CN113318681A - Improved heavy soda ash production device and method - Google Patents
Improved heavy soda ash production device and method Download PDFInfo
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- CN113318681A CN113318681A CN202110883428.5A CN202110883428A CN113318681A CN 113318681 A CN113318681 A CN 113318681A CN 202110883428 A CN202110883428 A CN 202110883428A CN 113318681 A CN113318681 A CN 113318681A
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Abstract
The invention discloses an improved heavy soda ash production device and a method, wherein the improved heavy soda ash production device comprises the following steps: preparing heavy soda by taking light soda and a sodium carbonate solution as raw materials, carrying out solid-liquid separation on discharged heavy soda crystal slurry through a centrifugal machine, sending the obtained heavy soda to a fluidized bed for drying and cooling, and sending mother liquor to a mother liquor barrel after heat exchange; introducing tail gas of a drying section of the fluidized bed and tail gas of a cooling section into a cyclone separator, separating to obtain heavy soda ash dust and dust-containing air, mixing the heavy soda ash dust and light soda ash for a hydration reaction, and sending the dust-containing air to a tail gas washing tower; the tail gas washing tower re-absorbs the heavy soda ash in the dust-containing air to generate part of low-grade steam, and the low-grade steam and the high-grade steam enter a steam system together. The production control of the invention is convenient to operate, DCS automatic control and adjustment can be realized in the procedures of hydration, centrifugation, calcination and cooling, the produced heavy soda has uniform granularity and high purity, and the comprehensive utilization of the tail gas of the heavy soda is realized.
Description
Technical Field
The invention relates to the field of combined soda ash production, in particular to an improved soda ash production device and method.
Background
The heavy soda production has a large specific gravity in the combined soda production, the hydration reaction temperature in the heavy soda process is controlled between 95 ℃ and 105 ℃, the hydration reaction is self-exothermic, the temperature fluctuation is large, the heavy soda yield can be influenced, the hydration reaction temperature must be strictly controlled, the heavy soda crystal slurry discharged from the hydration reactor is separated by a centrifuge, the solid part enters a fluidized bed for drying and cooling to obtain the heavy soda, the tail gas of the heavy soda is generally directly exhausted after simple treatment, the equipment corrosion is easy to cause, the tail gas of the fluidized bed contains a part of heavy soda and certain energy, the direct exhaust not only causes the waste of resources and energy, but also the long-term exhaust of dust particles contained in the tail gas can generate adverse effects on the environment, and the normal production of the heavy soda production area is influenced.
Disclosure of Invention
The invention aims to overcome the defects in the prior art, and provides an improved heavy soda ash production device and method, which are convenient for treating heavy soda ash tail gas, avoid the waste of resources and energy, realize the comprehensive utilization of the heavy soda ash tail gas and ensure the continuous and stable operation of a hydration reactor.
The purpose of the invention can be realized by the following technical scheme.
The improved heavy soda production device comprises a hydration reactor, a centrifuge and a fluidized bed, wherein a discharge port of the hydration reactor is connected with an inlet of the centrifuge through a pipeline, a solid outlet of the centrifuge is connected with the fluidized bed through a pipeline, and a liquid outlet of the centrifuge is connected with a tube side inlet of a heat exchanger through a pipeline;
the tail gas outlet of the drying section and the tail gas outlet of the cooling section of the fluidized bed are both connected to the feed inlet of a cyclone separator through pipelines, the gas outlet of the cyclone separator is connected with the gas inlet of a tail gas washing tower through a pipeline, the heavy sodium carbonate outlet of the cyclone separator is connected with a hydration reactor through a pipeline, and the hydration reactor is also connected with a light sodium carbonate input pipeline; the tail gas washing tower is characterized in that a circulating liquid outlet of the tail gas washing tower is connected with an inlet of a liquid discharge valve through a circulating pump, one of two outlets of the liquid discharge valve is connected with the circulating liquid inlet of the tail gas washing tower, the other outlet of the two outlets of the liquid discharge valve is connected with a liquid inlet of a mother liquid barrel, and a liquid outlet of the mother liquid barrel is connected with a hydration reactor; a steam outlet of the tail gas washing tower is connected to a steam system through a steam heat pump;
the heat exchanger tube pass outlet is connected with a liquid inlet of the mother liquid barrel through a pipeline, the heat exchanger shell pass inlet is connected with a washing water pipeline, and the heat exchanger shell pass outlet is connected with a water inlet of the tail gas washing tower through a pipeline.
The heat exchanger adopts a corrugated pipe heat exchanger, and the corrugated pipe heat exchanger is a tube type heat exchanger.
And a gas control valve is arranged on a drying furnace gas pipeline connected with the fluidized bed drying section and a cooling furnace gas pipeline connected with the cooling section, and a gas control valve and a gas pressure gauge are arranged on a gas transmission pipeline connected between the tail gas washing tower and the steam heat pump.
The purpose of the invention can be realized by the following technical scheme.
The improved production method of the heavy soda ash comprises the following steps:
firstly, carrying out hydration reaction on light soda and a sodium carbonate solution serving as raw materials in a hydration reactor to prepare heavy soda, carrying out solid-liquid separation on discharged heavy soda crystal slurry through a centrifugal machine to obtain heavy soda and mother liquor after centrifugation, conveying the heavy soda to a fluidized bed for drying and cooling, exchanging heat between the mother liquor and water, conveying the cooled mother liquor to a mother liquor barrel, and conveying the heated water to a tail gas washing tower to serve as tail gas washing water;
step two, mixing the tail gas at the temperature of 130 +/-3 ℃ in the drying section of the fluidized bed and the tail gas at the temperature of 80 +/-3 ℃ in the cooling section, introducing the mixture into a cyclone separator, separating to obtain heavy soda ash dust and dust-containing air, conveying the heavy soda ash dust to a hydration reactor, mixing the heavy soda ash dust with calcined light soda ash for hydration reaction, and conveying the dust-containing air to a tail gas washing tower;
and step three, the tail gas washing tower re-absorbs the heavy soda ash contained in the dust-containing air, the generated tail gas washing liquid is recycled, part of low-grade steam is generated simultaneously, and the low-grade steam and the high-grade steam enter a steam system together through a steam heat pump.
In the first step, the weight percentage of the light sodium carbonate and the sodium carbonate solution is 1:0.7-1: 1.
In the step one, sodium dodecyl benzene sulfonate is added as a surfactant in the hydration reaction, the addition amount accounts for 0.8 to 1.5 percent of the weight sum of the sodium carbonate solution and the sodium dodecyl benzene sulfonate, the hydration reaction temperature is 95 to 105 ℃, and the hydration reaction time is 5 to 10 min.
And (2) exchanging heat between the mother liquor obtained by the separation of the centrifugal machine and water in the step one, conveying the cooled mother liquor to a mother liquor barrel, conveying the heated water to a tail gas washing tower to be used as tail gas washing water, and adjusting the water flow of a heat exchanger according to the temperature of a hydration reactor.
And in the third step, the tail gas washing liquid in the tail gas washing tower is recycled, and when the concentration of sodium carbonate in the tail gas washing liquid is 270-400 g/L, the tail gas washing liquid is conveyed to a hydration reactor through a mother liquid barrel to carry out hydration reaction.
In the third step, the steam heat pump is selected according to the physical properties of the high-grade steam and the low-grade steam, and the injection coefficient of the steam heat pump is calculated by the following formula:
in the formula uqRepresenting the injection coefficient of the heat pump,
the enthalpy correction coefficient of the mixed steam is obtained,H s、H 0、H qrespectively the enthalpy values of high-grade steam, mixed steam and low-grade steam,φ 1、φ 2、φ 3respectively a working nozzle and a mixing chamberThe velocity coefficients of the diffusion chamber are respectively 0.95, 0.975 and 0.9;ξfor the correction factor, the value was 1.1 in the calculation.
Compared with the prior art, the technical scheme of the invention has the following beneficial effects:
the mother liquor obtained by the separation of a centrifuge and water exchange heat through a heat exchanger, the cooled mother liquor is conveyed to a mother liquor barrel, the heated water is conveyed to a tail gas washing tower to be used as tail gas washing water, so that the problem of overhigh temperature of a hydration reactor is solved, the purposes of regulating and controlling the reaction temperature of the hydration reactor and increasing the washing water temperature are achieved, the normal operation of a heavy soda hydrator is ensured, the consumption of cooling water of the hydration reactor is reduced, and the hydration reaction time is controlled by adjusting the adding amount proportion of light soda and the mother liquor so as to realize large-scale production.
In the invention, dry gas from a fluidized bed is mixed with cooling gas at the temperature of 130 +/-3 ℃, and the mixed furnace gas is subjected to primary purification by a cyclone separator to remove heavy soda ash contained in the mixed furnace gas; the system water and the centrifuge separation mother liquor are subjected to heat exchange and then enter a tail gas washing device to carry out secondary purification on tail gas, and the mother liquor returns to a heavy soda ash system to carry out hydration reaction. The tail gas energy is absorbed by the washing liquid of the tail gas washing tower and converted into low-pressure steam, the low-pressure steam is mixed with the high-pressure steam at the heat pump and enters the steam system, so that the waste of the tail gas energy is avoided and the steam consumption is saved while the furnace gas heavy soda ash is recycled, meanwhile, the self-absorption function of the heat pump reduces the loss of high-grade steam, and the problem of the emission of the heavy soda ash tail gas is solved.
The method treats the heavy soda tail gas, not only can recycle the heavy soda components in the heavy soda tail gas, but also can recycle the heat carried in the heavy soda tail gas, thereby reducing the usage amount of the raw steam, saving energy, reducing emission, effectively improving the environment of a production device area, avoiding the waste of resources and energy, realizing the comprehensive utilization of the heavy soda tail gas, and simultaneously ensuring the continuous and stable operation of a hydration reactor by controlling the usage amounts of cooling water, mother liquor and light soda.
Drawings
FIG. 1 is a schematic diagram of the improved soda ash production process of the present invention.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
As shown in figure 1, the improved heavy soda production device mainly comprises a hydration reactor, a centrifuge, a fluidized bed, a heat exchanger, a cyclone separator, a tail gas washing tower, a mother liquor barrel and a steam heat pump.
The device comprises a hydration reactor, a heat exchanger, a mother liquid barrel, a washing water pipeline, a tail gas washing tower, a washing water pipeline, a tail gas washing tower, a fluidized bed inlet, a heat exchanger tube side inlet, a washing water pipeline, a tail gas washing tower, a washing water pipeline, a washing water inlet, a washing water outlet, a washing water inlet, a washing water outlet, a washing water inlet, a washing water outlet, a washing water inlet, a washing tank, a. The heat exchanger adopts a corrugated pipe heat exchanger, and the corrugated pipe heat exchanger is a shell and tube heat exchanger.
The fluidized bed drying section is connected with a drying furnace gas pipeline, the cooling section is connected with a cooling furnace gas pipeline, and gas quantity control valves are arranged on the drying furnace gas pipeline and the cooling furnace gas pipeline. The dry section tail gas export and the cooling section tail gas export of fluidized bed are respectively through two imports of pipeline connection to tee bend, and the tee bend export is through pipeline connection to cyclone feed inlet, cyclone gas outlet passes through pipeline connection tail gas scrubbing tower air inlet, and is provided with the draught fan on this pipeline, cyclone heavy matter soda exports through pipeline connection hydration reactor, and heavy matter soda exports and sets up rotatory discharge valve. The tail gas washing tower circulation liquid discharge port is connected the drain valve import through the circulating pump, two exports of drain valve, one of them is connected to the circulation liquid import of tail gas washing tower, and the inlet of mother's liquid bucket is connected to another, hydration reactor is connected to the liquid outlet of mother's liquid bucket. The steam discharge port of tail gas washing tower passes through the gas-supply line and is connected to steam heat pump, two feed inlets of steam heat pump, one of them steam discharge port of connecting the tail gas washing tower, another connection high pressure steam pipeline, steam heat pump discharge gate passes through pipe connection steam system. And a gas flow control valve and a gas pressure gauge are arranged on a gas transmission pipeline connected between the tail gas washing tower and the steam heat pump.
The improved heavy soda production method comprises the steps of carrying out solid-liquid separation on crystal slurry after hydration reaction, drying and cooling a solid phase, carrying out heat exchange between the liquid phase and tail gas washing water, removing heavy soda dust in tail gas from heavy soda tail gas after drying and cooling through a cyclone separator, removing heavy soda tail gas with dust, reabsorbing heavy soda in furnace gas through a tail gas washing tower, simultaneously converting tail gas energy into low-grade steam energy, and finally enabling the low-grade steam to enter a steam system together with high-grade steam through a heat pump, wherein the method specifically comprises the following steps:
firstly, carrying out hydration reaction on light soda and a sodium carbonate solution serving as raw materials to prepare heavy soda, carrying out solid-liquid separation on discharged heavy soda crystal slurry through a centrifugal machine, centrifuging to obtain heavy soda and mother liquor, wherein the heavy soda contains 3-5% of free water, the heavy soda is sent to a fluidized bed for drying and cooling, the mother liquor exchanges heat with water, the cooled mother liquor is sent to a mother liquor barrel, the heated water is sent to a tail gas washing tower to serve as tail gas washing water, and the water flow of the heat exchanger can be adjusted according to the temperature of a hydration reactor.
Wherein, in the step one, the weight percentage of the light sodium carbonate and the sodium carbonate solution is 1:0.7-1:1, sodium dodecyl benzene sulfonate is added in the hydration reaction as a surfactant, the adding amount accounts for 0.8-1.5% of the weight sum of the sodium carbonate solution and the sodium dodecyl benzene sulfonate, the hydration reaction temperature is 95-105 ℃, and the hydration reaction time is 5-10 min.
And step two, the temperature of tail gas of a drying section of the fluidized bed is 130 +/-3 ℃, the temperature of tail gas of a cooling section is 80 +/-3 ℃, the tail gas of the drying section and the tail gas of the cooling section are equivalently mixed, the steam temperature can reach about 103 ℃, the mixture is introduced into a cyclone separator, heavy soda dust and dust-containing air are obtained through separation, the heavy soda dust is discharged from the cyclone separator through a cyclone discharge valve and is conveyed to a hydration reactor to be mixed with calcined light soda for hydration reaction, and the dust-containing air is conveyed to a tail gas washing tower through a pipeline, so that the first purification of the tail gas is completed.
And step three, the tail gas washing tower re-absorbs the heavy soda ash contained in the dust-containing air, the generated tail gas washing liquid is recycled, part of low-grade steam is generated simultaneously, the low-grade steam is connected with high-grade steam through a steam heat pump, and the low-grade steam and the high-grade steam jointly enter a steam system after self-absorption through the heat pump, so that secondary purification of the tail gas is completed, and the utilization efficiency of the heavy soda ash tail gas is improved. And tail gas washing liquid in the tail gas washing tower is recycled through a circulating pump, the concentration of the tail gas washing liquid is analyzed at regular time, and when the concentration of sodium carbonate in the tail gas washing liquid is 270-400 g/L, the tail gas washing liquid is discharged into a mother liquid barrel and conveyed to a hydration reactor again for hydration reaction.
Wherein, the steam heat pump is selected according to the physical properties of high-grade steam and low-grade steam, and the injection coefficient of the steam heat pump can be calculated by the following formula:
in the formula uqRepresenting the injection coefficient of the heat pump,
the enthalpy correction coefficient of the mixed steam is obtained,H s、H 0、H qrespectively the enthalpy values of high-grade steam, mixed steam and low-grade steam,φ 1、φ 2、φ 3the velocity coefficients of the working nozzle, the mixing chamber and the diffusion chamber are respectively 0.95, 0.975 and 0.9;ξfor the correction factor, the value was 1.1 in the calculation.
Example 1
Adding light soda ash and a sodium carbonate solution into a hydration crystallizer according to the weight percentage of 1:0.8, carrying out water and reaction for 5 minutes at the temperature of 95 ℃, adding sodium dodecyl benzene sulfonate as a surfactant, wherein the adding amount accounts for 0.9 percent of the weight of the sodium carbonate solution and the sodium dodecyl benzene sulfonate, carrying out solid-liquid separation on crystal slurry after the hydration reaction through a centrifugal machine, sending a liquid phase to a heat exchanger for heat exchange, wherein the water content of solid-phase heavy soda ash is 4.0 percent, sending the solid-phase heavy soda ash to a fluidized bed for drying and cooling, equivalently mixing tail gas of a drying section of the fluidized bed at the temperature of 130 +/-3 ℃ and tail gas of a cooling section at the temperature of 80 +/-3 ℃, introducing the mixture into a cyclone separator, carrying out cyclone separation on the tail gas to obtain heavy soda dust and dust-containing air, mixing the heavy soda dust and the calcined light soda for carrying out the hydration reaction again, sending the dust-containing air to a tail gas washing tower to recycle the heavy soda component in the tail gas, and meanwhile, the generated low-grade steam and the high-grade steam enter a steam system together through a steam heat pump, the concentration of sodium carbonate in the circulating mother liquor is detected once every 1h, and when the content of the sodium carbonate is 270g/L-400g/L, the sodium carbonate is sent to a hydration reactor for reaction.
Example 2
Adding light soda ash and a sodium carbonate solution into a hydration crystallizer according to the weight percentage of 1:0.7, carrying out water and reaction for 7 minutes at the temperature of 100 ℃, adding sodium dodecyl benzene sulfonate as a surfactant, wherein the adding amount accounts for 1.1% of the weight of the sodium carbonate solution and the sodium dodecyl benzene sulfonate, carrying out solid-liquid separation on crystal slurry after the hydration reaction through a centrifugal machine, sending a liquid phase to a heat exchanger for heat exchange, wherein the water content of solid-phase heavy soda ash is 3.0%, sending the solid-phase heavy soda ash to a fluidized bed for drying and cooling, equivalently mixing tail gas of a drying section of the fluidized bed at the temperature of 130 +/-3 ℃ with tail gas of a cooling section at the temperature of 80 +/-3 ℃, leading the steam temperature to reach about 103 ℃, introducing the tail gas into a cyclone separator, carrying out cyclone separation on the tail gas to obtain heavy soda dust and dust-containing air, mixing the heavy soda dust with calcined light soda ash for carrying out the hydration reaction again, sending the dust-containing air to a tail gas washing tower to recycle heavy soda components in the tail gas, and meanwhile, the generated low-grade steam and the high-grade steam enter a steam system together through a steam heat pump, the concentration of sodium carbonate in the circulating mother liquor is detected once every 1h, and when the content of the sodium carbonate is 270g/L-400g/L, the sodium carbonate is sent to a hydration reactor for reaction.
Embodiment 3
Adding light soda ash and a sodium carbonate solution into a hydration crystallizer according to the weight percentage of 1:1, carrying out water and reaction for 8 minutes at 102 ℃, adding sodium dodecyl benzene sulfonate as a surfactant, wherein the addition amount of the sodium dodecyl benzene sulfonate accounts for 0.8 percent of the weight of the sodium carbonate solution and the sodium dodecyl benzene sulfonate, carrying out solid-liquid separation on crystal slurry after the hydration reaction through a centrifugal machine, sending a liquid phase to a heat exchanger for heat exchange, wherein the water content of solid-phase heavy soda ash is 5.0 percent, sending the solid-phase heavy soda ash to a fluidized bed for drying and cooling, equivalently mixing tail gas of a drying section of the fluidized bed at 130 +/-3 ℃ and tail gas of a cooling section at 80 +/-3 ℃, leading the steam temperature of the tail gas to reach about 103 ℃, introducing the tail gas into a cyclone separator, carrying out cyclone separation on the tail gas to obtain heavy soda dust and dust-containing air, mixing the heavy soda dust and the calcined light soda ash for carrying out the hydration reaction again, sending the dust-containing air to a tail gas washing tower to recycle the heavy soda component in the tail gas, and meanwhile, the generated low-grade steam and the high-grade steam enter a steam system together through a steam heat pump, the concentration of sodium carbonate in the circulating mother liquor is detected once every 1h, and when the content of the sodium carbonate is 270g/L-400g/L, the sodium carbonate is sent to a hydration reactor for reaction.
Example 4
Adding light soda ash and a sodium carbonate solution into a hydration crystallizer according to the weight percentage of 1:1, carrying out water and reaction for 10 minutes at 105 ℃, adding sodium dodecyl benzene sulfonate as a surfactant, wherein the addition amount of the sodium dodecyl benzene sulfonate accounts for 1.5 percent of the weight of the sodium carbonate solution and the sodium dodecyl benzene sulfonate, carrying out solid-liquid separation on crystal slurry after the hydration reaction through a centrifugal machine, sending a liquid phase to a heat exchanger for heat exchange, wherein the water content of solid-phase heavy soda ash is 4.0 percent, sending the solid-phase heavy soda ash to a fluidized bed for drying and cooling, equivalently mixing tail gas of a drying section of the fluidized bed at 130 +/-3 ℃ and tail gas of a cooling section at 80 +/-3 ℃, introducing the mixture into a cyclone separator, carrying out cyclone separation on the tail gas to obtain heavy soda ash dust and dust-containing air, mixing the heavy soda dust and the calcined light soda ash for carrying out the hydration reaction again, sending the dust-containing air to a tail gas washing tower to recover the heavy soda ash component in the tail gas, and meanwhile, the generated low-grade steam and the high-grade steam enter a steam system together through a steam heat pump, the concentration of sodium carbonate in the circulating mother liquor is detected once every 1h, and when the content of the sodium carbonate is 270g/L-400g/L, the sodium carbonate is sent to a hydration reactor for reaction.
The basic principle, the process flow and the patent advantages of the invention are stated above, the heavy soda component in the heavy soda tail gas is effectively recovered by the process flow of the invention in principle, the heat of the tail gas is recycled, the steam usage amount is reduced, the continuous and stable operation of a hydration reactor is ensured by controlling the usage amounts of cooling water, mother liquor and light soda, and the process has certain practical value for the heavy soda process of combined soda production.
While the present invention has been described in terms of its functions and operations with reference to the accompanying drawings, it is to be understood that the invention is not limited to the precise functions and operations described above, and that the above-described embodiments are illustrative rather than restrictive, and that various changes and modifications may be effected therein by one skilled in the art without departing from the scope or spirit of the invention as defined by the appended claims.
Claims (8)
1. An improved heavy soda production device comprises a hydration reactor, a centrifuge and a fluidized bed, wherein a discharge outlet of the hydration reactor is connected with an inlet of the centrifuge through a pipeline;
the tail gas outlet of the drying section and the tail gas outlet of the cooling section of the fluidized bed are both connected to the feed inlet of a cyclone separator through pipelines, the gas outlet of the cyclone separator is connected with the gas inlet of a tail gas washing tower through a pipeline, the heavy sodium carbonate outlet of the cyclone separator is connected with a hydration reactor through a pipeline, and the hydration reactor is also connected with a light sodium carbonate input pipeline; the tail gas washing tower is characterized in that a circulating liquid outlet of the tail gas washing tower is connected with an inlet of a liquid discharge valve through a circulating pump, one of two outlets of the liquid discharge valve is connected with the circulating liquid inlet of the tail gas washing tower, the other outlet of the two outlets of the liquid discharge valve is connected with a liquid inlet of a mother liquid barrel, and a liquid outlet of the mother liquid barrel is connected with a hydration reactor; a steam outlet of the tail gas washing tower is connected to a steam system through a steam heat pump;
the heat exchanger tube pass outlet is connected with a liquid inlet of the mother liquid barrel through a pipeline, the heat exchanger shell pass inlet is connected with a washing water pipeline, and the heat exchanger shell pass outlet is connected with a water inlet of the tail gas washing tower through a pipeline.
2. The improved soda ash production plant as claimed in claim 1, wherein said heat exchanger is a bellows heat exchanger, and said bellows heat exchanger is a shell and tube heat exchanger.
3. An improved heavy soda ash production device as claimed in claim 1, wherein the drying furnace gas line connected to the drying section of the fluidized bed and the cooling furnace gas line connected to the cooling section are both provided with a gas control valve, and the gas line connected between the tail gas scrubbing tower and the steam heat pump is provided with a gas control valve and a gas pressure gauge.
4. A method for producing soda ash heavy by the improved soda ash heavy production plant of any of the above claims 1 to 3, characterized by comprising the following processes:
firstly, carrying out hydration reaction on light soda and a sodium carbonate solution serving as raw materials in a hydration reactor to prepare heavy soda, carrying out solid-liquid separation on discharged heavy soda crystal slurry through a centrifugal machine to obtain heavy soda and mother liquor after centrifugation, conveying the heavy soda to a fluidized bed for drying and cooling, exchanging heat between the mother liquor and water through a heat exchanger, conveying the cooled mother liquor to a mother liquor barrel, and conveying the heated water to a tail gas washing tower to serve as tail gas washing water;
step two, mixing the tail gas at the temperature of 130 +/-3 ℃ in the drying section of the fluidized bed and the tail gas at the temperature of 80 +/-3 ℃ in the cooling section, introducing the mixture into a cyclone separator, separating to obtain heavy soda ash dust and dust-containing air, conveying the heavy soda ash dust to a hydration reactor, mixing the heavy soda ash dust with calcined light soda ash for hydration reaction, and conveying the dust-containing air to a tail gas washing tower;
thirdly, the tail gas washing tower absorbs the heavy soda ash contained in the dust-containing air again, the generated tail gas washing liquid is recycled, meanwhile, part of low-grade steam is generated, and the low-grade steam and the high-grade steam enter a steam system together through a steam heat pump; wherein, when the concentration of sodium carbonate in the tail gas washing solution is 270g/L-400g/L, the tail gas washing solution is conveyed to a hydration reactor through a mother solution barrel to carry out hydration reaction.
5. The improved soda ash production device for producing soda ash with heavy weight as claimed in claim 4, wherein the weight percentage of the light soda ash and the sodium carbonate solution in the first step is 1:0.7-1: 1.
6. The improved production method of soda ash with heavy weight as claimed in claim 4, wherein sodium dodecylbenzene sulfonate is added as surfactant in the first hydration reaction, the addition amount is 0.8% -1.5% of the sum of the weight of sodium carbonate solution and sodium dodecylbenzene sulfonate, the hydration reaction temperature is 95-105 ℃, and the hydration reaction time is 5-10 min.
7. The improved production method of soda ash with heavy weight by the soda ash production device according to claim 4, characterized in that the mother liquor obtained by the separation by the centrifuge in the step one exchanges heat with water by the heat exchanger, the mother liquor after temperature reduction is conveyed to the mother liquor barrel, the water after temperature increase is conveyed to the tail gas washing tower as tail gas washing water, and the water flow rate of the heat exchanger is adjusted according to the temperature of the hydration reactor.
8. The improved soda ash production plant for producing soda ash according to claim 4, wherein the steam heat pump in step three is selected according to the physical properties of the high-grade steam and the low-grade steam, and the injection coefficient of the steam heat pump is calculated according to the following formula:
in the formula uqRepresenting heat pump injection coefficient， 
Is prepared by mixing and steamingThe vapor enthalpy value correction coefficient is obtained by the following steps,H s、H 0、H qrespectively the enthalpy values of high-grade steam, mixed steam and low-grade steam,φ 1、φ 2、φ 3the velocity coefficients of the working nozzle, the mixing chamber and the diffusion chamber are respectively 0.95, 0.975 and 0.9;ξfor the correction factor, the value was 1.1 in the calculation.
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Citations (5)
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