WO1992001627A1

WO1992001627A1 - High surface area hydrated lime and methods

Info

Publication number: WO1992001627A1
Application number: PCT/US1991/005226
Authority: WO
Inventors: David L. Moran; Massoud Rostam-Abadi
Original assignee: Research Corporation Technologies, Inc.
Priority date: 1990-07-24
Filing date: 1991-07-24
Publication date: 1992-02-06
Also published as: EP0559650A4; CA2087173A1; EP0559650A1; CA2087173C; AU8409891A

Abstract

Hydrated lime having high surface area and small particle size is prepared by hydrating lime with an aqueous hydration solution of an organic solvent, and preferably washing the resulting hydrate with an aqueous solution of an organic solvent prior to drying. The high surface area hydrates of the invention are excellent sorbents for SO2 removal from gas streams.

Description

HIGH SURFACE AREA HYDRATED LIME AND METHODS

CROSS-REFERENCE TO RELATED APPLICATION

This is a continuation-in-part of copending U.S. application Serial No. 07/557,590 filed July 24, 1990, the disclosure of which is incorporated herein by reference.

BACKGROUND OF THE INVENTION

Field of the Invention

This invention relates generally to hydrated lime and methods for preparation and use thereof and, more particularly, the invention is directed to an improved process for making hydrated lime having favorable physical properties such as high surface area, high porosity, and small particle size, which in turn provide favorable SO₂ capture properties.

Description of Related Technology

Dry sorbent injection technologies offer many advantages over other systems, notably wet flue gas systems, for desulfurization in controlling the emissions of SO₂ produced during combustion of high sulfur coal. Some dry sorbent injection technologies, including furnace sorbent injection (FSI), boiler economizer injection, and post furnace ductinjection/humidification (Coolside) systems have been extensively researched.

A distinguishing factor of dry processes is the injection of a calcium-based sorbent such as hydrated lime (Ca(OH)₂) into different locations within a pulverized coal boiler unit. In FSI systems, calcium sulfate is formed by reaction of calcium oxide (CaO) (formed by calcining of calcium carbonate or calcium hydroxide) with SO₂. Under boiler economizer and

Coolside conditions, CaSO₃ is the major product of the reaction between Ca(OH)₂ and SO₂.

A major objective of research has been to identify sorbent properties that result in enhanced SO₂ capture in order to reduce operating costs and the amount of waste products. In FSI systems, the

superiority of calcium hydroxide over calcium carbonate as a sorbent has been attributed to the smaller mean particle size, higher surface area, higher pore volume, larger mean pore diameter, and plate-like grain

structure (as opposed to sphere-like grain structure) of CaO derived from Ca(OH)₂ compared to that derived from calcium carbonate. In boiler economizer and

Coolside studies, improved SO₂ removal performance has been reported for calcium hydroxide with high porosity, high surface area, and small particle size.

Thus, it is desirable to provide calcium hydroxide having high surface area, high porosity, and small particle size for use in SO₂ sorption, and for other physical processes relying on the sorptive capabilities of calcium hydroxide.

In the past, conventional hydrates of calcium produced by slaking lime (CaO) produced by burning limestone (CaCO₃) in a kiln have been limited with respect to these desirable physical properties. Such hydrates have been characterized as having surface areas in the range of about 10-25 m²/g, mean particle diameters of about 1.7-10 micrometers, pore volumes in the range of about 0.1-0.25 cc/g, and crystallite sizes of greater than about 200 Angstroms (based on a + c axis dimensions). Several investigators have

reportedly prepared small quantities of limes hydrated by contact with an aqueous alcohol solution having surface areas in the range of 35-50 m²/g. Bestek, et al. U.S. Patent No. 4,636,379 (January 13, 1987) describes a seven-stage continuous methanol/water hydration process in which hydrates having surface areas in the range of about 35-55 m²/g are reportedly produced. These hydrates are believed to exhibit mean particle diameters of about 1 to about 2, and typically about 1.4, micrometers. Reportedly, very small quantities of hydrates having surface areas as high as 80 m²/g have been obtained by calcining (dehydrating) commercial hydrated lime and rehydrating it using an alcohol-water hydration method.

There remains a need in the field for an industrially practical, efficient method of preparing high surface area hydrated lime having all the

necessary physical properties for efficient sulfur dioxide sorption, and for other purposes.

SUMMARY OF THE INVENTION

It is an object of the invention to overcome one or more of the problems described above.

According to the invention, high surface area hydrated lime is prepared in an efficient, practical process wherein lime, which has been prepared directly by calcining limestone, is hydrated by contact with an aqueous solution of a slaking rate retarding organic solvent. According to the inventive method, lime is mixed at a temperature which is sufficiently low to produce a homogeneous slurry with an aqueous/organic solvent hydration solution containing a sufficient amount of water relative to the lime to result in a desired degree of hydration, at least partially

hydrating the lime at a moderately elevated

temperature, further hydrating the resulting lime paste at the boiling point of the hydration solution, and drying the resulting powder at an elevated temperature to produce a high surface area hydrated lime product.

In preferred embodiments, the organic solvent is a lower alcohol, and the lime may be a high surface area lime prepared by calcining limestone under low temperature, low carbon dioxide conditions. The hydrated lime may be washed in an aqueous/organic solvent in order to displace water prior to drying to further increase surface area and reduce particle size.

In addition to the inventive method, the invention comprehends the high surface area hydrated lime product, and methods of sorbing SO₂ from waste gas streams using the high surface area hydrated lime as a sorbent.

The invention allows the physical properties of hydrated lime to be controlled for optimum

suitability for use in any of a variety of dry sorbent injection systems for SO₂ removal.

Other objects and advantages will be apparent to those skilled in the art from the following detailed description, taken in conjunction with the drawings and the appended claims.

BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a schematic flow diagram of one embodiment of a process for preparing high surface area hydrated lime according to the invention.

Figure 2 is a schematic flow diagram of another embodiment of a process for preparing high surface area hydrated lime according to the invention.

Figure 3 is a schematic flow diagram of a modified form of the process of Figure 2. Figure 4 is a graphical depiction

illustrating the effect of the processing temperature profile on the physical properties of high surface area hydrated lime products.

Figure 5 is a graphical depiction of temperature profiles obtained in processing several different limes into hydrates.

Figures 6A, 6B and 6C graphically depict the degree of SO₂ removed from waste gas streams as a function of surface area for several hydrated limes under furnace sorbent injection, boiler economizer, and Coolside conditions, respectively.

Figure 7 is a graph illustrating cumulative pore volume vs. pore diameter for high surface area and commercial hydrated limes.

DETAILED DESCRIPTION OF THE INVENTION

According to the invention, lime which has been prepared directly by calcining limestone is hydrated by contact with an aqueous solution of an organic solvent which is effective in retarding the rate of hydration ("slaking") of the lime. If desired, the product can be washed with another solution of an organic solvent in a post-hydration wash step in order to displace water before drying in order to further increase surface area and reduce particle size. The inventive method is capable of producing a hydrate with an N₂-BET surface area of greater than 35 m²/g, and preferably greater than 55 m²/g. Surface areas of up to 85 m²/g are readily obtainable.

Preferred organic solvents useful in the hydration and washing steps are lower alcohols,

particularly methanol and ethanol. Throughout the following description, whenever reference is made to "alcohol" such reference is made to the preferred materials, but these teachings are to be understood to apply to useful organic solvents generally. The scope of the invention is not to be construed as being limited by such reference to the preferred alcohols.

Lime which has been prepared either commercially in a kiln at a high temperature and/or under high carbon dioxide concentration conditions or in a kiln, fluidized bed reactor, entrained flow reactor, or other calciner under conditions of low temperature and low carbon dioxide concentration conditions may be used as a starting material.

Figure 1 illustrates a process for hydrating lime using so-called "commercial" limes which are defined as being produced by calcining limestone in kilns in an environment having a relatively high (e.g., greater than 25 vol. %) CO₂ level and/or at high temperatures (i.e., above 1100°C) at a residence time of about 1 to about 3 hours or higher, depending on the type of kiln.

According to the procedure of Figure 1, lime (preferably minus 100 mesh in size) is mixed with an alcohol-water solution in a mixing stage 1 maintained at a temperature, preferably below about 40°C, which is sufficiently low to achieve a homogeneous slurry.

All or less than all, and preferably about 50%, of the water required in the process is added in the mixing stage. Any remaining portion of the water is added in the hydrator 2, located downstream. The alcohol-water solution required for the overall process need contain only a sufficient amount of water relative to the lime to result in a desired degree of hydration, usually at least 0.9 and preferably at least about 1 and less than about 2 times (highly preferably about 1.0 to about 1.4 times) the stoichiometric amount of water relative to lime and about 0.5:1 to about 5:1 (preferably about 1:1 to about 3:1) volumetric ratios of alcohol to water. For each kilogram of lime about 0.4 to about 4 liters (preferably about 0.8 to about 1.4 liters) of hydration solution is used.

Ratios of alcohol to water in excess of 5:1 may be used, especially with highly reactive limes, where hydration solutions may contain up to 75 to 85 vol.% alcohol, if desired. For example, with a

hydration solution containing 85 vol.% alcohol, the alcohol to water ratio is about 5.67:1. Such high ratios of alcohol to water are especially suitable with limes having very high surface areas (e.g. 10 m²/g or more).

In all embodiments of the invention, thorough mixing of the hydration solution and the lime is important. High speed, intensive mixing is very helpful, and may be necessary with very reactive limes, for good heat transfer. For extremely reactive limes, cooling of the mixing vessel may be required. An alternative approach is to use a split water stream to minimize the rapid temperature rise when a highly reactive lime is processed. In embodiments using an alcohol wash step, greater amounts of water may be used, since it will be displaced in the wash step.

The alcohol or other solvent in the hydration solution retards the slaking rate, and maintains the temperature of the hydration mixture below the boiling point of water (thus preventing or minimizing the degree of gas phase hydration, which would inhibit surface area development). In addition, the use of alcohol or other solvents lowers surface tension and helps prevent agglomeration, which leads to increases in surface area due to increased dispersion. The solvent also lowers the solubility of the hydrate, thus promoting precipitation of hydrate from the solution of lime in water.

Hydroxyl carboxylic acids and/or surfactants or other additives may be used in combination with the alcohol in the hydration solution to further reduce the hydration rate, thus increasing hydrate surface area and decreasing hydrate particle size. Acid

concentrations of 3 wt.% or less based on water are preferred, and concentrations of about 0.5 to 1 wt.% are highly preferred. Surfactant concentrations of 2 wt.% or less are preferred, depending on molecular weight, and concentrations in the range of 0.2 to 1 wt.%, and preferably less than 0.5 wt.% are typical.

Useful acids include lactic acid, glyceric acid, citric acid, maleic acid, tartaric acid, gluconic acid, and others. Useful surfactants include those of the Triton X series, sodium dodecyl sulfate, sodium abietate, Vinsol, etc. Acids are believed to function by inhibiting the growth of calcium hydroxide

precipitates in order to affect the size and shape of the crystals. Surfactants function by sorbing onto the surface of the calcium hydroxide nuclei, and cause the crystals to better disperse by repulsion due to ionic or steric stabilization.

Other useful additives which affect hydration rates and hydrate properties include phosphates, borates, fluorides, sulfates, and silicates, as well as sugars (e.g. sucrose, glucose, etc.) and

lignosulfonates which contain sulfonate and carboxylate groups.

The slurry from the mixing vessel 1 enters a hydrator 2 which may be integral with the mixer 1 and which can include a preheating stage, a paste mixing stage, and preferably a drying stage. The types of mixing elements (blades) used in each stage are selected to accomplish thorough mixing of the slurry, paste, and the powder phases present in the hydrator. The mixing stage 1 and the hydrator 2 can be

incorporated into one vessel, or in separate single or multi-staged vessels, with or without internal walls to physically separate stages, as desired. Similarly, each of the preheating and paste mixing stages can be incorporated in one mixer/hydrator or hydrator vessel, or in separate single or multistaged vessels, with or without internal walls. The drying stage can be accomplished in a separate vessel, preferably in a vacuum drier, or may be incorporated into a single vessel which includes the hydrator 2 and the mixer 1, if desired.

The remaining portion of the hydration water, if any, can be added in the preheating stage or in the paste mixing stage of the hydrator 2. In the

preheating stage, the slurry is heated, autogenously or by external heating means, if necessary, to a

temperature, preferably at least about 40°C and up to about 70°C, which is sufficiently high to sustain the hydration reaction. The temperature may vary depending on the type of organic solvent used. The residence time in the preheating stage is typically between about 1 and about 10 minutes. In the paste mixing stage, the partially hydrated paste from the preheating stage is heated autogenously to the boiling point of the

hydration solution due to the exothermic nature of the hydration reaction. Hydration temperature is dependent on the boiling point of the hydration solution.

(Methanol boils at 64°C, and ethanol boils at 80°C at atmospheric pressure.) The residence time in this stage is typically between about 3 and about 10

minutes. The crude product exiting the paste mixing stage is in powdered form. In the drying stage, the crude product is heated, possibly autogenously (although heat may be applied from an external source, if necessary) to about 60 to about 110°C for a residence time of about 3 to about 30 minutes. Additional hydration occurs during the drying stage with the final product typically containing greater than about 90 wt.% calcium

hydroxide, depending on the purity of the lime.

Greater than about 95% conversion of calcium oxide to calcium hydroxide requires greater amounts of water, which in turn leads to undesirable degrees of grit formation, and possibly to reduction in attainable surface area. About 90% conversion (hydration) is optimum for obtaining high surface area and small particle size.

The drying stage can be accomplished in a separate vessel (preferably a vacuum drier) to provide greater operating flexibility. The drying stage can also be accomplished in two separate vessels consisting of an atmospheric drier and a vacuum drier to improve alcohol recovery. If all of the hydration solution is driven off in the hydration stages, no drying stage separate from the preheating and paste mixing stages is needed.

Use of water at less than a 1.2 times

stoichiometric ratio typically results in less than about 90% hydration. Operation at more than 1.5 times stoichiometric ratio of water can result in the

production of large quantities of grit, depending on the ratio of hydration solution to lime. When an alcohol wash step is used (see Figure 3) , however, a stoichiometric ratio of 1.5 appears to result in optimum hydrate surface area.

For hydration solutions containing about 1.0 to about 1.4 stoichiometric amounts of water with respect to lime, low hydrate surface areas (less than 30 m²/g) result when less than about a 1:1 volumetric ratio of alcohol to water is used. An alcohol to water ratio of greater than about 3 : 1 results in the

production of soft agglomerates, which require milling. Surface area begins to decrease if alcohol to water ratios exceed about 6:1.

Total residence time in the hydrator is determined by the time required to evaporate hydration solution, which is a function of the reactivity (and thus surface area) of the lime and the amount of liquid present. Sufficient hydration solution should be present to prevent hydration temperatures from

exceeding about 115°C.

At startup, the hydrator 2 is preferably provided with a flow of nitrogen or other inert gas to purge oxygen-containing gas from the hydrator. The nitrogen purge can also be used during operation to provide heat for the drying and/or preheating stages (if needed), maintain pressurization of the hydrator to about 1 to about 15 psig to prevent leakage of oxygen into the system, and remove the organic solvent vapor generated during operation. The solvent vapor/nitrogen stream enters a condenser 4 to recover and cool the solvent which is then recycled to the mixing vessel 1. The nitrogen stream exiting the condenser 4 is heated to about 80 to about 110°C in a heater 5 and recycled to the hydrator 2.

Alternatively, or in addition, heating for the preheating and drying stages, if necessary, can be provided by external heating units, such as steam jackets.

The hydrate exiting the hydrator 2 can be subjected to an air classification and milling stage 3, if necessary, to separate any undesired grit particles formed during the hydration process. Thus, hydrates with surface areas between about 35 and about 50 m²/g and mean particle diameters between about 1 and about 3 micrometers are produced, depending on the hydration conditions and type and properties of the lime used.

The foregoing parameters, and those which follow, are derived from observations of batch mode operation, and while they may vary somewhat with continuous operation, are believed to be consistent with results obtainable under continuous operation conditions.

Figures 2 and 3 illustrate embodiments of the inventive process wherein high surface area hydrates are made using limes having relatively high surface areas, produced by calcining limestone under low temperature, low carbon dioxide conditions.

According to the embodiment of Figure 2, higher surface area hydrates can be made using limes that are produced by calcining limestone (preferably greater than about 95% calcium carbonate) in a calciner 6, preferably at atmospheric pressure and for residence times of about 1 to about 3 hours at temperatures between about 800 and about 1100°C (generally less than 950°C, preferably less than 900°C) under a gas

environment in which the partial pressure of carbon dioxide (CO₂) is as low as possible, i.e. below about 0.25 atmospheres (25 vol.%) (preferably below about 0.2 atmospheres (20 vol.%)) for calcinations carried out at atmospheric pressure. If desired, calcining may be carried out below atmospheric pressure. The percentage of calcium carbonate (preferably greater than about 95 wt.%) in the limestone from which lime is made is important to the ultimate hydrate surface area. Inert impurities, such as silicates, aluminum and iron oxides, and magnesium carbonates and oxides, do not hydrate and their presence lowers the surface area of the hydrated lime product.

Low CO₂ partial pressure and low calcination temperature conditions are ideal for producing, depending on the properties of the limestone feed, limes with N₂-BET surface areas at least about 2.5 m²/g, and preferably at least about 3.5 m²/g. The

temperature and residence time are selected to minimize growth of crystallites (i.e. to minimize sintering). A fluid bed reactor (such as a circulating fluid bed reactor) or an entrained flow reactor are ideal for the calcination because of their excellent mass and heat transfer characteristics which allow calcination to be accomplished at low temperatures and at residence time comparable to those of commercial kilns. A commercial kiln operated at low temperatures and purged with air or an inert gas to dilute the CO₂ concentration can also be used. The limestone particle size preferably is minus 1 inch in size for a commercial kiln, minus 8 mesh in size for standard fluid bed reactors, and minus 50 mesh in size for circulating fluid bed and entrained flow reactors.

Calcination conditions (pressure,

temperature, gas flow rate, CO₂ partial pressure, and residence time) needed to obtain lime with a given surface area are related to the reactor configuration and limestone properties. Several impurities in limestone such as aluminum oxides, iron oxides and alkali metals lower lime surface area during

calcination due to their lowering of eutectic

temperatures of calcium-based compounds (i.e.,

increased fluxing). For high purity limestone (greater than 98% calcium carbonate and less than 0.05% total alkali) the influence of calcination conditions on lime surface area is not critical. Some calcination conditions may be varied (e.g. extremely high temperatures such as 1200°C may be used) if other conditions (e.g. short residence times such as 1 to 10 seconds) are favorable. Selection of appropriate conditions is within the skill of those familiar with the art, guided by the present

disclosure.

Hydrates may be prepared from the high surface area limes either without (Figure 2) or with (Figure 3) a post-hydration wash step.

As in Figure 1, the mixing and hydrator stages of Figures 2 and 3 may be embodied in separate vessels or in a single vessel, and the preheating, paste mixing and drying stages of the hydrator can be formed in a single hydrator vessel (with or without internal walls to physically separate stages) which may also include the mixing stages, in particular when "commercial" lime is being processed. If preheating, paste mixing and drying stages are carried out in a such vessel without internal walls, a twin screw blade is preferred to transfer and blend the paste.

Reference to the various stages by different reference numerals and illustration in the figures of separate mixing and hydrator vessels is exemplary only, and is not to be construed to limit the invention.

In Figure 2, the lime (preferably minus 100 mesh in size) is mixed with an alcohol-water hydration solution in a mixing stage 7 maintained at a

temperature (e.g., below about 40°C, preferably below about 30°C) selected to produce a homogeneous slurry. All or less than all, preferably about 50%, of the water required in the process is added in the mixing stage 7, as described in the embodiment of Figure 1. Any remaining portion of the water is added in the hydrator 8. The alcohol-water solution required for the overall process preferably should contain at least about 0.9 and preferably at least about l and less than about 2 times the stoichiometric amount of water

(preferably about 1.0 to about 1.4 or about 1.1 to about 1.7 if a post-hydration wash step (Figure 3) is used) and at least about 0.5:1, and preferably up to about 5:1 (highly preferably about 1:1 to about 3:1) volumetric ratios of alcohol to water. For each kilogram of lime about 0.4 to about 4 liters

(preferably about 0.8 to about 1.5 liters) of solution is used. In general, a lower mixing temperature is preferred for more reactive limes. Surface area of hydrate tends to increase as mixing temperature is lowered. Lower temperatures also avoid thermal runaway due to the exothermic nature of the hydration reaction.

The slurry from the mixing vessel 7 enters a hydrator 8, which is similar to that of Figure 1.

However, little or no preheating by external means is needed to initiate the hydration reaction with high surface area limes due to their enhanced reactivity.

(In such cases, an external heat source may be used, if desired, to assist in drying.) The remaining portion of the hydration water, if any, can be added in the preheating stage or in the paste mixing stage of the hydrator. The temperatures in the hydrator are between about 40 and about 70°C in the preheater stage, between about 60 and about 80°C in the paste stage, and between about 80 and about 110°C in the drying stage, depending on the type of solvent used. Residence times ranging between about 5 and about 30 minutes in the hydrator, depending on the reactivity of the lime and type and amount of solvent used, are typical. The drying stage is similar to the embodiment of Figure 1. The drying stage is not required if the hydrate is to be processed using a post-hydration wash step. At startup, the hydrator 8 is preferably provided with a flow of nitrogen or another inert gas to purge oxygen-containing gas from the hydrator, similar to the embodiment of Figure 1. The nitrogen purge can also be used during operation to provide heat required for the drying and/or preheating stages, maintain pressurization of the hydrator to about 1 to about 15 psig to prevent ignition of the organic solvent, and remove the organic solvent vapor generated during operation. The solvent vapor/nitrogen stream enters a condenser 10 to recover and cool the solvent which is then recycled to the mixing stage 7. The nitrogen stream exiting the condenser 10 is heated to about 80 to about 110°C in a heater 11 and recycled to the hydrator 8. Alternatively, or in addition, heating for the preheating and drying stages, if necessary, could be provided by external heating units, such as steam jackets.

Thus, hydrated lime with a surface area of about 50 to about 80 m²/g is prepared depending on the surface area of the lime feed and hydration conditions. The crude product obtained can be classified and milled at 9 to separate undesirable grit particles formed during hydration.

The reactivity of the hydrate can be further enhanced by using a post-hydration wash step to

displace water prior to drying to further increase surface area and reduce particle size, as described below in connection with Figure 3.

Retained water will inhibit surface area development due to agglomeration and recrystallization, and may result in pore structure collapse during drying.

Also, displacement of water prior to drying helps avoid undesirable gas phase (steam) hydration. The use of a wash step allows the use of greater amounts of water during hydration, if desired, in order to increase the degree of hydration, since the wash step displaces excess water before drying. The wash step also provides rapid cooling of hydrated material, which is beneficial since high temperature soaking of hydrates in liquid is detrimental to surface area development.

Figure 3 depicts an alternative to the embodiment of Figure 2 using a post-hydration wash step, and uses common reference numerals to represent elements which are common to both embodiments. In Figure 3, however, the hydator 8 does not include a drying stage. The nitrogen purge line and heater are not shown in Figure 3, but may be utilized, if desired, for the purposes used in the embodiments of Figures 1 and 2.

The hydrate prepared according to the

embodiment of Figure 2 without drying, classification, and milling, is washed in a vessel 12 with about 0.7 to about 4.5 liters of about 70 to about 98% by volume (preferably 90-95 wt.%) alcohol (or other organic solvent) solution per kilogram of hydrate (about 1 to about 6 liters per kilogram of feed lime). The alcohol may but need not be the same type of alcohol used in the hydration step. It is preferred, however, to use the same type of alcohol in both steps, in order to avoid an additional separation step. A surfactant or other dispersing agent could also be added during the wash step to further reduce the hydrate particle size.

The wash step is carried out at atmospheric pressure or slightly above and at a temperature

sufficiently low to avoid recrystallization of hydrate crystals, preferably at about 30-50°C, highly

preferably at less than about 40°C, for about 15 to 60 minutes in a single stage vessel,, or in multiple stages for shorter time periods in each stage.

Low temperatures are preferred during the wash step to prevent reaction of alcohol with hydrate, and recrystallization of hydrate. It is important that the wash liquid contain at least about 1-2 vol.% water, in order to avoid the undesirable reaction of calcium with alcohol to produce calcium alkoxides. The

presence of even small amounts of water in the wash liquid pushes the alkoxide formation reaction to the left, minimizing or eliminating consumption of alcohol, thereby improving the economics of the process. High concentrations of alcohol (greater than about 90%) minimize the amount of separation needed for recycle.

The crude product enters a single or multistage solid-liquid separator 13 (such as a

centrifuge) for no more than 30 minutes to separate the alcohol solution from the hydrate, preferably to below 20% wt.% liquid. The crude product then enters an atmospheric or vacuum drier 14 operating at

temperatures between about 60 to about 110°C,

preferably 60-80°C. The drier may be purged with nitrogen or other inert gas to enhance the transport of alcohol vapor from the drier to the condenser 10. The hydrate exiting the drier can be air classified and milled at 9 to reduce its mean particle diameter. The final hydrated lime product typically has a surface area of about 50 to about 85 m²/g depending on the surface area of the lime feed and conditions during hydration (8) and washing (12) .

The alcohol-water solution from the solid-liquid separator 13 is recycled to the mixing vessel 7, to the wash vessel 12, and to the condenser 10, which in Figure 3 is a scrubber. Vapors from the hydrator 8 and the drier 14 also enter the scrubber 10 for recovery of alcohol. Depending upon the flow rates and. temperatures of the vapor streams and alcohol-water stream entering the scrubber 10, some cooling will be necessary to ensure complete condensation of the

alcohol vapor as well as to achieve the proper

temperature (below 40°C) of the alcohol-water stream entering the wash vessel 12.

Under certain hydration conditions, depending on the alcohol-water ratio in the hydration solution, the amount of excess water used during hydration, and composition of the alcohol vapors entering the scrubber 10, the liquid recycle stream entering the scrubber may have to be adjusted to maintain the proper

concentration of alcohol (70 to 98 vol.% purity) in the wash step. If needed, a liquid-liquid separator 15 is used to separate alcohol from the solution for a

portion of the recycle stream entering the mixing stage 7. The concentrated alcohol stream is added to the scrubber recycle stream to increase the alcohol

concentration. The water stream is recycled back to the mixing stage 7. The liquid-liquid separator 15, if needed, may be a distillation unit (vacuum, flash, or atmospheric), or a reactor in which a solid material is used to preferentially adsorb or react with water. A liquid-liquid separation step is not needed if the concentration of alcohol in the liquid stream exiting the solid-liquid separator 13 is sufficiently high.

In the process described, less than 3% alcohol (usually less than 1%) will typically be

consumed during the hydration step. Any other losses are due to other processing steps (leaks, etc.).

Therefore, consumption of alcohol is minimal.

Figure 3 illustrates the use of a post-hydration wash step wherein the feed lime has

relatively high surface area, and is produced by calcining limestone under conditions of low temperature and low carbon dioxide concentration. The wash step can also be used in processing of "commercial" limes (as in Figure 1) , if desired, and may reduce the particle size and, possibly, increase the surface area of the resulting hydrate.

The use of lime produced in calciners

operating at low temperatures under low CO₂ condition and/or the post-hydration washing step enhances surface area of hydrated lime, while the use of the multi-stage reactor configuration according to the embodiment of Figures 1 and 2 results in fewer processing steps and greater simplicity and flexibility than prior high surface area hydrated lime preparation methods.

If desired, mixing and hydration can be carried out in the same reactor at varying temperatures along the length of the reactor, especially if the reactor has plug flow characteristics or if relatively low reactivity "commercial" limes are utilized.

Whether the premixing and hydration stages are carried out in separate vessels or in a single vessel, or whether or not the stages of the hydrator are separated, the water/alcohol hydration solution (or the components thereof) may be introduced to the system separately from each other. For example, hydration water may be introduced in two (or more) separate streams to the mixing stage 1 or 7 and the hydrator 2 or 8 as shown in Figures 1-3 when either commercial lime or high surface area, relatively reactive lime is being processed, and this procedure may be particularly desirable when relatively reactive limes are used. In any case, introduction of the second (downstream) water stream should preferably occur at a point in the system before the lime/hydration solution mixture reaches the boiling point of alcohol or other organic solvent. If desired, and in particular with highly reactive limes, lime may be mixed in the premixing stage with a hydration solution that contains all the necessary alcohol and about 5 to 35% of the hydration water with separate, preferably downstream addition of the remaining water to the hydrator. Alternatively, dry lime and an alcohol/water mixture may be introduced separately to the mixing or preheating stages of the hydrator. This scheme is preferable when the mixer 7 and hydrator 8 are combined into a single vessel. An advantage of this method of feeding dry lime is that particle size of feed lime is not limited to below about 100 mesh and lime particles as large as three inches can be routinely fed into the reactor.

Thus, the advantages of the present invention over the prior art include (1) the preparation of hydrates having surface areas of at least 50 m²/g, generally in the range of 55 to 85 m²/g compared to only 35 to 55 m²/g reported in some prior art; (2) the preparation of hydrates of comparable or improved physical properties (such as high surface area, small particle size and high porosity) compared to those of the prior art using fewer processing steps than prior art processes; and (3) the preparation of hydrates whose surface areas (80 m²/g) are comparable to those of prior art hydrates, which are prepared using

relatively expensive and more complicated processes.

One important characteristic of the high surface area hydrates of the invention is the provision of both high surface area and small particle size, which is an important factor in SO₂ sorption and other applications where sorption efficiency is important.

In particular, the invention provides means for optimizing the surface area and other physical properties of hydrated lime for SO₂ capture in a simple, commercially practical process. By the use of relatively reactive limes (i.e., those having surface areas of at least 2.5 m²/g and up to about 30 m²/g, typically up to about 10 m²/g) the need for external preheating is eliminated or minimized. The process may be conveniently carried out in a single reaction vessel with advantageous use of a post-hydration wash step, staged hydration (split water streams), high

concentrations of organic solvent (e.g., 75-85 vol.%) in the hydration solution, and the use of hydration solution additives to maximize product surface area, and the flexibility to use pebble lime in the hydration process.

Ideally, the process integrates the use of highly reactive lime feed, organic solvent-water hydration in a single reactor vessel without the use of an external heat source to initiate or maintain the hydration reaction, and an organic solvent wash step.

Judicious selection of feed lime properties and hydration conditions allows the hydrate product to be tailored for the type of dry sorbent injection system with which the sorbent is intended to be used.

EXAMPLES

The practice of the invention will be

illustrated by the following specific examples, which are not to be understood to limit the scope of the invention.

EXAMPLE 1

Table 1 presents physical properties of eighteen hydrated limes (designated A-O, HSA1, HSA2 and HSA3) that were prepared from two commercial limes made by burning limestone in a kiln under high temperature and CO₂ conditions, from one lime.made by processing limestone in a rotary kiln under low temperature and CO₂ conditions, and from six limes made by processing limestone in fluidized bed reactors under low

temperature and CO₂ conditions. The hydrated limes made from fluidized bed lime were prepared with and without a post-hydration alcohol wash step. Table 1 also presents surface area and crystallite size data for a hydrate (HSAG) made according to the procedure of Bestek U.S. Patent No. 4,636,379.

Chemical compositions of sorbents were determined by X-ray fluorescence. Surface areas were obtained by N₂-adsorption in conjunction with the one point BET method. Pore volumes and pore size

distributions (pores smaller than 0.25 micrometers) were determined by nitrogen adsorption. Sorbent particle size analyses were performed on a

Micromeritics Sedigraph 5100 particle size analyzer with particles dispersed in Sedisperse brand dispersant in an ultrasonic bath prior to particle size

measurement. The HSA hydrates were examined by X-ray diffraction (XRD) and the data were used for

determination of crystallite size using the Scherrer equation.

The commercial hydrates A and B were prepared by water hydration. Hydrate surface area ranged from 20 to 25 m²/g, and mean hydrate particle size ranged from 1.7 to 3.5 micrometers.

Inventive hydrates C and D were made from commercial limes by hydrating with a 1.2 stoichiometric ratio of water to lime and a volumetric ratio of ethanol to water of 2:1 with maximum temperatures below 115°C. More particularly, in each case 1.82 kg lime was hydrated with a solution comprising 0.70 liter water and 1.40 liter ethanol. No alcohol wash step was used. Hydrate surface area in each case was about 40 m²/g, with a mean particle diameter of 1.0-2.7

micrometers.

Hydrate E was made from lime produced in a continuous rotary tube kiln. The kiln had an inner diameter of 4 inches and a length of 72 inches, and was heated by a three-zone furnace rated at 2000°F

(1092°C). The limestone, 8x50 mesh, was calcined at 1800°F (982°C) for 30 to 60 minutes under 5 1/min (STP) nitrogen purge. The limestone feed rate was 1.6 kg/hour. 1.82 kg of the resulting lime was hydrated at maximum temperatures below 115°C with a hydration solution comprising 0.70 liter of water and 1.70 liter ethanol. The surface area of the resulting hydrate was 50-55 m²/g with a mean hydrate particle diameter of 0.7-1.0 micrometers.

Hydrates were also made from lime prepared by calcining limestone in a fluidized bed reactor. These hydrates were made without (hydrates F-J) and with (hydrates K-O) an ethanol wash step.

For each of hydrates F-O, 60 gram samples of 16x40 mesh limestone were heated in a 1 inch ID batch fluidized bed reactor at a rate of 20°C/min to a calcination temperature of 880°C and held at this temperature for 60 minutes. The limes were produced under a nitrogen purge flowing at a rate of 3 1/min (STP).

In the preparation of hydrates F-J, 5 gram samples of lime were hydrated at maximum temperatures below 115°C with a hydration solution using a

stoichiometric water to lime ratio of 1.2, except in the case of hydrate H which used a 1.5 stoichiometric ratio, and a volumetric ethanol to water ratio of 2:1. (In each case other than sample H the hydration

solution contained 1.9 ml water and 3.8 ml ethanol. For sample H, the hydration solution contained 2.4 ml water and 4.8 ml ethanol.)

For samples F-J, surface area ranged from 70-79 m²/g.

Samples K-O were prepared by hydrating limes at a stoichiometric water to lime ratio of 1.5 and an ethanol to water volumetric ratio of 2:1 at maximum temperatures below 115°C. In each case, the hydration solution contained 2.4 ml water and 4.8 ml ethanol.

Immediately following hydration, each moist hydrate was washed in 20 ml anhydrous ethanol (4 liters per kilogram of lime) at a temperature of 20 to 40°C. Hydrate surface areas ranging from 79-84 m²/g were obtained.

The results for samples A-J illustrate the effect of calcination conditions on the physical properties of hydrated lime.

The surface areas of hydrates made from commercial Burlington lime were about 40 m²/g compared to 50-55 m²/g for rotary kiln lime and 70-79 m²/g for FBR limes. Hydrates prepared using a post-hydration wash step exhibited higher surface areas, depending on the hydration conditions, and in separate tests were determined to have higher sulfur capture capacities (60 minutes sulfation time at 850°C) than hydrates prepared without the wash step.

The HSA1, HSA2 and HSA3 samples were made in a bench-scale hydrator which has the capacity to produce up to seven pounds of hydrated lime per batch. For preparation of each of these samples, 1.82 kg of lime was introduced to the reactor. The hydration solution containing 1.2 to 1.3 times stoichiometric water (1.2 to 1.3 × H₂O) and 2.0 to 2.5 volumetric ratio of ethanol to water (A:W = 2.0 to 2.5) was then added to the hydrator at room temperature. Due to the differences in reactivity of the three limes used to produce HSA1, HSA2 and HSA3 , slightly different hydration solutions and methods were used to produce each hydrated lime product. The conditions which were selected to make the products were 1.3 × H₂O and A:W = 2.0 for Salem lime (HSA3), 1.2 × H₂O and A:W = 2.4 for Burlington lime prepared in a rotary kiln at 1800°F (HSA1) , and 1.2 × H₂O and A:W = 2.5 for Shasta lime prepared in a fluidized bed reactor at 1650°F (HSA2).

During production of HSA1 and HSA2 (which were prepared from extremely reactive limes), all of the alcohol and 50% of the water were added to the lime initially to allow 30 to 60 seconds for the slurry to be homogenized before adding the remaining 50% of the water. After adding the first 50% of the water, the temperature typically rose 10 to 20°C, while after the second water addition, the temperature very quickly rose to the boiling point of the solution. During these two hydration tests, no external heating was required to start the reaction, although external heat was provided after the completion of hydration to insure that the final products were dry. During the tests performed with the commercial Salem lime,

external heating was required to initiate the reaction.

For these three tests, the products were dried at a temperature of about 110°C for about fifteen minutes and were then cooled to about 60 to 80°C. The products were then ejected into a filter bag and transferred into plastic containers to be shipped to the site of the dry sorbent injection facilities.

Lime Ethanol- Hydrate

Surface StoichioWater Ethanol Surface Mean Hydrate Pore Crystallite

Area metric Ratio Wash Area Particle Size Volume Size

Hydrate Limestone (m² /g). Water (Y;Y) (1/kg lime) (m² /g) (micrometers) (cc/g) (Angstroms)

Hydrates Made Prom Fluidized Bed Lime

F Burlington 17 1.2 2:1 0 79 NA 0.45 NA

G Salem 18 1.2 2: 1 0 76 NA NA NA

H Shasta 28 1.5 2:1 0 76 NA NA NA

I Fredonia 17 1.2 2: 1 0 70 NΛ NA NA

J Rogers 14 1.2 2:1 0 75 NA NA NA City

Hydrates Made From Fluidized Bed Lime Using Wash Step

K Burlington 17 1.5 2:1 4 79 NA NA NA

L Salem 18 1.5 2: 1 4 80 NA NA NA

M Shasta 28 1.5 2: 1 4 84 NA NA NA

N Fredonia 17 1.5 2:1 4 79 NA NA NA

O Rogers 14 1.5 2: 1 4 79 NA NA NA City

EXAMPLE 2 - COMPARISON BETWEEN INVENTIVE HYDRATED

LIME AND THE PRIOR ART

Typical properties of commercial hydrates, hydrates prepared by the inventive process and those reported in Bestek U.S. Patent No. 4,636,379 are summarized in Table 2. In addition to having higher surface areas, the inventive hydrates have smaller mean particle diameters, higher pore volumes and smaller calcium hydroxide crystallite size than those of the prior art. The enhanced properties of the HSA hydrate make this material a superior sorbent for controlling the emission of sulfur dioxide (SO₂) .

EXAMPLE 3 - PRODUCTION OF OPTIMUM HSA HYDRATED LIME

FOR VARIOUS DRY SORBENT INJECTION PROCESSES

Effect of Feed Lime Properties and Hydration

Conditions on Hydrated Lime Production and Properties

The parameters of hydration conditions, the choice of reactor type, and the properties of feed lime are important for production of hydrates with desired properties (surface area, particle size, and flow characteristics). These parameters influence the shape of the temperature profile (temperature history) which the reactants are subjected to during preheating and hydration stages.

In Figure 4, three temperature profiles

(temperature vs. reactor distance) are shown. In general (at a given alcohol to water ratio), except as noted below, conditions which shift the profile to right decrease hydrate particle size and surface area; conditions which shift the profile to left increase surface area and particle size. The profile can be shifted to the left by using:

1) more reactive lime, i.e., high surface area lime;

2) less alcohol (for a given lime, however, this would decrease surface area and increase particle size;

3) a continuous stirred tank reactor to

obtain a sudden temperature rise of the reactant (thermal shock); and,

4) a reaction accelerator.

The profile can be shifted to the right by using:

1) less reactive lime;

2) more alcohol (this results in increased surface area and decreased particle size, depending on A:W ratio);

3) reaction inhibitors; 4) gradual heating of reactants in a reactor, similar to the approach of U.S. 4,636,379 where a pre-heating stage is used before a hydration reactor; and, 5) controlled temperature rise of reactants by staged water addition.

The profiles shown in Figure 5 were obtained during production of HSA1, HSA2 and HSA3 (see Example 1 and Table 1) according to the invention in a batch reactor. The hydrates were tested in pilot-scale systems under Coolside, boiler economizer, and furnace sorbent injection conditions.

Overview of Dry Sorbent Injection Processes

In dry SO₂ removal processes, the sorbent powder reacts with SO₂ to form a dry product which is removed in the particulate collector. Three general approaches are available or under development for bringing calcium-based sorbents into contact with the SO₂:

1. Furnace injection of calcium carbonate, calcium oxide, or calcium hydroxide at temperatures between 1100 and 1250°C (2012-2282ºF).

2. Economizer injection of calcium hydroxide at temperatures between 450 and 550ºC (842-1022°F).

3. Post furnace injection of calcium hydroxide into combustion products at high relative humidity at temperatures between 50 and 250°C (122-482°F) (Coolside process).

A brief summary of the chemistry of each process is given below. Furnace Dry Sorbent Injection

When hydrated lime is used as a sorbent, the following two-step reactions occur:

Ca(OH)₂⇒ CaO + H₂O (1)

CaO + SO₂ + 1/2 O₂⇒ CaSO₄ (2)

The rate of sulfur capture depends on complex interactions between sulfation kinetics, sintering, and build up of a CaSO₄ product layer barrier.

Since CaO is porous, the SO₂ reaching the surface must diffuse through the CaO pores. As

sulfation proceeds, CaSO₄ builds up on the CaO surface, which requires that the SO₂ diffuses through the CaSO₄ to reach unreacted CaO. It is generally accepted that sulfation can be limited by any of the following processes:

1. Bulk diffusion of SO₂ to the particle.

2. Diffusion of SO₂ through the pores.

3. Diffusion of SO₂ through the CaSO₄ layer.

4. Filling of the small pores, causing a decrease in reactive area (pore

plugging).

5. Build up of CaSO₄ at the entrance of a pore causing pore closure.

6. Loss of surface area due to sintering. 7. Reduced kinetic reaction rates at low temperatures.

Typically, the rate is limited by either internal or external diffusion processes. For high sulfur coal applications, diffusion of SO₂ across the product layer (due to the increase in molar volume when converting from CaO to CaSO₄, i.e., 16.9 vs. 48

cm³/mole) limits the ultimate calcium utilizations which are achievable. At lower SO₂ levels, the

resistance due to bulk diffusion of SO₂ to the particle surface approaches that of the product layer diffusion. Physical properties of the calcined sorbent will influence its ability to capture SO₂. Indeed, investigators have shown a generally consistent trend of increasing utilization with increasing CaO surface area, at least up to 40 m²/g. Attempts to increase utilization by increasing the area of the raw hydrates up to 80 m²/g have not been successful due to a square law dependence of sintering (step 6) and hence loss of surface area at typical furnace injection temperatures. Particle size also significantly influences SO₂

removals. Laboratory tests conducted under FSI

conditions at 1100ºC with CaO derived from Ca(OH)₂ have revealed that CaO conversion to CaSO₄ in inversely related to particle diameter to the 0.2 to 0.35 power. Studies have shown that reduction in particle size from 10 to l micrometers resulted in increased SO₂ removal, but no benefit was observed below this size. It is speculated that diffusion resistances within the particle are eliminated at particles sizes of 1-2 micrometers and further reductions offers no additional benefit. Pore plugging can be minimized if a sorbent has a high volume of larger pores (between 0.01 and 0.1 micrometers).

Economizer Dry Sorbent Injection

The amount of SO₂ capture depends on three competing reactions:

Ca(OH)₂ + SO₂⇒ CaSO₃ + H₂O (3)

Ca(OH)₂ + CO₂ ⇒ CaCO₃ + H₂O (4)

Ca(OH)₂⇒ CaO + H₂O (5) The formation of sulfite (reaction 3)

competes with the reaction between the abundant CO₂ and Ca(OH)₂ to form CaCO₃ (reaction 4). Furthermore, dehydration (reaction 5) forms relatively unreactive CaO, reducing the amount of Ca(OH)₂ available for reaction.

The intrinsic rates (which are related to pore surface area of sorbent) of reactions (3) and (4) are very fast even at 490°C. However, because of the low concentration of SO₂ in the flue gas, reaction (3) is controlled by bulk diffusion of SO₂ for particles larger than 5 micrometers (diffusion rate for spherical particles is inversely related to particle size to the second power), whereas reaction (4) is controlled by intrinsic rate. As a result, the relative rates for reactions (3) and (4) depend both on pore surface area and particle size of the sorbent. Increasing pore surface area would favor the carbonation reaction (4) if particle diameter is held constant. Decreasing particle size and holding pore surface area constant would favor reaction (3). A sorbent with high pore surface area and small particle size would be expected to show high SO₂ removal efficiency under boiler economizer conditions.

Post-furnace Sorbent Injection/Humidifier (Coolside)

In this process the hydrate is injected either upstream or downstream of a water spray. The sorbent particles are wetted by inertial impaction with droplets or bulk condensation. SO₂ is removed by the entrained sorbent/liquid droplets in the ductwork, forming calcium sulfite:

Ca(OH)₂ + SO₂⇒ CaSO₃ + H₂O (6)

Results of laboratory-scale experiments indicate that significant sulfur capture can only occur if the sorbent is physically wetted.

The capture of sulfur by the slurry droplet is controlled by a number of processes, including: 1. The rate of transport of sulfur to the external surface of the droplet.

2. The rate of dissolution of the calcium hydroxide within the droplet.

3. The rate of dissolution and transport of sulfur within the liquid phase.

4. The rate of the intrinsic chemical

reaction between sulfur and calcium species.

5. The rate of diffusion of reactants or products through calcium sulfite layer (product layer diffusion).

6. The rate of diffusion of reactants or products through pores.

The bulk diffusion of SO₂ to the droplet

(step l) is believed to be the limiting resistance for sulfur capture for about one half of the droplet lifetime. During this period physical properties of the sorbent do not influence the rate of sulfur

capture.

The most probable limiting mechanism for the remaining life of the droplet is diffusion of reactant or product through a product layer of calcium sulfite on the surface of unreacted hydrated lime (step 5). In this case the rate of reaction at any conversion level should vary as the square of the initial surface area. However, if a large portion of surface area is

associated with small pores, pore plugging and pore diffusion limitation will also result. The rate of sulfur capture would also be proportional to the initial surface area of hydrate if surface reaction kinetics (step 4) or dissolution of hydrate (step 2) are the limiting mechanisms. Results of Sulfur Dioxide Removal Testing

Furnace sorbent injection tests of the three inventive calcium hydroxide sorbents and those of U.S. 4,636,379 and commercial hydrates were performed in a 14 kw pilot-scale Innovative furnace reactor at the

U.S. EPA. The sorbents were injected into the furnace at a temperature of 1200°C, at Ca/S ratios of 1:1 and 2:1, and at an SO₂ concentration of 2500 ppm. Several tests were repeated to verify the data.

Boiler economizer tests of the sorbents were performed in a bench-scale flow reactor. The tests were performed under differential conditions with respect to the SO₂ concentration (i.e., very low sample feed rates were used, SO₂ concentration remained essentially constant at 3000 ppm, and Ca/S approaching zero). Reaction temperatures of 540°C and 2.0 second residence times were selected. Five to ten repeat tests were made to confirm the data.

Coolside tests of the sorbents (except the hydrate of U.S. 4,636,379) were performed in the 100 kw Coolside pilot unit located in the R&D Department of the Consolidation Coal Company. The test program involved testing the sorbents at Ca/S ratios of 0.5, 1.0, and 2.0 and approaches to adiabatic saturation temperature of 25 and 35°F. One of the tests was repeated to confirm the data, and a test was performed using a commercial hydrated lime that had given the best performance during four years of examining the Coolside unit. The common conditions were 300°F inlet flue gas temperature, 1500 ppm inlet SO₂ content (dry basis), and 125°F adiabatic saturation temperature. The flue gas flow rate was set at 175 scfm, which provided a 2.0 second humidifier residence time. SO₂ removals reported include capture both in the

humidifier and the baghouse. Figures 6A, 6B and 6C and Table 3 show the effect of hydrate surface area on SO₂ capture (at Ca/S = 2.0) under different dry sorbent injection

conditions. Under identical test conditions, optimum products made by the invention removed substantially more SO₂ than both the commercial hydrates and products made by Bestek et al. U.S. 4,636,379. It is clearly seen that there is an optimum surface area of hydrate for maximum sulfur capture in each of the three systems. Under FSI conditions, the HSA1 (50 m²/g) showed the highest SO₂ capture (98%) followed by HSA3 (40 m²/g) and HSA2 (60 m²/g) which removed 89% and 83%, respectively. The SO₂ removal for the product made according to U.S. 4,636,374 (40 m²/g) and the

commercial hydrate were 78% and 60%, respectively.

Enhanced performance of the inventive hydrates could be related to their smaller particle size, higher surface area, and greater pore volume. Pore volume analyses of raw sorbents, shown in Figure 7, indicate the volume of pores between 0.01 and 0.1 micrometers (10 and 100 nm) was substantially higher for the HSA1 and HSA2 hydrates than for commercial hydrate A in Table 1. Pore volumes of hydrated limes are expected to correlate with pore volumes of the corresponding calcines. Due to the increase in molar volumes when converting from CaO to CaSO₄ (16.9 vs. 46.0 cm³/mole), pore plugging is known to limit the sulfation reaction. Therefore, sorbents with a high volume of larger pores are expected to capture more SO₂.

Under boiler economizer conditions, the SO₂ capture for HS1l, HSA2, HSA3, U.S. 4,636,379 hydrate (HSAG) and the commercial hydrate were 80%, 75%, 51%, 61% and 55%, respectively. Under Coolside conditions the SO₂ removal was 67% for HSA1, 81% for HSA2, 65% for HSA3, and 50% for the commercial hydrate. As described above, in the Coolside process a hydrate with high surface area is desired.

Hydrate Properties Important for SO₂ Capture and

Hydration Methods

Figure 5 shows temperature profiles obtained during production of HSA1, HSA2, and HSA3 hydrated limes (see Table 1) in a batch hydrator. The

conditions used to prepare HSA2 (60 m²/g), Profile A, provided the highest surface area hydrate. This hydrate showed the best SO₂ capture under Coolside conditions. As shown in Figure 6C, in the Coolside process the capture is directly related to hydrate surface area.

The conditions used to prepare HSAl (50 m²/g), Profile B, provided the smallest particle size. This hydrate was the most reactive hydrate for FSI and boiler economizer applications (see Figures 6A and 6B). Hydrate (HSA3) produced according to Profile C using a commercial lime had a comparable surface area to that of the product made according to Bestek process (U.S. 4,636,379). This hydrate showed the lowest SO₂ capture in the Coolside and boiler economizer processes.

Profile D in Figure 5 is the optimum profile for producing a hydrate for the boiler economizer process. From a processing point of view, the best conditions to achieve profile D is to hydrate an intermediate surface area lime, i.e., 3 m²/g lime and to use more alcohol than was used to achieve Profile B (an A:W ratio of 2:4:1 was used for Profile B). The use of more alcohol in the hydration solution will shift Profile B to the right (toward Profile D). The key processing variable is to use just enough alcohol to manufacture a dry hydrate (with minimum use of external heat) with desired properties for boiler economizer applications.

Profile D can also be achieved by hydrating the 8 m²/g lime; but this alternative is not as desirable. With a very reactive lime, i.e., one having a surface area greater than 6 m²/g, a large amount of alcohol is required to shift Profile A to D. This, however, results in formation of loose agglomerates with effective diameters greater than 5 micrometers. The reactivity of the alcohol hydrate made with

commercial lime (Profile C) cannot be improved

substantially with further optimization of the

hydration process variable because of the low

reactivity of the feed lime.

Based on the foregoing data, the following conclusions can be made.

The optimum hydrates for maximizing SO₂ removal under FSI or boiler economizer conditions appear to have surface areas in the range of 40 to 50 m²/g, mean particle diameters below about 2.5 microns, and pore volumes above about 0.25 cc/g. Hydrates with surface areas above 50 m²/g would likely be more effective for capturing SO₂ if their particle size could be significantly reduced (i.e., to less than 1 micron).

The best method for producing hydrates for optimizing SO₂ capture under FSI or boiler economizer conditions involves hydration of a 1.5 to 3.0 m²/g lime with 1.0 to 1.2 times stoichiometric water and 2.0:1 to 3.0:1 volumetric ratio of alcohol to water. Use of larger amounts of water and/or alcohol would appear to result in the production of undesirable large

agglomerates. Under the hydration conditions stated here, some preheating of the slurry could be performed in the reactor to initiate the hydration reaction.

A highly preferred hydrate surface area for maximizing SO₂ capture under boiler economizer

conditions appears to be in the range of 45 to 50 m²/g. Based on the foregoing data, hydrates having optimum properties for SO₂ removal in the Coolside process have surface areas of at least about 55 m²/g (e.g. about 60 m²/g), mean particle diameters of below about 5 micrometers, and pore volumes above about 0.3 cc/g. For this system, particle size of hydrates appears to be of secondary importance.

The optimum method for producing hydrates for the Coolside process involves principally the use of the most reactive starting lime available (2.5-10 m²/g or greater surface area). Although the use of

hydration solutions containing 1.1 to 1.3 times

stoichiometric water and 2.0 to 3.0 volumetric ratio of alcohol to water has proven effective for producing materials with very high SO₂ captures, it may be possible that the use of larger quantities of water or alcohol could further enhance the SO₂ capturing ability of hydrates for Coolside process because large

agglomerate sizes do not appear to adversely affect SO₂ removal rates. Hydrates prepared from the very

reactive limes mentioned here would not require an external preheater.

The foregoing detailed description is given for clearness of understanding only, and no unnecessary limitations should be understood therefrom, as

modifications within the scope of the invention will be apparent to those skilled in the art.

Claims

We claim:

1. A method of preparing hydrated lime comprising the steps of:

(a) thoroughly mixing lime, at a temperature sufficiently low to produce a homogeneous slurry prior to hydration of said lime, with an aqueous hydration solution of an organic solvent which has a boiling point less than that of water and which retards the rate of hydration of said lime, to produce a

homogeneous slurry, said solution containing an amount of water less than about two times the stoichiometric amount of water relative to said lime yet sufficient to provide a desired degree of hydration and at least about 0.5 volume of said organic solvent per volume of water, said lime being prepared by calcining limestone to directly produce said lime;

(b) introducing the slurry of step (a) to a hydrator comprising a single vessel which is free of internal physical separations;

(c) at least partially hydrating said lime at a temperature sufficiently high to cause hydration of said lime to produce a partially hydrated lime paste;

(d) hydrating said paste further at the boiling point of said hydration solution to produce a hydrated lime powder; and,

(e) drying said powder to produce a hydrated lime product.

2. The method of claim 1 wherein said hydrator contains a drying stage for carrying out said step (e) .

3. The method of clai.m 1 wherein said hydrated lime product is subjected to air

classification and milling to remove grit therefrom.

4. The method of claim 1 wherein said organic solvent is an alcohol selected from the group consisting of methanol and ethanol.

5. The method of claim 4 wherein said hydration solution of step (a) contains at least 0.9 times the stoichiometric amount of water relative to said lime, between about 0.5 and about 5 volumes of alcohol per volume of water, and is present in a ratio to said lime of about 0.4 to about 4 liters per kg.

6. The method of claim 5 wherein said water to lime ratio is in the range of about 1.0 to about 1.4 times the stoichiometric amount, said volumetric ratio of alcohol to water is in the range of about 1:1 to about 3:1, and the ratio of hydration solution to lime is in the range of about 0.8 to about 1.4 liters per kg.

7. The method of claim 5 wherein said step (a) is carried out at about 40°C or less, said slurry is heated to a temperature of about 40 to about 70°C for about 1 to about 10 minutes, and said paste is maintained at said solution boiling point for about 3 to about 10 minutes.

8. The method of claim 1 wherein said hydration solution further comprises at least one additive selected from the group consisting of hydroxyl carboxylic acids, surfactants, phosphates, borates. fluorides, sulfates, silicates, sugars, and lignosulfonates.

9. The method of claim 1 wherein said mixing step (a) is carried out to said vessel of step (b) .

10. The method of claim 1 wherein all of said organic solvent and less than all of said water of said hydration solution are mixed with said lime to form said slurry of step (a) and the remainder of said hydration solution water is introduced to said hydrator separately from said slurry.

11. The method of claim 10 wherein said slurry contains about 50% or less of said hydration solution water.

12. The method of claim 1 wherein said organic solvent comprises about 75 to about 85 vol.% of said hydration solution.

13. A method of preparing hydrated lime comprising the steps of:

homogeneous slurry, said solution containing an amount of water less than two times the stoichiometric amount of water relative to said lime yet sufficient to provide a desired degree of hydration and at least about 0.5 volume of said organic solvent per volume of water, said lime being prepared by calcining limestone to directly produce said lime;

(b) introducing the slurry of step (a) to a hydrator comprising at least a preheating stage and a paste mixing stage;

(d) hydrating said paste further at the boiling point of said hydration solution to produce a hydrated lime powder;

(e) washing said hydrated lime powder in an aqueous washing solution comprising an organic solvent at a temperature sufficiently low to inhibit

recrystallization of said hydrated lime; and,

(f) separating and drying said hydrated lime to produce a hydrated lime product.

14. The method of claim 13 wherein said organic solvent of said hydration solution of step (a) is an alcohol selected from the group consisting of methanol and ethanol.

15. The method of claim 13 wherein said hydration solution of step (a) contains at least 0.9 times the stoichiometric amount of water relative to said lime, between about 0.5 and about 5 volumes of alcohol per volume of water, and is present in a ratio to said lime of about 0.4 to about 4 liters per kg.

16. The method of claim 14 wherein said step (a) is carried out at about 40°C or less, said slurry is heated to a temperature of about 40 to about 70°C in said preheating stage for about 1 to about 10 minutes. and said paste is maintained at said solution boiling point in said paste mixing stage for about 3 to about 10 minutes.

17. The method of claim 13 wherein said organic solvent of said washing solution is an alcohol selected from the group consisting of methanol and ethanol.

18. The method of claim 17 wherein said washing solution comprises about 70 to about 98 vol.% alcohol.

19. The method of claim 18 wherein said washing solution is used in a ratio of about 0.7 to about 4.5 liters per kg. of hydrated lime.

20. The method of claim 13 wherein said washing solution is separated from said hydrated lime prior to said drying step (f).

21. The method of claim 11 wherein said washing step is carried out at about 40°C or less.

22. The method of claim 13 wherein said mixing step (a) is carried out in said vessel of step (b).

23. A method of preparing hydrated lime comprising the steps of:

(a) thoroughly mixing lime, at a temperature sufficiently low to produce a homogeneous slurry prior to hydration of said lime, in a mixing stage with an aqueous hydration solution of an organic solvent which has a boiling point less than that of water and which retards the rate of hydration of said lime, to produce a homogeneous slurry, said solution containing an amount of water less than two times the stoichiometric amount of water relative to said lime yet sufficient to provide a desired degree of hydration and at least about 0.5 volume of said organic solvent per volume of water, said lime being prepared by calcining limestone to directly produce said lime;

(d) hydrating said paste further in said paste mixing stage at the boiling point of said

hydration solution to produce a hydrated lime powder; and,

(e) drying said powder in a drying stage to produce a hydrated lime product, at least said steps (b)-(d) being carried out in a single vessel.

24. The method of claim 23 wherein said vessel is free of internal physical separations between said stages.

25. The method of claim 23 wherein said organic solvent is an alcohol selected from the group consisting of methanol and ethanol.

26. The method of claim 25 wherein said hydration solution of step (a) contains at least 0.9 times the stoichiometric amount of water relative to said lime, between about 0.5 and about 5 volumes of alcohol per volume of water, and is present in a ratio to said lime of about 0.4 to about 4 liters per kg.

27. The method of claim 26 wherein said step (a) is carried out at about 40°C or less, said slurry is heated to a temperature of about 40 to about 70°C in said preheating stage for about 1 to about 10 minutes, and said paste is maintained at said solution boiling point in said paste mixing stage for about 3 to about 10 minutes.

28. The method of claim 23 wherein at least said steps (a) -(d) are carried out in a single vessel.

29. The method of claim 23 wherein at least said steps (b)-(e) are carried out in a single vessel.

30. The method of claim 23 wherein said steps (a)-(e) are carried out in a single vessel.

31. A method of preparing hydrated lime comprising the steps of:

(a) thoroughly mixing lime, at a temperature sufficiently low to produce a homogeneous slurry prior to hydration of said lime, in a mixing stage with an aqueous hydration solution of an organic solvent which has a boiling point less than that of water and which retards the rate of hydration of said lime, to produce a homogeneous slurry, said solution containing an amount of water less than about two times the

stoichiometric amount of water relative to said lime yet sufficient to provide a desired degree of hydration and at least about 0.5 volume of said organic solvent per volume of water, said lime being prepared by calcining limestone to directly produce said lime;

hydration solution to produce a hydrated lime powder;

recrystallization of said hydrated lime; and

(f) separating and drying said hydrated lime to produce a hydrated lime product, at least said steps (b)-(d) being carried out in a single vessel.

32. The method of claim 31 wherein said vessel is free of internal physical separations between said mixing, preheating and paste mixing stages.

33. The method of claim 31 wherein said organic solvent is an alcohol selected from the group consisting of methanol and ethanol.

34. The method of claim 33 wherein said hydration solution of step (a) contains at least 0.9 times the stoichiometric amount of water relative to said lime, between about 0.5 and about 5 volumes of alcohol per volume of water, and is present in a ratio to said lime of about 0.4 to about 4 liters per kg.

35. The method of claim 34 wherein said step (a) is carried out at about 40°C or less, said slurry is heated to a temperature of about 40 to about 70°C in said preheating stage for about 1 to about 10 minutes, and said paste is maintained at said solution boiling point in said paste mixing stage for about 3 to about 10 minutes.

36. The method of claim 31 wherein said organic solvent of said washing solution is an alcohol selected from the group consisting of methanol and ethanol.

37. The method of claim 36 wherein said washing solution comprises about 70 to about 98 vol.% alcohol.

38. The method of claim 37 wherein said washing solution is used in a ratio of about 0.7 to about 4.5 liters per kg. of hydrated lime.

39. The method of claim 31 wherein said steps (a)-(d) are carried out in a single vessel.

40. A method of preparing hydrated lime comprising the steps of:

homogeneous slurry, said solution containing an amount of water less than two times the stoichiometric amount of water relative to said lime yet sufficient to provide a desired degree of hydration and at least about 0.5 volume of said organic solvent per volume of water, said lime having a surface area of at least about 2.5 m²/g and being prepared by calcining

limestone to directly produce said lime;

(b) introducing the slurry of step (a) to a hydrator comprising a paste mixing stage;

(c) hydrating said lime in said paste mixing stage at the boiling point of said hydration solution to produce a hydrated lime powder; and,

(d) drying said powder to produce a hydrated lime product, said steps (a)-(c) being carried out without the application of heat from a source external to said hydration reaction.

41. The method of claim 40 wherein said hydrator contains a drying stage for carrying out said step (d) .

42. The method of claim 40 wherein said organic solvent is an alcohol selected from the group consisting of methanol and ethanol.

43. The method of claim 42 wherein said hydration solution of step (a) contains at least 0.9 times the stoichiometric amount of water relative to said lime, between about 0.5 and about 5 volumes of alcohol per volume of water, and is present in a ratio to said lime of about 0.4 to about 4 liters per kg.

44. The method of claim 43 wherein said step (a) is carried out at about 40°C or less, said slurry is heated to a temperature of about 40 to about 70°C in said preheating stage for about 1 to about 10 minutes, and said paste is maintained at said solution boiling point in said paste mixing stage for about 3 to about 10 minutes.

45. The method of claim 40 wherein mixing and hydrating steps (a)-(c) are carried out in a single vessel free of internal physical separations.

46. The method of claim 40 wherein said lime is prepared by calcining limestone at a temperature of about 800 to about 1100°C in a gas environment wherein the partial pressure of carbon dioxide is about 0.25 atmospheres or less.

47. The method of claim 46 wherein said calcining step is carried out at or below atmospheric pressure in a fluid bed reactor or entrained flow reactor.

48. The method of claim 47 wherein said limestone comprises at least about 95% CaCO₃ before calcining.

49. The method of claim 44 wherein said mixing step (a) is carried out at less than about 30°C.

50. The method of claim 40 wherein all of said organic solvent and less than all of said water of said hydration solution are mixed with said lime to form said slurry of step (a) and the remainder of said hydration solution water is introduced to said hydrator separately from said slurry.

51. The method of claim 50 wherein said slurry contains about 50% or less of said hydration solution water.

52. The method of claim 51 wherein said slurry contains about 5 to about 35% of said hydration solution water and the remainder thereof is introduced to said hydrator prior to said hydration solution reaching its boiling point.

53. A method of preparing hydrated lime comprising the steps of:

limestone to directly produce said lime;

(c) hydrating said lime in said paste mixing stage at the boiling point of said hydration solution to produce a hydrated lime powder;

(d) washing said hydrated lime powder prior to drying in an aqueous washing solution comprising an organic solvent at a temperature sufficiently low to inhibit recrystallization of said hydrated lime; and,

(e) separating and drying said hydrated lime to produce a hydrated lime product, said steps (a)-(c) being carried out without the application of heat from a source external to said hydration reaction.

54. The method of claim 53 wherein said organic solvent is an alcohol selected from the group consisting of methanol and ethanol.

55. The method of claim 54 wherein said hydration solution of step (a) contains at least 0.9 times the stoichiometric amount of water relative to said lime, between about 0.5 and about 5 volumes of alcohol per volume of water, and is present in a ratio to said lime of about 0.4 to about 4 liters per kg.

56. The method of claim 55 wherein said step (a) is carried out at about 40°C or less, said slurry is heated to a temperature of about 40 to about 70°C in said preheating stage for about 1 to about 10 minutes, and said paste is maintained at said solution boiling point in said paste mixing stage for about 3 to about 10 minutes.

57. The method of claim 53 wherein said mixing and hydrating steps (a)-(c) are carried out in a single vessel free of internal physical separations.

58. The method of claim 53 wherein said lime is prepared by calcining limestone at a temperature of about 800 to about 1100°C in a gas environment wherein the partial pressure of carbon dioxide is about 0.25 atmospheres or less.

59. The method of claim 53 wherein said mixing step (a) is carried out at less than about 30°C.

60. The method of claim 53 wherein said washing step (d) is carried out at about 40°C or less.

61. The method of claim 54 wherein said organic solvent of said washing solution is an alcohol selected from the group consisting of methanol and ethanol.

62. The method of claim 61 wherein said washing solution comprises about 70 to about 98 vol.% alcohol.

63. The method of claim 62 wherein said washing solution is used in a ratio of about 0.7 to about 4.5 liters per kg. of hydrated lime.

64. The method of claim 53 wherein all of said organic solvent and less than all of said water of said hydration solution are mixed with said lime to form said slurry of step (a) and the remainder of said hydration solution water is introduced to said hydrator separately from said slurry.

65. The method of claim 64 wherein said slurry contains about 50% or less of said hydration solution water.

66. The method of claim 65 wherein said slurry contains about 5 to about 35% of said hydration solution water and the remainder thereof is introduced to said hydrator prior to said hydration solution reaching its boiling point.

67. A method according to claim 1 for preparing hydrated lime having a surface area of at least about 40 to about 50 m²/g, a mean particle diameter of below about 2.5 microns, a pore volume above about 0.25 cc/g for use in SO₂ removal from gas streams under furnace sorbent injection or boiler economizer conditions wherein said lime of step (a) has a surface area of about 1.5 to about 3.0 m²/g, said hydration solution contains about 1.0 to about 1.2 times the stoichiometric amount of water relative to said lime, and the volumetric ratio of said organic solvent to said water is about 2.0:1 to about 3.0:1.

68. The method according to claim 67 wherein said hydrated lime has a surface area of about 45 to about 50 m²/g for use in SO₂ removal from gas streams under boiler economizer conditions.

69. A method according to claim 40 for preparing hydrated lime having a surface area of at least about 55 m²/g, a mean particle diameter of below about 5 microns, and a pore volume above about 0.3 cc/g for use in SO₂ removal from gas streams under post-furnace sorbent injection/humidification (Coolside) conditions wherein said lime of step (a) has a surface area of about 2.5 to about 30 m²/g, said hydration solution contains about 1.1 to about 1.3 times the stoichiometric amount of water relative to said lime, and the volumetric ratio of said organic solvent to said water is about 2.0:1 to about 3.0:1.

70. Hydrated lime made according to the method of any of claims 1-69.

71. Hydrated lime having a surface area of at least about 35 m²/g, mean particle diameter of less than about 2.5 micrometers, and pore volume of at least about 0.25 cc/g.

72. The hydrated lime of claim 71 wherein the average crystallite size thereof is about 160

Angstroms or less.

73. The hydrated lime of claim 71 wherein said surface area is in the range of about 35 to about 85 m²/g, said mean particle diameter is in the range of about 0.5 to about 2.5 micrometers, and said pore volume is in the range of about 0.25 to about 0.6 cc/g.

74. The hydrated lime of claim 71 wherein said surface area is greater than 55 m²/g.

75. The hydrated lime of claim 71 wherein said mean particle diameter is less than 1 micrometer.

76. The hydrated lime of claim 71 wherein said surface area is greater than 55 m²/g and said mean particle diameter is less than 1 micrometer.

77. A method of removing SO₂ from a gas stream, comprising the step of contacting said stream with an effective amount of the hydrated lime made by the method of any one of claims 1-69.

78. A method of removing SO₂ from a gas stream, comprising the step of contacting said stream with an effective amount of the hydrated lime of any one of claims 71-76.