A method and apparatus for accelerated reforming fuel with oxygen

 

(57) Abstract:

The invention relates to a method and apparatus for obtaining deformirovannykh gases. Natural gas and oxygen is burned in the burner at the first stage to obtain carbon dioxide and water. The combustion products are served on the second stage in an elongated mixing tube. Moreover, the mixing tube open circuit deformirovannykh gases to the furnace. Through the injector inject the mixture of the second stream of gaseous hydrocarbon and oxygen in the second stage for reaction with the products of combustion from the first stage to obtain deformirovannykh hydrogen and carbon monoxide that comes from the mixing pipe and enter the path deformirovannykh gases. Gas and oxygen to hydrogen is injected at the second stage and mixed with the combustion products to interact with carbon dioxide and water to form a carbon monoxide and hydrogen. The method and apparatus are particularly suited for use of the obtained reformed gas as a complement to install direct reduction of iron in which the iron ore is reduced to iron in a shaft furnace. The method and apparatus can also be used to obtain heated enriched natural gas for use in caches can be used as a means of regulating the temperature of the reformed gas, fed into the shaft furnace. The invention improves the performance of the installation. 3 S. and 26 C.p. f-crystals, 6 ill., table 2.

The invention relates mainly to a method and apparatus for obtaining deformirovannykh gases. More specifically, the present invention relates to a method and apparatus for obtaining deformirovannykh gases to improve the performance of existing reforming devices, producing reformed gases.

Methods of obtaining deformirovannykh gases are widely used all over the world and find particular application in connection with installations of direct reduction iron (DRI). In DRI plants in large quantities using reformed gases for reduction of iron ore (FeO) iron (Fe) within shaft furnace. Received in the shaft furnace iron is then processed into steel of various grades for the production of such products as wire, rods, beams, etc.

Reformirovanie gases used in shaft furnaces, basically, is a mixture of hydrogen (H2) and carbon monoxide (CO) in a typical aspect ratio of 1.5: 1, respectively. These past reforming gases (H2and participate in the shaft furnace in the following reactions, metallical the shares show 400 m3WITH or H2react with iron oxide (FeO) for education 400 m3CO2or H2O to obtain each metric ton of iron recovered from FeO. Chemical calculations require that the ratio of reductants (CO+H2to oxidants (CO2+H2About) was greater than about 2:1 before any reaction recovery. So reformirovannoy gas flowing into the shaft furnace must have a sufficient number of reducers to ensure the conversion of 400 m3reductants in oxidants per ton of iron, and also be relevant reducing agents oxidizing agents 2: 1 after all FeO will be restored in Fe.

The metallization process is performed in a shaft furnace in which the iron oxide is fed from above into the hopper and is distributed in the furnace by using multiple distribution terminals. Shaft furnace has three zones, in which the process: reduction zone, transition zone and cooling zone. The furnace is provided basl (the section with the largest diameter), which has openings connected to the bottom part of the recovery zone through which gases from Basle go into the oven for passing up through the layer of ironstone (N2and WITH) plus CO2H2O and enriched natural gas. Typical gases coming from base are as follows: CO2=2,5%; CO=38,0%; H2=56,0%; CH4=2,0%; N2=1,5%.

Nitrogen is present from the air penetrating into the reaction zone at different points, and also due to the fact that the natural gas used in the process may contain up to 2% nitrogen. The typical temperature of the gas coming from Basle approximately 1650oF (898,9oC). This temperature is achieved after adding enriched gas in reformirovannoy gas from the reforming device.

Enriched with natural gas is injected to obtain a carbon source in the reaction zone. It provides an introduction of the carbon in the iron in the reaction zone via the following reaction carburizing:

3Fe+CH4-->Fe3C+2H2< / BR>
This reaction is endothermic and reduces the temperature of the layer of iron oxide. Number of loaded iron oxide, the temperature coming from base gases, the relation of H2/CO and the number deformirovannogo gas CO2to a large extent govern in a control loop. The most effective control technologies ogle of base gas. Many plants operate when the content in the area of recovery from about 2.5 to 3.5% SN4in coming from base gas and from about 20.0 to 50.0% of CH4in the cooling zone. However, the introduction of CH4as enriched gas in reformiruetsya gases entering basl, tend to reduce the temperature coming from base gases, which makes it difficult to regulate the temperature coming from base gases.

The traditional process of obtaining deformirovannykh gas installations DRI (direct reduction iron) perform in the reforming devices supplied gaseous hydrocarbons such as natural gas, methane, propane, etc. react with H2And CO2(at approximately from 1900 to 2000oF (1037,8-1093,3oC)) in the presence of a catalyst to obtain reductants CO and H2(see EN 2069090).

Central to the equipment takes a furnace comprising a casing with a refractory lining, filled with a catalyst containing tubes reforming device. Fuel is burnt in the casing at a pressure slightly above atmospheric, while the mixture of natural gas, H2And CO2passed through tubes containing pellets can produce the same time, they are endothermic (requires heat) and require a catalyst to accelerate the reaction of the reformer. Therefore, the casing has multiple burners to obtain the necessary heat.

The feed gas (natural gas, methane or propane) into the tubes of the reformer from an external source, whereas CO2served in the tubes of the reformer in the form of furnace exhaust gas from the shaft furnace. The required amount of water (H2O) is introduced to the feed pipe for reforming gas mixture. The feed gas, N2And CO2mixed and heated in the completed catalyst tubes for reforming to call in the pipes for reforming the following two reactions reforming:

CH4+CO2-->2SD+2H2;

CH4+H2O-->+3H2.

Typical reformirovannoy gas coming out of the pipes for the reforming gas has a temperature of approximately 1700oF (926,7oC) and the following composition (anhydrous basis): N2=58,0%; CO2=2,5%; CH4=0.5% and N2=to 1.0%. Quality deformirovannogo gas is determined by the ratio of reductants (H2O+CO) to oxidants (CO2+H2O), the higher the ratio, the better. A typical ratio wasswa and velocity deformirovannogo gas is affected by various factors. Such factors include the performance of the reforming device, the temperature in the pipes of the reforming device and the size of the burner reforming device. If the performance of the reforming device (flow rate deformirovannogo gas) increases above the design capacity of the reforming device, the heat load developed burners reforming device also increases. As the heat load increases, the catalyst in the center of the pipe reforming device becomes colder because of the increased heat consumption, exhaust through the pipe. Cooler catalyst tends to increase the potential unwanted deposits of carbon in the tubes, thus reducing the overall performance of a reforming process. The excess in the process of project performance can significantly affect both the quality (composition), and the flow rate deformirovannogo gas.

By increasing the temperature in the reforming device will also increase the temperature of the pipes. This may cause thermal stress and possible deformation or damage of the material (usually silicon carbide tubes reforming device. Damage to the pipe reforming device can Visva for some fire power and burning characteristics. The combustion of fuel in excess of the design capacity of the reforming device, can lead to unacceptable temperature profile along the length of the pipe reforming device and to a possible overheating of the refractory material of the furnace shell reforming device. The reforming device is typical limit of 2200oF (1204oC). Unacceptable temperature profile can affect the activity of the catalyst and the flow of the reformer in the pipe and result in deterioration of the quality of deformirovannogo gas. This can lead to reduced speeds metallization in the shaft furnace and/or to receive the recovered iron low quality.

Based on the above most installations of direct reduction of iron are not able to increase their production deformirovannykh gases from the reforming device above its performance. On the other hand, as a rule, the shaft furnace there is a possibility to increase from 20% to 30% release of the restored iron, if it were possible to additionally submit reformiruetsya gases to flow in the furnace reactions metallization. If you want to improve the performance of the shaft furnace installation, the following solutions are possible: either install to install n. None of these solutions is not advantageous from the viewpoint of cost. The cost of a new set of pipes and reforming furnace installation requires millions of dollars of investment, and these new pipes may not always be necessary because of market demand and the overall flexibility of the production cycle. Procurement of recovered iron from another manufacturer is subject to fluctuations in market prices and availability, and also not a satisfactory solution to increase the production of recovered iron.

Proceeding from the above, it is necessary to find a relatively low-cost solution to increase production deformirovannykh gas demand to increase production recovered iron when there is market demand for it, and so you can reduce the productivity of existing reforming device, when market conditions dictate a reduction in output.

Based on the above objective of the present invention is to provide a simple device for obtaining deformirovannogo gas and method of manufacturing deformirovannykh gases.

Another objective of the present invention is to provide a device and SP the production capacity of existing gas reforming device.

A further object of the present invention is to provide a device and method of producing deformirovannogo gas for use in installations of direct reduction of iron for more deformirovannykh gases to improve the performance of existing reforming devices.

Another object of the present invention is to provide a device and method of producing deformirovannogo gas, which can be used in conjunction with existing gas reforming device for temperature control fully deformirovannykh gases.

Another object of the present invention is to provide a device and method of producing deformirovannogo gas for use in installations of direct reduction of iron for more deformirovannykh gases to improve the performance of existing reforming device and which can be used for temperature control fully deformirovannykh gases.

Another object of the present invention is to provide a device and method of producing deformirovannogo gas for use in installations of direct reduction of iron to obtain dopeeee can be used to regulate the quantity of enriched natural gas, to be feed into the furnace of the recovery of iron.

These and other objectives of the present invention are solved in that in the method of obtaining deformirovannykh gases according to the invention sets the mixing pipe in such a place that it was surrounded by existing reformed gases ignite the mixture of the first stream of gaseous hydrocarbon and oxygen in the first stage to obtain the burning gases, serves referred burning gases to the second stage in the axial direction, introducing a second stream of gaseous hydrocarbon and oxygen at the second stage in a direction coaxial with the said burning gases, provide the reaction of burning gas with a second stream of gaseous hydrocarbons in the second stage to obtain deformirovannykh hydrogen and carbon monoxide, and supply the received deformirovannykh hydrogen and carbon monoxide from the mixing pipe in existing reformed gases. Gaseous hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture.

At the first stage by means of ignition, provide carbon dioxide and water, which serves to Deut is odorata and oxygen is introduced into the mixing pipe in the form of a vortex flow and use the heat existing deformirovannykh gases for ignition of the first stream of gaseous hydrocarbon and oxygen in the first stage. Then provide cooling of the first stage, which is the ignition and carry out pre-heating the second stream of gaseous hydrocarbon and oxygen prior to its introduction into the second stage.

Perform pre-heating the second stream of gaseous hydrocarbon and oxygen before putting them on the second stage and use the pre-heated gaseous hydrocarbon and oxygen before their submission to the second stage for cooling the first stage.

The task is solved in that in the method of additions number deformirovannykh gases used in installations of direct reduction of iron, in which the primary reformirovannoy the gas is fed into the furnace from the main reforming device and passed through the iron ore for iron, according to the invention ignite the mixture of the first stream of gaseous hydrocarbons and oxygen in the first stage to obtain carbon dioxide and water, serves dioxide and water in the second step, introducing a second stream of gaseous hydrocarbon and oxygen in the second stage, provide the reaction of carbon dioxide and water with the second portion of the gaseous hydrocarbons in the second stage to obtain wtorek the primary circuit deformirovannogo gas in the furnace. Gaseous hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture. However, the second stage is performed in the mixing tube located in the primary circuit deformirovannogo gas to be fed into the furnace, and a second thread mentioned gaseous hydrocarbon and oxygen is introduced into the mixing pipe in the form of a vortex flow.

The mixing tube is installed in the present collector, containing reformed gases from the main reforming device, and, in addition, involves the use of heat from the audience deformirovannykh gases to initiate the initial ignition of the first stream of gaseous hydrocarbon and oxygen in the first stage. Additional gaseous hydrocarbon is injected in the second stage to obtain enriched natural gas for use in the process of direct reduction of iron. The number of enriched natural gas deformirovannom gas regulate when feeding into the furnace through the electoral changing the volumetric flow rate of the second stream of gaseous hydrocarbons in the second stage, and the temperature and/or the number riforme first stream of gaseous hydrocarbon and oxygen in the first stage and/or volumetric flow rate of the second stream of gaseous hydrocarbons in the second stage.

The problem is solved also by the fact that the gas reforming device for receiving deformirovannykh gases according to the invention includes a burner for burning a mixture of the first stream of gaseous hydrocarbon and oxygen in the first stage for receiving the products of combustion, an elongated mixing tube provided for the second stage, in which the said combustion products is served in the axial direction, and the mixing tube open circuit deformirovannykh gases to the furnace, and a nozzle for introducing a mixture of the second stream of gaseous hydrocarbon and oxygen in the second stage for reaction with the products of combustion from the first stage to obtain deformirovannykh hydrogen and carbon monoxide, coming from the mixing pipe and enter the path deformirovannykh gases. When the hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture. The burner includes a mixer with Venturi nozzle including a Venturi nozzle having a diverging portion that is open in the mixing pipe, the camera near the Venturi nozzle for receiving the second stream of gaseous hydrocarbon and oxygen, and the camera is open ng device includes a vortex nozzle in the mouth of the chamber in the mixing pipe for a message vortex motion to the second stream of gaseous hydrocarbon and oxygen as it is received in the mixing tube, moreover, the mixing tube has a refractory lining.

The burner includes a tube having a nozzle at its front end for receiving the first stream of gaseous hydrocarbon, and a tube surrounding the first chamber for receiving the first stream of oxygen, and the combustion chamber immediately before the nozzle, open the mixing pipe, a tubular cooling jacket surrounding the combustion chamber and cooling jacket has an inlet channel and outlet channel for the passage of cooling medium into and out of the cooling jacket, and the nozzle of the burner pipe and the chamber opened into the combustion chamber for passing the first stream of hydrocarbon and oxygen in the combustion chamber for combustion therein, a second chamber for receiving the second stream of gaseous hydrocarbon and oxygen and having a mouth in the mixing pipe below along the flow from the combustion chamber for passing a second stream of gaseous hydrocarbon and oxygen in a mixing pipe for mixing with the combustion products from the combustion chamber, and also includes a vortex nozzle at the mouth of the second chamber inside the mixing pipe for a message vortex motion to the second stream of gaseous hydrocarbon and oxygen as it is received in the mixing pipe.

In addition, the burner includes a pipe burner for connection to a source of the first stream of gaseous hydrocarbon and having a nozzle at its lower end in the course of the flow chamber surrounding the pipe burner for connection to a source of the first flow of oxygen and having a nozzle at its lower end in the course of a stream and the said nozzles open into the combustion chamber, while the mixing tube has many passing longitudinally annular channels extending in the axial direction in the mixing pipe, and the channels include a first external channel, passing forward in the mixing pipe, water return channel, attached to the outer channel and passing back into the mixing tube, and the inner channel attached to the return channel at its rear end and open on the inside of the mixing tube at its front end in place, separated by an interval in the axial direction behind the front end of the mixing pipe, while the inner channel surrounds the combustion chamber, the outer channel has an input means of the second flow of gaseous hydrocarbon and oxygen inside the channel near its rear end, the second stream of hydrocarbon and oxygen passes through the said channels and enters smesitel vortex nozzle at its mouth above in the course of the stream from the nozzle for a message whirl first stream of oxygen as it passes through the nozzle into the combustion chamber.

When the hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture, and the burner includes a tube having a nozzle at its front end for receiving the first stream of gaseous hydrocarbon, and a tube surrounding the first chamber for receiving the first stream of oxygen, and the combustion chamber located in front of the nozzle and open into the mixing pipe, the nozzle and the first chamber open into the combustion chamber for passing a first stream of gaseous hydrocarbon and the first stream of oxygen into the combustion chamber for burning.

The present invention is further explained in the detailed description and the accompanying drawings, on which:

in Fig.1 is a diagram of a typical installation of direct reduction of iron that includes a shaft furnace and a reforming device for direct reduction of iron using deformirovannykh gases;

In Fig.2 is a diagram showing the present invention used in connection with the shaft furnace and the reforming device shown in Fig. 1;

In Fig. 3 is a diagram of the device of accelerated reforming oxygen fuel (OFBR) and technological process in the STS accelerated reforming of oxygen with fuel, included in the composition of the present invention, showing the reforming device in the collector (the collector) deformirovannykh gases;

In Fig.5 shows a cross section of a second variant of the device of accelerated reforming of oxygen with fuel in accordance with the present invention, showing the reforming device installed in the manifold deformirovannykh gases; and

In Fig. 6 presents a cross section of a third variant of the device of accelerated reforming of oxygen with fuel in accordance with the present invention, showing the reforming device installed in the manifold deformirovannykh gases.

On the drawings and in particular Fig.1 and 2 shows the diagram of a method and apparatus for direct reduction of metal oxides, such as iron ore, which is particularly suitable in the present invention. Shows the method and the device are typical industrial device and method used in many installations of direct reduction iron (DRI). The device may include a shaft furnace 2, in which iron ore (FeO) is reduced to iron (Fe) using deformirovannykh gases. Reformed gases get in the reforming device 4 and Pogranichny hopper 10, from which iron ore 12 serves in the metering hopper 14, and from which it dissipate in the furnace 2 through the distribution of rods 16. Shaft furnace 2 has three zones: zone recovery "And" generally cylindrical shape, the transition zone and the cooling zone. Basl shaft furnace 6 is an elongated section that is located approximately in the middle part of the furnace 2, and has a few channels 18 located around its inner perimeter, and a hole in the center of the furnace 2 near bottom zone recovery "And". Near the top of the furnace 2 is provided upper outlet 20 for gas, which gas exits the top of the furnace 2. For intake of cooling gas in the cooling zone "C" are provided with appropriate inlet 22 for the cooling gas. Near the top of the cooling zone "C" to release gas from the furnace is provided by the exhaust channels 24 for furnace gas, mainly carbon dioxide (CO2). In the bottom part of the furnace 2 is provided a rotary shutter 26 for gas, which is vibrating screen 28 that is designed to remove received direct recovery of chilled iron.

The reforming device 4, as a rule, represents a furnace, including the e 30 on the sides of the tubes 32 are vertically suitable burner 34 to obtain the necessary supply of heat.

The feed gas, such as natural gas, methane or other suitable gaseous hydrocarbons, enters the pipe 32 reforming device through the pipeline 36 gas supply from an external source, such as the main circuit of the installation. Typically, the feed gas is natural gas, which may contain from about 96 to 98% methane and about to 2.0% nitrogen. The feed gas is fed from its source by pipe 36 to the heater 38. Branched from the pipe 36 of the gas flow channels 40 are connected with a burner 34 for the supply of natural gas in the burner 34 reforming device. The pipe 42 from the exhaust pipe 24 of the furnace containing the pump 44 is provided for supplying furnace gas from the furnace 2 through the scrubber 46 in the pipe 36 of the feed gas before it is input to the heater 38. The pipe 36 for supplying gas comes out of the heater 38 and attached to the pipe 32 reforming device for the supply of intake gas in the pipe 32. The water supply 48 is attached to the channel 36 of the gas supply after the heater 38 and below along the flow from the pipe 32 for introduction of H2O in the gas flowing in the pipe 32. The blower 50 is attached to the pipe 52, passing through podagra the h pipe 32 reforming device, pass through the respective pipes 54 to the collector 8, where the accumulated gases from different sets of tubes 32, and then through the channel 56 submission to Basel 6 shaft furnace 2. The channel 58 is attached to the channel 56 in base 6 to add enriched natural gas to gas from the reservoir for receiving gas into basl 6. Gas from base passes through holes in Basle 6 and passes through a layer of iron oxide in the reduction zone of the furnace, as shown by the arrows.

The mixture of natural gas (or other suitable hydrocarbon, such as methane and propane) with H2O and CO2enters reforming device 4 through the pipes 32, containing an appropriate catalyst, such as Nickel or a mixture of Nickel with aluminum oxide and reacts with the generation of reductants CO and H2in accordance with the following reactions:

CH4+CO2-->2CO+2H2;

CH4+H2O-->+3H2.

Reformirovannoy gas discharged from pipe 53, as a rule, can contain 58,0% N2, 38% CO, 0.5% OF CH4, 2.5% OF CO2and 1.0% N2and to have a temperature of 1650oF (898,9oC). This reformirovannoy gas passes through the channel 56 where add-enriched natural gas for the generation of gas for base, Lesa, providing the course of the following reactions metallization in the reaction zone:

FeO+H2-->Fe+H2O;

FeO+WITH-->Fe+CO2.

After recovery, the obtained iron (Fe) flows through the transition zone In the cooling zone "C" of the furnace, where the iron is cooled by the cooling gas. Cooling gas is typically natural gas with the ambient temperature. After cooling, the obtained iron discharged through a rotary shutter 26 for gas vibrating screen 28 and is transported away from the stove.

In accordance with the present invention a device of accelerated reforming (OFBR) 60 oxygen with fuel to generate secondary deformirovannogo gas to increase performance standard or primary reforming device. (For descriptive purposes on reformirovannoy the gas obtained in the existing reforming device 4, in this description referred to as the primary reformirovannoy gas, while reformirovannoy gas, obtained using the method and device of the present invention, referred to as secondary reformirovannoy gas). The device of accelerated reforming 60 oxygen with the fuel can also be used for podemos in the shaft furnace 2, as will be described below.

As shown in Fig.2 and 3, the device of accelerated reforming 60 oxygen fuel installed below along the flow to the primary reforming device 4 in the collector 8 deformirovannogo gas. However, the device of accelerated reforming 60 oxygen with fuel in accordance with the present invention may be installed in other places so that in such places was achieved excellent mixing of the secondary deformirovannykh gases introduced from the device of accelerated reforming 60 oxygen with fuel, with the primary reformed gas. Such other places can be the location of the device accelerated reforming unit 30 of the oxygen with the fuel in Basle 6 shaft furnace for the introduction of secondary deformirovannykh gases directly into basl 6 or the location of the device accelerated reforming 60 oxygen with the fuel in the channel 56 for deformirovannykh gases that they come from the manifold 8 in Basel 6 of the furnace 2.

The device of accelerated reforming 60 oxygen with fuel to the burner 62, in which the oxygen and natural gas burners are mixed and burned. The inlet channel 64 in the reforming device 60 is equipped with inlet for natural gas for injection of oxygen into the chamber 70, surrounding the tube 66 of the burner. The oxygen comes out of the camera 70 and mixed with natural gas, and the mixture is burned, the products of combustion flow in a mixing tube 72.

The reforming device 60 also includes an inlet channel 74 (or channels) to enter deformirovannogo natural gas and oxygen in an elongated mixing tube 72, preferably through the vortex nozzle 75, in place of the lower course of the stream from the combustion gases of the burner. Reformirovannoy natural gas and oxygen is mixed with the combustion products of natural gas and oxygen burner in an elongated mixing tube 72 for receiving the reforming reactions in the mixing tube 72.

The device of accelerated reforming unit 60 in accordance with the present invention provides a two-step process of obtaining deformirovannykh gases. The first provided 76 (phase I), in which the ratio close to the stoichiometric mix and ignite the natural gas and oxygen torch with stable toplevelitem flame. The combustion of natural gas with oxygen provides the following stoichiometric reaction stage I:

CH4+2O2-->CO2+2H2O.

Burning gases after Vospominanie is respectfully in vortex form, pre-specified number deformirovannogo natural gas and oxygen, to produce the following reactions phase II:

H4+CO2-->2SD+2H2;

H4+H2About-->+3H2.

The result of the device of accelerated reforming fuel with oxygen will receive the following gases: CO, H2N2O, CH4and CO2. In the resulting gases CH4is enriched with natural gas obtained through additional quantities of natural gas to hydrogen supplied to the phase II moreover gas, which is required for the reaction occurring at stage II, and which is consumed at the same time.

Although the device of accelerated reforming fuel with oxygen and method in accordance with the present invention is described as using the supply of natural gas and oxygen as the phase I and phase II, provides that can be used in a variety of gaseous hydrocarbons such as natural gas, propane, methane, etc., and the source of oxygen may be oxygen industrial quality, air or mixtures thereof.

In Fig.4-6 shows the different variants of the device of accelerated reforming fuel with oxygen, which may be the STV accelerated reforming 80 fuel with oxygen installed in the end wall 82 of the reservoir 8 primary deformirovannogo gas and includes a mixing tube 84 with a refractory lining, attached to the wall 82 of the collector deformirovannogo gas and passing into the manifold 8. The outer tube 86 is installed in the rear end of the mixing pipe and surrounds the elongated intermediate pipe 88, which is separated from it by a radial gap and coaxial with it. In the intermediate pipe 88 is provided by the inner tube 90 and is separated from her inner radial gap and coaxial with it.

The outer tube 86 forms an annular chamber 92 surrounding the intermediate pipe 88 which is closed at its outer end corresponding partition 94. The intermediate pipe 88 is held in the axial direction from the rear end of the outer tube 86 and forms an annular chamber 96 with the inner tube 90, which is closed at its outer end corresponding partition 98.

The outer tube 86 is supplied with the first channel 100, associated with the chamber 92 for connection with a source of oxygen to hydrogen. The second channel 102 in the outer tube 86, associated with the chamber 92, is provided as a means of connection of the source of natural gas reforming chamber 92. Alternatively, natural gas may be mixed with oxygen to enter the chamber through one channel.

In the intermediate pipe 88 includes a channel 104, aligned with Ira 96. The inner tube 90 has on its outer end a channel 106 that is associated with its internal space, for connection with a source of natural gas.

On the front end of the inner tube 90 is provided, as shown, the nozzle 108 of the heat-resistant alloy steel, such as SS-310, Inconel Hastelloy, etc., the Venturi Nozzle 110, made of refractory material, is installed in the intermediate pipe 88 coaxially with the front part of the front inner end of the inner tube 90 and is located so that the neck 112 of the Venturi nozzle 110 was located in front of the inner channel of the front end of the nozzle 108 of the inner tube 90 and the diverging portion 114 of the Venturi nozzle 110 is opened in the mixing tube 84. Vortex nozzle 116 is installed, as shown, between the outer tube 86 and the intermediate pipe 88, and the Venturi nozzle 110 is coaxially and forth for a short distance beyond the vortex nozzle 116 inside the mixing pipe 84. Vortex nozzle may be in the form of angled vanes or ribs installed on the perimeter of the front end of the chamber 92 between the outer tube 86 and the intermediate pipe 88. Vortex nozzle 116 is preferably made of stainless steel and has the shape of a spiral naprave four to six blades depending on the size of the device accelerated reforming 80 fuel with oxygen.

In accordance with the variant shown in Fig.4, the natural gas flows through the channel 106 in the inner tube 90 and passes through the nozzle 108 in the neck 112 of the Venturi nozzle 110. The oxygen flows through the channel 104 in the chamber 96 between the inner tube 90 and the intermediate pipe 88, and then passes into the neck 112 of the Venturi nozzle. The area of the exit nozzle 108 and the area of the passage at the end of the chamber 96 is chosen so as to obtain a relatively high rate of introduction of gas burners and oxygen burner in the neck 112 of the Venturi nozzle 110, which is approximately 220 to 800 feet per second (64,01-243,8 m/sec).

Oxygen and natural gas burners faced each other in the neck 112 of the Venturi nozzle 110, providing the conditions of good mixing. Diverging portion 114 of the Venturi nozzle 110 preferably has a length of approximately 2-4 times the diameter of the neck 112 and is designed for mixing oxygen and natural gas and education toplevelitem flames zone 118 of phase I. the Flame initially occurs when ignited, the mixture of the oxygen-natural gas in region 118 diverging portion 114 of the Venturi nozzle 110 by the heat and the physical mixing of the surrounding primary deformirovannogo gas in the reservoir surrounding in the range from about 1600 to 1700oF (871,1-926,7oC). Phase I is preferred flame with very little visible radiation, in the course of which the reaction of stoichiometric quantities of natural gas and oxygen to produce water and carbon dioxide. In the variant shown in Fig.4, the Venturi nozzle preferably made from a refractory material due to high temperature toplevelitem flame. At higher heat capacity (more than 2 million British thermal units per hour (1,055106kW/h)), you should use water-cooled mixing Venturi nozzle. When such increased heat capacity of the gas nozzle 108 may be equipped with a number of axial holes to improve mixing with the surrounding oxygen flow.

Natural gas or other gaseous hydrocarbon and oxygen are available on their respective channels 102 and 100 in the chamber 92 with the exact ratio. Oxygen and natural gas out of the chamber through the gas jet nozzle 116 inside the mixing tube 84 in an area of 120 stage II front end of the Venturi nozzle 110. Vortex nozzle 116 performs two functions. First, it must provide sufficient swirling motion of the mixture gas of oxygen to ensure any, she should wash the inner surface 122 of the mixing pipe 84 for cooling, which is necessary due to thermal emission of the combustion products of phase I due to their high temperature.

The mixing zone 118 phase I and combustion take place, essentially, in the diverging portion 114 of the Venturi nozzle 110. The mixing and reaction zone 120 phase II begin and flow in a mixing tube 84 immediately below in the course of the stream from the front end of the Venturi nozzle 110. As noted earlier, the gaseous products of combustion phase I react with a mixture of natural gas and oxygen on phase II with the formation of secondary deformirovannykh gases - carbon monoxide and hydrogen. These gases come from the mixing tube 84 in the manifold 8 deformirovannykh gases and complement the primary reformed gases flowing into the shaft furnace 2.

In Fig. 5 shows a second variant of the device of accelerated reforming 150 fuel with oxygen, embodying the present invention. As in the previous embodiment, shown reforming device 150 is installed in the wall 82 of the reservoir 8 primary deformirovannogo gas. The reforming device 150 includes a mixing pipe 152 refractory lining attached to the wall 82 collegiales pipe 152 and surrounds the elongated cooling jacket 156, which is separated from the mixing pipe 152 radial gap and coaxial with it. The inner tube 158 is provided a cooling jacket 156 and separated from her inner radial gap and coaxial with it.

The outer tube 154 forms an annular chamber 160 around the cooling jacket 156, which is closed at its rear end by a corresponding partition wall 162. The cooling jacket 156 passes in the axial direction from the end of the outer tube 154 and forms a chamber 164 with the inner tube 158, which is closed at its rear end of the respective wall 166.

The cooling jacket 156 may be formed by the outer tube 160 cooling shirts, coaxial with the outer tube 154 and separated from the outer tube 154 internal radial gap to form with it an annular chamber 160. As shown, the outer tube 168 cooling jacket is in the mixing pipe 152 beyond the front end of the outer tube 152. The inner tube 170 of the cooling jacket of smaller diameter than the outer tube 164 of the cooling jacket, is provided inside the outer tube 168 cooling shirts and coaxially with it for education between them an annular gap. Intermediate pipe 172 coolant jacket located between the through channels 174 and 176, respectively. The front ends of the inner and outer tubes 170 and 168 of the cooling jacket are interconnected by a trailing element 178. Intermediate pipe 172 of the cooling jacket is separated from the backside a gap in the axial direction from the trailing element 178 so as to form a communication between the inner and outer annular channels 174 and 176 on the front end of the cooling jacket 156. The outer channel 176 is closed at its rear end closing element 180, passing radially from the rear end of the outer tube 168 of the cooling jacket to the wall of the intermediate pipe 172 jacket water cooling. The rear end of the inner channel 174 is closed by a closing element 182, which is located between the rear end of the tube 172 of the cooling jacket and the inner tube 170 of the cooling jacket.

The inlet channel 184 cooling medium associated with the internal channel 174, is provided in the wall of the intermediate pipe 172 cooling jacket near its rear end and is located behind the trailing element 180 of the outer channel 176. Outlet 186 cooling medium provided in the wall of the outer tube 168 cooling jacket near its outer end and is connected with an outer channel 176. With this design, the end of the channel 174, flow forward through the internal channel 174, around the front end of the intermediate pipe 172 of the cooling jacket and back through the outer channel 176 to the outer channel 186, where it exits the cooling jacket 156.

The outer tube 154 is provided first channel 188 associated with the chamber 160 for connection with a source of oxygen to hydrogen. The second channel 190 in the outer tube 154, which is also connected with the chamber 160, is provided as a means of communication source of natural gas reforming chamber 160. Alternatively, natural gas can be mixed with oxygen and feeding into the chamber through one channel.

In the wall of the inner tube 170 of the jacket water cooling provides a channel 192 in alignment with the rear end of the intermediate pipe 172 jacket water cooling associated with the chamber 164 for connection of a source of oxygen torch with camera 164. The inner tube 158 has at its outer end channel 193 associated with its internal space for connection with a source of natural gas.

As shown, the front end of the inner tube 158 ends at a point separated by a gap from the rear side of the front end of the inner tube 170 cooling jacket 156. On the front inner end of the inner tube 158, 194. Vortex nozzle, similar to the vortex nozzle, described in accordance with the variant shown in Fig. 4, is installed, as shown, between the inner tube 158 and the inner tube 170 of the cooling jacket on the front inner end of the chamber 164. Also provided swirl nozzle 200 at the front end of the chamber 160 located about the outer tube 168 cooling shirt.

In the design of the reforming device, as shown in Fig.5, the oxygen burner flows through the channel 192 inside the chamber 160 and exits the chamber 160 through variou nozzle 198 in an area of 196 stage I, having a swirling motion. Natural gas flows in the inner tube 158 channel 193 and passes through the nozzle 194 in the mixing zone 196 of phase I, is mixed with a whirling moving oxygen. The rate of introduction of gas may range from 220 to 800 feet per second (64,01-243,8 m/sec). The heat from the initially recovered gases from the manifold 8 ignites the mixture of oxygen with the fuel in the zone 196 of phase I in place immediately before the nozzle 194 with the formation of high-temperature toplevelitem flame inside the cooling jacket 156. Natural gas and oxygen react in stoichiometric ratio with the formation of water and carbon dioxide.

High heat capacity of the mixing zone phase I (natural gas and oxygen torch) provided by the water-cooled combustion chamber (phase I). It is also designed to stabilize the combustion, so that the area of the mixing phase I functioned at a relatively higher temperature of the burning gas.

The third variant of the device of accelerated reforming 250 topcasino, the reforming device 250 is installed in the wall 82 of the reservoir 8 primary deformirovannogo gas existing installation of direct reduction of iron DRI. In this embodiment, natural gas and oxygen to hydrogen is preheated before feeding into phase II. The mixing tube 252 is attached to the wall 82 of the reservoir 8 deformirovannogo gas and goes inside it. The design of the mixing pipe 252 provides for the installation of the heater 254, intended for reforming gas. The mixing pipe 252 includes an outer tube 256 heater, which passes through the wall 82 of the reservoir 8. The outer tube 256 heater is located around the inner pipe 258 heater, which has a diameter smaller than the outer tube 256 heater, and coaxially with it. Intermediate pipe heater 260 is located between the inner and outer longitudinally passing through the annular channels 262 and 264, respectively. The front ends of the inner and outer tubes 258 and 256 heater connected closing element 266. The inner end of the intermediate pipe 260 heater on the back side separated by a gap from the trailing element 266 so that between the inner and outer channels 262 and 264 existed swany of heat-resistant alloy steel, such as SS-310, Inconel, Hastelloy, etc.,

Pipe 268 phase I of smaller diameter than the inner tube 258 heater, passes through the inner tubes 258 heater coaxially with it, forming an annular exhaust channel 270 heater 254 between its outer wall and

the inner wall of the inner tube 258 heater. The trailing element 272 passes from the rear end of the outer tube 256 heater to the outer pipe wall 268 of phase I, while the rear end of the intermediate pipe heater 260 is attached so that it closes the external channel 264. The rear end of the inner tube 258 heater is separated by a gap from the trailing element 272 so that the inner channel 262 and the inlet channel 270 is interconnected. The front end of the intake channel 270 can be provided by vortex nozzle 273.

The outer tube 256 heaters provided for the first channel 274 linking with external channel 264 heater, for connection of a source of oxygen to hydrogen, with an external channel 264. The second channel 276 the outer tube 256 heater is provided as a means of connection of the source of natural gas reforming with external channel 264. Alternatively, natural gas and oxygen can be mixed and served in the has a smaller diameter than the pipe 268 phase I, for the education of the camera 280 between the pipe 268 phase I and the inner pipe 278 burner. The trailing element 282 passing between the rear end of the tube 268 phase I and the outer pipe wall 278 of the burner causes the rear end of the camera 280.

In the wall of the pipe 268 phase I includes a channel 284, coaxially with the rear part of the trailing element 272 associated with the camera 280, for attachment of a source of oxygen burner to the camera 280. Inner tube 278 burner at its outer end has a channel 286 associated with its internal space, for connection to a source of natural gas.

In the pipe 268 phase I in the middle of its length and the front end is provided by the nozzle 288. The design of the nozzle preferably includes obtaining in the field mixing of phase I in front of the tube 268 phase I speed the introduction of oxygen in the range from approximately 200 to 400 feet per second (60,96-121,92 m/sec). The front end of the camera 280, immediately behind the rear end of the nozzle 288, provided the vortex nozzle 292, for a message swirling motion to the flow of oxygen to enter into the zone 290 phase I. The vortex nozzles can be used spiral blades having an angle ranging from 10o45orelative to the longitudinal axis.

In the design of the reforming device, as shown in Fig.5, natural gas burner passes through the channel 286 in the pipe 278 burner and comes out of the tube 278 burner through the nozzle 294 in an area of 290 phase I. the Oxygen burner into the chamber 280 through the channel 284 and passes through the vortex nozzle 292 and nozzle 288 in the area of phase I within the front part of the tube 268 phase I. Oxygen after the vortex nozzles 292 becomes slightly twist as it enters the zone of phase I, and is mixed in this area with natural gas. A gaseous mixture of oxygen-natural gas is ignited from the heat in the collector 8 gases for reforming education stable toplevelitem flame in the area of phase I.

Natural gas and oxygen to hydrogen, enter the heater 256 on their respective channels 274 and 276 and pass forward through the external channel 264, go back through the internal channel 262, again change direction and go forward channel 270 in the mixing zone 296 phase II immediately before the front end of labor is preliminary heated with natural gas and oxygen to initiate the reforming reaction to obtain deformirovannykh gases, then out of the front end of the mixing pipe 252 to the collector 8.

In the variant shown in Fig.6, natural gas and oxygen to hydrogen is pre-heated before it is supplied into the zone 296 phase II to improve the efficiency of the reformer. As shown in the drawings, the mixing pipe 254 heater is inserted into a manifold so that a significant portion of the external surface of the heater in contact with the heated Reformirovanie gases for utilization of heat. The ratio of the length of the mixing tube to the diameter (L/D) supported in the range of about 3 to 9, depending on the existing space inside the collector to deformirovannykh gases or other places, such as Basel shaft furnace, to obtain a sufficient amount of time of the presence of gases in phase II to complete the reaction.

The entire process in accordance with the present invention is divided into two phases, phase I and phase II. In the process of mixing and combustion phase I pre-specified number of oxygen and natural gas at close to the stoichiometric ratio (2: 1) mix and burn when using a mixing device of the first stage. Thanks to the nozzle device here fuss is aceteline length passes into the reservoir gases of the primary reformer.

A stoichiometric mixture of oxygen and natural gas in the area of phase I is first ignited by contact with the primary Reformirovanie gases in the manifold. Reformed gases in the manifold typically have a temperature of 1700oF (926,7oC) and a gauge pressure of 15 pounds per square inch (103,43 kPa). Through the use of the sensing element 300 of combustion (see Fig.3), such as ultraviolet sensor, the led burning or thermocouple, it can be adjusted to obtain and maintain in the mixing pipe is highly stable combustion. The content of the products of combustion of fuel with oxygen is mainly CO2(33,3%) and H2O (66,6%) by volume, and peak temperature of the products of combustion are in the range from 4000 to 4500oF (2204,4-2482,2oC). Material mixing pipe variants shown in Fig. 4 and 5 (steel with a refractory lining, stainless steel or Inconel) not designed for operation in this temperature range for an extended period of time. It is therefore necessary that the mixing and reaction of stage II proceeded as quickly as possible.

In the process of mixing and reactions of phase II pre-specified number of natural g is Orada mixed with natural gas as a catalyst to initiate the reforming reactions inside the mixing pipe. Swirling motion at the input of natural gas and oxygen in the area of phase II has two functions. First, swirling the mixture cools the inner surface of the mixing pipe and the protection of the refractory lining of the mixing tube from thermal damage. Secondly, it is used in the reaction phase II products of combustion phase I CO2and H2About that have substantially higher temperatures, react faster with gas CH2and O2reforming getting deformirovannykh gases (H2and WITH), and preheated methane (CH4).

The ratio of length to diameter (L/D) of phase II of the mixing pipe is chosen for [certain] time presence at the reactions of reforming. The mixing tube acts as an insulating pipes to prevent premature mixing of the combustion products of phase I and gases for reforming stage II with external gases in the manifold, resulting in essentially all the oxygen to hydrogen is involved in the reactions inside the mixing pipe. The relationship L/D from 3 to 9, usually enough for a good mix between the products of phase I and gases for reforming stage II.

Some of the bundle is moved in the enriched gas to a shaft furnace. The presence of enriched natural gas at the second stage allows you to efficiently regulate the temperature and carbon content in the whole mixture deformirovannykh gases entering basl shaft furnace, thereby providing regulation by the reforming device in accordance with the present invention, the carburizing reaction in the reaction zone of the shaft furnace. By changing the amount of excess natural gas to be fed to the phase II, you can change the number of enriched natural gas that is present in all submitted deformirovannykh gases (primary and secondary).

The composition of the gas obtained in the device of accelerated reforming fuel with oxygen in accordance with the present invention is very similar to the composition of the gases produced in the reforming device, as for the relationship (H2+CO/H2O+CO2), and the relationship of H2/CO. Thus, the reformed gases such quality produced using the device and method in accordance with the present invention with the additional advantage associated with the presence of preheated methane (as enriched natural gas in the amount of from 3 to 4% vol.) throughout the composition deformirovannogo ity in the introduction of cold enriched methane (natural gas) in reformirovannoy gas before introduction into Basel. In addition, the presence of excess gas in the mixing phase II also provides accurate control over the entire temperature range deformirovannykh gases, and also provides a cooling medium for the material of the mixing pipe.

In table I below is an example of the respective volumetric flow rates of the gases and the performance of the process of direct reduction iron (DRI) for a typical installation for direct production of iron using primary deformirovannogo gas from the reforming installation device. The table shows the results of simple calculations, the number of necessary additional deformirovannogo gas receivable in the device of accelerated reforming fuel with oxygen (OFBR) in accordance with the present invention for achieving the full effect of increasing plant performance DRI. The data in table I is designed to increase performance (or speed metallization) shaft furnace, producing 70 tons/hour, 5 tons/hour. The flow of gases in table I are given in standard cubic feet per hour (1 cubic foot per hour=0,028 m3/hour).

To simplify the number deformirovannogo gas in table I was the This is a simplified (and comprehensive) view of the combined reactions of phase I and phase II are described here. As you can see from this equation for the reaction of one volume of reagents is obtained 2 volume deformirovannykh gases.

The method using the device of accelerated reforming fuel with oxygen (OFBR) is a two-step process in which all natural gas and all the oxygen is burned in stages and not all together, as shown in the above chemical equation. In table I it is assumed that this (existing) composition deformirovannogo gas (dry volume) includes H2= 58%, SD= 38%, CO2= 2,5%, SN4=0.5% and N2=to 1.0%. In addition, it was also suggested that the process of reforming OFBR is 100% effective and that all natural gas and oxygen to hydrogen into CO and2. It should be clear that the real process is not 100% effectiveness, and efficiency of the reformer ranges from approximately 50 to 90%.

In the following table II shows the preferred ranges and the percentage of volumetric flow rates of natural gas and oxygen when performing phase I and phase II of the process using the device of accelerated reforming fuel with oxygen. Velocity is given as the set value and may vary significantly from the ranks deformirovannykh gases in the installation and from the whole process. With regard to table II, it is assumed that the performance of the direct reduction of iron increases by 5 tons per hour and the basic requirements of the process in accordance with table I are performed effectively.

When using the data of table II as standard in one example, the method and device in accordance with the present invention adjusted combustion in the burner phase I, approximately 25% of the total natural gas using the device of accelerated reforming fuel with oxygen consumption and oxygen burners mounted in the amount close to the stoichiometric proportion. Consumption of natural gas for reforming established in the amount of 75% of the total natural gas used in the process. The flow of oxygen to hydrogen, established in the amount of 20% of the total amount of oxygen used in the system. Volume deformirovannykh gases obtained through a system OFBR, set as 5% of the total deformirovannogo gas. The number of enriched natural gas are shown in table II, but, for example, could amount to 25,000 standard cubic feet per hour (scfh) (700 m3/hour), approximately half of the natural gas reforming. The operator mouth is formirovanija gas and carbon content during the process of direct reduction of iron.

Depending on the design of the mixer (burner) phase I, the peak temperature of combustion products oxygen-natural gas (33% CO2and 66.6% H2O) phase I are relatively high and can range somewhere from about 3500oF (1926,7o(C) up to 4500oF (2482,2oC). The oscillation is related to the construction of the mixer stage I. If it is preferable for the mixing of oxygen with natural gas, you get an adiabatic (theoretical maximum) temperature of the gas. If you use the burner to the mixing nozzle, you get a relatively lower temperature combustion gas, from about 3500oF (1926,7o(C) up to 4000oF (2204,4oC). The process of mixing and mixer stage I should be chosen carefully, based on the material node of the mixing pipe below along the flow. The mixing tube with a refractory lining allows higher peak flame temperature, while mixing stainless steel pipe will require a relatively lower temperature of the burner with a nozzle for mixing the fuel with oxygen during the mixing phase I.

Phase II natural gas and oxygen to hydrogen comes whirling in the form of a surrounding p 2-->2SD+2H2;

CH4+H2O-->+3H2.

If you reach the right mix deformirovannykh gases, as in the use of the vortex nozzle and the mixing tube with the correct ratio of length to diameter, the products of the reactions of phase II will contain very little unused CO2and/or H2O. higher temperature CO2and H2About the phase II favorable to increase reaction rates and obtain CO and H2. The introduction of enriched natural gas on the phase II helps improve the mixing and use 2And CO2during the reforming process, the reduction of temperature on the phase I to improve the durability of the material of the mixing pipe and preheating enriched natural gas using thermal energy of phase I.

The favorable temperature range for mixing and reforming phase II is approximately 1800oF (982,2o(C) up to 3500oF (1926,7oC). The products of phase II consist of deformirovannykh gas (CO+H2O), preheated natural gas, and the remaining or unreacted, CO2and H2Acting With regard to tables I and II, when using the Lamani phase I 3500oF (1926,7oC) the equilibrium temperature is estimated as 2300oF (1260oC). The final equilibrium temperature of all deformirovannykh gases in the manifold, after mixing with Reformirovanie gases OBFR, is estimated as 1680oF (915,6oC). This 30oF (16,7oC) exceeds the temperature by way OBFR.

The device of accelerated reforming fuel with oxygen in accordance with the present invention provides means for regulating the total number deformirovannykh gases to be issued, the temperature of all (primary and secondary) deformirovannykh gases and the quantity of enriched natural gas, present in the total number of deformirovannykh gases. By changing the flow rate of natural gas in the burner phase I, maintain the amount of oxygen that is close to stoichiometric, and is proportional to the change in the rate of flow of natural gas in phase II, you can change the number deformirovannykh gases produced in the device of accelerated reforming fuel with oxygen, which in turn modifies the full amount subject to the filing deformirovannogo gas.

If you change the volumetric rate of ticengo ratio, but do not change the volumetric flow rates of gases in phase II, we will change the temperature of the gas obtained in the device of accelerated reforming fuel with oxygen. The temperature of the secondary deformirovannykh gases from the device of accelerated reforming fuel with oxygen will increase with increasing volumetric flow rate of natural gas in the burner and will decrease with decreasing volumetric flow rate of natural gas in the burner. The increase or decrease in the temperature of the secondary gas will raise or lower the temperature of the entire supply of natural gas for mixing with the primary Reformirovanie gases.

If you change the volumetric rate of flow of natural gas in phase II without any changes of volumetric flow rates of the gases in the burner phase I, you should change the number of enriched natural gas in the secondary deformirovannom gas obtained in the device of accelerated reforming fuel with oxygen, and thereby change the total number of enriched natural gas throughout the volume deformirovannogo gas. However, in this case, the variation of the velocity volumetric flow phase II leads to a change in temperature of the secondary deformirovannogo gas. Ovelia will cause a temperature increase.

Thus, through selective changes of volumetric flow rates of the gases on the phase I and/or phase II you can adjust the number deformirovannogo gas temperature deformirovannogo gas and the amount of enriched gas in the entire volume deformirovannykh gases without the need for any change in the operation of the gas reforming device main installation or use of other control methods.

Correct temperature control deformirovannykh gases flowing into the shaft furnace, it is important to maintain a high quality of iron, obtained by direct recovery by preventing okomkovanija [ore] at elevated temperatures, gas or reducing speed plating at low gas temperatures. It is more efficient to operate at elevated temperatures that can be tolerated without the occurrence of okomkovanija.

Although the present invention described above with reference to its specific options, obviously, can be made numerous changes, modifications and variations without deviating from the concepts listed here. So assume that it includes all such changes, modifications, and variations that fall is characterized in that that (a) provide for the mixing pipe in such a place that it was surrounded by existing reformed gases; (b) ignite the mixture of the first stream of gaseous hydrocarbon and oxygen in the first stage to obtain the burning gases; (C) serves referred burning gases to the second stage in the axial direction; (d) introducing a second stream of gaseous hydrocarbon and oxygen at the second stage in a direction coaxial with the said burning gases, and (e) provide for the reaction of burning gas with a second stream of gaseous hydrocarbons in the second stage to obtain deformirovannykh hydrogen and carbon monoxide; (f) supply obtained deformirovannykh hydrogen and carbon monoxide from the mixing pipe in existing reformed gases.

2. The method according to p. 1, wherein the gaseous hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture.

3. The method according to p. 2, characterized in that the ignition of the first stage provide carbon dioxide and water, which is served on the second stage.

4. The method according to p. 2, characterized in that the second stage is carried out in when and oxygen is introduced into the mixing pipe in the form of a vortex flow.

6. The method according to p. 1, characterized in that use existing heat deformirovannykh gases for ignition of the first stream of gaseous hydrocarbon and oxygen in the first stage.

7. The method according to p. 2, characterized in that provide cooling of the first stage, which is the ignition.

8. The method according to p. 2, characterized in that perform pre-heating the second stream of gaseous hydrocarbon and oxygen prior to its introduction into the second stage.

9. The method according to p. 2, characterized in that perform pre-heating the second stream of gaseous hydrocarbon and oxygen before putting them on the second stage and use the pre-heated gaseous hydrocarbon and oxygen before their submission to the second stage for cooling the first stage.

10. Way to add the number deformirovannykh gases used in installations of direct reduction of iron, in which the primary reformirovannoy the gas is fed into the furnace from the main reforming device and passed through the iron ore for iron, characterized in that a) ignite the mixture of the first stream of gaseous hydrocarbons and oxygen in the first stage to receive asnago hydrocarbon and oxygen in the second stage; (d) ensure the reaction of carbon dioxide and water with the second portion of the gaseous hydrocarbons in the second stage to obtain secondary deformirovannykh hydrogen and carbon monoxide and (e) introducing the secondary reformed hydrogen and carbon monoxide in the primary circuit deformirovannogo gas in the furnace.

11. The method according to p. 10, wherein the gaseous hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture.

12. The method according to p. 11, characterized in that the second step is performed in a mixing tube located in the primary circuit deformirovannogo gas to be fed into the furnace.

13. The method according to p. 11, characterized in that the second thread mentioned gaseous hydrocarbon and oxygen is introduced into the mixing pipe in the form of a vortex flow.

14. The method according to p. 11, wherein the mixing tube is installed in the present collector, containing reformed gases from the main reforming device, and, in addition, involves the use of heat from the audience deformirovannykh gases to initiate the initial ignition of the first flow golytely gaseous hydrocarbon is injected in the second stage to obtain enriched natural gas for use in the process of direct reduction of iron.

16. The method according to p. 15, characterized in that the number of enriched natural gas deformirovannom gas regulate when feeding into the furnace through the electoral changing the volumetric flow rate of the second stream of gaseous hydrocarbons in the second stage.

17. The method according to p. 11, characterized in that the temperature and/or the number deformirovannogo gas regulate when feeding into the furnace through selective changes of volumetric flow rates of the first stream of gaseous hydrocarbon and oxygen in the first stage and/or volumetric flow rate of the second stream of gaseous hydrocarbons in the second stage.

18. The gas reforming device for receiving deformirovannykh gases, characterized in that it contains a) a burner for burning a mixture of the first stream of gaseous hydrocarbon and oxygen in the first stage for receiving products of combustion; (b) an elongated mixing tube provided for the second stage, in which the said combustion products is served in the axial direction, and the mixing tube open circuit deformirovannykh gases to the furnace, and (C) a nozzle for introducing a mixture of the second stream of gaseous hydrocarbon and oxygen in the second stage for R the s out of the mixing pipe and enter the path deformirovannykh gases.

19. The gas reforming device according to p. 18, characterized in that the hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture.

20. The gas reforming device according to p. 18, wherein the burner includes a mixer with Venturi nozzle including a Venturi nozzle having a diverging portion that is open in the mixing pipe, the camera near the Venturi nozzle for receiving the second stream of gaseous hydrocarbon and oxygen, and the camera is open in the mixing pipe below along the flow from the diverging portion of the Venturi nozzle.

21. The gas reforming device according to p. 20, characterized in that it includes a vortex nozzle in the mouth of the chamber to a mixing pipe for a message vortex motion to the second stream of gaseous hydrocarbon and oxygen as it is received in the mixing pipe.

22. The gas reforming device according to p. 20, wherein the mixing tube has a refractory lining.

23. The gas reforming device according to p. 18, wherein the burner comprises a tube having a nozzle at its front end for receiving the first stream of gaseous hydrocarbon, pricemat the mixing tube, a tubular cooling jacket surrounding the combustion chamber and cooling jacket has an inlet channel and outlet channel for the passage of cooling medium into and out of the cooling jacket, and the nozzle of the burner pipe and the chamber opened into the combustion chamber for passing the first stream of hydrocarbon and oxygen in the combustion chamber for combustion therein, a second chamber for receiving the second stream of gaseous hydrocarbon and oxygen, with the mouth in the mixing pipe below along the flow from the combustion chamber for passing a second stream of gaseous hydrocarbon and oxygen in a mixing pipe for mixing with the combustion products from the combustion chamber.

24. The gas reforming device according to p. 23, characterized in that it includes a vortex nozzle at the mouth of the second chamber inside the mixing pipe for a message vortex motion to the second stream of gaseous hydrocarbon and oxygen as it is received in the mixing pipe.

25. The gas reforming device according to p. 24, characterized in that it includes a vortex nozzle at the mouth of the first chamber inside the mixing pipe for a message vortex motion to the first oxygen stream as it is received in the mixing pipe.

27. Gas reforming-us is La message whirl first stream of oxygen as it passes through the nozzle into the combustion chamber.

28. The gas reforming device according to p. 27, characterized in that the hydrocarbon is natural gas, methane or propane, and oxygen is the oxygen of industrial quality, air or a mixture.

29. The gas reforming device according to p. 27, wherein the burner comprises a tube having a nozzle at its front end for receiving the first stream of gaseous hydrocarbon, and a tube surrounding the first chamber for receiving the first stream of oxygen, and the combustion chamber located in front of the nozzle and open into the mixing pipe, the nozzle and the first chamber open into the combustion chamber for passing a first stream of gaseous hydrocarbon and the first stream of oxygen into the combustion chamber for burning.

 

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