CN112209411A - Prevention of NH in production of soda ash by ammonia-soda process3And CO2Development of gas loss system - Google Patents
Prevention of NH in production of soda ash by ammonia-soda process3And CO2Development of gas loss system Download PDFInfo
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- CN112209411A CN112209411A CN202010155310.6A CN202010155310A CN112209411A CN 112209411 A CN112209411 A CN 112209411A CN 202010155310 A CN202010155310 A CN 202010155310A CN 112209411 A CN112209411 A CN 112209411A
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
- C01D7/18—Preparation by the ammonia-soda process
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D7/00—Carbonates of sodium, potassium or alkali metals in general
- C01D7/12—Preparation of carbonates from bicarbonates or bicarbonate-containing product
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Abstract
The present invention relates to the development of a system for recovering ammonia that is catalytically active in the process of making soda ash by the ammonia-soda process, and for recovering carbon dioxide gas used in the process, and which system recovers ammonia and carbon dioxide gas into the production process.
Description
Technical Field
The present invention relates to the development of a system for recovering ammonia, which is catalytically active in the process for the preparation of soda ash by the ammonia-soda process, and carbon dioxide gas used in the process, and which recovers ammonia and carbon dioxide gas into the production process.
Background
The main raw materials of the ammonia-soda process are salt, limestone and anthracite, and ammonia plays a catalytic role in the process. Most suitably limestone (96% -98% CaCO)3(calcium carbonate)) is hard and contains small amounts of silica and impurities. Limestone is made to a suitable particle size.
In the ammonia-soda process, limestone is burned to obtain CaO (calcium oxide), and anthracite is used to obtain CO2。
The raw salt enters the reaction in the form of a saturated, pure salt solution (brine), usually obtained from rock salt.
In this process, (NH) is added4)HCO3(ammonium bicarbonate) when added to a saturated crude salt solution, the ammonium chloride solution formed dissolves and NaHCO3(sodium bicarbonate) precipitated as a solid; if NaHCO3Is filtered, separated and calcined to be converted into Na2CO3(sodium carbonate), as shown in equation 1:
2NaHCO3+heat→Na2CO3+H2O+CO2
formula 1. obtaining sodium carbonate
For the ammonia-soda process, the recovery of ammonia is very important, since this process will be realized at a more suitable cost. The economic success of the ammonia-soda process depends on the recovery of nearly all of the ammonia used in the process. Most of the ammonia used was treated with sodium bicarbonate filtrate and with NH4In the form of Cl. Small amounts of ammonium hydroxide are present in the form of ammonium carbonate and ammonium bicarbonate. In addition, ammonia can also be present in some of the precipitates and solutions separated in this process.
In the literature, all solutions and precipitates consisting of ammonia in the ammonia-soda process are sent to an ammonia recovery system. By the action of heat, ammonium hydroxide, ammonium carbonate and ammonium bicarbonate are decomposed and separated in an ammonia recovery system. The ammonium chloride enters the reaction by adding lime milk to the medium and ammonium hydroxide is obtained. The ammonium hydroxide is heated and ammonia is recovered.
2NH4Cl+Ca(OH)2→CaCl2+2NH3+2H2O
Equation 2. obtaining ammonia
The water vapor supplied through the bottom of the separation column raises almost all of the ammonia in the medium. NH (NH)3And stripped CO2Gas is discharged from the upper part of the separation tower which is in a filling type and CaCl2Unreacted NaCl and the remaining residue (including excess lime) are taken from the bottom of the separation column.
In the known art, the NH being recovered3And CO2The gas is retained in the absorber column system of the ammonia-soda process system along with saturated pure salt solution. If NH is not substituted3The gas remains in the absorption system and, if it is no longer used, the absorption system cannot be operated efficiently due to the large loss of ammonia, and therefore the production of alkali is uneconomical. Retention of NH by addition of saturated salt solution3And CO2Gas is not practical. Since saturated salt solutions containing ammonia are used in the carbonation system and production. In addition, the salt solution containing ammonia used corresponds to the production grade.
Therefore, in view of all of the above problems, improvements in the related art are needed.
Disclosure of Invention
The present invention relates to the development of a system for recovering carbon dioxide used in the ammonia-soda process, and ammonia that is catalytic in the preparation of soda ash by the ammonia-soda process, and to the ammonia obtained (denoted as NH)3) And carbon dioxide gas (expressed as CO)2) Recycled to the production process, thereby eliminating the aforementioned drawbacks and bringing new advantages to the related art. The main object of the present invention is to provide a process for recovering a product obtained when using the ammonia-soda processCarbon dioxide and ammonia off-gas.
It is another object of the present invention to prevent environmental pollution by incorporating exhaust gases into the system.
It is another object of the present invention to make the ammonia soda process more economical for producing soda ash.
In order to achieve the above object, the present invention relates to a recovery system of ammonia and carbon dioxide gas, the ammonia being catalytically effective in the production of soda ash by an ammonia-soda process, the carbon dioxide gas being used in the ammonia-soda process; the recovery system includes:
i. an absorption tower for producing ammonia-containing brine, wherein the brine is a raw material of the ammonia-soda process;
a distillation column in which the liquids are separated from each other;
a carbon dioxide scrubbing unit comprising an automatic valve and a circulation pump for recovering off-gas from the carbonation tower;
a filtered gas scrubbing unit comprising an automated valve and a circulation pump for recovering the off-gas obtained from the filtering step.
The absorber tower includes at least one fill pack.
In the main embodiment of the invention, the absorption tower funnel is connected to the input of the filtered gas scrubbing unit by specially designed piping.
The length of the carbonic acid gas washing unit is between 10 and 16 meters, and the width of the carbonic acid gas washing unit is between 2 and 3 meters. The carbon dioxide scrubbing unit is made of a glass reinforced polymer material.
The carbon dioxide scrubbing unit comprises at least one filler package.
In a preferred embodiment of the present invention, the carbon dioxide scrubbing unit comprises at least one circulation pump.
In a preferred embodiment of the present invention, the circulation pump is located in a lower portion of the carbonic acid gas scrubbing unit and is at least 1 meter lower than the output area.
In a preferred embodiment of the invention, at least one automatic valve for increasing the pressure in the unit is provided in the carbonated washing unit funnel.
In a preferred embodiment of the invention, the filtered gas scrubbing unit has a length of between 10 and 16 meters and a width of between 2 and 3 meters.
In a preferred embodiment of the invention, the filtered gas scrubbing unit comprises at least one filler package.
In a preferred embodiment of the invention, the filtered gas scrubbing unit comprises at least one circulation pump.
In a preferred embodiment of the invention, the circulation pump is located in the lower part of the filtered gas scrubbing unit and at least 1 meter below the output area.
In a preferred embodiment of the invention, at least one automatic valve increasing the unit peak pressure is provided in the filtered gas scrubbing unit funnel.
The present invention is a method for recovering ammonia and carbon dioxide gas, the ammonia being catalytically useful in the production of soda ash by an ammonia-soda process in which the carbon dioxide gas is used, wherein the method comprises:
i. the filtered waste gas enters a filtered gas washing unit through a filtering pipeline, wherein the filtered waste gas is a filtering product obtained after an ammonia-soda process, and the filtered gas washing unit comprises at least one circulating pump and/or at least one automatic valve;
treating the filtered off-gas entering the filtered gas scrubbing unit with brine, sending the filtered off-gas to an absorption tower and entering a system;
passing the gas that cannot be recovered in the absorber column to the filtered gas scrubbing unit through a funnel designed;
the brine in the filtered gas scrubbing unit retreats gases that do not enter the absorber tower, reintroduces the gases into the absorber tower and is incorporated into the system;
v. conveying the off-gas from the carbonation tower through a carbonation conduit to a carbonation gas scrubbing unit comprising at least one circulation pump and/or at least one automatic valve;
treating the carbonated off-gas entering the carbonation scrubbing unit with brine, sending the carbonated off-gas to the absorber tower and into a system.
In a preferred embodiment of the present invention, in step (ii), the efficiency of brine recovery of spent ammonia and carbon dioxide gas is increased by 400% to 500% by the circulation pump in the filtered gas washing unit.
In a preferred embodiment of the present invention, in step (ii), the peak pressure of the filtered gas scrubbing unit is increased to 200mmHg to 700mmHg by an automatic valve of the funnel part of the filtered gas scrubbing unit.
In a preferred embodiment of the present invention, in step (v), the efficiency of brine recovery of spent ammonia and carbon dioxide gas is increased to 400% to 500% by the circulation pump in the carbonic acid gas scrubbing unit.
In a preferred embodiment of the present invention, in step (v), the carbonated scrubbing unit peak pressure is increased to 200mmHg to 700mmHg by an automatic valve of a funnel portion of the carbonated scrubbing unit.
In a preferred embodiment of the invention, more ammonia and carbon dioxide gases are recovered, by means of the brine used in the process, up to 400% to 500%.
Drawings
FIG. 1 is a general schematic diagram of a prior art system;
FIG. 2 is a schematic representation of a filtration and carbonation scrubbing unit in a prior art system; FIG. 3 is a schematic representation of a filtration and carbonation scrubbing unit in the proposed system.
List of reference numerals:
10 carbonization tower
11 carbon dioxide output part
20 filter part
21 part for filtering waste gas
30 distillation column
31 distillation column outlet
40 absorption tower
41 absorption tower funnel part
42 first absorbent fill pack
43 second absorbent Filler Package
44 absorption gas washing part
45 absorption exhaust gas input part
46 absorbed saline solution input
47 absorption column input
50 carbon dioxide scrubbing unit
51 carbonic acid gas washing unit funnel
52 carbonate scrubbing unit salt solution input
53 first carbonic acid gas washing filler bag
54 carbon dioxide gas washing
55 second hydrochloric acid gas scrubbing packing bag
56 carbonic acid gas washing unit input part
57 carbonic acid gas washing unit output part
60 filtered gas scrubbing unit
61 Filter gas washing Unit funnel
62 filtered gas scrubbing unit salt input
63 first filtered gas scrubbing unit fill pack
64 filtered gas scrubbing unit
65 second step gas washing unit filling bag
66 filtered gas scrubbing unit output
67 filtered gas scrubbing unit input
70 automatic valve
80 circulating pump
Detailed Description
The invention relates to the recovery of ammonia and carbon dioxide gas in an ammonia-soda process, and the recycling of the recovered ammonia and carbon dioxide gas, wherein the ammonia plays a role of a catalyst in the process of producing soda by adopting the ammonia-soda process. The present invention is illustrated by examples, which are only for the purpose of easier understanding of the present invention and do not have any limiting effect. In the ammonia-soda process, when (NH)4)HCO3(ammonium bicarbonate) was added to a saturated pure salt solution, ammonium chloride was dissolved, and NaHCO was added3(sodium bicarbonate) was isolated and precipitated as a solid. If NaHCO3Is filtered, separated and calcined, and it is converted to Na2CO3(sodium carbonate). Thereby, a sodium carbonate product as shown in formula 1 was obtained.
2NaHCO3+heat→Na2CO3+H2O+CO2
Formula 1. obtaining sodium carbonate (soda) from ammonium bicarbonate
NH3The gas being ammonia (NH)4Cl，NH4OH，NH4HCO3，(NH4)2CO3) Is discharged from the carboniser 19 in the form of a mixture of NH3The gas plays a role of catalyst in the process of producing sodium carbonate by ammonia-soda process. In the prior art, these compounds are conveyed from the carbonization outlet (11) to the filter (20) as NH in the distillation column (30)3And CO2And (5) recovering the gas. In the absorption column 40, NH is recovered3And CO2The gas is stored in saturated brine. In case of NH3The gas is not retained in the absorption tower 40 and is no longer used, and the absorption system cannot operate in an efficient manner due to the large loss of ammonia, and the production of soda ash is uneconomical.
Once the ammonia-soda process is applied, NH is lost from the funnel or other portion of the process in order to obtain the desired benefit from the ammonia-soda process3Must be added to the system. Therefore, the absorption columns of those systems using the ammonia-soda process contain NH3And CO2Has the following characteristics, which should be kept together in a limited amount of saturated brine:
a-recovering them from the distillation column 30,
b-they are not retained in the carboniser 10,
c-they come from the filter house 20,
d-they cannot remain in the absorber column 40.
In the ammonia-soda process, the total amount of saturated salt solution is increased to maintain more NH3And CO2The gas is uneconomicalIn (1). This is because saturated brine is not a raw material for producing soda ash.
The concentrations of ammonia and carbonic acid gas from the distillation column 30, the filtration section 20, and the absorption column 40 are low and the volumes are large. Thus, the NH present in the gas is maintained with a limited amount of saturated brine3And CO2The gas is not very effective and some NH3And CO2Gas is released from the system to the atmosphere through the funnel portion. Thus, NH3The gas loss is large.
The change of any one of the flow rate, the temperature and the pressure of the system in the ammonia-soda process can further cause NH in the system3The amount of loss increases.
The equations given below are the most important steps in the ammonia-soda process:
burning limestone and slaking burnt lime
CaCO3(k)→CaO(k)+CO2(g)-Q
C(k)+O2(g)→CO2(g)+Q
CaO(k)+H2O(s)→Ca(OH)2+Q
Formula 2. burning limestone and slaked burnt lime
Preparation of salt solutions
The salt solution may be prepared from limestone, sea salt or natural brine. Ca in the salt must be removed+2And Mg+2If not removed, a precipitate CaCO may form in saturated solutions of ammonia3And MgCO3。
Preparation of aqueous salt solutions containing ammonia
An aqueous salt solution containing ammonia is prepared by feeding ammonia into a saturated salt solution, and the process is carried out in an absorption tower.
Introducing CO into the saline solution containing ammonia2And isolating NaHCO3
(NH4)2CO3+H2O+CO2→2NH4HCO3
NH4HCO3+NaGl→NaHCO3+NH4Cl
Formula 3 introduction of CO into ammonia-containing brine solution2And isolating NaHCO3
Calcined NaHCO3
2NaHCO3→Na2CO3+H2O+CO2
Equation 4. calcinated NaHCO3
The part related to the ammonia-soda process is realized in the production part of the system. Recovery of gases such as ammonia and carbon dioxide is achieved in the filtered gas unit 60, the absorption tower 40 and the carbon dioxide scrubbing unit 50.
As described above, the recovery of ammonia and carbon dioxide gas is achieved by adding brine to the system. Thus, an increase in the gas recovery efficiency can be achieved by increasing the ammonia/gas ratio in the brine or by increasing the pressure in the column.
In the present system, NH from distillation column 30 is shown in FIG. 23And CO2The gas is recovered in the absorption tower 40 and the NH that cannot be retained in the carbonization tower 103And CO2The gas is recovered in the carbonic acid gas scrubbing unit 50; NH from the filter house 203And CO2The gas is recovered in the filtration and washing unit 60; those gases that cannot be retained in the absorption tower 40 are recovered by brine in the filtered gas washing unit 60.
In the present system, since the brine for recovering the offgas has a specific use in the system, the gas that cannot be retained is released into the atmosphere through the filtered gas scrubbing unit 60, the carbonic acid gas scrubbing unit 50, and the funnel 41 of the absorption tower.
In the proposed system, as shown in fig. 3, the first modification is that the filtered gas unit 60 and the carbonation scrubbing unit 50 each include a circulation pump 80. Due to the addition of the circulation pump 80 in the filtered gas scrubbing unit 60 and the carbonated gas scrubbing unit 50, brine may be re-fed into the units from the first filtered gas scrubbing unit fill pack 63 and the first carbonated fill pack 53.
The circulation pump 80 is disposed approximately at least one meter below the filtered gas scrubbing unit output 67 and the carbonated gas scrubbing unit output 57. In the gas scrubbing unit, there is no liquid level filling and no liquid level draining. The capacity of the circulation pump (80) is the capacity at which the ammonia/gas brine ratio is most effective.
As mentioned above, the basic principle of the invention consists in increasing the ammonia/gas ratio in the brine. In this system, the defined brine, which is mainly treated with ammonia, is circulated at a high level within the unit by means of a circulation pump 80 placed on the gas scrubbing unit. Thus, with the proposed system, the water circulation capacity 80 is at least four times greater than existing systems. High volumes of ammonia and carbon dioxide gas may contact more brine.
The gas scrubber design in the proposed system is similar. The gas scrubbing unit is made of glass reinforced polyester material and has a length of about 10 to 16 meters and a width of between 2 and 3 meters. The gas scrubbing unit includes a brine input; an ammonia-containing brine output part; a gas input to bring ammonia and carbon dioxide gas to the column; and at least one packing bag for handling salt-containing water gas.
The circulation pump 80 is provided on the carbonic acid gas scrubbing unit 50 and the filtered gas scrubbing unit 60.
In a preferred embodiment of the invention, the gas scrubbing unit is made of a glass-reinforced polyester material. Thereby, a gas scrubbing unit with high corrosion resistance, low cost and long service life can be employed.
In the current system, ammonia and carbon dioxide gases that cannot be held in the finite brine by the absorber tower 40 are vented to the atmosphere through a funnel. Another modification of the proposed system is the funnels, which are the output locations for ammonia and carbon dioxide gases that cannot be retained in the absorber column 40, which are connected by piping to the filtered gas scrubbing unit 60. Thereby, the exhaust gas, which is delivered from the hopper to the atmosphere under normal conditions, can be reabsorbed by the brine by being delivered to the filtered gas washing unit 60.
NH is also known from the literature3And CO2The absorption efficiency of the gas is related to the pressure in the cell. NH as the pressure in the cell increases3And CO2The absorption efficiency of the gas is also high. In the preferred system of the present invention, the automatic valves 70 provided in the carbonate gas scrubbing unit gas input 56 and the filtered gas scrubbing unit gas input 57 are located in the carbonate gas scrubbing unit gas output 57 and the filtered gas scrubbing unit gas output 67. Based on the above arrangement, automatic valves 70 for regulating the peak pressures of the carbonated wash unit 50 and filtered gas wash unit 60 are provided in the lines leading from the carbonated wash unit 50 and filtered gas wash unit 60 to the carbonated output 57 and to the filtered gas wash unit gas output 67. Accordingly, the peak pressures of the carbonate scrubbing unit 50 and the filtered gas scrubbing unit 60 are the same as the pressures of the carbonate scrubbing unit input 56 and the filtered gas scrubbing unit gas input 67. With this recommended system, the peak pressures of the carbonate scrubbing unit 50 and the filtered gas scrubbing unit 60 are between 200mm hg and 700mm hg. Thus, the carbonate gas scrubbing unit 50 and the filtered gas scrubbing unit 60 will function at pressure values between 200mm Hg and 700mm Hg. By recommending a system, the efficiency of the tower will increase, and NH3And CO2The loss of (2) will be reduced.
After the production of soda by the ammonia-soda process, the operating principle of the proposed system is implemented by four separate systems applied simultaneously. In the following description, the details of the operation of these four separation systems are presented in detail.
After the carbonation process in the carbonation tower 10 is completed, ammonia and carbon dioxide gas as exhaust gas are transferred to the carbonation scrubbing unit 50 through a specially designed pipe. The carbonate scrubbing unit includes at least one carbonation fill pack 53, at least one circulation pump 80, at least one automatic valve 70, a carbonate scrubbing unit input 56, and a carbonate scrubbing unit effluent output 57 and a carbonate scrubbing unit brine output 52. Ammonia and carbon dioxide off-gas from the output of the carbonate scrubbing unit 56 are treated with brine in the carbonate scrubbing unit 54. Here, the brine may maintain a specific ratio of ammonia. In the current system, brine and ammonia are transferred through piping to the absorber 40 where the ammonia can be stored in brine, increasing the brine required by the system. In the preferred system, the carbonate scrubbing unit 50 includes a circulation pump 80 and an automatic valve 70 located in the carbonate scrubbing unit funnel 51. With these particular designs, ammonia and carbon dioxide off-gas from the carbon dioxide scrubbing unit input 56 may be treated multiple times within the unit by brine and circulation pump 80. Accordingly, more ammonia and carbon dioxide off-gas can be preserved in the limited brine and can be transferred to the absorption tower 40. Another improvement of the filtered gas scrubbing unit 60 is the automatic valve 70 which prevents the discharge of exhaust gas, and in addition, increases the peak pressure within the unit and the efficiency of absorption of exhaust gas from the brine, i.e., ammonia and carbon dioxide gas that cannot be stored in existing systems and is discharged to the atmosphere from a hopper.
Ammonia and carbon dioxide gas, which are exhaust gases from the filter section 20, are sent to the filtered gas scrubbing unit 60 through specially designed piping. The filtered gas scrubbing unit 60 includes at least one fill pack 65, at least one circulation pump 80, at least one automatic valve 70, an exhaust gas input 67, an exhaust gas output 60, and at least one brine input 62. The carbon dioxide off-gas and ammonia from the filtered gas scrubbing unit input 62 are treated with brine in the filtered gas scrubbing section 64. Here, the brine may retain a certain proportion of ammonia. In prior systems, brine is fed to the absorber 40 along with ammonia, which may be held in brine, which is fed through a pipe as needed by the system. In the proposed system, the filtered gas scrubbing unit 60 comprises at least one circulation pump 80 and at least one automatic valve 70 at the filtered gas scrubbing unit funnel 61. With these particular designs, ammonia and carbon dioxide off-gas from filtered gas scrubbing unit input 62 can be treated multiple times within the unit by brine and circulation pump 80. Accordingly, more ammonia and carbon dioxide off-gas can be preserved by the limited brine and can be transferred to the absorption tower 40. Another modification in the filtered gas scrubbing unit 60 is the automatic valve 70, ammonia and carbon dioxide gases that cannot be conserved in the system, preventing the exhaust gas from being discharged from the filtered gas scrubbing unit funnel 61 to the atmosphere, and in addition, they increase the peak pressure within the unit, thereby increasing the efficiency of absorbing exhaust gas in brine.
The absorption column 40 in the ammonia-soda process production system basically functions to produce brine containing ammonia. In this column, ammonia and carbon dioxide off-gases recovered from the system are collected there. The absorber tower 40 includes at least one fill pack 42, a gas scrubbing section, at least one brine input 46, and at least one flue gas input 45. In the absorber 40, in order to retain the exhaust gas that cannot be retained by the limited brine, the absorber funnel 41 is connected to the filtered gas scrubbing unit input 67 by specially designed piping. Thereby, the ammonia and carbon dioxide waste gas which is not retained by the absorption tower 40 is treated again by the brine, and the efficiency of the system for recovering the waste gas is increased.
Ammonia and carbon dioxide off-gas obtained after the treatment in the distillation column 30 are transferred to the absorption column 40 and the off-gas in the absorption column 40 in the system is similarly treated so as to be contained in the system.
The scope of protection of the invention is not limited to the illustrative disclosure described above. This is because similar embodiments can be obviously obtained from the above disclosure by a person skilled in the relevant art without departing from the main principle of the present invention.
Claims (20)
1. A recovery system for ammonia, which is catalytic in the production of soda ash by an ammonia-soda process, and for carbon dioxide gas, which is used in the ammonia-soda process, wherein the recovery system comprises:
i. an absorption tower (40) for producing brine containing ammonia, wherein the brine is a raw material of the ammonia-soda process;
a distillation column (30) in which the liquids are separated from each other;
a carbonic acid gas scrubbing unit (50) comprising an automatic valve (70) and a circulation pump (80) for recovering off-gas in the carbonizer (10);
a filtered gas washing unit (60) for recovering the off-gas obtained from the filtering section (20), comprising an automatic valve (70) and a circulation pump (80).
2. The system of claim 1, wherein the absorber column (40) comprises at least one packing pack.
3. The system according to claim 1, wherein the absorption tower funnel (41) is connected to the input (67) of the filtered gas scrubbing unit by a designed pipe.
4. The system of claim 1, wherein the carbon dioxide scrubbing unit (50) is between 10 and 16 meters in length and between 2 and 3 meters in width.
5. The system of claim 1, wherein the carbon dioxide scrubbing unit (50) is made of a glass reinforced polymer material.
6. The system of claim 1, wherein the carbonate scrubbing unit (50) comprises at least one fill pack.
7. The system of claim 1, wherein the carbonic acid gas scrubbing unit (50) comprises at least one circulation pump (80).
8. The system of claim 7, wherein the circulation pump (80) is located in a lower portion of the carbonated scrubbing unit (50) and is at least 1 meter below an output area (57).
9. The system of claim 1, wherein at least one automatic valve (70) to increase unit pressure is provided in the carbonated wash unit funnel (51).
10. The system according to claim 1, wherein the filtered gas scrubbing unit (60) has a length of between 10 and 16 meters and a width of between 2 and 3 meters.
11. The system of claim 1, wherein the filtered gas scrubbing unit (60) comprises at least one fill pack.
12. The system according to claim 1, wherein the filtered gas scrubbing unit (60) comprises at least one circulation pump (80).
13. The system of claim 12, wherein the circulation pump (80) is located in a lower portion of the filtered gas scrubbing unit and is at least 1 meter below the output area (66).
14. A system according to claim 1, wherein at least one automatic valve (70) increasing the unit peak pressure is provided in the filtered gas washing unit funnel (61).
15. A method for recovering ammonia that is catalytic in the production of soda ash by an ammonia-soda process and carbon dioxide gas that is used in the ammonia-soda process, wherein the method comprises:
i. the filtered exhaust gas is passed through a filtering conduit into a filtered gas washing unit (60), said filtered exhaust gas coming from the filtered product after the ammonia-soda process, said filtered gas washing unit (60) comprising at least one circulation pump (80) and/or at least one automatic valve (70);
treating the filtered off-gas entering the filtered gas scrubbing unit (60) with brine, sending the filtered off-gas to an absorption column (40) and bringing it into the system;
feeding the gas that cannot be recovered in the absorption column (40) to the filtered gas washing unit (60) through a funnel designed;
the brine in the filtered gas scrubbing unit (60) retreats the gas that did not enter the absorber, reintroduces the gas into the absorber (40), and is incorporated into the system;
v. conveying the off-gas from the carbonation tower (10) through a carbonation conduit to a carbonation gas scrubbing unit (50), the carbonation gas scrubbing unit (50) comprising at least one circulation pump (80) and/or at least one automatic valve (70);
treating the carbonated off-gas entering the carbonation scrubbing unit (50) with brine, sending the carbonated off-gas to the absorber tower (40), and incorporating into the system.
16. The recovery method of ammonia and carbon dioxide gas as claimed in claim 15, wherein in step (ii), the efficiency of brine recovery of spent ammonia and carbon dioxide gas is increased by 400% to 500% by providing a circulation pump (80) in the filtered gas washing unit (60).
17. The recovery method of ammonia and carbon dioxide gas as claimed in claim 15, wherein in the step (ii), the peak pressure of the filtered gas washing unit (60) is increased to 200mmHg to 700mmHg by an automatic valve (70) of a funnel part (61) of the filtered gas washing unit.
18. A method for the recovery of ammonia and carbon dioxide gas as claimed in claim 15, wherein in step (v), the efficiency of brine recovery of spent ammonia and carbon dioxide gas is increased to 400% to 500% by the circulation pump in the carbon dioxide scrubbing unit (50).
19. A method of recovering ammonia and carbon dioxide gas according to claim 15, wherein in step (v), the peak pressure of the carbonic acid gas scrubbing unit (50) is increased to 200mmHg to 700mmHg by an automatic valve (70) of a funnel portion (51) of the carbonic acid gas scrubbing unit.
20. A method of recovering ammonia and carbon dioxide gas as claimed in claim 15, wherein 400% to 500% of ammonia gas and carbon dioxide gas are recovered by the fixed brine used in the method.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| TR2019/10474 | 2019-07-12 | ||
| TR2019/10474A TR201910474A2 (en) | 2019-07-12 | 2019-07-12 | DEVELOPING A SYSTEM THAT PREVENTS LOSSES OF NH3 and CO2 GASES IN SODA ASH PRODUCTION WITH THE SOLVAY PROCESS |
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| CN112209411A true CN112209411A (en) | 2021-01-12 |
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| CN202010155310.6A Pending CN112209411A (en) | 2019-07-12 | 2020-03-06 | Prevention of NH in production of soda ash by ammonia-soda process3And CO2Development of gas loss system |
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| CN (1) | CN112209411A (en) |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1458065A (en) * | 2003-06-06 | 2003-11-26 | 王修立 | Recovering process for NH3 and CO2 from production of low salt low potassium heavy sodium carbonate |
| CN101708858A (en) * | 2009-11-28 | 2010-05-19 | 大连化工研究设计院 | Method for producing low-salt high-quality dense soda ash |
| CN101717100A (en) * | 2009-11-28 | 2010-06-02 | 大连化工研究设计院 | Method for producing low-salt high-quality soda ash dense |
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| CN104556155A (en) * | 2014-12-25 | 2015-04-29 | 唐山三友化工股份有限公司 | Method for producing sodium carbonate by utilizing chlor-alkali ammonia-alkali tailings |
| PL420588A1 (en) * | 2017-02-21 | 2018-08-27 | Ciech R&D Spółka Z Ograniczoną Odpowiedzialnością | Method for producing sodium carbonate integrated with carbon dioxide capture by ammonia process |
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2019
- 2019-07-12 TR TR2019/10474A patent/TR201910474A2/en unknown
-
2020
- 2020-02-06 EA EA202090251A patent/EA202090251A1/en unknown
- 2020-03-06 CN CN202010155310.6A patent/CN112209411A/en active Pending
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| CN1458065A (en) * | 2003-06-06 | 2003-11-26 | 王修立 | Recovering process for NH3 and CO2 from production of low salt low potassium heavy sodium carbonate |
| CN101708858A (en) * | 2009-11-28 | 2010-05-19 | 大连化工研究设计院 | Method for producing low-salt high-quality dense soda ash |
| CN101717100A (en) * | 2009-11-28 | 2010-06-02 | 大连化工研究设计院 | Method for producing low-salt high-quality soda ash dense |
| CN102698585A (en) * | 2012-06-29 | 2012-10-03 | 青岛碱业股份有限公司 | Method for recyling carbon dioxide in boiler flue gas |
| CN104556155A (en) * | 2014-12-25 | 2015-04-29 | 唐山三友化工股份有限公司 | Method for producing sodium carbonate by utilizing chlor-alkali ammonia-alkali tailings |
| PL420588A1 (en) * | 2017-02-21 | 2018-08-27 | Ciech R&D Spółka Z Ograniczoną Odpowiedzialnością | Method for producing sodium carbonate integrated with carbon dioxide capture by ammonia process |
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| Publication number | Publication date |
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| TR201910474A2 (en) | 2019-08-21 |
| EA202090251A1 (en) | 2021-01-29 |
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