Abstract:
A system and a process for capture and absorption of sulfur dioxide and carbon dioxide by an ammonia method at normal pressure are disclosed. The system has a dilute ammonia water supply device connected with sulfur dioxide and carbon dioxide absorption devices; an induced draft fan is connected with a heat exchanger connected with the sulfur dioxide absorption device; a sulfur dioxide absorption tower is connected with a carbon dioxide absorption tower; cooling devices in the sulfur dioxide and carbon dioxide absorption towers share a cooling water inlet and outlet pipe; the sulfur dioxide and carbon dioxide absorption devices respectively restore ammonia concentration to original ammonia water concentration by supplementing concentrated ammonia water; the sulfur dioxide and carbon dioxide absorption devices respectively pump solutions into the heat exchangers, then the solutions enter crystallization tanks; solid-liquid separation is performed through centrifuges, and the liquid continues to circulate in the system.

Description:
CROSS REFERENCE OF RELATED APPLICATION 
       [0001]    This is a U.S. National Stage under 35 U.S.C 371 of the International Application PCT/CN2012/071026, filed Feb. 10, 2012, which claims priority under 35 U.S.C. 119(a-d) to CN 201120040452.4 and CN 201110039363.2, filed Feb. 16, 2011. 
     
    
     BACKGROUND OF THE PRESENT INVENTION 
       [0002]    1. Field of Invention 
         [0003]    The present invention relates to a field of chemical or biological purification of waste gas by gas-liquid contact, and in particular, relates to a system and a process for capture and absorption of sulfur dioxide and carbon dioxide by an ammonia method at normal pressure. 
         [0004]    2. Description of Related Arts 
         [0005]    At present, the emission reduction of sulfur dioxide and carbon dioxide is in general performed separately, that is, first perform desulfurization and then perform decarbonization. The flue gas desulfurization techniques mainly include limestone-gypsum wet method, rotary spraying semi-dry method, in-furnace limestone injection and tail-section humidifying activation, seawater desulfurization, electron beam desulfurization, circulating fluidized bed flue gas desulfurization, and the like. Among which, the wet -type limestone method is at present the most widely used tail-section flue gas desulfurization technique around the world. In this technique lime slurry or lime is used to absorb sulfur dioxide in the flue gas in an absorption tower, resulting in the products of calcium sulfite and calcium sulfate, with the desulfurization efficiency of 75%-95%. The main problems of this method are the low dissolubility and utilization efficiency of absorption agent (lime or limestone), and large amounts of ash produced, causing the desulfurization equipment and pipeline prone to scaling and plugging, and it also produces secondary pollution caused by the process products. In the dry and the semi-dry desulfurization methods, due to the short contact time between the absorption agent and the flue gas, the desulfurization efficiency is generally in the range of 50%-75%, a low desulfurization efficiency, and there is also secondary pollution of solid pollutants. The recovery methods mainly include Wellman-Lord method, activated carbon method, ammonia method, and the like. In the Wellman-Lord method, sodium sulfite is used as the absorption agent, and the desulfurization efficiency can reach 95%, but the investment and operation costs are relatively high. In the activated carbon method, although the desulfurization efficiency can reach 98%, the process is complex, along with great technical difficulty and high consumption of activated carbon. In the ammonia method, the desulfurization efficiency is generally in the range of 95%-99%, the desulfurization product can be directly used as fertilizer, and no waste water or other wastes are produced. The ammonia method has incomparable advantages over other techniques, but this method often has the problem of relatively high loss of ammonia in the tail gas, which may directly lower the desulfurization efficiency. The carbon reduction techniques both at home and abroad mainly include absorption method, adsorption method, membrane separation method, storage method, and the like, but there are certain shortcomings for each of these methods. 
       SUMMARY OF THE INVENTION 
       [0006]    The present invention aims at providing a system and a process for capture and absorption of sulfur dioxide and carbon dioxide by an ammonia method at normal pressure, which have the advantages of high desulfurization and carbon reduction efficiency, simple process flow, simplified system structure, and low investment and operation costs. 
         [0007]    In order to realize the above-mentioned scheme, the technical solution of the present invention is set as follows. A system for the capture and absorption of sulfur dioxide and carbon dioxide by an ammonia method at normal pressure comprises a dilute ammonia water supply device, a sulfur dioxide absorption device, and a carbon dioxide absorption device. Wherein the sulfur dioxide absorption device comprises a normal-pressure sulfur dioxide absorption tower, a second heat exchanger, a sulfur dioxide crystallization tank, an ammonium sulfate product centrifuge, a first mother liquor tank, a fifth and a sixth pumps, wherein the sulfur dioxide absorption tower comprises a first tank body, a first cooling device positioned inside the first tank body, and a first and a second spraying devices positioned inside and at the upper part and the middle part of the first tank body respectively. The carbon dioxide absorption device comprises a normal-pressure carbon dioxide absorption tower, a third heat exchanger, a carbon dioxide crystallization tank, an ammonium bicarbonate product centrifuge, a second mother liquor tank, a seventh and an eighth pumps, wherein the carbon dioxide absorption tower comprises a second tank body, a second cooling device positioned inside the second tank body, and a third and a fourth spraying devices positioned inside and at the upper part and the middle part of the second tank body respectively. The dilute ammonia water supply device is respectively connected with the first and the third spraying devices through pipelines, an induced draft fan is connected with the gas inlet of a first heat exchanger through a pipeline, the exhaust port of the first heat exchanger extends into the lower part of an inner cavity of the first tank body through a pipeline, the bottom of the first tank body is connected with the inlet of the fifth pump through a pipeline, the outlet of the fifth pump is connected with the inlet of the second heat exchanger through a pipeline, the outlet of the second heat exchanger is connected with the inlet of the sulfur dioxide crystallization tank through a pipeline, the outlet of the sulfur dioxide crystallization tank is connected with the inlet of the ammonium sulfate product centrifuge through a pipeline, the outlet of the ammonium sulfate product centrifuge is connected with the inlet of the first mother liquor tank through a pipeline, the outlet of the first mother liquor tank is connected with the sixth pump through a pipeline, the sixth pump is connected with the second spraying device through a pipeline, a first pipeline is connected between the inlets of the fifth and the sixth pumps, a high-concentration ammonia water storage tank is respectively connected with the inlets of the first and the second pumps through pipelines, the outlets of the first and the second pumps are respectively connected with the second and the fourth spraying devices, the upper part of the first tank body is communicated with the lower part of the inner cavity of the second tank body through an exhaust pipe, the first and the second cooling water inlet pipes on the first and the second cooling devices are connected together with a cooling water inlet pipe of the first heat exchanger, the first and the second cooling water outlet pipes on the first and the second cooling devices are connected together with a cooling water outlet pipe of the first heat exchanger, the first and the second regulating valves are respectively arranged on the first and the second cooling water inlet pipes, the bottom of the second tank body is connected with the inlet of the seventh pump through a pipeline, the outlet of the seventh pump is connected with the inlet of the third heat exchanger through a pipeline, the outlet of the third heat exchanger is connected with the inlet of the carbon dioxide crystallization tank through a pipeline, the outlet of the carbon dioxide crystallization tank is connected with the inlet of the ammonium bicarbonate product centrifuge through a pipeline, the outlet of the ammonium bicarbonate product centrifuge is connected with the inlet of the second mother liquor tank through a pipeline, the outlet of the second mother liquor tank is connected with the eighth pump through a pipeline, the eighth pump is connected with the fourth spraying device through a pipeline, and a second pipeline is connected between the inlets of the seventh and the eighth pumps. 
         [0008]    According to the system of the present invention for the capture and absorption of sulfur dioxide and carbon dioxide by the ammonia method at normal pressure, the dilute ammonia water supply device comprises a dilute ammonia water storage tank, and a third and a fourth pumps, wherein the dilute ammonia water storage tank is respectively connected with the inlets of the third and the fourth pumps through pipelines, the outlets of the third and the fourth pumps are respectively connected with the first and the third spraying devices, and the first and the second valves are respectively arranged on the pipelines between the dilute ammonia water storage tank and the third and the fourth pumps. 
         [0009]    A process for capture and absorption of sulfur dioxide and carbon dioxide by an ammonia method at normal pressure comprises following steps of: 
         [0010]    (1) pumping flue gas of coal-fired power plant after dedusting treatment into a first heat exchanger via an induced draft fan, and cooling the flue gas through the first heat exchanger to a temperature required by a production process; 
         [0011]    (2) letting the flue gas of the coal-fired power plant after dedusting and cooling treatment enter a sulfur dioxide absorption tower from the first heat exchanger via a bottom of the sulfur dioxide absorption tower, pumping dilute ammonia water absorption solution capable of capturing and absorbing sulfur dioxide from a dilute ammonia water storage tank into a first spraying device of the sulfur dioxide absorption tower through a third pump and spraying the dilute ammonia water absorption solution downward, thus allowing the flue gas and the dilute ammonia water absorption solution to be in countercurrent contact to undergo gas-liquid dual-phase reaction, and generating an ammonium sulfate solution through absorption of sulfur dioxide, wherein a chemical reaction takes place in two processes: a first process of chemical reaction between the dilute ammonia water and the sulfur dioxide to generate ammonium sulfite, and a second process of chemical reaction between the ammonium sulfite and the ammonia water to generate ammonium sulfate; and then letting the flue gas after a removal of sulfur dioxide enter a carbon dioxide absorption tower through an exhaust pipe; 
         [0012]    (3) stopping an injection of the dilute ammonia water absorption solution into the sulfur dioxide absorption tower when unsaturated ammonium sulfate solution in the sulfur dioxide absorption tower reaches a liquid level required by the process; 
         [0013]    (4) when spraying downward the dilute ammonia water absorption solution through the first spraying device of the sulfur dioxide absorption tower, pumping the ammonium sulfate solution in the sulfur dioxide absorption tower into a second heat exchanger via a fifth pump for cooling, then sending into a sulfur dioxide crystallization tank, further sending saturated ammonium sulfate crystalline solid and the unsaturated ammonium sulfate solution together into an ammonium sulfate product centrifuge through a pipeline for solid-liquid separation, separating out crystalline solids of ammonium sulfate fertilizer, discharging remaining unsaturated ammonium sulfate solution into a first mother liquor tank through the pipeline, then sucking out and pumping into a second spraying device of the sulfur dioxide absorption tower through a sixth pump for downward spraying, further pumping the unsaturated ammonium sulfate solution at the bottom of the sulfur dioxide absorption tower directly into the second spraying device of the sulfur dioxide absorption tower for downward spraying through the sixth pump on a first pipeline, and allowing countercurrent absorption reaction to occur between the sulfur dioxide gas in the flue gas inside the sulfur dioxide absorption tower and the downward sprayed absorption solutions which include the unsaturated ammonium sulfate solution and the previously sprayed dilute ammonia water absorption solution, with both solutions working either simultaneously or separately, thus achieving absorption of sulfur dioxide and turning the ammonium sulfate solution from the unsaturated solution into the saturated solution; 
         [0014]    (5) pumping high-concentration ammonia water from the high-concentration ammonia water storage tank through a first pump, and supplementing the high-concentration ammonia water into the sulfur dioxide absorption tower in which the separation of ammonium sulfate fertilizer product has been completed, thus restoring the concentration of the solution in the sulfur dioxide absorption tower to a concentration level of the dilute ammonia water absorption solution as at the beginning; 
         [0015]    (6) allowing the flue gas of the coal-fired power plant after the sulfur dioxide removal treatment, which is exhausted from the exhaust pipe at an upper part of the sulfur dioxide absorption tower, to enter the carbon dioxide absorption tower from the bottom, pumping the dilute ammonia water absorption solution capable of capturing and absorbing carbon dioxide from the dilute ammonia water storage tank into the third spraying device of the carbon dioxide absorption tower through a fourth pump and spraying downward, letting the flue gas and the dilute ammonia water absorption solution be in countercurrent contact to undergo gas-liquid dual-phase reaction, and generating an ammonium bicarbonate solution through the absorption of carbon dioxide, and then exhausting the flue gas after the removal of sulfur dioxide and carbon dioxide through the pipeline at a top of the carbon dioxide absorption tower; 
         [0016]    (7) stopping the injection of the dilute ammonia water absorption solution into the carbon dioxide absorption tower when the unsaturated ammonium bicarbonate solution in the carbon dioxide absorption tower reaches the liquid level required by the process; 
         [0017]    (8) when spraying downward the dilute ammonia water absorption solution through the third spraying device of the carbon dioxide absorption tower, pumping the ammonium bicarbonate solution in the carbon dioxide absorption tower into the third heat exchanger via a seventh pump for cooling, then sending into the carbon dioxide crystallization tank, further sending the saturated ammonium bicarbonate crystalline solid and the unsaturated ammonium bicarbonate solution together into the ammonium bicarbonate product centrifuge through the pipeline for solid-liquid separation, separating out the crystalline solid of ammonium bicarbonate fertilizer, discharging the remaining unsaturated ammonium bicarbonate solution into a second mother liquor tank through the pipeline, then sucking out and pumping into a fourth spraying device of the carbon dioxide absorption tower through an eighth pump for downward spraying, enabling the unsaturated ammonium bicarbonate solution at the bottom of the carbon dioxide absorption tower to pass through the second pipeline, and directly pumping into the fourth spraying device of the carbon dioxide absorption tower for downward spraying through the eighth pump on the second pipeline, and allowing countercurrent absorption reaction to occur between carbon dioxide gas in the flue gas inside the carbon dioxide absorption tower and the downward sprayed absorption solutions which include the unsaturated ammonium bicarbonate solution and the previously sprayed dilute ammonia water absorption solution, with both solutions working either simultaneously or separately, thus achieving the absorption of carbon dioxide and turning the ammonium bicarbonate solution from the unsaturated solution to the saturated solution; 
         [0018]    (9) pumping the high-concentration ammonia water from the high-concentration ammonia water storage tank through the second pump, and supplementing the high-concentration ammonia water into the carbon dioxide absorption tower in which the separation of ammonium bicarbonate fertilizer product has been completed, thus restoring the concentration of the solution in the carbon dioxide absorption tower to the concentration level of the dilute ammonia water absorption solution as at the beginning; 
         [0019]    (10) repeating the above steps in a circulating manner. 
         [0020]    According to the process of the present invention for the capture and absorption of sulfur dioxide and carbon dioxide by the ammonia method at normal pressure, the reaction temperature in the sulfur dioxide absorption tower is controlled to be within the range of 65-80° C. through the first cooling device, and the reaction temperature in the carbon dioxide absorption tower is controlled to be within the range of 40-50° C. through the second cooling device. 
         [0021]    According to the process of the present invention for the capture and absorption of sulfur dioxide and carbon dioxide by the ammonia method at normal pressure, the concentration of the dilute ammonia water solution in either of the sulfur dioxide absorption tower and the carbon dioxide absorption tower is controlled to be within the range of 6%-8% by mass. 
         [0022]    By adopting the above scheme, according to the system and the process of the present invention for the capture and absorption of sulfur dioxide and carbon dioxide by the ammonia method at normal pressure, the sulfur dioxide absorption tower and the carbon dioxide absorption tower are employed to allow sulfur dioxide and carbon dioxide in the flue gas of the coal-fired power plant to respectively undergo countercurrent contact and thorough reaction with the dilute ammonia water absorption solution, and respectively generate the ammonium sulfate solution and the ammonium bicarbonate solution; the produced unsaturated ammonium sulfate solution and the ammonium bicarbonate solution are to be used in a flexible manner, the processing step of supplementing the high-concentration ammonia water is added, and the cooling devices are arranged in the sulfur dioxide absorption tower and the carbon dioxide absorption tower; so that the production working conditions required by the process can be well controlled, the sulfur dioxide and carbon dioxide gas in the flue gas of the coal-fired power plant can be well captured and absorbed, the desulfurization and carbon reduction efficiency is high, the emission of the sulfur dioxide and carbon dioxide greenhouse gas is reduced, the ammonium sulfate and ammonium bicarbonate fertilizers are simultaneously produced; the unique design of the process pipeline can enable the capture system to operate flexibly, reduce the power consumption during the operation of the system, and meanwhile, more effectively enhance the capture and absorption capability of the sulfur dioxide and carbon dioxide gas in the flue gas of the coal-fired power plant; and the system and the process of the present invention have simple process flow, simplified system structure, and low investment and operation costs. 
         [0023]    These and other objectives, features, and advantages of the present invention will become apparent from the following detailed description, the accompanying drawings, and the appended claims. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0024]    The FIGURE is a structural diagram of a system for capture and absorption of sulfur dioxide and carbon dioxide by an ammonia method at normal pressure according to a preferred embodiment of the present invention. 
       
    
    
       [0025]    The present invention is further described through the following embodiments with the combination of the accompanying drawings. 
       DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT 
       [0026]    As shown in FIGURE, a system for capture and absorption of sulfur dioxide and carbon dioxide by an ammonia method at normal pressure comprises a dilute ammonia water supply device  1 , an induced draft fan  2 , a first heat exchanger  3 , a high-concentration ammonia water storage tank  4 , a first pump  5 , a second pump  6 , a sulfur dioxide absorption device  7 , and a carbon dioxide absorption device  8 . 
         [0027]    The dilute ammonia water supply device  1  comprises a dilute ammonia water storage tank  11 , a third pump  12 , and a fourth pump  13 ; the dilute ammonia water storage tank  11  is respectively connected with the inlets of the third pump  12  and the fourth pump  13  through pipelines, and a first valve  30  and a second valve  40  are respectively arranged on the pipelines between the dilute ammonia water storage tank  11  and the third and the fourth pumps  12 ,  13 . 
         [0028]    The sulfur dioxide absorption device  7  comprises a normal-pressure sulfur dioxide absorption tower  71 , a second heat exchanger  72 , a sulfur dioxide crystallization tank  73 , an ammonium sulfate product centrifuge  74 , a first mother liquor tank  75 , a fifth pump  76  and a sixth pump  77 , wherein the sulfur dioxide absorption tower  71  comprises a first tank body  711 , a first cooling device  712  positioned inside the first tank body  711 , and a first spraying device  713  and a second spraying device  714  which are positioned at the upper part and the middle part of the first tank body  711  and the outlet of the third pump  12  is connected with the first spraying device  713  through a pipeline. 
         [0029]    The carbon dioxide absorption device  8  comprises a normal-pressure carbon dioxide absorption tower  81 , a third heat exchanger  82 , a carbon dioxide crystallization tank  83 , an ammonium bicarbonate product centrifuge  84 , a second mother liquor tank  85 , a seventh pump  86 , and an eighth pump  87 , wherein the carbon dioxide absorption tower  81  comprises a second tank body  811 , a second cooling device  812  positioned inside the second tank body  811 , and a third spraying device  813  and a fourth spraying devices  814  positioned at the upper part and the middle part of the second tank body  811 ; and the outlet of the fourth pump  13  is connected with the third spraying device  813  through a pipeline. 
         [0030]    The induced draft fan  2  is connected with the gas inlet of the first heat exchanger  3  through a pipeline, the exhaust port of the first heat exchanger  3  extends into the lower part of an inner cavity of the first tank body  711  through a pipeline, the bottom of the first tank body  711  is connected with the inlet of the fifth pump  76  through a pipeline, the outlet of the fifth pump  76  is connected with the inlet of the second heat exchanger  72  through a pipeline, the outlet of the second heat exchanger  72  is connected with the inlet of the sulfur dioxide crystallization tank  73  through a pipeline, the outlet of the sulfur dioxide crystallization tank  73  is connected with the inlet of the ammonium sulfate product centrifuge  74  through a pipeline, the outlet of the ammonium sulfate product centrifuge  74  is connected with the inlet of the first mother liquor tank  75  through a pipeline, the outlet of the first mother liquor tank  75  is connected with the sixth pump  77  through a pipeline, the sixth pump  77  is connected with the second spraying device  714  through a pipeline, a first pipeline  9  is connected between the inlets of the fifth pump  76  and the sixth pump  77 ; the high-concentration ammonia water storage tank  4  is respectively connected with the inlets of the first pump  5  and the second pump  6  through pipelines, the outlets of the first pump  5  and the second pump  6  are respectively connected with the second spraying device  714  and the fourth spraying device  814 ; the upper part of the first tank body  711  is communicated with the lower part of the inner cavity of the second tank body  811  through an exhaust pipe  7111 , a first cooling water inlet pipe  7121  of the first cooling device  712  and a second cooling water inlet pipe  8121  of the second cooling device  812  are respectively connected with a cooling water inlet pipe  31  of the first heat exchanger  3 ; a first cooling water outlet pipe  7122  of the first cooling device  712  and a second cooling water outlet pipe  8122  of the second cooling device  812  are respectively connected with a cooling water outlet pipe  32  of the first heat exchanger  3 ; a first regulating valve  10  and a second regulating valve  50  are respectively arranged on the first cooling water inlet pipe  7121  and the second cooling water inlet pipe  8121 ; the bottom of the second tank body  811  is connected with the inlet of the seventh pump  86  through a pipeline, the outlet of the seventh pump  86  is connected with the inlet of the third heat exchanger  82  through a pipeline, the outlet of the third heat exchanger  82  is connected with the inlet of the carbon dioxide crystallization tank  83  through a pipeline, the outlet of the carbon dioxide crystallization tank  83  is connected with the inlet of the ammonium bicarbonate product centrifuge  84  through a pipeline, the outlet of the ammonium bicarbonate product centrifuge  84  is connected with the inlet of the second mother liquor tank  85  through a pipeline, the outlet of the second mother liquor tank  85  is connected with the eighth pump  87  through a pipeline, the eighth pump  87  is connected with the fourth spraying device  814  through a pipeline, and a second pipeline  20  is connected between the inlet of the seventh pump  86  and the inlet of the eighth pump  87 . 
         [0031]    A process employing the system described above for capture and absorption of sulfur dioxide and carbon dioxide comprises following steps of: 
         [0032]    (1) pumping flue gas of coal-fired power plant after dedusting treatment into a first heat exchanger  3  via an induced draft fan  2 , and cooling through the first heat exchanger  3  to a temperature required by a production process; 
         [0033]    (2) letting the flue gas of the coal-fired power plant after dedusting and cooling treatment enter an inner cavity of a sulfur dioxide absorption tower  71  via the first heat exchanger  3  and a bottom of the sulfur dioxide absorption tower  71 , pumping dilute ammonia water absorption solution capable of capturing and absorbing sulfur dioxide, from a dilute ammonia water storage tank  11  into a first spraying device  713  of the sulfur dioxide absorption tower  71  through a third pump  12  and spraying downward; controlling a reaction temperature in the sulfur dioxide absorption tower  71  to be within a range of 65-80° C. through a first cooling device  712 , wherein specifically the reaction temperature of the solution in the sulfur dioxide absorption tower  71  is controlled by regulating a circulation quantity of water through a first regulating valve  10  on a first cooling water inlet pipe  7121  of the first cooling device  712 ; thus allowing the flue gas and the dilute ammonia water absorption solution to be in countercurrent contact to undergo gas-liquid dual-phase reaction, and generating an ammonium sulfate solution through absorption of sulfur dioxide, wherein a chemical reaction takes place in two processes: a first process of chemical reaction between the dilute ammonia water and sulfur dioxide to generate ammonium sulfite, and a second process of chemical reaction between the ammonium sulfite and the ammonia water to generate ammonium sulfate; and then letting the flue gas after a removal of sulfur dioxide enter a carbon dioxide absorption tower  81  through an exhaust pipe  7111 ; 
         [0034]    (3) stopping an injection of the dilute ammonia water absorption solution into the sulfur dioxide absorption tower  71  when unsaturated ammonium sulfate solution in the sulfur dioxide absorption tower  71  reaches a liquid level required by the process; 
         [0035]    (4) when spraying downward the dilute ammonia water absorption solution through the first spraying device  713  of the sulfur dioxide absorption tower  71 , pumping the ammonium sulfate solution in the sulfur dioxide absorption tower  71  into a second heat exchanger  72  via a fifth pump  76  for cooling, then sending into a sulfur dioxide crystallization tank  73 , further sending saturated ammonium sulfate crystalline solid and the unsaturated ammonium sulfate solution together into an ammonium sulfate product centrifuge  74  through a pipeline for solid-liquid separation, separating out the crystalline solid of ammonium sulfate fertilizer, discharging the remaining unsaturated ammonium sulfate solution into a first mother liquor tank  75  through the pipeline, then sucking out and pumping into a second spraying device  714  of the sulfur dioxide absorption tower  71  through a sixth pump  77  for downward spraying, enabling the unsaturated ammonium sulfate solution at the bottom of the sulfur dioxide absorption tower  71  to pass through a first pipeline  9 , and directly pumping into the second spraying device  714  of the sulfur dioxide absorption tower  71  for downward spraying through the sixth pump  77  on the first pipeline  9 , and allowing countercurrent absorption reaction to occur between the sulfur dioxide gas in the flue gas inside the sulfur dioxide absorption tower  71  and the downward sprayed absorption solutions which include the unsaturated ammonium sulfate solution and the previously sprayed dilute ammonia water absorption solution, with both solutions working either simultaneously or separately, thus achieving absorption of sulfur dioxide and turning the ammonium sulfate solution from the unsaturated solution to the saturated solution; 
         [0036]    (5) pumping high-concentration ammonia water from a high-concentration ammonia water storage tank  4  through a first pump  5 , and supplementing the high-concentration ammonia water into the sulfur dioxide absorption tower  71  in which the separation of ammonium sulfate fertilizer product has been completed, thus restoring the concentration of the solution in the sulfur dioxide absorption tower  71  to a concentration level of the dilute ammonia water absorption solution as at the beginning, which is 6%-8% by mass; 
         [0037]    (6) allowing the flue gas of the coal-fired power plant after the sulfur dioxide removal treatment to enter the carbon dioxide absorption tower  81  from the bottom, pumping the dilute ammonia water absorption solution capable of capturing and absorbing carbon dioxide from the dilute ammonia water storage tank  11  into a third spraying device  813  of the carbon dioxide absorption tower  81  through a fourth pump  13  and spraying downward, controlling the reaction temperature in the carbon dioxide absorption tower  81  to be within the range of 40-50° C. through a second cooling device  812 , wherein specifically the reaction temperature of the solution in the carbon dioxide absorption tower  81  is controlled by regulating the circulation quantity of the water through a second regulating valve  50  on a second cooling water inlet pipe  8121  of the second cooling device  812 , thus allowing the flue gas and the dilute ammonia water absorption solution to be in countercurrent contact to undergo gas-liquid dual-phase reaction, and generating an ammonium bicarbonate solution through absorption of carbon dioxide, and then exhausting the flue gas after the removal of sulfur dioxide and carbon dioxide through the pipeline at a top of the carbon dioxide absorption tower  81 ; 
         [0038]    (7) stopping the injection of the dilute ammonia water absorption solution into the carbon dioxide absorption tower  81  when the unsaturated ammonium bicarbonate solution in the carbon dioxide absorption tower  81  reaches the liquid level required by the process; 
         [0039]    (8) when spraying downward the dilute ammonia water absorption solution through the third spraying device  813  of the carbon dioxide absorption tower  81 , pumping the ammonium bicarbonate solution in the carbon dioxide absorption tower  81  into a third heat exchanger  82  via a seventh pump  86  for cooling, then sending into a carbon dioxide crystallization tank  83 , further sending the saturated ammonium bicarbonate crystalline solid and the unsaturated ammonium bicarbonate solution together into an ammonium bicarbonate product centrifuge  84  through the pipeline for solid-liquid separation, separating out the crystalline solid of ammonium bicarbonate fertilizer, discharging the remaining unsaturated ammonium bicarbonate solution into a second mother liquor tank  85  through the pipeline, then sucking out and pumping into a fourth spraying device  814  of the carbon dioxide absorption tower  81  through an eighth pump  87  for downward spraying, enabling the unsaturated ammonium bicarbonate solution at the bottom of the carbon dioxide absorption tower  81  to pass through a second pipeline  20 , and directly pumping into the fourth spraying device  814  of the carbon dioxide absorption tower  81  for downward spraying through the eighth pump  87  on the second pipeline  20 , and allowing countercurrent absorption reaction to occur between the carbon dioxide gas in the flue gas inside the carbon dioxide absorption tower  81  and the downward sprayed absorption solutions which include the unsaturated bicarbonate solution and the previously sprayed dilute ammonia water absorption solution, with both solutions working either simultaneously or separately, thus achieving the absorption of carbon dioxide and turning the ammonium bicarbonate solution from the unsaturated solution to the saturated solution; 
         [0040]    (9) pumping the high-concentration ammonia water from the high-concentration ammonia water storage tank  4  through a second pump  6 , and supplementing the high-concentration ammonia water into the carbon dioxide absorption tower  81  in which the separation of ammonium bicarbonate fertilizer product has been completed, thus restoring the concentration of the solution in the carbon dioxide absorption tower  81  to the concentration level of the dilute ammonia water absorption solution as at the beginning, which is 6%-8% by mass; and 
         [0041]    (10) repeating the above steps in a circulating manner. 
         [0042]    According to the system and the process for the capture and absorption of sulfur dioxide and carbon dioxide by the ammonia method at normal pressure of the present invention, the sulfur dioxide absorption tower  71  and the carbon dioxide absorption tower  81  are employed to allow sulfur dioxide and carbon dioxide in the flue gas of the coal-fired power plant to respectively undergo countercurrent contact and thorough reaction with the dilute ammonia water absorption solution, and respectively generate the ammonium sulfate solution and the ammonium bicarbonate solution; the produced unsaturated ammonium sulfate solution and the ammonium bicarbonate solution are to be used in a flexible manner, the processing step of supplementing the high-concentration ammonia water is added, and the first cooling device  712  and the second cooling device  812  are respectively arranged in the sulfur dioxide absorption tower  71  and the carbon dioxide absorption tower  81 ; so that the production working conditions required by the process can be well controlled, the sulfur dioxide and carbon dioxide gas in the flue gas of the coal-fired power plant can be well captured and absorbed, the desulfurization and carbon reduction efficiency is high, the emission of the sulfur dioxide and carbon dioxide greenhouse gas is reduced, the ammonium sulfate and ammonium bicarbonate fertilizers are simultaneously produced; the unique design of the process pipeline can enable the capture system to operate flexibly, reduce the power consumption during the operation of the system, and meanwhile, more effectively enhance the capture and absorption capability of the sulfur dioxide and carbon dioxide gas in the flue gas of the coal-fired power plant; and the system and the process of the present invention have simple process flow, simplified system structure, and low investment and operation costs. 
         [0043]    The above embodiments are merely used for describing the preferential ways of implementation of the present invention, and do not impose any limits on the scope of the invention; and on the premise of not deviating from the design spirit of the present invention, various deformations and improvements to the technical scheme of the invention made by those skilled in the field shall fall within the protection scope of the present invention defined by the claims. 
       INDUSTRIAL APPLICABILITY 
       [0044]    The system and the process for the capture and absorption of sulfur dioxide and carbon dioxide by the ammonia method at normal pressure of the present invention are mainly applied to flue gas purification and emission reduction of sulfur dioxide and carbon dioxide in the coal-fired power plant, the sulfur dioxide and carbon dioxide gas in the flue gas of the coal-fired power plant can be well captured and absorbed, the desufurization and carbon reduction efficiency is high, the emission of the sulfur dioxide and carbon dioxide greenhouse gas is reduced, and the ammonium sulfate and the ammonium bicarbonate fertilizers are simultaneously produced, so that the industrial applicability is very high. 
         [0045]    One skilled in the art will understand that the embodiment of the present invention as shown in the drawings and described above is exemplary only and not intended to be limiting. 
         [0046]    It will thus be seen that the objects of the present invention have been fully and effectively accomplished. Its embodiments have been shown and described for the purposes of illustrating the functional and structural principles of the present invention and is subject to change without departure from such principles. Therefore, this invention includes all modifications encompassed within the spirit and scope of the following claims.