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INVENTION
Russian Federation Patent RU2161168

EFFICIENT UTILIZATION OF FUELS AND WASTE containing chlorine and / or moisture

Name of the inventor: Norman L. DICKINSON (US); Kloska Michael K. (US); Robert G. Murray (US)
The name of the patentee: ENERTEK ENVAYRONMENTAL, INC. (US)
Address for correspondence: 191186, St. Petersburg, and / I 230, "ARS-Patent", VM Rybakov
Starting date of the patent: 1996.06.05

The method is intended for eco-efficient utilization of energy resources and various waste products. The method provides improved fuel structure, increasing its energy density and reduced impurity level in relation to low grade coals and / or carbonaceous wastes such solid waste fuels made from waste or waste water by formation of low-grade fuel, carbonaceous waste, or mixtures thereof Water slurries with a viscosity that allows them to carry out further processing. This initial suspension is heated under pressure (118), typically in the presence of a base (109) to a temperature at which there are significant changes in the physical and molecular levels, characterized by cleaving large parts are in low grade coals or carbonaceous wastes in a bound oxygen state in the form of carbon dioxide (147). Under these conditions, the solids of the initial suspension (103) substantially lose their fibrous and hydrophilic structure and disintegrate into smaller carbonized particles, which leads to the formation of the char slurry with dramatically improved rheology, ie. E. Capable of supporting significantly higher concentrations solid (and thus higher energy density) with acceptable viscosity. The invention provides energy security and air quality.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 is a diagram of an embodiment of the process of the invention, wherein the low rank coals and / or carbonaceous wastes in the form of a dilute suspension heated by indirect heat exchange under pressure, and converted to char slurry fuel with a high energy density and a low chlorine content.

FIG. 2 represents a variant of a process of the invention, wherein the low rank coals and / or carbonaceous wastes in the form of a dilute slurry under pressure and the preliminary phase direct heating with a stepped explosive release of steam from the char slurry and its conversion into slurry fuel on the basis of carbonized material with high energy density and a low chlorine content.

FIG. 3 represents a variant of a process of the invention, wherein the low rank coals and / or carbonaceous wastes in the form of a viscous suspension subjected to pressure, heat, are fed to the reactor with two mechanical screws providing backflow of fluid and solid carbonaceous substances, and converted into a fuel slurry char with high energy density and a low chlorine content.

FIG. 4 - is a schematic cross section along line 4-4 in FIG. 3.

DETAILED DESCRIPTION OF THE INVENTION

Option, which is illustrated by FIG. 1 relates to the implementation of the invention in relation to low grade coals and / or carbonaceous wastes containing non-combustible material heavier than water and / or one or more anions, such as chlorine, having corrosion properties, and / or atmospheric pollutants, and / or one or more ka IST newly forming a slag at temperatures of combustion and / or polluting. The municipal solid waste (MSW) are considered as an example, which may be modified by appropriate preseparirovaniya, but also derived from the existing landfill.

Carbonaceous waste is fed to the plant through a pipeline 101. Make-up water, waste water and / or suspension (such as untreated waste water) are served if required, on channel 102. Carbonaceous waste is crushed and mixed with recirculating water or make-up section 103 in the initial preparation of the fuel slurry as which can be used the equipment described in US patent N 4624417, relating to a "wet resource recovery." In section 103, heavy debris planting takes place and dirt and carbon material are dispersed, so they may be of separated metal, glass and other inorganic inclusions are heavier than water. Thus separated from the plant material derived via conduit or conduits 104. Section 103 may also be equipped to separate ingredients less dense than water, which are output on another line (not shown).

A suspension consisting mainly of carbonaceous wastes, is fed to the main hub 105 (as is any suitable dewatering device can be employed), which removes from it most of the water to form a pumpable carbonaceous slurry. The separated water is returned to the section 103 via a recirculation pump 106 of the main channel 107. Hardware section 103 and can work with low-grade coal and / or other carbonaceous wastes as described in the section "Background Art", or in a mixture with MSW or separately, in pauses between processing MSW.

It became a viscous carbonaceous slurry leaving the section (or sections) preparing a suspension of the starting fuel channel 108, the alkaline solution (or slurry) can be added to entering channel 109. Alkali is added in an amount which is at least a chemical equivalent of acid-forming anions in carbonaceous slurry. Alkalis are excellent agents that promote cleavage and neutralization of acid anions. However, in some cases, priority may be removing ka IST new, including forming toxins and potentially toxic metals. In such cases, the channel 109, instead of the alkali may be added solubilizing agents effective with respect to these elements, including, in particular, certain acids or chelating agents.

For some easily hydrolyzed wastes alkali additive prior to slurry carbonization results in an increase of soluble organic products at the expense of solid char, so that in such situations often be preferable to reduce or cancel the additive of alkali line 109 and neutralize acidic products at one or more points after or during slurry carbonization.

The apparatus 110 of heat transfer, such as a pump provides sufficient pressure to pump the carbonaceous slurry through the mixer 11, the gas and the slurry, wherein the slurry is contacted with a mixture of steam and gas carbonization flowing through the channel 112 and / or other heated fluid (not shown) . Gas-vapor mixture transfers heat directly to the slurry, raising its temperature. The heated slurry and noncondensed gas come together in surge tank 113, which separates residual gas and steam, which are displayed on the channel 114. The discharged gas, mainly carbon dioxide, is some heat value and can be fed into a furnace, boiler, or some another device (not shown) for recovery of its heat. Receiver 113 may be provided with heating means and thermally insulated for storing sensible heat, and there may be one or more mixers and / or recirculation channel 110 to a pump (not shown) to maintain uniformity of slurry properties.

In parallel with section 103, or instead may be one or more other types of preparation sections (not shown) adapted for fossil fuels or carbonaceous wastes to be slurry carbonization alone or in conjunction with materials fed conveyor 101. For example, low-grade coal, high grade coal, other fossil fuels and / or produced and / or utilizuemaya coal fines may be subject to preparation and / or grinding enrichment, as is usually done for a suitable initial suspension. IST solid obtained by conventional extraction of dry waste, ground and simply be dispersed in water or recirculation water feeding. Wood waste can be ground, subjected to magnetic separation to separate the iron and turn it into pulp. Other fossil fuel and / or waste such as sewage sludge, may require only the selection of water content. While high-grade coals, particularly those containing chlorine or substances forming the slag can be processed in a similar manner, sometimes more advantageous to skip a suspension based on these coals by equipment for slurry carbonization and blend it with solid char and / or suspension thereof. When required, carbonaceous slurry may be free of small particles by hydroclone hydroclone or adapted for this purpose. If necessary to make significant further dilution of the carbonaceous slurry in order to separate the inorganic substances, the purified slurry may undergo dehydration device 105 or similar purpose device.

This further prepared carbonaceous slurry may be introduced directly into the channel or channel 115 between section 103 and a device 110 (not shown) to the stage of carbonization or carbonization joint. This suspension may be fed into the receiver 113 and the channel 116 or channel 117 for receiving a high pressure line boot device 118. The charging device 118 may refer to a class of pumps, extruders, screws, or other known devices for pressurizing; thus possible to use one or more such devices in series or in parallel. mixer may be installed in the reception line of the charging device 118 (not shown). In addition, virtually dry or semi-dry low-grade coal, carbonaceous wastes, high-grade coals and / or other fossil fuels can be added directly to the receiver 113 through an additional channel (not shown). The charging apparatus 118 selects the carbonaceous slurry from the receiver 113 (and in some cases from the channel 117) and provides sufficient pressure to move it through subsequent equipment for the application of pressure and to maintain the slurry in a liquid state when heated.

Carbonaceous slurry flows from the device 118 to the cold side of the low temperature heat exchanger 119, where it is heated indirectly by means of the char slurry from a channel 125 to a temperature approaching the temperature of the substance. From heat exchanger 119 the heated carbonaceous slurry flows to the cold part of the high temperature heat exchanger 120, where it is heated indirectly by means of the char slurry from the channel 123. Each of the heat exchangers 119 and 120 may consist of a single or of multiple heat exchange modules arranged in series or in parallel. A device which separates the water from the heated carbonaceous solid substances (not shown) may be mounted between heat exchangers 119 and 120. In this case, preferably the separated water is sent to the corresponding heat exchanger (not shown) for taking heat from it, whereas the partially dehydrated the slurry flows to the heat exchanger 120.

The hot carbonaceous slurry flows from exchanger 120 to a heater 121, which is introduced as a supplement or alternative heat exchange in heat exchangers 119 and 120. Moreover, the heater 121 serves to compensate for heat losses and the irreversibility of heat exchange by providing a direct thermal balance required to raise the temperature to a suspension of value suitable for the carbonation reactions. The heat in the heater 121 is transferred indirectly, with steam (including steam mixed with gas released during the wet oxidation of the soluble organic component in the purification, as will be described with reference to FIG. 2), a special heat transfer fluid, a tube furnace, electric resistance elements, spirals, heated by hot flue gas or turbine exhaust gases and / or other suitable heat source. Alternatively, heat can be supplied to the heater 121 directly to the suspension by injection of high pressure steam (e.g. steam released during the wet oxidation of the cleaning process - see Figure 2..), The hot flue gas from the burner and / or small amounts of air or oxygen-containing gas.

In some embodiments, bleeding from the heater 121 to the entrance of the hot part of the heat exchanger 120 may take a period of time sufficient to complete the carbonization reaction. If a particular carbonaceous slurry requires more length of stay at a higher temperature than that provided by pumping time, the reactor 122 may be introduced to increase the reaction time in the reactor as a supplement or alternative energy supply 122 to the slurry in heater 121 may be provided with a jacket for heating by indirect a hot fluid which may alternatively be injected directly into the reactor along with hot slurry for the transfer of the surplus heat. In addition, it may be provided in channel 147 for discharging carbonization gas from the reactor as it is formed in order to shift the equilibrium of the slurry carbonization reactions upward char yield. Gas output channel 147 is hot and has a significant vapor content. In the interest of most of the contained sensible and latent heat can usually be removed, for example by means of heat exchangers (not shown) or by making direct contact with the slurry in the mixer 111 for example.

As a complement and / or alternative to adding alkali lye channel 109 through the connector 124 can be introduced into the channel, leaving the reactor section 122, a channel or entering the reactor 122 (this embodiment not shown). Dilute char slurry whose viscosity is significantly reduced, and the gas emitted during the carbonation reaction (the composition of which can be modified by the coolant injection), flow further through the channel 123 to the hot side of the high temperature heat exchanger 120 in which they transfer heat indirectly carbonaceous slurry which has been partially heated in the heat exchanger 119. The cooled by heat exchange in heat exchanger 120 char slurry and carbonization gas coming through the channel 125 to the hot part of the low temperature heat exchanger 119. The cooled char slurry may be further cooled by indirect heat exchange and / or direct contact with water, air or other cooling fluid (this process can be an alternative to the suspension cooled in heat exchangers 119, 120). As an alternative and / or supplement to the introduction of alkali channel 109 and / or channel 124, it can be injected into the channel 125 through the connector 126.

Cooled in heat exchanger 119 the slurry to the desired temperature, together with the carbonization gas is supplied through the channel 127 to the pressure reducer 128. The device 128 can serve to simultaneously reduce the particle size in the suspension using this kinetic energy released by increasing the volume of the suspension. The reduced pressure increases the volume of carbonization gas and increases the excretion of vapor resulting from evaporation of water from the slurry mixture as it moves toward the separator 129 and the gas suspension. In separator 129, the gas and steam separation, which receives, as described above, the channel 112 to the mixer 111.

Dilute char slurry, passing the separator 129 flows through the channel 130 to the device 131 char concentration. Concentrator 131 is illustrated as a centrifuge but it can be an evaporator, filter, or any other suitable device that separates slurry from the water discharged through the channel 132 from wet char, which is displayed in a conduit 133. Concentrator 131 may be adapted to wash the wet char before deducing the net and / or recirculating water from a channel 134, which meets with the fallout from the washing channel 132.

Recirculating water together with precipitation of washing accumulates in the recycle drum 135 from which it is pumped with an additional water pump 136 through the channel 137 in the slurry preparation section 103. However, it is usually required to remove soluble cleaning products, to prevent excessive accumulation of soluble compounds and their suspension. These cleaning products can be subjected before discharge treatment, a well-known technology in the water treatment or as described in U.S. Patent N 4898107. Alternatively, cleaning products can be separated from the hot slurry in the channel 123, as will be described with reference to FIG. 2, and subjected to wet oxidation to produce high pressure steam, heat supply to the heater 121 through direct or indirect and removing salt present in the form of brine. According to another embodiment, the water in the recirculation channel 137 may be processed by conventional processing methods effluent water in order to remove or reduce the content of dissolved materials and their suspension before reuse in section 103.

Wet char falling through conduit 133 is mixed in mixer 139 with clean and / or recycle water from the channel 134 in adjustable proportions to obtain the desired viscosity of the slurry. The resulting fuel product flowing through the channel 140 to the sizing device 141, in which the particles are removed with dimensions greater than the required, after which it is fed (if necessary with water) through the channel 142 to the device 143 to reduce the particle size, from which a suspension with reduced-size particles is returned via pump 144 to the slurry recirculation device 141. Due to the presence of this loop reduce the particle size of the maximum particle size in the suspension is in accordance with the specified size range, and then the slurry is discharged through a conduit 145 into the storage tank 146 of the final product, where it stored for future use or sale. The reservoir 146 is preferably provided with a mixer (mixer) or a recirculation system to maintain the uniformity of the product. Optionally, high-grade coal and / or other fossil fuel (dry, semi-liquid or as a slurry with sufficient energy density), but also liquid fuels, such as diesel fuel can be mixed with the finished slurry carbonized substances contained in reservoir 146, bypassing the carbonization circuit.

The finished slurry is stored in tank 146 or for use in place of its preparation, or for transportation through a pipeline into the tanks, water or other means in place of using 150 152 or type thermal power plant for the treatment of solid phase suspension.

In some cases, the circuit described particle size reduction may be combined into a single device which prevents the passage of too large particles and reduces their size to acceptable values. Sometimes, however, is justified with the grinding particle sizes lying within a certain range to ensure optimal particle size distribution, allows to achieve the maximum concentration of solids, i.e. maximum energy density at the specified viscosity.

Although a significant reduction in the content of inorganic impurities is achieved in the separation by density, carried out in the section 103, a sharp reduction in the size of the particles resulting slurry carbonization and / or subsequent mechanical comminution may, in some cases, result in the release of additional inorganic material which can be separated (due to its density, other physical and / or chemical properties), at any point of the reactor 122 and preferably upstream of the separator 131 with a hydroclone, flotation or any other suitable device.

If the char slurry is free of large particles that can clog the equipment installed downstream, the circuit 141-144 may be omitted. If the feedstock contains significant amounts of extractable anions or ka new LIU, the slurry can simply be adjusted to the desired viscosity in the device 131, instead of being subjected to complete separation with repeated to form a slurry in pure water. Alternatively, the circuit 141-144 particle size reduction can be placed in front of the hub 131.

example 1
In accordance with the embodiment illustrated FIG. 1, densified RDF, produced by dry resource recovery was ground to a particle size of 0.3 cm, mixed with sodium hydroxide and the aqueous suspension was transferred to a concentration of 7.2% by weight and a viscosity of 300 cps. Calorific value of the suspension based on the source of fuel (RDF) was 310 kcal / kg of the suspension at an oxygen content of 36.2% when calculated on the dry weight.

After increasing the pressure in the initial suspension IST she fed in a continuous pilot plant capacity of 285 kg / h, which used centrifugal and diaphragm pump. Preheating the slurry was carried out by three electrical heaters with a liquid coolant, the pressure and temperature of the suspension in the reactor and supported. After removal of the char slurry reactor temperature and its pressure is reduced by explosive evaporation to atmospheric pressure. Formed during explosive evaporation vapor and the gas is further cooled in a condenser with water cooling, the non-condensable gas is burned, and the condensate is pumped into the storage tank. The slurry after depressurization dehydrated using a filter press; particle size reduction performed using a mill.

The product obtained in a pilot plant under the conditions described, being diluted with water to a total solids content of 51.8% by weight, had an apparent viscosity of 500 cps, the calorific value of 3670 Kcal / kg slurry and an oxygen content of 13.9% in dry weight, based on the . Simultaneously the described conditions provides a level of chlorine extraction exceeding 94%, which was increased further by washing in the filter press. In addition, in the finished product, according to the analysis, it was significantly reduced content of nitrogen, sulfur, titanium, calcium, sodium, potassium, and trace metals such as mercury, antimony, arsenic, cadmium, lead, cobalt, copper, manganese and zinc.

Based on these test results, computer modeling was carried out installation of 500 t / day, corresponding to the embodiment of FIG. 1 and is used as a raw material of solid waste. With the use of standard methods and was found in the evaluation of the input value of the action of such a facility. The estimated total capital cost for the installation, with integrated wet extraction equipment resources amounted to 36.9 million US dollars at a rate of 15% reservation. Operating expenses (including maintenance) in the first year were estimated at 11.4 million dollars, including the financing of capital expenditures, debt service and depreciation. This corresponds to 69 USD. / T MSW, excluding revenue from the sale of recovered recyclable materials and the finished fuel suspension. Considering that the selling price of fuel is 7.73 USD. / Million kcal, net operating costs are down to 36 USD. / T MSW.

FIG. 2 illustrates another embodiment of the invention with respect to processing low rank coals and / or carbonaceous waste. It uses some of the elements and operations described with reference to FIG. 1 in particular, preparatory operations involving the addition of alkali or solubilizing agents, removal of inorganics, the selection of water content, particle size reduction and / or blending of carbonaceous wastes, low rank coals, other fossil fuels, and mixtures thereof.

Further, as shown in FIG. 2 prepared viscous slurry is fed to the channel 201. The carbonaceous slurry flows to the gas mixer 202 and the slurry in which it contacts the gas-vapor mixture supplied through the channel 203 and / or other heated fluids. Gas-vapor mixture gives off heat directly to the slurry, raising its temperature. The preheated slurry flows to the first device 204 increasing fluid pressure. The device 204 raises the pressure of the slurry to a level substantially lower pressure vapor mixture in the channel 205, so that the two streams may join in a second mixer 206. Any noncondensing gases and condensing steam dilute and raise the temperature of the slurry, which flows to the second pressurization unit 207 . The device 207 raises the pressure of the slurry to a level substantially lower pressure vapor mixture in the channel 208, so that the two streams may join in a third mixer 209. Any noncondensing gases and condensing steam further dilute and raise the temperature of the slurry that is supplied to the third device 210 pressurization. The device 210 and pressurizes the slurry to a level in the steam-gas mixture duct 211 substantially lower pressure, so that the two streams may join in a fourth mixer 212. Any noncondensing gases and condensing steam further dilute and raise the temperature of the slurry that enters the fourth device 213 pressurization. Device 213 similarly pressurizes the slurry to a level substantially lower pressure vapor mixture in the channel 214, so that the two streams may join in a fifth mixer 215. Any noncondensing gases and the steam condensing in the mixer 215 further dilute and raise the temperature of the slurry to a value of required for the slurry carbonization reactions.

Hot carbonaceous slurry is sent from the mixer 215 to the heater 216, which serves as a complement or alternative to the direct heat in devices 202-215. The heater 216 heat is transferred indirectly desired manner, for example using steam from an external source, a suitable fluid coolant, the tubular furnace, electric resistance elements, spirals, heated by hot flue gas or turbine exhaust gas and / or other suitable heat source. Alternatively, heat can be supplied to the heater 216 directly to the suspension by injection of high pressure steam from an external source, the hot flue gas from the burner and / or small amounts of air or oxygen-containing gas.

Although devices 204, 207, 210 and 213 to pressurize been described and shown in FIG. 2 as a discrete device, two or more of them may be separate units of a single device and / or receive power from a single source. Further, in the settings can include both more and less than four of such devices, which may be used as pumps, extruders, screws, and other known devices or combinations thereof.

The non-condensable gases can be separated and output from the main stream immediately after the mixers 202, 206, 209, 212 and / or 215. The output non-condensable gases can be fed to the furnace, boiler and / or other devices for disposal of any contained therein residual heat. Furthermore, between the devices to increase the pressure in the heated slurry may be conducted to its dehydration viscosity that allows the slurry to conduct further processing. The moisture removal is thereafter routed to a heat recovery device enclosed in it and / or it is re-directed to the preparation section (not shown).

Depending on the installation, pumping between the heater 216 and the separator 220 and gas suspension can take sufficient time to complete the carbonization reaction. If a particular carbonaceous slurry requires more length of stay at a higher temperature than the pumping time is provided to increase the reaction time, the reactor may be introduced 217. The reactor 217 may be provided with means to separate carbonization gas as it is formed, with its excretion by undepicted channel. In addition or as an alternative to the energy input in the heater 121 slurry reactor 122 may be jacketed for indirect heating by means of hot fluid which can alternatively be injected directly into the reactor along with hot slurry for the transfer of the additional thermal energy. As a complement or alternative to the heater 216 reactor 217 may be jacketed for indirect heating by means of hot fluid which can alternatively be injected directly into the reactor along with hot slurry for the transfer of the additional thermal energy.

For some easily hydrolyzed wastes alkali additive prior to slurry carbonization results in an increase of soluble organic products at the expense of solid char, so that in such situations often be preferable to reduce or eliminate the alkali additive in the section of preparation of the propellant suspension, and neutralize acidic products at one or more points, after or during slurry carbonization. As slurry carbonization products leave the reactor 217 through the channel 218 in the channel 219 of the supplemental channel can be injected solution or suspension of an alkali; alkali can be introduced into the channel and entering the reactor 217 (this embodiment not shown).

The channel 218 leads to the separator gas and liquid 220, made for example in the form of water trap. The separator 220 separates the gases generated during carbonization slurry and a gas introduced into the flow (and / or formed by wet oxidation of soluble organic products, as will be described hereinafter), and their removal channel 221. The gas channel 221 It is hot and has a significant vapor content. In the interest of most of the contained sensible and latent heat can usually be removed, for example by means of heat exchangers (not shown) or by making direct contact with the slurry, for example in the channel 201. Steam condensable from this stream it represents a potentially valuable source of relatively pure water.

Char slurry after the separator 220 flows through the channel 220 to the first stage separator 223 for separating the liquid and solid phases, the upper output of which is connected to the second stage separator 224 for separating the liquid and solid phases. As the separators 223 and 224 may be used, for example, hydroclone shown in FIG. 2. Naturally, the number of steps and the flow arrangement between them can be modified as needed. It is desirable that as much as possible of solid char with recycled water (which may contain dissolved gases) withdrawn through the bottom outlet of separators 223 and 224, which are configured in such a way that in the upper output is displayed portion coming from the separator 220 the liquid, which is a product of washing of the soluble organic and inorganic compounds.

There is also another cause for the withdrawal of this product through the upper outlet of separators based on the density difference. Despite the attention given to the conditions to maximize the yield of solid char and limiting (so far as possible) the formation of gas (carbon dioxide), carbonation slurry - is a form of pyrolysis which can result in the formation of small amounts of liquid hydrocarbons and / or tar. Furthermore, some particularly resistant polymers can not be decomposed and remain (but clicking under the action of temperature into a liquid form). These insoluble materials having a relatively high melting point as the cooling of the product can lead to clogging of subsequent stages equipment. However, having a lower density than water, they are located in the washing zone and consequently the products coming along with the water and dissolved organic substances for destruction by wet oxidation with generation of useful heat in the process of oxidation.

The pressure in the stream outputted through the top outlet of the separator 224 is increased by pump 225, which delivers the flow into mixer 226, where it mixes with the compressed oxygen-containing gas which enters through the channel 227 and to the extent that is possible, oxidizes the organic matter in the stream to carbon dioxide and water. In order to provide sufficient time to achieve the desired level of oxidation, a special section of the reactor 228. The oxidation releases sufficient heat to raise the temperature of the mixture to a level corresponding to the conversion of part of the water contained in it into steam.

A mixture of hot steam, gases and water that contains inorganic substances in solution or suspension (brine) enters the channel 229 in the separator 230 and a pair of brine. The separator 230 separates the vapor and gases which are output from the pressure control unit 231 and the channel 214 and fed to mixer 215 to heat the preheated suspension as already described. Brine secreted in the separator 230 is discharged from the process through a pressure reducer 232. It contains significant amounts of heat which must be disposed of in a suitable heat exchange equipment.

If the oxidizing agent supplied through the channel 227 is air, the vapor phase at the outlet 230 of the separator will have significant contents of nitrogen, which will accompany the slurry fully heated while passing through the reactor 217 to the separator 220. The partial pressure of nitrogen, the partial pressures with folded gases released by oxidation and slurry carbonization makes it necessary to maintain the pressure in the area between the device 213 and the separators 220 and 230 is much greater than the pressure of saturated water vapor. Additionally, heat loss associated with the formation of saturated steam in this case will be higher than when using industrial oxygen. The choice of oxidant is usually determined by local economic conditions, particularly the price of purchased oxygen.

Flow from the lower exit 223 and hydroclone 224 enters the channel 233 to the gear 234. The pressure drop on the output gear 234 results in explosive vaporization of the water from the slurry (optionally together with dissolved gases) while moving the mixture to the first stage separator 235 for separating char and suspension. The separator 235 separates steam from the slurry and flows through the channel 211 to the mixer 212, as previously described. The suspension is partially cooled and has become more concentrated as a result of the evaporation of the water contained in it comes from the bottom of the separator 235 to the second gearbox 236.

The pressure drop on the output gear 236 results in explosive vaporization of another portion of the water from the slurry (optionally together with dissolved gases) in the mixture flows to the second stage separator 237 for separating char and suspensions. The separator 237 separates steam from the slurry and flows through the channel 208 to the mixer 209, as previously described. The suspension is partially cooled and has become more concentrated as a result of the evaporation of the water contained in it comes from the bottom of the separator 237 to the third gear unit 238.

The pressure drop on the output gear 238 results in explosive vaporization of another portion of the water from the slurry (optionally together with dissolved gases) in the mixture flows to the third stage separator 239 for separating char and suspensions. The separator 239 separates steam from the slurry and flows through the channel 205 to the mixer 206, as previously described. The cooled slurry whose temperature is now only slightly higher than its boiling point at atmospheric pressure, and the concentration of which increased due to the evaporation portion contained therein water supplied from the lower output of the separator 239 to accumulator 240 from which further shows a small amount of vapor, whereby slurry cooled to the boiling point at atmospheric pressure. The steam from the accumulator 240 may be fed through the channel 203 for mixing with the incoming channel 210 the initial slurry (raw slurry fuel) in the mixer 203, as previously described. As shown in FIG. 2, separators 235, 237 and 239 may be formed as a water trap, the bottom of which outputs can be provided with a special tank (not shown) to maintain the required level of the suspension and to prevent release of steam in this direction.

Although devices 223, 224, 235, 237, 239 and 240 of the char slurry was considerable moisture and dissolved compounds removed it may be necessary to further concentrating the slurry to the desired viscosity. Then dilute slurry is supplied from the separator 240 through the channel 241 to the device 242 char concentration. Concentrator 242 is illustrated as a centrifuge but it can be an evaporator, filter, or any other suitable device that separates the water from the slurry withdrawn through the channel 243 from wet char, which is displayed in a conduit 244. Concentrator 242 may be adapted to wash the wet char prior to its excretion clean and / or recycled water from the channel 245, which occurs by precipitation in the washing channel 243.

Recycled water from precipitation with washing accumulates in the recycle drum 246 from which it is pumped with an additional water pump 247 through the channel 248 in the cooking section of the propellant suspension or recycle water treatment (not shown). It may be necessary, in addition to the brine is removed via the gearbox 232, to remove soluble cleaning products, for example through the flow control device 249 to prevent excessive accumulation of soluble compounds and their suspension. These cleaning products can be subjected before discharge treatment, a well-known technology in the water treatment or as described in U.S. Patent N 4,898,107. Recycled water from the channel 248 can be processed by conventional processing methods effluent water in order to remove or reduce the content of dissolved materials and their suspension before reuse in the fuel slurry preparation section (not shown).

Wet char falling through conduit 244 is mixed in mixer 250 with clean and / or recycled water from the channel 245 in adjustable proportions to obtain the desired viscosity of the slurry. Expansion volume and high velocity resulting from the action units 233, 235 and 237 lead to considerable fragmentation of particles. Nevertheless, it may be necessary to further particle size reduction. In this case, the fuel product is fed through the channel 251 to the calibration unit 252, which removes particles with dimensions greater than the required, after which it flows (if necessary with water) on channel 253 to device 254 to reduce the particle size of which suspension of particles with reduced size is returned via pump 255 to the slurry recirculation device 252. Due to the presence of this loop reduce the particle size of the maximum particle size in the suspension is in accordance with the specified size range, and then the slurry is discharged through a conduit 256 into the storage tank 257 of the finished product, where it is stored for future use or sale. The reservoir 257 is preferably provided with a mixer (mixer) or a recirculation system to maintain the uniformity of the product. Optionally, high-grade coal and / or other fossil fuel (dry, semi-liquid or as a slurry with sufficient energy density), but also liquid fuels, such as diesel fuel can be mixed with the finished slurry carbonized substances contained in reservoir 257, bypassing the carbonization circuit.

Depicted in FIG. 2 devices 252-255 for particle size reduction in some cases may be combined into a single device which prevents the passage of too large particles and reduces their size to acceptable values. Sometimes, however, is justified with the grinding particle sizes lying within a certain range to ensure optimal particle size distribution, allows to achieve the maximum concentration of solids, i.e. maximum energy density at the specified viscosity.

Although a significant reduction in the content of inorganic impurities is achieved in the separation by density, carried out in a slurry preparation section (not shown), drastic particle size reduction resulting slurry carbonization and / or subsequent mechanical comminution may, in some cases, result in the release of additional inorganic material which can It is separated (due to its density, other physical and / or chemical properties), at any point of the reactor 217 and preferably upstream of the separator 242 using a hydroclone, flotation or any other suitable device.

If the char slurry is free of large particles that can clog the equipment installed downstream, 252-255 circuit particle size reduction can not be applied. If the feedstock contains significant amounts of extractable anions or ka new LIU, the slurry can simply be adjusted to the desired viscosity in the device 242, instead of being subjected to complete separation with repeated to form a slurry in pure water. Alternatively, the circuit 252-255 particle size reduction can be placed in front of the hub 242.

To facilitate understanding in FIG. 2 shows the three stage pressure reduction in the char slurry. The more stages, into which the total reduction in pressure, the closer the system approaches the ideal (reversible) heat transfer and the less heat is required from the stage of oxidation in reactor 228 and / or the heater 216. The heat generated by the oxidation is dependent on the water-soluble organic compounds, the feedstock characteristics, temperature and time of carbonization and the choice of adding the alkali. In general, the goal is to maximize the production of solid char, which corresponds to minimizing production of soluble organics. The lower the yield of soluble organics, the larger the number of steps required to explosive evaporation achieve internal heat balance the system (without the assistance of heater 216). In many cases this number may be more than three. The heat generated by the oxidation, and can be adjusted by varying the pressure. Increasing the pressure increases the volume of water discharged as brine (ie to reduce the water converted into steam). Although in the ideal case a minimum amount of brine discharged water sufficient to ensure its free output from the system, it may be necessary to drop more water to maintain a heat and / or water balance. Another possibility is to control the variation of the degree of washing, ie fraction stream output from the upper output hydroclone to the pump 225. Lower rates correspond to washing, higher concentrations of organics and salts, and vice versa.

Carbonaceous slurry (slurry fuel) in the channel 210 has been determined as a viscous. Since the viscosity - a function of concentration, it can serve as a measure of the amount of water that must be heated to carbonization temperature and cooled again, in other words, a measure of the amount of heat that must be transferred. In the embodiment of FIG. 1, in which the bulk of the heat transfer occurs in the heat exchangers, viscosity is an important factor determining heat transfer rate and thus the required heat transfer surface area. The number and the cost of providing such a surface rapidly increases with viscosity. It is necessary to balance the opposing factors: the higher the viscosity, the lower the load, but lower heat transfer rate (and possibly more pronounced tendency to clogging of channels). Thus, the viscosity is mainly chosen for economic reasons.

The embodiment of FIG. 2 provides an I / O cycle, the heating / cooling without heat exchangers, thus avoiding the restrictions on the viscosity inherent to the embodiment of FIG. 1. In the embodiment of FIG. 2 it is possible to increase the concentration of suspension entering the carbonation step up to a paste. Importantly, the viscosity during heating is reduced several times by increasing the temperature and dilution, and as a result of carbonization reactions themselves. Because of this the most cost-effective level of viscosity (concentration) is often (though not always) is higher. It should be borne in mind that the ratio between the duration of heating and cooling in itself does not affect the costs, when these processes are carried out by pumping simple water and steam, as above hydroclone efficiency at a relatively low viscosity.

example 2
The second computer modeling applied to the plant with a capacity of 500 tons of solid waste daily (input) according to the embodiment of FIG. 2: when it is carrying out using the results of experimental check of the pilot plant described in Example 1. Using standard methods and was found input evaluation value in place of such an installation. The estimated total capital cost for the installation, with integrated wet extraction equipment resources amounted to 29.5 million US dollars at a rate of 15% reservation. Operating expenses (including maintenance) in the first year were valued at $ 10.5 million, including the financing of capital expenditures, debt service and depreciation. This corresponds to $ 63. / Ton of MSW, excluding revenue from the sale of recovered recyclable materials and the finished fuel suspension. Assuming that the selling price of fuel is 7.73 USD. / Million kcal, net operating costs are down to 42 USD. / T MSW.

FIG. 3 illustrates another embodiment of the invention which minimizes the ratio between heating and cooling, and provide direct heat transfer, without the use of heat transfer surfaces. It uses some of the elements and operations described with reference to FIG. 1 in particular, preparatory operations involving the addition of alkali or solubilizing agents, removal of inorganics, the selection of water content, particle size reduction and / or blending of carbonaceous wastes, low rank coals, other fossil fuels, and mixtures thereof. The concept version of FIG. 3 is advancing carbonaceous solids against a pressure gradient in the liquid by means of mechanical screw, so that the heat contained in the hot liquid in direct contact with the carbonaceous solids, is transferred to them, thereby providing the desired heat and therefore the reaction slurry carbonization.

As shown in FIG. 3, viscous slurry prepared starting fuel is fed to the channel 301 and its pressure is increased to a predetermined operating value in the device 302, increasing the pressure. As such pump device may be applied, an extruder, a screw or other known device or a combination of these devices. Device 302 from the pressurized viscous slurry flows into a vertical cylindrical vessel 303 in which a vertical worm conveyor uses two vertical rotating screws 304 and 305. The screws 304 and 305 rotate in opposite directions and are arranged so as to limit the flow of fluid between each the screw and the adjacent wall of the reactor. Augers 304 and 305 are located relative to each other so that one edge of the screw blade almost touches the other axis. The augers rotate synchronously, so that the closed volumes formed between adjacent turns of the screws are moved toward the upper end of the reactor 303, where the pressure is highest. As shown in FIG. 4, the reactor 303 has a double cylinder shape with a minimum gap between the turns of the screws and walls.

As explained previously, the carbonaceous slurry feed to the reactor 303 through the channel 301, it should be sufficiently dilute so that the pressure therein can be improved effectively. After increasing the pressure in a dilute suspension device 302 and feeds it to the reactor 303 its thickening produced by removing most of the water added for transporting, through the mesh filter 344. The pressure control valve 308 is operated so as to maintain a substantial pressure differential at the strainer 344, so that the water removal is carried out without reducing pressure in the reactor 303. Withdrawal added for the transport of water increases the concentration of the slurry carbonaceous solids, which are moved upward by rotating the screw windings 304 and 305.

Dashed line 306 corresponds to the cross section of the reactor 303, wherein the backflow fluid downward toward the flow of concentrated slurry upward absent or minimal. Highly concentrating the slurry can be achieved in that the lower section of said screw track pitch is made progressively decreasing the line so that the slurry as its upward movement under the action of the rotating screw is mechanically compressed. This densely packed slurry effectively prevents fluid flow in the reactor section 303. Above cross-section 306 turns the screw have a larger pitch so that the mechanical pressure on the carbonaceous solid slurry phase moving upward weakens, which allows to increase the liquid content in the slurry. This more dilute slurry allows the fluid to form a flow directed by a pressure gradient from the top down in it, i.e. against the direction of particulate movement. As this fluid stream may be below section 306, it should be removed from the reactor through a 345 mesh screen and further through the channel 309. The control valve 310 serves to ensure that a predetermined pressure is ensured during retraction of the fluid inside the reactor 303.

Solid carbonaceous particles above the line 306 are able to capture some amount of water; their concentration in the suspension is reduced, so that the hot water gets to flow down. As we move up the solids reactor 303 under the action of the screws 304 and 305, they are contacted by hot water flowing downward, are heated to the desired slurry carbonization temperature, and temperature is close to the temperature of hot water. The reactor volume and screw speed are selected to provide sufficient time to complete this direct heat transfer. Despite the attention given process conditions, carbonization suspension - is a form of pyrolysis which can result in the formation of small amounts of liquid hydrocarbons and / or tar. These insoluble materials having a relatively high melting point as the cooling of the product can lead to clogging of the equipment and the subsequent steps may lead to additional costs for the potential treatment of recirculating water. To prevent them, the hot water flow downwardly below the line 311 may be restricted by changing the pitch of the screws 304 and 305, so that a substantial proportion of hot water is removed via the channel 312. Pressure control device 313 controls the flow rate of the hot water in the channel 312 and the pressure reactor 303 above the line 311. a third filter screen 346 mounted between the screws 304, 305 and the reactor 303, the output from the reactor to prevent solids with hot water. The turns of the screws 304 and 305 by scratching the surface of the filter 346 to prevent buildup thereon carbonaceous solids. Part of the water removed from the slurry through the channel 312 may be cleaned and / or treated to remove and / or destroy the formed resin and / or hydrocarbons using known methods and / or wet oxidation, as indicated in the description of Figures . 2. If necessary, derived after the hot water treatment can be reintroduced into the reactor 303 through the channel 343 at a point above line 311 in order to provide the desired heating and concentration of solid particles flow downwards.

Above the solid carbonaceous particles 311 are able to capture some amount of water so that their concentration falls, and the hot water has to flow downwards. To compensate for heat losses and the irreversibility of heat exchange, hot water, high pressure steam or other fluids are introduced into the reactor 303 through the channel 314. Additionally, the reactor may be jacketed (not shown) for the indirect heating by hot fluid and as a supplement / or alternatives to the supply of energy through the channel 314.

Behavior carbonaceous slurry within the reactor with two screws will depend on the size of the reactor 303 and the screws 304 and 305, and the physical properties of the solid and liquid phases of the slurry. If the clearance between the walls of the reactor and the windings of the screws 304 and 305, and virtually no suspension of extremely concentrated, the device will act as an extruder and all material will be transported in the moving direction of the cavities between the windings. If between the screws and the walls of the reactor there are large gaps, and the suspension is diluted, the device will mix the slurry as it as it flows counter to the displacement direction of the cavities between the windings. Between these two processes there is an area of ​​such physical parameters of the equipment, which, in combination with certain slurry characteristics will provide the desired process oncoming fluid and carbonaceous solids. This reciprocal movement will take place when the combination of physical parameters and characteristics of the suspension will generate a continuous column of wet carbonaceous particles in the reactor height, if sufficient mechanical restrictions to generate backflow of solids. Wherein the mechanical force acting on the solid particles must remain below the "damage threshold" when a mechanical force (usually less than 7 kg / cm ^2, when measured as the pressure in the fluid) is proportional to the volume of water removed, and is not associated with These exponential dependence.

A vertical column formed by oppositely rotating screws, operated so that moving up solids reach the desired slurry carbonization temperature at the upper end of the reactor 303. Driven rotation of the auger 316 moves the horizontal solid carbonaceous particles together with a certain volume of water from the screws 304 and 305 into vessel 307 (which is virtually the same pressure as the reactor 303) and further to the outlet 347. the volume of vessel 307, and screw speed 316 such that sufficient time is provided to complete the desired slurry carbonization reactions. (Not shown in order to compensate for heat losses and / or in addition to heat supplied to the reactor 303 through the channel 314, hot water and / or high pressure steam may be injected through the channel 318 into the vessel 317. Moreover, vessel 317 may be jacketed ) for indirect heating by means of hot fluid. For certain values ​​of temperature, pressure and feed material during slurry carbonization it may be advantageous to partially or completely remove the carbonization gas and steam from the horizontal vessel with screw channel 315.

For some easily hydrolyzed wastes alkali additive prior to slurry carbonization results in an increase of soluble organic products at the expense of solid char, so that in such situations often be preferable to reduce or eliminate the alkali additive section slurry preparation and neutralize acidic products at one or more points after or during slurry carbonization.

From the vessel 317 char slurry flows through the channel 319 to the cold part of the indirect heat exchanger 320 where it is cooled by water, air, or another cold fluid coming from the duct 321 to the ambient temperature. This fluid respectively heated to a temperature close to the temperature slurry and flows through the channel 322 for further heating with a view to its use as hot water, high pressure steam and / or other fluid injected into the vessel 317 through the channel 318, and / or reactor 303 through the channel 314. The heat exchanger 320 may comprise one or more heat exchange modules arranged in series and / or parallel.

Cooled to a suitable temperature in heat exchanger 320, the slurry along with carbonization gas flows through the channel 323 to the pressure reducer 324 that reduces the pressure of the mixture. The device 324 may also serve to reduce the particle size in the suspension using the kinetic energy released by increasing the volume of the suspension. The reduced pressure increases the volume of carbonization gas and increases the excretion of vapor resulting from evaporation of water from the slurry mixture as it moves toward the separator 325 and the gas suspension, where the separation of gas and steam, which are displayed on the channel 326. The discharged gas, mainly carbon dioxide, It represents a certain value and the heat can be fed into a furnace, boiler, or some other device for its waste heat (not shown). In addition, gas and residual steam can be directed to the utilization device perceptible and latent heat.

Although the channels 307, 310, 312 and 326 of the char slurry was considerable moisture and dissolved compounds removed it may be necessary to further concentrating the slurry to the desired viscosity. Then dilute slurry is supplied from the separator 325 through the channel 327 to the device 328 char concentration. Concentrator 328 is illustrated as a centrifuge but it can be an evaporator, filter, or any other suitable device that separates water from the slurry. The separated water is discharged into the channel 329, while the wet char is output in conduit 330. Concentrator 328 may be adapted to wash the wet char prior to its excretion clean and / or recycle water from a channel 331, which occurs by precipitation in the washing channel 329.

Remote water is fed through the channel 248 in the slurry preparation section or recycle water treatment (not shown). It may be necessary to remove soluble cleaning products, for example, through the flow control device 333, to prevent excessive accumulation of soluble compounds and their suspension. These cleaning products can be subjected before discharge treatment, a well-known technology in the water treatment or as described in U.S. Patent N 4,898,107. Wet char falling through conduit 330 is mixed in mixer 334 with clean and / or recycle water from the channel 331 in adjustable proportions to obtain the desired viscosity of the slurry. Expansion volume and high velocity resulting from steps gear 328, and a crushing under the action of the screws 304, 305 and 316 lead to considerable fragmentation of particles. Nevertheless, it may be necessary to further particle size reduction. In this case, the fuel product is fed through the channel 335 to the calibration unit 336, which removes particles with dimensions greater than the required, after which it is fed (if necessary with water) through the channel 337 to the device 338 to reduce the particle size of which suspension of particles with reduced size is returned via pump 339 to the slurry recirculation device 336. Due to the presence of this loop reduce the particle size of the maximum particle size in the suspension is in accordance with the specified size range, and then the slurry is discharged through a conduit 340 into the storage tank 341 of the finished product, where it is stored for future use or sale. The reservoir 341 is preferably provided with a mixer (mixer) or a recirculation system to maintain the uniformity of the product. Optionally, high-grade coal and / or other fossil fuel (dry, semi-liquid or as a slurry with sufficient energy density), but also liquid fuels, such as diesel fuel can be mixed with the finished slurry carbonized substances contained in reservoir 341, bypassing the carbonization circuit.

Devices 336-339 for particle size reduction in some cases may be combined into a single device which prevents the passage of too large particles and reduces their size to acceptable values. Sometimes, however, is justified with the grinding particle sizes lying within a certain range to ensure optimal particle size distribution, allows to achieve the maximum concentration of solids, i.e. maximum energy density at the specified viscosity.

Although a significant reduction in the content of inorganic impurities is achieved in the separation by density, carried out in a slurry preparation section (not shown), drastic particle size reduction resulting slurry carbonization and / or subsequent mechanical comminution may, in some cases, result in the release of additional inorganic material which can It is separated (due to its density, other physical and / or chemical properties), at any point of the vessel 317 and preferably upstream of the separator 328 using a hydroclone, flotation or any other suitable device.

If the char slurry is free of large particles that can clog the equipment installed downstream, 336-339 circuit particle size reduction can not be applied. If the feedstock contains significant amounts of extractable anions or ka new LIU, the slurry can simply be adjusted to the desired viscosity in the device 328, instead of being subjected to complete separation with repeated to form a slurry in pure water. Alternatively, the circuit 336-339 particle size reduction can be placed in front of the hub 328.

The advantage of direct heat transfer over indirect in this case is to reduce hardware costs due to exclusion of the heat transfer surfaces and reduce thermal energy required for operation in the steady state. One of the advantages of the invention embodiment of FIG. 3 consists in that the solids content of the heat exchange section 303 of the reactor can be maintained at an optimum concentration level from the viewpoint of efficient transport with very little effect on the thermal efficiency.

As the consideration of the above embodiments, the overall thermal efficiency of fuel combustion depends on several factors such as the moisture content of the fuel, the extent of carbon combustion, excess air, the temperature output of the flue gas and parasitic losses due to fuel supply, ventilation, removal of ash consumption energy (including pressure drop) from air pollution control devices (GLC), and so on. g. Natural gas has been called the perfect fuel since it is almost or completely free from moisture, carbon burnout degree almost equal to 100% with nominal excess air, the temperature output from the flue gas can be minimized with minimal parasitic losses as flue gas clean enough (no ash, low levels of nO _x and CO emission). Ash-free distillate fuel, probably is in second place. It requires several high excess air for complete combustion, and usually results in parasitic losses slightly higher than in the case of natural gas because of the necessity to use the fuel pump. For fuels from residual oils, substantially free from moisture, high degree of combustion with moderate excess air, but soot blowers may be required of the device. The temperature of the flue gas withdrawn, as a rule, should be above the acid dew point, require equipment to control ash emissions, such as baghouse, and depending on the sulfur content may require the use of lime or the use of scrubbers, which means that the loss rate of low to moderate.

Carbon fuels are significantly different for the ash content, moisture content, sulfur and nitrogen. In general their most efficient combustion is achieved for the coal dust burners which provide a high degree of combustion air at a moderate excess. The temperature of flue gases to be displayed above the acid dew point. Parasitic losses, including the losses associated with grinders and SGC devices, range from moderate to high, depending on the level of impurities. In addition, coal dust requires more residence time in the combustion process than natural gas and liquid fuels. When coal fuel is burnt in the combustion chambers in mechanical layer, with vibrating or moving grates, to achieve a high degree of combustion of carbon requires a large excess of air, respectively, and parasitic losses higher than that for the coal dust burner.

MSW, mass in case of combustion using moving grates or fluidized bed, or as RDF, has the lowest combustion efficiency. High moisture content and unstable in the MSW requires excess air at 100-150%, to provide an acceptable level of combustion, at much higher losses associated with shredders, solids conveyors for, fans for air supply, fabric filters, devices for SGC acid _gas, NO x, traces of toxic metals and dioxins. In connection with the greater volume of flue gas, the need to achieve efficient combustion of carbon and stringent requirements on gas emissions, parasitic losses increase to a level almost twice the rate for the equivalent coal-fired boilers.

With the present invention, MSW and other low grade carbonaceous fuels and wastes are converted into a uniform liquid fuel which can be burned like fuel oil, with the exception that may need to increase productivity tools for removing ash (although its level remained below the level typical for a coal dust and MSW). In addition, the majority of toxic metals and chlorine are removed from the finished slurry, simplifying or even makes it unnecessary to use these substances emissions control systems. Reactivity is so high that virtually 100% carbon combustion is achieved at an excess of air not higher than 15%. Unlike current practice, does not require any devices for SGC acid gas or _NO x. The only factor that reduces the efficiency, the moisture content is about 50%.

To evaluate the indicators achieved by the present invention was carried out slurry carbonization applied to samples of RDF, lignite coal, and a mixture containing 50% of brown coal (CU) and 50% RDF (dry weight) in a laboratory setting and in a continuous pilot plant, referred to in Examples 1 and 2. Table 1 shows the content limits (in weight% moisture at zero), the combustion heat (in dry form and in suspension) and rheological characteristics of the propellant and the final carbonized product (CP). Carbonized product of brown coal and the mixture BU / IST was obtained in a laboratory setting, and of RDF - a pilot.

Through slurry carbonization reduced oxygen content was achieved for each carbonaceous fuel, while the dry heat of combustion of carbonized product was increased. Oxygen was deduced from the carbonaceous solids in a gas - carbon dioxide. With respect to the oxygen content of RDF was reduced by 64% (based on dry weight), and the calorific value increased by 72% (based on dry weight). Furthermore, by using the present invention the solids content in the product char slurry was increased to 51.8% by weight, ie. E. More than 460% relative to the starting fuel slurry. The heat of combustion of the char slurry amounted to 3670 kcal / kg suspension. The solids content in the mixture of lignite / RDF was higher than in the slurry of each component separately, due to the bimodal distribution of particle sizes mixture. In separate experiments to evaluate the effectiveness of wet grinding RDF char solids content of the starting material slurry was 49.2% by weight, whereas grinding permitted to carry the content by weight of 51.8% at the same viscosity.

When processing according to the present invention, the concentration of chlorine in the carbonized IST in the case of adding sodium hydroxide (NaOH) was reduced by 85% compared to baseline IST. When added to the initial slurry of lime (CaO) content of chlorine was reduced by 91%. In separate experiments, char product was washed with water containing no chlorine and the chlorine content was further reduced. The chlorine content in the mixture of the carbonized lignite / RDF was lower than when using only LIU (in the case of adding to the starting slurry CaO and NaOH) due to that contained in the lignite reacting with the chlorine alkali.

To confirm the quality of slurry fuel obtained according to the present invention, the char slurry that was obtained in the experiments in a pilot plant mentioned in Examples 1 and 2, burned in the boiler simulator for the coal dust (UE) with a capacity of 164,000 kcal / h. In addition, the suspension obtained from IST described method was mixed with 7.5% diesel fuel (DF) and combusted in the same simulator. Further, the suspension obtained from brown coal, RDF, and a blend of 50% lignite with 50% RDF (dry weight) were burnt under pressure in the pilot fluid bed reactor (RSPS). Combustion conditions and impurity content in the flue gas without any SGC devices are shown in Table 2.

The emission of impurities from the combustion of all five suspensions fuel was extremely low. Despite the fact that the excess air was only 15,0-40,3%, emissions of carbon monoxide (CO) for fuel suspensions based on RDF was 67-96% below the level in accordance with the new standards for emission for municipal incinerators (NSCR USA, 1994 YG). This low level of CO emissions were achieved due to the high reactivity of the char slurry (high content of volatile components as compared with a fixed carbon), increased uniformity, improved mixing of the fuel with air.

Since slurry carbonization extracted a significant proportion of the chlorine and sulfur anion / ka new LIU toxic metals, HCL were significantly lower emissions requirements, even without selective noncatalytic or catalytic abatement methods. Although the measured content _of SO ₂ emissions for the suspension of the IST slightly exceeded the requirements NSCR, we must note that these requirements are consistent with the share of allowable concentration for boilers, coal-fired, according to the Supplement to the Clean Air Act (DZCHV). To a suspension based on carbonized mixture lignite / RDF emissions were 72% lower than for suspensions based on brown coal, and in both cases they conform DZCHV Phase II. Without the use of slurry carbonization SO ₂ emissions from the source of lignite or brown coal mixture / IST would not meet these requirements. Furthermore, emissions of mercury (Hg) for fuel suspensions based RDF char were 95% below the level NSCR provided through removal of a considerable part of the mercury during operation and resource extraction slurry carbonization.

print version
Publication date 06.11.2006gg

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