CN112044249B - Carbon dioxide tail gas absorbing device and method for carbon dioxide decomposition reaction - Google Patents
Carbon dioxide tail gas absorbing device and method for carbon dioxide decomposition reaction Download PDFInfo
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Abstract
一种碳解反应二氧化碳尾气吸收装置及其吸收方法，所属化工领域，装置包括一级射流吸收罐，第一动力流体泵、二级射流吸收罐、第二动力流体泵、喷淋吸收罐和第三动力流体泵；一级射流吸收罐和二级射流吸收罐内部分别设置有耦合分配器和射流器，喷淋吸收罐内部设置有一级淋洗器、第一填料区、第二填料区、第一喷淋圈和第二喷淋圈。本发明方法利用二级射流一级喷淋联合吸收，并采用两层淋洗回收，能够大幅度提高CO2吸收率；采用射流搅拌方式，加快吸收，生成的NaHCO3直接用于碳解反应而不必分离，从而缩短碳解反应时间；本发明装置内部没有转动设备部件，结构简单、操作方便、设备成本低、维修方便，综合节能达到20％。
A carbon decomposition reaction carbon dioxide tail gas absorption device and an absorption method thereof, belonging to the field of chemical industry, the device comprises a primary jet absorption tank, a first power fluid pump, a secondary jet absorption tank, a second power fluid pump, a spray absorption tank and a third power fluid pump; the primary jet absorption tank and the secondary jet absorption tank are respectively provided with a coupling distributor and an ejector, and the spray absorption tank is provided with a primary leacher, a first filler area, a second filler area, a first spray circle and a second spray circle. The method of the present invention utilizes a secondary jet and a primary spray for combined absorption, and adopts a two-layer leaching recovery, which can greatly improve the CO2 absorption rate; the jet stirring method is adopted to accelerate the absorption, and the generated NaHCO3 is directly used for the carbon decomposition reaction without separation, thereby shortening the carbon decomposition reaction time; there is no rotating equipment component inside the device of the present invention, the structure is simple, the operation is convenient, the equipment cost is low, the maintenance is convenient, and the comprehensive energy saving reaches 20%.
Description
Technical Field
The invention belongs to the field of chemical industry, and particularly relates to a carbon dioxide tail gas absorption device and an absorption method thereof for a carbon dioxide decomposition reaction.
Background
Borax production by processing boron magnesium ore with carbon alkali method is a gas, liquid and solid three-phase reaction. The reaction consisted of five steps: 1. CO 2 Diffusion enters a gas-liquid interface through a gas film; 2. CO 2 Dissolving in liquid phase, and diffusing into liquid phase body through liquid film; 3. dissolved CO 2 React with alkali to generate HCO 3 - ；4、HCO 3 - And dissolved part of CO 2 Then the powder is diffused to the surface of the mineral powder through a liquid film between liquid phases, and if the cooked mineral powder is loose and porous, the powder also needs to enter the interior of the mineral powder through the diffusion in a capillary; 5. HCO (hydrogen chloride) 3 - And dissolved part of CO 2 Reacting with minerals. In these five reaction steps, HCO 3 - And dissolving CO 2 The reaction with the fine ground boron magnesium ore is the slowest step. Thus, the carbon alkali method has the following disadvantages: 1. the reaction time is long, generally 18-20 hours; 2. the leaching (decomposition) rate of boron is lower than that of the pressurized alkaline method by more than 5 percent; 3. CO 2 The utilization rate is low, generally only 50% -60%; 4. the equipment utilization rate is low and the energy consumption is high.
Currently, in the prior art, CO 2 The recycling method includes physical absorption method, chemical absorption method, adsorption separation method, etc., and the recycling method uses an absorption tower and an analysis tower to realize recycling, so that the problems of complicated equipment and complex operation are existed. CO 2 The recycling method also has a membrane separation method, and the membrane separation method needs pretreatment, and has the problems of expensive equipment and high cost. Because of these COs 2 The recovery method has respective problems, so the method for producing borax by the carbonization method is not used for CO all the time 2 Recycling.
Thus, the first and second substrates are bonded together,CO enhancement 2 The utilization rate, the material consumption and the energy consumption are reduced, the reaction time for preparing borax is shortened, and the problem that borax is not solved by a carbonization method is solved. Novel CO is urgently needed 2 Absorption device for improving CO 2 The utilization rate is improved, the economic benefit is improved, and the technical blank of carbon dioxide tail gas absorption in the carbonization reaction is filled.
Disclosure of Invention
Aiming at the technical problems, the invention provides a carbon dioxide tail gas absorbing device for a carbon dioxide decomposition reaction and an absorbing method thereof, and the invention utilizes the two-stage jet flow and one-stage spraying combined absorption and adopts two-layer leaching recovery, thereby greatly improving CO 2 Absorption rate; adopts a jet stirring mode to accelerate absorption and generate NaHCO 3 Directly used for the carbonization reaction without separation, thereby shortening the time of the carbonization reaction; the efficient recycling of the carbon dioxide tail gas of the carbonization reaction can shorten the borax preparation time, improve the production efficiency and improve the CO 2 Utilization rate, CO reduction 2 Environmental pollution, CO reduction 2 The cost and energy consumption of tail gas absorption equipment. The specific technical scheme is as follows:
the carbon dioxide tail gas absorbing device for the carbon dioxide decomposition reaction comprises a primary jet absorption tank 1, a first power fluid pump 11, a secondary jet absorption tank 2, a second power fluid pump 21, a spray absorption tank 3 and a third power fluid pump 31; the primary jet absorption tank 1 is internally provided with a coupling distributor I12 and a jet device I13, the secondary jet absorption tank 2 is internally provided with a coupling distributor II 22 and a jet device II 23, and the spray absorption tank 3 is internally provided with a primary drip washer 32, a first filling area 33, a second filling area 34, a first spray ring 35 and a second spray ring 36;
the feeding port of the first power fluid pump 11 is connected with the side wall discharging port of the primary jet absorption tank 1 through a pipeline, the discharging port of the first power fluid pump 11 is connected with the lower power fluid inlet of the coupling distributor I12 through a pipeline, and the upper gas inlet of the coupling distributor I12 is connected with carbon decomposition CO 2 The tail gas inlet pipeline 41, a top liquid inlet of the primary jet absorption tank 1 is connected with a first absorption liquid inlet pipeline 42, and the primary jet absorption tank 1The bottom discharge port is connected with a carbon decomposition material conveying pipeline 45, the top gas outlet of the primary jet absorption tank 1 is connected with the upper end gas inlet of the coupling distributor II 22 through a pipeline, the bottom discharge port of the secondary jet absorption tank 2 is connected with the top feed port of the primary jet absorption tank 1 through a pipeline, the feed port of the second power fluid pump 21 is connected with the side wall discharge port of the secondary jet absorption tank 2 through a pipeline, the discharge port of the second power fluid pump 21 is connected with the lower end power fluid inlet of the coupling distributor II 22 through a pipeline, the top liquid inlet of the secondary jet absorption tank 2 is connected with a second absorption liquid inlet pipeline 43, the top gas outlet of the secondary jet absorption tank 2 is connected with the gas inlet of the primary shower 32 through a pipeline, the bottom discharge port of the spray absorption tank 3 is connected with the top feed port of the secondary jet absorption tank 2 through a pipeline, the feed port of the third power fluid pump 31 is connected with the side wall discharge port of the spray absorption tank 3 through a pipeline, the discharge port of the third power fluid pump 31 is connected with the power fluid inlet of the primary shower 32, the first power fluid inlet 35 and the third power fluid inlet of the spray absorption tank 3 through a branch pipeline, and the third power fluid inlet of the spray pump 36 is connected with the side wall of the spray absorption tank 44;
the ejector I13 is connected with the coupling distributor I12, and the ejector II 23 is connected with the coupling distributor II 22; the jet device I13 and the jet device II 23 are respectively composed of a power fluid inlet, a guide ring, a power nozzle and CO 2 The suction inlet, the mixing cavity, the diffusion cavity and the absorption liquid outlet are formed; the coupling distributor I12 and the coupling distributor II 22 are respectively formed by an absorption liquid inlet pipe, an absorption liquid distribution cavity and CO 2 Suction pipe and CO 2 A dispensing chamber.
The first packing region 33 and the second packing region 34 are filled with white steel structured packing;
the carbon dioxide tail gas absorption method for the pyrolysis reaction adopts the carbon dioxide tail gas absorption device for the pyrolysis reaction, and comprises the following steps:
firstly, respectively introducing absorption liquid into a primary jet absorption tank 1, a secondary jet absorption tank 2 and a spray absorption tank 3; upper end gas of coupling distributor I12The body inlet is communicated with carbon decomposition CO 2 An exhaust gas intake duct 41;
the absorption liquid consists of an absorbent and an absorption accelerator, wherein the absorbent is Na with the mass concentration of 15-20% 2 CO 3 The water solution, the absorption promoter is diethanolamine, and the addition amount of the diethanolamine is Na 2 CO 3 4-5% of the mass; the carbon decomposition of CO 2 The tail gas is 40-50 ℃ and contains 5-6% of CO by volume 2 Is characterized by comprising a carbon decomposition reaction tail gas;
step 2, starting and operating equipment, wherein the first power fluid pump 11 absorbs the absorption liquid in the primary jet absorption tank 1, the absorption liquid enters an absorption liquid distribution cavity of the coupling distributor I12 through a pipeline after being boosted by an impeller of the first power fluid pump 11, and the absorption liquid distributed by the absorption liquid distribution cavity enters the jet I13 through a power fluid inlet of the jet I13 and is then ejected through a power nozzle of the jet I13 to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 Tail gas is sucked into the ejector I13; inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed and are accelerated to be discharged due to energy exchange, potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the bottom of the tank through the power nozzle of the jet device I13 at an included angle of 60 degrees in the vertical downward direction, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 3, carbon decomposition CO without participating in the reaction 2 The tail gas escapes from the primary jet absorption tank 1 and is led to a gas inlet of a coupling distributor II 22 of the secondary jet absorption tank 2 through a pipeline to be subjected to secondary absorption; the second power fluid pump 21 absorbs the absorption liquid in the second jet absorption tank 2, the absorption liquid enters an absorption liquid distribution cavity of the coupling distributor II 22 through a pipeline after being boosted by an impeller of the second power fluid pump 21, and the absorption liquid distributed by the absorption liquid distribution cavity passes through the power fluid of the jet device II 23The inlet enters the ejector II 23 and then is ejected out through a power nozzle of the ejector II 23 to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 Tail gas is sucked into the ejector II 23; inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed and are accelerated to be discharged due to energy exchange, potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the bottom of the tank through the power nozzle of the jet device II 23 at an included angle of 60 degrees in the vertical downward direction, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 4, carbon decomposition CO escaping from the secondary jet absorption tank 2 2 The tail gas is led to a gas inlet of the first-stage leacher 32 of the spray absorption tank 3 through a pipeline; carbon decomposition of CO 2 The tail gas is accelerated by pulse exchange with the flushing liquid of the first-stage leaching device 32, and forms tiny and uniform liquid drops along with the flushing liquid being sprayed out, so as to lead the CO to be carbonized 2 The tail gas and the absorption liquid have larger contact area, better and fully mixed, and CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed; simultaneously, the third power fluid pump 31 pumps the absorption liquid from the spray absorption tank 3, and branches and conveys the absorption liquid to the second spray ring 36, the first spray ring 35 and the first-stage leaching device 32, and the absorption liquid conveyed to the second spray ring 36 and the first spray ring 35 forms leaching liquid for leaching and absorbing the CO which escapes and rises 2 The absorption liquid delivered to the first stage 32 forms a rinse liquid for the purposes of carbon splitting CO 2 The next cycle of tail gas is absorbed;
step 5, unabsorbed carbon decomposition CO 2 The tail gas sequentially passes through the first filling area 33, the first spray ring 35, the second filling area 34 and the second spray ring 36, and finally is emptied from the top end of the spray absorption tank 3; evacuated carbon decomposition CO 2 The tail gas contains CO 2 The volume content is 0.5-1%; na not participating in reaction in absorption liquid 2 CO 3 The solution reacts with NaHCO generated after the reaction 3 The solution is discharged through a discharge port at the bottom end of the primary jet absorption tank 1 and is supplied to the subsequent preparation of the carbolysis ingredients of borax;
in the step 2, the step 3 and the step 4, the internal operating pressures of the primary jet absorption tank 1, the secondary jet absorption tank 2 and the spray absorption tank 3 are respectively 0.2 MPa-0.3 MPa, and the internal operating temperature is the ambient temperature.
Compared with the prior art, the carbon dioxide tail gas absorption device and the carbon dioxide tail gas absorption method have the beneficial effects that:
1. NaHCO generated by the device and the method 3 The method is directly used for the pyrolysis reaction without separation, so that the pyrolysis reaction time can be effectively shortened by more than 10 percent; so that the production time of borax preparation is shortened from 19 to 20 hours to 15 to 18 hours.
2. The device adopts three-stage absorption and organic combination for use, and the CO in the tail gas is carbonized 2 The absorptivity is above 80%, CO 2 The utilization rate is improved by more than 8 percent, and the CO is improved 2 Utilization rate, CO reduction 2 Environmental pollution;
3. the device has the advantages of no rotating equipment parts, high jet stirring speed, good absorption effect, simple equipment structure, convenient operation, low equipment cost, convenient maintenance and comprehensive energy conservation of up to 20 percent.
Drawings
Fig. 1 is a schematic structural diagram of a carbon dioxide tail gas absorbing device for a pyrolysis reaction according to embodiment 1 of the present invention: wherein, the device comprises a 1-primary jet absorption tank, a 11-first power fluid pump, a 12-coupling distributor I and a 13-jet device I; 2-second-stage jet absorption tank, 21-second power fluid pump, 22-coupling distributor II, 23-jet device II, 3-spray absorption tank, 31-third power fluid pump, 32-first-stage leaching device, 33-first packing area, 34-second packing area, 35-first spray ring, 36-second spray ring, 41-carbon decomposition CO 2 Tail gas inlet pipeline, 42-first absorption liquid inlet pipeline, 43-second absorption liquid inlet pipeline, 44-third absorption liquid inlet pipeline and 45-carbon decomposition material conveying pipeA lane; the line segments represent the pipes and the arrows indicate the flow direction.
Detailed Description
The invention will be further described with reference to specific embodiments and fig. 1, but the invention is not limited to these embodiments.
Example 1
As shown in fig. 1, a carbon dioxide tail gas absorbing device for a carbon dioxide decomposition reaction comprises a primary jet absorption tank 1, a first power fluid pump 11, a secondary jet absorption tank 2, a second power fluid pump 21, a spray absorption tank 3 and a third power fluid pump 31; the primary jet absorption tank 1 is internally provided with a coupling distributor I12 and a jet device I13, the secondary jet absorption tank 2 is internally provided with a coupling distributor II 22 and a jet device II 23, and the spray absorption tank 3 is internally provided with a primary drip washer 32, a first filling area 33, a second filling area 34, a first spray ring 35 and a second spray ring 36;
the feeding port of the first power fluid pump 11 is connected with the side wall discharging port of the primary jet absorption tank 1 through a pipeline, the discharging port of the first power fluid pump 11 is connected with the lower power fluid inlet of the coupling distributor I12 through a pipeline, and the upper gas inlet of the coupling distributor I12 is connected with carbon decomposition CO 2 Tail gas air intake pipe 41, first absorption liquid feed liquor pipeline 42 is connected to the top feed liquor mouth of first jet absorption jar 1, first jet absorption jar 1's bottom discharge gate is connected and is decomposed material pipeline 45, first jet absorption jar 1's top gas outlet passes through the upper end gas inlet of pipe connection coupling distributor II 22, second jet absorption jar 2's bottom discharge gate passes through the top feed inlet of pipe connection first jet absorption jar 1, second jet absorption jar 2's lateral wall discharge gate is passed through to the feed inlet of second power fluid pump 21, second jet absorption jar 2's discharge gate passes through the lower extreme power fluid inlet of pipe connection coupling distributor II 22, second jet absorption jar 2's top feed liquor mouth is connected and is decomposed material pipeline 43, second jet absorption jar 2's gas outlet passes through the gas inlet of pipe connection one-level drip washing ware 32, second jet absorption jar 3's bottom discharge gate passes through the pipe connection second jet absorption jar 2's lateral wall discharge gateThe top end feed inlet of the collecting tank 2, the feed inlet of the third power fluid pump 31 is connected with the side wall discharge outlet of the spray absorption tank 3 through a pipeline, the discharge outlet of the third power fluid pump 31 is connected with the power fluid inlet of the primary leaching device 32, the power fluid inlet of the first spray ring 35 and the power fluid inlet of the second spray ring 36 through pipeline branches, and the side wall liquid inlet of the spray absorption tank 3 is connected with a third absorption liquid inlet pipeline 44;
the ejector I13 is connected with the coupling distributor I12, and the ejector II 23 is connected with the coupling distributor II 22; the jet device I13 and the jet device II 23 are respectively composed of a power fluid inlet, a guide ring, a power nozzle and CO 2 The suction inlet, the mixing cavity, the diffusion cavity and the absorption liquid outlet are formed; the coupling distributor I12 and the coupling distributor II 22 are respectively formed by an absorption liquid inlet pipe, an absorption liquid distribution cavity and CO 2 Suction pipe and CO 2 A dispensing chamber.
The first packing region 33 and the second packing region 34 are filled with white steel structured packing;
the primary jet absorption tank 1 and the secondary jet absorption tank 2 are respectivelyIs a tank container of (a); the lower diameter and height of the spray absorption tank 3 are +.>The diameter and the height of the upper part are
The distance between the upper end face of the coupling distributor I12 and the tank bottom of the primary jet absorption tank 1 is 600mm, and the distance between the upper end face of the coupling distributor II 22 and the tank bottom of the secondary jet absorption tank 2 is 600mm;
the number of the jet devices I13 is 6, the jet devices I13 are uniformly distributed in 360 degrees, and an included angle of 60 degrees is formed between the jet devices I13 and the vertical downward direction; the number of the jet devices II 23 is 6, the jet devices II are uniformly distributed in 360 degrees, and the jet devices II 23 form an included angle of 60 degrees with the vertical downward direction.
The carbon dioxide tail gas absorption method for the pyrolysis reaction adopts the carbon dioxide tail gas absorption device for the pyrolysis reaction, and comprises the following steps:
step 1, respectively introducing absorption liquid into a primary jet absorption tank 1, a secondary jet absorption tank 2 and a spray absorption tank 3, wherein the absorption liquid inlet flow of the primary jet absorption tank 1 is 800kg/h, the absorption liquid inlet flow of the secondary jet absorption tank 2 is 300kg/h, and the absorption liquid inlet flow of the spray absorption tank 3 is 200kg/h; the upper end gas inlet of the coupling distributor I12 is communicated with carbon decomposition CO 2 An exhaust gas intake duct 41;
the absorption liquid consists of an absorbent and an absorption promoter, wherein the absorbent is Na with the mass concentration of 15 percent 2 CO 3 The water solution, the absorption promoter is diethanolamine, and the addition amount of the diethanolamine is Na 2 CO 3 4% of mass; the carbon decomposition of CO 2 The tail gas is 40-50 ℃ and contains 5% CO by volume 2 Is characterized by comprising a pyrolysis reaction tail gas.
Step 2, starting and operating the equipment, wherein the first power fluid pump 11 absorbs the absorption liquid in the primary jet absorption tank 1, and the pump flow is 20m 3 After the pressure of the absorption liquid is increased by the impeller of the first power fluid pump 11, the absorption liquid enters an absorption liquid distribution cavity of the coupling distributor I12 through a pipeline, the absorption liquid distributed by the absorption liquid distribution cavity enters the ejector I13 through a power fluid inlet of the ejector I13, and then is sprayed out through a power nozzle of the ejector I13 to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 The tail gas was sucked into the ejector I13 at a suction amount of 600Nm 3 /h; inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed and are accelerated to be discharged due to energy exchange, potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the bottom of the tank through the power nozzle of the jet device I13 at an included angle of 60 degrees in the vertical downward direction, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 Is sucked byCollecting;
step 3, carbon decomposition CO without participating in the reaction 2 The tail gas escapes from the primary jet absorption tank 1 and is led into a coupling distributor II 22 of the secondary jet absorption tank 2 through a pipeline to be secondarily absorbed; the second power fluid pump 21 sucks the absorption liquid in the secondary jet absorption tank 2, and the pump flow is 20m 3 After the pressure of the absorption liquid is increased by the impeller of the second power fluid pump 21, the absorption liquid enters an absorption liquid distribution cavity of the coupling distributor II 22 through a pipeline, the absorption liquid distributed by the absorption liquid distribution cavity enters the ejector II 23 through a power fluid inlet of the ejector II 23, and then is sprayed out through a power nozzle of the ejector II 23 to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 Tail gas is sucked into the ejector II 23; inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed, the fluid is intensively mixed in the mixing area and is accelerated to be discharged due to energy exchange, the potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the tank bottom by the power nozzle of the jet device II 23 in a vertical downward direction at an included angle of 60 DEG, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 4, carbon decomposition CO escaping from the secondary jet absorption tank 2 2 The tail gas is led to the gas inlet of the first-stage leacher 32 of the spray absorption tank 3 through a pipeline to carry out CO decomposition 2 The tail gas is accelerated by pulse exchange with the flushing liquid of the first-stage leaching device 32, and forms tiny and uniform liquid drops along with the flushing liquid being sprayed out, so as to lead the CO to be carbonized 2 The tail gas and the absorption liquid have larger contact area, better and fully mixed, and CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed; at the same time, the third power fluid pump 31 pumps the absorption liquid from the spray absorption tank 3, and the pump flow rate is 20m 3 And branched to the second spray ring 36, the first spray ring 35 and the first shower 32, and to the second spray ring 36 and the first showerThe absorption liquid at the spray ring 35 forms a eluent for eluting and absorbing the CO which escapes and rises 2 The absorption liquid delivered to the first stage 32 forms a rinse liquid for the purposes of carbon splitting CO 2 The next cycle of tail gas is absorbed;
step 5, unabsorbed carbon decomposition CO 2 The tail gas sequentially passes through the first filling area 33, the first spray ring 35, the second filling area 34 and the second spray ring 36, and finally is emptied from the top end of the spray absorption tank 3; evacuated carbon decomposition CO 2 The tail gas contains CO 2 The volume content is 0.5-1%; na not participating in reaction in absorption liquid 2 CO 3 The solution reacts with NaHCO generated after the reaction 3 The solution is discharged through a discharge port at the bottom end of the primary jet absorption tank 1 and is supplied to the subsequent preparation of the carbolysis ingredients of borax.
In the step 2, the step 3 and the step 4, the internal operating pressures of the primary jet absorption tank 1, the secondary jet absorption tank 2 and the spray absorption tank 3 are all 0.2MPa, and the internal operating temperature is the ambient temperature.
The effect achieved by the embodiment after 8000 hours of operation is as follows: absorbing and decomposing CO 2 CO in tail gas 2 24Nm of gas 3 /h, naHCO is generated 3 160kg/h, the reaction time is saved by 10%.
Example 2
A carbon dioxide tail gas absorbing device for a carbon decomposition reaction has the same structure as in the embodiment 1.
The carbon dioxide tail gas absorption method for the pyrolysis reaction adopts the carbon dioxide tail gas absorption device for the pyrolysis reaction, and comprises the following steps:
step 1, respectively introducing absorption liquid into a primary jet absorption tank 1, a secondary jet absorption tank 2 and a spray absorption tank 3, wherein the absorption liquid inlet flow of the primary jet absorption tank 1 is 600kg/h, the absorption liquid inlet flow of the secondary jet absorption tank 2 is 240kg/h, and the absorption liquid inlet flow of the spray absorption tank 3 is 160kg/h; the upper end gas inlet of the coupling distributor I12 is communicated with carbon decomposition CO 2 An exhaust gas intake duct 41;
the absorption liquid consists of an absorbent and an absorption promoter, wherein the absorbent is of a massNa at a concentration of 20% 2 CO 3 The water solution, the absorption promoter is diethanolamine, and the addition amount of the diethanolamine is Na 2 CO 3 5% of mass; the tail gas is 40-50 ℃ and contains 5% CO by volume 2 Is characterized by comprising a pyrolysis reaction tail gas.
Step 2, starting and operating the equipment, wherein the first power fluid pump 11 absorbs the absorption liquid in the primary jet absorption tank 1, and the pump flow is 20m 3 After the pressure of the absorption liquid is increased by the impeller of the first power fluid pump 11, the absorption liquid enters an absorption liquid distribution cavity of the coupling distributor I12 through a pipeline, the absorption liquid distributed by the absorption liquid distribution cavity enters the ejector I13 through a power fluid inlet of the ejector I13, and then is sprayed out through a power nozzle of the ejector I13 to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 The tail gas was sucked into the ejector I13 at a suction amount of 600Nm 3 /h; inhaled carbon decomposition CO 2 Tail gas expands rapidly in a negative pressure area and is beaten into tiny bubbles by a power fluid; in the mixing chamber, CO 2 The gas and the absorption liquid are fully mixed, and the potential energy of the mixed liquid is increased through the diffusion cavity after the gas and the absorption liquid are discharged in an accelerating way due to energy exchange; then the jet device I13 is emitted to the tank bottom by a power nozzle in a vertical downward direction with an included angle of 60 degrees, and the dragging action of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 3, carbon decomposition CO without participating in the reaction 2 The tail gas escapes from the primary jet absorption tank 1 and is led into a coupling distributor II 22 of the secondary jet absorption tank 2 through a pipeline to be secondarily absorbed; the second power fluid pump 21 sucks the absorption liquid in the secondary jet absorption tank 2, and the pump flow is 20m 3 After the pressure of the absorption liquid is increased by the impeller of the second power fluid pump 21, the absorption liquid enters an absorption liquid distribution cavity of the coupling distributor II 22 through a pipeline, the absorption liquid distributed by the absorption liquid distribution cavity enters the ejector II 23 through a power fluid inlet of the ejector II 23, and then is sprayed out through a power nozzle of the ejector II 23 to form high-speed fluid; the kinetic energy of the fluid is the mostLarge potential energy and minimum potential energy, and can be used in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 Tail gas is sucked into the ejector II 23; inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed, the fluid is intensively mixed in the mixing area and is accelerated to be discharged due to energy exchange, the potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the tank bottom by the power nozzle of the jet device II 23 in a vertical downward direction at an included angle of 60 DEG, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 4, carbon decomposition CO escaping from the secondary jet absorption tank 2 2 The tail gas is led to the gas inlet of the first-stage leacher 32 of the spray absorption tank 3 through a pipeline to carry out CO decomposition 2 The tail gas is accelerated by pulse exchange with the flushing liquid of the first-stage leaching device 32, and forms tiny and uniform liquid drops along with the flushing liquid being sprayed out, so as to lead the CO to be carbonized 2 The tail gas and the absorption liquid have larger contact area, better and fully mixed, and CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed; at the same time, the third power fluid pump 31 pumps the absorption liquid from the spray absorption tank 3, and the pump flow rate is 20m 3 And is branched and conveyed to the second spray ring 36, the first spray ring 35 and the first-stage leaching device 32, and the absorption liquid conveyed to the second spray ring 36 and the first spray ring 35 forms leaching liquid for leaching and absorbing the CO which escapes and rises 2 The absorption liquid delivered to the first stage 32 forms a rinse liquid for the purposes of carbon splitting CO 2 The next cycle of tail gas is absorbed;
step 5, unabsorbed carbon decomposition CO 2 The tail gas sequentially passes through the first filling area 33, the first spray ring 35, the second filling area 34 and the second spray ring 36, and finally is emptied from the top end of the spray absorption tank 3; evacuated carbon decomposition CO 2 The tail gas contains CO 2 The volume content is 0.5-1%; na not participating in reaction in absorption liquid 2 CO 3 The solution reacts with NaHCO generated after the reaction 3 The solution is discharged through a discharge port at the bottom end of the primary jet absorption tank 1 and is supplied to the subsequent preparation of the carbolysis ingredients of borax.
In the step 2, the step 3 and the step 4, the internal operating pressures of the primary jet absorption tank 1, the secondary jet absorption tank 2 and the spray absorption tank 3 are all 0.3MPa, and the internal operating temperature is the ambient temperature.
The effect achieved by the embodiment after 8000 hours of operation is as follows: absorbing and decomposing CO 2 CO in tail gas 2 Gas 27Nm 3 /h, naHCO is generated 3 180kg/h, the reaction time is saved by 16%.
Example 3
A carbon dioxide tail gas absorbing device for a carbon decomposition reaction has the same structure as in the embodiment 1.
The carbon dioxide tail gas absorption method for the pyrolysis reaction adopts the carbon dioxide tail gas absorption device for the pyrolysis reaction, and comprises the following steps:
step 1, respectively introducing absorption liquid into a primary jet absorption tank 1, a secondary jet absorption tank 2 and a spray absorption tank 3, wherein the absorption liquid inlet flow of the primary jet absorption tank 1 is 700kg/h, the absorption liquid inlet flow of the secondary jet absorption tank 2 is 290kg/h, and the absorption liquid inlet flow of the spray absorption tank 3 is 190kg/h; the upper end gas inlet of the coupling distributor I12 is communicated with carbon decomposition CO 2 An exhaust gas intake duct 41;
the absorption liquid consists of an absorbent and an absorption promoter, wherein the absorbent is Na with the mass concentration of 17 percent 2 CO 3 The water solution, the absorption promoter is diethanolamine, and the addition amount of the diethanolamine is Na 2 CO 3 4.5% of mass; the tail gas is 40-50 ℃ and contains 6% CO by volume 2 Is characterized by comprising a pyrolysis reaction tail gas.
Step 2, starting and operating the equipment, wherein the first power fluid pump 11 absorbs the absorption liquid in the primary jet absorption tank 1, and the pump flow is 20m 3 After the pressure of the absorption liquid is increased by the impeller of the first power fluid pump 11, the absorption liquid enters the absorption liquid distribution cavity of the coupling distributor I12 through a pipeline, and the absorption liquid distributed by the absorption liquid distribution cavity enters through the power fluid inlet of the ejector I13The high-speed fluid is injected into the ejector I13 and then is ejected out through a power nozzle of the ejector I13 to form the high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 The tail gas was sucked into the ejector I13 at a suction amount of 600Nm 3 /h; inhaled carbon decomposition CO 2 Tail gas expands rapidly in a negative pressure area and is beaten into tiny bubbles by a power fluid; in the mixing chamber, CO 2 The gas and the absorption liquid are fully mixed, and the potential energy of the mixed liquid is increased through the diffusion cavity after the gas and the absorption liquid are discharged in an accelerating way due to energy exchange; then the jet device I13 is emitted to the tank bottom by a power nozzle in a vertical downward direction with an included angle of 60 degrees, and the dragging action of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 3, carbon decomposition CO without participating in the reaction 2 The tail gas escapes from the primary jet absorption tank 1 and is led into a coupling distributor II 22 of the secondary jet absorption tank 2 through a pipeline to be secondarily absorbed; the second power fluid pump 21 sucks the absorption liquid in the secondary jet absorption tank 2, and the pump flow is 20m 3 After the pressure of the absorption liquid is increased by the impeller of the second power fluid pump 21, the absorption liquid enters an absorption liquid distribution cavity of the coupling distributor II 22 through a pipeline, the absorption liquid distributed by the absorption liquid distribution cavity enters the ejector II 23 through a power fluid inlet of the ejector II 23, and then is sprayed out through a power nozzle of the ejector II 23 to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 Tail gas is sucked into the ejector II 23; inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed, the fluid is intensively mixed in the mixing area and is accelerated to be discharged due to energy exchange, the potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the tank bottom by the power nozzle of the jet device II 23 in a vertical downward direction at an included angle of 60 DEG, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 4, carbon decomposition CO escaping from the secondary jet absorption tank 2 2 The tail gas is led to the gas inlet of the first-stage leacher 32 of the spray absorption tank 3 through a pipeline to carry out CO decomposition 2 The tail gas is accelerated by pulse exchange with the flushing liquid of the first-stage leaching device 32, and forms tiny and uniform liquid drops along with the flushing liquid being sprayed out, so as to lead the CO to be carbonized 2 The tail gas and the absorption liquid have larger contact area, better and fully mixed, and CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed; at the same time, the third power fluid pump 31 pumps the absorption liquid from the spray absorption tank 3, and the pump flow rate is 20m 3 And is branched and conveyed to the second spray ring 36, the first spray ring 35 and the first-stage leaching device 32, and the absorption liquid conveyed to the second spray ring 36 and the first spray ring 35 forms leaching liquid for leaching and absorbing the CO which escapes and rises 2 The absorption liquid delivered to the first stage 32 forms a rinse liquid for the purposes of carbon splitting CO 2 The next cycle of tail gas is absorbed;
step 5, unabsorbed carbon decomposition CO 2 The tail gas sequentially passes through the first filling area 33, the first spray ring 35, the second filling area 34 and the second spray ring 36, and finally is emptied from the top end of the spray absorption tank 3; evacuated carbon decomposition CO 2 The tail gas contains CO 2 The volume content is 0.5-1%; na not participating in reaction in absorption liquid 2 CO 3 The solution reacts with NaHCO generated after the reaction 3 The solution is discharged through a discharge port at the bottom end of the primary jet absorption tank 1 and is supplied to the subsequent preparation of the carbolysis ingredients of borax.
In the step 2, the step 3 and the step 4, the internal operating pressures of the primary jet absorption tank 1, the secondary jet absorption tank 2 and the spray absorption tank 3 are all 0.2MPa, and the internal operating temperature is the ambient temperature.
The effect achieved by the embodiment after 8000 hours of operation is as follows: absorbing and decomposing CO 2 CO in tail gas 2 26Nm of gas 3 /h, naHCO is generated 3 170kg/h, saving 13% of reaction time.
Claims (8)
1. The carbon dioxide tail gas absorbing device for the carbon dioxide decomposition reaction is characterized by comprising a primary jet absorption tank (1), a first power fluid pump (11), a secondary jet absorption tank (2), a second power fluid pump (21), a spray absorption tank (3) and a third power fluid pump (31); the jet flow absorption tank comprises a primary jet flow absorption tank body (1), a secondary jet flow absorption tank body (2) and a jet flow absorption device (36), wherein a coupling distributor I (12) and a jet flow device I (13) are arranged in the primary jet flow absorption tank body (1), a coupling distributor II (22) and a jet flow device II (23) are arranged in the secondary jet flow absorption tank body (2), and a primary leaching device (32), a first filling area (33), a second filling area (34), a first spraying ring (35) and a second spraying ring (36) are arranged in the spraying absorption tank body (3); the feeding port of the first power fluid pump (11) is connected with the side wall discharge port of the primary jet absorption tank (1) through a pipeline, the discharge port of the first power fluid pump (11) is connected with the lower end power fluid inlet of the coupling distributor I (12) through a pipeline, and the upper end gas inlet of the coupling distributor I (12) is connected with carbon dioxide CO 2 Tail gas intake pipe (41), first absorption liquid intake pipe (42) are connected to the top feed inlet of one-level efflux absorption jar (1), the lower extreme power fluid entry of coupling distributor II (22) is connected through the bottom discharge gate of one-level efflux absorption jar (1), the top gas outlet of one-level efflux absorption jar (1) is through the upper end gas entry of pipe connection coupling distributor II (22), the top feed inlet of one-level efflux absorption jar (1) is passed through to the bottom discharge gate of second level efflux absorption jar (2), the feed inlet of second power fluid pump (21) is through the lateral wall discharge gate of pipe connection second level efflux absorption jar (2), the discharge gate of second power fluid pump (21) is through the lower extreme power fluid entry of pipe connection coupling distributor II (22), the top feed inlet of second level efflux absorption jar (2) is connected second absorption liquid feed inlet (43), the gas outlet is through the gas entry of pipe connection one-level efflux leaching ware (32), the bottom of spray absorption jar (3) is through the lateral wall discharge gate of second level efflux absorption jar (2), the top of spray pump (3) is through the lateral wall discharge gate of pipe connection third power fluid pump (31), the top of second level efflux absorption jar (2) is connected through the lateral wall of pipe connection third jet absorption jar (3), the top of spray pump (2) is connected through the lateral wall of pipe connection, power fluid inlet of first spray ring (35)The side wall liquid inlet of the spray absorption tank (3) is connected with a third absorption liquid inlet pipeline (44);
the ejector I (13) is connected with the coupling distributor I (12), and the ejector II (23) is connected with the coupling distributor II (22); the jet device I (13) and the jet device II (23) are respectively composed of a power fluid inlet, a guide ring, a power nozzle and CO 2 The suction inlet, the mixing cavity, the diffusion cavity and the absorption liquid outlet are formed; the coupling distributor I (12) and the coupling distributor II (22) are respectively formed by an absorption liquid inlet pipe, an absorption liquid distribution cavity and CO 2 Suction pipe and CO 2 A dispensing chamber; the first packing region (33) and the second packing region (34) are filled with white steel structured packing;
the primary jet absorption tank (1) and the secondary jet absorption tank (2) are respectivelyIs a tank container of (a); the diameter and the height of the lower part of the spray absorption tank (3) are +.>The diameter and the height of the upper part are
2. The carbon dioxide tail gas absorbing device for the pyrolysis reaction according to claim 1, wherein the distance between the upper end face of the coupling distributor I (12) and the tank bottom of the primary jet absorption tank (1) is 600mm, and the distance between the upper end face of the coupling distributor II (22) and the tank bottom of the secondary jet absorption tank (2) is 600mm.
3. The carbon dioxide tail gas absorbing device for the pyrolysis reaction according to claim 1, wherein the number of the jet devices I (13) is 6, the jet devices I (13) are uniformly distributed in 360 degrees, and an included angle of 60 degrees is formed between the jet devices I (13) and the vertical downward direction; the number of the jet devices II (23) is 6, the jet devices II (23) are uniformly distributed in 360 degrees, and the jet devices II (23) form an included angle of 60 degrees with the vertical downward direction.
4. A carbon dioxide tail gas absorption method for a carbon dioxide decomposition reaction, a carbon dioxide tail gas absorbing device for a pyrolysis reaction according to claim 1, comprising the steps of:
step 1, firstly, respectively introducing absorption liquid into a primary jet absorption tank (1), a secondary jet absorption tank (2) and a spray absorption tank (3); the upper gas inlet of the coupling distributor I (12) is communicated with carbon decomposition CO 2 A tail gas inlet pipe (41);
step 2, starting and operating equipment, wherein a first power fluid pump (11) absorbs absorption liquid in a primary jet absorption tank (1), the absorption liquid enters an absorption liquid distribution cavity of a coupling distributor I (12) through a pipeline after being boosted by an impeller of the first power fluid pump (11), and the absorption liquid distributed by the absorption liquid distribution cavity enters the jet I (13) through a power fluid inlet of the jet I (13) and is then sprayed out through a power nozzle of the jet I (13) to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 Tail gas is sucked into the ejector I (13); inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed and are accelerated to be discharged due to energy exchange, potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the bottom of the tank by the power nozzle of the jet device I (13) at an included angle of 60 degrees in the vertical downward direction, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 3, carbon decomposition CO without participating in the reaction 2 The tail gas escapes from the primary jet absorption tank (1) and is led to a gas inlet of a coupling distributor II (22) of the secondary jet absorption tank (2) through a pipeline for secondary absorption; the second power fluid pump (21) absorbs the absorption liquid in the secondary jet absorption tank (2), and the absorption liquid enters the coupling branch through a pipeline after being boosted by the impeller of the second power fluid pump (21)The absorption liquid distribution cavity of the adapter II (22) is used for enabling absorption liquid distributed by the absorption liquid distribution cavity to enter the ejector II (23) through a power fluid inlet of the ejector II (23) and then to be ejected through a power nozzle of the ejector II (23) to form high-speed fluid; at the moment, the kinetic energy of the fluid is the largest and the potential energy is the smallest, and the fluid can be in CO 2 Negative pressure is generated at the suction inlet to lead the carbon to be decomposed into CO 2 Tail gas is sucked into the ejector II (23); inhaled carbon decomposition CO 2 The tail gas expands rapidly in the negative pressure area and is beaten into tiny bubbles by the power fluid, and CO is in the mixing cavity 2 The gas and the absorption liquid are fully mixed and are accelerated to be discharged due to energy exchange, potential energy of the mixed liquid is increased through the diffusion cavity, then the mixed liquid is emitted to the bottom of the tank by the power nozzle of the jet device II (23) at an included angle of 60 degrees in the vertical downward direction, and the dragging effect of the absorption liquid increases CO 2 Absorption effect, CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed;
step 4, carbon decomposition CO escaping from the secondary jet absorption tank (2) 2 The tail gas is led to a gas inlet of a first-stage leaching device (32) of the spray absorption tank (3) through a pipeline to carry out CO decomposition 2 The tail gas is accelerated by pulse exchange with the flushing liquid of the first-stage leaching device (32) and forms tiny and uniform liquid drops along with the flushing liquid being sprayed out, so as to lead the CO to be decomposed 2 The tail gas and the absorption liquid have larger contact area, better and fully mixed, and CO 2 And Na (Na) 2 CO 3 Reaction to produce N a HCO 3 And absorbed; simultaneously, the third power fluid pump (31) pumps the absorption liquid out of the spray absorption tank (3) and branches and conveys the absorption liquid to the second spray ring (36), the first spray ring (35) and the first-stage leaching device (32), and the absorption liquid conveyed to the second spray ring (36) and the first spray ring (35) forms leaching liquid for leaching and absorbing CO rising from escaping 2 The absorption liquid delivered to the first stage (32) forms a flushing liquid for CO decomposition 2 The next cycle of tail gas is absorbed;
step 5, unabsorbed carbon decomposition CO 2 The tail gas sequentially passes through a first filling area (33), a first spray ring (35), a second filling area (34) and a second spray ring (36), and finally the tail gas flows from the top end of the spray absorption tank (3)Evacuating; na not participating in reaction in absorption liquid 2 CO 3 The solution reacts with NaHCO generated after the reaction 3 The solution is discharged through a discharge port at the bottom end of the primary jet absorption tank (1) and is supplied to the subsequent preparation of the carbolysis ingredients of borax.
5. The method for absorbing carbon dioxide tail gas from pyrolysis reaction according to claim 4, wherein in step 1, the absorbing liquid consists of an absorbent and an absorption promoter, wherein the absorbent is Na with mass concentration of 15% -20% 2 CO 3 The water solution, the absorption promoter is diethanolamine, and the addition amount of the diethanolamine is Na 2 CO 3 4 to 5 percent of the mass.
6. The method for absorbing carbon dioxide tail gas from a pyrolysis reaction according to claim 4, wherein said carbon dioxide is CO 2 The tail gas is 40-50 ℃ and contains 5-6% of CO by volume 2 Is characterized by comprising a pyrolysis reaction tail gas.
7. The method for absorbing carbon dioxide tail gas in a pyrolysis reaction according to claim 4, wherein in the step 2, the step 3 and the step 4, the internal operating pressures of the primary jet absorption tank (1), the secondary jet absorption tank (2) and the spray absorption tank (3) are respectively 0.2-0.3 MPa, and the internal operating temperature is the ambient temperature.
8. The method for absorbing carbon dioxide tail gas from a pyrolysis reaction according to claim 4, wherein in step 5, the carbon dioxide is decomposed into CO 2 The tail gas contains CO 2 The volume content is 0.5-1%.
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