RU169609U1 - Installation for producing synthesis gas from coal-water fuel - Google Patents

Abstract

The utility model relates to devices for the combustion and thermal processing of coal and can be used at thermal stations, in boiler houses to produce energy and high-quality synthesis gas from low-grade steam coal. The installation comprises a vertically mounted gas generator with a gasification chamber for coal-water fuel and a separator connected to it for separating gaseous gasification products and mineral wastes. The unit is equipped with a control diaphragm for the synthesis gas produced in the generator. Gas burners are installed in the plane of impact of VUT jets with the formation of a combustion chamber. A radiative heat exchanger-separator is installed in the lower conical part of the generator housing for the final heating of the fuel-injection pump before it is fed into the combustion chamber. Two mutually directed nozzles serve as a jet mill. A bunker with a lock and an intermediate bunker for ash discharge is placed under the radiation heater. The separator for separating gaseous products of gasification and mineral wastes also in the lower part has a hopper with a lock and an intermediate hopper for ash discharge. Above the separator for the separation of gaseous products of gasification and mineral waste, an intermediate heater VUT is installed. The installation for ensuring its commissioning has fuel oil supply with shutoff valves, a combustion product outlet into the boiler pipe with shutoff valves and an additional air supply with shutoff valves. The installation allows you to increase the efficiency and effectiveness of the production of synthesis gas from coal-water fuel and transfer boiler rooms with fuel oil

Description

The utility model relates to energy, and in particular to devices for burning and thermal processing of coal, and can be used at thermal stations, in boiler rooms to receive energy and high-quality synthesis gas from low-grade thermal coal.

A gas generator is known for gasifying a water-coal slurry and burning solid or water-coal fuel (VUT), including a vertical reaction chamber with a fluidized bed of solid or water-coal fuel, a gas distribution grill made with a window in the central part, means for supplying solid fuel located in the lower part of the chamber under a gas distribution grid, an ash outlet device, the reaction chamber being provided with a vertical partition dividing it into gasification and combustion compartments, and into odke reinforced inclined heat pipes arranged in the upper parts of the condensing gasification compartment, and lower, the evaporator in the fuel burning compartment located in the flue gas distribution grid box spring-loaded plates; gas tight screens located in compartments and made in the form of vertical heat pipes connected to collectors, and the collector of vertical heat pipes located in the gasification compartment is in communication with a container for a water-coal suspension and with a pipe for supplying a water-coal suspension (Pat.RF No. 1775464, publ. . 11/15/1992).

The disadvantages of the known gas generator are as follows. For the purpose of gasification of water-coal fuel (VUT), it uses air supplied under a gas distribution grill, as a result of which the generated generator gas contains a significant amount of nitrogen ballasting gas, which requires purification of the generator gas before it is supplied to the consumer.

Heat transfer from the combustion compartment to the gasification compartment occurs only through the partition separating them, and not through the entire lateral surface of the gasification compartment, which reduces the temperature and, hence, the rate of occurrence of gas-fired gasification reactions.

This is further aggravated by the fact that the combustion of HLF or coal in a fluidized bed takes place at lower temperatures (approximately 200-300 ° C) than when they are sawed, as a result of which the intensity of the process of gasification of HLW is further reduced.

The use of direct-flow heating of the gasification part of the gas generator by the products of fuel combustion is also relatively ineffective compared to countercurrent.

In addition, in the known technical solution does not use the energy potential contained in the flue gas from the combustion of fuel.

Known electric arc plasma reactor for coal gasification, containing a chamber with an electromagnetic coil, rod electrodes and nozzles for introducing reagents and outputting reaction products, while nozzles for introducing reagents are made in the form of annular channels located on the reactor lid, arranged in concentric circles, each channel equipped with a vertical tube for introducing coal and a tangential nozzle for supplying flue gases, and on the inner wall of the reactor at the same level with the electromagnetic coil Execute the annular groove, whose height is equal to the height of the electromagnetic coil (Pat.RF №2087525, publ. 20.08.1997).

The disadvantages of the known reactor are as follows.

The presence of high temperatures (above 3000-4000 ° K) requires the manufacture of the interior walls of the plasma reactor from materials resistant to carbon dioxide, water vapor and oxygen, which is part of the flue gases, since the supposed protection of the walls of the reactor by flowing slag is ineffective, and in the case of low-ash coals just be absent. In general, this reduces the reliability of the proposed electric arc plasma reactor for coal gasification.

The disadvantage is the low efficiency of the gasification process in a plasma reactor, since only 31.5% of the flue gas is used directly for coal gasification, and the remaining 68.5% is represented by ballast (nitrogen), which is not only not involved in the gasification process, but is a thermal ballast both when it is heated in the gasification process, and when it is cooled after completion of the synthesis gas production process.

The effect of flue gas ballasting is also associated with increased air consumption during the combustion of coal, which serves as a source of flue gases, since in this case the coefficient of excess air is 1.35-1.4, and for this reason, the source flue gas contains a significant amount of oxygen, which is 4 -6% (volumetric).

In addition, upon completion of the gasification process, the resulting synthesis gas has a low heat of combustion, since the gasification products are ballasted with nitrogen, from which they must be cleaned before being transferred to the consumer.

The principal drawback of all high-temperature (over 3000-4000 ° K) coal gasification reactors is that although the mass-average temperature of the process lies in the region of significantly lower temperatures of about 2000 ° K, harmful substances are formed in the reaction mixture in small amounts during mixing and cooling cyan (CN) and hydrocyanic acid (HCN), which are stored in gasification products.

A known installation of plasma-thermal processing of coal-water fuel into synthesis gas, including a coal dust bin, an oxidizer tank, a mixer, a dispersing device, a pump for pumping a coal-water suspension, a heater, a gas blower, a chimney, a gasification column, a heat exchanger of the first stage of a gasification column, a quenching device for synthesis gas, plasma reactor, heat exchanger of the second stage of the gasification column, distributor of gasified mixture, plasma sources, heat exchanger for pumping hot synthesis gas, a synthesis gas purification device, a burner and a combustion device of a gasification column (Pat. RF No. 2047650, publ. 10.11.1995).

A disadvantage of the known technical solution is the complexity of the installation, in which the process of heating the water-coal suspension proceeds in two stages, first in the heater for preheating the water-coal suspension to 500-600 ° K, and then in the lower part of the tubular heat exchanger of the first gasification stage, with the synthesis part being burned in the heat exchanger gas, and the gasification process of the water-coal suspension proceeds in three stages, first in the quenching device, which is the outlet of the plasma reactor, then in the upper part of the heat exchange and then in the plasma reactor itself, as well as the need to use a high-temperature plasma reactor to implement the third stage of gasification, the use of which requires the use of special materials resistant to high temperatures (2500-3000 ° K) in a chemically aggressive environment (СО ₂ , Н ₂ O etc.).

The known installation also overestimated the energy costs for the production of synthesis gas, which is associated with the introduction of a vapor-gas suspension, consisting of carbon monoxide, carbon dioxide, hydrogen, water vapor and unreacted coal particles, into a plasma reactor, in which water vapor is used as a reagent, which leads to additional ballasting of gaseous products of gasification with water vapor and simple hydrocarbons formed at high temperatures 2500-3000 ° K.

The scheme of interaction between plasma jets of steam and jets of a gasified mixture used in the installation, the organization of the return of unreacted particles of the organic part of coal to the reaction zone before they are completely converted to gas, equally applies to solid particles that make up the mineral part of coal that do not react with the vapor phase and as a result, they will accumulate in the high-temperature zone of the plasma reactor. Due to the high temperatures created in the plasma reactor (2500-3000 ° K) and the length of stay in it, the metal oxides that make up the mineral part of coal will melt and their chemical interaction with carbon will form with the formation of metals, their carbides and carbon monoxide, that a significant part of the energy will be spent and that as a whole will reduce the calorific value of the synthesis gas by enriching it with carbon monoxide.

A known installation for processing coal into synthesis gas from coal-water fuel, which contains a hopper for crushed coal, a water tank and a dispersant connected thereto for producing coal-water fuel, a vertically mounted gas generator with a gasification chamber for coal-water fuel and a separator connected to it for the separation of gaseous gasification products and mineral waste. The installation also contains a pump for supplying coal-water fuel, a pipe cooler for synthesis gas and a separator for separating condensed water (Pat.RF No. 2190661, publ. 10.10.2002).

In this installation, a colloidal dispersed fuel system with an average surface particle size of the dispersed phase of not more than 1 μm is used as a coal water fuel.

The temperature of the coolant in the annulus of the reactor is maintained in the range of 400 (1000 ° C, and the temperature in the pipes is in the range of 200 ... 800 ° C.

A disadvantage of the known installation is the low efficiency of the synthesis gas production process, which is due to the following factors:

- the preparation of a colloidal dispersed fuel system in an interactive mechanochemical reactor (dispersant) is accompanied by grinding not only the organic, but also the mineral (ash) part of coal with an average surface particle size of the dispersed phase of not more than 1 μm, which significantly increases the energy consumption for grinding coal in general, and the use of an interactive mechanochemical reactor for the preparation of the fuel system increases the cost of the installation as a whole;

- the use of a once-through tube cooler for cooling synthesis gas is also ineffective compared to counterflow;

- independent heating of the coolant supplied to the annulus of the reactor to 1000 ° C in the presence of hot air cooling the synthesis gas after the tube cooler leads to unnecessary energy costs for heating the dispersed fuel system;

- the recommended gasification temperature range of 200-800 ° C does not ensure the effective conduct of this process in the case of using low-reaction coals, such as anthracite.

The technical result, which is achieved by the claimed utility model, is to increase the efficiency of the installation for producing synthesis gas from coal-water fuel.

The specified technical result is achieved in that the installation for the production of synthesis gas from coal-water fuel, including a preparation system for coal-water fuel, a vertically mounted gas generator with a gasification chamber for coal-water fuel and a separator connected to it for separating gaseous gasification products and mineral wastes, in contrast to the prototype, is provided a coal-water jet mill installed in the upper part of the gasification chamber for water-coal fuel, which is made in the form of a polo cylinder with tangential gas burners located in the plane of impact of the water-carbon jets and operating on the synthesis of gas and air supplied by a compressor driven by a gas turbine operating on flue gases from a generator; VUT is heated sequentially in coolers of the mineral part of the generator and separator itself for separating gaseous products of gasification and mineral waste, then in the gas cooler in front of the gas turbine and in the radiation countercurrent heater VUT in the lower conical part of the gas generator.

In the proposed installation, the operation efficiency of the installation is increased due to the fact that with the adopted cylindrical arrangement of the gasification of coal-water fuel (VUT), in the lower conical part of which the heater is installed VUT, which creates the conditions for the organization of countercurrent heat exchange between the gasification of water-carbon fuel and combustion products of synthesis gas and the removal of mineral parts from gasification products. Air-gas burners tangentially located in the gasification chamber contribute to high-quality mixing of gasified components, aligning temperature profiles along the cross section of the gasification chamber, which also helps to increase the efficiency of the gasification process. A distinctive feature of the installation is the presence of heat exchangers on the silos of the separator of combustion products and behind them. This design allows you to cool the synthesis gas to the required operating temperature of the gas turbine. The air heater at the outlet of the synthesis gas allows you to return part of the thermal energy to the gasification zone.

The use of turbocharging allows the gasification process to be carried out at elevated pressure, which increases the concentration of reacting substances with an increase in its speed and can significantly reduce the overall dimensions of the installation.

The use of a jet mill for HLW in the gasification chamber allows the use of HLW with grinding up to 100 microns, which reduces the cost of preparing HLW.

The costs of the resulting synthesis gas, aimed at maintaining the required process temperature, are interconnected in such a way that carbon dioxide and part of the water vapor included in the composition of the flue gases produced by the combustion of synthesis gas are fully used for gasification of the fuel-oil mixture. The remaining part of the carbon, which is part of the gasified part of the fuel-and-chemical mixture, is gasified by the water, which is part of the gasified fuel-and-oil mixture. By adjusting the amount of water directed to the preparation of the fuel-and-chemical compound, it is possible to regulate the process of gasification of the chemical-grade coal and gas over a fairly wide range. Thus, the gasification process is always automatically balanced for the starting components, which increases the degree of efficiency of the use of flue gases.

The gas generator is designed to directly supply synthesis gas to the boiler furnaces and its sufficiently high temperature is not a negative property: the heat energy will be given to the boiler’s working fluid and, when condensing tail surfaces are used in it, all the heat of condensation of water vapor will be useful. Losses in comparison with direct burning of coal in the boiler and when using a gas generator in the latter case will be less, so the efficiency when working on gas is 6 ... 10% higher than on coal. The use of this installation will allow without the reconstruction of boilers to switch from expensive fuel oil to coal.

The utility model is illustrated by the drawings shown in figures 1, 2.

In FIG. 1 shows a schematic diagram of the proposed installation for producing synthesis gas from water-carbon fuel, in FIG. 2 is a cross-sectional view of a burner device of an installation.

The installation comprises a fuel-oil supply system 1 connected to a fuel oil supply system 2, which are connected in series through a common pipe 3: cooler 4 of the hopper 5 for collecting the mineral part from the gasification chamber 6; cooler 7 of the hopper 8 for collecting the mineral part from the separator 9 for the separation of gaseous products of gasification and mineral waste; the first heater 10 WUT; the second radiation heater 11 VUT. Both heaters 10 and 11 of the VUT are connected in series with each other and at the outlet by two pipelines with spray nozzles, which are located opposite each other along the axis of the gas generator in the upper part of the gasification chamber and form a jet mill 12. In the upper part of the gasification chamber 6, gas burners 13 are tangentially located, interconnected by an air duct 14 and with an air compressor 15 by an air duct 16, through an air heater 17 and an adjustable mixing device 18, also the burners 13 are connected to the air supply from the cat Flax locking through check valves 19. Gas burners 13 are arranged in a horizontal plane passing through the middle of the distance between the spray nozzles VUT which form a jet mill 12 and connected by pipelines with a radiation heater 11 VUT. Synthesis - gas after exiting the WUT heater 10 through two channels: through channel 20 to the gas turbine 21 and through channel 22 through the control diaphragm 23 into the air heater 17. Gases leaving the gas turbine 21 through channel 24 enter the channel 22. Gas duct 25 after the air heater 17 is connected to the boilers (not shown in Fig. 1) through the shutter 26 and to the chimney through the shutter 27. To remove ash from the bins 5 and 9 in the lower parts of them are installed locks with intermediate bins 28 and 29 and shutters 30, 31 and 32, 33.

Installation works as follows.

The start of the gas generator is carried out on fuel oil through pipeline 2, the pipeline 1 for the fuel-and-oil production unit is closed. Air is supplied to the gasification chamber 6 through valves 19, which is mixed with fuel oil sprayed in the jet mill 12, the mixture is ignited (incendiary device not shown) and a swirling flow moves down the chamber 6, warming the walls of refractory bricks. The combustion products pass through the separator 9 and the heater 10 and in full flow into the gas turbine 21, the control diaphragm 23 is closed. The turbine 21 rotates the air compressor 15, while the air is fed through the pipe 16 through the air heater 17 to the burner 13. The combustion products enter after the turbine 21 through the air heater 17 into the boiler pipe through the open shutter 27, while the shutter 26 is closed for supplying gas to the boilers, also the gas supply to the mixing device 18 is closed. When the unit is heated up, the turbine 21 enters the design mode, the air pressure in the duct 14 exceeds the pressure of the air coming from the boiler room, the non-return valves 19 shut off - the installation works on air from the compressor 15. After complete heating of the chamber 6, the fuel oil supply through the pipe 2 is gradually reduced and the BUT supply through the pipe 1 is proportionally increased. After the fuel oil supply is stopped, the installation operates in gasification mode: the shutter 26 is opened and the gases go to the boilers that are transferred from fuel oil to the synthesis gas, the shutter 27 is closed, the control diaphragm 23 and the mixing device 18 are transferred to the operating mode. Gas with air through the burners 13 is fed into the gasification chamber 6, there they ignite from high temperature, which maintains it at the required level, ensuring endothermic reactions of coal carbon and water from the WUT, which, after the jet mill 12, scatter to the walls of the chamber 6, where they are picked up by tangential high-temperature the combustion products flowing out of the burners 13. In the form of a circular vortex, the reaction mass spirals downward, gradually turns into a mixture of hydrogen and carbon monoxide, slightly ballasted oduktami combustion gas: carbon monoxide and nitrogen of air. With a circular rotation of the gas flow, the mineral part of the fuel-injection unit is beaten off to the wall of the chamber 6 and is lowered into the hopper 5 through it, where it is cooled through the walls by passing through the heater 4. Gases from the middle lower part of the chamber 6 enter the cyclone separator 9, where the mineral part of the WCF is beaten to the walls and lowered into them in the hopper 8, where it is cooled through the walls of the VUT passing through the heater 7. Then the purified gases pass through the WUT heater 10, then they enter the gas turbine 21 and through it and in parallel through the regulating diaphragm 23 through the channels 22 and 24 into the air heater 17 and then partly through the mixing device 18 to the burners 13, the rest to the boilers through the gas duct 25. VUT after the heater 10, it enters the final superheat in the radiation heater 11 and then through two pipes to the jet mill 12, where the steam-coal mixture is sprayed and crushed through two nozzles directed at each other upon collision of two collisions sputtered jets. In this case, the coal part of the particles, as the most porous, enters from the high-pressure pipe VUT (3 ... 4 MPa) into the gas cavity with a low pressure (0.2 (0.3 MPa) and collapses, thereby repeatedly increasing the area of its reaction with water. The mineral part, as the most dense, almost does not deteriorate and is therefore well separated in the circular motion of the flow. The mineral part of the bins 5 and 8 is periodically removed by filling with the help of lock devices consisting of intermediate bins 28, 29 of the shutters 30, 31 , 32 and 33. Last allow they can be removed without lowering the pressure in chamber 6. to remove the mineral part of the fuel-and-chemical assembly. All the heat released during the combustion of part of the gas produced in the installation is completely transferred back to the process and to the boiler installation, with the exception of losses to the environment (they are inevitable in any installation with high internal temperature).

Example.

We will consider the operability of the proposed installation using an example of a boiler room operating on fuel oil.

The maximum boiler heat output when operating on fuel oil will be:

Q ₁ = D (i _x -i _PV ) η = 25000 (2791-418.7) 0.89 / 3600 = 1466 kW.

where D = 25 t / h - steam capacity of the boiler DE-25-14;

i _x = 2791 kJ / kg - enthalpy of saturated steam;

i _pv = 418.7 kJ / kg - enthalpy of feed water;

η _km = boiler efficiency DE-25-14 when operating on fuel oil.

For calculation, we take with a margin:

Q ₁ = 2 MBt.

To ensure this heat output, the consumption of Berezovsky brown coal B2-R is required (provided that we will burn it in the form of gas obtained from it with Q ^p _n = 13.02 MJ / kg):

In _angle = Q ₁ / Q ^p _{n =} 2 / 13,03 = 0,154 kg / s.

How much water is needed to conduct steam gasification of this coal consumption?

Steam gasification reaction:

Н ₂ О + С = Н ₂ + СО-130500 J / mol

18 + 12 = 2 + 28

Quantitatively, the mass of 1 mol of a substance is the mass of a substance in grams, numerically equal to its atomic or molecular weight

q _gasif = 130.5 / 12 = 10.875 kJ / g = 10875 kJ / kg.

For 1 kg of carbon, 18/12 = 1.5 kg of water is required.

Learned from 1 kg of carbon:

Hydrogen N ^g = 2/12 = 0.167 kg;

Carbon monoxide СО ^g = 28/12 = 2, ЗЗ kg.

The amount of water will decrease by:

ΔW ^g = 18/12 = l, 5 kg.

Unbound carbon with hydrogen will be less than the total no more than ΔС ^p = (V ^g -W ^p ) = 48-33 = 15%.

So, in 1 kg of fuel there will be the following amount of carbon that can connect with water:

C _gas = (C ^p -ΔC ^p ) / 100 = (44.2-15) / 100 = 0.292 kg.

For this amount of carbon to conduct steam gasification, theoretically, the following amount of water will be required:

G ^t _water = 0.292⋅1.5 = 0.438 kg.

Theoretically, to conduct steam gasification, it will be necessary to add water to the fuel:

ΔG _water = G ^t _water -W ^p / 100 = 0.438-0.33 = 0.108 kg.

Since the gasification process is far from ideal (coal particles have a specific size and the process will take place on their surface; the mixture formation of coal particles and water vapor is also not ideal), the moisture content of VUT must be increased to 50% and then its composition of 1 kg of coal will be as follows :

C ^p = 0.442 kg; N ^p = 0.031 kg; About ^p = 0.144 kg; S ^p = 0.002 kg; A ^p = 0.047 kg; W ^p = 0.5 kg.

The mass of fuel-grade fuel from 1 kg of coal will be 1.166 kg.

In 1 kg VUT will be:

With ^p _VUT = 0.379 kg (37.9%); N ^r _VUT = 0.026 kg (2.6%); About ^r _VUT = 0.123 kg (12.3%); S ^p _VUT = 0.0017 kg (0.17%); A ^r _VUT = 0.04 kg (4%); W ^p _VUT = 0.429 kg (42.9%).

VUT are heated by burning gasification products leaving the reactor with a temperature of t ₁ = 673 K (at a pressure of 3 MPa it will be a vapor-coal mixture) to a temperature of t ₂ = 1273 K. In this case, softening and melting of the mineral part of coal should be avoided.

To do this, you need to bring the following amount of heat for 1 kg of fuel-efficient fluid into the reactor:

Q _load = [W ^r _BUT (i ₂ -i ₁ )] / 100 + [(100-W ^r _BUT ) (with _{angle 2} t ₂ -C _{angle 1} t ₁ ] / 100 =

[42.9 · (4642-3276)] / 100 + [(100-42.9) (3.051-1273-

-1.901⋅673)] / 100 = 2055 kJ / kg.

GSSSD 187-99 Water. Specific volume and enthalpy at temperatures of 0 ... 1000 ° C and pressures of 0.001 ... 1000 MPa: enthalpy for water at an absolute pressure of 0.2 MPa:

at t ₁ = 673 K i ₁ = 3276 kJ / kg;

at t ₂ = 1273K i ₁ = 4642 kJ / kg.

with _angl1 ⁼ 1.901 kJ / (kg K) is the heat capacity of dry coal at t ₁ = 673 K;

with _ugl2 ⁼ 3.051 kJ / (kg K) is the heat capacity of dry coal at t ₁ = 1273 K.

VUT consumption:

In _VUT = 1,166 1,166-0,124 In _coal = = 0.145 kg / s.

The heat output of the burner will be for heating the mixture:

Q _mountain ^arp = In _VUT Q _nag / (lq ₅ ) = 0.145-2055 / (l-0.05) = 314 kW.

The heat productivity of the burner device for the endothermic gasification reaction will be:

Q _{peak load} ⁼ _VUT C _gas q _gasif / [1,166 (1-q ₅ )] =

= 0.145⋅0.292⋅10873 / [1.166 (1-0.05)] = 416 kW.

The total amount of heat that provides gasification:

Q _gop ^sum = Q _gop ^load + Q _react ^heat = 314 + 416 = 730 KBT.

This is a third of the boiler heat output, but this energy is stored in the form of physical heat of the gas mixture and in chemical energy stored in combustible elements: hydrogen and carbon monoxide, which will be useful for gasification and further operation of boiler rooms.

The composition of the produced gas from 1 kg of HLF (assuming that the carbon from the volatile hydrocarbons completely reacts with water, this part of the produced hydrogen compensates for the heat production of the volatile):

HydrogenN _gas = N ^g С ^p _VUT = 0.167⋅0.379 = 0.063 kg / kg (VUT);

Carbon monoxide CO _gas = СО ^g С ^p _VUT = 2,33⋅0,379 = 0,883 kg / kg (VUT);

Water W _gas = W ^r _VUT -ΔW ^g C ^r _VUT = 0.429-1.5-0.3⋅79 = -0.14 kg / kg (VUT), this indicates that part of the carbon from the volatiles does not react with water that goes beyond our accepted assumptions.

The calorific value of the gas mixture obtained from 1 kg of HLW will be (without ballast):

О _gasWUT = Н _gas Q _Н2 + СО _gas Qco =

= 0.063⋅120500 + 0.883⋅10100 = 16510 kJ / kg (VUT),

where Q _H2 is the calorific value of hydrogen (120500 kJ / kg);

Qco is the calorific value of CO (10100 kJ / kg).

The calorific value of the gas mixture obtained from 1 kg of gas will be (without ballast):

Q _gas = Q _{gas WUT} / (N _gas + CO _gas ) = 16510 / (0.063 + 0.883) = 17452 kJ / kg.

This is a theoretical value that does not take into account the ballast components: CO ₂ from the combustion of gas to maintain the reaction, nitrogen of the air going to combustion. The calculation of ballast components is carried out by the method of successive approximations: for this, the amount of ballast gases is set, the calorific value of the gas is determined from them; determine the required flow rate of this gas and air, necessary to maintain the reaction in the generator, determine the amount of ballast gases formed. Repeat until the accepted and received values are equal.

The total gas productivity of the generator for combustible components:

G _{total gg} = (H _gas + CO _gas ) _VUT = (0.063 + 0.883) 0.145 = 0.137 kg / s.

The required amount of combustible components (G _yy consumption) to maintain the desired temperature in the generator:

G _gg = Q _mountains ^sum / Q _gas = 730/17452 = 0.0418 kg / s

This is part of the total fuel consumption:

G _{gg /} G _total = 0.0418 / 0.137 = 0.305 (30.5%).

When burning this gas, it will be released:

Water G Water _supply = (18/2) N _gas = (18/2) 0.063 = 0.567 kg;

CO ₂ (carbon dioxide) G _BSO2 =

= СО _gas (12 + 32) / (12 + 16) = 0.883⋅44 / 28 = 1.387 kg;

Air _nitrogen G _Bazot = (0.78 / 0.21) [(16/2) N _gas + CO _gas 16 / (12 + 16)] =

= (0.78 / 0.21) [(16/2) 0.063 + 0.883⋅16 / (12 + 16)] = 3.576 kg.

The total release of ballast gases (water can be eliminated - it will go to the formation of hydrogen and carbon monoxide in the generator):

G _{Bg =} G _BS02 + G _Bazot = 1.387 + 3.576 = 4.963 kg.

Their consumption in generator gas will be:

G _{Bg.g Bg} = G G _{yy =} 4,96⋅0,0418 ₌ 0,207 kg / sec.

Total gas capacity for combustible components:

G _total = G _{total gg} + G _Bg.g = 0.126 + 0.207 = 0.333 kg / s

Generator gas balancing:

K _B = G _Br.g / G _total = 0.207 / 0.333 = 0.621 (62.1%).

The calorific value of the gas mixture obtained from 1 kg of gas will be with ballast:

Q _{gas B} = Q _gas / (1 + K _B ) = 17452 / (1 + 0.621) = 10768 kJ / kg.

This figure does not take into account the additional gas flow with the ballast going to combustion, this is another 30.5%, which will be:

Q _{gas B} = Qgaz / (1 + K _B ) = 10768 / (1 + 0.305) = 8951 kJ / kg.

Also, the amount of physical heat supplied with gas and air entering the burner is not taken into account in the calculation, and this is almost 5% of the additional thermal energy:

ΔQ _rop ^{load rp} = 0.05 Q _rop ^нarp = 0.05-416 = 20.8 kW.

Accordingly, the required gas consumption for combustion and the amount of ballast in the gas will decrease by 5%, which will convict its calorific value to:

Q _{gas B} = Q _gas (1.05) ² = 8951 (1.05) ² = 9869 kJ / kg.

To calculate the gas generator, the calorific value of the gas produced by it is taken Q _{gas B} = 10 MJ / kg (14.1 MJ / nm ³ ).

Gas density:

ρ _gtl = 0.01 [l, 96CO ₂ + 1.52H ₂ S + 1.25N ₂ + 1.43O ₂ + 1.25CO + 0.0899H ₂ +

+ Σ (0.536m + 0.045n) C _m H _n +0.717 CH ₄ ], kg / nm ³ .

ρ _gtl = 0.01 [l, 96⋅24 + l, 25⋅61 + l, 25⋅14.2 + 0.0899⋅0.94] = l, 4l kg / nm ³ .

where CO ₂ = 24%; N ₂ = 61%; CO = 14.2%; H ₂ = 0.94%.

Estimated consumption of generator gas, taken to the burner for its normal operation:

The ^gas _races = (Q _gor ^cymm -ΔQ _rop ^LOAD) / Q _B = _raz (730-20,8) / 10000 = 0.07 Nm ³ / s

= (0.05 kg / s), which in percentage terms will be 100⋅0.05 / 0.333 = 15% of the total generator productivity.

The amount of heat that VUT will receive in gas heaters when the VUT is heated from 20 ° C to 400 ° C.

Q = Q _{pod.VUT naked} = [W ^p _VUT (i ₂ -i _1)] / 100 + [(100-W ^p _VUT) (c _ugl2 t ₂ - c _ugl1 t _1)] / 100 =

= [42.9⋅ (3275-128)] / 100 + [(100-42.9) (2.15-400-1.67⋅20)] / 100 = 1852 kJ / kg.

GSSSD 187-99 Water. Specific volume and enthalpy at temperatures of 0 ... 1000 ° C and pressures of 0.001 ... 1000 MPa: enthalpy for water at an absolute pressure of 0.2 MPa:

at t ₁ = 20 ° C i ₁ = 128 kJ / kg;

at t ₂ = 400 ° C i ₂ = 3275 kJ / kg.

with _carbon1 ⁼ 1.67 kJ / (kg K) - heat capacity of dry coal at t ₁ = 20 ° C;

with _carbon2 = 2.15 kJ / (kg K) is the heat capacity of dry coal at t ₂ = 400 ° C.

In this case, the gas cools from at t _{1 g} = 1000 ° C to:

t _{2 g} = t _{1 g} -Q _inlet G _VUT / (with _gas G _{raz B} ) = 1000-1852⋅0.137 / (1.25⋅0.145) = 652 ° С.

What power will the gas turbine give with the following gas parameters in front of it t _{1 t} = t _{2 g} = 652 ° C, pressure p _{1 t} = 0.25 MPa, gas flow rate G _{raz B} = 0.145 kg / s: behind the turbine p _{2 t} = 0.02 MPa.

It is known that gas turbine units (GTU) using ordinary inert gases (He, N2, CO2, Ne, etc.) at a temperature level of 650-750 ° C have a low effective efficiency. cycle. In them, the share of the turbine power spent on gas compression is 65-80%, and only 20-35% of the turbine power is the useful work of the cycle, which can be additionally removed from the shaft, for example, by an electric generator.

The power on the turbine shaft is determined from the expression:

N _T = N _T ⋅M _T ⋅η _T ,

where N _t is the available differential of enthalpy in J / kg (enthalpy ΔH = С _rgaz ⋅Т) is the energy associated with this state of gas - temperature, pressure, speed); M _t = G _{raz B} = 0.145 kg, s - gas flow through the turbine; η _Т - effective turbine efficiency (0.7-0.8). For average gas values in a turbine:

ΔH _Τ = c _praз (t _{1 t} -t _2t ) = 1.25 (625-300) = 406 kJ / kg and then

N _T = 406⋅0.145⋅0.7 = 41 kW.

The air flow rate that will provide the turbine power at a pressure behind the compressor p _2k = 0.25 MPa and air temperatures up to t _1k = 20 ° C and after t _2k = 150 ° C:

G _w ⁼ N _T η _c / (p ₂ v ₂ -p ₀ v ₀ ) = N _T η _κ / [v ₀ p ₀ (T ₂ / T ₂ -1)] =

= 41000⋅0.7⋅ / [0.772⋅10 ⁵ (323 / 293-1)] = 0.91 kg / s.

There is enough power with a margin to drive the compressor. You can let most of the gas through the regulating diaphragm into the boilers through the air heater, which will further reduce the gas consumption for the gas generator’s own needs. Thus, the proposed installation for producing synthesis gas from water-coal fuel (VUT) allows, within a fairly wide range, to regulate the ratio between the combusted synthesis gas and gasified VUT.

The inventive installation is industrially applicable, as it includes real-life elements, the manufacture and installation of which is not difficult.

The inventive installation according to the principle of operation provided by a new set of essential features, allows for the high-quality gasification of high-temperature fuel from various coal to transfer fuel oil boiler plants to coal-fired.

Claims (1)

Installation for producing synthesis gas from water-coal fuel (VUT), including a vertically mounted gas generator with a gasification chamber for water-coal fuel and a separator connected to it for separating gaseous products of gasification and mineral waste, characterized in that it is equipped with a radiation heater VUT, located in the lower the conical part of the body of the gas generator, with a cooled VUT bunker for collecting the mineral part of gasification products and with a lock and an intermediate hopper for removing mineral oh part of the gasification products from the installation; the separator for separating gaseous products of gasification and mineral waste in the lower conical part of its body is equipped with a cooled VUT bunker for collecting the mineral part of gasification products and with a gateway and an intermediate hopper for removing the mineral part of gasification products from the installation; a countercurrent heater VUT is installed in the duct leaving the separator for separating gaseous products of gasification and mineral waste, and the duct is divided into two arms at the outlet: one to the gas turbine, the second through the control diaphragm to the air heater, which is connected to the air compressor through the duct, driven by a gas turbine; in the gas duct at the outlet of the air heater, an adjustable gas and air mixing device is installed, associated with gas burners tangentially installed in the upper part of the gasification chamber; gas burners are located in a horizontal plane, passing in the middle of the distance between the spray nozzles of the WCF, which are connected by pipelines to the radiation heater of the WCF; VUT heaters are connected in series between each other and at the outlet by two pipelines with spray nozzles, which are located opposite each other along the axis of the gas generator in the upper part of the gasification chamber and form a jet mill; the installation is equipped with devices for its commissioning on fuel oil: a fuel oil pipeline with shut-off valves connected to the VUT feed pipe, an air duct with shut-off valves connected to a gas-air mixture supply pipe to gas burners, an additional gas duct with shut-off valves connected to a gas duct with shut-off valves going to the boilers, into the boiler pipe.

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