supplied to the gasification burner 12a via the dry feed line 3 at a predetermined supply rate under a predetermined pressure in an edge-cutting state with the intermediate hopper 22. Here, the number of series of the lock hopper feeders 2 is the delivery flow rate of the particulate difficult-to-slurry solid carbonaceous raw material from the dry pulverizer 1 to the lock hopper feeder 2 and the particulate particles in the gasification burner 12a. Flow rate of the non-slurrying solid carbonaceous raw material, the upper hopper 21, the intermediate hopper 22, and the lower hopper 2
It may be appropriately determined in consideration of the capacity of 3 and the like. But,
Considering the complexity of the above-mentioned operation in the lock hopper feeder 2, it is preferable that the number is as small as possible.

By the way, in the present invention, the switching of the supply line of the particulate fine non-slurrying solid carbonaceous raw material from the dry crushing device 1 to the lock hopper feeder 2 as described above, the lock hopper valves 24, 25 and A series of operations such as opening and closing of 26 and pressurization of the intermediate hopper 22 and the lower hopper 23 are performed by sequence control, whereby the particulate fine refractory solid carbonaceous raw material is fed to the gasification burner 12a at a constant rate. Continuous supply at a flow rate is possible. In the method of the present invention,
The dry feed method by the pressure lock hopper method of the particulate difficult-to-slurry solid carbonaceous raw material is not limited to the method as described above, and the fine-particle difficult-to-slurry solid carbonaceous raw material is gasified. Any method may be used as long as continuous supply at a constant flow rate to the burner 12a is possible. Further, the pressure lock hopper method is not limited, and an air lock feeder method or the like may be adopted.

Next, in the method of the present invention, the easily slurried solid carbonaceous raw material is also pulverized first as in the case of the hardly slurried solid carbonaceous raw material. That is, the easily slurried solid carbonaceous material is supplied to the wet crushing device 4 and is wet crushed in the presence of water similarly supplied to the wet crushing device 4 to form the fine slurried solid carbonaceous material. A solid carbonaceous raw material / water slurry in which the raw materials are dispersed is obtained. The degree of wet pulverization varies depending on the kind of the easily slurried solid carbonaceous raw material, but fine particles having an average particle diameter of usually 20 to 80 μm, preferably 40 to 50 μm are preferable. When the average particle size exceeds 80 μm, the fine particle-like easily-solidified solid carbonaceous raw material is uniformly dispersed in water when the solid carbonaceous raw material / water slurry is stirred in the slurry tank 5 described later. Therefore, it becomes difficult to obtain a slurry having a uniform concentration, and in the wet feed line 7, wear or blockage occurs in the pump 6 or in the bent portion of the pipe, or in the gasification burner 12b. It is not preferable that something happens. If the average particle size is less than 20 μm, further improvement of the pulverizing effect cannot be expected, and it takes time for the pulverizing process in the wet pulverizer 4 to reduce productivity, which is not preferable. The wet pulverizer is not particularly limited, and any wet mill selected from wet mills such as ball mills, rod mills and pin mills used in the known Texaco method can be used.

In the present invention, the concentration (content) of the finely divided, easily slurried solid carbonaceous raw material in the solid carbonaceous raw material / water slurry discharged from the wet pulverizer 4 as described above is usually 50 to 50%. 70% by weight, preferably 60
It is desirable that the content be ˜65% by weight. If the concentration of the easily slurried solid carbonaceous raw material is lower than 50% by weight, during gasification with oxygen gas in the reaction chamber 10 of the gasification furnace 9,
The calorific value due to the combustion of the easily fed slurry-like solid carbonaceous material / water slurry that is wet-fed and the difficultly-slurried solid carbonaceous material that is dry-fed is low, so the rate of the oxidation reaction is high and the cold gas efficiency, that is, However, the yield of the total amount of carbon monoxide gas and hydrogen gas from the solid carbonaceous raw material becomes low, which is not preferable. On the other hand, when the concentration of the easily slurried solid carbonaceous raw material becomes higher than 70% by weight, the slurry becomes too viscous, and the fine particulate solid carbonaceous raw material is mixed with water by stirring the slurry in the slurry tank 5. It becomes difficult to disperse uniformly, so that a homogeneous slurry cannot be obtained, the slurry combustion in the reaction chamber 10 of the gasification furnace 9 becomes unstable, and the slurry in the slurry tank 5 or the wet feed line 7 is It is not preferable because a problem such as clogging due to sedimentation of the particulate solid carbonaceous raw material from the slurry occurs. If the concentration of the easily slurried solid carbonaceous raw material is in the range of 50 to 60% by weight or in the range of 65 to 70% by weight, the above-mentioned unfavorable phenomenon may occur.

The solid carbonaceous raw material / water slurry discharged from the wet pulverizer 4 is sent to the slurry tank 5 by a pump (not shown in FIG. 1) or the like. In the slurry tank 5, the slurry tank 5
The solid carbonaceous raw material / water slurry supplied to the inside is maintained in a stirring state by an appropriate stirring means, and the finely divided, easily slurried solid carbonaceous raw material is uniformly dispersed in water. Quality raw material and water slurry,
This prevents clogging of the slurry outlet of the slurry tank 5 due to the deposition of the fine particulate slurry-like solid carbonaceous material on the bottom of the tank. As the stirring means,
Known methods such as mechanical stirring with a stirrer and an external circulation method with a pump can be used. In the method of the present invention, it is also possible to dry-mill the solid carbonaceous raw material easily slurried using a dry mill as described above, and then mix it with water to obtain a solid carbonaceous raw material / water slurry. However, as an industrial operation, the above-mentioned wet pulverization method is advantageous.

A solid carbonaceous raw material / water slurry having a uniform concentration is extracted from a slurry outlet (not shown) of a slurry tank 5, pressurized by a pump 6, passed through a wet feed line 7, and gasified. It is introduced into the gasification burner 12b of the furnace 9 at a predetermined feed rate.

Further, in the present invention, introduction of the difficult-to-slurry solid carbonaceous raw material into the gasification burner 12a through the dry feed line 3 described above and the easily slurried solid carbonaceous raw material through the wet feed line 7 described above. Simultaneously with the introduction of the water slurry into the gasification burner 12b, a substantially pure oxygen gas (hereinafter abbreviated as "oxygen gas") pressurized to a predetermined pressure as a gasifying agent, that is, an oxidant, is supplied as an oxygen feed. It is introduced into each of the gasification burners 12a and 12b through the line 8 at a predetermined flow rate. Here, the supply amount of the oxygen gas is the amount of the generated gas obtained by the partial oxidation reaction of the difficult-to-slurry solid carbonaceous raw material and the easily-slurried solid carbonaceous raw material, which are supplied into the reaction chamber 10 of the gasification furnace 9, It should be selected so that the desired cold gas efficiency described below can be achieved. That is, with respect to the easily slurried solid carbonaceous raw material / water slurry that is wet-fed, the amount of oxygen required for complete combustion of the easily slurried solid carbonaceous raw material is usually 30 to 50%, preferably 40 to 45. It is desirable to be set to%. Further, with respect to the difficult-to-slurry solid carbonaceous raw material that is dry-fed, the amount of oxygen required for complete combustion of the easily-slurried solid carbonaceous raw material that is wet-fed is 5 to 20%, preferably 8 to 15%. It is desirable to be set to%. Further, the total supply amount of oxygen gas is generally 35 to 35, which is the amount of oxygen required for complete combustion of the easily slurried solid carbonaceous raw material supplied into the reaction chamber 10 of the gasification furnace 9 by the wet feed.
It is desired to be 55%, preferably 48 to 53%.

Further, in the present invention, by maintaining the supply amount of oxygen gas in the above range, troubles of the supply device such as the dry pulverization device 1 and the lock hopper feeder 2 may cause the solidified carbonaceous raw material which is difficult to slurry. When the supply is stopped, the oxygen gas is temporarily supplied at the same amount as it is, but the supply amount of the oxygen gas is, as described above, the wet-slurried solid carbonaceous raw material / water slurry. The amount of oxygen required for complete combustion of the easily slurried solid carbonaceous raw material in the gasification furnace 9
Oxygen does not remain in the gas generated from the product and the safety is ensured, which is one of the features of the method of the present invention. In this case, of the oxygen gas supplied, the amount for the difficult-to-slurry solid carbonaceous raw material is the oxidative reaction of the easily-slurried solid carbonaceous raw material in the wet-fed easily slurryable solid carbonaceous raw material / water slurry. However, the gasification temperature rises temporarily until the supply amount of oxygen gas to the hard-to-slurry solid carbonaceous raw material is reduced, but the degree of increase is within an allowable range as described later. Yes, a system that can ensure the safety of the gasification plant will be configured.

When the supply amount of oxygen gas is larger than the above range, the ratio of the oxidation reaction of the difficult-to-slurry solid carbonaceous raw material and the easily slurryable solid carbonaceous raw material becomes high, and the gasification furnace 9
The cold gas efficiency in the generated gas from the above becomes too low, which is not preferable. Further, if the supply amount of oxygen gas is less than the above range, the partial oxidation reaction of the difficult-to-slurry solid carbonaceous raw material and the easily-slurried solid carbonaceous raw material is not carried out to the desired degree, so that the gasification furnace is also required. The cold gas efficiency in the generated gas from No. 9 becomes too low, or the gasification temperature becomes lower than the melting temperature of the ash content in the easily-slurried solid carbonaceous raw material that is wet-fed, and the ash content is not sufficiently melted. However, it is not preferable because the metal components such as heavy metals contained in the dry-fed hard-to-slurry solid carbonaceous raw material are not effectively collected. In order to surely suppress the occurrence of such an unfavorable phenomenon, it is desirable that the supply amount of oxygen gas be within the above-mentioned preferable range.

Further, the method of the present invention, as described above,
At the same time as introducing the difficult-to-slurry solid carbonaceous raw material into the gasification burner 12a through the dry feed line 3,
Another feature is the simultaneous gasification of so-called dry feed and wet feed, in which the easily slurried solid carbonaceous raw material / water slurry is introduced into the gasification burner 12b through the wet feed line 7. The ratio of the feed amount of the dry-fed difficult-to-slurry solid carbonaceous raw material to the feed amount of the easily-slurried solid carbonaceous raw material / water slurry fed from the gasification furnace 9 is the above-mentioned oxygen gas supply ratio. Even if the cold gas efficiency in the generated gas reaches a desired value described later, and the supply of the difficult-to-slurry solid carbonaceous raw material does not stop the supply of oxygen gas to the gasification burner 12a following it. The reaction chamber 10 of the gasification furnace 9 accompanying a temporary temperature rise of the generated gas due to consumption of oxygen gas corresponding to the amount of the difficult-to-slurry solid carbonaceous material to the oxidation reaction of the easily-slurried solid carbonaceous material. The temperature within should be determined to be at least 2000 ° C or less.

Therefore, the above-mentioned supply ratio varies depending on the types of the difficult-to-slurry solid carbonaceous raw material and the easily slurried solid carbonaceous raw material and the gasification temperature during steady operation, and cannot be unconditionally limited. Coal such as subbituminous coal, bituminous coal, and anthracite is used as the easily slurried solid carbonaceous raw material, and the gasification temperature during steady operation is 1400 to 1
When maintained in the range of 450 ° C., the difficult-to-slurry solid carbonaceous raw material per 1000 kg / hr of the easily-slurried solid carbonaceous raw material (anhydrous basis) in the easily-slurried solid carbonaceous raw material / water slurry ( The amount supplied on an anhydrous basis is, for example, usually 350 to 450 kg when using coal such as peat, lignite, and lignite having a water content of about 10 to 20 wt% as the difficult-to-slurry solid carbonaceous material.
/ Hr, preferably 390 to 420 kg / hr, when using plastic waste such as waste polystyrene, usually 150 to 250 kg / hr, preferably 180 to 20
When sludge containing 0 kg / hr and about 80% by weight of water is used, it is usually 50 to 150 kg / hr, preferably 100 to 120 kg / hr.

When the ratio of the supply amount of the difficult-to-slurry solid carbonaceous raw material to the supply amount of the easily-slurried solid carbonaceous raw material / water slurry is lower than the above range, the amount of the difficult-to-slurry solid carbonaceous raw material used is Is reduced, and it is not possible to effectively utilize the raw material, which is not preferable. When the ratio exceeds the above range, the supply of oxygen gas to the gasification burner 12a follows the supply of the difficult-to-slurry solid carbonaceous raw material due to the problem of the sensor system that catches it. Therefore, it is not possible to stop it, so that a temporary temperature rise of the gas generated due to the consumption of oxygen gas corresponding to the amount of the difficult-to-slurry solid carbonaceous raw material to the oxidation reaction of the easily-slurried solid carbonaceous raw material. Is more than 2000 ° C., which causes a problem that the life of the refractory bricks lined along the tips of the gasification burners 12a and 12b and the inner wall of the reaction chamber in the gasification furnace is adversely affected, which is not preferable. Furthermore, in order to ensure that such an unfavorable phenomenon does not occur, the above ratio should be within the above preferred range.

In the present invention, the difficult-to-slurry solid carbonaceous raw material, the easily-slurried solid carbonaceous raw material / water slurry and the oxygen gas are respectively gasified at the top of the gasification furnace 9 as described above. It is introduced into the gasification burners 12a and 12b which are axially charged into the reaction chamber 10 of the furnace 9 with the discharge port facing downward. That is, in the present invention, a total of two gasification burners are installed at the top of the gasification furnace 9, and these gasification burners 12a and 12b are of the annular type.
It is preferably a flow channel burner.

A flow of the fine particulate non-slurrying solid carbonaceous raw material supplied into the gasification burner 12a through the dry feed line 3 and the wet feed line 7
The flow of the easily slurried solid carbonaceous raw material / water slurry supplied into the gasification burner 12b under pressure is introduced through the central conduits of the gasification burners 12a and 12b, respectively. On the other hand, the flow of the oxygen gas flowing through the oxygen feed line 8 is branched into two at a predetermined flow rate ratio, one of which is supplied into the gasification burner 12a and the other of which is supplied into the gasification burner 12b. The flow of the oxygen gas supplied to the gasification burners 12a and 12b is the same as that of the gasification burner 12a, respectively.
It is introduced through the annular tubes of a and 12b.
The introduction of the solid carbonaceous raw material and the oxygen gas into the gasification burners 12a and 12b is not limited to the above-mentioned method, and the flow of the oxygen gas is changed to the gasification burner 12a.
The solid slurry carbonaceous raw material and the slurry slurry solid carbonaceous raw material / water slurry may be introduced into the central conduits a and 12b, and into the annular pipes of the gasification burners 12a and 12b.

Further, in the present invention, the cooling coil is wound around the outside of the gasification burners 12a and 12b in a spiral shape and the cooling water is cooled to prevent the gasification burners 12a and 12b from being exposed to a high temperature. It is desirable to do. The installation location of the gasification burner 12a is not limited to the top portion of the gasification furnace 9 described above, and the fine particulate difficult-to-slurry solid carbonaceous raw material in the reaction chamber 10 of the gasification furnace 9 described later. If a residence time sufficient to allow the partial oxidation reaction based on the contact between the gasification furnace and the oxygen gas to be performed can be performed to a desired degree, the discharge port of the gasification furnace 9 is provided at a side portion or a lower portion of the reaction chamber 10. May be placed sideways.

The gasification burner according to the present invention has a total of 2 for partial oxidation of the difficult-to-slurry solid carbonaceous raw material and partial oxidation of the easily-slurried solid carbonaceous raw material / water slurry.
Although it is assumed that the book gasification burners 12a and 12b are provided, the present invention is not limited thereto. That is, the flow of the fine particle-like non-slurry solid carbonaceous raw material introduced into the gasification burner through the dry feed line 3 and the flow of the easily slurried solid carbonaceous raw material / water slurry are uniformly mixed, and the gasification is performed. If the stable injection from the discharge port of the burner can be achieved, it may be one annular type two-flow burner. In this case, the dry feed line 3 and the wet feed line 7 are connected on the upstream side of the solid carbonaceous raw material supply port of the gasification burner, and the flow of the particulate difficult-to-slurry solid carbonaceous raw material and the easily slurried solid are provided. The carbonaceous raw material and the flow of the water slurry may be combined and introduced into the gasification burner from the solid carbonaceous raw material supply port in a mixed state of gas phase, liquid phase and solid phase. And
While introducing a mixed flow of a gas phase, a liquid phase and a solid phase consisting of the difficult-to-slurry solid carbonaceous raw material and the easily slurried solid carbonaceous raw material / water slurry through the central conduit of the gasification burner, the flow of the oxygen gas is changed. Introduced through the annular tube of the gasification burner, or vice versa, the gas phase,
A mixed flow of liquid and solid phases is introduced through the annular tube of the gasification burner, and the stream of oxygen gas is introduced through the central conduit of the gasification burner.

Furthermore, the type of gasification burner is
The present invention is not limited to the above-mentioned annular two-channel burner, but is a double annular burner (that is, three-channel burner).
It can also be. In this case, dry feed line 3
Through the central conduit of the gasification burner, either one of the flow of the fine particle-like difficult-to-slurry solid carbonaceous raw material or the flow of the easily-slurried solid carbonaceous raw material / water slurry supplied into the gasification burner through Introduced through
The other is introduced through an annular tube outside the gasification burner. Then, the flow of the oxygen gas is introduced through the intermediate annular tube of the gasification burner, whereby two streams of the fine particle difficult-to-slurry solid carbonaceous raw material and the easily-slurried solid carbonaceous raw material / water slurry are formed. Let it flow in between.

The difficult-to-slurry solid carbonaceous raw material and oxygen gas, and the easily slurried solid carbonaceous raw material and oxygen gas introduced into the gasification burners 12a and 12b, respectively, are supplied to the gasification burners 12a and 12b, respectively. The gas is injected from the discharge port into the reaction chamber 10 of the gasification furnace 9 having a high temperature, and these collide with each other to form a spray, which mix with each other and form a flame. The particles of the difficult-to-slurry solid carbonaceous raw material and the particles of the easily slurried solid carbonaceous raw material are used in the reaction chamber 10 of the gasification furnace 9 (a refractory 13 such as refractory bricks is provided around the reaction chamber 10). ) And is partially oxidized. By this partial oxidation, a flammable gas containing carbon monoxide and hydrogen as main components from the difficult-to-slurry solid carbonaceous raw material and the easily-slurried solid carbonaceous raw material,
That is, synthesis gas is generated.

The combustion temperature for the partial oxidation reaction in the reaction chamber 10 of the gasification furnace 9, that is, the gasification temperature, and the pressure in the reaction chamber, that is, the gasification pressure, are as described above. That is, when coal such as subbituminous coal, bituminous coal, anthracite is used as the easily slurried solid carbonaceous material, the gasification temperature is higher than the melting temperature of the ash contained in the coal. . Usually 1200-1500 ℃,
It is preferably 1400 to 1450 ° C., and the gasification pressure is usually 3 to 250 kg / cm ² G, preferably 30 to
It is preferably 100 kg / cm ² G. And
The size of the reaction chamber 10 is mainly carbon monoxide and hydrogen generated by the partial oxidation reaction of the difficult-to-slurry solid carbonaceous raw material and the easily slurryable solid carbonaceous raw material under the gasification conditions as described above. The combustible gas as a component is preferably sized so that the residence time in the reaction chamber 10 is 1 to 30 seconds, preferably 2 to 10 seconds.

When the residence time of the generated gas in the reaction chamber 10 is less than 1 second, the partial oxidation reaction of the difficult-to-slurry solid carbonaceous raw material and the easily-slurried solid carbonaceous raw material proceeds to a desired degree. Since it does not, the cold gas efficiency in the generated gas becomes too low, or the gasification temperature becomes lower than the melting temperature of the ash in the easily slurried solid carbonaceous raw material that is wet fed, and the melting of the ash is Insufficiently performed, the metal components such as heavy metals contained in the dry-slurried difficult-to-slurry solid carbonaceous raw material become insufficiently scattered from the hard-to-slurry solid-carbonaceous raw material, and the metal component is effective. It is not preferable that it is no longer collected. In addition, the reaction chamber 1 for the generated gas
If the residence time in 0 exceeds 30 seconds, the reaction chamber 10
Is too large and the device becomes large, which is not preferable from the economical point of view. In addition, when the residence time of the generated gas in the reaction chamber 10 is less than 2 seconds or exceeds 10 seconds, the above-described undesirable phenomenon may occur.

In the method of the present invention, the ash contained in the wet-fed raw material for solidified slurry carbonaceous is melted by the above-mentioned partial oxidation reaction, and the reaction chamber 1
It adheres to the 0 wall and runs down the wall. On the other hand, the metal components such as heavy metals contained in the hard-to-slurry solid carbonaceous raw materials such as dry-fed plastic wastes react as they are or as metal oxides when the hard-to-slurry solid carbonaceous raw material is burned. The heavy metal (or its oxide) is scattered in the chamber 10 and adheres to the wall of the reaction chamber 10. While the heavy metal (or its oxide) is dissolved in the ash content in the molten slurry-like solid carbonaceous raw material in a molten state. , Along with the molten ash content along the wall of the reaction chamber 10.

The molten ash content containing the heavy metal component is then further flowed down through the reaction chamber 10 to descend into the cooling water 14 stored at the bottom of the quenching chamber 11 of the gasification furnace 9, where Is solidified by. Then, the solidified heavy metal component-containing ash is not dispersed in the cooling water 14 but settles at the bottom of the quenching chamber 11 due to its own weight.
5 together with cooling water 14 and removed by mechanical means such as a lock hopper. As the cooling water 14, for example, recirculated water from a gas cleaning step on the downstream side (not shown in FIG. 1) or the like is appropriately replenished into the rapid cooling chamber 11 from the rapid cooling water line 16.

Since the solidified ash extracted as described above contains most of the heavy metal components dissolved therein, the heavy metal components that cause problems such as pollution are
It rarely comes out of the solidified ash. Therefore, the solidified ash thus obtained can be utilized for applications such as landfill even if it contains heavy metals.

On the other hand, the combustible gas generated in the reaction chamber 10, that is, the synthesis gas, passes through the interconnecting passage between the reaction chamber 10 and the quench chamber 11 and enters the quench chamber 11. It is guided, sprayed as quenching water from the quenching water line 16, and cooled by coming into contact with the cooling water 14 stored at the bottom of the quenching chamber 11. This contact may be performed by a known method such as a gasification process using the Texaco method. That is, it is preferable that the contact between the synthesis gas and the cooling water is performed by discharging the high temperature synthesis gas from a dip tube (not shown in FIG. 1) below the surface of the cooling water,
In addition, the dip tube is a saw-tooth to help disperse the syngas throughout the cooling water so that the syngas can be effectively cooled by intimately contacting the syngas with the cooling water. Those having a dispersing device such as a low edge are preferred.

The pressure in the quenching chamber 11 should be selected so that the cooling water 14 accumulated at the bottom of the quenching chamber 11 is at least sufficient to maintain the liquid state, and the reaction chamber 10 and The pressure inside the reaction chamber 10, that is, the pressure substantially equal to the gasification pressure, is maintained by the interconnecting passage with the quenching chamber 11. The temperature of the cooling water 14 in the quenching chamber 11 is 100 to 250 ° C., preferably 150 to 250 ° C.
It is preferably set to 230 ° C. If the temperature is below 100 ° C,
Heat is recovered from the hot synthesis gas to produce the quench chamber 11
The amount of water vapor generated in the gas decreases, and the amount of water vapor required for the water gas conversion reaction in the downstream process cannot be carried along with the generated gas. When the temperature exceeds 250 ° C, the pressure in the quenching chamber 11 also increases. However, the cooling water 14 is flushed, which is not preferable in any case.

The synthesis gas comes into contact with the cooling water 14 as described above, is cooled to a temperature in the range of 200 to 230 ° C., and while passing through the cooling water 14, unconverted granular carbon and the like. While leaving at least a part of the suspended solids in the cooling water 14, it is taken out of the gasification furnace 9 through the generated gas taking-out port 17. In this case, a large amount of water vapor is generated in the quenching chamber 11 and is entrained in the flow of the synthesis gas taken out of the gasification furnace 9 in a saturated state. this is,
In the downstream process, additional water vapor necessary for increasing the hydrogen / carbon monoxide ratio (molar ratio) is supplied by the water gas shift reaction.

In the present invention, as described above, the carbon conversion rate (gas) is obtained by the partial oxidation of the dry-slurry difficult-to-slurry solid carbonaceous raw material and the wet-feed easily slurried solid carbonaceous raw material. The weight ratio of carbon in the evolved gas to carbon in the total solid carbonaceous raw material supplied to the gasification furnace) is at least 95% by weight or more,
It is preferable that 97 to 99% by weight of the generated gas 13 be taken out from the generated gas outlet 17 of the gasification furnace 9.

The generated gas 13 contains water vapor in a saturated state as described above, but its composition is such that coal such as subbituminous coal, bituminous coal, or anthracite is used as the raw material for solidified slurry carbonaceous material. And when using substantially pure oxygen gas as the gasifying agent, on a dry gas mol% basis,
_{H 2: 30~40, CO: 30~50} , CO 2: 10~
30, H ₂ S: 0-5, COS: 0-1, N ₂ : 0
5, Ar: 0 to 1 and CH _4: 0 to 1 (provided that sum of these components is 100 mol%) carbon monoxide (CO)
It is a combustible gas containing gas and hydrogen (H ₂ ) gas as main components. Therefore, in the present invention, the generated gas 13
The cold gas efficiency (that is, the ratio of the total amount of carbon monoxide gas and hydrogen gas from the difficult-to-slurry solid carbonaceous material and the easily slurried solid carbonaceous material) is 60% or more, preferably 65% or more. Is desirable. When the cold gas efficiency of the generated gas 13 is lower than 60%, the reaction between the difficult-to-slurry solid carbonaceous raw material and the easily-slurried solid carbonaceous raw material and oxygen gas is more like combustion than partial oxidation, and the difficult-to-use slurry is generated. It is not preferable because the low-grade solid carbon raw material such as the modified solid carbonaceous raw material cannot be effectively utilized.

The combustible gas taken out from the generated gas outlet 17 of the gasification furnace 9, that is, the generated gas 13, is
For example, it can be used as a fuel gas after being subjected to necessary treatment such as removal of unnecessary gas described later. Alternatively, the gas such as carbon monoxide and hydrogen contained therein can be used as a raw material for chemical synthesis, for example, for synthesizing chemical products such as ammonia, alcohol, aldehyde, and hydrocarbon.

That is, among the non-metallic harmful components contained in the combustion raw materials such as the hard-to-slurry solid carbonaceous raw material and the easy-slurry solid carbonaceous raw material, the sulfur component is H ₂ S or CO.
It becomes S and the chlorine component changes to HCl. Most of the nitrogen component becomes nitrogen gas, and part of it becomes NH ₃ .
In addition to useful CO, the carbon component becomes CO ₂ . The above-mentioned generated gas can be easily removed in a high-pressure state by a commonly used technique such as reticizole process, selexol process, acid gas removal equipment such as MEA, Claus equipment, etc. can do. Further, when the detoxified gas is burned, a slight amount of thermal NOx is produced, but this is not a practically problematic amount. Furthermore, there is no concern about the generation of dioxins, which is a problem in the incineration process using a normal garbage incinerator.

By the way, in the method of the present invention, the gasification furnace 9
In the reaction chamber 10 of No. 3, which is flammable, containing carbon monoxide and hydrogen, which is generated by partial oxidation of the dry-fed difficult-to-slurry solid carbonaceous raw material and the wet-feed easily slurried solid carbonaceous raw material. The gas is introduced into the quenching chamber 11 of the gasification furnace 9 and the cooling water stored in the bottom of the quenching chamber 11 is passed through for cooling treatment, but the method is not limited to this method, and the flammability is not limited. It is also possible to introduce the gas into the waste heat boiler, cool it in the waste heat boiler and produce steam.

[0052]

EXAMPLES Next, the method of the present invention will be described in more detail with reference to examples and comparative examples, but the method of the present invention is not limited to these examples unless it exceeds the gist. The methods of measuring various characteristics in the following examples and comparative examples are as follows.

Example 1 Using the partial oxidation device having the structure shown in FIG. 1, the gasification treatment of the difficult-to-slurry solid carbonaceous raw material by the simultaneous gasification of the dry feed system and the wet feed system was carried out as follows. went. (Gasification treatment during steady operation) As a solidified solid carbonaceous raw material having a hard slurry, the water content in the form is 20% by weight, and the industrial analysis values (constant humidity base) shown in Table 5 and the elements shown in Table 6 511 kg / hr of brown coal (Greek coal) with analytical value and high calorific value, that is, 409 on a dry basis
The powder was supplied to a dry mill, which is the dry crushing apparatus 1, at a supply rate of kg / hr, and dry crushed. The crushed brown coal had an average particle size of 44 μm, and the particle size distribution was 44 μm.
Those having a particle size of m or less were 50% by weight in the form of fine particles.

Subsequently, the pulverized product of the brown coal was sent to the lock hopper feeder 2. The lock hopper feeder 2 including an upper hopper 21, an intermediate hopper 22 and a lower hopper 23, connection pipes for connecting the respective hoppers, and lock hopper valves 24, 25 and 26 provided in the connection pipes is 2 series are installed, switching between these series, the lock hopper valve 24,
A series of operations such as opening and closing of 25 and 26, pressurization of the intermediate hopper 22 and the lower hopper 23 with pressurized nitrogen gas were performed by sequence control. By this operation, the pulverized product of the brown coal was charged into the reaction chamber 10 at the upper part of the gasification furnace 9 at a supply rate of 409 kg / hr (anhydrous basis) under a pressure of 50 kg / cm ² G. Gasification burner 12a installed as described above
Was continuously introduced through the dry feed line 3.

On the other hand, as an easily slurried solid carbonaceous raw material, an industrial analysis value shown in Table 5 (constant humidity base), an elemental analysis value shown in Table 6 and a subbituminous coal having a high calorific value (Australia, Great Greta) 100) on a dry basis
At a supply rate of 0 kg / hr, it is supplied to the wet mill which is the wet pulverizer 4 and at the same time, water is supplied to the wet mill at a rate of
It was supplied at a supply rate of 2.5 kg / hr and was subjected to wet pulverization. As a result, a slurry of the crushed subbituminous coal and water was produced, and the solid content in the slurry, that is, the concentration of the crushed subbituminous coal was 64% by weight.

The crushed subbituminous coal has an average particle diameter of 44 μm, and the particle diameter distribution is 44 μm.
The following was 50% by weight of fine particles. Next, the crushed subbituminous coal discharged from the wet mill
1562.5 kg / of water slurry is delivered by a pump
It was sent to the slurry tank 5, which is an intermediate tank, at a rate of supply of hr. The slurry tank 5 is equipped with a stirrer, and the subbituminous coal / water slurry charged into the slurry tank 5 and stored up to a predetermined level is sufficiently stirred by the stirrer and has a concentration of 64 wt. % Homogeneous slurry and the deposition of subbituminous coal particles in the slurry on the bottom of the slurry tank 5 was prevented. Therefore,
1562.5 kg / of the above-mentioned crushed bituminous coal / water slurry
The slurry is taken out from the slurry outlet at the bottom of the slurry tank 5 at a rate of hr and is pumped to 50 kg / cm ² G by the pump 6.
To the gasification furnace 9 through the wet feed line 7.
The discharge port at the top of the reactor was continuously introduced into the gasification burner 12b charged in the reaction chamber 10.

At the same time as the dry feed of the pulverized lignite crushed material into the gasification burner 12a and the wet feed of the pulverized subbituminous coal / water slurry into the gasification burner 12b, a gasifying agent is introduced at the same time. As 50kg
/ Cm ² G through the oxygen feed line 8 under pressure 79
A flow of oxygen gas having a concentration of 99.7% by volume flowing at a rate of 9 Nm ³ / hr is branched into two, and one flow is 143 N
It was introduced into the gasification burner 12a at a rate of m ³ / hr, and the other stream was introduced into the gasification burner 12b as a balance thereof at a rate of 656 Nm ³ / hr. Therefore,
The amount of the oxygen gas introduced into the gas feed burner 12a on the dry feed side and the gasification burner 12b on the wet feed side is set such that the oxygen required for complete combustion of the pulverized subbituminous coal / water slurry to be wet fed. The amount of oxygen gas is 9% and 41.5% respectively, and the total amount of the oxygen gas introduced into the gasification furnace 9 is required for complete combustion of the wet-fed pulverized bituminous coal / water slurry. It was 50.5% of the above-mentioned oxygen gas amount.

The pulverized brown coal, pulverized subbituminous coal / water slurry and oxygen gas introduced into the gasification burners 12a and 12b, respectively, are then introduced into the reaction chamber 10 of the gasification furnace 9 through respective outlets. Jetting at high temperature formed a flame. The gasification conditions in the reaction chamber 10 are pressure 38 kg /
cm ² G, temperature 1400 ° C., residence time 6 seconds. Therefore, in the reaction chamber 10, the dry-blended brown coal pulverized product and the wet-fed subbituminous coal pulverized product are partially oxidized by the oxygen gas and generated.
Then, it is introduced into a quenching chamber 11 located at the lower part of the reaction chamber 10, sprayed as quenching water from a quenching water line 16, and the cooling water 1 accumulated at the bottom of the quenching chamber 11
The generated gas 13 accompanied by water vapor in a saturated state by passing through the inside of No. 4 was taken out from the generated gas take-out port 17. The amount and composition of the evolved gas 13 are shown in Table 1 on a dry gas basis.
It was as follows.

[0059]

[Table 1]

Therefore, the carbon conversion rate in the above gasification treatment was 97.0%, and the cold gas efficiency was 69.0.
%Met. In addition, ash was extracted from the ash discharge port 15 at the bottom of the gasification furnace 9 together with the cooling water 14 at a rate of 245.0 kg / hr.

(Gasification treatment when the feed on the dry feed side is stopped) During the steady operation of the gasification furnace 9, the lock hopper feeder 2 broke down, so that the raw coal on the dry feed side (Greek coal) was crushed. Gasification burner for things 1
The supply to 2a was stopped. On the other hand, the pulverized product / water slurry of the subbituminous coal (Australia, Great Greta coal) on the wet feed side was temporarily 1562.5 kg / hr.
(However, the crushed product of the subbituminous coal is 10 on a dry basis.
Gasification burner 1 with the supply rate of 00 kg / hr)
Introduced in 2b. Also, the oxygen gas is temporarily
It is supplied while a ratio of 9 nm ³ / hr, these, the dry feed side of the gasification 12a is introduced at a rate of 143 nm ³ / hr, and, in the wet feed side of the gasification burner 12b 656Nm ³ / hr Was introduced in the ratio of.

The pressure in the reaction chamber 10 of the gasification furnace 9 was maintained at 38 kg / cm ² G as in the steady operation, but 143 Nm ³ / from the dry feed side gasification burner 12a.
Since the oxygen gas supplied at the rate of hr was also consumed in the partial oxidation reaction of the subbituminous coal pulverized product / water slurry, the temperature of the reaction chamber 10, that is, the gasification temperature increased to 2000 ° C. Amount and composition of dry gas 13 taken out from the dry gas take-out port 17 of the gasification furnace 9 (dry gas basis)
Table 2 shows that oxygen gas does not remain in the generated gas, and it was found that the gasification operation can be safely performed even in the case of a trouble such as the supply stop of the solid carbonaceous raw material by the dry feed method.

[0063]

[Table 2]

The carbon conversion rate at this time was 97.0% as in the steady operation, but the cold gas efficiency was 57.
4%.

Example 2 (Gasification during steady operation) Lignite (Greek charcoal) 409 kg / hr as a solid carbonaceous raw material that is difficult to slurry
Instead of (anhydrous base), a dry pulverization device with a supply rate of 195 kg / hr (100% polystyrene conversion) of waste polystyrene (having polystyrene resin as a main component) having the elemental analysis values and the higher heating value shown in Table 2 The average particle size is 44 μm, and the particle size distribution is 50 μm or less.
In the same manner as in Example 1 except that the pulverized product of waste polystyrene of weight% was used, the gasification treatment of the non-slurry solid carbonaceous raw material was carried out by the simultaneous gasification of the dry feed system and the wet feed system. Dry feed side gasification burner 12
The amount of the oxygen gas introduced into a was 8.9% of the amount of the oxygen gas necessary for complete combustion of the wet-fed pulverized subbituminous coal / water slurry, and The total amount of the oxygen gas introduced into the reactor was 50.4% of the amount of the oxygen gas required for complete combustion of the wet-ground pulverized subbituminous coal / water slurry.

The residence time in the reaction chamber 10 of the gasification furnace 9 was 6 seconds, and the amount and composition of the generated gas 13 taken out from the generated gas take-out port 17 were as shown in Table 3 on a dry gas basis.

[0067]

[Table 3]

Therefore, the carbon conversion rate in the above gasification treatment was 97.0%, and the cold gas efficiency was 72.4.
%Met. Further, ash was extracted from the ash discharge port 15 at the bottom of the gasification furnace 9 together with the cooling water at a rate of 146.0 kg / hr. This ash contained a small amount of heavy metals contained in the waste polystyrene of the solid slurry carbonaceous raw material, but they were both dissolved in the ash solids under normal environmental conditions. Then it did not seep outside.

(Gasification treatment when the feed on the dry feed side is stopped) During the steady operation of the gasification furnace 9, the lock hopper feeder 2 broke down. Burner 12a
Supply to. In this case, the gasification process, the amount and composition of the obtained generated gas on the dry gas basis, etc. were temporarily processed in exactly the same manner as in the case of the gasification process when the feed on the dry feed side of Example 1 was stopped. The same result as in Example 1 was obtained.

Example 3 (Gasification during steady operation) Lignite (Greek coal) 409 kg / hr as a solid carbonaceous raw material that is difficult to slurry
Instead of (anhydrous basis), sludge having a water content of 80% by weight and having an elemental analysis value and a higher calorific value shown in Table 2 was 570 kg / hr, that is, 114 kg / hr on an anhydrous basis. At a supply rate of 50 μm, the powder was supplied to a dry mill that is the dry crushing apparatus 1 and was dry crushed, and by this dry crushing, the average particle size was 44 μm, and the particle size distribution was 50 μm or less. Except that a sludge crushed product was obtained in a weight percentage, in exactly the same manner as in Example 1,
Gasification treatment of a solid carbonaceous raw material which was difficult to slurry was performed by simultaneous gasification of dry feed method and wet feed method.

The residence time in the reaction chamber 10 of the gasification furnace 9 was 6 seconds, and the amount and composition of the generated gas 13 taken out from the generated gas take-out port 17 were as shown in Table 4 on a dry gas basis.

[0072]

[Table 4]

Therefore, the carbon conversion rate in the above gasification treatment was 97.0%, and the cold gas efficiency was 60.8.
%Met. Further, ash was extracted from the ash discharge port 15 at the bottom of the gasification furnace 9 together with the cooling water at a rate of 182.4 kg / hr. This ash contained a small amount of heavy metals contained in the sludge as the difficult-to-slurry solid carbonaceous raw material, but all of them were in the state of being dissolved inside the ash solid matter, and the normal environment It did not seep outside under the conditions.

(Gasification treatment when the feed on the dry feed side is stopped) During the steady operation of the gasification furnace 9, the lock hopper feeder 2 broke down, so that the gasification burner of the sludge crushed raw material on the dry feed side Supply to 12a was stopped. In this case, the same treatment as in the case of the gasification treatment at the time of stopping the raw material supply on the dry feed side of Example 1 was performed temporarily, and the gasification temperature, the amount of the generated gas obtained on a dry gas basis, and the The same results as in Example 1 such as composition were obtained.

[0075]

[Table 5]

[0076]

[Table 6]

Comparative Example 1 Using the partial oxidation apparatus having the structure shown in FIG. 2, gasification treatment of the difficult-to-slurry solid carbonaceous raw material and the easily slurried solid carbonaceous raw material by the wet feed method is performed as follows. It was That is, as the hard-to-slurry solid carbonaceous raw material, the same brown coal (Greek coal) used in Example 1 was 511 kg / hr, that is, 409 on a dry basis.
It is supplied to the wet mill 31 of the wet pulverizer at a supply rate of kg / hr, and the wet mill 31 is supplied with 51% of water at the same time.
It was supplied at a rate of 1 kg / hr and subjected to a wet pulverization process.
As a result, a slurry of the pulverized brown coal and water was produced, and the solid content in the slurry, that is, the concentration of the pulverized brown coal was 40% by weight. The crushed brown coal particles had an average particle size of 44 μm, and the particle size distribution was such that 50% by weight of particles having a particle size of 44 μm or less were in the form of fine particles.

Next, the brown coal pulverized product / water slurry discharged from the wet mill 31 is supplied to a pump for 10 minutes.
It was sent to the slurry tank 33 at a supply rate of 22 kg / hr. The water supply rate to the wet mill 31 was set to be less than 511 kg / hr and the solid content concentration in the slurry was set to be higher than 40% by weight. Despite such agitation, solid contents could be deposited on the bottom of the slurry tank 33, etc., and a homogeneous slurry could not be manufactured.

On the other hand, as the easily slurried solid carbonaceous raw material, the same subbituminous coal (Australia, Great Greta coal) used in Example 1 was used on an anhydrous basis of 1000.
It is supplied to another wet mill 32 at a supply rate of kg / hr, and 562.5 kg of water is simultaneously supplied to the wet mill 32.
It was supplied at a supply ratio of / hr and was subjected to a wet pulverization process. As a result, a slurry of the crushed subbituminous coal and water was produced, and the solid content in the slurry, that is, the concentration of the crushed subbituminous coal was 64% by weight. The crushed subbituminous coal particles have an average particle size of 44 μm, and the particle size distribution is 50 μm or less.
It was in the form of fine particles of weight%. Therefore, the subbituminous coal pulverized product / water slurry discharged from the wet mill 32 was sent to the slurry tank 33 at a supply rate of 1562.5 kg / hr by a delivery pump.

The slurry tank 33 is provided with a stirrer, and the ground lignite crushed product supplied as described above.
The water slurry and the subbituminous coal crushed product / water slurry are stored here to a predetermined level and then sufficiently stirred to obtain a solid content,
That is, a pulverized product of brown coal, a pulverized product of subbituminous coal and a water slurry having a total concentration of 54.5% by weight of the pulverized product of brown coal and the pulverized product of subbituminous coal were obtained.

Next, this brown coal crushed product / subbituminous coal crushed product
The water slurry was extracted from the slurry outlet at the bottom of the slurry tank 33 at a rate of 2584.5 kg / hr, pressurized to 50 kg / cm ² G by the pump 34, passed through the wet feed line 35, and released at the top of the gasification furnace 37. Was continuously introduced into the gasification burner 38 charged in the reaction chamber 371. At the same time, oxygen gas with a concentration of 99.7% by volume was used as a gasifying agent at 50 kg / cm.
Through the oxygen feed line 36 under the pressure of ² G, 92
The gasification burner 38 was continuously introduced at a supply rate of 5 Nm ³ / hr. Therefore, the supply amount of the oxygen gas is 5 times the oxygen gas amount necessary for complete combustion of the brown coal crushed product, the subbituminous coal crushed product, and the subbituminous coal crushed product in the water slurry.
It was 8.5%.

2584.5 kg of the above-mentioned brown coal pulverized product, subbituminous coal pulverized product, and water slurry introduced into the gasification burner 38.
/ Hr and the oxygen gas 925 Nm ³ / hr were subsequently injected at a high temperature into the reaction chamber 371 of the gasification furnace 37 from the outlet of the gasification burner 38 to form a flame. The gasification conditions in the reaction chamber 371 are pressure 38 kg / cm
² G, temperature 1400 ° C., residence time 6 seconds. Therefore, in the reaction chamber 371, the wet-ground pulverized product of brown coal and the pulverized product of subbituminous coal are generated by being partially oxidized by the oxygen gas, and then the reaction chamber 3
The generated gas 373 that is guided to the quenching chamber 372 located at the lower part of 71 and passes through the inside of the cooling water 374 stored at the bottom of the quenching chamber 372 to entrain steam in a saturated state.
Was taken out from the generated gas take-out port 375 of the gasification furnace 37. The amount and composition of the generated gas 373 were as shown in Table 7 on a dry gas basis.

[0083]

[Table 7]

Therefore, although the carbon conversion rate in the above gasification treatment was 97.0%, the cold gas efficiency was 60.
It was as low as 3%, which was not satisfactory.

Comparative Example 2 Wet mill 31 was used as a solid carbonaceous raw material for making a slurry difficult.
The same waste polystyrene as that used in Example 2 was used in place of the brown coal supplied at a supply rate of 09 kg / hr (anhydrous basis), and was supplied to the wet mill 31 at a supply rate of 195 kg / hr. At the same time, the water in the mill 31 was changed to 511 kg / hr and 292.5 kg / h.
It was supplied at a ratio of r and wet-milled to obtain a solid polystyrene, that is, a waste polystyrene crushed product / water slurry having a concentration of 40% by weight of the waste polystyrene crushed product, and the crushed waste contained in the slurry. The polystyrene particles had an average particle size of 44 μm, and the particle size distribution was such that particles having a particle size of 44 μm or less were in the form of fine particles of 50% by weight.
The slurry tank 33 is supplied with the waste polystyrene pulverized product / water slurry discharged from the wet mill 31 and the subbituminous coal pulverized product / water slurry discharged from the wet mill 32,
A solid tank, that is, a waste polystyrene crushed product / a subbituminous coal crushed product / water slurry having a total concentration of 58.3% by weight of the waste polystyrene crushed product and the subbituminous coal crushed product, a slurry tank From the slurry outlet at the bottom of 33,
In place of the brown coal crushed product / subbituminous coal crushed product / water slurry extracted at a rate of 2584.5 kg / hr, the waste polystyrene crushed product / subbituminous coal crushed product / water slurry was replaced with 205
Gasification burner 38 of oxygen gas having a concentration of 99.7% by volume as a gasifying agent, which was taken out at a rate of 0 kg / hr
Supply rate to 925 Nm ³ / hr and 868 Nm
³ / hr, so that the supply amount of the oxygen gas is the amount of the oxygen gas required for complete combustion of the waste polystyrene pulverized product, the subbituminous coal pulverized product, and the subbituminous coal pulverized product in the water slurry. 54.9%, and the waste polystyrene pulverized product / subbituminous coal pulverized product / water slurry 2050 kg / hr and the oxygen gas 868 Nm ³ / hr introduced into the gasification burner 38 are gasified. Except that a flame was formed by injecting from a discharge port of the burner 38 into the reaction chamber 371 of the gasification furnace 37 at a high temperature, the wet slurry feed-resistant solid carbonaceous raw material and Gasification treatment of the easily slurried solid carbonaceous raw material was performed.

The residence time in the reaction chamber 371 of the gasification furnace 37 was 6 seconds, and the amount and composition of the generated gas 373 taken out from the generated gas take-out port 375 were as shown in Table 8 on a dry gas basis.

[0087]

[Table 8]

Therefore, although the carbon conversion rate in the above gasification treatment was 97.0%, the cold gas efficiency was 6%.
The value was 7.9%, which was lower than that in the case where the waste polystyrene was dry fed as the difficult-to-slurry solid carbonaceous raw material (in the case of Example 2).

Comparative Example 3 As a solid carbonaceous raw material for making a slurry difficult, 4 was added to the wet mill 31.
The same sludge as used in Example 3 was used instead of lignite supplied at a supply rate of 09 kg / hr (anhydrous basis), 570 kg / hr, that is, 114 k on an anhydrous basis.
The water is supplied to the wet mill 31 at a supply rate of g / hr, and water is simultaneously supplied to the wet mill 31 at 511 kg / hr.
Of the solid content, that is, the concentration of the sludge pulverized product is 1
A 2% by weight sludge crushed product / water slurry was obtained, and the crushed sludge particles contained in the slurry had an average particle size of 4
The particle size distribution was 4 μm, and the particle size distribution was 44 μm or less and was 50% by weight in the form of fine particles. In the slurry tank 33, the sludge crushed product / water slurry discharged from the wet mill 31 The sub-bituminous coal pulverized product and the water slurry discharged from the wet mill 32 are supplied, and the solid content, that is, the concentration of the sludge pulverized product and the sub-bituminous coal pulverized product is 44.3% by weight in total. Thing / sub-bituminous coal crushed product / water slurry was obtained, and crushed brown coal / sub-bituminous coal crushed product / water was extracted from the slurry outlet at the bottom of the slurry tank 33 at a rate of 2584.5 kg / hr. Instead of the slurry, the sludge crushed product, subbituminous coal crushed product, and water slurry were extracted at a rate of 2512.5 kg / hr, and a gasification burner for oxygen gas having a concentration of 99.7% by volume as a gasifying agent. Offer to 38 The supply rate was changed to 925 Nm ³ / hr and changed to 893 Nm ³ / hr. Therefore, the supply amount of the oxygen gas was such that the sludge crushed product, the subbituminous coal crushed product, and the subbituminous coal crushed product in the water slurry. The amount of oxygen gas required for complete combustion was 56.5%, and the sludge crushed product / subbituminous coal crushed product / water slurry 2512.5 kg / hr introduced into the gasification burner 38 High-purity oxygen gas 893 Nm ³ / hr was injected at a high temperature into the reaction chamber 371 of the gasification furnace 37 from the outlet of the gasification burner 38, and a flame was formed in exactly the same manner as in Comparative Example 1. The wet feed method was used to gasify the difficult-to-slurry solid carbonaceous raw material and the easily-slurried solid carbonaceous raw material.

The residence time in the reaction chamber 371 of the gasification furnace 37 was 6 seconds, and the amount and composition of the generated gas 373 taken out from the generated gas take-out port 375 were as shown in Table 9 on a dry gas basis.

[0091]

[Table 9]

Therefore, although the carbon conversion rate in the above gasification treatment was 97.0%, the cold gas efficiency was 5%.
It was as low as 3.4%, which was not satisfactory. For reference, the lignite (Greek coal) having a water content of 20% by weight and having an industrial analysis value (constant humidity base) shown in Table 1 and an elemental analysis value shown in Table 2 and a high calorific value is used. Table 10 shows the gasification performance data for the case of gasification by the wet feed method and the case of gasification by the dry feed method.
Shown in

[0093]

[Table 10]

[0094]

According to the method of the present invention, in the method of partially oxidizing a solid carbonaceous raw material in the presence of oxygen to gasify it, it is generally difficult to form a high-concentration slurry with water (the slurry concentration is 40% by weight). However, even if it is gasified by the wet feed method, it is possible to gasify the difficult-to-slurry solid carbonaceous raw material by the dry feed method, because the calorific value is low and only gas with low cold gas efficiency can be obtained. As a result, it is possible to produce a gas having a high cold gas efficiency, and it is possible to effectively use the low-quality coal such as peat, lignite, lignite, plastics, sludge and the like, which are the raw material solidified carbonaceous materials that are difficult to slurry. Moreover, high-quality coal such as subbituminous coal, bituminous coal, anthracite and petroleum coke, which is relatively easy to be made into a high-concentration slurry with water, at the same time as gasification of the difficult-to-slurry solid carbonaceous raw material by the dry feed method. By gasifying the easily slurried solid carbonaceous raw material with a wet feed, it is possible to solve the problem of supply instability, which is a disadvantage of the gasification process by the dry feed method, and safely perform the gasification process. .

[Brief description of drawings]

FIG. 1 is a flow chart of an oxidizer showing an embodiment of a gasification treatment method of a solid slurry carbonaceous raw material which is difficult to slurry by simultaneous gasification of a dry feed system and a wet feed system of the present invention.

FIG. 2 is a flow chart showing an example of an oxidizer used for carrying out Comparative Examples 1, 2 and 3 of the present invention.

[Explanation of symbols]

 1 Dry Grinding Device 2 Rock Hopper Feeder 3 Dry Feed Line 4 Wet Grinding Device 5, 33 Slurry Tank 6, 34 Pump 7, 35 Wet Feed Line 8, 36 Oxygen Feed Line 9, 37 Gasification Furnace 10, 371 Reaction Chamber 11, 372 quenching chamber 12a, 12b, 38 gasification burner 13,373 generated gas 14,374 cooling water 15 ash discharge port 16 quenching water line 17,375 generated gas outlet 21 upper hopper 22 intermediate hopper 23 lower hopper 24, 25, 26 Lock hopper valve 31, 32 Wet mill

─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. ⁶ Identification number Reference number within the agency FI Technical display location B09B 3/00 (72) Inventor Toshio Tsujino 1-12-32 Nishihonmachi, Ube City Yamaguchi Prefecture Ube Industries Ube headquarters

Claims (1)

[Claims] 1. A solid carbonaceous raw material is simultaneously introduced into a gasification furnace by using both a dry feed method and a wet feed method, and at a temperature higher than a melting temperature of ash in the solid carbonaceous raw material under pressure. A gas of a difficult-to-slurry solid carbonaceous raw material obtained by simultaneous gasification of a dry feed system and a wet feed system, which is characterized in that a flammable gas containing carbon monoxide and hydrogen is generated by partial oxidation. Chemical treatment method.