JPS6142759B2 - - Google Patents

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a partial oxidation process for producing synthesis gas, fuel gas or reducing gas with superheated steam as a by-product.

In the partial oxidation method, approximately
The 815-1930°C exit gas stream must be cooled below the equilibrium temperature for the desired gas composition. This cooling is currently performed by quenching the exiting gas stream with water or by cooling the gas stream in a gas cooler. This cooling results in a saturated flow. These two types of gas cooling significantly increase entropy and reduce thermal efficiency. This problem is partially solved by the present invention in which superheated steam is produced with sensible heat extracted from the highest temperature hot effluent gas stream exiting the partially oxidized gas generator.

The production of saturated but not superheated steam is disclosed in US Pat. No. 3,528,930.

The present invention produces H ₂ by partially oxidizing a fuel containing carbon and hydrogen with a free oxygen-containing gas at a temperature of 815-1930°C and a pressure of about 1-250 atm absolute in the reaction zone of a free-flow non-catalytic gas generator. A method for producing a gas mixture containing CO and CO, the method comprising: extracting sensible heat from an uncooled effluent gas stream from a gas generator by sequentially passing the effluent gas stream through first and second heat exchange zones; The sensible heat taken out in the second heat exchange area is used to convert the flowing water into steam by indirect heat exchange, and the sensible heat taken out in the first heat exchange area is used to convert at least a portion of the forewater steam into superheated steam. The present invention provides a method for producing a mixed gas containing H ₂ and CO. At least a portion of the superheated steam produced by the method of the invention can be continuously recycled into the gas generator as a dispersion medium or carrier for the fuel or as a temperature moderator. Also, at least a portion of the superheated steam can be continuously sent to a steam turbine and used to generate mechanical power or electric power.
The thermal efficiency of a steam turbine is high due to the high steam temperature. According to one embodiment of the invention, the hot gas stream from the partially oxidized gas generator is sequentially passed through first and second heat exchange zones. A stream of steam is continuously generated within the second heat exchange zone or gas cooler.
The steam stream is then continuously generated as a superheated steam stream by heat exchange with the hot gas stream from the gas generator in the first heat exchange zone.

Another embodiment of the method of the invention includes three heat exchange zones. In the first heat exchange zone, a continuous flow of heat transfer fluid absorbs a portion of the sensible heat of the hot effluent gas stream emerging from the gas generator. A portion of the heated heat exchange fluid is continuously sent to a third heat exchange zone (which functions as a superheater) to exchange heat with a continuous stream of steam. This steam had been generated in the second heat exchange zone by heat exchange between water and the effluent gas stream emerging from the first heat exchange zone.

A continuous stream of superheated steam is removed from the superheater,
Used in this method or for external use. Advantageously, the pressure of the superheated steam is higher than the pressure within the gas generator.

In another embodiment of the invention, a portion of the steam or heat transfer fluid is mixed with the effluent gas stream in the first heat exchange section.

In one form of this embodiment, hot effluent gas from the gas generator is passed directly through a first heat exchange zone comprising a shell and tube heat exchanger to a pressure higher than the pressure of the effluent gas. heat exchange with a continuous stream of steam, converting the steam into a continuous stream of superheated steam and reducing the temperature of the effluent gas. A portion of the steam is continuously mixed into the effluent gas through openings provided in the tube wall, thereby creating a gap between the surface of the tube and the effluent gas stream passing through the first heat exchange zone. be provided with a steam protective sheath.

Advantageously, the steam produced by the method of the invention is at a higher pressure than the effluent gas, so that the steam flows through the opening in the wall of the tube without being compressed further. .

In another form of this embodiment, the hot effluent gas exiting the gas generator optionally passes through a solids separation zone that is approximately the same temperature and pressure as inside the gas generator before being passed through a shell and tube heat exchanger. to exchange heat with a continuous stream of heat transfer gas that cools the effluent gas stream and heats the heat transfer gas. A portion of this heat transfer gas is released into the effluent gas stream through openings in the walls of the heat exchanger tubes and header and is transferred between the tube and header surfaces and the effluent gas stream. Provide a protective sheath or curtain for hot gases.
The heated heat transfer gas exiting the first heat exchange zone is admitted into the third heat exchange zone for indirect heat exchange with the vapor stream from the second heat exchange zone, thereby causing the heat transfer gas to and produce a superheated steam stream. The mixture of the effluent gas from the first heat exchange zone and the discharged portion of the heat transfer gas is purified to produce a raw effluent product gas. A portion of the purified raw effluent product gas is mixed as a blended gas with the cooled heat transfer gas exiting the third heat exchange zone, and the mixed gas enters the first heat exchange zone as a heat transfer gas. It will be done.

Hereinafter, the present invention will be explained in detail with reference to the drawings.

The present invention provides an improved partial oxidation gasification process for producing raw synthesis gas, reducing gas or fuel gas with valuable superheated steam as a by-product. This gas includes H ₂ and CO, and generally includes one or more of H ₂ O, CO ₂ , H ₂ S, COS, CH ₄ , N ₂ , Ar, and particulate carbon.

A continuous effluent gas stream of synthesis gas, reducing gas or fuel gas is produced in a refractory lined reaction zone of a separate free-flow enclosed non-catalytic partially oxidized fuel gas generator. The gas generator preferably consists of a vertical pressure vessel made of aluminum, such as that disclosed in US Pat. No. 2,992,906.

A wide range of combustible organic materials containing carbon and hydrogen are reacted in a gas generator, optionally in the presence of a reduced temperature gas, with a gas containing free oxygen to generate the effluent gas stream.

It can optionally contain a variety of elements commonly used in partial oxidation gas generators, including gaseous, liquid and solid hydrocarbons, carbonaceous materials and mixtures thereof; Such fuels can also be used in accordance with the present invention.
In fact, almost any combustible gas containing organic material, fossil fuel, or slurry thereof can be used. For example, (1) a pumpable slurry of solid carbonaceous fuels such as coal, lignite, particulate carbon, petroleum coke, concentrated sewage sludge, and mixtures thereof; (2) a temperature moderator gas or (3) a gas-solid suspension, such as a finely divided solid carbonaceous fuel dispersed in either a gaseous hydrocarbon; (3) an atomized liquid hydrocarbon; or atomized water and carbon particles; Temperature moderator
There are gas-liquid-solid dispersions, such as those dispersed in a gas. Hydrocarbon fuels may contain 0 to 10% by weight of sulfur and 0 to 15% by weight of carbon.

The term liquid hydrocarbons, as used herein to refer to suitable charging feedstocks, includes liquefied petroleum gas, petroleum extracts and residues, gasoline, naphtha, kerosene, crude oil, asphalt, gas oil, heavy oil, tar sands oil. , shale oil, coal liquefied oil, aromatic hydrocarbons (benzene, toluene, xylene, etc.), coal tar, circulating light oil obtained from catalytic cracking,
Contains various substances such as coker gas oil and mixtures thereof by furfural extraction. Gaseous hydrocarbon fuels used herein to indicate suitable gaseous charge feedstocks include methane, ethane, propane, butane, pentane, natural gas, water gas, coke oven gas, refinery gas, acetylene.・
Includes tail gas, ethylene off gas, syngas and mixtures thereof. Gaseous and liquid raw materials can be mixed and used simultaneously, and can contain paraffin compounds, olefin compounds, naphthenic compounds, and aromatic compounds in arbitrary proportions.

Fuels containing carbon and hydrogen can also be used such as carbohydrates, cellulose materials, aldehydes, organic acids, alcohols, ketones, oxidized fuel oils, waste liquids, by-products from chemical processing containing oxidized organic matter, and their There are oxidized hydrocarbon-based organic substances, including mixtures.

The fuel feedstock can be at room temperature or can be preheated to a temperature in the range of 315-650°C, for example 530°C, preferably below its decomposition temperature. Preheating the fuel is
This can be done by non-contact heat exchange or direct contact with superheated or saturated steam generated later in the process. The fuel can be introduced into the combustor in a vaporized mixture with a temperature moderator or in a liquid phase. Suitable temperature moderators include superheated steam, saturated steam, unsaturated steam, water, _CO2- rich gases, a portion of the cooled exhaust steam from turbines used downstream in the process, nitrogen in the air, This includes by-product nitrogen from conventional air separators and mixtures thereof.

The use of a temperature moderator to moderate the temperature in the reaction zone is generally related to the carbon to hydrogen ratio in the charge and the oxygen content of the oxidant stream. While some gaseous hydrocarbon fuels do not require a temperature moderator, liquid hydrocarbon fuels use a temperature moderator along with a sufficient amount of pure oxygen. A temperature moderator can be included in the mixture with the reactant stream. Alternatively, the temperature moderator can be placed into the reaction zone of the gas generator by a separate tube within the fuel combustor.

0-100 of superheated steam generated later in the process
% can be used for preheating and dispersing liquid hydrocarbon fuels or for preheating and transferring solid hydrocarbon fuels that can be placed into gas generators.

The weight ratio between the total amount of H ₂ O and the total amount of fuel introduced into the reaction zone of the gas generator is generally between 0 and 5.

When a relatively small amount of H ₂ O is pumped into the reaction zone, e.g., through the combustor to cool the combustor tip, it can be used as fuel, a free oxygen-containing gas, a temperature moderator, or a combination thereof.
_H2O can be mixed. In that case,
Mixing ratio of water and fuel is 0.0-1.0, preferably 0.0-0.2
It is convenient to do so.

"Oxygen-containing gas" used in this specification
The term refers to air, oxygen-enriched air, i.e., air with an oxygen content greater than 21 mol%, and nearly pure oxygen, i.e., oxygen with a concentration greater than 95 mol% (the remainder being _N2 and noble gases). be. Oxygen-containing gas can be supplied to the combustor at temperatures ranging from room temperature to 985°C. The ratio of free oxygen in the oxidizer to carbon in the charging material (C/O, atom/atom) is preferably about 0.7 to 1.5.

The feed stream is directed by the fuel combustor into the reaction zone of the fuel gas generator. A suitable fuel combustor is the annular combustor disclosed in US Pat. No. 2,928,460.

The feed stream is approximately
Autogenic temperature of 815-1930℃ and approx. 1-250℃
The reaction is carried out by partial oxidation without a catalyst at absolute atmospheric pressure. The reaction time in the fuel gas generator is generally 1 to 10 seconds. The outflow gas from the gas generator contains CO, H ₂ , CO ₂ , H ₂ O, CH ₄ , N ₂ ,
Composed of Ar, H ₂ S, COS, etc. Particulate carbon (based on the weight of carbon in the feed) is generally 0.2 to 20% by weight from liquid feeds, while that from gaseous hydrocarbon feeds is usually negligible. The specific composition of the effluent gas will depend on the actual operating conditions and feed streams. Synthesis gas consists mostly of H ₂ +CO. Most or all of the H ₂ O and CO ₂ are removed for reducing gases. For fuel gas the content of CH ₄ is maximized.

Preheating of the fuel can be carried out by indirect heat exchange or direct contact with superheated, saturated or unsaturated steam produced by the method of the invention.

A continuous stream of hot effluent gas having approximately the same pressure and temperature as the reaction zone pressure and temperature exits the axial outlet of the gas generator and enters the first heat exchange zone. If desired, a solids separation region (not shown) can be provided between the gas generator outlet and the first heat exchange region. The solids separation region may include a free flow catch pot or slug chamber. This slug chamber can be inserted into the line before the first heat exchanger. This slag chamber eliminates any solid material contained in the hot effluent gas stream, i.e. at least a portion of particulate carbon ash, slag, refractories and mixtures thereof or slag exiting the gas generator; Ash, refractory debris can be separated from the effluent gas stream,
It is recovered with a very low pressure drop in the line.
A typical slag chamber that can be employed is disclosed in US Pat. No. 3,528,930.

A portion of the sensible heat of the uncooled effluent gas stream originating from the gas generator or solids separation zone is recovered in the first heat exchange zone. This heat is used to convert steam generated in other parts of the process into superheated steam at a higher pressure than the pressure within the gas generator.

1 and 3, superheated steam in lines 39, 42 is generated in heat exchanger 16 by heat exchange between the steam and the effluent gas stream from the gas generator. 2 and 4, superheated steam in line 39 is generated in heat exchanger 55 by heat exchange between a heat transfer fluid and steam. The heat transfer fluid has been previously heated in the heat exchanger 16 by heat exchange with the effluent gas stream from the gas generator.

In FIG. 1, the outflow gas flow from gas generator 1 is
It passes through a heat exchanger 16 forming a first heat exchange area. Its passage takes place in a non-contact heat exchange with the steam generated in a heat exchanger (ie gas cooler) 23 located immediately downstream and forming a second heat exchange zone. By definition, “contactless”
The term means that the two gas streams do not mix. If possible, these two flows should flow in opposite directions. However, the two streams can also flow in the same direction. FIG. 1 shows a heat exchanger 16 consisting of a conventional tube and outer box. Steam is admitted into the heat exchanger's outer box, superheated steam exits from the outer box, and the hot effluent gas is directed into tubes or multiple coils. This structure can be reversed to allow hot effluent gas to flow into the outer box. Any heat exchanger that can withstand the temperature and pressure of the fluid can be used. Heat-resistant metals and heat-resistant ceramics can be used as constituent materials.

The steam stream that is converted to superheated steam has a temperature between 150 and 375
It enters the first heat exchanger at a temperature of about 400 to 600 degrees Celsius and a pressure of about 4 to 260 atmospheres absolute and is transferred to the first heat exchanger at a temperature of about 400 to 600 degrees C and a pressure of about 4 to 260 atmospheres absolute.
from the heat exchanger. Superheated steam can be generated at a higher pressure than the pressure in the reaction zone of the gas generator. Therefore, when this superheated steam is used in a turbine for generating mechanical energy or electrical energy, efficiency becomes high. The exiting gas stream, which has approximately the same temperature and pressure as the temperature and pressure in the reaction zone, is approximately
It enters the first heat exchanger at a temperature of 815-1930°C and a pressure of about 1-250 atmospheres absolute (e.g. 3.5-250 atmospheres absolute).

The partially cooled exit gas stream is approximately 315~
At a temperature of 1430°C and a pressure of approximately 3.5 to 250 atmospheres absolute, it exits the first heat exchange zone and enters the second heat exchange zone, gas cooler 23, where it undergoes non-contact heat exchange with the boiler feed water. In this second heat exchange region, the temperature of the exiting gas stream drops significantly, but the pressure changes little.

That is, the temperature of the raw effluent gas stream leaving the second heat exchanger is approximately 160-370°C, and the pressure is from the pressure in the reaction zone of the gas generator to the line, the solids removal zone, and the first and second minus the normal pressure drop across the heat exchanger, ie, a total pressure drop of about 2 atmospheres absolute or less. The raw effluent gas contains the following components in mole percent: _H2 70~10, CO 15
~57, _CO2 0-5, _H2O 0-20, _N2 0-75,
Ar 0-1.0, CH ₄ 0-25, H ₂ S 0-2.0, COS
0-0.1. Unreacted particulate carbon is about 0-20% by weight (based on the weight of carbon in the feedstock). Second
The effluent gas from the heat exchanger can be sent to a downstream gas purification and purification zone to remove undesirable components.

Boiler water enters the second heat exchange zone at a temperature of about room temperature to 360°C and exits as unsaturated or saturated steam at a temperature of about 150 to 375°C and a pressure of 4.5 to 260 absolute pressures. Advantageously, this steam can be generated at a higher pressure than the pressure in the reaction zone of the gas generator. Second heat exchanger 2
In No. 3, the outflow gas stream and the boiler water flow in opposite directions, but they can also flow in the same direction.
Also, in another embodiment, the steam flow can be generated within the tube and the effluent gas flow can be directed into the outer box.

Approximately 0 of the steam generated in the second heat exchange area
~100% by weight is placed into the first heat exchanger resulting in superheated steam at a higher pressure than the pressure in the gas generator. Some of the steam can be used elsewhere in the process or used externally. The saturated or unsaturated superheated steam thus produced can be used to provide heat. For example, steam can be used to preheat the feedstock that is fed to the gas generator. In this way, at least a portion of the steam generated in the method of the invention can preheat a hydrocarbon-based fuel to a temperature of about 430° C. below the decomposition temperature of the fuel. This steam can also be used as a temperature moderator in a gas generator.

At least a portion of the superheated steam generated in the process of the invention can be passed into a partially oxidized gas generator where it can react and contribute to the amount of hydrogen in the effluent gas stream. Furthermore, the thermal efficiency of this method can be increased. The problem of condensation that occurs when steam and fuel are mixed can be avoided using superheated steam. A portion of the superheated steam can be used as the working fluid in a turbocompressor to compress the air sent to the air separator to produce nearly pure oxygen (95 mole percent or more). At least a portion of the pure oxygen can be supplied as an oxidizing agent to the gas generator. Superheated steam can also be used as a working fluid for turbine generators. Starting from very high levels of superheated steam, converting heat to electricity increases conversion efficiency.

The first and second heat exchangers 16 and 23 are connected to each other. The advantage of such an arrangement is that it simplifies the design and reduces the dimensions of each heat exchanger, thereby reducing the cost of the device. Heat exchange units of conventional design can be assembled. Even if one of the units has to be replaced for repair, downtime of the equipment can be reduced.
In another embodiment, the first and second heat exchange regions can be housed within a common outer box.

Another embodiment of an apparatus for carrying out the method of the invention is shown in FIG. A hot gas stream exiting the gas generator or free-flowing solids or slag separation zone whose temperature and pressure are approximately equal to the temperature and pressure in the reaction zone enters the first heat exchanger 16. This effluent gas stream undergoes a non-contact heat exchange with a relatively cold heat transfer fluid to bring the temperature of the heat transfer fluid to approximately 985-1540°C.
Raise to ℃. At the same time, the effluent gas stream is cooled to about 315-1430°C and leaves the first heat exchange zone at a pressure of about 2.7-255 atmospheres absolute directly to the second heat exchanger or gas cooler 23. enter. In the gas cooler 23, the effluent gas stream exchanges heat with the boiler water in a non-contact manner. Boiler water enters the gas cooler 23 at a temperature of about room temperature to 360°C,
It leaves there as a saturated or unsaturated vapor at about 150-375°C and about 4.5-260 atmospheres absolute. Advantageously, this steam can be generated at a higher pressure than the pressure in the reaction zone of the gas generator. The effluent gas flow is approx.
It exits the gas cooler 23 at 160 DEG -370 DEG C. and the pressure in the reaction zone of the gas generator minus the normal pressure drops in the lines and vessels.

While heat exchange is taking place in heat exchangers 16, 23, a continuous flow of steam from second heat exchanger 23 and heat transfer fluid from first heat exchanger 16 in third heat exchanger 55 By non-contact heat exchange between
Superheated steam of 400-600°C and approximately 4.5-260 atmospheres absolute is generated. This superheated steam can be generated at a higher pressure than the pressure within the reaction zone of the gas generator. The heat transfer fluid enters heat exchanger 55 from heat exchanger 16 at a temperature of about 985-1540°C and exits heat exchanger 55 at a temperature of about 455-1205°C. The pressure of the heat transfer fluid hardly changes before and after entering and exiting the heat exchanger 55. heat exchanger 5
The heat transfer fluid exiting 5 is recycled into the first heat exchanger 16 where it undergoes non-contact heat exchange with the effluent gas stream from the gas generator. This device allows the sensible heat contained in the effluent gas stream from the gas generator to be used to generate superheated steam in a relatively clean environment.

A portion of the raw effluent gas stream can be used as a heat transfer fluid. Alternatively, at least a portion of the raw effluent gas stream can be purified and purified by removing undesirable components with conventional equipment. At least a portion of this product gas can be used as a heat transfer medium. For example, _H2 containing the following components (mol%)
A mixture of +CO can be produced. _H2 10~48, CO
15-48, remainder N ₂ +Ar. Additionally, nearly pure, ie, 98 mole percent or more, hydrogen can be produced from the effluent gas stream by well-known gas cleaning and purification techniques, including water gas reactions, for use as a heat transfer fluid.

The heat transfer fluid circulated between heat exchangers 16 and 55 can be either gaseous or liquid and can be H ₂ O, helium, nitrogen, argon, hydrogen or H ₂ +CO. be able to. Alternatively, depending on the temperature and pressure operating conditions and the phase of the heat transfer fluid, gaseous or liquid sodium, potassium, Mercury or sulfur can be used. In this case,
Cooling of these heat transfer fluids below their freezing temperature must be avoided.

In another example, the heat transfer fluid can change state during heat exchange. For example, heat exchanger 16
In this case, a liquid phase heat transfer fluid can be changed to a gas phase. In heat exchanger 55, the heat transfer fluid is then turned into a liquid phase and pumped to heat exchanger 16.

A conventional heat exchanger consisting of an outer box and tubes can be used. As mentioned above, the 2
The direction of flow of different types of fluids can be made the same or reversed. Line and gas generator 1
By appropriately insulating the heat exchangers 16, 23, and 55, the temperature drop between these parts can be made very small, for example, 5°C.
Heat-resistant metals and fire-resistant materials can be used as constituent materials.

Figure 3 shows the first tube consisting of multiple tubes and coils.
A heat exchanger 16A is shown. Headers can be placed inside or outside the outer box. Openings are provided in the walls of the tube and header through which the
At least a portion of the steam passing through the outer box, e.g.
50 mole percent, more preferably 3 to 25 mole percent, is introduced into the tube while the remaining steam is superheated in the outer box. In the tube or header, the steam is mixed with an effluent gas stream which is passed directly into the tube from the gas generator at a slightly lower pressure, about 0.35 to 3.5 atmospheres or less. However, prior to this mixing, the relatively cool mixed vapor forms a continuously flowing protective sheath or curtain between the effluent gas stream flowing through the tube and the inner surface of the tube at a temperature of approximately 815-1930°C. Form. In a similar manner, the surfaces of the header which are normally contacted by the hot effluent gas stream can be covered with a protective sheath or curtain of continuously flowing steam. By doing so, the surfaces of the tube and header can be cooled and protected from corrosive gases, and furthermore, the adhesion of ash, slag, soot, etc. can be prevented.

Alternatively, heat exchanger 16A can be configured such that the hot effluent gas stream passes through the outer box and the steam passes through the tubes. In this case as well, at least a portion of the steam
For example, 1 to 50% by volume, preferably 3 to 25% by volume, can be pumped from the tube into the outer box. Additionally, this vapor forms a protective sheath between the outer surfaces of the tubes and headers and the effluent gas stream. The remaining steam passing through the tube is superheated.

Near the downstream end, the temperature of the exiting gas stream is lower than the temperature at which corrosion from the H ₂ S it contains occurs, so no holes are made in the pipes and headers in that area to divert the steam. Or reduce the number of holes. For similar reasons, high quality materials are only required at the upstream end of the tube.

The diameter of the hole provided in the pipe and header is approximately 0.025 ~
Can be made as small as 1.6mm. These holes are provided around the circumference of the tube and their number is determined such that a protective sheath is formed around the entire circumference of the tube. Facilitates thermal expansion of the tube,
Two metals can be slip-jointed to allow vapor release. For example, longitudinally spaced ridges on the male end of the slide joint provide a controlled gap to allow a designed amount of leakage when the joint is assembled. As the structural material, heat-resistant porous materials including metals and ceramics can be used.

The steam stream to be converted to superheated steam enters the first heat exchanger at a temperature of about 150-375°C and a pressure of about 4.5-260 atmospheres absolute. Superheated steam is approximately 400-600
It exits the first heat exchanger at a temperature of 0.degree. C. and a pressure of 4 to 260 atmospheres absolute. The superheated steam is higher than the pressure within the reaction zone of the gas generator. The steam therefore flows through the holes provided in the heat exchanger wall without being compressed.

While the effluent gas stream is moving through the first heat exchanger, its moisture content increases by a range of 1 to 50 mol%, such as about 3 to 25 mol%. If the effluent gas stream leaving the first heat exchanger undergoes a water gas reaction downstream of the process, the molar ratio of the gas mixture
It is desirable to mix a sufficient amount of steam into the effluent gas stream in the first heat exchange zone to achieve a H ₂ O/CO of 0.5 to 8.

A partially cooled effluent gas stream exiting the first heat exchanger having a temperature of, e.g., about 315 to 1430°C and a pressure of about 3 to 250 atmospheres absolute to generate steam that is superheated in the first heat exchange zone. is almost the same as the second
into the heat exchange area of the boiler, where it exchanges heat with the boiler water in a non-contact manner.

The temperature and pressure conditions within the second heat exchange zone in this example are approximately the same as in the other examples.

Yet another embodiment of the invention is shown in FIG. The hot effluent gas stream from the gas generator or free flowing solids and slag removal area enters a heat exchanger similar to that shown in FIG. However, instead of steam, at least a portion of the heat transfer gas is mixed into the hot effluent gas stream. This creates a continuously flowing relatively cool protective sheath between the tube and header surfaces and the effluent gas stream flowing through heat exchanger 16A from the gas generator. The unmixed portion of the heat transfer gas is approximately
After being heated to 700-1540°C, it is introduced into the third heat exchanger 55, where it directly exchanges heat with steam to generate superheated steam.

At the same time, the effluent gas stream through the first heat exchanger 16A is cooled to 315-1430°C and about 3
It exits heat exchanger 16A at ~250 atmospheres.

This effluent gas stream is purified by removing its solids such as carbon particles and ash, and optionally by removing acid gases such as CO ₂ , H ₂ S, and COS. At least a portion of the purified and purified effluent gas, e.g. 1-50% by volume, preferably 3-25% by volume, is mixed with the cooled heat transfer fluid exiting the third heat exchanger to transfer heat to the first heat exchanger. A purified effluent gas stream is formed which is mixed with the effluent gas stream in an exchanger. It is then passed through the first heat exchanger 16 as a mixed gas heat transfer gas at a temperature in the range of approximately 90-1315°C, for example 315-760°C.

The conditions in the second heat exchanger and the pressures and temperatures of the boiler water and generated steam are generally within the same ranges as in other embodiments of the invention.

When heat exchange is performed between heat exchangers 16A and 23,
A continuous superheated steam stream having a temperature of about 400-600°C and a pressure of about 4.5-260 atmospheres absolute is combined with the continuous steam stream from the second heat exchanger 23 and the heat transfer fluid from the first heat exchanger 16A. Third heat exchanger 5 by non-contact heat exchange between
5. Advantageously, the superheated steam is generated at a higher pressure than the pressure in the reaction zone of the gas generator. The heat transfer fluid is in the second heat exchanger 1
6A enters the heat exchanger 55 at a temperature in the range of about 425-1540°C, preferably 425-985°C, for example in the range of about 250-1370°C, preferably 310-815°C.
It comes out of the heat exchanger 55 at a temperature of about 35~
At 370° C., the effluent product gas stream is mixed into a recirculation component whose pressure is higher than the pressure of the raw effluent gas stream before being passed from the gas generator into the first heat exchanger 16A. Non-contact heat exchange is performed with the incoming discharge gas stream.

Referring again to FIGS. 1-4, the method of the invention will now be described in detail. All tubes and components should be thermally insulated as much as possible to reduce heat loss.

Referring first to FIG. 1, a free-flow non-catalytic partial oxidation gas generator 1 lined with refractory material has an upper flanged inlet 3 and a downstream flanged outlet 4.
and a reaction area 5 in a closed state. An annular combustor 6 having a central passage 7 coinciding with the central axis of the gas generator 1 is attached to the inlet 3 . center passage 7
has an inlet 8, and a conical nozzle 9 is provided at the lower end of the combustor 6. The combustor 6 is provided with a coaxial annular passage 10 . This passage 10 is the entrance 1
1 and a conical discharge passage 12. Other combustor designs may also be used.

A flanged inlet 15 of a conventional high temperature heat exchanger 16 is connected to the outlet 4 . Heat exchanger 16 has an inner tube or multiple coil 17, an outer box 20, and a downstream flanged outlet 21. gas generator 1
A free-flowing solids or slag separator (not shown) can optionally be inserted between the outlet 4 of the heat exchanger 16 and the inlet 15 of the heat exchanger 16. This separator provides little or no pressure drop in the gas stream. An outlet 21 of the heat exchanger 16 is connected to an upstream flanged inlet 22 of a gas cooler 23 . This gas cooler 23 is a conventional one having an inner tube 24, an outer box 25, and a flanged outlet 26 on the downstream side.

A continuous flow of liquid or gaseous fuel, or solid fuel in the form of a pumpable slurry, is admitted into the apparatus of FIG. 1 via tube 30 and supplied via tube 31. It is optionally mixed into the steam stream and the saturated steam stream supplied through tube 53. This mixing takes place in a mixer (not shown). This mixed flow passes through the pipe 33,
It is passed through the inlet 11, the passage 10 and the discharge passage 12 to the reaction region 5 of the gas generator 1.

At the same time, a continuous stream of gas containing free oxygen is admitted from the tube 34 through the central passage 7 of the combustor 6 and the nozzle 9 into the reactor 5 of the gas generator 1, where it is mixed with fuel and steam. .

The continuous stream of effluent gas leaving the gas generator 1 through the outlet 4 is sent to a heat exchanger 16 where it is generated by a gas cooler 23 and mixed into a vapor stream flowing in the opposite direction to the effluent gas stream. Ru. for example,
The steam rising inside the outer box 20 of the heat exchanger 6 turns into superheated steam and passes through the outlet 38, the pipe 39, the valve 41, and the pipe 31.
It is sent through pipe 33, where it is mixed with the hydrocarbon-based fuel sent through pipe 30. If desired, the superheated steam flow is routed from heat exchanger (also called superheater) 16 to pipe 42, valve 43, and pipe 4.
4 to the steam turbine.

The partially cooled effluent gas stream exits superheater 16 through outlet 21 and enters waste heat boiler 23 through inlet 22 . In the gas cooler 23, the effluent gas stream exchanges heat in a non-contact manner with the boiler water flowing in the opposite direction. The boiler water absorbs at least a portion of the remaining sensible heat of the effluent gas stream and becomes steam. Boiler water in tube 45 enters heat exchanger 23 through inlet 46 . This boiler water is in outer box 2.
5, turns into steam and exits the pipe 4 from the outlet 47.
Go out into 8. This steam enters the superheater 16 through an inlet 49 where it is converted into superheated steam. A portion of the steam is transferred to the gas cooler 2 for use in other applications.
3 through outlet 50 to pipe 51, valve 52, pipe 53
It can also be retrieved via

The cooled exit gas stream is routed through bottom outlet 26 and tube 54.
The gas can exit the gas cooler 23 through the gas cooler 23 and be sent to a conventional gas purification and purification area.

Refer now to FIG. The device shown in this figure has a bottom flanged inlet 56, a top flanged outlet 57, and an inner tube or coil 58.
The apparatus is similar to that shown in FIG. 1, except for the outer box 59 and the third heat exchanger 55, which includes a side outlet 60. From the pipe 61, a circulator 62, such as a pump, compressor or blower, directs a gaseous or liquid heat transfer fluid through a pipe 63 and an inlet 64 into the housing 20 of the heat exchanger 16. , thence through an outlet 65 and a tube 66 into an inlet 67 of the heat exchanger (also called superheater) 55 . after that,
The hot heat transfer fluid descends within the outer box 59 and exits through the bottom outlet 60 for recirculation to the heat exchanger 16.

The device of FIG. 2 operates in much the same way as the device of FIG. The main difference is the use of a heat transfer fluid that is circulated between heat exchangers 16 and 55. In the heat exchanger 16, the heat transfer fluid stream absorbs a portion of the sensible heat of the effluent gas stream from the gas generator 1 and is heated. As previously discussed, the heat transfer fluid within heat exchanger 16 rises within outer box 20 for non-contact heat exchange with the discharge gas stream flowing downwardly within tubes 17.
Next, in the heat exchanger 55, the sensible heat provided by the heat transfer fluid continuously descending the outer box 59 is sufficient to convert the continuous steam flow to superheated steam. This steam was generated in a waste heat boiler. At least a portion of the steam generated in the gas cooler 23 is admitted into the superheater 55 through the outlet 47, the tube 48 and the flanged inlet 56. Superheated steam from pipe 39 or steam from pipe 53 can also be introduced into gas generator 1 as a temperature moderator and a transport medium for fuel. Preferably, the exit gas flow passes through the tubes of heat exchangers 16, 23 connected in series.

In the apparatus shown in FIG. 3, the configurations of the gas generator 1, superheater and gas cooler 23 are generally the same as those of the apparatus shown in FIG.
6A has a somewhat different structure, having an inner tube or multiple coil 17, an outer box 20, a downstream header 19, and a flanged outlet 21, with the inner tube 17 being continuous with the headers 18 and 19.

A continuous stream of effluent gas leaving outlet 4 of gas generator 1 is sent to heat exchanger 16A and gas cooler 23
exchange heat with the steam generated by A source of steam from another source can be supplied through pipes 27, 28, 29, 32, 49. A portion of the steam rising up the outer box 20 of the heat exchanger 16A is removed through the holes 33 in the walls of the tubes 17 and the upstream header 18 and mixed with the hot effluent gas stream from the gas generator 1. Ru. The remaining steam is converted into superheated steam and then passed through outlet 38 and pipe 7.
9, 39, valve 41, and pipe 31 to pipe 35, where it is mixed with a hydrocarbon-based fuel. Superheated steam flow may also be provided from superheater 16A through pipe 42, valve 43, and pipe 44 to steam turbine 70. There, it turns a turbine and then comes out through a pipe 71. Turbine 70 drives an air compressor 72 and a generator 73. Compressor 7
2 is supplied with air through a tube 74 and exits through a tube 75. In the air separation area 76, the compressed air is separated into nitrogen (tube 77) and oxygen (tube 78). Superheated steam can also be removed from superheater 16A through outlet 38, pipes 79, 80, valve 81 and pipe 82.

The slightly cooled effluent gas stream containing said steam exits superheater 16A through outlet 21 and enters inlet 22 of waste heat boiler 23. gas cooler 23
The mixed gas stream descending within the gas cooler 23 exchanges heat with the boiler water rising within the gas cooler 23. The heated boiler water absorbs the remaining sensible heat in the gas mixture and turns into steam. In other words, water for boiler is pipe 4.
5 into the inlet 46 of the heat exchanger 23. This boiler water rises in the outer box 25 and turns into steam, which exits from the outlet 47 through the pipe 48. A portion of this steam is used at outlet 5 for other purposes.
0 through pipe 51, valve 52 and pipe 53.

The cooled gas mixture enters the tube 54 from the gas cooler 23 through the bottom outlet and is sent to the gas purification and purification zone. The purified and purified product gas can be used as synthesis gas, reducing gas, or fuel gas depending on the composition. For example, the purified product gas can be sent to a combustor of a gas turbine. The combustion gas burned in the combustor is sent to the expansion turbine, which rotates the turbine. This turbine drives a turbo compressor and a turbine generator. A turbo compressor can be used to compress the air used in this device.

Next, refer to FIG. The apparatus shown in this figure is similar to the apparatus shown in FIG. 2, except that it has a gas purification and purification region 91.

The recycled portion of the effluent gas stream in the pipe 115 is compressed by a gas compressor to a higher pressure than the raw effluent gas stream leaving the gas generator 1. The compressed, cooler recycle gas is mixed in line 68 with the heat transfer gas exiting from superheater 55 through lower outlet 60 and line 61. gas circulator 6
2, heat transfer gas is routed through tube 63, inlet 64, and downstream header 13 of heat exchanger 16A. In the heat exchanger 16A, the heat transfer gas flows through a plurality of tubes 1.
7 and exits through the header 14 and exit 15. While moving through heat exchanger 16A, some of the heat transfer fluid escapes through small holes in the walls of the tubes and headers. This leaking gas is mixed with the exit gas stream and a slightly cooled gas stream exits through outlet 21. The heated heat transfer gas flows from the outlet 65 to the tube 66 and the inlet 67 of the heat exchanger 55.
from there, descend inside the outer box 59, and exit 6.
0 and circulated through the heat exchanger 16A.

The heat transfer gas is heated in tubes 17 of heat exchanger 16A. Then, in heat exchanger 55, the amount of sensible heat provided by the continuously descending heat transfer gas stream in outer box 59 heats the vapor stream ascending in tubes 58 to produce superheated steam. is sufficient to cause it to occur.

The superheated steam is exited through pipe 39 and a portion thereof is passed through pipe 40, valve 41 and pipes 105, 31 into pipe 35 where it is mixed with the fuel from pipe 30. This mixed gas is introduced into the gas generator 1 via the combustor 6. The remaining superheated steam is transferred to pipe 1.
06, valve 107, and pipe 108 to the outside. Alternatively, a portion of the superheated steam can be used as the working fluid for the steam turbine 70.

Saturated or unsaturated steam in tube 48 is generated in gas cooler 23. Additional steam from other parts of the apparatus is routed through pipe 95, valve 96, and pipe 97.
It can be entered via . gas cooler 23
at least a portion of the effluent gas stream exiting from 1 to
100% by volume can be placed into the gas purification and purification region 91. If desired, a portion of the gas flow can be bypassed through the purification and purification region via line 124, valve 125, and line 126. Cleaned and purified product gas is generated in region 91 and at least a portion thereof is returned to compressor 69 as a constituent gas. The remaining product gas can be used, for example, as fuel gas in the combustor of a gas turbine. This gas turbine is used to drive compressors and generators. At least a portion of the steam for the superheater 55 is supplied to the boiler water through the pipes 45 and 46.
and the tube 24 through the outer box 25 of the heat exchanger 23.
The remaining sensible heat can be generated by the heat exchanger 23 by absorbing at least a portion of the residual sensible heat in the gas mixture with the steam and the effluent gas stream descending therein. At least a portion of this steam is passed through outlet 47, pipes 98, 48, and inlet 56 into superheater 55. The superheated steam from pipe 39 and the steam from pipe 53 can be admitted into the gas generator 1 as a temperature moderator and as a transport medium for the hydrocarbon-based fuel. Alternatively, the effluent gas stream from the gas generator 1 can be transferred to the heat exchanger 1 connected in series.
6.23 tubes can be passed through. In this case, the heat transfer gas in tube 63 passes through the outer box of heat exchanger 16A. A portion of the heat transfer fluid enters the tube through holes in the walls of the tube and header and is mixed with the effluent gas stream descending therethrough. However, first a protective sheath of heat transfer gas forms on the inner surfaces of the tube and header. It is also possible to provide a leak hole only in the upstream header.

The cooled effluent gas stream leaving tube 54 is transferred to tube 11.
7, valve 118 and pipe 119 to purification and purification area 91. The gas purified and purified in this way is transferred to the pipes 120, 121, the valve 122,
It exits through tube 123. If the product gas in tube 123 is a fuel gas, a portion of it is combusted in the gas furnace to generate heat. Alternatively, a portion of the fuel gas can be sent to the combustor of the gas turbine. The combustion gases are sent to an expansion turbine to drive the turbine. The product gas may consist of synthesis gas, reducing gas or pure oxygen. tube 54
At least a portion of the mixture of effluent gas stream and leakage gas in tube 124, valve 125 and tube 126
can be bypassed to the purification and purification area through.

A portion of the product gas in tube 120 is used as a replacement gas for the heat transfer gas that leaks through the holes in tube 17 and headers 13,14. This replacement gas is cooler than the heat transfer gas in tube 61 and passes through tube 130, valve 131, and tube 115 to compressor 69.
is sent to the outer box 20 of the heat exchanger 16A.
is compressed at a pressure higher than the pressure of the exiting gas stream in. As mentioned above, the compressed replacement gas is mixed with the heat transfer gas from tube 61 and the resulting gas mixture is circulated through the loop between heat exchangers 16A and 55.

The following examples are illustrative of the method of the invention. The method is carried out continuously and the values being carried out are hourly values for all material flows. Capacity indicates the value at 0° C. and 1 atm, and pressure is absolute pressure.

Example 1 This example is illustrated in FIG. In a free-flow non-catalytic gas generator, by partially oxidizing a hydrocarbon fuel (described below) with oxygen having a purity of approximately 99.7% by volume.
^89896m3 of raw synthesis gas is continuously generated.
The fuel is a pumpable slurry containing 470.3 Kg of carbon particles recovered by subsequent purification of the raw syngas product and 26014 Kg of reduced crude oil. The crude oil has the following final composition (% by weight): C 85.87, H ₂
11.10, S 2.06, N ₂ 0.78, O ₂ 0.16, Ash 0.04.
Furthermore, the API weight of the reduced crude oil is 12.5 (specific gravity
0.983), calorific value of 10185 Cal/g, and viscosity of Saybolt, Second Furol (1170 centistokes) at 50°C. Next, approximately 13,007 kg of superheated steam with a pressure of approximately 40.8 atm and a temperature of 399°C generated using this method.
is mixed into the reduced crude oil at a temperature of about
Create a gas mixture at 295℃. This gas mixture is continuously admitted into the annular passage of the annular combustor and from there is discharged into the reaction zone of the gas generator. Approximately 260℃
of oxygen is continuously introduced into the center passage of the combustor and mixed with the superheated steam and crude oil mixture.

Reactions involving partial acids occur in the free-flow reaction zone of the gas generator to produce a continuous effluent stream of raw synthesis gas at 1305° C. and 28.2 atmospheres. The raw hot synthesis gas effluent stream from the gas generator passes through a separate heat exchanger or superheater where it is heated up to 1125°C by heat exchange with a continuous stream of saturated steam stream generated after this process. cooled down. 65738Kg of saturated steam enters the superheater at 253℃ and 41.5 atm. And 400
℃, 40.8 atm superheated steam 65738 kg comes out from the superheater. As mentioned above, a portion of this superheated steam is passed into the gas generator, preferably mixed with crude oil. A portion of the superheated steam is used, for example, as working fluid for a turbo compressor of an air separation device for free oxygen generation, which is sent to a gas generator.

The slightly cooled raw syngas stream exiting the superheater is then passed into another gas cooler tube for heat exchange with 65738 Kg of boiler water flowing continuously through the gas cooler outer box. Cool to approximately 270℃. As a result, about 65,738 kg of the by-product saturated steam at about 253° C. and about 41.5 atmospheres is produced. As mentioned above, at least a portion of this saturated steam is passed into a superheater to become superheated steam. The remaining saturated steam is used for purposes such as preheating free oxygen-containing gas.

The pressure of the continuous effluent stream of raw synthesis gas leaving the gas cooler after heat exchange with boiler water is equal to the pressure in the reaction zone of the gas generator minus the normal pressure drop in the tubes and heat exchanger. Almost equal.
This pressure drop can be less than about 1.35 atmospheres. The composition of the raw synthesis gas stream exiting the gas cooler is as follows. _H2 41.55%, CO 41.59%, _CO2 4.61%,
_H2O 11.46%, _H2S 0.40%, COS 0.02%, _CH4
0.13%, _N2 0.21%, Ar 0.03%. The raw syngas effluent contains approximately 474.5 Kg of unconverted particulate carbon. Particulate carbon and other gaseous impurities can be removed from the raw synthesis gas in a downstream gas purification and purification region. It is also possible to mix a portion of the superheated gas into the synthesis gas stream and then convert the carbon monoxide in the gas stream to hydrogen and carbon dioxide by a water gas reaction. This CO ₂ can later be removed to produce a hydrogen-containing gas stream.

Embodiment 2 Embodiment 2 corresponds to the apparatus shown in FIG.

The type and amount of material fed to the free flow non-catalytic gas generator in this example is approximately the same as that of the feed material in Example 1. Similarly, the composition and amount of raw synthesis gas and the amounts of saturated and superheated steam produced are approximately the same in Examples 1 and 2. Furthermore, the operating temperatures and pressures in the gas generator and associated heat exchanger and the associated material stream and product temperatures and pressures are also approximately the same in the two embodiments.

In Example 2, 9361 Kg of hydrogen is continuously circulated between heat exchanger 16 and superheater 55 as a heat transfer fluid.

The raw synthesis gas stream from the gas generator at 1305°C and 28.2 atmospheres is cooled to 1124°C by heat exchange with a heat transfer fluid in heat exchanger 16. The heat transfer fluid enters heat exchanger 16 at 455°C and leaves there at 805°C. The continuous stream of raw synthesis gas is then cooled to 271°C in heat exchange with boiler water in gas cooler 23. The saturated steam at 252°C generated in the gas cooler 23 is sent to the superheater 55, where it undergoes non-contact heat exchange with the incoming heat transfer fluid at 805°C to produce superheated steam at 400°C and 40.8 atm. Continuous flow. The heat transfer fluid exits superheater 55 at a temperature of 455°C.

Example 3 Example 3 corresponds to the apparatus shown in FIG.

The type and amount of material provided to the gas generator is approximately the same as in Example 1. Similarly,
The composition and amount of raw synthesis gas are also approximately the same as in Example 1. The hot raw synthesis gas effluent stream from the gas generator passes through the tubes of a heat exchanger (superheater) 16A consisting of an outer box and tubes, where the saturated It is cooled to 1125°C by heat exchange with a continuous stream of steam. 253℃ and
Saturated steam at 41.5 atm enters the outer box of the 65738 kg superheater. Approximately 90% by volume of this saturated steam is
It exits the heat exchanger as superheated steam at 400°C and 40.8 atm. As explained in Example 1, a part of this superheated steam is preferably mixed with crude oil,
Put it into the gas generator. If desired, a portion of the superheated steam can be supplied as working fluid to the turbo compressor as described above. The remainder of the saturated steam, i.e. approximately 6573Kg placed in the superheater
The saturated steam escapes through small holes in the walls of the tube and upstream header and mixes with the hot, raw synthesis gas that passes therethrough. The steam sheath then wraps around the inner surface of the tube, preventing it from being corroded by the raw synthesis gas. Furthermore, neither carbon nor ash adheres to the inner surface of the tube.

The slightly cooled raw syngas stream leaving the superheater, mixed with the leaking steam inside the superheater, is sent to a conventional gas cooler and fed to its outer box.
Approximately 271℃ due to heat exchange with 65738Kg of boiler water
Cool until cool. This results in approximately 253℃ and approx.
Approximately 65,738 kg of saturated steam at 41.5 atmospheres is produced as a by-product. This steam is sent to superheater 16A to be made into superheated steam.

The pressure of the continuous output stream of raw synthesis gas leaving the gas cooler after heat exchange with boiler water is the pressure in the reaction zone of the gas generator less the normal pressure drop in the tubes and heat exchanger. approximately equal to the value. This pressure drop can be less than about 1.35 atmospheres.
The composition of the raw synthesis gas stream exiting the gas cooler is as follows. (Units are mol% in dry state). _H2
46.95, CO 46.99, _CO2 5.19, _H2S 0.45, COS
0.02, _CH4 0.14, _N2 0.23, Ar 0.03. The raw syngas effluent contains approximately 474.5 Kg of unconverted particulate carbon. These carbon and other gaseous impurities can be removed from the raw synthesis gas in a downstream gas purification and purification region. If desired, a portion of the superheated steam can be mixed into the synthesis gas stream and then the carbon monoxide in the gas stream converted to hydrogen and carbon dioxide by a water gas reaction. The CO ₂ can then be removed to produce a hydrogen-containing gas stream.

Example 4 Example 4 corresponds to the apparatus shown in FIG.

In this example, the type and amount of material fed to the free-flow non-catalytic gas generator is approximately the same as that described in Example 1. Similarly, the composition and amount of raw synthesis gas and the amount of saturated and superheated steam generated are also approximately the same as in Example 1. Additionally, the operating temperatures and pressures within the gas generator and associated heat exchanger and associated material flows and products are also approximately the same as in Example 1.

In Example 4, 9361 generated later in this method
Kg of hydrogen is continuously circulated between heat exchanger 16A and superheater 55 as a heat transfer fluid.

Continuous effluent stream of raw synthesis gas at 1305° C. and 28.2 atm from the gas generator into heat exchanger 16A.
It is cooled down to 1125°C by exchanging heat with the heat transfer fluid entered at a temperature of 455°C. The heat transfer fluid is heated to 805°C when it exits heat exchanger 16A.
The temperature of the continuous stream of raw synthesis gas mixed with leaked hydrogen in the heat exchanger is lowered by heat exchange with boiler water in the gas cooler 23.
A continuous stream of 253°C saturated steam generated in the gas cooler is mixed with replacement hydrogen and sent to the superheater 55.
As a result of non-contact heat exchange with the heat transfer fluid entering at a temperature of 805°C in the superheater 55, it is converted into superheated steam at 400°C and 40.8 atm.

[Brief explanation of the drawing]

1 to 4 are schematic diagrams showing different examples of apparatus for carrying out the method of the invention. 1... Gas generator, 16, 16A... Heat exchanger, 17, 24, 58... Tube, 20, 25, 59
... Outer box, 23 ... Gas cooler, 55 ... Superheater.

Claims (1)

[Claims] 1. A fuel containing carbon and hydrogen is heated at 815-1930°C and 1-250°C in the reaction zone of a free-flow non-catalytic gas generator.
A method for producing a gas mixture containing H ₂ and CO by partial oxidation with a gas containing free oxygen under conditions of absolute atmospheric pressure, the method comprising: and a second heat exchange region to remove sensible heat from the outflow gas stream, and the sensible heat stolen in the second heat exchange region is used to convert the water flow by indirect heat exchange. Converting at least a portion of said steam into steam at a temperature of 150 to 375°C and a pressure of 4 to 260 absolute atmospheres, using the sensible heat emitted in the first heat exchange zone, A method for producing a mixed gas, which comprises converting atmospheric pressure into superheated steam and sending at least a portion of this superheated steam to a steam turbine as a working fluid. 2. In the method described in claim 1,
The steam turbine is used to compress the air supplied to the air separation unit, which generates oxygen of 95 mole percent purity or higher for reaction in the gas generator, which is heated Before introducing at least a portion of the steam into the reaction zone of the gas generator and the fuel into the gas generator, about 460
A method characterized by preheating to a temperature of °C, but below its decomposition temperature. 3 Fuel containing carbon and hydrogen is heated at 815-1930°C and 1-250°C in the reaction zone of a free-flow non-catalytic gas generator.
A method for producing a gas mixture containing H ₂ and CO by partial oxidation with a gas containing free oxygen under conditions of absolute atmospheric pressure, the method comprising: and a second heat exchange region to remove sensible heat from the outflow gas stream, and the sensible heat stolen in the second heat exchange region is used to convert the water flow by indirect heat exchange. The steam is converted into steam at a temperature of 150 to 375° C. and at an absolute pressure of 4 to 260, and is sent from the second heat exchange zone to a third heat exchange zone, which is connected to the first and second heat exchange zones. Sensible heat is transferred from the first heat exchange zone by a heat transfer fluid circulated between a third heat exchange zone, where the steam is transferred to the flow of the heat transfer fluid. Using the sensible heat emitted in the first heat exchange zone, at least a portion of the steam is heated to a temperature of 400 to 600° C. and 4 to 260 atmospheric pressures absolute by superheating by indirect heat exchange with A method for producing a mixed gas, comprising converting the mixture into superheated steam and sending at least a part of this superheated steam to a steam turbine as a working fluid. 4. In the method according to claim 3, the heat transfer fluid comprises sodium, potassium, mercury,
A process characterized in that it is sulfur or hydrogen obtained from the effluent product gas by heat exchange followed by purification, water gas reaction and purification. 5. A method according to claim 3, wherein at least a portion of the superheated steam is used as a working fluid in a steam turbine used to compress air supplied to an air separation unit, said unit being used for gas generation. It generates oxygen with a purity of 95 mol% or higher for the reaction in the gas generator, and the fuel is preheated to a temperature of approximately 460℃ (but below its decomposition temperature) before being put into the gas generator. And furthermore,
directing at least a portion of the purified and optionally purified gas stream into a combustion chamber of the gas turbine;
A method characterized in that combustion gases from the combustion chamber are introduced into an expansion turbine for power generation. 6 Fuel containing carbon and hydrogen is heated at 815-1930°C and 1-250°C in the reaction zone of a free-flow non-catalytic gas generator.
A method for producing a gas mixture containing H ₂ and CO by partial oxidation with a gas containing free oxygen under conditions of absolute atmospheric pressure, the method comprising: and a second heat exchange region to remove sensible heat from the outflow gas stream, and the sensible heat stolen in the second heat exchange region is used to convert the water flow by indirect heat exchange. Converting at least a portion of said steam into steam at a temperature of 150 to 375°C and a pressure of 4 to 260 absolute atmospheres, using the sensible heat emitted in the first heat exchange zone, At least a portion of the purified, purified, and optionally purified gas stream is converted to superheated steam at atmospheric pressure and placed into a gas turbine combustor, from which the combustion product gases are used to generate power. A method for producing a mixed gas, characterized by introducing the mixed gas into an expansion turbine. 7 Fuel containing carbon and hydrogen is heated at 815-1930°C and 1-250°C in the reaction zone of a free-flow non-catalytic gas generator.
A method for producing a gas mixture containing H ₂ and CO by partial oxidation with a gas containing free oxygen under conditions of absolute atmospheric pressure, the method comprising: and a second heat exchange region to remove sensible heat from the outflow gas stream, and the sensible heat stolen in the second heat exchange region is used to convert the water flow by indirect heat exchange. The steam is converted into steam at a temperature of 150 to 375° C. and at an absolute pressure of 4 to 260, and is sent from the second heat exchange zone to a third heat exchange zone, which is connected to the first and second heat exchange zones. Sensible heat is transferred from the first heat exchange zone by a heat transfer fluid circulated between a third heat exchange zone, where the steam is transferred to the flow of the heat transfer fluid. Using the sensible heat emitted in the first heat exchange zone, at least a portion of the steam is heated to a temperature of 400 to 600° C. and 4 to 260 atmospheric pressures absolute by superheating by indirect heat exchange with The heat transfer fluid is sodium, potassium, mercury, sulfur, or hydrogen obtained from the effluent product gas by heat exchange followed by purification, water gas reaction, and purification, and the heat transfer fluid is converted into superheated steam. A method for producing a mixed gas, characterized in that at least a part of the mixed gas is introduced into a reaction region of a gas generator as a carrier for fuel to be supplied to the gas generator.