WO2022166209A1 - Combined apparatus for producing heavy soda ash by utilizing co2 concentrated gas for ammonium chloride drying and carbonation - Google Patents

Combined apparatus for producing heavy soda ash by utilizing co2 concentrated gas for ammonium chloride drying and carbonation Download PDF

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Publication number
WO2022166209A1
WO2022166209A1 PCT/CN2021/118219 CN2021118219W WO2022166209A1 WO 2022166209 A1 WO2022166209 A1 WO 2022166209A1 CN 2021118219 W CN2021118219 W CN 2021118219W WO 2022166209 A1 WO2022166209 A1 WO 2022166209A1
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Prior art keywords
ammonium chloride
gas
ammonia
washing
dryer
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PCT/CN2021/118219
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French (fr)
Chinese (zh)
Inventor
李黎峰
胡斌
胡书亚
张沫
李相福
方华东
陈学峰
李林
冯青天
孔维斌
常佳伟
孙颖
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中国天辰工程有限公司
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Publication of WO2022166209A1 publication Critical patent/WO2022166209A1/en

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/16—Halides of ammonium
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/06—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour flowing through the materials or objects to be dried

Definitions

  • the utility model relates to the field of chemical production and manufacturing, in particular to a combined device for drying ammonium chloride and carbonizing heavy alkali by utilizing CO2 concentrated gas.
  • the soda ash industry is not only a basic chemical raw material, but also a bulk product that is directly put on the market. In terms of its production scale, it is one of the top ten largest products in the chemical industry.
  • ammonia-alkali method is inseparable from the original salt and limestone. Therefore, it should be close to the production area of salt and limestone; the combined alkali method needs to be matched with a synthetic ammonia plant; the trona processing must have abundant local trona resources, etc.
  • Combined alkali method also known as Hou's alkali method, is characterized in that the raw material ammonia is produced in the form of ammonium chloride product, and two products of soda ash and ammonium chloride are produced at the same time.
  • Ammonia is not only a production medium, but also a kind of main ingreadient. Both ammonia and carbon dioxide come from the synthetic ammonia plant, and the soda ash plant can only be produced jointly with the synthetic ammonia plant, and cannot be set up alone. my country's current soda ash process in the combined alkali process accounts for more than 50%.
  • ammonium chloride needs to be obtained by drying wet ammonium chloride.
  • the wet ammonium chloride from the centrifuge is sent to the fluidized bed through a belt conveyor, and heated, dried and cooled by using hot air as a fluidizing medium and steam.
  • this process has the following problems:
  • the belt conveyor used in this process is an air-to-air equipment, and the free ammonia in the wet ammonium chloride is easily volatilized, causing environmental pollution and harsh operating environment.
  • the traditional ammonium chloride drying process is open drying, that is, the tail gas at the top of the fluidized bed needs to be evacuated by dry dust removal by a bag filter or wet dust removal by a spray tower. Due to the existence of ammonium chloride, the discharged high-temperature wet exhaust gas may produce white smoke. As the national environmental emission standards continue to improve, the ammonium chloride drying process for dry dust removal will no longer be applicable.
  • Wet ammonium chloride contains a certain amount of free ammonia, so the dry exhaust gas contains a certain amount of ammonia gas.
  • the wet dedusting and drying ammonium chloride process requires a large amount of water or acid for dedusting and ammonia removal.
  • the maximum shrinkage in the alkali combination process is only 151.15 kg/t alkali, that is, for every 1 ton of ammonium or ammonia produced, the mother liquor only shrinks by about 0.055m3 of water.
  • a large amount of washing water will easily cause the expansion of the alkali mother liquor, the increase of the ammonia steaming load, the difficulty in processing the acid washing waste liquid, and the high cost of the processing technology. And other issues.
  • the utility model provides a combined device for ammonium chloride drying and carbonization to make heavy alkali by utilizing CO2 concentrated gas, which solves the technical problems of serious pollution, high process cost and unstable operation of the ammonium chloride drying device in the prior art. question.
  • an embodiment of the present utility model provides a combined device for ammonium chloride drying and carbonization to produce heavy caustic using CO concentrated gas, including:
  • the heating device is used for heating the CO 2 rich gas to generate the CO 2 fluidizing gas, wherein;
  • a dryer arranged downstream of the heating device the bottom of the dryer is passed into the CO 2 fluidization gas generated by the heating device, and the dryer heats the wet ammonium chloride to the process temperature to generate dry chlorine ammonium, water vapor, ammonia and carbon dioxide, wherein the water vapor, the ammonia and the carbon dioxide are discharged from the top of the dryer with the CO fluidizing gas, the water vapor, the ammonia and the carbon dioxide are discharged from the top of the dryer Ammonia, the carbon dioxide and the CO fluidizing gas form a first fluidizing gas;
  • the fluidizing gas outputted after the gas passes through the dedusting and washing device is the second fluidizing gas, and the second fluidizing gas includes gas CO 2 ;
  • the second fluidized gas outputted by the dust removal and washing device is input to the carbon compression device, and the carbon compression device mixes the second fluidized gas with ammonia brine to generate heavy alkali.
  • the dedusting and washing device includes:
  • the dry dedusting device is used for dedusting the first fluidizing gas to produce solid ammonium chloride
  • a wet scrubbing device is arranged downstream of the dry dust removal device, and the wet scrubbing device is used for step-by-step scrubbing of the first fluidizing gas to produce ammonium chloride washing water and a liquid containing free ammonia in stages.
  • the dry dust removal equipment includes:
  • the wet washing equipment includes:
  • a dechlorination washing tower disposed downstream of the dry dust removal device, the dechlorination washing tower is used for washing the first fluidized gas to generate ammonium chloride washing water;
  • the ammonia removal condenser is arranged downstream of the chlorine removal washing tower, and the ammonia removal condenser is used for washing the first fluidized gas processed by the chlorine removal washing tower to generate a condensate containing free ammonia.
  • the wet washing equipment further includes:
  • the ammonia removal washing tower is arranged downstream of the ammonia removal condenser, and the ammonia removal washing tower is used for washing the first fluidized gas treated by the ammonia removal condenser to generate washing water containing free ammonia.
  • the compression carbonization device includes:
  • a compressor disposed downstream of the dedusting and scrubbing device, the compressor compresses the second fluidizing gas to produce compressed carbon dioxide;
  • a carbonization tower is arranged downstream of the compressor, and the carbonization tower reacts the compressed carbon dioxide with ammonia brine to produce heavy alkali.
  • the combined device for ammonium chloride drying and carbonization to make heavy alkali using CO 2 concentrated gas also includes:
  • a feed mixing device arranged upstream of the dryer, the feed mixing device mixes the wet ammonium chloride filter cake and dry ammonium chloride, produces wet ammonium chloride, and inputs the wet ammonium chloride to the in the dryer.
  • the combined device for drying ammonium chloride and carbonization to make heavy caustic using CO 2 concentrated gas also includes:
  • a discharging device the inlet of the discharging device is connected with the dryer and the dust removal and washing device, and the outlet of the discharging device is connected with the feeding mixing and conveying device;
  • the discharging device processes the dry ammonium chloride produced by the dryer and the solid ammonium chloride produced by the dust removal and washing device to produce dry ammonium chloride.
  • the dryer includes: a fluidized bed with an internal heat exchanger or a tubular airflow dryer.
  • the embodiment of the present utility model provides a combined device for ammonium chloride drying and carbonization to make heavy alkali by using CO2 concentrated gas, the CO2 concentrated gas heated by CO2 concentrated gas is used as fluidizing gas, and the dust removal and washing device is used to
  • the first fluidizing gas produced after the drying of wet ammonium chloride is processed step by step to obtain solid ammonium chloride, ammonium chloride washing water and liquid containing free ammonia, and the ammonium chloride containing washing water produced by classification can be sent to make ammonia water , used for ammonia desulfurization in the thermal power plant supporting the combined alkali plant; it can also be sent to the combined alkali semi-steam ammonia tower or the II process as make-up water.
  • the free ammonia-containing liquid produced by the classification is sent to the combined alkali ammonia distillation tower for evaporation and recovery of ammonia and carbon dioxide. That is, the waste water obtained by the step-by-step treatment of the fluidized gas by the dust-removing and washing device in the present invention is fully utilized, and is not excreted, and there is no need for an additional waste water treatment system to process the chlorine-containing and ammonia-containing waste water. Therefore, namely, The process cost is reduced, and the pollution to the environment is reduced.
  • Fig. 1 shows the structural representation of a kind of combined device that utilizes CO concentrated gas to carry out ammonium chloride drying and carbonization to produce heavy alkali provided by an embodiment of the present utility model
  • FIG. 2 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model
  • FIG. 3 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model
  • FIG. 4 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model
  • FIG. 5 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model
  • FIG. 6 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model
  • Figure 7 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali using CO concentrated gas provided by Comparative Example 1;
  • Figure 8 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by Comparative Example 2;
  • FIG. 9 is a schematic structural diagram of a combined device for drying ammonium chloride and carbonization to produce heavy alkali using CO 2 concentrated gas provided by Comparative Example 3.
  • Ammonia brine H Heavy alkali M; wet ammonium chloride filter cake A; dry ammonium chloride B; solid ammonium chloride C; free ammonia-containing liquid D, free ammonia-containing condensate D1, and free-containing washing water D2 ; Wash water E containing ammonium chloride; CO2 rich gas F; The first fluidizing gas G1; The second fluidizing gas G2.
  • a plurality of means at least two, such as two, three, etc., unless otherwise expressly and specifically defined. All directional indications (such as up, down, left, right, front, back, top, bottom%) in the embodiments of the present invention are only used to explain the relationship between various components under a certain posture (as shown in the accompanying drawings). If the specific posture changes, the directional indication also changes accordingly. Furthermore, the terms “comprising” and “having”, and any variations thereof, are intended to cover non-exclusive inclusion.
  • a process, method, system, product or device comprising a series of steps or units is not limited to the listed steps or units, but optionally also includes unlisted steps or units, or optionally also includes For other steps or units inherent to these processes, methods, products or devices.
  • Fig. 1 shows the structural representation of the combined device of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali provided by an embodiment of the present utility model, as shown in Fig. 1, this utilizes CO2 concentrated gas to carry out ammonium chloride drying Combined plant with carbonization to make soda, including:
  • Heating device 1 a dryer 2 arranged downstream of the heating device 1, one end of the dryer 2 is input with wet ammonium chloride, and the bottom of the dryer 2 is passed into the CO2 fluidizing gas generated by the heating device 1; it is arranged downstream of the dryer 2 The dust removal and washing device; and the carbon compression device 4.
  • Step S101 Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
  • Step S102 Pass the CO fluidized gas heated by the heating device 1 into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process. temperature, producing dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 with CO 2 fluidization gas, water vapor, ammonia, carbon dioxide and CO 2
  • the fluidizing gas forms the first fluidizing gas G1;
  • Step S103 Input the first fluidized gas G1 into the dedusting and washing device 3 for step-by-step treatment to obtain solid ammonium chloride C, ammonium chloride washing water and liquid D containing free ammonia.
  • the output fluidizing gas is the second fluidizing gas G2, and the second fluidizing gas G2 includes gas CO 2 ; wherein, the produced ammonium chloride-containing washing water E can be sent to make ammonia water for use in the thermal power plant that is matched with the combined alkali plant Ammonia desulfurization; it can also be sent to the combined alkali semi-steam ammonia tower or the II process as make-up water.
  • the liquid D containing free ammonia produced by classification is sent to the double alkali ammonia distillation tower for evaporation and recovery of ammonia and carbon dioxide.
  • Step S104 The second fluidizing gas G2 is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
  • the CO2 fluidizing gas ie, the second fluidizing gas G2
  • the CO2 fluidizing gas is compressed and then sent to the carbonization tower to react with ammonia brine H to form heavy alkali (sodium bicarbonate crystallization). Excess CO2 gas can be vented high before the compressor.
  • the embodiment of the present utility model provides a combined device for ammonium chloride drying and carbonization to produce heavy alkali using CO2 concentrated gas, using the CO2 concentrated gas F heated by the CO2 concentrated gas as fluidizing gas, and using a dust removal and washing device to clean wet chlorine
  • the first fluidizing gas G1 produced after drying of ammonium chloride is processed step by step to obtain solid ammonium chloride C, ammonium chloride washing water and liquid D containing free ammonia, and the ammonium chloride containing washing water E produced by classification can be sent to Ammonia water is produced for ammonia desulfurization in the thermal power plant supporting the combined alkali plant; it can also be sent to the combined alkali semi-steamed ammonia tower or the II process as make-up water.
  • the liquid D containing free ammonia produced by classification is sent to the double alkali ammonia distillation tower for evaporation and recovery of ammonia and carbon dioxide. That is, the waste water obtained by the step-by-step treatment of the fluidized gas by the dust-removing and washing device in the present invention is fully utilized, and is not excreted, and there is no need for an additional waste water treatment system to process the chlorine-containing and ammonia-containing waste water. Therefore, namely, The process cost is reduced, and the pollution to the environment is reduced.
  • FIG. 2 shows a combined device for drying ammonium chloride and carbonizing heavy caustic soda using CO2 concentrated gas provided by another embodiment of the present utility model.
  • the dust removal and washing device 3 includes: The dry dust removal equipment 31; and the wet cleaning equipment 32 arranged downstream of the dry dust removal equipment 31.
  • the combined process of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali as shown in Figure 2 is used to carry out the combined process of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali, including the following steps:
  • Step S101 Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
  • Step S102 pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature to produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein, water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 along with CO 2 fluidizing gas, and water vapor, ammonia, carbon dioxide and CO 2 fluidizing gas form the first fluidizing gas gas G1;
  • Step S1031 Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C;
  • Step S1032 Input the first fluidized gas G1 after the dedusting treatment by the dry dedusting equipment 31 into the wet scrubbing equipment 32 for step-by-step washing to produce ammonium chloride washing water and free ammonia-containing liquid D by classification.
  • the fluidizing gas output from the first fluidizing gas G1 after passing through the dust removal and washing device is the second fluidizing gas G2, and the second fluidizing gas G2 includes the gas CO 2 ;
  • Step S104 The second fluidizing gas G2 is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
  • the dry dust removal device 31 may only include a cyclone.
  • the dry dust removal device 31 may also only include a bag filter.
  • the dry dust removal device 31 may include a cyclone separator and a bag filter, wherein the bag filter is arranged downstream of the cyclone.
  • This embodiment further embodies step S103 in Embodiment 1, that is, the specific washing process in which the first fluidized gas G1 is washed step by step in the dedusting and washing device in the embodiment of the present utility model, that is, most of the solids are first removed.
  • Ammonium chloride C then remove ammonium chloride, and then remove free ammonia, so that the fluidization gas can be classified, and the washing water or solid ammonium chloride C obtained by classification can be reused uniformly.
  • FIG. 3 shows a combined device for drying ammonium chloride and carbonizing heavy caustic soda using CO2 concentrated gas provided by another embodiment of the present utility model.
  • the combined device of ammonium chloride drying and carbonization to make heavy alkali carries out the combined process of ammonium chloride drying and carbonization to make heavy alkali using CO2 concentrated gas, including the following steps:
  • Step S101 Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
  • Step S102 pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature to produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein, water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 along with CO 2 fluidizing gas, and water vapor, ammonia, carbon dioxide and CO 2 fluidizing gas form the first fluidizing gas gas G1;
  • Step S1031 Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C;
  • Step S10321 Input the first fluidized gas G1 after the dedusting treatment by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water;
  • Step S10322 Input the first fluidized gas G1 washed by the chlorine removal washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia;
  • Step S10323 The first fluidized gas G1 washed by the ammonia-removing condenser 322 is input into the ammonia-removing washing tower 323 for washing to generate washing water D2 containing free ammonia.
  • the gasification gas G2 includes the gas CO 2 ;
  • Step S104 The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
  • G2 ie, the CO 2 stream gas
  • step S1032 specifically removes ammonium chloride and free ammonia for three times in sequence, and sequentially removes the first fluidized gas G1.
  • the free ammonia and ammonium chloride in the gas G1, and the free ammonia-containing washing water D2 produced can be used as washing water by a debasing filter or other uses.
  • Figure 4 shows a combined device for ammonium chloride drying and carbonization to make heavy alkali by using CO2 rich gas provided by another embodiment of the present utility model. As shown in Figure 4, using CO2 rich gas for drying ammonium chloride and The combined device for carbonization to heavy alkali also includes a feed mixing device 5 arranged upstream of the dryer 2, and the combined device for ammonium chloride drying and carbonization to heavy alkali shown in FIG. Carry out the combined process of ammonium chloride drying and carbonization to make heavy alkali, including the following steps:
  • Step S100 Mix the wet ammonium chloride filter cake A and the dry ammonium chloride B in the feed mixing device 5 to generate wet ammonium chloride. That is, before the wet ammonium chloride is input into the dryer 2 for drying, the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the wet ammonium chloride produced after thorough mixing is dried. Reduces the probability of fluid bed scarring in dryer 2 when being dried in dryer 2.
  • Step S101 Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
  • Step S102 pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature to produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein, water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 along with CO 2 fluidizing gas, and water vapor, ammonia, carbon dioxide and CO 2 fluidizing gas form the first fluidizing gas gas G1;
  • Step S1031 Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C;
  • Step S10321 Input the first fluidized gas G1 after the dedusting treatment by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water;
  • Step S10322 Input the first fluidized gas G1 washed by the chlorine removal washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia;
  • Step S10323 The first fluidizing gas G1 washed by the ammonia-removing condenser 322 is input into the ammonia-removing scrubbing tower 323 for third-stage washing to generate free ammonia-containing washing water D2.
  • the gasification gas G2 includes the gas CO 2 ;
  • Step S104 The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
  • G2 ie, the CO 2 stream gas
  • Example 3 in the embodiment of the present utility model, the use of CO2 concentrated gas to carry out the combined process of ammonium chloride drying and carbonization to make heavy alkali, wet ammonium chloride filter cake A and dry ammonium chloride B are in the feed mixing device 5. Mixing in ammonium chloride yields wet ammonium chloride.
  • step S101 that is, before the wet ammonium chloride is input into the dryer 2 for drying
  • the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the resulting When wet ammonium chloride is dried in dryer 2, the probability of fluid bed scarring in dryer 2 is reduced.
  • the combined device for ammonium chloride drying and carbonization to produce heavy alkali also includes: a discharge device 6, the inlet of the discharge device 6 is connected with the dryer 2 and the dust removal and washing device 3, and the outlet of the discharge device 6 is mixed with the feed Conveyor connection.
  • the combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali as shown in Figure 5 is used to carry out the combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali, including the following steps:
  • Step S100 Mix the wet ammonium chloride filter cake A with a water content of 6% wt and the dry ammonium chloride B returned from the discharge device 6 in the feed mixing device 5 to generate wet ammonium chloride, wherein the dry ammonium chloride B It was conveyed to the feed mixing device 5 at a speed of 13000 Kg/h. That is, before the wet ammonium chloride is input into the dryer 2 for drying, the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the wet ammonium chloride produced after thorough mixing is dried. Reduces the probability of fluid bed scarring in dryer 2 when being dried in dryer 2.
  • Step S101 Input the CO2 rich gas F from the synthetic ammonia plant into the heating device 1 at a speed of 35000Nm 3 /h for heating to 190° C. to generate CO2 fluidizing gas, wherein the pressure of the CO2 rich gas F is 0.1MPaG;
  • Step S102 pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride obtained in step S100 into the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature, Produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 with CO fluidization gas, water vapor, ammonia, carbon dioxide and CO fluidize The gas constitutes the first fluidizing gas G1; wherein the dry ammonium chloride B is transferred to the discharge device 6, and the temperature of the first fluidizing gas G1 at this time is about 80°C;
  • Step S1031 Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C; transfer the solid ammonium chloride C to the discharge device 6; that is, in step S1031, the first fluidized gas Most of the solid ammonium chloride C in gas G1 is removed;
  • Step S10311 The discharge device 6 processes the dry ammonium chloride B produced by the dryer 2 and the solid ammonium chloride C produced by the dry dust removal device 31 to produce dry ammonium chloride B, and transmits part of the dry ammonium chloride B To the feed mixing device 5, in the feed mixing device 5, the wet ammonium chloride filter cake A and the dry ammonium chloride B are thoroughly mixed to produce wet ammonium chloride. Play the role of making full use of dry ammonium chloride B.
  • Step S10321 Input the first fluidized gas G1 that has been dedusted by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water, and the dechlorination washing tower 321 passes through the circulating pump and the circulating cooler.
  • the washing water contains about 3.2kg/h of ammonium chloride, and the discharged washing water is about 63kg/h.
  • the temperature of the first fluidizing gas G1 discharged after passing through the dechlorination washing tower 321 is about 50°C.
  • Step S10322 Input the first fluidized gas G1 washed by the dechlorination washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia, and the discharge rate of the condensate D1 containing free ammonia is 3.2 m 3 /h, the concentration of ammonia is the titer (approximately pure ammonia 137kg/h), the condensate D1 containing free ammonia can be used to recover ammonia through the ammonia distillation tower, and then enter the combined alkali process system as make-up water, and pass through the ammonia removal washing tower.
  • the temperature of the first fluidizing gas G1 after 323 is about 25°C.
  • Step S10323 Input the first fluidized gas G1 washed by the chlorine removal washing tower 321 into the ammonia removal washing tower 323 for washing to generate free ammonia-containing washing water D2, and the generated free ammonia washing water can be deduplicated and filtered. Machine for washing or other use.
  • the second fluidizing gas G2 includes gas CO 2 ;
  • Step S104 The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
  • G2 ie, the CO 2 stream gas
  • the embodiment of the present utility model is provided with a discharge device 6, that is, one more step S10311 is added than the embodiment, that is, the discharge device 6 removes the dry ammonium chloride B produced by the dryer 2 and the dry dust removal equipment 31.
  • the solid ammonium chloride C produced is processed to produce dry ammonium chloride B, and part of the dry ammonium chloride B is transferred to the feed mixing device 5, where the wet ammonium chloride filter cake A and Dry Ammonium Chloride B is mixed well, yielding Wet Ammonium Chloride. Play the role of making full use of dry ammonium chloride B.
  • the pressure of the fluidizing gas is sufficient to meet the needs of drying and closed circulation, and the fluidized bed drying of ammonium chloride requires a large amount of fluidizing gas and a sufficiently large pressure. Therefore, there is no need to set up additional pressurizing devices such as blowers, avoiding the need for When the pressurizing device 7 such as a blower is used, the operation is stopped due to the failure of the blower, which improves the work efficiency.
  • the CO2 rich gas F is the CO2 rich gas F discharged from the synthetic ammonia plant. Since the pressure of the CO2 rich gas F discharged from the synthetic ammonia plant is 0.1 MPa, it has a relatively high pressure, and the pressure of the CO2 rich gas F with this pressure after passing through the heating device 1 is enough to satisfy the drying and closing requirements.
  • the dryer 2 includes: a fluidized bed or a tubular airflow dryer 2 with an internal heat exchanger.
  • the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidizing gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
  • Fig. 6 shows the combined device for drying ammonium chloride and carbonization to make heavy alkali by utilizing CO2 concentrated gas provided by the embodiment of the utility model, including: a feed mixing device 5, a dryer 2 arranged downstream of the feed mixing device 5 , the heating device 1 arranged upstream of the dryer 2, the discharging device 6 and the dry dust removal device 31 arranged downstream of the dryer 2, wherein the discharging device 6 is also arranged downstream of the dry dust removal device 31, and is arranged in the dry dust removal device 31.
  • the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidizing gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower compresses the carbon dioxide and ammonia brine. H reacts to produce dibasic.
  • the combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali as shown in Figure 6 is used to carry out the combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali, including the following steps:
  • Step S100 Mix the wet ammonium chloride filter cake A with a water content of 6% wt and the dry ammonium chloride B returned from the discharge device 6 in the feed mixing device 5 to generate wet ammonium chloride, wherein the dry ammonium chloride B It was conveyed to the feed mixing device 5 at a speed of 13000 Kg/h. That is, before the wet ammonium chloride is input into the dryer 2 for drying, the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the wet ammonium chloride produced after thorough mixing is dried. Reduces the probability of fluid bed scarring in dryer 2 when being dried in dryer 2.
  • Step S101 input the CO2 rich gas F from the synthetic ammonia plant into the heating device 1 at a speed of 35000Nm 3 /h to be heated to 190° C. to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.1MPaG;
  • Step S102 pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride obtained in step S100 into the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature, Produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 with CO fluidization gas, water vapor, ammonia, carbon dioxide and CO fluidize The gas constitutes the first fluidizing gas G1; wherein the dry ammonium chloride B is transferred to the discharge device 6, and the temperature of the first fluidizing gas G1 at this time is about 80°C;
  • Step S1031 Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C; transfer the solid ammonium chloride C to the discharge device 6; that is, in step S1031, the first fluidized gas Most of the solid ammonium chloride C in gas G1 is removed;
  • Step S10311 The discharge device 6 processes the dry ammonium chloride B produced by the dryer 2 and the solid ammonium chloride C produced by the dry dust removal device 31 to produce dry ammonium chloride B, and transmits part of the dry ammonium chloride B To the feed mixing device 5, in the feed mixing device 5, the wet ammonium chloride filter cake A and the dry ammonium chloride B are thoroughly mixed to produce wet ammonium chloride. Play the role of making full use of dry ammonium chloride B.
  • Step S10321 Input the first fluidized gas G1 that has been dedusted by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water, and the dechlorination washing tower 321 passes through the circulating pump and the circulating cooler.
  • the washing water contains about 3.2kg/h of ammonium chloride, and the discharged washing water is about 63kg/h.
  • the temperature of the first fluidizing gas G1 discharged after passing through the dechlorination washing tower 321 is about 50°C.
  • Step S10322 Input the first fluidizing gas G1 washed by the dechlorination washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia, and the discharge rate of the condensate D1 containing free ammonia is 3.2 m 3 /h, the concentration of ammonia is the titer (about 137kg/h of pure ammonia), the condensate D1 containing free ammonia can be used to recover ammonia through the ammonia distillation tower, and then enter the combined alkali process system as make-up water, and pass through the ammonia removal washing tower.
  • the temperature of the first fluidizing gas G1 after 323 is about 25°C.
  • the second fluidizing gas G2 includes gas CO 2 ;
  • Step S104 The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
  • G2 ie, the CO 2 stream gas
  • the second fluidizing gas G2 is input to the compressor after the compression carbonization device, and the compressor compresses the CO2 fluidizing gas (ie, the second fluidizing gas G2) to 0.4MPaG and then sends it to the carbonization tower to react with ammonia brine H to generate Dibasic (crystallized sodium bicarbonate). Excess CO2 gas can be vented at a high point before the compressor.
  • the compressor compresses the CO2 fluidizing gas (ie, the second fluidizing gas G2) to 0.4MPaG and then sends it to the carbonization tower to react with ammonia brine H to generate Dibasic (crystallized sodium bicarbonate). Excess CO2 gas can be vented at a high point before the compressor.
  • the CO2 rich gas F from the synthetic ammonia plant is not used as the fluidizing gas, but the CO2 rich gas F is used to directly compress the carbonization device, and the ammonium chloride is dried in a closed cycle.
  • Fig. 7 shows the structural representation of the combined device of ammonium chloride drying and carbonization to produce heavy alkali in the prior art.
  • the combined device of ammonium chloride drying and carbonization to produce heavy alkali includes:
  • pressurizing device 7 eg blower
  • the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidized gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
  • the wet ammonium chloride filter cake A52000kg/h of water 6%wt from upstream passes through the feed mixing device 5, and enters the dryer 2 after mixing with the returned dry ammonium chloride B 13000kg/h, the thermal cycle from the heating device 1
  • the gas at 190°C is fed into the dryer 2 from the bottom, and the heat exchanger in the dryer 2 is fed with heating steam.
  • the circulating gas discharged from the top of the dryer 2 is about 80°C, and most of the solid ammonium chloride C is removed by the dry dust removal equipment 31. Afterwards, it enters the dechlorination washing tower 32132, and the dechlorination washing tower 321 is circulated and sprayed through a circulating pump and a circulating cooler.
  • the exhaust temperature at the top of the dechlorination washing tower 321 is about 50°C
  • the washing water discharged from the kettle of the chlorine washing washing tower 321 contains about 3.2 kg/h of ammonium chloride
  • the discharged washing water is about 63 kg/h.
  • the circulating gas entering the ammonia removing condenser 322 is cooled and condensed, the temperature of the circulating gas discharged from the ammonia removing condenser 322 is 25°C, the condensate containing free ammonia at the bottom of the ammonia removing condenser 322 is D13.2m3/h, and the ammonia concentration is 50 drops (pure ammonia is about 137kg/h), this part of the condensate can be used as make-up water to enter the combined alkali process system after the ammonia is recovered by the ammonia distillation tower.
  • the ammonia removal washing tower 323 is not provided.
  • the circulating gas 35000Nm3/h discharged from the ammonia removal condenser 322 is pressurized to 0.03MPaG by the blower 7, heated to 190°C by the heating device 14, and then sent to the dryer 22 again.
  • the CO2 concentrated gas F ( ⁇ 0.1MPaG) from the ammonia synthesis plant is directly sent to the compression carbonization device to be compressed to 0.4MPaG and then sent to the carbonization tower to react with the ammonia brine H to generate heavy alkali.
  • Comparative Example 2 The CO2 concentrated gas F from the synthetic ammonia plant is not used as the fluidizing gas, but the CO2 concentrated gas F is used to directly compress the carbonization device.
  • the drying of ammonium chloride is a closed cycle, but the ammonia and chlorine removal of the circulating gas is not carried out. Graded wash.
  • Fig. 8 shows the structural representation of the combined device of ammonium chloride drying and carbonization to produce heavy alkali in the prior art, and the combined device of this ammonium chloride drying and carbonization to heavy alkali includes:
  • pressurizing device 7 eg blower
  • the outlet end of the tower 323 is connected to the input end of the pressurizing device 7; wherein, the dryer 2 includes a fluidized bed with an internal heat exchanger.
  • the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidized gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
  • the wet ammonium chloride filter cake A52000kg/h with a water content of 6%wt from the upstream passes through the feed mixing device 5, and after mixing with the returned dry ammonium chloride B13000kg/h, it enters the dryer 2, and the hot circulating gas from the heating device 1 190°C is added to the dryer 22 from the bottom, and the heat exchanger in the dryer 2 is fed with heating steam.
  • the circulating gas discharged from the top of the dryer 2 is about 80°C.
  • the ammonia removal washing tower 323 After removing most of the solid ammonium chloride C through the dry dust removal equipment 31 , enter the ammonia removal washing tower 323 to remove the residual ammonium chloride and ammonia gas, add 3m3/h of fresh washing water at the top of the ammonia removal washing tower 323, and the washing water at the bottom of the ammonia removal washing tower 323 contains about 3.2 kg/h of ammonium chloride , the ammonia concentration is 24 titers (pure ammonia is about 137kg/h), and the discharged washing water is about 6.2m3/h. Because this part of the washing water contains ammonium chloride, it cannot be effectively used as supplementary water to enter the combined alkali process system.
  • the circulating gas 35000Nm3/h discharged from the ammonia removal washing tower 323 is pressurized to 0.03MPaG by the blower 7, heated to 190°C by the heating device 14, and then sent to the dryer 22 again.
  • the CO2 concentrated gas F ( ⁇ 0.1MPaG) from the ammonia synthesis plant is directly sent to the compression carbonization device to be compressed to 0.4MPaG and then sent to the carbonization tower to react with ammonia brine H to generate heavy alkali.
  • This comparative example 3 does not use the CO2 rich gas F from the synthetic ammonia plant as the fluidizing gas, but uses the CO2 rich gas F to directly compress the carbonization device, and the ammonium chloride drying is the traditional open air drying.
  • Fig. 9 shows the structural representation of the combined device of ammonium chloride drying and carbonization to produce heavy alkali in the prior art, and the combined device of this ammonium chloride drying and carbonization to produce heavy alkali includes:
  • the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidized gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
  • the wet ammonium chloride filter cake A52000kg/h with a water content of 6%wt from the upstream passes through the feed mixing device 5, and enters the dryer 2 after mixing with the returned dry ammonium chloride B13000kg/h, and the fresh air is pressurized by the blower 7 to After 0.025MPaG, it is sent to the heating device 1 and heated to 190 °C, and then added to the dryer 2 from the bottom. At the same time, the heat exchanger in the dryer 2 is fed with heating steam.
  • the circulating gas discharged from the top of the dryer 2 is about 80 °C.
  • the equipment 31 After dry dust removal After the equipment 31 removes most of the solid ammonium chloride C, it enters the ammonia removal washing tower 323 to remove the residual ammonium chloride and ammonia gas.
  • the top of the ammonia removal washing tower 323 is added with 100m3/h of fresh washing water, and the bottom of the ammonia removal washing tower 323 is washed.
  • the water content of ammonium chloride is about 3.2kg/h
  • the ammonia concentration is about 1.4 titers (pure ammonia is about 137kg/h)
  • the discharged washing water is about 103.2m3/h. It is very huge and cannot be effectively used as make-up water to enter the combined alkali process system.
  • the tail gas 35000Nm3/h discharged from the ammonia removal washing tower 32334 is pressurized to 0.001MPaG by the blower 7 and then discharged into the atmosphere.
  • the CO2 rich gas F ( ⁇ 0.1MPaG) from the ammonia synthesis plant is directly sent to the compression carbonization device to be compressed to 0.4MPaG and then sent to the carbonization tower to react with the ammonia brine H to generate heavy alkali.
  • the consumption of fresh water includes the amount of fresh water recovered from wet ammonium chloride filter cake A and the amount of fresh water added for washing;
  • the electricity fee is 0.5 yuan/kWh
  • the fresh water fee is 0.6 yuan/ton
  • the ammonia fee is 3,000 yuan/ton.
  • the annual operating cost represents the sum of the total electricity cost of the pressurizing device 7, such as the blower, and the compressor, the cost of fresh water and the cost of saving ammonia.
  • Example 5 the annual operating cost is the same as that of Comparative Example 1, but there is a blower pressurizing device 7 in Comparative Example 1, while there is no pressurizing device 7 in Example 6, relying entirely on CO2
  • the pressure of concentrated gas F has high stability and avoids shutdown due to blower failure.

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Abstract

Provided a combined apparatus for producing heavy soda ash by utilizing CO2 concentrated gas for ammonium chloride drying and carbonation, which solves the problems of high process costs and severe pollution from an ammonium chloride drying apparatus in existing technology. The combined apparatus comprises: a heating apparatus (1), a drying device (2) arranged downstream of the heating apparatus (1), a dust removal and washing apparatus (3) arranged downstream of the drying device (2), and a carbon compression apparatus (4). The combined apparatus utilizes CO2 concentrated gas as a fluidizing gas, the dust removal and washing apparatus (3) is used to perform stage-by-stage treatment on a first fluidizing gas (G1) produced after wet ammonium chloride is dried, ammonium chloride wash water (D1) and a free ammonia-containing liquid (D2) are obtained, and the ammonium chloride-containing wash water (D1) produced at an isolated stage may be sent to produce ammonia water, which is used in ammonia-based desulfurization of a supporting thermal power plant of a combined soda plant. Wastewater obtained by using the dust removal and washing apparatus (3) to perform stage-by-stage treatment on the fluidizing gas is amply utilized and not discharged, and an additional wastewater treatment system to treat chlorine-containing and ammonia-containing wastewater is unnecessary.

Description

利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置 Utilize CO 2 Combined device for ammonium chloride drying with concentrated gas and carbonization to make heavy caustic soda 技术领域technical field
本实用新型涉及化工生产制造领域，具体涉及利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置。The utility model relates to the field of chemical production and manufacturing, in particular to a combined device for drying ammonium chloride and carbonizing heavy alkali by utilizing CO2 concentrated gas.
背景技术Background technique
纯碱工业就其特点而言，既是基本化工原料，又是直接投放市场的大宗产品，就其生产规模而言，属于化学工业最大的前十位产品之一。目前，各国生产纯碱的主要方法有三种：氨碱法、联碱法、天然碱加工法，这是因为采用的原料和生产方法不同而各据特点，例如氨碱法离不开原盐和石灰石，因此要靠近盐和石灰石产地；联碱法需要与合成氨厂配套；天然碱加工必须当地有丰富的天然碱资源等。In terms of its characteristics, the soda ash industry is not only a basic chemical raw material, but also a bulk product that is directly put on the market. In terms of its production scale, it is one of the top ten largest products in the chemical industry. At present, there are three main methods for producing soda ash in various countries: ammonia-alkali method, combined alkali method, and trona processing method. This is because the raw materials and production methods used are different and have their own characteristics. For example, the ammonia-alkali method is inseparable from the original salt and limestone. Therefore, it should be close to the production area of salt and limestone; the combined alkali method needs to be matched with a synthetic ammonia plant; the trona processing must have abundant local trona resources, etc.
联碱法又称侯氏制碱法，联碱法的特点是原料氨以氯化铵产品的形式产出，同时生产纯碱和氯化铵两种产品，氨不但是生产媒介，更是一种主要原料。其氨及二氧化碳都来源于合成氨装置，纯碱装置只能与合成氨装置联合生产，不能单独设置。我国目前纯碱工艺中联碱法占50％以上。Combined alkali method, also known as Hou's alkali method, is characterized in that the raw material ammonia is produced in the form of ammonium chloride product, and two products of soda ash and ammonium chloride are produced at the same time. Ammonia is not only a production medium, but also a kind of main ingreadient. Both ammonia and carbon dioxide come from the synthetic ammonia plant, and the soda ash plant can only be produced jointly with the synthetic ammonia plant, and cannot be set up alone. my country's current soda ash process in the combined alkali process accounts for more than 50%.
联碱法的产品之一，氯化铵需要由湿氯化铵经干燥处理后得到。传统的干燥工艺离心机出来的湿氯化铵通过皮带输送机送入流化床，并利用热空气作为流化介质和蒸汽进行加热干燥和冷却。目前，此工艺有如下问题：One of the products of the combined alkali method, ammonium chloride needs to be obtained by drying wet ammonium chloride. In the traditional drying process, the wet ammonium chloride from the centrifuge is sent to the fluidized bed through a belt conveyor, and heated, dried and cooled by using hot air as a fluidizing medium and steam. At present, this process has the following problems:
(1)此工艺采用的皮带输送机为对空设备，湿氯化铵中的游离氨易挥发出来，造成环境污染和操作环境恶劣。(1) The belt conveyor used in this process is an air-to-air equipment, and the free ammonia in the wet ammonium chloride is easily volatilized, causing environmental pollution and harsh operating environment.
(2)传统的氯化铵干燥工艺为开式干燥，即流化床顶部尾气需要采用布袋除尘器干法除尘或者喷淋塔湿法除尘后排空。由于氯化铵的存在，排放的高温含湿尾气可能产生白烟，对于国家环境排放标准不断的提高，因此干法除尘的氯化铵干燥工艺将不再适用。湿氯化铵中含有一定的游离氨，因此干燥尾气中含有一定的氨气，湿法除尘干燥氯化铵工艺则需要大量的水或酸进行除尘除氨，联碱过程最大收缩量仅为151.15kg/t碱，即每生产1吨铵或氨，母液仅收缩约0.055m3水，大量的洗水容易造成联碱母液膨胀、蒸氨负荷加大、酸洗废液难以处理、处理工艺费用昂贵等问题。(2) The traditional ammonium chloride drying process is open drying, that is, the tail gas at the top of the fluidized bed needs to be evacuated by dry dust removal by a bag filter or wet dust removal by a spray tower. Due to the existence of ammonium chloride, the discharged high-temperature wet exhaust gas may produce white smoke. As the national environmental emission standards continue to improve, the ammonium chloride drying process for dry dust removal will no longer be applicable. Wet ammonium chloride contains a certain amount of free ammonia, so the dry exhaust gas contains a certain amount of ammonia gas. The wet dedusting and drying ammonium chloride process requires a large amount of water or acid for dedusting and ammonia removal. The maximum shrinkage in the alkali combination process is only 151.15 kg/t alkali, that is, for every 1 ton of ammonium or ammonia produced, the mother liquor only shrinks by about 0.055m3 of water. A large amount of washing water will easily cause the expansion of the alkali mother liquor, the increase of the ammonia steaming load, the difficulty in processing the acid washing waste liquid, and the high cost of the processing technology. And other issues.
因此，传统的氯化铵干燥工艺已经不满足绿色环保、稳定运行的生产要求。Therefore, the traditional ammonium chloride drying process can no longer meet the production requirements of green environmental protection and stable operation.
实用新型内容Utility model content
有鉴于此，本实用新型提供了利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，解决了现有技术中氯化铵干燥装置污染严重、工艺成本高、运行不稳定的技术问题。In view of this, the utility model provides a combined device for ammonium chloride drying and carbonization to make heavy alkali by utilizing CO2 concentrated gas, which solves the technical problems of serious pollution, high process cost and unstable operation of the ammonium chloride drying device in the prior art. question.
为使本实用新型的目的、技术手段和优点更加清楚明白，以下结合附图对本实用新型作进一步详细说明。In order to make the purpose, technical means and advantages of the present utility model more clearly understood, the present utility model will be further described in detail below with reference to the accompanying drawings.
根据本实用新型的一个方面，本实用新型实施例提供了一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，包括： According to one aspect of the present utility model, an embodiment of the present utility model provides a combined device for ammonium chloride drying and carbonization to produce heavy caustic using CO concentrated gas, including:
加热装置，所述加热装置用于将CO 2浓气加热，产生CO 2流化气，其中； a heating device, the heating device is used for heating the CO 2 rich gas to generate the CO 2 fluidizing gas, wherein;
设置在所述加热装置下游的干燥器，所述干燥器的底部通入所述加热装置产生的CO 2流化气，所述干燥器将所述湿氯化铵加热至工艺温度，产生干氯化铵、水蒸气、氨气和二氧化碳，其中，所述水蒸气、所述氨气以及所述二氧化碳随所述CO 2流化气从所述干燥器的顶部排出，所述水蒸气、所述氨气、所述二氧化碳以及所述CO 2流化气组成第一流化气； A dryer arranged downstream of the heating device, the bottom of the dryer is passed into the CO 2 fluidization gas generated by the heating device, and the dryer heats the wet ammonium chloride to the process temperature to generate dry chlorine ammonium, water vapor, ammonia and carbon dioxide, wherein the water vapor, the ammonia and the carbon dioxide are discharged from the top of the dryer with the CO fluidizing gas, the water vapor, the ammonia and the carbon dioxide are discharged from the top of the dryer Ammonia, the carbon dioxide and the CO fluidizing gas form a first fluidizing gas;
设置在所述干燥器下游的除尘洗涤装置，所述除尘洗涤装置将所述第一流化气逐级处理得到固体氯化铵、氯化铵洗水以及含游离氨的液体，所述第一流化气经过所述除尘洗涤装置后输出的流化气为第二流化气，所述第二流化气包括气体CO 2；以及 A dedusting and washing device arranged downstream of the dryer, the dedusting and washing device processes the first fluidized gas step by step to obtain solid ammonium chloride, ammonium chloride washing water and a liquid containing free ammonia, and the first fluidized gas is The fluidizing gas outputted after the gas passes through the dedusting and washing device is the second fluidizing gas, and the second fluidizing gas includes gas CO 2 ; and
碳压缩装置，经所述除尘洗涤装置输出的第二流化气输入至所述碳压缩装置，所述碳压缩装置将所述第二流化气与氨盐水混合，产生重碱。In the carbon compression device, the second fluidized gas outputted by the dust removal and washing device is input to the carbon compression device, and the carbon compression device mixes the second fluidized gas with ammonia brine to generate heavy alkali.
在本实用新型一实施例中，所述除尘洗涤装置包括：In an embodiment of the present utility model, the dedusting and washing device includes:
设置在所述干燥器下游的干式除尘设备，所述干式除尘设备用于对所述第一流化气进行除尘，产生固体氯化铵；以及a dry dedusting device disposed downstream of the dryer, the dry dedusting device is used for dedusting the first fluidizing gas to produce solid ammonium chloride; and
设置在所述干式除尘设备下游的湿式洗涤设备，所述湿式洗涤设备用于对所述第一流化气进行逐级洗涤，分级产生氯化铵洗水以及含游离氨的液体。A wet scrubbing device is arranged downstream of the dry dust removal device, and the wet scrubbing device is used for step-by-step scrubbing of the first fluidizing gas to produce ammonium chloride washing water and a liquid containing free ammonia in stages.
在本实用新型一实施例中，所述干式除尘设备包括：In an embodiment of the present utility model, the dry dust removal equipment includes:
旋风分离器；和/或cyclones; and/or
布袋除尘器。Bag filter.
在本实用新型一实施例中，所述湿式洗涤设备包括：In an embodiment of the present invention, the wet washing equipment includes:
设置在所述干式除尘设备下游的除氯洗涤塔，所述除氯洗涤塔用于对所述第一流化气进行洗涤，产生氯化铵洗水；以及a dechlorination washing tower disposed downstream of the dry dust removal device, the dechlorination washing tower is used for washing the first fluidized gas to generate ammonium chloride washing water; and
设置在所述除氯洗涤塔下游的除氨冷凝器，所述除氨冷凝器用于对经过所述除氯洗涤塔处理后的第一流化气进行洗涤，产生含游离氨的冷凝液。The ammonia removal condenser is arranged downstream of the chlorine removal washing tower, and the ammonia removal condenser is used for washing the first fluidized gas processed by the chlorine removal washing tower to generate a condensate containing free ammonia.
在本实用新型一实施例中，所述湿式洗涤设备还包括：In an embodiment of the present invention, the wet washing equipment further includes:
设置在所述除氨冷凝器下游的除氨洗涤塔，所述除氨洗涤塔用于对经过除氨冷凝器处理后的第一流化气进行洗涤，产生含游离氨的洗水。The ammonia removal washing tower is arranged downstream of the ammonia removal condenser, and the ammonia removal washing tower is used for washing the first fluidized gas treated by the ammonia removal condenser to generate washing water containing free ammonia.
在本实用新型一实施例中，所述压缩碳化装置包括：In an embodiment of the present invention, the compression carbonization device includes:
设置在所述除尘洗涤装置下游的压缩机，所述压缩机将所述第二流化气进行压缩，产生压缩二氧化碳；以及a compressor disposed downstream of the dedusting and scrubbing device, the compressor compresses the second fluidizing gas to produce compressed carbon dioxide; and
设置在所述压缩机下游的碳化塔，所述碳化塔将所述压缩二氧化碳与氨盐水进行反应，产生重碱。A carbonization tower is arranged downstream of the compressor, and the carbonization tower reacts the compressed carbon dioxide with ammonia brine to produce heavy alkali.
在本实用新型一实施例中，利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置还包括： In an embodiment of the present utility model, the combined device for ammonium chloride drying and carbonization to make heavy alkali using CO 2 concentrated gas also includes:
设置在所述干燥器上游的进料混合装置，所述进料混合装置将湿氯化铵滤饼和干氯化铵混合，产生湿氯化铵，并将所述湿氯化铵输入至所述干燥器中。A feed mixing device arranged upstream of the dryer, the feed mixing device mixes the wet ammonium chloride filter cake and dry ammonium chloride, produces wet ammonium chloride, and inputs the wet ammonium chloride to the in the dryer.
在本实用新型一实施例中，利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，还包括： In an embodiment of the present utility model, the combined device for drying ammonium chloride and carbonization to make heavy caustic using CO 2 concentrated gas also includes:
出料装置，所述出料装置的进口与所述干燥器以及所述除尘洗涤装置连接，所述出料装置的出口与所述进料混合输送装置连接；A discharging device, the inlet of the discharging device is connected with the dryer and the dust removal and washing device, and the outlet of the discharging device is connected with the feeding mixing and conveying device;
所述出料装置将所述干燥器产生的干氯化铵以及所述除尘洗涤装置产生的固体氯化铵进行处理，产生干氯化铵。The discharging device processes the dry ammonium chloride produced by the dryer and the solid ammonium chloride produced by the dust removal and washing device to produce dry ammonium chloride.
在本实用新型一实施例中，所述干燥器包括：内置换热器的流化床或者管式气流干燥器。In an embodiment of the present invention, the dryer includes: a fluidized bed with an internal heat exchanger or a tubular airflow dryer.
本实用新型实施例提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，利用CO 2浓气加热后的CO 2浓气作为流化气，利用除尘洗涤装置对湿氯化铵经过干燥后产生的第一流化气进行逐级处理得到固体氯化铵、氯化铵洗水以及含游离氨的液体，而分级产生的含氯化铵洗水可送去制作氨水，用于与联碱厂配套的热电厂氨法脱硫；也可送至联碱半蒸氨塔或者II过程作为补水。分级产生的含游离氨的液体被送去联碱蒸氨塔进行蒸发回收氨和二氧化碳。即本实用新型采用了除尘洗涤装置对流化气进行逐级处理得到的废水得到了充分的利用，并没被排泄出去，也无需要额外的废水处理系统进行处理含氯含氨废水，因此，即降低了工艺成本，又减少了对环境的污染。 The embodiment of the present utility model provides a combined device for ammonium chloride drying and carbonization to make heavy alkali by using CO2 concentrated gas, the CO2 concentrated gas heated by CO2 concentrated gas is used as fluidizing gas, and the dust removal and washing device is used to The first fluidizing gas produced after the drying of wet ammonium chloride is processed step by step to obtain solid ammonium chloride, ammonium chloride washing water and liquid containing free ammonia, and the ammonium chloride containing washing water produced by classification can be sent to make ammonia water , used for ammonia desulfurization in the thermal power plant supporting the combined alkali plant; it can also be sent to the combined alkali semi-steam ammonia tower or the II process as make-up water. The free ammonia-containing liquid produced by the classification is sent to the combined alkali ammonia distillation tower for evaporation and recovery of ammonia and carbon dioxide. That is, the waste water obtained by the step-by-step treatment of the fluidized gas by the dust-removing and washing device in the present invention is fully utilized, and is not excreted, and there is no need for an additional waste water treatment system to process the chlorine-containing and ammonia-containing waste water. Therefore, namely, The process cost is reduced, and the pollution to the environment is reduced.
附图说明Description of drawings
图1所示为本实用新型一实施例提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； Fig. 1 shows the structural representation of a kind of combined device that utilizes CO concentrated gas to carry out ammonium chloride drying and carbonization to produce heavy alkali provided by an embodiment of the present utility model;
图2所示为本实用新型另一实施例提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； 2 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model;
图3所示为本实用新型另一实施例提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； 3 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model;
图4所示为本实用新型另一实施例提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； 4 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model;
图5所示为本实用新型另一实施例提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； 5 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model;
图6所示为本实用新型另一实施例提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； 6 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by another embodiment of the present utility model;
图7所示为对比例1提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； Figure 7 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali using CO concentrated gas provided by Comparative Example 1;
图8所示为对比例2提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图； Figure 8 shows a schematic structural diagram of a combined device for ammonium chloride drying and carbonization to produce heavy alkali by utilizing CO concentrated gas provided by Comparative Example 2;
图9所示为对比例3提供的一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图。 FIG. 9 is a schematic structural diagram of a combined device for drying ammonium chloride and carbonization to produce heavy alkali using CO 2 concentrated gas provided by Comparative Example 3.
附图标记：Reference number:
加热装置1；干燥器2；除尘洗涤装置3：干式除尘设备31、湿式洗涤设备32、、除氯洗涤塔321、除氨冷凝器322、除氨洗涤塔323；碳压缩装置4；进料混合装置5；出料装置6；加压装置7，第一加压装置71，第二加压装置72； Heating device 1; dryer 2; dedusting and washing device 3: dry dedusting equipment 31, wet scrubbing equipment 32, chlorine removal washing tower 321, ammonia removal condenser 322, ammonia removal washing tower 323; carbon compression device 4; feed Mixing device 5; discharging device 6; pressing device 7, first pressing device 71, second pressing device 72;
氨盐水H；重碱M；湿氯化铵滤饼A；干氯化铵B；固体氯化铵C；含游离氨的液体D、含游离氨的冷凝液D1、含游离含的洗水D2；含氯化铵洗水E；CO2浓气F；第一流化气G1；第二流化气G2。Ammonia brine H; heavy alkali M; wet ammonium chloride filter cake A; dry ammonium chloride B; solid ammonium chloride C; free ammonia-containing liquid D, free ammonia-containing condensate D1, and free-containing washing water D2 ; Wash water E containing ammonium chloride; CO2 rich gas F; The first fluidizing gas G1; The second fluidizing gas G2.
具体实施方式Detailed ways
本实用新型的描述中，“多个”的含义是至少两个，例如两个，三个等，除非另有明确具体的限定。本实用新型实施例中所有方向性指示(诸如上、下、左、右、前、后、顶、底……)仅用于解释在某一特定姿态(如附图所示)下各部件之间的相对位置关系、运动情况等，如果该特定姿态发生改变时，则该方向性指示也相应地随之改变。此外，术语“包括”和“具有”以及它们任何变形，意图在于覆盖不排他的包含。例如包含了一系列步骤或单元的过程、方法、系统、产品或设备没有限定于已列出的步骤或单元，而是可选地还包括没有列出的步骤或单元，或可选地还包括对于这些过程、方法、产品或设备固有的其它步骤或单元。In the description of the present invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise expressly and specifically defined. All directional indications (such as up, down, left, right, front, back, top, bottom...) in the embodiments of the present invention are only used to explain the relationship between various components under a certain posture (as shown in the accompanying drawings). If the specific posture changes, the directional indication also changes accordingly. Furthermore, the terms "comprising" and "having", and any variations thereof, are intended to cover non-exclusive inclusion. For example, a process, method, system, product or device comprising a series of steps or units is not limited to the listed steps or units, but optionally also includes unlisted steps or units, or optionally also includes For other steps or units inherent to these processes, methods, products or devices.
另外，在本文中提及“实施例”意味着，结合实施例描述的特定特征、结构或特性可以包含在 本实用新型的至少一个实施例中。在说明书中的各个位置出现该短语并不一定均是指相同的实施例，也不是与其它实施例互斥的独立的或备选的实施例。本领域技术人员显式地和隐式地理解的是，本文所描述的实施例可以与其它实施例相结合。Additionally, reference herein to an "embodiment" means that a particular feature, structure, or characteristic described in connection with the embodiment can be included in at least one embodiment of the present invention. The appearances of the phrase in various places in the specification are not necessarily all referring to the same embodiment, nor a separate or alternative embodiment that is mutually exclusive of other embodiments. It is explicitly and implicitly understood by those skilled in the art that the embodiments described herein may be combined with other embodiments.
下面将结合本实用新型实施例中的附图，对本实用新型实施例中的技术方案进行清楚、完整地描述，显然，所描述的实施例仅是本实用新型一部分实施例，而不是全部的实施例。基于本实用新型中的实施例，本领域普通技术人员在没有作出创造性劳动前提下所获得的所有其他实施例，都属于本实用新型保护的范围。The technical solutions in the embodiments of the present utility model will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present utility model. Obviously, the described embodiments are only a part of the embodiments of the present utility model, rather than all the implementations. example. Based on the embodiments of the present invention, all other embodiments obtained by those of ordinary skill in the art without creative work fall within the protection scope of the present invention.
实施例1：Example 1:
图1所示为本实用新型一实施例提供的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置的结构示意图，如图1所示，该利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，包括：Fig. 1 shows the structural representation of the combined device of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali provided by an embodiment of the present utility model, as shown in Fig. 1, this utilizes CO2 concentrated gas to carry out ammonium chloride drying Combined plant with carbonization to make soda, including:
加热装置1；设置在加热装置1下游的干燥器2，干燥器2的一端输入湿氯化铵，干燥器2的底部通入加热装置1产生的CO 2流化气；设置在干燥器2下游的除尘洗涤装置；以及碳压缩装置4。 Heating device 1; a dryer 2 arranged downstream of the heating device 1, one end of the dryer 2 is input with wet ammonium chloride, and the bottom of the dryer 2 is passed into the CO2 fluidizing gas generated by the heating device 1; it is arranged downstream of the dryer 2 The dust removal and washing device; and the carbon compression device 4.
采用图1所示的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置进行利用CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺，包括如下步骤：The combined process of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali is used as shown in Figure 1 to carry out the combined process of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali, including the following steps:
步骤S101：将CO2浓气F输入至加热装置1进行加热，产生CO 2流化气，其中，CO2浓气F的压强为0.05～0.15MPa； Step S101: Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
步骤S102：将经过加热装置1加热后的CO 2流化气从干燥器2的底部通入干燥器2，将湿氯化铵输入至干燥器2，干燥器2将湿氯化铵加热至工艺温度，产生干氯化铵B、水蒸气、氨气和二氧化碳，其中，水蒸气、氨气以及二氧化碳随CO 2流化气从干燥器2的顶部排出，水蒸气、氨气、二氧化碳以及CO 2流化气组成第一流化气G1； Step S102: Pass the CO fluidized gas heated by the heating device 1 into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process. temperature, producing dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 with CO 2 fluidization gas, water vapor, ammonia, carbon dioxide and CO 2 The fluidizing gas forms the first fluidizing gas G1;
步骤S103：将第一流化气G1输入至除尘洗涤装置3中进行逐级处理得到固体氯化铵C、氯化铵洗水以及含游离氨的液体D，第一流化气G1经过除尘洗涤装置后输出的流化气为第二流化气G2，第二流化气G2包括气体CO 2；其中，产生的含氯化铵洗水E可送去制作氨水，用于与联碱厂配套的热电厂氨法脱硫；也可送至联碱半蒸氨塔或者II过程作为补水。分级产生的含游离氨的液体D被送去联碱蒸氨塔进行蒸发回收氨和二氧化碳。 Step S103: Input the first fluidized gas G1 into the dedusting and washing device 3 for step-by-step treatment to obtain solid ammonium chloride C, ammonium chloride washing water and liquid D containing free ammonia. After the first fluidized gas G1 passes through the dedusting and washing device The output fluidizing gas is the second fluidizing gas G2, and the second fluidizing gas G2 includes gas CO 2 ; wherein, the produced ammonium chloride-containing washing water E can be sent to make ammonia water for use in the thermal power plant that is matched with the combined alkali plant Ammonia desulfurization; it can also be sent to the combined alkali semi-steam ammonia tower or the II process as make-up water. The liquid D containing free ammonia produced by classification is sent to the double alkali ammonia distillation tower for evaporation and recovery of ammonia and carbon dioxide.
步骤S104：将第二流化气G2与氨盐水H在压缩碳化装置中进行混合，产生重碱。Step S104: The second fluidizing gas G2 is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
第二流化气G2被输入至压缩碳化装置后CO 2流化气(即第二流化气G2)被压缩后送入碳化塔与氨盐水H反应生成重碱(碳酸氢钠结晶)。多余的CO 2气可以在压缩机之前高点放空。 After the second fluidizing gas G2 is input to the compressed carbonization device, the CO2 fluidizing gas (ie, the second fluidizing gas G2) is compressed and then sent to the carbonization tower to react with ammonia brine H to form heavy alkali (sodium bicarbonate crystallization). Excess CO2 gas can be vented high before the compressor.
本实用新型实施例提供的一种利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，利 用CO2浓气加热后的CO2浓气F作为流化气，利用除尘洗涤装置对湿氯化铵经过干燥后产生的第一流化气G1进行逐级处理得到固体氯化铵C、氯化铵洗水以及含游离氨的液体D，而分级产生的含氯化铵洗水E可送去制作氨水，用于与联碱厂配套的热电厂氨法脱硫；也可送至联碱半蒸氨塔或者II过程作为补水。分级产生的含游离氨的液体D被送去联碱蒸氨塔进行蒸发回收氨和二氧化碳。即本实用新型采用了除尘洗涤装置对流化气进行逐级处理得到的废水得到了充分的利用，并没被排泄出去，也无需要额外的废水处理系统进行处理含氯含氨废水，因此，即降低了工艺成本，又减少了对环境的污染。The embodiment of the present utility model provides a combined device for ammonium chloride drying and carbonization to produce heavy alkali using CO2 concentrated gas, using the CO2 concentrated gas F heated by the CO2 concentrated gas as fluidizing gas, and using a dust removal and washing device to clean wet chlorine The first fluidizing gas G1 produced after drying of ammonium chloride is processed step by step to obtain solid ammonium chloride C, ammonium chloride washing water and liquid D containing free ammonia, and the ammonium chloride containing washing water E produced by classification can be sent to Ammonia water is produced for ammonia desulfurization in the thermal power plant supporting the combined alkali plant; it can also be sent to the combined alkali semi-steamed ammonia tower or the II process as make-up water. The liquid D containing free ammonia produced by classification is sent to the double alkali ammonia distillation tower for evaporation and recovery of ammonia and carbon dioxide. That is, the waste water obtained by the step-by-step treatment of the fluidized gas by the dust-removing and washing device in the present invention is fully utilized, and is not excreted, and there is no need for an additional waste water treatment system to process the chlorine-containing and ammonia-containing waste water. Therefore, namely, The process cost is reduced, and the pollution to the environment is reduced.
实施例2：Example 2:
图2所示为本实用新型另一实施例提供的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，如图2所示，除尘洗涤装置3包括：设置在干燥器2下游的干式除尘设备31；以及设置在干式除尘设备31下游的湿式洗涤设备32。采用图2所示的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置进行利用CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺，包括以下步骤：FIG. 2 shows a combined device for drying ammonium chloride and carbonizing heavy caustic soda using CO2 concentrated gas provided by another embodiment of the present utility model. As shown in FIG. 2 , the dust removal and washing device 3 includes: The dry dust removal equipment 31; and the wet cleaning equipment 32 arranged downstream of the dry dust removal equipment 31. The combined process of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali as shown in Figure 2 is used to carry out the combined process of utilizing CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali, including the following steps:
步骤S101：将CO2浓气F输入至加热装置1进行加热，产生CO 2流化气，其中，CO2浓气F的压强为0.05～0.15MPa； Step S101: Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
步骤S102：将CO 2流化气从干燥器2的底部通入干燥器2，将湿氯化铵输入至干燥器2，干燥器2将湿氯化铵加热至工艺温度，产生干氯化铵B、水蒸气、氨气和二氧化碳，其中，水蒸气、氨气以及二氧化碳随CO 2流化气从干燥器2的顶部排出，水蒸气、氨气、二氧化碳以及CO 2流化气组成第一流化气G1； Step S102: pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature to produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein, water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 along with CO 2 fluidizing gas, and water vapor, ammonia, carbon dioxide and CO 2 fluidizing gas form the first fluidizing gas gas G1;
步骤S1031：将第一流化气G1输入至干式除尘设备31进行除尘处理，产生固体氯化铵C；Step S1031: Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C;
步骤S1032：将经过干式除尘设备31进行除尘处理后的第一流化气G1输入至湿式洗涤设备32中进行逐级洗涤，分级产生氯化铵洗水以及含游离氨的液体D。Step S1032: Input the first fluidized gas G1 after the dedusting treatment by the dry dedusting equipment 31 into the wet scrubbing equipment 32 for step-by-step washing to produce ammonium chloride washing water and free ammonia-containing liquid D by classification.
经过步骤S1031以及步骤S1032对第一流化气G1进行分级处理后，即第一流化气G1经过除尘洗涤装置后输出的流化气为第二流化气G2，第二流化气G2包括气体CO 2； After the first fluidizing gas G1 is classified in steps S1031 and S1032, that is, the fluidizing gas output from the first fluidizing gas G1 after passing through the dust removal and washing device is the second fluidizing gas G2, and the second fluidizing gas G2 includes the gas CO 2 ;
步骤S104：将第二流化气G2与氨盐水H在压缩碳化装置中进行混合，产生重碱。Step S104: The second fluidizing gas G2 is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
可选的，干式除尘设备31可以仅包括旋风分离器。干式除尘设备31还可以仅包括布袋除尘器。干式除尘设备31可以包括旋风分离器以及布袋除尘器，其中，布袋除尘器设置在旋风分离器的下游。Optionally, the dry dust removal device 31 may only include a cyclone. The dry dust removal device 31 may also only include a bag filter. The dry dust removal device 31 may include a cyclone separator and a bag filter, wherein the bag filter is arranged downstream of the cyclone.
本实施例对实施例1中的步骤S103进行了进一步的具体化，即本实用新型实施例将第一流化气G1在除尘洗涤装置被逐级洗涤的具体洗涤过程，即先除去大部分的固体氯化铵C、然后再除去氯化铵、然后再去除游离氨，从而能够对流化气进行分级处理，分级处理得到的洗水或者固 体氯化铵C均一一得到再利用。This embodiment further embodies step S103 in Embodiment 1, that is, the specific washing process in which the first fluidized gas G1 is washed step by step in the dedusting and washing device in the embodiment of the present utility model, that is, most of the solids are first removed. Ammonium chloride C, then remove ammonium chloride, and then remove free ammonia, so that the fluidization gas can be classified, and the washing water or solid ammonium chloride C obtained by classification can be reused uniformly.
实施例3：Example 3:
图3所示为本实用新型另一实施例提供的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，如图3所示，湿式洗涤设备32包括设置在干式除尘设备31下游的除氯洗涤塔321、设置在除氯洗涤塔321下游的除氨冷凝器322以及设置在除氨冷凝器322下游的除氨洗涤塔323；采用图5所示的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置进行利用CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺，包括以下步骤：FIG. 3 shows a combined device for drying ammonium chloride and carbonizing heavy caustic soda using CO2 concentrated gas provided by another embodiment of the present utility model. As shown in FIG. The downstream dechlorination washing tower 321, the ammonia removal condenser 322 arranged at the downstream of the dechlorination washing tower 321, and the ammonia removal washing tower 323 arranged at the downstream of the ammonia removal condenser 322; The combined device of ammonium chloride drying and carbonization to make heavy alkali carries out the combined process of ammonium chloride drying and carbonization to make heavy alkali using CO2 concentrated gas, including the following steps:
步骤S101：将CO2浓气F输入至加热装置1进行加热，产生CO 2流化气，其中，CO2浓气F的压强为0.05～0.15MPa； Step S101: Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
步骤S102：将CO 2流化气从干燥器2的底部通入干燥器2，将湿氯化铵输入至干燥器2，干燥器2将湿氯化铵加热至工艺温度，产生干氯化铵B、水蒸气、氨气和二氧化碳，其中，水蒸气、氨气以及二氧化碳随CO 2流化气从干燥器2的顶部排出，水蒸气、氨气、二氧化碳以及CO 2流化气组成第一流化气G1； Step S102: pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature to produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein, water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 along with CO 2 fluidizing gas, and water vapor, ammonia, carbon dioxide and CO 2 fluidizing gas form the first fluidizing gas gas G1;
步骤S1031：将第一流化气G1输入至干式除尘设备31进行除尘处理，产生固体氯化铵C；Step S1031: Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C;
步骤S10321：将经过干式除尘设备31进行除尘处理后的第一流化气G1输入至除氯洗涤塔321进行洗涤，产生氯化铵洗水；Step S10321: Input the first fluidized gas G1 after the dedusting treatment by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water;
步骤S10322：将经过除氯洗涤塔321洗涤后的第一流化气G1输入至除氨冷凝器322中进行洗涤，产生含游离氨的冷凝液D1；Step S10322: Input the first fluidized gas G1 washed by the chlorine removal washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia;
步骤S10323：将经过除氨冷凝器322洗涤后的第一流化气G1输入至除氨洗涤塔323进行洗涤，产生含游离氨的洗水D2。Step S10323: The first fluidized gas G1 washed by the ammonia-removing condenser 322 is input into the ammonia-removing washing tower 323 for washing to generate washing water D2 containing free ammonia.
经过步骤S1031、步骤S10321、步骤S10322以及步骤S10323对第一流化气G1进行分级处理后，即第一流化气G1经过除尘洗涤装置后输出的流化气为第二流化气G2，第二流化气G2包括气体CO 2； After steps S1031, S10321, S10322 and S10323 are used to classify the first fluidizing gas G1, that is, the fluidizing gas output from the first fluidizing gas G1 after passing through the dust removal and washing device is the second fluidizing gas G2. The gasification gas G2 includes the gas CO 2 ;
步骤S104：将第二流化气G2(即CO 2流气)与氨盐水H在压缩碳化装置中进行混合，产生重碱。 Step S104: The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
相对于实施例2，本实用新型实施例在对第一流化气G1进行处理时，湿式洗涤的步骤，即步骤S1032具体分别依次除氯化铵、除游离氨的三次洗涤，依次除去第一流化气G1中的游离氨以及氯化铵，得到的含游离氨的洗水D2产生的游离氨的洗水可以去重碱过滤机做洗水或者其他使用。Compared with Example 2, when the first fluidized gas G1 is treated in the embodiment of the present invention, the step of wet scrubbing, that is, step S1032, specifically removes ammonium chloride and free ammonia for three times in sequence, and sequentially removes the first fluidized gas G1. The free ammonia and ammonium chloride in the gas G1, and the free ammonia-containing washing water D2 produced can be used as washing water by a debasing filter or other uses.
实施例4：Example 4:
由于在步骤S102中的湿氯化铵是湿氯化铵与部分干氯化铵B混合而成的，但是在干燥器2 干燥时，降低流化床进料含水量，造成流化床结疤严重，需要经常清洗。因此，图4所示为本实用新型另一实施例提供的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，如图4所示，利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置还包括设置在干燥器2上游的进料混合装置5，采用图4所示的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置进行利用CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺，包括以下步骤：Since the wet ammonium chloride in step S102 is formed by mixing wet ammonium chloride and part of dry ammonium chloride B, when the dryer 2 is drying, the water content of the fluidized bed feed is reduced, resulting in the formation of fluidized bed scarring Severe and requires frequent cleaning. Therefore, Figure 4 shows a combined device for ammonium chloride drying and carbonization to make heavy alkali by using CO2 rich gas provided by another embodiment of the present utility model. As shown in Figure 4, using CO2 rich gas for drying ammonium chloride and The combined device for carbonization to heavy alkali also includes a feed mixing device 5 arranged upstream of the dryer 2, and the combined device for ammonium chloride drying and carbonization to heavy alkali shown in FIG. Carry out the combined process of ammonium chloride drying and carbonization to make heavy alkali, including the following steps:
步骤S100：将湿氯化铵滤饼A和干氯化铵B在进料混合装置5中进行混合，产生湿氯化铵。即在湿氯化铵输入干燥器2进行干燥之前，将湿氯化铵滤饼A和干氯化铵B在进料混合装置5中进行混合，当充分混合后产生的湿氯化铵在干燥器2中被干燥时，降低干燥器2中的流化床结疤的概率。Step S100: Mix the wet ammonium chloride filter cake A and the dry ammonium chloride B in the feed mixing device 5 to generate wet ammonium chloride. That is, before the wet ammonium chloride is input into the dryer 2 for drying, the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the wet ammonium chloride produced after thorough mixing is dried. Reduces the probability of fluid bed scarring in dryer 2 when being dried in dryer 2.
步骤S101：将CO2浓气F输入至加热装置1进行加热，产生CO 2流化气，其中，CO2浓气F的压强为0.05～0.15MPa； Step S101: Input the CO2 rich gas F into the heating device 1 for heating to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.05-0.15MPa;
步骤S102：将CO 2流化气从干燥器2的底部通入干燥器2，将湿氯化铵输入至干燥器2，干燥器2将湿氯化铵加热至工艺温度，产生干氯化铵B、水蒸气、氨气和二氧化碳，其中，水蒸气、氨气以及二氧化碳随CO 2流化气从干燥器2的顶部排出，水蒸气、氨气、二氧化碳以及CO 2流化气组成第一流化气G1； Step S102: pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride to the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature to produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein, water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 along with CO 2 fluidizing gas, and water vapor, ammonia, carbon dioxide and CO 2 fluidizing gas form the first fluidizing gas gas G1;
步骤S1031：将第一流化气G1输入至干式除尘设备31进行除尘处理，产生固体氯化铵C；Step S1031: Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C;
步骤S10321：将经过干式除尘设备31进行除尘处理后的第一流化气G1输入至除氯洗涤塔321进行洗涤，产生氯化铵洗水；Step S10321: Input the first fluidized gas G1 after the dedusting treatment by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water;
步骤S10322：将经过除氯洗涤塔321洗涤后的第一流化气G1输入至除氨冷凝器322中进行洗涤，产生含游离氨的冷凝液D1；Step S10322: Input the first fluidized gas G1 washed by the chlorine removal washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia;
步骤S10323：将经过除氨冷凝器322洗涤后的第一流化气G1输入至除氨洗涤塔323进行第三级洗涤，产生含游离氨的洗水D2。Step S10323: The first fluidizing gas G1 washed by the ammonia-removing condenser 322 is input into the ammonia-removing scrubbing tower 323 for third-stage washing to generate free ammonia-containing washing water D2.
经过步骤S1031、步骤S10321、步骤S10322以及步骤S10323对第一流化气G1进行分级处理后，即第一流化气G1经过除尘洗涤装置后输出的流化气为第二流化气G2，第二流化气G2包括气体CO 2； After steps S1031, S10321, S10322 and S10323 are used to classify the first fluidizing gas G1, that is, the fluidizing gas output from the first fluidizing gas G1 after passing through the dust removal and washing device is the second fluidizing gas G2. The gasification gas G2 includes the gas CO 2 ;
步骤S104：将第二流化气G2(即CO 2流气)与氨盐水H在压缩碳化装置中进行混合，产生重碱。 Step S104: The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
相对于实施例3，本实用新型实施例的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺，将湿氯化铵滤饼A和干氯化铵B在进料混合装置5中进行混合，产生湿氯化铵。在步骤S101之前(即在湿氯化铵输入干燥器2进行干燥之前)，将湿氯化铵滤饼A和干氯化铵B在进料混合装置5中进行混合，当充分混合后产生的湿氯化铵在干燥器2中被干燥时，降低干燥器2 中的流化床结疤的概率。With respect to Example 3, in the embodiment of the present utility model, the use of CO2 concentrated gas to carry out the combined process of ammonium chloride drying and carbonization to make heavy alkali, wet ammonium chloride filter cake A and dry ammonium chloride B are in the feed mixing device 5. Mixing in ammonium chloride yields wet ammonium chloride. Before step S101 (that is, before the wet ammonium chloride is input into the dryer 2 for drying), the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the resulting When wet ammonium chloride is dried in dryer 2, the probability of fluid bed scarring in dryer 2 is reduced.
实施例5：Example 5:
由于在步骤S100中，需要将将湿氯化铵滤饼A和干氯化铵B在进料混合装置5中进行混合，因此，如图5所示，本实用新型实施例中的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，还包括：出料装置6，出料装置6的进口与干燥器2以及除尘洗涤装置3连接，出料装置6的出口与进料混合输送装置连接。采用图5所示的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置来进行利用CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺，包括如下步骤：Since in step S100, the wet ammonium chloride filter cake A and the dry ammonium chloride B need to be mixed in the feed mixing device 5, therefore, as shown in FIG. The combined device for ammonium chloride drying and carbonization to produce heavy alkali also includes: a discharge device 6, the inlet of the discharge device 6 is connected with the dryer 2 and the dust removal and washing device 3, and the outlet of the discharge device 6 is mixed with the feed Conveyor connection. The combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali as shown in Figure 5 is used to carry out the combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali, including the following steps:
步骤S100：将含水6％wt的湿氯化铵滤饼A和出料装置6返回的干氯化铵B在进料混合装置5中进行混合，产生湿氯化铵，其中干氯化铵B以13000Kg/h的速度被输送至进料混合装置5中。即在湿氯化铵输入干燥器2进行干燥之前，将湿氯化铵滤饼A和干氯化铵B在进料混合装置5中进行混合，当充分混合后产生的湿氯化铵在干燥器2中被干燥时，降低干燥器2中的流化床结疤的概率。Step S100: Mix the wet ammonium chloride filter cake A with a water content of 6% wt and the dry ammonium chloride B returned from the discharge device 6 in the feed mixing device 5 to generate wet ammonium chloride, wherein the dry ammonium chloride B It was conveyed to the feed mixing device 5 at a speed of 13000 Kg/h. That is, before the wet ammonium chloride is input into the dryer 2 for drying, the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the wet ammonium chloride produced after thorough mixing is dried. Reduces the probability of fluid bed scarring in dryer 2 when being dried in dryer 2.
步骤S101：将合成氨厂来的CO2浓气F以35000Nm 3/h的速度输入至加热装置1进行加热至190℃，产生CO 2流化气，其中，CO2浓气F的压强为0.1MPaG； Step S101: Input the CO2 rich gas F from the synthetic ammonia plant into the heating device 1 at a speed of 35000Nm 3 /h for heating to 190° C. to generate CO2 fluidizing gas, wherein the pressure of the CO2 rich gas F is 0.1MPaG;
步骤S102：将CO 2流化气从干燥器2的底部通入干燥器2，将步骤S100中得到的湿氯化铵输入至干燥器2，干燥器2将湿氯化铵加热至工艺温度，产生干氯化铵B、水蒸气、氨气和二氧化碳，其中，水蒸气、氨气以及二氧化碳随CO 2流化气从干燥器2的顶部排出，水蒸气、氨气、二氧化碳以及CO 2流化气组成第一流化气G1；其中干氯化铵B被传输至出料装置6中，第一流化气G1此时的温度约为80℃； Step S102: pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride obtained in step S100 into the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature, Produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 with CO fluidization gas, water vapor, ammonia, carbon dioxide and CO fluidize The gas constitutes the first fluidizing gas G1; wherein the dry ammonium chloride B is transferred to the discharge device 6, and the temperature of the first fluidizing gas G1 at this time is about 80°C;
步骤S1031：将第一流化气G1输入至干式除尘设备31进行除尘处理，产生固体氯化铵C；将固体氯化铵C传输至出料装置6中；即在步骤S1031中，第一流化气G1中的固体氯化铵C大部分被去除；Step S1031: Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C; transfer the solid ammonium chloride C to the discharge device 6; that is, in step S1031, the first fluidized gas Most of the solid ammonium chloride C in gas G1 is removed;
步骤S10311：出料装置6将干燥器2产生的干氯化铵B以及干式除尘设备31产生的固体氯化铵C进行处理，产生干氯化铵B，并将部分干氯化铵B传输至进料混合装置5中，在进料混合装置5中，湿氯化铵滤饼A和干氯化铵B被充分混合，产生湿氯化铵。起到将干氯化铵B充分利用的作用。Step S10311: The discharge device 6 processes the dry ammonium chloride B produced by the dryer 2 and the solid ammonium chloride C produced by the dry dust removal device 31 to produce dry ammonium chloride B, and transmits part of the dry ammonium chloride B To the feed mixing device 5, in the feed mixing device 5, the wet ammonium chloride filter cake A and the dry ammonium chloride B are thoroughly mixed to produce wet ammonium chloride. Play the role of making full use of dry ammonium chloride B.
步骤S10321：将经过干式除尘设备31进行除尘处理后的第一流化气G1输入至除氯洗涤塔321中进行洗涤，产生氯化铵洗水，除氯洗涤塔321通过循环泵、循环冷却器做循环喷淋，对第一流化气G1中的氯化铵进行洗涤，产生氯化铵洗水，洗水含氯化铵约为3.2kg/h，排出的洗水约为63kg/h。此时，经过除氯洗涤塔321后排出的第一流化气G1的温度约为50℃。Step S10321: Input the first fluidized gas G1 that has been dedusted by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water, and the dechlorination washing tower 321 passes through the circulating pump and the circulating cooler. Do circulating spray to wash the ammonium chloride in the first fluidizing gas G1 to produce ammonium chloride washing water, the washing water contains about 3.2kg/h of ammonium chloride, and the discharged washing water is about 63kg/h. At this time, the temperature of the first fluidizing gas G1 discharged after passing through the dechlorination washing tower 321 is about 50°C.
步骤S10322：将经过除氯洗涤塔321洗涤后的第一流化气G1输入至除氨冷凝器322中进行洗涤，产生含游离氨的冷凝液D1，含游离氨的冷凝液D1的排出速度为3.2m 3/h，氨的浓度为滴度(约纯氨137kg/h)，含游离氨的冷凝液D1可以经蒸氨塔回收氨后，进一步作为补水进入联碱工艺系统，经过除氨洗涤塔323后的第一流化气G1的温度约为25℃。 Step S10322: Input the first fluidized gas G1 washed by the dechlorination washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia, and the discharge rate of the condensate D1 containing free ammonia is 3.2 m 3 /h, the concentration of ammonia is the titer (approximately pure ammonia 137kg/h), the condensate D1 containing free ammonia can be used to recover ammonia through the ammonia distillation tower, and then enter the combined alkali process system as make-up water, and pass through the ammonia removal washing tower. The temperature of the first fluidizing gas G1 after 323 is about 25°C.
步骤S10323：将经过除氯洗涤塔321洗涤后的第一流化气G1输入至除氨洗涤塔323中进行洗涤，产生含游离氨的洗水D2，产生的游离氨的洗水可以去重碱过滤机做洗水或者其他使用。Step S10323: Input the first fluidized gas G1 washed by the chlorine removal washing tower 321 into the ammonia removal washing tower 323 for washing to generate free ammonia-containing washing water D2, and the generated free ammonia washing water can be deduplicated and filtered. Machine for washing or other use.
经过步骤S1031-S1034对第一流化气G1进行分级处理后，即第一流化气G1经过除尘洗涤装置后输出的流化气为第二流化气G2，第二流化气G2的温度约为25℃，第二流化气G2包括气体CO 2； After the first fluidizing gas G1 is classified in steps S1031-S1034, that is, the fluidizing gas output from the first fluidizing gas G1 after passing through the dust removal and washing device is the second fluidizing gas G2, and the temperature of the second fluidizing gas G2 is about 25°C, the second fluidizing gas G2 includes gas CO 2 ;
步骤S104：将第二流化气G2(即CO 2流气)与氨盐水H在压缩碳化装置中进行混合，产生重碱。 Step S104: The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
相对于实施例4，本实用新型实施例设置了出料装置6，即比实施例多了一个步骤S10311，即出料装置6将干燥器2产生的干氯化铵B以及干式除尘设备31产生的固体氯化铵C进行处理，产生干氯化铵B，并将部分干氯化铵B传输至进料混合装置5中，在进料混合装置5中，湿氯化铵滤饼A和干氯化铵B被充分混合，产生湿氯化铵。起到将干氯化铵B充分利用的作用。Compared with Example 4, the embodiment of the present utility model is provided with a discharge device 6, that is, one more step S10311 is added than the embodiment, that is, the discharge device 6 removes the dry ammonium chloride B produced by the dryer 2 and the dry dust removal equipment 31. The solid ammonium chloride C produced is processed to produce dry ammonium chloride B, and part of the dry ammonium chloride B is transferred to the feed mixing device 5, where the wet ammonium chloride filter cake A and Dry Ammonium Chloride B is mixed well, yielding Wet Ammonium Chloride. Play the role of making full use of dry ammonium chloride B.
在实际应用时，CO 2作为干燥氯化铵的流气时，为了满足干燥和闭式循环的需要，而氯化铵流化床干燥需要大量的流化气和足够大的压力，因此，现有技术中常采用鼓风机等加压装置7来增大CO 2流气的压力，但是鼓风机一旦发生故障，那么整个工艺过程即停止，降低了工作效率。因此，在本实用新型一实施例中，在没经过加热装置1加热之前，CO2浓气F的压强为0.05～0.15MPa，具有该压强的CO2浓气F在经过加热装置1后产生的CO 2流化气的压强足以满足干燥和闭式循环的需要，以及氯化铵流化床干燥需要大量的流化气和足够大的压力，因此，无需额外再设置鼓风机等加压装置7，避免了采用鼓风机等加压装置7时因鼓风机发生故障而停止工作的情况，提高了工作效率。 In practical application, when CO 2 is used as the flow gas for drying ammonium chloride, in order to meet the needs of drying and closed circulation, the fluidized bed drying of ammonium chloride requires a large amount of fluidizing gas and sufficient pressure. Therefore, the existing In the technology, a pressurizing device 7 such as a blower is often used to increase the pressure of the CO 2 flow, but once the blower fails, the entire process will be stopped, reducing the work efficiency. Therefore, in an embodiment of the present invention, before being heated by the heating device 1, the pressure of the CO2 rich gas F is 0.05-0.15 MPa, and the CO2 rich gas F with this pressure generates CO2 after passing through the heating device 1. The pressure of the fluidizing gas is sufficient to meet the needs of drying and closed circulation, and the fluidized bed drying of ammonium chloride requires a large amount of fluidizing gas and a sufficiently large pressure. Therefore, there is no need to set up additional pressurizing devices such as blowers, avoiding the need for When the pressurizing device 7 such as a blower is used, the operation is stopped due to the failure of the blower, which improves the work efficiency.
具体的，CO2浓气F为合成氨厂排出的CO2浓气F。由于合成氨厂排出来的CO2浓气F的压强在0.1MPa，具有较高的压强，具有该压强的CO2浓气F在经过加热装置1后产生的CO 2流化气的压强足以满足干燥和闭式循环的需要，以及氯化铵流化床干燥需要大量的流化气和足够大的压力，因此，无需额外再设置鼓风机等加压装置7，且干燥氯化铵需要大量的流化气，因此有效利用了合成氨厂排出来的CO2浓气F，降低了合成氨厂对环境的污。 Specifically, the CO2 rich gas F is the CO2 rich gas F discharged from the synthetic ammonia plant. Since the pressure of the CO2 rich gas F discharged from the synthetic ammonia plant is 0.1 MPa, it has a relatively high pressure, and the pressure of the CO2 rich gas F with this pressure after passing through the heating device 1 is enough to satisfy the drying and closing requirements. The need for circulation, and the drying of the ammonium chloride fluidized bed requires a large amount of fluidizing gas and a large enough pressure, therefore, there is no need to set up additional pressurizing devices 7 such as blowers, and drying ammonium chloride requires a large amount of fluidizing gas, Therefore, the CO2 rich gas F discharged from the synthetic ammonia plant is effectively used, and the pollution of the synthetic ammonia plant to the environment is reduced.
可选的，干燥器2包括：内置换热器的流化床或者管式气流干燥器2。Optionally, the dryer 2 includes: a fluidized bed or a tubular airflow dryer 2 with an internal heat exchanger.
可选的，压缩碳化装置包括：设置在除尘洗涤装置3下游的压缩机，压缩机将第二流化气G2进行压缩，产生压缩二氧化碳；以及设置在压缩机下游的碳化塔，碳化塔将压缩二氧化碳与 氨盐水H进行反应，产生重碱。Optionally, the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidizing gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
实施例6：Example 6:
图6所示为本实用新型实施例提供的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置，包括：进料混合装置5、设置在进料混合装置5下游的干燥器2、设置在干燥器2上游的加热装置1、设置在干燥器2下游的出料装置6以及干式除尘设备31、其中出料装置6也设置在干式除尘设备31的下游，设置在干式除尘设备31下游的除氯洗涤塔321、设置在除氯洗涤塔321下游的除氨冷凝器322、设置在除氨冷凝器322下游的压缩碳化装置；其中，干燥器2包括内置换热器的流化床。压缩碳化装置包括：设置在除尘洗涤装置3下游的压缩机，压缩机将第二流化气G2进行压缩，产生压缩二氧化碳；以及设置在压缩机下游的碳化塔，碳化塔将压缩二氧化碳与氨盐水H进行反应，产生重碱。Fig. 6 shows the combined device for drying ammonium chloride and carbonization to make heavy alkali by utilizing CO2 concentrated gas provided by the embodiment of the utility model, including: a feed mixing device 5, a dryer 2 arranged downstream of the feed mixing device 5 , the heating device 1 arranged upstream of the dryer 2, the discharging device 6 and the dry dust removal device 31 arranged downstream of the dryer 2, wherein the discharging device 6 is also arranged downstream of the dry dust removal device 31, and is arranged in the dry dust removal device 31. The dechlorination washing tower 321 downstream of the dedusting equipment 31, the ammonia removal condenser 322 arranged downstream of the chlorine removal washing tower 321, and the compression carbonization device arranged downstream of the ammonia removal condenser 322; wherein, the dryer 2 includes an internal heat exchanger. fluidized bed. The compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidizing gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower compresses the carbon dioxide and ammonia brine. H reacts to produce dibasic.
采用图6所示的利用CO2浓气进行氯化铵干燥和碳化制重碱的联合装置来进行利用CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺，包括如下步骤：The combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali as shown in Figure 6 is used to carry out the combined process of using CO2 concentrated gas for ammonium chloride drying and carbonization to produce heavy alkali, including the following steps:
步骤S100：将含水6％wt的湿氯化铵滤饼A和出料装置6返回的干氯化铵B在进料混合装置5中进行混合，产生湿氯化铵，其中干氯化铵B以13000Kg/h的速度被输送至进料混合装置5中。即在湿氯化铵输入干燥器2进行干燥之前，将湿氯化铵滤饼A和干氯化铵B在进料混合装置5中进行混合，当充分混合后产生的湿氯化铵在干燥器2中被干燥时，降低干燥器2中的流化床结疤的概率。Step S100: Mix the wet ammonium chloride filter cake A with a water content of 6% wt and the dry ammonium chloride B returned from the discharge device 6 in the feed mixing device 5 to generate wet ammonium chloride, wherein the dry ammonium chloride B It was conveyed to the feed mixing device 5 at a speed of 13000 Kg/h. That is, before the wet ammonium chloride is input into the dryer 2 for drying, the wet ammonium chloride filter cake A and the dry ammonium chloride B are mixed in the feed mixing device 5, and the wet ammonium chloride produced after thorough mixing is dried. Reduces the probability of fluid bed scarring in dryer 2 when being dried in dryer 2.
步骤S101：将合成氨厂来的CO2浓气F以35000Nm 3/h的速度输入至加热装置1进行加热至190℃，产生CO 2流化气，其中，CO2浓气F的压强为0.1MPaG； Step S101: input the CO2 rich gas F from the synthetic ammonia plant into the heating device 1 at a speed of 35000Nm 3 /h to be heated to 190° C. to generate CO2 fluidized gas, wherein the pressure of the CO2 rich gas F is 0.1MPaG;
步骤S102：将CO 2流化气从干燥器2的底部通入干燥器2，将步骤S100中得到的湿氯化铵输入至干燥器2，干燥器2将湿氯化铵加热至工艺温度，产生干氯化铵B、水蒸气、氨气和二氧化碳，其中，水蒸气、氨气以及二氧化碳随CO 2流化气从干燥器2的顶部排出，水蒸气、氨气、二氧化碳以及CO 2流化气组成第一流化气G1；其中干氯化铵B被传输至出料装置6中，第一流化气G1此时的温度约为80℃； Step S102: pass the CO fluidization gas into the dryer 2 from the bottom of the dryer 2, input the wet ammonium chloride obtained in step S100 into the dryer 2, and the dryer 2 heats the wet ammonium chloride to the process temperature, Produce dry ammonium chloride B, water vapor, ammonia and carbon dioxide, wherein water vapor, ammonia and carbon dioxide are discharged from the top of dryer 2 with CO fluidization gas, water vapor, ammonia, carbon dioxide and CO fluidize The gas constitutes the first fluidizing gas G1; wherein the dry ammonium chloride B is transferred to the discharge device 6, and the temperature of the first fluidizing gas G1 at this time is about 80°C;
步骤S1031：将第一流化气G1输入至干式除尘设备31进行除尘处理，产生固体氯化铵C；将固体氯化铵C传输至出料装置6中；即在步骤S1031中，第一流化气G1中的固体氯化铵C大部分被去除；Step S1031: Input the first fluidized gas G1 to the dry dust removal equipment 31 for dedusting treatment to generate solid ammonium chloride C; transfer the solid ammonium chloride C to the discharge device 6; that is, in step S1031, the first fluidized gas Most of the solid ammonium chloride C in gas G1 is removed;
步骤S10311：出料装置6将干燥器2产生的干氯化铵B以及干式除尘设备31产生的固体氯化铵C进行处理，产生干氯化铵B，并将部分干氯化铵B传输至进料混合装置5中，在进料混合装置5中，湿氯化铵滤饼A和干氯化铵B被充分混合，产生湿氯化铵。起到将干氯化铵B充分利用的作用。Step S10311: The discharge device 6 processes the dry ammonium chloride B produced by the dryer 2 and the solid ammonium chloride C produced by the dry dust removal device 31 to produce dry ammonium chloride B, and transmits part of the dry ammonium chloride B To the feed mixing device 5, in the feed mixing device 5, the wet ammonium chloride filter cake A and the dry ammonium chloride B are thoroughly mixed to produce wet ammonium chloride. Play the role of making full use of dry ammonium chloride B.
步骤S10321：将经过干式除尘设备31进行除尘处理后的第一流化气G1输入至除氯洗涤塔321中进行洗涤，产生氯化铵洗水，除氯洗涤塔321通过循环泵、循环冷却器做循环喷淋，对第一流化气G1中的氯化铵进行洗涤，产生氯化铵洗水，洗水含氯化铵约为3.2kg/h，排出的洗水约为63kg/h。此时，经过除氯洗涤塔321后排出的第一流化气G1的温度约为50℃。Step S10321: Input the first fluidized gas G1 that has been dedusted by the dry dedusting equipment 31 into the dechlorination washing tower 321 for washing to generate ammonium chloride washing water, and the dechlorination washing tower 321 passes through the circulating pump and the circulating cooler. Do circulating spray to wash the ammonium chloride in the first fluidizing gas G1 to produce ammonium chloride washing water, the washing water contains about 3.2kg/h of ammonium chloride, and the discharged washing water is about 63kg/h. At this time, the temperature of the first fluidizing gas G1 discharged after passing through the dechlorination washing tower 321 is about 50°C.
步骤S10322：将经过除氯洗涤塔321洗涤后的第一流化气G1输入至除氨冷凝器322中进行洗涤，产生含游离氨的冷凝液D1，含游离氨的冷凝液D1的排出速度为3.2m 3/h，氨的浓度为滴度(约纯氨137kg/h)，含游离氨的冷凝液D1可以经蒸氨塔回收氨后，进一步作为补水进入联碱工艺系统，经过除氨洗涤塔323后的第一流化气G1的温度约为25℃。 Step S10322: Input the first fluidizing gas G1 washed by the dechlorination washing tower 321 into the ammonia removal condenser 322 for washing to generate a condensate D1 containing free ammonia, and the discharge rate of the condensate D1 containing free ammonia is 3.2 m 3 /h, the concentration of ammonia is the titer (about 137kg/h of pure ammonia), the condensate D1 containing free ammonia can be used to recover ammonia through the ammonia distillation tower, and then enter the combined alkali process system as make-up water, and pass through the ammonia removal washing tower. The temperature of the first fluidizing gas G1 after 323 is about 25°C.
经过步骤S1031-S1033对第一流化气G1进行分级处理后，即第一流化气G1经过除尘洗涤装置后输出的流化气为第二流化气G2，第二流化气G2的温度约为25℃，第二流化气G2包括气体CO 2； After the first fluidizing gas G1 is classified in steps S1031-S1033, that is, the fluidizing gas output from the first fluidizing gas G1 after passing through the dust removal and washing device is the second fluidizing gas G2, and the temperature of the second fluidizing gas G2 is about 25°C, the second fluidizing gas G2 includes gas CO 2 ;
步骤S104：将第二流化气G2(即CO 2流气)与氨盐水H在压缩碳化装置中进行混合，产生重碱。 Step S104: The second fluidizing gas G2 (ie, the CO 2 stream gas) is mixed with the ammonia brine H in the compressed carbonization device to generate heavy alkali.
第二流化气G2被输入至压缩碳化装置后的压缩机中，压缩机将CO 2流化气(即第二流化气G2)压缩至0.4MPaG后送入碳化塔与氨盐水H反应生成重碱(碳酸氢钠结晶)。多余的CO 2气可以在压缩机之前高点放空。 The second fluidizing gas G2 is input to the compressor after the compression carbonization device, and the compressor compresses the CO2 fluidizing gas (ie, the second fluidizing gas G2) to 0.4MPaG and then sends it to the carbonization tower to react with ammonia brine H to generate Dibasic (crystallized sodium bicarbonate). Excess CO2 gas can be vented at a high point before the compressor.
对比例1：Comparative Example 1:
不采用合成氨厂来的CO2浓气F作为流化气，而采用CO2浓气F直接去压缩碳化装置，同时氯化铵干燥为闭式循化。The CO2 rich gas F from the synthetic ammonia plant is not used as the fluidizing gas, but the CO2 rich gas F is used to directly compress the carbonization device, and the ammonium chloride is dried in a closed cycle.
图7所示为现有技术中氯化铵干燥和碳化制重碱的联合装置的结构示意图，结合图7，该氯化铵干燥和碳化制重碱的联合装置包括：Fig. 7 shows the structural representation of the combined device of ammonium chloride drying and carbonization to produce heavy alkali in the prior art. With reference to Fig. 7, the combined device of ammonium chloride drying and carbonization to produce heavy alkali includes:
进料混合装置5、设置在进料混合装置5下游的干燥器2、设置在干燥器2上游的加热装置1、设置在加热装置1上游的加压装置7(例如鼓风机)、设置在干燥器2下游的出料装置6以及干式除尘设备31、其中出料装置6也设置在干式除尘设备31的下游，设置在干式除尘设备31下游的除氯洗涤塔321、设置在除氯洗涤塔321下游的除氨冷凝器322、设置在除氨冷凝器322下游的除氨洗涤塔323，其中除氨洗涤塔323的出口端与加压装置7的输入端连接；其中，干燥器2包括内置换热器的流化床。压缩碳化装置，压缩碳化装置包括：设置在除尘洗涤装置3下游的压缩机，压缩机将第二流化气G2进行压缩，产生压缩二氧化碳；以及设置在压缩机下游的碳化塔，碳化塔将压缩二氧化碳与氨盐水H进行反应，产生重碱。 Feed mixing device 5, dryer 2 arranged downstream of feed mixing device 5, heating device 1 arranged upstream of dryer 2, pressurizing device 7 (eg blower) arranged upstream of heating device 1, arranged in the dryer 2. The downstream discharge device 6 and the dry dust removal device 31, wherein the discharge device 6 is also arranged downstream of the dry dust removal device 31, and the dechlorination washing tower 321 is arranged downstream of the dry dust removal device 31. The ammonia removal condenser 322 downstream of the tower 321 and the ammonia removal washing tower 323 arranged downstream of the ammonia removal condenser 322, wherein the outlet end of the ammonia removal washing tower 323 is connected to the input end of the pressurizing device 7; wherein, the dryer 2 includes Fluidized bed with internal heat exchanger. Compression carbonization device, the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidized gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
采用该氯化铵干燥和碳化制重碱的联合装置来进行氯化铵干燥和碳化制重碱的联合工艺包括如下步骤：Adopt the combined device of this ammonium chloride drying and carbonization to make heavy alkali to carry out the combined process of ammonium chloride drying and carbonization to make heavy alkali, and comprises the following steps:
上游来的含水6％wt的湿氯化铵滤饼A52000kg/h通过进料混合装置5，并与返回的干氯化铵B 13000kg/h混合后进入干燥器2，加热装置1来的热循环气190℃从底部加入干燥器2，同时干燥器2内置换热器通入加热蒸汽，干燥器2顶部排出的循环气约为80℃，经干式除尘设备31除去大部分固体氯化铵C后，进入除氯洗涤塔32132，除氯洗涤塔321通过循环泵、循环冷却器做循环喷淋。除氯洗涤塔321塔顶排气温度约为50℃，除氯洗涤塔321塔釜排出的洗水含氯化铵约为3.2kg/h，排出的洗水约为63kg/h。进入除氨冷凝器322的循环气进行冷却冷凝，除氨冷凝器322排出的循环气温度25℃，除氨冷凝器322底部的含游离氨的冷凝液D13.2m3/h，氨浓度为50滴度(纯氨约137kg/h)，此部分冷凝液经蒸氨塔回收氨后，可以作为补水进入联碱工艺系统。在本实施例中不设置除氨洗涤塔323。除氨冷凝器322排出的循环气35000Nm3/h经鼓风机7加压到0.03MPaG后经加热装置14加热至190℃后重新送入干燥器22中。The wet ammonium chloride filter cake A52000kg/h of water 6%wt from upstream passes through the feed mixing device 5, and enters the dryer 2 after mixing with the returned dry ammonium chloride B 13000kg/h, the thermal cycle from the heating device 1 The gas at 190°C is fed into the dryer 2 from the bottom, and the heat exchanger in the dryer 2 is fed with heating steam. The circulating gas discharged from the top of the dryer 2 is about 80°C, and most of the solid ammonium chloride C is removed by the dry dust removal equipment 31. Afterwards, it enters the dechlorination washing tower 32132, and the dechlorination washing tower 321 is circulated and sprayed through a circulating pump and a circulating cooler. The exhaust temperature at the top of the dechlorination washing tower 321 is about 50°C, the washing water discharged from the kettle of the chlorine washing washing tower 321 contains about 3.2 kg/h of ammonium chloride, and the discharged washing water is about 63 kg/h. The circulating gas entering the ammonia removing condenser 322 is cooled and condensed, the temperature of the circulating gas discharged from the ammonia removing condenser 322 is 25°C, the condensate containing free ammonia at the bottom of the ammonia removing condenser 322 is D13.2m3/h, and the ammonia concentration is 50 drops (pure ammonia is about 137kg/h), this part of the condensate can be used as make-up water to enter the combined alkali process system after the ammonia is recovered by the ammonia distillation tower. In this embodiment, the ammonia removal washing tower 323 is not provided. The circulating gas 35000Nm3/h discharged from the ammonia removal condenser 322 is pressurized to 0.03MPaG by the blower 7, heated to 190°C by the heating device 14, and then sent to the dryer 22 again.
自合成氨厂CO2浓气F(～0.1MPaG)直接送至压缩碳化装置压缩至0.4MPaG后送入碳化塔与氨盐水H反应生成重碱。The CO2 concentrated gas F (~0.1MPaG) from the ammonia synthesis plant is directly sent to the compression carbonization device to be compressed to 0.4MPaG and then sent to the carbonization tower to react with the ammonia brine H to generate heavy alkali.
对比例2：Comparative Example 2:
对比例二不采用合成氨厂来的CO2浓气F作为流化气，而采用CO2浓气F直接去压缩碳化装置，氯化铵干燥为闭式循化，但循环气的除氨除氯不进行分级洗涤。Comparative Example 2 The CO2 concentrated gas F from the synthetic ammonia plant is not used as the fluidizing gas, but the CO2 concentrated gas F is used to directly compress the carbonization device. The drying of ammonium chloride is a closed cycle, but the ammonia and chlorine removal of the circulating gas is not carried out. Graded wash.
图8所示为现有技术中氯化铵干燥和碳化制重碱的联合装置的结构示意图，该氯化铵干燥和碳化制重碱的联合装置包括：Fig. 8 shows the structural representation of the combined device of ammonium chloride drying and carbonization to produce heavy alkali in the prior art, and the combined device of this ammonium chloride drying and carbonization to heavy alkali includes:
进料混合装置5、设置在进料混合装置5下游的干燥器2、设置在干燥器2上游的加热装置1、设置在加热装置1上游的加压装置7(例如鼓风机)、设置在干燥器2下游的出料装置6以及干式除尘设备31、其中出料装置6也设置在干式除尘设备31的下游，设置在干式除尘设备31下游的除氨洗涤塔323，其中，除氨洗涤塔323的出口端与加压装置7的输入端连接；其中，干燥器2包括内置换热器的流化床。压缩碳化装置，压缩碳化装置包括：设置在除尘洗涤装置3下游的压缩机，压缩机将第二流化气G2进行压缩，产生压缩二氧化碳；以及设置在压缩机下游的碳化塔，碳化塔将压缩二氧化碳与氨盐水H进行反应，产生重碱。 Feed mixing device 5, dryer 2 arranged downstream of feed mixing device 5, heating device 1 arranged upstream of dryer 2, pressurizing device 7 (eg blower) arranged upstream of heating device 1, arranged in the dryer 2. The downstream discharge device 6 and the dry dust removal device 31, wherein the discharge device 6 is also arranged downstream of the dry dust removal device 31, and is arranged in the ammonia removal washing tower 323 downstream of the dry dust removal device 31, wherein the ammonia removal washing tower 323 The outlet end of the tower 323 is connected to the input end of the pressurizing device 7; wherein, the dryer 2 includes a fluidized bed with an internal heat exchanger. Compression carbonization device, the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidized gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
采用该氯化铵干燥和碳化制重碱的联合装置来进行氯化铵干燥和碳化制重碱的联合工艺包括如下步骤：Adopt the combined device of this ammonium chloride drying and carbonization to make heavy alkali to carry out the combined process of ammonium chloride drying and carbonization to make heavy alkali, and comprises the steps:
上游来的含水6％wt的湿氯化铵滤饼A52000kg/h通过进料混合装置5，并与返回的干氯化铵B13000kg/h混合后进入干燥器2，加热装置1来的热循环气190℃从底部加入干燥器22，同时干燥器2内置换热器通入加热蒸汽，干燥器2顶部排出的循环气约为80℃，经干式除尘设备31除去大部分固体氯化铵C后，进入除氨洗涤塔323除去残留的氯化铵和氨气，除氨洗涤塔323顶部加入3m3/h的新鲜洗水，除氨洗涤塔323底部洗水含氯化铵约为3.2kg/h，氨浓度为24滴度 (纯氨约137kg/h)，排出的洗水约为6.2m3/h，此部分洗水由于含有氯化铵，无法有效作为补水进入联碱工艺系统。除氨洗涤塔323排出的循环气35000Nm3/h经鼓风机7加压到0.03MPaG后经加热装置14加热至190℃后重新送入干燥器22中。The wet ammonium chloride filter cake A52000kg/h with a water content of 6%wt from the upstream passes through the feed mixing device 5, and after mixing with the returned dry ammonium chloride B13000kg/h, it enters the dryer 2, and the hot circulating gas from the heating device 1 190°C is added to the dryer 22 from the bottom, and the heat exchanger in the dryer 2 is fed with heating steam. The circulating gas discharged from the top of the dryer 2 is about 80°C. After removing most of the solid ammonium chloride C through the dry dust removal equipment 31 , enter the ammonia removal washing tower 323 to remove the residual ammonium chloride and ammonia gas, add 3m3/h of fresh washing water at the top of the ammonia removal washing tower 323, and the washing water at the bottom of the ammonia removal washing tower 323 contains about 3.2 kg/h of ammonium chloride , the ammonia concentration is 24 titers (pure ammonia is about 137kg/h), and the discharged washing water is about 6.2m3/h. Because this part of the washing water contains ammonium chloride, it cannot be effectively used as supplementary water to enter the combined alkali process system. The circulating gas 35000Nm3/h discharged from the ammonia removal washing tower 323 is pressurized to 0.03MPaG by the blower 7, heated to 190°C by the heating device 14, and then sent to the dryer 22 again.
自合成氨厂的CO2浓气F(～0.1MPaG)直接送至压缩碳化装置压缩至0.4MPaG后送入碳化塔与氨盐水H反应生成重碱。The CO2 concentrated gas F (~0.1MPaG) from the ammonia synthesis plant is directly sent to the compression carbonization device to be compressed to 0.4MPaG and then sent to the carbonization tower to react with ammonia brine H to generate heavy alkali.
对比例3：Comparative Example 3:
本对比例三不采用合成氨厂来的CO2浓气F作为流化气，而采用CO2浓气F直接去压缩碳化装置，氯化铵干燥为传统的空气开式干燥。This comparative example 3 does not use the CO2 rich gas F from the synthetic ammonia plant as the fluidizing gas, but uses the CO2 rich gas F to directly compress the carbonization device, and the ammonium chloride drying is the traditional open air drying.
图9所示为现有技术中氯化铵干燥和碳化制重碱的联合装置的结构示意图，该氯化铵干燥和碳化制重碱的联合装置包括：Fig. 9 shows the structural representation of the combined device of ammonium chloride drying and carbonization to produce heavy alkali in the prior art, and the combined device of this ammonium chloride drying and carbonization to produce heavy alkali includes:
进料混合装置5、设置在进料混合装置5下游的干燥器2、设置在干燥器2上游的加热装置1、设置在加热装置1上游的第一加压装置71(例如鼓风机)、设置在干燥器2下游的出料装置6以及干式除尘设备31、其中出料装置6也设置在干式除尘设备31的下游，设置在干式除尘设备31下游的除氨洗涤塔323，设置在除氨洗涤塔323下游的第二加压装置72，其中除氨洗涤塔323的出口端与第二加压装置72的输入端连接；其中，干燥器2包括内置换热器的流化床。压缩碳化装置，压缩碳化装置包括：设置在除尘洗涤装置3下游的压缩机，压缩机将第二流化气G2进行压缩，产生压缩二氧化碳；以及设置在压缩机下游的碳化塔，碳化塔将压缩二氧化碳与氨盐水H进行反应，产生重碱。The feed mixing device 5, the dryer 2 arranged downstream of the feed mixing device 5, the heating device 1 arranged upstream of the dryer 2, the first pressurizing device 71 (such as a blower) arranged upstream of the heating device 1, the The discharge device 6 downstream of the dryer 2 and the dry dust removal device 31, wherein the discharge device 6 is also arranged downstream of the dry dust removal device 31, and the ammonia removal washing tower 323 is arranged downstream of the dry dust removal device 31. The second pressurizing device 72 downstream of the ammonia scrubbing tower 323, wherein the outlet end of the ammonia removing scrubbing tower 323 is connected to the input end of the second pressurizing device 72; wherein, the dryer 2 includes a fluidized bed with an internal heat exchanger. Compression carbonization device, the compression carbonization device includes: a compressor arranged downstream of the dust removal and washing device 3, the compressor compresses the second fluidized gas G2 to generate compressed carbon dioxide; and a carbonization tower arranged downstream of the compressor, the carbonization tower will compress Carbon dioxide reacts with ammonia brine H to produce heavy base.
采用该氯化铵干燥和碳化制重碱的联合装置来进行氯化铵干燥和碳化制重碱的联合工艺包括如下步骤：Adopt the combined device of this ammonium chloride drying and carbonization to make heavy alkali to carry out the combined process of ammonium chloride drying and carbonization to make heavy alkali, and comprises the steps:
上游来的含水6％wt的湿氯化铵滤饼A52000kg/h通过进料混合装置5，并与返回的干氯化铵B13000kg/h混合后进入干燥器2，新鲜空气经鼓风机7加压至0.025MPaG后送入加热装置1加热到190℃后从底部加入干燥器2，同时干燥器2内置换热器通入加热蒸汽，干燥器2顶部排出的循环气约为80℃，经干式除尘设备31除去大部分固体氯化铵C后，进入除氨洗涤塔323除去残留的氯化铵和氨气，除氨洗涤塔323顶部加入100m3/h的新鲜洗水，除氨洗涤塔323底部洗水含氯化铵约为3.2kg/h，氨浓度约为1.4滴度(纯氨约137kg/h)，排出的洗水约为103.2m3/h，此部分洗水由于含有氯化铵且量十分巨大，无法有效作为补水进入联碱工艺系统。除氨洗涤塔32334排出的尾气35000Nm3/h经鼓风机7加压到0.001MPaG后排入大气。The wet ammonium chloride filter cake A52000kg/h with a water content of 6%wt from the upstream passes through the feed mixing device 5, and enters the dryer 2 after mixing with the returned dry ammonium chloride B13000kg/h, and the fresh air is pressurized by the blower 7 to After 0.025MPaG, it is sent to the heating device 1 and heated to 190 °C, and then added to the dryer 2 from the bottom. At the same time, the heat exchanger in the dryer 2 is fed with heating steam. The circulating gas discharged from the top of the dryer 2 is about 80 °C. After dry dust removal After the equipment 31 removes most of the solid ammonium chloride C, it enters the ammonia removal washing tower 323 to remove the residual ammonium chloride and ammonia gas. The top of the ammonia removal washing tower 323 is added with 100m3/h of fresh washing water, and the bottom of the ammonia removal washing tower 323 is washed. The water content of ammonium chloride is about 3.2kg/h, the ammonia concentration is about 1.4 titers (pure ammonia is about 137kg/h), and the discharged washing water is about 103.2m3/h. It is very huge and cannot be effectively used as make-up water to enter the combined alkali process system. The tail gas 35000Nm3/h discharged from the ammonia removal washing tower 32334 is pressurized to 0.001MPaG by the blower 7 and then discharged into the atmosphere.
自合成氨厂的CO2浓气F(～0.1MPaG)直接送至压缩碳化装置压缩至0.4MPaG后送入碳化塔与氨盐水H反应生成重碱。The CO2 rich gas F (~0.1MPaG) from the ammonia synthesis plant is directly sent to the compression carbonization device to be compressed to 0.4MPaG and then sent to the carbonization tower to react with the ammonia brine H to generate heavy alkali.
将本实用新型的实施例6以及对比例1、对比例2、对比例3进行了工艺参数和经济对比， 如下表所示：The embodiment 6 of the present utility model and comparative example 1, comparative example 2, comparative example 3 are carried out technological parameter and economic contrast, as shown in the following table:
Figure PCTCN2021118219-appb-000001
Figure PCTCN2021118219-appb-000001
其中，上表中：Among them, in the above table:
1.新鲜水的消耗包括从湿氯化铵滤饼A回收的水和洗涤加入的新鲜水量；1. The consumption of fresh water includes the amount of fresh water recovered from wet ammonium chloride filter cake A and the amount of fresh water added for washing;
2.电费按照0.5元/度，新鲜水费用按照0.6元/吨，氨费用按照3000元/吨计。2. The electricity fee is 0.5 yuan/kWh, the fresh water fee is 0.6 yuan/ton, and the ammonia fee is 3,000 yuan/ton.
3.每年运行费用表示加压装置7、例如鼓风机，和压缩机的总电费、新鲜水的费用和节省氨的费用的总和。3. The annual operating cost represents the sum of the total electricity cost of the pressurizing device 7, such as the blower, and the compressor, the cost of fresh water and the cost of saving ammonia.
4.表中的负号表示节省的意思。4. The minus sign in the table means saving.
从上表可以看出，采用实施例5，每年的运行费用与对比例1相同，但对比例1中存在了鼓风加压装置7，而实施例6中没有加压装置7，完全依靠CO2浓气F的压力，稳定性高，避免了因鼓风机故障而造成停车。As can be seen from the above table, using Example 5, the annual operating cost is the same as that of Comparative Example 1, but there is a blower pressurizing device 7 in Comparative Example 1, while there is no pressurizing device 7 in Example 6, relying entirely on CO2 The pressure of concentrated gas F has high stability and avoids shutdown due to blower failure.
采用对比例2，没有进行分级除氯除氨，虽然电费与实施例6相同，但每年新鲜水的费用和氨损失的费用多大333.312万元。Using the comparative example 2, without grading dechlorination and ammonia removal, although the electricity cost is the same as that of Example 6, the annual cost of fresh water and ammonia loss is 3,333,120 yuan.
采用对比例3，采用大量的新鲜水进行洗涤，排向大气的尾气含氨量仍达到了1185mg/Nm3，远超环保排放标准。除了每年运行电费817.536万外，还需要考虑处理这103.2m3/h的含氯含氨废水的额外费用。Using Comparative Example 3, using a large amount of fresh water for washing, the ammonia content of the exhaust gas discharged to the atmosphere still reached 1185mg/Nm3, far exceeding the environmental protection emission standard. In addition to the annual operating electricity cost of 8,175,360, it is also necessary to consider the additional cost of treating the 103.2m3/h chlorine-containing ammonia-containing wastewater.
以上对一种直接利用合成氨厂来的CO2浓气进行氯化铵干燥和碳化制重碱的联合工艺实用新型进行了具体实施例的描述。本领域技术人员可以借鉴本实用新型的内容进行修改工艺设备类型、设备组合、处理方法、修改参数等环节来实现相应的其他目的，其相关改变都没有脱离本实用新型的内容，凡在本实用新型创造的精神和原则之内，所做的任何修改、等同替换、改进等，均应包含在本实用新型创造的保护范围之内。A specific embodiment has been described above for a combined process utility model of directly utilizing the CO2 rich gas from the synthetic ammonia plant to dry ammonium chloride and carbonize to produce heavy caustic soda. Those skilled in the art can refer to the content of the present invention to modify the process equipment types, equipment combinations, processing methods, modifying parameters and other links to achieve other corresponding purposes. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the new invention should be included in the protection scope of the present invention.

Claims (10)

  1. 一种利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于，包括： A combined device for ammonium chloride drying and carbonization to make heavy alkali utilizing CO concentrated gas is characterized in that, comprising:
    加热装置，所述加热装置用于将CO 2浓气加热，产生CO 2流化气，其中； a heating device, the heating device is used for heating the CO 2 rich gas to generate the CO 2 fluidizing gas, wherein;
    设置在所述加热装置下游的干燥器，所述干燥器的底部通入所述加热装置产生的CO 2流化气，所述干燥器将所述湿氯化铵加热至工艺温度，产生干氯化铵、水蒸气、氨气和二氧化碳，其中，所述水蒸气、所述氨气以及所述二氧化碳随所述CO 2流化气从所述干燥器的顶部排出，所述水蒸气、所述氨气、所述二氧化碳以及所述CO 2流化气组成第一流化气； A dryer arranged downstream of the heating device, the bottom of the dryer is passed into the CO 2 fluidization gas generated by the heating device, and the dryer heats the wet ammonium chloride to the process temperature to generate dry chlorine ammonium, water vapor, ammonia and carbon dioxide, wherein the water vapor, the ammonia and the carbon dioxide are discharged from the top of the dryer with the CO fluidizing gas, the water vapor, the ammonia and the carbon dioxide are discharged from the top of the dryer Ammonia, the carbon dioxide and the CO fluidizing gas form a first fluidizing gas;
    设置在所述干燥器下游的除尘洗涤装置，所述除尘洗涤装置将所述第一流化气逐级处理得到固体氯化铵、氯化铵洗水以及含游离氨的液体，所述第一流化气经过所述除尘洗涤装置后输出的流化气为第二流化气，所述第二流化气包括气体CO 2；以及 A dedusting and washing device arranged downstream of the dryer, the dedusting and washing device processes the first fluidized gas step by step to obtain solid ammonium chloride, ammonium chloride washing water and a liquid containing free ammonia, and the first fluidized gas is The fluidizing gas outputted after the gas passes through the dedusting and washing device is the second fluidizing gas, and the second fluidizing gas includes gas CO 2 ; and
    碳压缩装置，经所述除尘洗涤装置输出的第二流化气输入至所述碳压缩装置，所述碳压缩装置将所述第二流化气与氨盐水混合，产生重碱。In the carbon compression device, the second fluidized gas outputted by the dust removal and washing device is input to the carbon compression device, and the carbon compression device mixes the second fluidized gas with ammonia brine to generate heavy alkali.
  2. 根据权利要求1所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于，所述除尘洗涤装置包括： The combined device for ammonium chloride drying and carbonization to make heavy caustic by utilizing CO concentrated gas according to claim 1, is characterized in that, described dedusting and washing device comprises:
    设置在所述干燥器下游的干式除尘设备，所述干式除尘设备用于对所述第一流化气进行除尘，产生固体氯化铵；以及a dry dedusting device disposed downstream of the dryer, the dry dedusting device is used for dedusting the first fluidizing gas to produce solid ammonium chloride; and
    设置在所述干式除尘设备下游的湿式洗涤设备，所述湿式洗涤设备用于对所述第一流化气进行逐级洗涤，分级产生氯化铵洗水以及含游离氨的液体。A wet scrubbing device is arranged downstream of the dry dust removal device, and the wet scrubbing device is used for step-by-step scrubbing of the first fluidizing gas to produce ammonium chloride washing water and a liquid containing free ammonia in stages.
  3. 根据权利要求2所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于， The combined device for ammonium chloride drying and carbonization to make heavy alkali by utilizing CO concentrated gas according to claim 2, is characterized in that,
    所述干式除尘设备包括：The dry dust removal equipment includes:
    旋风分离器；和/或cyclones; and/or
    布袋除尘器。Bag filter.
  4. 根据权利要求2所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于， The combined device for ammonium chloride drying and carbonization to make heavy alkali by utilizing CO concentrated gas according to claim 2, is characterized in that,
    所述湿式洗涤设备包括：The wet washing equipment includes:
    设置在所述干式除尘设备下游的除氯洗涤塔，所述除氯洗涤塔用于对所述第一流化气进行洗涤，产生氯化铵洗水；以及a dechlorination washing tower disposed downstream of the dry dust removal device, the dechlorination washing tower is used for washing the first fluidized gas to generate ammonium chloride washing water; and
    设置在所述除氯洗涤塔下游的除氨冷凝器，所述除氨冷凝器用于对经过所述除氯洗涤塔处理后的第一流化气进行洗涤，产生含游离氨的冷凝液。The ammonia removal condenser is arranged downstream of the chlorine removal washing tower, and the ammonia removal condenser is used for washing the first fluidized gas processed by the chlorine removal washing tower to generate a condensate containing free ammonia.
  5. 根据权利要求4所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于，所述湿式洗涤设备还包括： The combined device for ammonium chloride drying and carbonization to make heavy caustic using CO concentrated gas according to claim 4, characterized in that, the wet scrubbing equipment further comprises:
    设置在所述除氨冷凝器下游的除氨洗涤塔，所述除氨洗涤塔用于对经过除氨冷凝器处理后的第一流化气进行洗涤，产生含游离氨的洗水。The ammonia removal washing tower is arranged downstream of the ammonia removal condenser, and the ammonia removal washing tower is used for washing the first fluidized gas treated by the ammonia removal condenser to generate washing water containing free ammonia.
  6. 根据权利要求1所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于，所述压缩碳化装置包括： The combined device for ammonium chloride drying and carbonization to make heavy caustic using CO concentrated gas according to claim 1, is characterized in that, described compression carbonization device comprises:
    设置在所述除尘洗涤装置下游的压缩机，所述压缩机将所述第二流化气进行压缩，产生压缩二氧化碳；以及a compressor disposed downstream of the dedusting and scrubbing device, the compressor compresses the second fluidizing gas to produce compressed carbon dioxide; and
    设置在所述压缩机下游的碳化塔，所述碳化塔将所述压缩二氧化碳与氨盐水进行反应，产生重碱。A carbonization tower is arranged downstream of the compressor, and the carbonization tower reacts the compressed carbon dioxide with ammonia brine to produce heavy alkali.
  7. 根据权利要求1所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于，还包括： Utilize CO2 concentrated gas according to claim 1 to carry out the combined device of ammonium chloride drying and carbonization to make heavy caustic soda, it is characterized in that, also comprises:
    设置在所述干燥器上游的进料混合装置，所述进料混合装置将湿氯化铵滤饼和干氯化铵混合，产生湿氯化铵，并将所述湿氯化铵输入至所述干燥器中。A feed mixing device arranged upstream of the dryer, the feed mixing device mixes the wet ammonium chloride filter cake and dry ammonium chloride, produces wet ammonium chloride, and inputs the wet ammonium chloride to the in the dryer.
  8. 根据权利要求7所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于，还包括： The combined device for ammonium chloride drying and carbonization to make heavy caustic using CO concentrated gas according to claim 7, is characterized in that, further comprising:
    出料装置，所述出料装置的进口与所述干燥器以及所述除尘洗涤装置连接，所述出料装置的出口与所述进料混合输送装置连接；A discharging device, the inlet of the discharging device is connected with the dryer and the dust removal and washing device, and the outlet of the discharging device is connected with the feeding mixing and conveying device;
    所述出料装置将所述干燥器产生的干氯化铵以及所述除尘洗涤装置产生的固体氯化铵进行处理，产生干氯化铵。The discharging device processes the dry ammonium chloride produced by the dryer and the solid ammonium chloride produced by the dedusting and washing device to produce dry ammonium chloride.
  9. 根据权利要求1所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于， The combined device for ammonium chloride drying and carbonization to make heavy alkali by utilizing CO concentrated gas according to claim 1, is characterized in that,
    所述干燥器包括：内置换热器的流化床或者管式气流干燥器。The dryer includes: a fluidized bed with an internal heat exchanger or a tubular airflow dryer.
  10. 根据权利要求1所述的利用CO 2浓气进行氯化铵干燥和碳化制重碱的联合装置，其特征在于，所述CO 2浓气为合成氨厂排出的CO 2浓气。 The combined device for ammonium chloride drying and carbonization to make heavy alkali by utilizing CO 2 rich gas according to claim 1, is characterized in that, the CO 2 rich gas is CO 2 rich gas discharged from a synthetic ammonia plant.
PCT/CN2021/118219 2021-02-04 2021-09-14 Combined apparatus for producing heavy soda ash by utilizing co2 concentrated gas for ammonium chloride drying and carbonation WO2022166209A1 (en)

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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2671713A (en) * 1952-11-18 1954-03-09 Olin Mathieson Separation and use of ammonium chloride in the ammonia soda process for producing sodium bicarbonate
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
CN106595227A (en) * 2016-11-28 2017-04-26 安德里茨（中国）有限公司 Ammonium chloride drying and cooling system and process
CN206469588U (en) * 2016-11-28 2017-09-05 安德里茨（中国）有限公司 Ammonium chloride is dried and cooling system
CN207849900U (en) * 2018-01-17 2018-09-11 江苏大江干燥设备有限公司 A kind of closed cycle fluidization system of ammonium chloride drying
CN112794347A (en) * 2021-02-04 2021-05-14 中国天辰工程有限公司 By using CO2Combined device and process for preparing heavy alkali by drying and carbonizing ammonium chloride in concentrated gas

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2671713A (en) * 1952-11-18 1954-03-09 Olin Mathieson Separation and use of ammonium chloride in the ammonia soda process for producing sodium bicarbonate
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
CN106595227A (en) * 2016-11-28 2017-04-26 安德里茨（中国）有限公司 Ammonium chloride drying and cooling system and process
CN206469588U (en) * 2016-11-28 2017-09-05 安德里茨（中国）有限公司 Ammonium chloride is dried and cooling system
CN207849900U (en) * 2018-01-17 2018-09-11 江苏大江干燥设备有限公司 A kind of closed cycle fluidization system of ammonium chloride drying
CN112794347A (en) * 2021-02-04 2021-05-14 中国天辰工程有限公司 By using CO2Combined device and process for preparing heavy alkali by drying and carbonizing ammonium chloride in concentrated gas

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