Patent Application
20230405521
This application claims the benefit under 35 U.S.C. 119(a) of Chinese Patent Application No. CN202210553874.4, filed May 19, 2022, which is hereby incorporated by reference herein in its entirety.
The present invention belongs to the technical field of environmental protection, and in particular relates to a device and method for staged absorption ammonia-based decarbonization.
Climate warming is a problem that affects the development of the entire human being. CO2 is the main contributor to climate warming. The industrial gas produced by the production activities of the chemical industry contains a large amount of CO2.
The chemical absorption method using ammonia as the absorption agent has the characteristics of strong absorption capacity, low corrosion, low regeneration energy consumption, low replenishing cost, low susceptibility to degradation by other components in the flue gas, and simultaneous removal of a variety of acidic gas pollutants, etc. A lot of research has been done on the absorption of CO2 using ammonia by domestic and foreign scholars.
Patent application publication CN108144428A proposes a process of sectional control and multi-point addition of ammonia, which is mainly divided into a pre-washing section, an absorption section, and a fine particle control section, each of which is provided with a number of spray layers. The pre-washing section cools the flue gas while concentrating the circulating washing liquid in the pre-washing section, and the absorption section absorbs and removes sulfur dioxide in the flue gas. The escape of ammonia and the generation of aerosols in each section are controlled. This method lacks emissions control for the removal of CO2 from industrial gases.
Patent CN101524621B provides a flue gas decarbonization system with staged absorption and regeneration, which is composed of an absorption system, a regeneration system and a heat exchange system, and has lower energy consumption than traditional technologies. However, this system is applicable to systems with ethanolamine as the desulfurizer, where energy saving effect is achieved by controlling the multi-stage regeneration liquid return and absorption system.
Patent application CN200880122376.2 discloses a multi-stage CO2 removal system and method for treating flue gas flow, where an absorber vessel is used, the flue gas flow is brought into contact with an ionic solution containing ammonia at a low temperature of 0-20° C., while the solution in the first absorption stage has a higher temperature and lower ammonia-to-carbon ratio than the solution in the third absorption stage. Ammonia escape can be reduced by controlling at low temperature, and having a lower temperature in the third stage, but a higher ammonia-to-carbon ratio in the third stage increases ammonia escape. This process has low decarbonization efficiency, high energy consumption, and serious ammonia escape.
Process gas 1, ammonium bicarbonate generating zone 2, ammonium bicarbonate generating zone circulating pump 3, ammonium bicarbonate generating zone heat exchanger 4, ammonia 5, decarbonization absorption zone 6, first-stage decarbonization absorption zone 7, liquid collector 8, second-stage decarbonization absorption zone 9, liquid collector 10, third-stage decarbonization absorption zone 11, first-stage decarbonization absorption zone circulating pump 12, first-stage decarbonization absorption zone heat exchanger 13, second-stage decarbonization absorption zone circulating pump 14, second-stage decarbonization absorption zone heat exchanger 15, third-stage decarbonization absorption zone circulating pump 16, third-stage decarbonization absorption zone heat exchanger 17, ammonia escape control system 18, ammonia escape control system water washing zone 19, liquid collector 20, ammonia escape control system acid washing zone 21, ammonia escape control system water washing zone circulating pump 22, desulfurization circulating liquid return 23, circulating liquid 24 from ammonia-based desulfurization system, flue gas discharge 25, ammonium bicarbonate discharge pump 26, crystallizer 27, solid-liquid separation equipment 28, packaging machine 29, and solid ammonium bicarbonate 30.
Provided is a method for staged absorption ammonia-based decarbonization, which uses an absorption circulating liquid containing ammonium salts to remove carbon dioxide in gas, and controls ammonia escape while realizing efficient decarbonization through staged solution composition control and reaction condition control.
At 10-30° C. and one atmospheric pressure, CO2 and ammonia react to produce ammonium carbamate and ammonium carbonate as the main products, and this reaction is a reversible reaction. Overall chemical reaction formula:
CO2+NH3+H2ONH4HCO8
In the actual reaction process, there are many intermediate reactions. The general process is as follows:
CO2+NH3NH2COONH4
Ammonium carbamate hydrolysis:
NH2COONH4+H2ONH4HCO3+NH3
Reaction between NH3 and H2O:
NH3+H2ONH4OH
Ammonium bicarbonate produced by hydrolysis reacts with ammonia to generate ammonium carbonate:
NH4HCO3+NH4OH(NH4)2CO3+H2O
Ammonium carbonate absorbs carbon dioxide to form ammonium bicarbonate:
(NH4)2CO3+H2O+CO22NH4HCO3
It can be seen from the above reactions that there are various complex chemical reactions between carbon dioxide and ammonia, and most of them are reversible reactions, and the solution composition is complex. To improve the efficiency of reaction between CO2 and ammonia while reducing ammonia escape requires reasonable staged solution composition control and reaction condition control.
Staged solution composition control may include concentration gradient control of ammonium carbonate, ammonium bicarbonate, ammonium carbamate, ammonia, or combinations thereof, which may be characterized by the molar ratio of total ammonia to total CO2.
Reaction condition control may include temperature control, pH control, and pressure control.
The cooled flue gas may be sequentially contacted with ammonium bicarbonate generating liquid and decarbonization absorption liquid to realize the synergistic control of ammonium bicarbonate generation, ammonium bicarbonate crystallization, carbon dioxide absorption, and ammonia escape, wherein:
The gas-liquid contact form for the ammonium bicarbonate generating liquid may be preferably of spray type, packing type, and bubbling type, and the gas-liquid contact form for the decarbonization absorption liquid is preferably of spray type and packing type.
The temperature control may reduce the temperature of the solution through a cold source, and the solution may be in contact with the flue gas to reduce the temperature of the flue gas. For the cold source, a refrigerator may be used to prepare chilled water, and the chilled water may cool down the solution through a heat exchanger or a coil. The temperature of the ammonium bicarbonate generating liquid may be controlled to be in the range 10-30° C., preferably 12-28° C., preferably 15-25° C., and most preferably 16-22° C. In the first stage, the temperature of the decarbonization absorption liquid may be higher than the temperature of the ammonium bicarbonate generating liquid. High solution temperature may be beneficial to reducing the capital cost in cooling equipment. The temperature of the decarbonization absorption liquids between the first stage and the final stage is usually higher than the temperature of the first stage decarbonization absorption liquid and the final-stage decarbonization absorption liquid. In the final stage, the temperature of the decarbonization absorption liquid may be lower than the temperature of the ammonium bicarbonate generating liquid, which may control ammonia escape. Preferably, the temperature of the ammonium bicarbonate generating circulating liquid may be controlled to be in the range 15° C. to 25° C. In the first stage, the temperature of the decarbonization absorption circulating liquid may be higher than the temperature of the ammonium bicarbonate generating circulating liquid, and in the final stage, the temperature of the decarbonization absorption circulating liquid may be lower than the temperature of the ammonium bicarbonate generating circulating liquid.
The pH control may be achieved through addition of ammonia or solution replacement between stages.
Ammonia is mainly added to the decarbonization absorption liquid, and may be added into the decarbonization absorption liquid in multiple stages separately. No or a little ammonia is added to the ammonium bicarbonate generating liquid, and the amount of ammonia added to the final-stage decarbonization absorption liquid may be lower than that of the previous stage or no ammonia is added. Preferably, ammonia is added to the first- and second-stage decarbonization absorption circulating liquids, and the amount of ammonia added to the second-stage decarbonization absorption circulating liquid may account for 80-50 wt % (weight-percent) of the total amount of ammonia added, preferably 75-55 wt %, more preferably 72%-57 wt %, and most preferably 60-65 wt % No ammonia is added to the final-stage decarbonization absorption circulating liquid and ammonium bicarbonate generating circulating liquid. Through multi-stage addition of ammonia, it is beneficial to controlling the solution composition, adjusting the pH value of the solution, and controlling ammonia escape while ensuring the decarbonization absorption efficiency. No or a little ammonia is added to the ammonium bicarbonate generating liquid to ensure the production of ammonium bicarbonate. The amount of ammonia added to the final-stage decarbonization absorption liquid may be lower than that of the previous stage or no ammonia is added, which may control ammonia escape.
Solution replacement may be conducted through pipe overflow or pump transportation to transport the solution of the previous stage to the next stage, which may control the solution composition and pH value. The pH value of the ammonium bicarbonate generating liquid may be lower than that of the decarbonization absorption liquid, and its content of ammonium bicarbonate may be greater than that of the decarbonization absorption liquid.
The pH value in the decarbonization absorption liquid may be ≥8.0, preferably ≥8.2, more preferably ≥8.5, and most preferably ≥9.0.
Pressure control may be achieved, for example, by providing control valves or liquid seals in the ammonia-based decarbonization system. A control valve or a liquid seal device may be provided on a gas pipe after the decarbonization absorption zone or after the ammonia escape control system to maintain the internal pressure of the system as required.
The ammonia-based decarbonization device may maintain normal pressure ±50 kPa, preferably normal pressure ±40 kPa, more preferably normal pressure ±30 kPa, and most preferably normal pressure ±25 kPa.
Provided is a device for staged absorption ammonia-based decarbonization, which may include a decarbonization system, an ammonia escape control system, an ammonium bicarbonate treatment system, an ammonia supply system, and a cooling system.
The decarbonization system may include zone control, including an ammonium bicarbonate generating zone and a decarbonization absorption zone, wherein the ammonium bicarbonate generating zone is provided with at least one stage of gas-liquid contactor, the decarbonization absorption zone is provided with at least two stages of gas-liquid contactors, and equipment/components that only allow gas to pass through are provided between the zones and stages.
One or more layers of demisters may be provided after the final stage of the decarbonization absorption zone, and no, one or more layers of demisters are provided in the remaining layers as required. The demister may be of baffle, ridge, packing and screen type, or combinations thereof.
The ammonia escape control system may include multi-stage washing circulation, and may be provided with at least one layer of acidic solution washing.
The cooling system may be used to lower the temperature of the ammonium bicarbonate generating circulating liquid and the decarbonization absorption circulating liquid.
The ammonium bicarbonate treatment system may include ammonium bicarbonate crystallization equipment and solid-liquid separation equipment.
The CO2 content in the process gas before decarbonization may be in the range 6-50 v % (volume-percent); preferably 8-40 v %; and more preferably 10-30 v %.
The CO2 content in the gas after the staged absorption ammonia-based treatment may be in the range 0-10 v %; preferably 0-8 v %; and preferably 0-6 v %.
Clean flue gas SO2 may have ≤10 mg/Nm3, preferably ≤5 mg/Nm3, and more preferably ≤2 mg/Nm3.
Clean flue gas ammonia escape may be ≤20 ppm, preferably 15 ppm, and more preferably 10 ppm.
CO2 removal efficiency may be ≥60%, preferably ≥70%, and more preferably ≥80%.
The methods may include using an absorption circulating liquid containing ammonium salts to remove carbon dioxide from a gas. The methods may include limiting ammonia escape by applying controlled compositions of the circulating liquid to the gas at different stages. Each stage may have a controlled reaction condition.
The controlled compositions may be characterized by a molar ratio of total ammonia to total CO2. The controlled compositions may include ammonium carbonate. The controlled compositions may include ammonium bicarbonate. The controlled compositions may include ammonium carbamate. The controlled compositions may include ammonia.
The methods may include cooling a flue gas. The methods may include, after the cooling, contacting the flue gas sequentially with an ammonium bicarbonate-generating circulating liquid. The methods may include, after the cooling, contacting the flue gas sequentially with a decarbonization absorption circulating liquid. The ammonium bicarbonate-generating liquid may be involved in at least one stage of gas-liquid contact. After the stage, a molar ratio of total ammonia to total CO2 in the ammonium bicarbonate-generating liquid may be in the range 1-3. The decarbonization absorption liquid may be involved in at least two stages of gas-liquid contact. After a first of the stages, a molar ratio of total ammonia to total CO2 in the decarbonization absorption liquid may be in the range 1.2-4. After a final stage of the stages, a molar ratio of total ammonia to total CO2 in the decarbonization absorption liquid may be in the range 1-3. After any stage that occurs between the first stage and the final stage, a molar ratio of total ammonia to total CO2 in the decarbonization absorption liquid may be in the range 1.5-4.5. The total ammonia may include ammonia and ammonium radicals. The total CO2 may include free CO2 and carbonized CO2.
The gas-liquid contact of the ammonium bicarbonate generating liquid may be of a spray type, a packing type, or a bubbling type. The gas-liquid contact of the decarbonization absorption liquid may be of a spray type or a packing type.
A pH value of the ammonium bicarbonate generating liquid may be lower than a pH value of the decarbonization absorption liquid. An ammonium bicarbonate content of the ammonium bicarbonate generating liquid may be greater than that of the decarbonization absorption liquid.
A pH value of the decarbonization absorption liquid may be greater than 8.0.
The methods may include adding to the ammonium bicarbonate generating liquid a first amount of ammonia. The methods may include adding to the decarbonization absorption liquid a second amount of ammonia that is more than the first amount. In the adding to the decarbonization absorption liquid, it may be that less ammonia is added to the decarbonization absorption liquid in the final stage than is that which is added to the decarbonization absorption liquid in a decarbonization stage before the final stage.
The adding to the decarbonization absorption liquid a second amount of ammonia may include distributing the second amount of ammonia only to multiple stages separately.
The contacting the flue gas with a decarbonization absorption circulating liquid may include performing the contacting at normal pressure ±50 kPa.
The methods may include controlling the reaction condition. The reaction condition may include one or more of temperature, pH and pressure.
The methods may include contacting the flue gas sequentially with: an ammonium bicarbonate-generating circulating liquid; and a decarbonization absorption circulating liquid. The controlling may include using a cold source to reduce a temperature of the ammonium bicarbonate generating liquid. The controlling may include using a cold source to reduce a temperature of the decarbonization absorption liquid.
The controlling may include between stages adding ammonia or replacing liquid of the ammonium bicarbonate generating liquid to control pH of the ammonium bicarbonate generating liquid. The controlling may include between stages adding ammonia or replacing liquid of the decarbonization absorption liquid to control pH of the decarbonization absorption liquid. The controlling may include between stages maintaining normal pressure of the contacting of the flue gas with the decarbonization absorption liquid using a control valve or liquid seal, not a control valve. The contacting may reduce the temperature of the flue gas.
The methods may include maintaining a temperature of ammonium bicarbonate generating liquid in the range 10-30° C.;
The methods may include, in a first stage of contacting the gas with decarbonization absorption liquid, maintaining the decarbonization absorption liquid at a temperature that is higher than a temperature of ammonium bicarbonate generating liquid. The methods may include, in a final stage of contacting the gas with decarbonization absorption liquid. The methods may include maintaining the decarbonization absorption liquid at a temperature that is higher than the temperature of ammonium bicarbonate generating liquid.
The methods may include releasing the gas in a state in which the gas has an SO2 concentration that is ≤10 mg/Nm3. The methods may include releasing the gas in a state in which ammonia escape is ≤20 ppm.
The CO2 may be removed at a CO2 removal efficiency that is ≥60%.
A CO2 content in the process gas before decarbonization may be in the range 6-50 v % (volume percent). A CO2 content in the gas after treatment may be in the range 0-10 v %.
The methods may include receiving the gas from an ammonia-based desulfurization process.
The apparatus may include apparatus for staged absorption ammonia-based decarbonization.
The apparatus may include a decarbonization system. The apparatus may include an ammonia escape control system. The apparatus may include an ammonium bicarbonate treatment system. The apparatus may include an ammonia supply system. The apparatus may include a cooling system.
The decarbonization system may include an ammonium bicarbonate generating zone. The decarbonization system may include a decarbonization absorption zone. The ammonium bicarbonate generating zone may include at least one stage of gas-liquid contact. The decarbonization absorption zone may include at least two stages of gas-liquid contact.
Components allowing only gas to pass through may be disposed between the zones. Components allowing only gas to pass through may be disposed between the stages.
The apparatus may include one or more layers of demisters after a final stage of the decarbonization absorption zone. The apparatus may include at least one layer of acidic solution washing.
The ammonia escape control system may include multi-stage washing cycle control. The cooling system may be configured to reduce a temperature of the ammonium bicarbonate generating liquid. The cooling system may be configured to reduce a temperature of the decarbonization absorption liquid. The ammonium bicarbonate treatment system may include ammonium bicarbonate crystallization equipment. The ammonium bicarbonate treatment system may include solid-liquid separation equipment.
The gas to be treated in the method of the present invention is any suitable gas, preferably the process gas after ammonia-based desulfurization.
The CO2 content in the gas is significantly reduced by the staged absorption ammonia method of the present invention. Specifically, the CO2 content in the process gas before decarbonization is 6-50 v %; preferably 8-40 v %; and more preferably 10-30 v %.
The CO2 content in the gas after the staged absorption ammonia-based treatment of the present invention is 0-10 v %; preferably 0-8 v %; and preferably 0-6 v %.
A method for staged absorption ammonia-based decarbonization protected by the present invention is preferably carried out in a device for staged absorption ammonia-based decarbonization defined by the present invention.
The beneficial effects of the invention are mainly reflected in decarbonization efficiency, ammonia escape, and production of ammonium bicarbonate fertilizer (abbreviated as ammonium bicarbonate). The decarbonization efficiency achieved by the method according to the invention is at least 60%, preferably at least 70%, and more preferably at least 80%. After decarbonization, the ammonia escape is smaller (800-5000 ppm), which can reduce the load of the ammonia escape control system, thereby reducing investment costs and operating costs. The ammonia escape after passing through the ammonia escape control system is ≤20 ppm, preferably 15 ppm, and more preferably 10 ppm. The solid content of ammonium bicarbonate in the ammonium bicarbonate generating zone is greater than 2 wt %, preferably greater than 5 wt %, and more preferably greater than 8 wt %. Meanwhile, the decarbonization device can partially absorb pollutant SO2 to obtain a lower SO2 concentration of less than 10 mg/Nm3, preferably less than 5 mg/Nm3, and more preferably less than 2 mg/Nm3.
Decarbonization efficiency=(Q1*w1−Q2*w2)/(Q1*w1)*100%
Q1 is the flow rate of dry flue gas under the standard state at the inlet of the decarbonization device, m3/h; w1 is the volume fraction of carbon dioxide in the flue gas at the inlet of the decarbonization device measured by the instrument, %; Q2 is the flow rate of dry flue gas under the standard state at the outlet of the decarbonization device, m3/h; and w2 is the volume fraction of carbon dioxide in the flue gas at the outlet of the decarbonization device measured by the instrument, %.
SO2 content in the gas may be determined according to HJ629-2011 Fixed Pollution Source Waste Gas—Determination of Sulfur Dioxide—Non-dispersive Infrared Absorption Method; the CO2 content may be determined according to HJ 870-2017 Fixed Pollution Source Waste Gas—Determination of Carbon Dioxide—Non-dispersive Infrared Absorption Method; and NH3 content may be tested according to HJ 533-2009 Determination of Ammonia in Ambient Air and Waste Gas—Nessler's Reagent Spectrophotometry.
Illustrative embodiments of apparatus and methods in accordance with the principles of the invention will now be described with reference to the accompanying drawings, which form a part hereof. It is to be understood that other embodiments may be utilized and that structural, functional and procedural modifications, additions or omissions may be made, and features of illustrative embodiments, whether apparatus or method, may be combined, without departing from the scope and spirit of the present invention.
The apparatus and methods may be include illustrative Example 1 and Comparative Examples 1 and 2 further illustrate the apparatus and the method and device for staged absorption ammonia-based decarbonization of the present invention.
Process gas 1 after ammonia-based desulfurization enters ammonium bicarbonate generating zone 2, and the solution is cooled down through ammonium bicarbonate generating zone circulating pump 3 and ammonium bicarbonate generating zone heat exchanger 4, and reacts with the flue gas to form ammonium bicarbonate. The ammonium bicarbonate solution/slurry is pumped into crystallizer 27 through ammonium bicarbonate discharge pump 26, and then passes through solid-liquid separation equipment 28 and packing machine 29 to obtain solid ammonium bicarbonate 30.
The gas further enters decarbonization absorption zone 6, which includes first-stage decarbonization absorption zone 7, second-stage decarbonization absorption zone 9, and third-stage decarbonization absorption zone 11 from bottom to top, and the zones are separated by liquid collectors. The liquid collector adopts a tray and gas cap structure, which allows the gas to pass through from bottom to top and collects the circulating liquid in the upper area. In the first-stage decarbonization absorption zone 7, the circulating liquid is cooled down through first-stage decarbonization absorption zone circulating pump 12 and first-stage decarbonization absorption zone heat exchanger 13, and contacts with the flue gas to absorb carbon dioxide, and part of the circulating liquid goes to the ammonium bicarbonate generating zone 2. The gas enters the second-stage decarbonization absorption zone 9 through liquid collector 8, and the circulating liquid is cooled down through second-stage decarbonization absorption zone circulating pump 14 and second-stage decarbonization absorption zone heat exchanger 15, and contacts with the flue gas to absorb carbon dioxide, and part of the circulating liquid goes to the first-stage decarbonization absorption zone 7. Ammonia 5 is fed into the first-stage decarbonization absorption zone 7 and the second-stage decarbonization absorption zone 9 through pipes. The gas enters the third-stage decarbonization absorption zone 11 through liquid collector 10, and the circulating liquid is cooled down through third-stage decarbonization absorption zone circulating pump 16 and third-stage decarbonization absorption zone heat exchanger 17, and contacts with the flue gas to absorb carbon dioxide, and part of the circulating liquid goes to the second-stage decarbonization absorption zone 9.
The gas continues to enter ammonia escape control system 18. The ammonia escape control system includes ammonia escape control system water washing zone 19 and ammonia escape control system acid washing zone 21 from bottom to top. The two zones are separated by a liquid collector. The liquid collector adopts a tray and gas cap structure, which allows the gas to pass through from bottom to top and collects the circulating liquid in the upper area. In the ammonia escape control system water washing zone 19, the circulating liquid is washed through circulating pump 22 in the ammonia escape control system water washing zone, and contacts with the flue gas to absorb free ammonia. The gas enters the ammonia escape control system acid washing zone 21 through liquid collector 20, circulating liquid 24 from the ammonia-based desulfurization system is used and contacts with the flue gas to absorb free ammonia, and the reacted solution (i.e., desulfurization circulating liquid) 23 returns to the desulfurization system. Flue gas after ammonia removal is discharged 25.
The temperature control reduces the temperature of the circulating liquid through a cold source, and the circulating liquid is in contact with the flue gas to reduce the temperature of the flue gas. For the cold source, a refrigerator is used to produce chilled water, and the chilled water cools down the circulating liquid through a plate heat exchanger. The circulating liquid is in spray contact with the flue gas to reduce the temperature of the flue gas. The temperature of the ammonium bicarbonate generating circulating liquid is controlled to be 20° C. to 25° C., and preferably 22° C. In the first stage, the temperature of the decarbonization absorption circulating liquid is higher than the temperature of the ammonium bicarbonate generating circulating liquid, and in the final stage, the temperature of the decarbonization absorption circulating liquid is lower than the temperature of the ammonium bicarbonate generating circulating liquid.
The pH control is through addition of ammonia and solution replacement between stages.
Ammonia is added to the first-stage and second-stage decarbonization absorption circulating liquids, and the amount of ammonia added to the second-stage decarbonization absorption circulating liquid accounts for 80−50 wt % of the total amount of ammonia added, preferably 60 wt %. No ammonia is added to the third-stage decarbonization absorption circulating liquid and ammonium bicarbonate generating circulating liquid.
Solution replacement is conducted through pipe overflow to transport the previous stage of circulating liquid to the next stage, which can control the solution composition and pH value. The pH value of the ammonium bicarbonate generating circulating liquid is lower than that of the decarbonization absorption circulating liquid, and the content of ammonium bicarbonate is greater than that of the decarbonization absorption circulating liquid.
In the decarbonization absorbing circulating liquid, the pH value is ≥8.0, preferably ≥8.2, more preferably ≥8.5, and most preferably ≥9.0.
The system operates under normal pressure (the actual pressure is slightly higher than the atmospheric pressure, and the specific pressure is shown in the table below), and no pressure control device is provided.
Among them, the solution composition and control conditions are shown in the following table:
Ammonia decarbonization adopts 99.6% anhydrous ammonia as absorbent, and the parameters of process gas 1 are shown in Table 1 below:
The main parameters of the process gas after being treated in the decarbonization absorption zone 6 are shown in Table 2 below:
The main parameters of the process gas after being treated by the ammonia washer 18 are shown in the following table:
Compared with Example 1, only the temperature control is different. The temperature control of the first- and second-stage decarbonization absorption zones is the same as that of the third stage, all being set at 20° C.
Because the temperature control of the first- and second-stage decarbonization absorption zones is relatively low, and the temperature difference relative to the cold source is reduced, the required heat exchange area of the heat exchanger 13 and the heat exchanger 14 increases, which increases equipment investment cost. Moreover, when the ambient temperature is 20° C., the cold sources of the first- and second-stage decarbonization absorption zone heat exchangers 13 and heat exchangers 15 in Example 1 can adopt cooling by air coolers using low-temperature ambient air to save operating costs. In Comparative Example 1, since the ambient temperature is the same as the target temperature and both are set to be 20° C., it is impossible to achieve cooling with an air cooler, and only chilled water with high energy consumption can be used for cooling.
Comparative Example 2, compared to Example 1, is only different in the addition of ammonia. Ammonia is added to the ammonium bicarbonate generating zone and the first, second and third decarbonization absorption zones at equivalent amounts.
Because the amount of ammonia added in the ammonium bicarbonate generating zone reaches 25 wt % of the total amount of ammonia added to the decarbonization process, ammonium bicarbonate cannot be generated in the solution, and ammonium bicarbonate crystals cannot be obtained. The amount of ammonia added in the third-stage decarbonization absorption zone reaches which leads to a large increase in decarbonization ammonia escape, and the ammonia escape of the process gas after treatment in the decarbonization absorption zone 6 reaches 6000 ppm.
As can be seen from the comparison of the example of the present invention and comparative examples as described above, through the staged solution composition control and reaction condition control by the processing with the method and device of the present invention, it is possible to achieve efficient decarbonization while controlling ammonia escape, thereby achieving excellent technical effects and economic effects.
All ranges and parameters disclosed herein shall be understood to encompass any and all subranges subsumed therein, every number between the endpoints, and the endpoints. For example, a stated range of “1 to 10” should be considered to include any and all subranges between (and inclusive of) the minimum value of 1 and the maximum value of 10; that is, all subranges beginning with a minimum value of 1 or more (e.g. 1 to 6.1), and ending with a maximum value of 10 or less (e.g., 2.3 to 9.4, 3 to 8, 4 to 7), and finally to each number 1, 2, 3, 4, 5, 6, 7, 8, 9, and 10 contained within the range.
Thus, apparatus and methods for staged absorption ammonia-based decarbonization have been provided. Persons skilled in the art will appreciate that the present invention may be practiced by other than the described embodiments, which are presented for purposes of illustration rather than of limitation. The present invention is limited only by the claims that follow.
| Number | Date | Country | Kind |
|---|---|---|---|
| 202210553874.4 | May 2022 | CN | national |
