CN215259901U - Glass kiln flue gas carbon dioxide's entrapment purification device - Google Patents
Glass kiln flue gas carbon dioxide's entrapment purification device Download PDFInfo
- Publication number
- CN215259901U CN215259901U CN202120367195.9U CN202120367195U CN215259901U CN 215259901 U CN215259901 U CN 215259901U CN 202120367195 U CN202120367195 U CN 202120367195U CN 215259901 U CN215259901 U CN 215259901U
- Authority
- CN
- China
- Prior art keywords
- flue gas
- carbon dioxide
- adsorption
- glass kiln
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Landscapes
- Separation Of Gases By Adsorption (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
The utility model relates to the technical field of carbon dioxide recovery, in particular to a device for capturing and purifying carbon dioxide in flue gas of a glass kiln, which comprises a carbon dioxide flue gas pretreatment system, a carbon dioxide capturing system and a carbon dioxide refining system which are connected in sequence, wherein the flue gas pretreatment system is connected with the glass kiln and is used for pretreating the flue gas discharged by the glass kiln; the carbon dioxide capture system is used for collecting SO in carbon dioxide2And NOXFurther absorbing, rapidly cooling and dedusting the flue gas, and adsorbing and desorbing carbon dioxide into high-concentration carbon dioxide gas by a pressure swing adsorption method; the carbon dioxide refining system can compress and dry carbon dioxide, and liquid carbon dioxide products are prepared after impurities are removed. The utility model provides a trapping purification device of glass kiln flue gas carbon dioxide concentrates the CO2 trapping in the flue gas through the pressure swing adsorption mode, reduces carbon dioxide and other pollutants to atmospheric emission.
Description
Technical Field
The utility model relates to a carbon dioxide retrieves technical field, is a entrapment purification device of glass kiln flue gas carbon dioxide particularly.
Background
Global warming is the biggest challenge facing mankind in the early century, and is not only an environmental problem but also an economic, political, human development and the like problem. From the late nineteenth century, the global air temperature has gone out steadily for thousands of years, entered the ascent passage, and may continue to rise substantially. In the atmosphere, the temperature rise is very strongly correlated with the rapid increase in the concentration of greenhouse gases, including carbon dioxide (CO2), methane (CH4), Nitrogen Oxides (NOX), chlorofluorocarbons (CFCS) and water vapor (H2O). While carbon dioxide is the most dominant greenhouse gas, its increased content contributes approximately 60% to the enhancement of the greenhouse effect.
Currently, the main industries of CO2 emission in China are high energy consumption industries such as electric power, steel, building materials, chemical industry and the like, wherein the building material industry accounts for about 15% of the emission of CO2 in national energy activities. As a pillar type industry of economic construction in China, the building material industry makes great contribution to economic development and social progress, and simultaneously consumes a large amount of resources and energy.
The carbon capture utilization and sequestration refers to an industrial process of separating carbon dioxide from an industrial emission source or directly utilizing or sequestering the carbon dioxide to realize CO2 emission reduction, is a novel technology with large-scale carbon dioxide emission reduction potential, is expected to realize low-carbon utilization of fossil energy, and is widely considered as one of the most important technologies for coping with global climate change and controlling greenhouse gas emission. The capture and separation of CO2 in the flue gas are the basis and precondition for realizing emission reduction measures such as the sealing and comprehensive utilization of the flue gas. At present, each large power generation group and oil system in China are also built into an industrial demonstration device for CO2 capture successively. But the carbon capture technology in the building material field, especially in the glass industry, is still blank.
As the temperature of flue gas after combustion in the glass kiln is up to 1200 ℃, the temperature of a waste heat boiler is required to be controlled at 600-650 ℃, and the temperature is generally reduced by mixing air, CO2 in the flue gas is diluted by a large amount of N2, so that the capture of carbon dioxide is very difficult.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to solve the not enough of prior art, provide a glass kiln flue gas carbon dioxide's entrapment purification device, reduce carbon dioxide and other pollutants to atmospheric emission.
In order to achieve the aim, the device for capturing and purifying the carbon dioxide in the flue gas of the glass kiln comprises a carbon dioxide flue gas pretreatment system, a carbon dioxide capture system and a carbon dioxide refining system which are sequentially connected, wherein the flue gas pretreatment system is connected with the glass kiln and is used for carrying out pretreatment of denitration, desulfurization, dust removal and temperature reduction on the flue gas discharged by the glass kiln; the carbon dioxide capture system is used for collecting SO in carbon dioxide2And NOXFurther absorbing, rapidly cooling the flue gas, and adsorbing and desorbing carbon dioxide into high-concentration carbon dioxide gas by a pressure swing adsorption method; the carbon dioxide purification systemThe system can compress and dry the carbon dioxide, and further remove impurities to prepare a food-grade liquid carbon dioxide product.
The utility model discloses still have following preferred technical scheme:
furthermore, the flue gas pretreatment system is arranged between the flue outlet of the glass kiln and the chimney, flue gas at the outlet of the glass kiln is introduced into the pretreatment system through a connecting pipeline, and after pretreatment, residual gas is discharged from the chimney.
Further, flue gas pretreatment systems, including glass kiln flue gas exhaust-heat boiler, flue gas electrostatic precipitator, flue gas denitrification facility, flue gas desulphurization unit and flue gas recirculation device, exhaust-heat boiler high temperature section is connected with flue gas electrostatic precipitator, flue gas electrostatic precipitator is connected with flue gas denitrification facility, be used for taking place redox reaction and accomplish flue gas denitration, flue gas denitrification facility is connected with flue gas exhaust-heat boiler low temperature section, be used for making the flue gas get back to flue gas exhaust-heat boiler low temperature section again and accomplish the heat transfer, flue gas exhaust-heat boiler export is divided into two the tunnel, the leading-in carbon dioxide entrapment system of exhaust-heat boiler export flue gas is crossed through first draught fan all the way, flue gas circulation fan is crossed all the way and is introduced flue gas exhaust-heat boiler export flue gas into flue gas exhaust-heat boiler entry.
Furthermore, the carbon dioxide capture system comprises a water washing desulfurization and denitrification device for cooling the flue gas and performing desulfurization and denitrification, and an adsorption and desorption device for adsorbing the carbon dioxide discharged waste gas to obtain high-concentration carbon dioxide.
Further, washing SOx/NOx control device include the washing desulfurizing tower, the filler is put in the washing desulfurizing tower, and the flue gas is followed washing desulfurizing tower lower part and is gone into in the tower, washing desulfurizing tower bottom is used for the flue gas to remove dust, and the middle part is equipped with from the top sulfur dioxide and the nitrogen dioxide that the desulfurizing liquid that flows downwards is arranged in absorbing the flue gas, the second draught fan is connected to the washing desulfurizing tower, sends the flue gas to the adsorption and desorption device.
Furthermore, the adsorption and desorption device comprises at least 7 pressure swing adsorption towers, the pressure swing adsorption towers are connected with the water washing desulfurization tower, filler and adsorbent are stored in each pressure swing adsorption tower and used for absorbing easily-adsorbed components in the flue gas, the difficultly-adsorbed components flow out from the top of the tower and are discharged after denitration, and then the easily-adsorbed components are desorbed to obtain high-concentration CO2, the pressure swing adsorption towers sequentially undergo the steps of adsorption, 3 times of uniform pressure drop, reverse release, 3 times of uniform pressure rise and final pressure rise, so that 2 adsorption towers are ensured to be in a state of feeding adsorption and producing carbon dioxide gas at any moment, and the pressure swing adsorption towers convey the high-concentration CO2 to a carbon dioxide refining system through connecting pipelines.
Furthermore, the carbon dioxide refining system comprises a compression adsorption device, a freezing liquefaction device and a rectification and finished product storage device which are sequentially connected.
Further, compression adsorption equipment includes buffer tank, compressor, desulfurization bed, adsorption bed, the buffer tank link to each other with carbon dioxide entrapment system, buffer tank and compressor, desulfurization bed, adsorption bed connect gradually, adsorption bed includes three adsorption tower, the adsorption tower adsorbs carbon dioxide gas respectively simultaneously, heats, cold blow, the adsorption bed is connected with freezing liquefaction device.
Further, the refrigeration liquefaction device comprises a refrigeration compressor, a condenser, a liquid storage device, a CO2 liquefaction device and a gas-liquid separator, wherein the refrigeration compressor, the condenser, the liquid storage device and the gas-liquid separator are sequentially connected into a cycle and used for cooling and liquefying carbon dioxide gas in the CO2 liquefaction device, and the carbon dioxide gas and light component gas are sent to a rectification and finished product storage device.
Further, the rectification and finished product storage device comprises a rectification tower and a food-grade product storage tank, wherein the rectification tower is connected with the food-grade finished product storage tank.
Beneficial effects of the utility model
The utility model provides a glass kiln flue gas carbon dioxide entrapment purification device's useful part lies in: the concentration of carbon dioxide discharged after combustion of the pure oxygen glass kiln is about 30-40%, the temperature of flue gas after combustion of the glass kiln is up to 1200 ℃, the temperature of a waste heat boiler is required to be controlled to be 600-650 ℃, so that the temperature is reduced by mixing air, and the CO in the flue gas is finally reduced2Is covered with a large amount of N2Dilution ofSo that the capture of carbon dioxide becomes very difficult. For the carbon dioxide capture process, the content of carbon dioxide determines the capture process and capture efficiency, so that the method for cooling the original glass kiln by using cold air is changed, the flue gas of the glass kiln after desulfurization, denitrification, temperature reduction and dust removal is reintroduced into the waste heat power generation boiler by the circulating fan, and the purpose of cooling is realized by circulating the flue gas on the premise of not changing the content of CO 2.
Pure oxygen glass kiln can generate a large amount of high CO2The flue gas with the content comprises 30-40% of carbon dioxide, 2-4% of nitrogen, 3-10% of oxygen, 50-60% of water and the balance of impurities such as carbon monoxide, nitric oxide, sulfur dioxide, dust and the like. The utility model discloses at first carry out the preliminary treatment of denitration, desulfurization, dust removal and cooling to glass kiln flue gas through flue gas preliminary treatment part, make the flue gas index accord with carbon entrapment technological requirement. Because the flue gas contains a small amount of acid gas, such as SO2，NOXAnd CO and the like, therefore, an alkali washing method is required to be adopted for deep removal, the flue gas treated by the flue gas pretreatment part is subjected to carbon-avoiding and deacidification pretreatment by a water washing desulfurizing tower, the flue gas is subjected to temperature reduction and dust removal, acid impurities in the flue gas are removed, water vapor is removed, and then the concentration of carbon dioxide is concentrated to be more than 95% by a pressure swing adsorption device to form high-concentration carbon dioxide gas. Then 95% of carbon dioxide gas is conveyed to a carbon dioxide refining part, is introduced into a buffer tank through a fan and then enters a compressor for pressurization, and then sequentially enters a desulfurization bed and an adsorption bed after cooling water separation and pressure stabilization, so that impurities such as sulfide, hydrocarbons, alcohol, aldehyde, ether, moisture and the like are removed under the action of pressure, and the gas without impurities is led out from the top of the adsorption bed and returns to an interstage outlet of the compressor; then is cooled and liquefied by a freezing and liquefying device and enters a rectifying tower. The light components of nitrogen and oxygen are all removed from the tower top, and a high-purity carbon dioxide product with the purity of more than 99.9 percent is obtained at the tower bottom. The carbon dioxide product is stored and transported through the finished product storage tank, and the use requirement is met. After the operation, the flue gas basically does not contain carbon dioxide any more, the near zero emission of the carbon dioxide in the glass production line is realized, the emission of the original sulfur dioxide and nitrogen oxide is sharply reduced, and the carbon dioxide is oxidizedThe sulfur emission amount is reduced to 5mg/Nm3And the pollution to the environment is greatly reduced. Provides a new idea for the clean production of industrial enterprises and has good social benefit.
Drawings
FIG. 1 is a schematic structural view of a glass kiln flue gas carbon dioxide capturing and purifying device of the present invention;
FIG. 2 is a schematic structural view of a glass kiln flue gas carbon dioxide flue gas pretreatment device of the present invention;
FIG. 3 is a schematic structural view of a glass kiln flue gas carbon dioxide water washing desulfurization device of the present invention;
FIG. 4 is a schematic structural view of a glass kiln flue gas carbon dioxide pressure swing adsorption device of the present invention;
FIG. 5 is a schematic structural view of a carbon dioxide refining section of a glass kiln flue gas according to the present invention;
in the drawings are labeled: 1-flue gas pretreatment system, 2-carbon dioxide capture system, 3-carbon dioxide refining system, 4-glass kiln, 5-chimney, 6-washing desulfurization and denitrification device, 7-adsorption and desorption device, 8-surge tank, 9-compressor, 10-desulfurization bed, 11-adsorption bed, 12-liquefaction device, 13-refrigeration device, 14-rectifying tower, 15, finished product storage tank, 101-flue gas waste heat boiler, 102-flue gas dust removal device, 103-denitrification device, 104-induced draft fan, 105-desulfurization device, 106-circulating fan, 201-washing desulfurization tower, 202-first cooler, 203-second cooler, 204-raw material cooler, 205-gas-liquid separator, 206-NaOH solution, 207-desulfurization solution buffer tank, 208-desalting cooler and 209-salt liquid separating tank.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.
As shown in fig. 1, the embodiment provides a flue gas pretreatment device for capturing and purifying carbon dioxide, which comprises a glass kiln, a flue gas waste heat boiler, a flue gas denitration device, a flue gas desulfurization device, a flue gas dust removal device and a flue gas recirculation device.
Referring to fig. 2, the flue gas at the outlet of the glass kiln is introduced into the flue gas waste heat boiler through a draught fan and a connecting pipeline. After the flue gas passes through the high-temperature section of the waste heat boiler, the flue gas enters a flue gas dust removal device for dust collection, after the dust collection, the flue gas is fully and uniformly mixed with ammonia water in a flue and then enters a flue gas denitration device, the flue gas denitration device is an SCR (selective catalytic reduction) reactor, and NO (nitric oxide) in the flue gasXAnd NH3And carrying out oxidation reduction reaction under the action of the catalyst to generate nitrogen and water, thereby completing the denitration process. Enters a desulphurization device after passing through a waste heat boiler to realize that the concentration of particulate matters at a flue gas outlet is less than 5mg/Nm3，SO2Concentration < 30mg/Nm3，NOXConcentration < 100mg/Nm3And the flue gas index requirement of the carbon dioxide capture system is met.
Former system adopts and mixes the cold wind cooling mode and realizes that stove export 1200 ℃ high temperature flue gas falls to 650 ℃, the utility model discloses a keep carbon dioxide concentration not to reduce, change the cooling of boiler gas circulation mode into, extract exhaust-heat boiler export 170 ℃ waste gas and replace the cold air to mix the kiln export flue gas through circulating fan, realize that the flue gas cooling reaches 600 and supplyes one's expenses flue gas exhaust-heat boiler to 650 ℃. In order to ensure micro-positive pressure in the glass kiln, the flue gas access point needs to be behind the gate valve of the glass kiln. The circulating air quantity is adjusted through an electric butterfly valve of the circulating fan.
The carbon dioxide trapping part comprises a water washing desulfurization and denitrification device and an adsorption desorption device.
Referring to fig. 3, the water washing desulfurization and denitrification device comprises a water washing desulfurization tower, flue gas enters the water washing desulfurization tower from the lower part of the water washing desulfurization tower under the action of an induced draft fan, the flue gas is rapidly cooled, meanwhile, trace dust carried in the gas is cleaned by a solvent, the temperature of the flue gas entering the water washing desulfurization tower is up to 140 ℃, the temperature of the flue gas entering the water washing desulfurization tower can be rapidly raised after the flue gas enters the water washing desulfurization tower, the lower part of the water washing desulfurization tower is connected with a first cooler, and the temperature is raised to about 8 DEGThe water washing liquid at 0 ℃ is cooled to below 40 ℃ through heat exchange and then returns to the desulfurizing tower for cooling and water washing, then the flue gas enters the middle part and is in countercurrent contact with the desulfurizing liquid flowing from top to bottom for avoiding carbon and deacidifying, sulfur dioxide and nitric oxide are absorbed by a solvent, and the absorbed desulfurizing solution is neutralized into NaNO through adding NaOH and solution to neutralize sulfate3And Na2SO4And the crystal is cooled and crystallized by a desalting cooler and then is separated from the system. The mother liquor separated by the salt-liquid separator is pumped back to the water washing desulfurizing tower for recycling. After water washing, desulfurization and denitrification, the flue gas is purified and cooled, and is sent to an adsorption and desorption device by a draught fan.
Referring to fig. 4, the adsorption and desorption device adopts a pressure swing adsorption natural desorption process, which is a 7-2-3-BD process, i.e., 7 adsorption towers in total, 2 adsorption towers being in an adsorption state, and 3 times of pressure equalization and reverse desorption processes. Above-mentioned flue gas gets into 2 adsorption towers that pressure swing adsorption device is in adsorption state, easily adsorb the component in the gas like carbon dioxide, water etc. is absorbed earlier, difficult adsorption component is like components such as nitrogen gas oxygen etc. and flows out evacuation after the denitration by the top of the tower, stop ventilating when the absorption forward position of easily adsorbing the component is about to arrive the top of the tower soon, carry out 3 after all descending with other towers, tentatively carry out the enrichment with the carbon dioxide in the adsorption tower, then put into carbon dioxide buffer tank through the negative step of putting high-purity carbon dioxide gas in the adsorption tower and supply carbon dioxide compression adsorption device to use. After the reverse discharge is finished, the tail gas enters the next adsorption cycle again after being subjected to 3 times of uniform rising and final rising of the top tail gas with other towers. The whole operation process is carried out at the temperature of the raw material gas entering the tower, and each adsorption tower enters the next cycle after the steps of adsorption, 3 times of pressure equalizing drop, reverse discharging, 3 times of pressure equalizing rise, final pressure rise and the like in sequence.
Table 1: process timing chart of adsorption tower in 7-2-3-BD flow
In the table: adsorption A, three-time average voltage drop (ED 1-ED 3), reverse discharge D, average voltage rise (ER 3-ER 1) and final voltage rise FR.
Adsorption A: and opening the program control valves V-A1 and V-A2, enabling the feed gas to enter the adsorption tower A, adsorbing easily-adsorbed components mainly comprising carbon dioxide on the surface of an adsorbent, absorbing easily-adsorbed components in the gas such as carbon dioxide, water and the like by the adsorbent, and allowing components not easily adsorbed such as nitrogen, oxygen and the like to flow out from the top of the adsorption tower A through the program control valve V-A2 as adsorption waste gas. And when the time of the adsorption step is over, closing the valves V-A1 and V-A2 to terminate the adsorption, and introducing the feed gas into another adsorption tower which finishes the final pressure boosting step, namely an adsorption tower B for adsorption.
Average pressure drop ED 1: opening the program control valves V-A4 and V-D4, carrying out pressure equalization on the adsorption tower A which finishes the adsorption step and the adsorption tower D which finishes the ER2 pressure equalization rise step, closing the V-A4 after the pressures of the two adsorption towers are basically equalized, and finishing the ED1 pressure equalization drop step of the adsorption tower A.
Average pressure drop ED 2: and continuously opening the program control valves V-A4 and V-E4, carrying out pressure equalization on the adsorption tower A which finishes the adsorption step and the adsorption tower E which finishes the ER3 pressure equalization rise step, closing the V-A4 and the V-E4 after the pressures of the two adsorption towers are basically equalized, and finishing the step of equalizing pressure drop ED2 of the adsorption tower A.
Average pressure drop ED 3: and (3) continuing to open the program control valves V-A4 and V-F4, carrying out pressure equalization on the adsorption tower A which finishes the adsorption step and the adsorption tower F which finishes the reverse release step D, and closing the V-A4 and the V-F4 after the pressures of the two adsorption towers are basically balanced to finish the step of equalizing pressure drop ED3 of the adsorption tower A.
Reverse amplification D: the programmable valve V-A3 was opened, and the gas in adsorption column A, which completed ED3 step, was vented from the bottom and the pressure was reduced. The reverse bleed gas was passed through valve V-A3 to a CO2 surge tank. When the pressure of the adsorption tower A is reduced to the normal pressure, the V-A3 is closed, and the reverse discharging step is completed.
Pressure-equalizing lift ER 1: after the reverse discharging step is finished, opening the program control valves V-A4 and V-C4, carrying out pressure equalization on the adsorption tower A and the adsorption tower C which finishes equal pressure drop of ED2, closing the valve V-C4 when the pressures of the two towers are basically equal, and finishing equal pressure rise ER1 of the adsorption tower A.
Pressure-equalizing lift ER 2: and after the step of increasing the ER1 by the uniform pressure is finished, opening the program control valves V-A4 and V-D4, equalizing the pressure of the adsorption tower A and the adsorption tower D which finishes the step of increasing the pressure of the ED1 by the uniform pressure, and closing the valve V-D4 when the pressure of the two towers is basically equal to each other to finish the step of increasing the ER2 by the uniform pressure of the adsorption tower A.
Pressure-equalizing lift ER 3: and after the step of increasing the ER2 by the uniform pressure is finished, opening the program control valves V-A4 and V-E4, equalizing the pressure of the adsorption tower A and the adsorption tower E which finishes the adsorption step, closing the valve V-E4 when the pressure of the two towers is basically equal, and finishing the step of increasing the ER3 by the uniform pressure of the adsorption tower A.
Final boost FR: after the pressure equalizing and raising step is completed, the program control valves V-A1 and V-A3 at the inlet and outlet ends of the adsorption tower at the final pressure raising (FR) step are opened with different opening degrees through a control program, so that the product gas and the feed gas can be simultaneously used for final pressure raising according to different proportional flow rates, and the pressure fluctuation of the product gas and the feed gas is reduced.
It can be seen from the process timing chart that in the process of pressure equalization and rise or pressure equalization of the adsorption towers, another group of adsorption towers are also in the process of pressure equalization, so the corresponding programmable valves should be opened, for example, when the adsorption tower A is in the process of pressure equalization and drop ED1, the programmable valves V-A4 and V-C4 are opened, and meanwhile, the adsorption tower E and the adsorption tower G are in the process of pressure equalization and rise ER3, so V-E5 and V-G5 are opened to satisfy the requirement that two groups of adsorption towers complete the pressure equalization operation at the same time.
And the carbon dioxide gas after desorption enters the carbon dioxide refining system, and the carbon dioxide refining system comprises a compression adsorption device, a freezing liquefaction device and a rectification and finished product storage device.
Referring to fig. 5, the compression adsorption device comprises a buffer tank, a compressor, a desulfurization bed and an adsorption bed, wherein the carbon dioxide feed gas with the purity of 95.0% from the pressure swing adsorption device firstly enters the buffer tank, and a temperature gauge and a pressure gauge are arranged on an inlet pipeline of the buffer tank to detect two process data. Then enters CO2The carbon dioxide gas at the outlet of the second-stage compression after compression firstly enters a desulfurization bed, sulfides are adsorbed by a desulfurizing agent in the bed under the action of pressure, the desulfurized gas enters an adsorption tower, and three combinations of adsorbents in the adsorption tower are used for removing impurities such as hydrocarbons, alcohol, aldehyde, ether, moisture and the like. The gas freed from impurities is withdrawn from the top of the adsorption bed and returned to the outlet between the compressor stages. In addition, CO gasified in the course of transferring the rectifying tower to the product tank2CO gasified by heat dissipation on surface of equipment2The gas is mixed and then returns to an interstage outlet of the compressor, and the lost CO is effectively recovered2And the product yield is improved. The mixed gas enters a refrigeration liquefaction device after being compressed by the compressor in three stages.
The adsorption bed is provided with 3 adsorption towers, each tower sequentially passes through the continuous operation process of adsorption A, heating H and cold blowing C, adsorption and regeneration are circularly reciprocated and are continuously and stably (see table 2) by program control, compared with the double-tower process, the adsorption-heating-cold blowing process continuous operation of the adsorbent during working is less in adsorbent consumption, less in gas consumption for regeneration and high in equipment efficiency. The gas escaping from the top of the rectifying tower is used as the regeneration gas of the adsorbent, and no external regeneration gas pollutes the bed layer.
Table 2: operation state of adsorption tower in different periods
Adsorption A: and opening the program control valves V-X1 and V-X2, enabling the feed gas to enter the adsorption tower X, adsorbing impurities such as moisture on the surface of the adsorbent, and enabling the carbon dioxide to flow out from the top of the adsorption tower A through the program control valve V-X2. At the end of the adsorption step time, the valves V-X1 and V-X2 are closed to terminate the adsorption, and the raw material gas enters another adsorption tower Z which has completed the cold blowing step for adsorption.
Heating H: opening the program control valves V-X3 and V-X4, leading the regenerated gas heated by steam and the raw material gas flow to reversely pass through the adsorption tower, leading the adsorbed impurities to flow out of the adsorption tower along with the regenerated gas, and regenerating the adsorbent. At the end of the heating step time, valves V-X3 and V-X4 were closed.
And C, cold blowing: opening the program control valves V-X5 and V-X6, introducing the gas escaping from the top of the rectification into the adsorption tower X which finishes the heating step to finish the cold blowing step, and closing the valves V-X5 and V-X6. The adsorption-heating-cold blowing process was repeated.
The freezing and liquefying device comprises a refrigeration compressor, a condenser, a liquid storage device, a pressure regulating valve and CO2A liquefying device, a gas-liquid separator and a pipeline, wherein the refrigeration compressor is a screw type or a piston type,the refrigerant is liquid ammonia or freon. The whole refrigeration liquefaction device is a circulation process, gaseous refrigerant enters a refrigeration compressor to be compressed, the compressor is connected with an evaporative condenser, the gaseous refrigerant is condensed into liquid refrigerant in the evaporative condenser, and the liquid refrigerant is stored in a liquid receiver.
The liquid refrigerant from the liquid reservoir is divided into four paths: one path is throttled and cooled by a regulating valve and then led to CO2In the liquefaction device, cold energy is transferred to carbon dioxide gas in the heat exchanger tube, so that the carbon dioxide gas is cooled and liquefied, and the carbon dioxide gas and light component gas are sent to the rectifying tower together. The liquid refrigerant between the liquefier tubes is vaporized and enters the gas-liquid separator, and the gas refrigerant returns to the refrigeration compressor for recycling.
The second path of liquid refrigerant in the liquid reservoir enters the raw material cooler after being throttled and depressurized by the regulating valve, the raw material gas in the tube is cooled to about 10 ℃, most of water in the gas is liquefied under the condition, and the liquefied water is separated in the water diversion tank. The liquid refrigerant is vaporized and enters the gas-liquid separator, and the gas refrigerant is returned to the refrigeration compressor.
And the third path of liquid refrigerant in the liquid reservoir is throttled and cooled by an adjusting valve and then introduced into a desalting cooler for crystallizing and using by-products of desulfurization and denitrification. The liquid refrigerant between the liquefier tubes is vaporized and enters the gas-liquid separator, and the gas refrigerant is returned to the refrigeration compressor.
And the fourth path of liquid refrigerant in the liquid receiver is throttled and cooled by an adjusting valve and then is introduced into a shell of a full condenser at the top of the rectification tower to be used for condensing tower top fractions in the condenser, the shell liquid refrigerant is vaporized and enters a gas-liquid separator, and the gas refrigerant is also returned to the refrigeration compressor for recycling.
The outlet pressure of the refrigeration compressor is between 2.0 and 2.6MPa (g), the pressure after passing through the regulating valve is between 0.1 and 0.35MPa, and the temperature is between minus 40 ℃ and minus 5 ℃.
The rectification and finished product storage device comprises a rectification tower and a food-grade product storage tank. Carbon dioxide via CO2Refrigeration device of liquefaction deviceThe liquid is liquefied and enters a rectifying tower, light components of nitrogen and oxygen are all removed from the top of the tower, a high-purity carbon dioxide product with the purity of over 99.9 percent is obtained at the bottom of the tower, and the high-purity carbon dioxide product is sent to food-grade CO2And the finished product storage tank is used for filling bottles or loading the tank into a tank car.
All parts are connected through pipelines with different pipe diameters, pipes, valves and flowmeters are arranged on the pipelines, detection instruments such as pressure meters and thermometers are installed on the pipelines, detection instruments such as pressure meters, temperature meters and liquid levels and safety facilities such as safety valves and pressure reducing valves are also installed on the equipment, instrument parameters of key parts are uniformly controlled by a PLC or DCS system program, and the automatic control device has the functions of measuring, adjusting, recording, alarming and the like and is operated automatically.
The above, only for the concrete implementation of this utility model, but the scope of protection of this utility model is not limited to this, and any person skilled in this technical field is in the technical scope of this utility model discloses, according to the technical scheme of this utility model and novel design add in equal replacement or change, all should be covered in the scope of protection of this utility model.
Claims (10)
1. The utility model provides a entrapment purification device of glass kiln flue gas carbon dioxide which characterized in that, is including the carbon dioxide flue gas pretreatment system, carbon dioxide entrapment system and the refined system of carbon dioxide that connect gradually, flue gas pretreatment system be connected with the glass kiln for carry out the preliminary treatment of denitration, desulfurization, dust removal and cooling to the flue gas that the glass kiln discharged.
2. The device for capturing and purifying carbon dioxide in glass kiln flue gas as claimed in claim 1, wherein the flue gas pretreatment system is arranged between the flue outlet of the glass kiln and the chimney, the flue gas at the outlet of the glass kiln is introduced into the pretreatment system through the connecting pipeline, and the pretreated residual gas is discharged from the chimney.
3. The capturing and purifying device for carbon dioxide in glass kiln flue gas as claimed in claim 2, the flue gas pretreatment system comprises a glass kiln flue gas waste heat boiler, a flue gas electric dust removal device, a flue gas denitration device, a flue gas desulfurization device and a flue gas recirculation device, the high-temperature section of the waste heat boiler is connected with a flue gas electric dust removal device which is connected with a flue gas denitration device, used for carrying out oxidation-reduction reaction to finish flue gas denitration, the flue gas denitration device is connected with the low-temperature section of the flue gas waste heat boiler, the flue gas waste heat boiler is used for enabling the flue gas to return to the low-temperature section of the flue gas waste heat boiler again to complete heat exchange, the outlet of the flue gas waste heat boiler is divided into two paths, one path of the flue gas waste heat boiler leads the flue gas at the outlet of the waste heat boiler into the carbon dioxide collecting system through the first draught fan, and the other path of the flue gas waste heat boiler leads the flue gas at the outlet of the flue gas waste heat boiler into the inlet of the flue gas waste heat boiler through the flue gas circulating fan.
4. The apparatus for capturing and purifying carbon dioxide from flue gas of glass kiln as claimed in claim 1, wherein the carbon dioxide capturing system comprises a water washing desulfurization and denitrification apparatus for cooling flue gas and desulfurization and denitrification and an adsorption and desorption apparatus for adsorbing carbon dioxide discharged from flue gas to obtain high concentration carbon dioxide.
5. The device for capturing and purifying the carbon dioxide in the flue gas of the glass kiln as claimed in claim 4, wherein the water-washing desulfurization and denitrification device comprises a water-washing desulfurization tower, the water-washing desulfurization tower is internally provided with a filler, the flue gas enters the tower from the lower part of the desulfurization water-washing tower, the bottom of the water-washing desulfurization tower is used for cooling and dedusting the flue gas, the middle part of the water-washing desulfurization tower is provided with a desulfurization solution flowing from top to bottom for absorbing sulfur dioxide and nitrogen dioxide in the flue gas, and the desulfurization water-washing tower is connected with a second induced draft fan and sends the flue gas to the adsorption and desorption device.
6. The apparatus for capturing and purifying carbon dioxide in flue gas of glass kiln as claimed in claim 5, wherein the adsorption and desorption apparatus comprises at least 7 pressure swing adsorption towers, the pressure swing adsorption towers are connected with the water washing desulfurization tower, each pressure swing adsorption tower is stored with filler and adsorbent for absorbing easily-adsorbed components in the flue gas, the components which are not easily adsorbed flow out from the top of the tower, are discharged after denitration, and then desorb the easily-adsorbed components to obtain high-concentration CO2, the pressure swing adsorption towers sequentially undergo the steps of adsorption, 3 times of pressure drop equalization, reverse release, 3 times of pressure rise, and final pressure rise, and it is ensured that 2 adsorption towers are in a state of feeding adsorption and producing carbon dioxide gas at any moment, and the pressure swing adsorption towers convey high-concentration CO2 to the carbon dioxide refining system through connecting pipes.
7. The device for capturing and purifying carbon dioxide in glass kiln flue gas as claimed in claim 1, wherein: the carbon dioxide refining system comprises a compression adsorption device, a freezing liquefaction device and a rectification and finished product storage device which are sequentially connected.
8. The device for capturing and purifying the carbon dioxide in the flue gas of the glass kiln as claimed in claim 7, wherein the compression and adsorption device comprises a buffer tank, a compressor, a desulfurization bed and an adsorption bed, the buffer tank is connected with the carbon dioxide capture system, the buffer tank, the compressor, the desulfurization bed and the adsorption bed are sequentially connected, the adsorption bed comprises three adsorption towers, the adsorption towers respectively adsorb, heat and cool blow the carbon dioxide gas at the same time, and the adsorption bed is connected with the freezing and liquefying device.
9. The apparatus for capturing and purifying carbon dioxide in flue gas of glass kiln as claimed in claim 8, wherein the freezing liquefaction device comprises a refrigeration compressor, a condenser, a liquid receiver, a CO2 liquefaction device and a gas-liquid separator, the refrigeration compressor, the condenser, the liquid receiver and the gas-liquid separator are connected in sequence into a cycle for cooling and liquefying carbon dioxide gas in the CO2 liquefaction device, and the cooled and liquefied carbon dioxide gas and light component gas are sent to the rectification and finished product storage device together.
10. The apparatus for capturing and purifying carbon dioxide in glass kiln as claimed in claim 9, wherein the rectification and storage device comprises a rectification column and a food-grade product storage tank, and the rectification column is connected with the food-grade product storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120367195.9U CN215259901U (en) | 2021-02-10 | 2021-02-10 | Glass kiln flue gas carbon dioxide's entrapment purification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202120367195.9U CN215259901U (en) | 2021-02-10 | 2021-02-10 | Glass kiln flue gas carbon dioxide's entrapment purification device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN215259901U true CN215259901U (en) | 2021-12-21 |
Family
ID=79501632
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202120367195.9U Active CN215259901U (en) | 2021-02-10 | 2021-02-10 | Glass kiln flue gas carbon dioxide's entrapment purification device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN215259901U (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114459236A (en) * | 2022-01-29 | 2022-05-10 | 西南化工研究设计院有限公司 | Energy-saving cement kiln flue gas carbon capture method |
| CN115445377A (en) * | 2022-09-06 | 2022-12-09 | 国网河北能源技术服务有限公司 | Carbon dioxide capture system for flue gas of thermal power generating unit |
| CN115779632A (en) * | 2022-12-01 | 2023-03-14 | 华中科技大学 | Charcoal capture CO 2 Method and system for preparing combustible gas by coupling photo-thermal catalytic conversion |
| WO2024174479A1 (en) * | 2023-02-21 | 2024-08-29 | 中建材玻璃新材料研究院集团有限公司 | Device for coupled oxygen-fuel combustion of cement and capture and purification of carbon dioxide in flue gas |
-
2021
- 2021-02-10 CN CN202120367195.9U patent/CN215259901U/en active Active
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114459236A (en) * | 2022-01-29 | 2022-05-10 | 西南化工研究设计院有限公司 | Energy-saving cement kiln flue gas carbon capture method |
| CN115445377A (en) * | 2022-09-06 | 2022-12-09 | 国网河北能源技术服务有限公司 | Carbon dioxide capture system for flue gas of thermal power generating unit |
| CN115445377B (en) * | 2022-09-06 | 2024-06-11 | 国网河北能源技术服务有限公司 | Carbon dioxide trapping system for flue gas of thermal power generating unit |
| CN115779632A (en) * | 2022-12-01 | 2023-03-14 | 华中科技大学 | Charcoal capture CO 2 Method and system for preparing combustible gas by coupling photo-thermal catalytic conversion |
| WO2024174479A1 (en) * | 2023-02-21 | 2024-08-29 | 中建材玻璃新材料研究院集团有限公司 | Device for coupled oxygen-fuel combustion of cement and capture and purification of carbon dioxide in flue gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN113310063A (en) | Device and method for capturing and purifying carbon dioxide in glass kiln flue gas | |
| CN215259901U (en) | Glass kiln flue gas carbon dioxide's entrapment purification device | |
| CN101874967B (en) | Process for removing acid gas with low-temperature methanol solution | |
| WO2022037204A1 (en) | Blast furnace gas desulfurization apparatus and method | |
| CN113975950B (en) | System and method for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA method | |
| WO2024174479A1 (en) | Device for coupled oxygen-fuel combustion of cement and capture and purification of carbon dioxide in flue gas | |
| CN109794137B (en) | Method and system for adsorbing, purifying, enriching and recovering nitrogen oxides in flue gas | |
| CN110683544A (en) | Method for improving concentration of carbon dioxide in tail gas of lime rotary kiln | |
| CN111495113A (en) | Fixed bed type low-temperature flue gas adsorption desulfurization system and method | |
| CN114405218A (en) | Low partial pressure waste gas CO2Trapping and purifying refining process | |
| CN103492048B (en) | For the low NO of drier xthe system and method for discharge regeneration | |
| CN212283448U (en) | Fixed bed type flue gas low-temperature adsorption desulfurization system | |
| CN210332252U (en) | To CO in cement kiln tail flue gas2Trapping, concentrating and utilizing system | |
| CN103159580B (en) | Method of purifying and extracting methane in waste landfill gas | |
| CN216457971U (en) | System for synchronously recycling carbon dioxide and nitrogen in flue gas by chemical method and PSA (pressure swing adsorption) method | |
| CN212327831U (en) | Environmental-friendly resourceful treatment system for fireflood tail gas | |
| CN215250669U (en) | Feed gas purification system for hydrogen production from coke oven gas | |
| CN211595550U (en) | Natural gas decarbonization system | |
| CN211595551U (en) | Natural gas decarbonization system | |
| CN113731098A (en) | Environmental-friendly resourceful treatment system and process flow for fireflooding tail gas | |
| CN203498341U (en) | Semi-coke tail gas desulfurization purifying device | |
| CN110227337A (en) | CO in a kind of pair of cement kiln end flue gas2Trapping concentrate with utilize system | |
| CN111362229A (en) | Method for preparing hydrogen for fuel cell from yellow phosphorus tail gas | |
| CN105779029A (en) | Semi-coke tail gas desulphurization purifier | |
| CN111214926A (en) | Waste gas recovery processing system and method based on LNG cold energy utilization |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |