EA043491B1 - DEVELOPMENT OF A SYSTEM THAT PREVENTS LOSSES OF NH3 AND CO2 GASES WHEN PRODUCING SODA ASH USING THE SOLVAY METHOD - Google Patents

Description

Field of technology

The present invention relates to the development of systems that provide regeneration of ammonia gas, which acts as a catalyst during the production of soda ash using the Solvay process, and regeneration of carbon dioxide used in the process, and which ensure the inclusion of regenerated ammonia and carbon dioxide gases in the process.

State of the art

The starting materials for the Solvay process are salt, limestone and anthracite. Ammonia acts as a catalyst in the method. The most suitable limestone (96-98% CaCO ₃ (calcium carbonate)) are types of limestone that are hard and that contain small amounts of silica and impurities. Ensure suitable limestone particle size and preparation.

In the Solvay method, limestone is fired to produce CaO (calcium oxide) and anthracite is used to produce CO2.

Crude salt is introduced into the reaction as a saturated and purified salt solution (brine) and is typically obtained from rock salt.

In the method, when crude salt (NH ₄ )HCO ₃ (ammonium bicarbonate) is added to a saturated solution, the resulting ammonium chloride solution is dissolved and NaHCO ₃ (sodium bicarbonate) is precipitated as a solid; if NaHCO ₃ is filtered and separated and calcined, it turns into Na2CO ₃ (sodium carbonate) as shown in equation 1.

Equation 1. Preparation of sodium carbonate.

NH ₄ HCO ₃ + NaCl θ NaHCO ₃ + NH ₄ C1

2NaHCO ₃ + heat Na ₂ CO ₃ + H ₂ O + CO ₂

The recovery of ammonia is extremely important for the Solvay process, since the process will be carried out at a more reasonable cost. The economic benefit of the ammonia method for producing soda depends on the recovery of almost all of the ammonia used in the method. A significant portion of the ammonia used is in the form of sodium bicarbonate filtrate and in the form of NH4Cl. Smaller amounts of ammonium hydroxide are present in the form of ammonium carbonate and ammonium bicarbonate. In addition, ammonia may also be present in some of the precipitates and solutions that are recovered from the process.

In the literature, all solutions and sediments containing ammonia in the Solvay method are sent to the ammonia regeneration system. As a result of the heat effect in it, ammonium hydroxide, carbonate and bicarbonate are decomposed and separated. Ammonium chloride is reacted with milk of lime added to the medium to produce ammonium hydroxide. This ammonium hydroxide is heated and ammonia is regenerated.

Equation 2. Ammonia production.

2NH ₄ C1 + Ca(OH) ₂ CaC1 ₂ + 2NH ₃ + 2H ₂ O

Water vapor introduced through the bottom of the decomposition device lifts almost all the ammonia in the medium. Gaseous NH ₃ and desorbed CO ₂ exit through the top of the decomposition column, which has a packed structure, and CaCl ₂ , unreacted NaCl and a residue including excess lime are collected from the bottom of said decomposition column.

In the prior art, recovered NH ₃ and CO ₂ gases are retained together with saturated purified salt water in an absorption column system present in systems using the Solvay process. In case the NH ₃ gas is not retained in the absorption system and in case it is not reused, the absorption system does not operate efficiently due to high loss of ammonia and hence the production of soda is not economically feasible. Increasing the amount of saturated salt water to retain NH ₃ and CO ₂ gases is not possible. This is because saturated salt water with ammonia is used in the carbonation system and production. In other words, salt water with ammonia is used in an amount that corresponds to productivity.

As a result, the presence of all of the above problems creates a need for improvement in the related art.

Application AU 2013234427 discloses a method for reusing by-products in the Merseburg process and in the Solvay process in a combined process for the production of soda ash and ammonium sulfate, which uses brine, ammonia and CO ₂ as starting materials. Combine (i) the Solvay process, in which pure evaporated salt is obtained by separating gypsum using CaQ ₂ -containing waste from the Solvay process, with (ii) the Merseburg process, in which the above gypsum, ammonia and CO ₂ are reacted together to produce ammonium sulfate and calcium carbonate.

Application GB 2159510 describes a method for producing calcium hydrogen phosphate dihydrate and/or anhydrous calcium hydrogen phosphate by introducing phosphoric acid, a water-soluble calcium salt and ammonia into a reaction, separating a precipitate from the resulting suspension, treating said precipitate to obtain a product, regenerating ammonia and a solution of a water-soluble calcium salt from remaining solution using calcium oxide or calcium hydroxide, with the specified ammonia and a solution of water-soluble

- 1 043491 calcium salts can be partially or completely returned to the process.

Application US 2015093309 describes a process for producing soda ash and ammonium sulfate by reusing by-products from the Merseburg and Solvay processes, which includes treating the brine with soda ash, which is a distiller waste, to desulfate the brine to produce gypsum, recovering pure salt from the desulfated brine solution and its use in the manufacture of soda ash in the Solvay method, washing the gypsum and reacting it with a solution of ammonia and carbon dioxide to produce CaCO ₃ and ammonium sulfate, separating CaCO ₃ from the ammonium sulfate solution and extracting solid ammonium sulfate, washing CaCO ₃ with subsequent calcination to form CO ₂ and lime, reuse of CO ₂ in the Solvay process to produce soda ash, reuse of lime with ammonium chloride obtained in the Solvay process, with ammonia regeneration and production of distiller waste containing CaCl ₂ as a by-product, reuse using distiller waste by-product to desulfate the brine and reusing the recovered ammonia.

Brief description of the invention

The present invention relates to the development of systems that provide recovery of carbon dioxide gases used in the process and ammonia, which acts as a catalyst, during the production of soda ash using the Solvay process, and which provide inclusion of the provided ammonia gases (shown as NH3) and dioxide carbon (shown as CO ₂ ) into the process in order to overcome the above disadvantages and provide new advantages to the related art.

The main object of the present invention is to provide a recovery system for the resulting waste gases of carbon dioxide and ammonia during the application of the Solvay process.

Another object of the present invention is to prevent environmental pollution by incorporating exhaust gases into the system.

Another object of the present invention is to make it economically feasible to produce soda ash using the Solvay process.

In order to achieve the above objects and those which can be deduced from the detailed description below, the present invention relates to a system for the recovery of ammonia gas, which acts as a catalyst during the production of soda ash by the Solvay process, and carbon dioxide used in the process. Accordingly, this system contains the following components:

i) an absorption column where salt water with ammonia is obtained as a starting material for the Solvay process, ii) a distillation column where the liquids are separated from each other, iii) a unit for washing the gas to be carbonated, containing an automatic valve and a circulation pump and which ensures the regeneration of waste gases in the carbonation column, iv) a unit for washing the gas to be filtered, containing an automatic valve and a circulation pump and which ensures the regeneration of the exhaust gases obtained in the filtration process.

Said absorption column contains at least one layer of filler.

In the main embodiment of the present invention, the outlet of the absorption column outlet pipe is connected to the inlet of the gas to be filtered washing unit by means of specially designed pipes.

Said unit for washing the gas to be carbonized has a length of 10-16 m and a width of 2-3 m. The unit for washing the gas to be carbonated is made of glass fiber reinforced polymer material.

The unit for washing the gas to be carbonized contains at least one layer of filler.

In a preferred embodiment of the present invention, the gas to be carbonated washing unit comprises at least one circulation pump.

In a preferred embodiment of the present invention, the circulation pump is located at the bottom of the gas-to-carbonate washing unit and at least 1 m lower than the outlet portion of the unit.

In a preferred embodiment of the present invention, the gas-to-carbonate washing unit comprises at least one automatic valve which increases the peak pressure in the unit at the outlet pipe portion.

In a preferred embodiment of the present invention, said gas-to-be-filtered washing unit has a length of 10 to 16 m and a width of 2 to 3 m.

In a preferred embodiment of the present invention, the gas to be filtered washing unit comprises at least one layer of filler.

In a preferred embodiment of the present invention, the gas to be filtered washing unit comprises at least one circulation pump.

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In a preferred embodiment of the present invention, said circulation pump of the unit for washing the gas to be filtered is located in the lower part and at least m lower than the section of the unit with the outlet opening.

In a preferred embodiment of the present invention, at least one automatic valve is provided in the outlet pipe portion of the gas scrubbing unit, which increases the peak pressure in the unit.

The present invention provides a method for the recovery of ammonia gas, which acts as a catalyst during the production of soda ash using the Solvay process, and carbon dioxide used in the process, where the following process steps are provided:

i) feeding the waste gases to be filtered, coming from the filtered products after the Solvay process, into a gas-to-be-filtered washing unit containing at least one of a circulation pump and/or an automatic valve, through pipes for supplying filtration, ii) treating the waste gases to be filtered gases entering the gas to be filtered washing unit with salt water and supplied to the absorption column and included in the system, iii) introducing gases that cannot be regenerated by salt water in the absorption column into the column to capture the gas to be filtered through specially designed bypass pipes, iv) re-treat gases that are not retained in the absorption column with salt water in the gas to be filtered washing unit, and re-feed to the absorption column, and include in the system,

v. supplying exhaust gases coming from the carbonization column to a gas-to-carbonate washing unit containing at least one of a circulation pump and/or an automatic valve through carbonization supply pipes, vi) treating exhaust gases to be carbonized entering the subject-washing unit carbonization of gas, using salt water, and feed them into the absorption column, and include in the system.

In the preferred embodiment of the present invention, in step (ii), by using the circulation pump present in the gas to be filtered washing unit, the recovery efficiency of waste ammonia and carbon dioxide gases by salt water is increased by 400-500%.

In the preferred embodiment of the present invention, in step (ii), by means of an automatic valve present in the outlet pipe portion of the gas to be filtered washing unit, the peak pressure in the gas to be filtered washing unit is increased to a pressure value of 200 to 700 mmHg.

In the preferred embodiment of the present invention, in step (v), by using the circulation pump present in the gas to be carbonated washing unit, the recovery efficiency of waste ammonia and carbon dioxide gases by salt water is increased by 400-500%.

In the preferred embodiment of the present invention, in step (v), by means of an automatic valve present in the outlet pipe portion of the gas to be carbonated washing unit, the peak pressure in the gas to be carbonated washing unit is increased to a value of 200 to 700 mmHg.

In a preferred embodiment of the present invention, more ammonia and carbon dioxide gases are recovered to a value of 400 to 500% using the closed cycle salt water present in the process.

Brief description of graphic materials

Fig. 1 is a general view of the existing system.

Fig. 2 is an illustrative illustration of gas to be filtered and gas to be carbonated washing units in an existing system.

Fig. 3 is an illustrative illustration of gas to be filtered and gas to be carbonated washing units in a preferred system.

Reference numbers:

- carbonization column;

- part with an outlet for carbon dioxide;

- part of the filtration;

- part of the waste gas to be filtered;

- distillation column;

- part with the outlet of the distillation column;

- absorption column;

- part with the outlet pipe of the absorption column;

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- the first layer of filler of the absorption column;

- second layer of absorption column filler;

- part of the washing of the gas to be absorbed;

- a part with an inlet for the exhaust gas to be absorbed;

- part with an inlet for salt water of the absorption column;

- inlet of the absorption column;

- unit for washing the gas to be carbonized;

- outlet pipe of the unit for washing the gas to be carbonized;

- a part with an inlet for salt water of a unit for washing the gas to be carbonized;

- the first layer of filler for the washing unit of the gas to be carbonized;

- installation for washing the gas to be carbonized;

- the second layer of filler for the washing unit of the gas to be carbonized;

- part with the inlet of the unit for washing the gas to be carbonized;

- part with the outlet of the unit for washing the gas to be carbonized;

- unit for washing the gas to be filtered;

- outlet pipe of the gas washing unit to be filtered;

- part with an inlet for salt water of the gas washing unit to be filtered;

- the first layer of filler for the gas washing unit to be filtered;

- gas washing unit of the gas washing unit to be filtered;

- the second layer of filler for the gas washing unit to be filtered;

- part with the outlet of the gas washing unit to be filtered;

- part with the inlet of the unit for washing the gas to be filtered;

- automatic valve;

- circulation pump.

Detailed Description of the Invention

In this detailed description, the subject matter of the invention relates to the recovery of ammonia gas, which acts as a catalyst during the production of soda ash using the Solvay process, and carbon dioxide used in the process; and to the inclusion of recovered ammonia and carbon dioxide gas in the method, and the subject matter of the invention is explained with reference to examples without giving any limiting effect only to make the subject matter more understandable.

If (NH4)HCO ₃ (ammonium bicarbonate) is added to a saturated purified salt solution in the Solvay process, the ammonium chloride formed dissolves and NaHCO ₃ (sodium bicarbonate) separates as a solid and precipitates. If NaHCO ₃ is filtered and separated and calcined, it turns into Na ₂ CO ₃ (sodium carbonate). In this way, sodium carbonate based products are obtained, the formation of which is expected after the process, as shown in equation 1.

Equation 1. Preparation of sodium carbonate (soda ash) from ammonium bicarbonate.

NH ₄ HCO ₃ + NaCl θ NaHCO ₃ + NH ₄ C1

2NaHCO ₃ + heat Na ₂ CO ₃ + H ₂ O + CO ₂

NH ₃ gas, which acts as a catalyst in the production of soda ash (Na2CO3) using the Solvay process, leaves the carbonation columns (10) in the form of ammonia-based compounds (NH4Cl, NH4OH, NH4HCO3, (NH ₄ )CO ₃ ). In the prior art, such compounds, which pass from the outlet portion (11) after carbonization to the filtration portion (20), are recovered as NH3 and CO ₂ gases in the distillation column (30). The recovered NH3 and CO2 gases are retained with saturated salt water in an absorption column (40). If NH3 gas is not retained in the absorption column (40) and reused, the absorption system does not operate efficiently due to high loss of ammonia, and hence the production of soda is not economically feasible.

In order to obtain the required efficiency of the Solvay process, during the implementation of the Solvay process, NH ₃ that is lost through the outlet pipes and other parts in the process must be added to the system. Accordingly, gases containing NH ₃ and CO ₂ that enter the absorption column in a Solvay system have the following characteristics and should be kept together with saturated salt water in limited quantities:

a) they are regenerated from the distillation column (30),

b) they cannot be retained in the carbonation column (10),

c) they come from the filtration part (20),

d) they cannot be retained in the absorption column (40).

In the Solvay process, it is not economically feasible to increase the amount of saturated salt water to retain more NH3 and _CO2 gases. The reason for this is that saturated salt water is used as a starting material in the production of soda ash.

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The concentration values of ammonia and carbon dioxide gases coming from the distillation column (30), the filtration portion (20) and the absorption column (40) are low, and their volume values are high. Consequently, containment of the NH3 and CO ₂ gases present in these gases with limited quantities of saturated salt water is not very effective, and some NH3 and CO ₂ gases are released into the atmosphere from the system through the vent pipes. Consequently, the loss of NH3 gas is significant.

Any type of changes in flow, temperature, pressure that occur in the system during the implementation of the Solvay method leads to even greater losses of NH3 in the system.

The most important steps of the Solvay process are described using the equations below.

Calcination of limestone and slaking of quicklime

Equation 2: Calcination of limestone and slaking of quicklime.

CaCO3 ( _TV ) CaO ( _TV ) + CO ₂ (gas) ^- Q

C(solid) + O2(gas) CO ₂ ( _Gas ) + Q

CaO ( _TV ) + H ₂ O ( _L ) Ca(OH) ₂ + Q

Preparation of salt solution

It can be obtained using rock salt, sea salt or natural salt waters. The Ca ⁺² and Mg ⁺² salts present in the salt must be removed, or if they are not removed, they precipitate in the form of CaCO ₃ and MgCO ₃ during the saturation of the solution with ammonia.

Making a salt water solution containing ammonia

A salt water solution containing ammonia was prepared by passing ammonia through a saturated salt solution. This method is carried out in absorption columns.

Passing CO2 through a salt water solution containing ammonia and separating NaHCO3

Equation 3: Passing CO ₂ through a salt water solution containing ammonia and separating NaHCO ₃ .

NH ₃ ( _ra3) + H ₂ O _(l ) “E NH4OH (solution) + Q

2ХНдОН (solution) + CO ₂ (gas) (CN ₄ ) ₂ CO ₃ (solution) + H ₂ O + Q (NH ₄ ) ₂ CO ₃ + H ₂ O + CO ₂ 2NH ₄ HCO ₃

NH ₄ HCO ₃ + NaCl NaHCO ₃ + NH ₄ C1

Calcination of NaHCO ₃

Equation 4: Calcination of NaHCO ₃ .

2NaHCO ₃ Na ₂ CO ₃ + H ₂ O + CO ₂

The parts associated with the Solvay method are carried out in the receiving parts of the system. Regeneration of gases such as ammonia and carbon dioxide is carried out in the gas to be filtered washing unit (60), in the absorption column (40) and in the gas to be carbonated washing units (50).

As can also be seen in the description above, the regeneration of ammonia and carbon dioxide gases is carried out with a limited amount of salt water in the system. Accordingly, an increase in the efficiency of regeneration of these gases is achieved by increasing the ratio of salt water with ammonia / gas or by increasing the pressure inside the columns.

In the existing system, as shown in Figure 2, NH3 and CO ₂ gases recovered from the distillation column (30) are regenerated in the absorption column (40); gaseous NH3 and CO ₂ that cannot be retained in the carbonation column (10) are regenerated in the gas to be carbonated washing unit (50); gaseous NH3 and CO2 coming from the filtration part (20) are regenerated in the unit (60) for washing the gas to be filtered; gases that cannot be retained in the absorption column (40) are regenerated in a unit (60) for washing the gas to be filtered with salt water.

In existing systems, gases that cannot be contained because the salt water used for exhaust gas regeneration has limited use in the system are released into the atmosphere through the gas to be filtered washing unit (60), the gas to be carbonated washing unit (50) and vent pipes. (41) absorption column.

In the preferred system shown in Figure 3, the first improvement is that each of the gas to be filtered washing unit (60) and the gas to be carbonated washing unit (50) contains one circulation pump (80). By adding a circulation pump (80) to the gas to be filtered washing unit (60) and to the gas to be filtered washing unit (50), salt water can be re-injected into the unit on top of the first layer (63) of the gas to be filtered washing unit filler and on top of the first layer (53) of the filler unit for washing the gas to be carbonized.

Said circulation pump (80) is located approximately at least 1 m lower relative to the part (66) with the outlet opening of the gas-to-be-filtered washing unit and the part (57) with the outlet opening of the gas-to-carbonate washing unit. Gas scrubbing units will not fill to level or discharge to level. The power of the circulation pumps (80) will be selected as the power at which the ratio of salt water with ammonia/gas provides the greatest efficiency.

As stated in the description above, the basic principle of the present invention is to provide an increase in the salt water ammonia/gas ratio. In the system, a limited amount of salt water is circulated in the units at a high level due to the placement of circulation pumps (80) in the gas scrubbing units, and said salt water is preferentially treated with ammonia. Thus, the preferred system provides water circulation capacity through the pumps (80) that provides at least 4 times the saltier water than the existing system. Ammonia and carbon dioxide gases are exposed in large volumes to much saltier water.

The gas scrubbing column designs present in the preferred system are similar to each other. Accordingly, the gas scrubbing units are made of glass fiber reinforced polyester material, and they have a length of about 10 to 16 m and a width of 2 to 3 m. The gas scrubbing units include a salt water inlet portion; part with an outlet for a solution of salt water with ammonia; a gas inlet portion where ammonia and carbon dioxide gases are delivered to the columns; and at least one layer of filler that allows said gases to be treated with salt water.

The target circulation pump (80) is located in the gas to be carbonated washing unit (50) and the gas to be filtered washing unit (60).

In a preferred embodiment of the present invention, more than one layer of filler is provided in the gas scrubbing units.

In a preferred embodiment of the present invention, the gas scrubbing units are made from glass fiber reinforced polyester materials. In this way, gas scrubbing units with high corrosion resistance, low cost and long service life can be used.

In existing systems, ammonia and carbon dioxide gases, which cannot be contained by the limited amount of salt water in the absorption column (40), are released into the atmosphere through a vent pipe portion. Another improvement that is present in the preferred system is that the outlet pipes (41), which are the outlet portions for ammonia and carbon dioxide gases that cannot be contained in the absorption column (40), are connected to the washing unit (60). gas to be filtered through pipes. Thus, exhaust gases discharged from the outlet pipe into the atmosphere under normal conditions can be re-exposed to salt water as they are directed to the gas to be filtered washing unit (60).

Also, as is known from the literature, the efficiency of absorption of gaseous NH3 and CO ₂ is related to the pressure in the blocks. As the pressure in the unit increases, the absorption efficiency of NH3 and _CO2 gases also increases. In a system that is preferred in accordance with the present invention, an automatic valve (70) is provided in the outlet pipe (51) of the gas to be carbonated washing unit and in the outlet pipe (61) of the gas to be filtered washing unit. In accordance with the said arrangement, an automatic valve (70) which regulates the peak pressure in the gas to be carbonated washing unit (50) and the gas to be filtered washing unit (60) present in the gas supply line leaving the gas to be carbonated washing unit (50) gas and a unit (60) for washing the gas to be filtered, is located in the outlet pipe (51) of the unit for washing the gas to be carbonized and in the outlet pipe (61) of the unit for washing the gas to be filtered. Thus, the peak pressure in the gas to be carbonated washing unit (50) and the gas to be filtered washing unit (60) and the pressure in the inlet portion (56) of the gas to be carbonated washing units and the inlet portion (67) of the gas to be filtered washing units gases are the same. According to a preferred system, the peak pressure values in the gas to be carbonated washing unit (50) and the gas to be filtered washing unit (60) are from 200 to 700 mmHg. Thus, the unit (50) for washing the gas to be carbonated and the unit (60) for washing the gas to be filtered will operate at a pressure value from 200 to 700 mmHg. Thus, in the preferred system, the efficiency of the columns will increase, and the losses of NH3 and CO ₂ will be

- 6 043491 decrease.

The principle of operation of the preferred system is carried out by using four separate systems simultaneously after obtaining soda ash using the Solvay method.

The operation of these four separate systems is described in detail in the descriptions below.

After completion of the carbonization process in the carbonization column (10), ammonia and carbon dioxide gases, which are exhaust gases, are transferred to the gas to be carbonated washing unit (50) through specially designed pipes. The gas-to-carbonate washing unit comprises at least one gas-to-carbonate washing unit filler layer (53); at least one circulation pump (80); at least one automatic valve (70); a gas inlet portion (56) of the gas-to-carbonate washing unit and a portion (57) with a waste gas outlet of the gas-to-carbonate washing unit; a part (52) with a salt water inlet of the gas to be carbonated washing unit. The waste gases ammonia coming from the inlet portion (56) of the gas to be carbonated washing unit and carbon dioxide are treated with salt water in the gas to be carbonated washing portion (54). In this part, salt water can retain certain proportions of ammonia. In the existing system, salt water is transferred to the absorption column (40) through pipes along with ammonia, which can be retained by the salt water, and salt water, which is required in the system, is added in the column. In the preferred system, the gas-to-carbonate washing unit (50) comprises a circulation pump (80) and an automatic valve (70) in the part (51) with the outlet pipe of the gas-to-carbonate washing unit. With these special structures, waste gases of ammonia coming from the inlet portion (56) of the gas to be carbonated washing unit and carbon dioxide can be treated many times with salt water inside the unit using the circulation pump (80). Accordingly, by using a limited amount of salt water, more waste ammonia and carbon dioxide gases can be retained and transferred to the absorption column (40). Another improvement present in the gas to be filtered washing unit (60) is the automatic valve (70), and it prevents the release of exhaust gases, namely ammonia and carbon dioxide gases, which cannot be stored in the existing system, being released into the atmosphere from the outlet pipe, Moreover, it provides an increase in the peak pressure in the unit and it can provide an increase in the absorption efficiency of exhaust gases in salt water.

Gaseous ammonia and carbon dioxide, which are waste gases coming from the filtration part (20), are sent to the gas to be filtered washing unit (60) through specially designed pipes. The block (60) for washing the gas to be filtered contains at least one layer (65) of filler; at least one circulation pump (80); at least one automatic valve (70); one part (67) with an inlet opening of the gas-to-be-filtered washing unit and one part (60) with an outlet opening for exhaust gas; at least one part (62) with a salt water inlet. The waste carbon dioxide and ammonia gases coming from the inlet portion (62) of the gas to be filtered washing unit are treated with salt water in the gas to be filtered washing portion (64). In this part, salt water can retain certain proportions of ammonia. In the current system, salt water is transferred to the absorption column (40) along with ammonia, which can be retained by the salt water, through pipes, and salt water is added to the column as needed by the system. In a preferred system, the gas-to-be-filtered washing unit (60) contains at least one circulation pump (80) and at least one automatic valve (70) in the part (61) with the outlet pipe of the gas-to-be-filtered washing unit. With these special structures, waste ammonia and carbon dioxide gases coming from the inlet portion (62) of the gas to be filtered washing unit can be treated many times with salt water inside the unit using the circulation pump (80). Accordingly, by using a limited amount of salt water, more waste ammonia and carbon dioxide gases can be retained and transferred to the absorption column (40). Another improvement present in the gas to be filtered washing unit (60) is an automatic valve (70), and ammonia and carbon dioxide gases, which cannot be stored in the existing system, ensure that exhaust gases are prevented from being released into the atmosphere from the outlet pipe (61). unit for washing the gas to be filtered, moreover, they increase the peak pressure inside the unit and thereby they can increase the absorption efficiency of waste gases in salt water.

The main function of the absorption column (40) in the Solvay process production system is to provide salt water with ammonia. In this column, the waste ammonia and carbon dioxide gases regenerated in the system are collected in this part. The absorption column (40) contains at least one fill layer (42), a gas scrubbing portion, at least one salt water inlet portion (46), and at least one salt water inlet portion (45).

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Claims (10)

exhaust gas inlet. In the absorption column (40), in order to retain waste gases that cannot be contained with a limited amount of salt water, the outlet pipe (41) of the absorption column is connected to the part (67) with the inlet of the gas-to-be-filtered washing unit through specially designed pipes. As a result, waste ammonia and carbon dioxide gases that cannot be retained in the absorption column (40) are treated with salt water one more time, and the exhaust gas regeneration efficiency of the system is increased. The waste gases of ammonia and carbon dioxide obtained after treatment in the distillation column (30) are transferred to the absorption column (40), and the waste gases in the absorption column (40) in the system are passed through similar treatment and included in the system. The scope of the present invention is set forth in the appended claims and is not to be limited by the illustrative embodiments set forth in the detailed description above. This is because one skilled in the art can obviously create similar embodiments in light of the above disclosures without departing from the basic principles of the present invention. CLAIM 1. A system for highly efficient recovery of gaseous ammonia, which acts as a catalyst during the production of soda ash in systems where the Solvay method is used, and carbon dioxide used in the method, wherein said system contains a carbonization column (10), a filtration column (20), and i) a distillation column (30), where the liquids from the filtration column (20) are separated from each other, ii) an absorption column (40), where salt water with ammonia is obtained, which is the starting material for the Solvay process, iii) a block (50 ) washing the gas to be carbonated, containing at least one automatic valve (70), which provides control of the peak pressure, and at least one circulation pump (80), which ensures the re-introduction of salt water into the block through its upper part and which provides regeneration ammonia and carbon dioxide gases produced in the carbonation column (10) by repeatedly treating said ammonia and carbon dioxide gases with a limited amount of saturated salt water, iv) a gas to be filtered washing unit (60) comprising at least one automatic valve ( 70), which provides peak pressure control, and at least one circulation pump (80), which re-introduces salt water into the unit through its upper part and which provides regeneration of ammonia and carbon dioxide gases produced in the filtration column (20) in by repeatedly treating said ammonia and carbon dioxide gases with a limited amount of saturated salt water, and connected to the outlet pipe portion of the absorption column (40). 2. The system according to claim 1, wherein said absorption column (40) contains at least one layer of filler. 3. The system according to claim 1, where said block (50) for washing the gas to be carbonized has a length of 10 to 16 m and a width of 2 to 3 m. 4. The system according to claim 1, where the block (50) for washing the gas to be carbonated is made of glass fiber reinforced polymer material. 5. System according to claim 1, where the unit (50) for washing the gas to be carbonated contains at least one layer of filler. 6. The system according to claim 1, where the specified circulation pump (80) is located in the lower part of the unit (50) for washing the gas to be carbonized and at least 1 m lower than the part (57) with the outlet opening. 7. The system according to claim 1, where said block (60) for washing the gas to be filtered has a length of 10 to 16 m and a width of 2 to 3 m. 8. System according to claim 1, where the block (60) for washing the gas to be filtered contains at least one layer of filler. 9. The system according to claim 1, where the specified circulation pump (80) is located in the lower part of the unit for washing the gas to be filtered and at least 1 m lower than the section (66) with the outlet opening. 10. A method for regenerating ammonia gases, which acts as a catalyst during the production of soda ash using the Solvay process, which is carried out in a carbonization column (10), a filtration column (20), a distillation column (30) and an absorption column (40), and dioxide carbon used in the process, which includes the following stages: i) supply the waste gases coming from the filtered products to be filtered -