The method of producing a liquid glass and reactor for the production of liquid glass

 

(57) Abstract:

The invention relates to methods of producing liquid glass hydrothermal alkaline treatment of silica-containing raw material and equipment for their implementation. The invention consists in the method of producing a liquid glass, which includes preparation of the suspension, the flow of slurry at a speed of 3-5 m/s for heating, it is heated, the synthesis of liquid glass, cooling and draining of liquid glass, while the suspension before it is fed into the synthesis of heat recovery with heat and pour out the liquid glass. The invention consists also in the reactor for the production of liquid glass with connections to the input and output of the product, which consists of several pipes connected with each other and having a heating zone, a soaking zone and the cooling zone, the tubes of the preheating zone cover or included in pipe cooling zones with the formation of a cavity between them, thereby creating a zone of recovery, and at the entrance of the reactor tangentially mounted pressure element, the pipe reactor can be arranged coaxially or sequentially. This invention reduces the energy consumption due to heating of the suspension recuperation of heat, and pour out the fluid the device for cooling liquid glass. 2 S. and 9 C.p. f-crystals, 6 ill.

The invention relates to methods of producing liquid glass hydrothermal alkaline treatment cremedelacreme raw materials and equipment for their implementation and can be applied in chemical, engineering and other industries.

Known methods for producing liquid glass from crushed quartz sand in an autoclave by heating to 160-190oC and a pressure of 8-12 bar [1, 2]. In the initial charge take significant >100% excess sand. The obtained intermediate with large density and viscosity is discharged through a system of piping and valves in the associated with the second autoclave vessel, where the water is. When mixed with liquid water glass get with desired density, and excess sand deposited on the wall of the second vessel, used in the re-production cycle.

In these methods, the production of liquid glass is a reduction reaction activity of alkaline solution due to the entry into the reaction zone of the finished silicate, getting together with excess sand after sludge diluted solution of liquid glass, which reduces the performance of these methods of obtaining and wasted energy to heat continuously recirculating the one or more sealed reaction tubes, interconnected elastic elements and rods with hinges, the extreme of which is attached to the pipe, and the middle - on the supports, while the average hinges are located at equal distance from the extreme and serve as the fulcrum of the autoclave to the Foundation [3].

To ensure mixing of the charge in the synthesis process in the autoclave should be brought into the oscillatory motion of the entire autoclave, which complicates the design of the equipment, and increases energy production.

Closest to the claimed technical solution is a tubular reactor and a method of producing a liquid glass using this reactor [4].

This rotating tubular reactor consists of several pipes are rigidly interconnected and are made in the form of single-line grocery coil is divided into three areas:

zone heating the reaction mixture (suspension);

- area of exposure (synthesis);

- cooling zone.

Such a rotating tubular reactor for the production of liquid glass, includes a horizontal heated housing with connections to the input and output of the product located on the axis of the housing, and is established at the pipes grocery coil and provided with a device for ajuha, installed on the reactor vessel, and a cylindrical baffle mounted inside the housing with a gap from the side of the output product, the tubes grocery coil made one-way, fixed in the direction of travel of the product on the inner surface of the walls of the casing and the casing.

Heating of such a reactor is carried out by burning fuel. To obtain liquid glass preparing a suspension of silica-containing materials and alkali solution and feed it into the pipe of the reactor for heating, where it passes through the heating zone, in which the heating carried out due to the heat coming from the combustion chamber, and then the synthesis zone (extracts) and the cooling zone. In this reactor for cooling liquid glass requires a device for cooling the inlet and outlet of water, and to heat the suspension requires the burning of fuel and, in addition, for the operation of the reactor it is necessary to ensure its rotation, which requires significant energy consumption for the production of liquid glass.

The invention is aimed at reducing energy consumption due to heating of the raw product - suspension recuperation of heat, and pour out the liquid glass and eliminate the need presenece.

The inventive method of producing a liquid glass has the following set of essential features:

the method of producing a liquid glass includes the preparation of a suspension of powdered silica raw material and alkali solution, the flow of suspension to heat, it heated, the synthesis of liquid glass and cooling with subsequent discharge of liquid glass, in contrast to the prototype, in this way, the feed preheating carried out with a speed of 3-5 m/s, and the suspension before it is fed into the synthesis of heat recovery with heat and pour out the liquid glass.

This set of features of the method of producing a liquid glass reduces energy costs by heating a suspension of the recuperation of heat, and pour out the liquid glass and ensures the feasibility of the method by supplying the heating speed of 3-5 m/s

In addition, in the present method when using all previously specified set of features liquid glass is poured at 50-60oC, which helps to eliminate the build-up of solid silicate on the wall of the pipe, causing obstruction of pipes and outlet of the reactor operating mode.

The inventive reactor for the production of liquid glass has the following sovocool is the space of a few pipes, rigidly interconnected and having a heating zone, a soaking zone and the cooling zone, in this case, unlike the prototype, it pipes the preheating zone cover pipes or are pipe cooling zones with the formation of a cavity between them, thereby creating a zone of recovery, and at the entrance of the reactor tangentially mounted pressure element.

When using the proposed reactor for the production of liquid glass due to the fact that it pipes the preheating zone cover or included in pipe cooling zones with the formation of a cavity between them, thereby creating a zone of recovery, and its inlet tangentially mounted pressure element, and also due to the fact that eliminates the need for rotation of the reactor, reduction of energy consumption for the production of liquid glass in comparison with the prototype.

In addition, in the inventive reactor tubes can be located coaxially inside each other and fixed with the formation of a cavity between each two adjacent tubes, each tube in the direction of travel of the product installed tangentially discharge element, and the Central pipe still connected to the connecting element with the outer tube.

When avalino-vertical location of the pipe reactor is minimal production area and provides a minimum energy loss, that reduces not only energy consumption, but also reduces overall production costs of liquid glass.

When coaxial-horizontal pipe arrangement reduces the capacity of the pump, the feed suspension, resulting in lower energy consumption for the production of liquid glass.

In addition, in the inventive reactor tubes can be arranged in series one behind the other and are interconnected by the connecting pipes, and the output of each of the connecting pipes in the form of nozzles and installed tangentially, with the tube of the cooling zone is made in the form of a coil included in the pipe zone heating with the formation of a cavity between them. The tubes can be arranged in series vertically and sequentially horizontally.

When a series-vertical pipe arrangement facilitates the installation and simplifies setup when you change the length of the synthesis of liquid glass, which reduces the cost of production of liquid glass.

When a series-vertical location of the pipe where the pipe zone recovery are above the pipe zone exposure decreases required production area.

When succession is Anenii duration of the synthesis of liquid glass, and reduced pump power feed suspension on the synthesis, reducing the overall cost of production of liquid glass.

The invention is illustrated by drawings.

In Fig. 1 shows a reactor with coaxial-vertically-arranged pipes. In Fig.2 - section a-a of Fig.1. In Fig.3 - section b-B of Fig.1. In Fig. 4 shows a reactor with a series of vertically spaced pipes. In Fig. 5 shows a reactor with coaxial horizontally spaced tubes. In Fig.6 is shown a reactor with a series of horizontally arranged tubes.

According to the claimed technical solution of liquid glass was prepared as follows.

First prepare a suspension of silica-containing materials (e.g., quartz sand, perlite, Tripoli or diatomite) and alkali solution. The prepared suspension served continuously with the feed speed of 3-5 m/s in the reactor through the inlet nozzle. Using a pressure element (nozzle or nozzles), installed at the entrance of the reactor, the suspension report of the rotational-translational motion whereby it passes through the pressure element mounted in each pipe passes through all of the tubes of the reactor. To p the th glass is carried out at 50-60oC.

This feed rate of the suspension in the reactor provides a complete passage of the product through all stages of the process (heating, synthesis and cooling) and receiving liquid glass, and heating the suspension up to the filing of the synthesis due to the recuperation of heat, and pour out the liquid glass reduces the energy consumption for its production.

Regardless of the components of the suspension at a speed feed her for heating less than 3 m/s due to the insufficient speed of the rotational-translational motion is not guaranteed that the product is passed through the pipe reactor, and at speeds above 5 m/s there is a necessity to create high pressure in the supply pipe more than 100 ATM, which causes the complexity of the design of the device and consequently leads to increased cost of production of liquid glass.

Drain liquid glass at a temperature of 50-60oC provides sufficient viscosity to drain and eliminates the build-up of solid silicate on the walls of the pipes. When the temperature of the discharge liquid glass less than 50oC does not provide adequate viscosity plum and starts sticking of solid silicate on the wall of the pipe, which ultimately leads to the obstruction of pipes and the reactor outlet of tx2">

The inventive method of producing a liquid glass is carried out in the proposed reactor. This reactor for the production of liquid glass consists of several sealed tubes are rigidly interconnected and having a preheating zone, a zone of synthesis (extracts) and the cooling zone. In this reactor pipe preheating zone cover pipes or are pipe cooling zones with the formation of a cavity between them, thereby creating a zone of recovery, and at the entrance of the reactor tangentially mounted pressure element (for example, a nozzle or injector).

In the inventive reactor tubes can be arranged coaxially or sequentially.

The inventive reactor coaxially inside each other with pipes consists of a Central pipe 1, the outer tube 2 and the tubes 3 and 4, located between the Central and outer tubes of 1.2. Tubes 1-4 (see Fig. 1) fixed to the formation of cavities between every two adjacent pipes. Each pipe in the direction of travel of the product installed tangentially pressure element 5 (nozzle or nozzle). The Central pipe 1 is connected by means of a connecting element 6 (pipe or hose) with the outer tube 2. To enter the original product in the reactor at the input of the Central Truvada reactor tube 1, made in the form of nozzles 5 (see Fig. 3). Outlet pipe 4 located between the Central pipe 1 and pipe 3, set the discharge port 8 output of the finished product.

To ensure the required temperature synthesis of liquid glass reactor installed in the hermetic casing which still has a heating element (not shown).

This reactor operates as follows.

Pre-prepared from a silica-containing material and a solution of alkali to the suspension by means of a pump (not shown) through the supply pipe 7, the end of which is still installed on the inlet of the reactor and is designed as a nozzle 5, served continuously with a speed of 3-5 m/s in the Central tube 1 to heat. The suspension passing through the nozzle 5, acquires the rotational-translational motion, in which it is in the Central pipe 1, mixed and heated to a certain temperature due to the recuperation of heat, and pour out the liquid glass, which is in the cavity, located between the Central pipe 1 and the pipe 4, rises up the Central pipe 1 and through the connecting element 6 and the pressure element 5, tangentially mounted in the outer tube 2, enters the cavity, raspolojenia (preheating zone) to the required temperature synthesis of liquid glass and is activated moving this down. Next, the reaction mixture through a pressure element 5, tangentially mounted in the pipe 3 enters the cavity located between the pipe 3 and the pipe 4, through the heating element installed in the casing, supported by the required temperature synthesis (the soaking zone) and occurs for a certain period of time at a given temperature synthesis of liquid glass thus obtained liquid glass moves up. After this liquid glass from this cavity through a pressure element 5, tangentially mounted in the pipe 4, and flows into the cavity located between the pipe 4 and the Central pipe 1 (cooling zone), where, being cooled, the finished product heats the suspension is applied to the Central tube 1, recuperation of heat. In the area of cooling liquid glass is moved down to the exhaust pipe 8 while continuing the mixing process, the temperature for a certain period of time decreases from a maximum value to a temperature plum (50-60oC). During this time, the reaction continues until final completion, lightens the finished product. Ready liquid glass through the outlet 8 is displayed in a container for storing liquid is P> The reactor sequential arrangement of pipes consists of pipes 9, 10, 11 zone heating tubes 12, 13,14 zone exposure and pipes 15, 16, 17 cooling zone, which is still connected to the connecting pipe 18. The output of each of the connecting pipe 18 is made in the form of the nozzle 5 and is mounted tangentially. Pipes 15, 16, 17 of the cooling zone is made in the form of a coil included respectively in the pipes 9, 10, 11 zone heating with the formation of a cavity between them, the pipe 14 zone excerpts connected with the pipe 11 zone heating connecting pipe 19. To enter the original product in the pipe 9 is installed inlet pipe 7. The socket end 7 of the input product is still installed on the reactor inlet in the pipe 9 and is made in the form of the nozzle 5. Outlet pipe 17 has an outlet 8 for displaying the finished product. To ensure the required temperature synthesis of liquid glass pipes 12, 13, 14 are installed in the hermetic casing which still has a heating element (not shown).

This reactor operates as follows.

Pre-prepared suspension continuously by means of a pump (not shown) through the supply pipe 7, the end of which is still installed on the input reev.

The suspension passing through the nozzle 5, acquires the rotational-translational motion, in which it is mixed and heated to a certain temperature due to the recuperation of heat, and pour out the liquid glass in the pipe 17, rises up through the pipe 9 and into the connecting pipe 18, down through which the output is made in the form of nozzle 5 mounted tangentially enters the pipe 10.

In the pipes 10 and 11, the process is repeated, resulting in the pipes 9, 10, 11 the reaction mixture for a certain period of time is heated to a predetermined temperature (preheating zone) and is activated.

From the pipe 11 zone heating the reaction mixture through the connecting pipe 18 enters the pipe 12, and then through the connecting pipe 18 into the pipes 13 and 14. The pipes 12, 13, 14 supported a certain period of time due to the heating element installed in the casing, the desired temperature (soaking zone), is a synthesis of the obtained liquid glass.

Then from the pipe 14 is obtained liquid glass through the connecting pipe 19 enters the pipe 15 provided in the pipe 11 with the formation of a cavity between them, where the cooled finished product, in Trueba 17. In pipes 16,17 continues cooling liquid glass, while the original product is heated suspension. In the pipes 15, 16, 17 (cooling zone) continuing the mixing process, the temperature for a certain period of time decreases from a maximum value to a temperature plum (50-60oC). During this time, the reaction continues until the final completion lightens the finished product, which through the exhaust pipe 8 is shown in a storage container (not shown). Move the product through the pipes of such a reactor is indicated by arrows in Fig.4.

When a series-vertical pipe arrangement it is possible to install the pipe zone recovery above the pipe zone exposure, while the reactor operates similarly to the reactor sequentially-stacked pipes.

In reactors with coaxially arranged pipes and reactors with successive pipes can be installed not only vertically, as shown in Fig.1 and 4, but also horizontally (see Fig. 5, 6). Reactors with a horizontally mounted tube with a coaxial arrangement of their or their sequential arrangement are similar to the respective reactors with ver.

When using the proposed reactor for the production of liquid glass due to the fact that it pipes the preheating zone cover or included in pipe cooling zones with the formation of a cavity between them, thereby creating a zone of recovery, and its inlet tangentially mounted pressure element, and also due to the fact that eliminates the need for rotation of the reactor, is provided as established by the calculation of the reduction of energy consumption for the production of liquid glass in comparison with the prototype by 25%.

In addition, this reactor does not require cooling unit with inlet and outlet water, which greatly simplifies its design.

When coaxial-vertical location of the pipe reactor is minimal production area and provides a minimum energy loss, which reduces not only energy consumption, but also reduces overall production costs of liquid glass.

When coaxial-horizontal pipe arrangement reduces the capacity of the pump, the feed suspension, which also leads to lower energy consumption for the production of liquid glass.

When a series-vertical pipe arrangement facilitates installation service and proshaetsia glass.

When a series-vertical location of the pipe where the pipe zone recovery are above the pipe zone exposure decreases required production area.

When a series-horizontal pipe arrangement facilitates installation service is quick changeover when changing the duration of the synthesis of liquid glass, and reduces the pump power feed suspension on the synthesis, reducing the overall cost of production of liquid glass.

Sources of information

1. Patent Germany N 3500649, C 01 B 33/32, 1985, "a Method for obtaining solutions of liquid glass".

2. Unaccepted application Germany N 3515233, C 01 B 33/32, 1985, "a Method for obtaining solutions of liquid glass".

3. Author's certificate N 235737, B 01 J 3/04, 1969 "Autoclave".

4. Author's certificate N 1560303, B 01 J 19/28, 1990, "a Rotating tubular reactor prototype.

1. The method of producing a liquid glass, comprising preparing a suspension of powdered silica raw material and alkali solution, the flow of suspension to heat, it heated, the synthesis of liquid glass and cooling with subsequent discharge of liquid glass, characterized in that the supply to the heating carried out with the speed of 3-P> 2. The method according to p. 1, characterized in that the liquid glass is poured at 50 - 60oC.

3. The reactor for the production of liquid glass with connections to the input and output of the product, consisting of several pipes are rigidly interconnected and having a heating zone, a soaking zone and the cooling zone, wherein the pipe zone heating cover pipes or are pipe cooling zones with the formation of a cavity between them, thereby creating a zone of recovery, and at the entrance of the reactor tangentially mounted pressure element.

4. The reactor under item 3, characterized in that the socket end of the input product, permanently installed at the entrance of the reactor, made in the form of a nozzle.

5. The reactor under item 3 or 4, characterized in that the pipes are coaxially inside each other and fixed with the formation of a cavity between each two adjacent tubes, each tube in the direction of travel of the product installed tangentially discharge element, and the Central pipe still connected to the connecting element with the outer tube.

6. The reactor under item 3 or 4, characterized in that the pipes are arranged in series one behind the other and are interconnected by the connecting pipes, and vidia made in the form of a coil, included in the pipe zone heating with the formation of a cavity between them.

7. The reactor under item 5, wherein the tubes are arranged vertically.

8. The reactor under item 5, wherein the tubes are arranged horizontally.

9. The reactor under item 6, wherein the tubes are arranged vertically.

10. The reactor under item 6, wherein the tubes are arranged horizontally.

11. The reactor under item 9, characterized in that the pipe zone recovery is located above the pipe zone exposure.

 

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