Boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device

Abstract

A boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device, comprising: an adsorption tower; a sealing separation component, the sealing separation component is arranged in the adsorption tower, and the sealing separation component divides the internal space of the adsorption tower into a plurality of cavity structures in the adsorption tower and along the gas flow path; fillers, which include various types of fillers according to the adsorption sequence, filler pore size, adsorption strength, and analytical conditions and are respectively filled in different cavity structures. Multiple layers of fillers are arranged inside the adsorption tower and are arranged according to the adsorption sequence, filler pore size, adsorption strength, and analytical conditions. A variety of different fillers are filled separately and then loaded together in the adsorption tower, and the filler layers are isolated. The present invention adopts sealing layer filling, and uses special sealing separation components between the filler layers to ensure that the fillers are not mixed, and it is simple and quick to replace a layer of fillers. After the present invention is put into use, the one-year attenuation rate of the pressure swing adsorption purification device is significantly reduced.

Description

Technical Field

[0001] The present invention belongs to the technical field related to raw gas purification equipment, and more specifically, particularly relates to a boiler flue gas carbon dioxide capture and nitrogen co-production device analytical gas purification device. Background Art

[0002] At present, the technical route used for capturing carbon dioxide from boiler flue gas in power plants is PSA pressure swing adsorption and ammonia absorption. The tail gas after capturing carbon dioxide is discharged directly or reused after simple filtration. This tail gas contains a large amount of toxic and harmful components such as aerosols. When these components are discharged, they will pollute the atmosphere. When used, they will cause great pollution and poisoning to the core separation materials in the subsequent utilization and purification devices.

[0003] The current technical status is to use physical cooling combined with multi-stage physical filtration to physically filter the particles with a diameter of 1-5 microns in the exhaust gas and then reuse them. The technical problems of this method are: it is impossible to remove toxic and harmful pollutants with a diameter of nanometers. Such aerosol toxic and harmful pollutants will adhere to the core separation material when the exhaust gas is purified, causing the separation material to be poisoned and the separation efficiency to be sharply reduced. The technical indicators of the product gas do not meet the standards, the product gas volume is reduced, and the product gas purity is reduced. Summary of the invention

[0004] 1. Technical issues

[0005] In summary, how to pre-purify the raw gas to improve the quality of the product gas has become an urgent problem to be solved by those skilled in the art.

[0006] (II) Technical solution

[0007] The present invention provides a decomposition gas purification device for a boiler flue gas capture carbon dioxide co-production nitrogen device. In the present invention, the decomposition gas purification device for a boiler flue gas capture carbon dioxide co-production nitrogen device comprises:

[0008] An adsorption tower, wherein the adsorption tower is a tank structure, a first gas port is provided at one end of the adsorption tower, and a second gas port is provided at the other end of the adsorption tower, wherein the first gas port and the second gas port are used for air intake and air discharge, respectively;

[0009] A sealing separation component, wherein a plurality of the sealing separation components are provided, and all of the sealing separation components are provided in the adsorption tower, and in the adsorption tower and along the gas flow path, the sealing separation components divide the internal space of the adsorption tower into a plurality of cavity structures;

[0010] The filler includes various types according to the adsorption order, filler pore size, adsorption strength, and analytical conditions, and is respectively filled in different cavity structures.

[0011] Preferably, in the boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device provided by the present invention, in the adsorption tower and along the gas flow path, the filler filled in the first cavity structure forms a first filler layer, and the first filler layer is a large-pore spherical adsorption filler with a diameter of 3-5 mm, a strength of 150 N, and a bulk density of 750 kg / m 3 The pore size is 5 nanometers, which is used to adsorb water and carbon dioxide in the mixed gas source. After adsorption by this filler layer, the dew point can be reduced to -60°C and the carbon dioxide concentration can be reduced to 2.8%.

[0012] Preferably, in the boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device provided by the present invention, in the adsorption tower and along the gas flow path, the filler filled in the second cavity structure forms a second filler layer, and the second filler layer is a medium-pore spherical adsorption filler with a diameter of 3-5mm, a strength of 80N, and a bulk density of 720kg / m 3 The pore size is 0.4-0.5 nanometers, which is used to improve the adsorption of impurities and compounds. The total content of impurities and compounds in the gas after adsorption by the second filler layer is less than 10μg / m3.

[0013] Preferably, in the boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device provided by the present invention, in the adsorption tower and along the gas flow path, the filler filled in the third cavity structure forms a third filler layer, and the third filler layer is a small-pore particle adsorption filler with a diameter of 1.0-1.3 mm, a strength of 65 N, and a bulk density of 700 kg / m 3 , pore size is 0.3-0.4 nanometers, used to adsorb residual impurities and compounds of 10μg / m3.

[0014] Preferably, in the analytical gas purification device for the boiler flue gas carbon dioxide capture and nitrogen co-production device provided by the present invention, each packing layer filled in the adsorption tower can be analyzed and replaced individually.

[0015] Preferably, in the analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas provided by the present invention, a plurality of adsorption towers are provided, and all of the adsorption towers are arranged in parallel.

[0016] Preferably, in the boiler flue gas carbon dioxide capture and nitrogen co-production device analysis gas purification device provided by the present invention, at least three adsorption towers are provided, and among all the adsorption towers shown, at least one adsorption tower is in the analysis working state, and at least two of the adsorption towers are in the adsorption working state.

[0017] Preferably, in the boiler flue gas carbon dioxide capture and nitrogen co-production device provided by the present invention, among all the adsorption towers, the number of adsorption towers in the adsorption working state is at least twice the number of adsorption towers in the desorption working state.

[0018] Preferably, in the boiler flue gas capture carbon dioxide and co-production nitrogen analysis gas purification device provided by the present invention, all of the adsorption towers include two working modes, namely, zero gas consumption mode and micro gas consumption mode, wherein the zero gas consumption mode does not discharge the raw gas, and the micro gas consumption mode discharges the raw gas, and the venting volume of the raw gas is 3%, that is, 3% gas loss.

[0019] Preferably, in the boiler flue gas capture carbon dioxide and co-production nitrogen device analytical gas purification device provided by the present invention, the boiler flue gas capture carbon dioxide and co-production nitrogen device analytical gas purification device adopts a zero gas consumption and micro gas consumption mixed working mode, wherein the zero gas consumption mode works for 3-4 hours, the micro gas consumption mode works for 1-2 hours, and the total switching time is 4-6 hours. The working process can be appropriately extended or shortened according to the working status; if the mixed process is not applicable, the zero gas consumption or micro gas consumption process is adopted alone.

[0020] (III) Beneficial effects

[0021] As can be seen from the above, the present invention provides a boiler flue gas carbon dioxide capture and nitrogen co-production device and an analytical gas purification device, comprising: an adsorption tower, the adsorption tower is a tank structure, a first gas port is provided at one end of the adsorption tower, and a second gas port is provided at the other end of the adsorption tower, the first gas port and the second gas port are respectively used for air intake and air discharge; a sealing separation component, a plurality of the sealing separation components are provided, all of the sealing separation components are arranged in the adsorption tower, and in the adsorption tower and along the gas flow path, the sealing separation component divides the internal space of the adsorption tower into a plurality of cavity structures; a filler, according to different adsorption order, filler pore size, adsorption strength, and analytical conditions, the filler includes a plurality of types and is respectively filled in different cavity structures.

[0022] In the present invention, multiple layers of fillers are arranged inside the adsorption tower. A variety of different fillers are arranged according to the order of adsorption, filler pore size, adsorption strength, and analysis conditions. The various different fillers are filled separately, and then loaded together in the adsorption tower, and the filler layers are isolated. The present invention adopts sealing layer filling, and a special sealing separation component is used between the filler layers to ensure that the fillers are not mixed, and it is simple and quick to replace a certain layer of filler; in actual use, if one of the fillers cannot be analyzed and regenerated after adsorption, it can be considered to replace this filler separately, and other fillers can continue to be used. After the present invention is put into use, it uses a mixed working mode to work continuously. Compared with before the adsorption purification device was used, the proportion of element increase was significantly reduced, and the proportion increase was <2%. The one-year attenuation rate of the pressure swing adsorption purification device has been significantly reduced. BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Figure 1 It is a schematic diagram of the structure of an adsorption tower in a desorption gas purification device of a boiler flue gas carbon dioxide co-production nitrogen device in one embodiment of the present invention;

[0024] Figure 2 This is a schematic structural diagram of an analytical gas purification device for a boiler flue gas carbon dioxide capture and nitrogen co-production device in an embodiment of the invention.

[0025] exist Figure 1 and Figure 2 In the figure, the corresponding relationship between the component names and the reference numerals is as follows:

[0026] Adsorption tower 1, sealing separation component 2, filler 3, raw gas delivery pipe 4, adsorption air intake pipeline 5, analysis air intake pipeline 6, proportional control valve 7. DETAILED DESCRIPTION

[0027] In order to make the objectives, technical solutions and advantages of the present invention more clear, the embodiments of the present invention will be further described in detail below with reference to the accompanying drawings.

[0028] Please refer to Figure 1 and Figure 2 ,in, Figure 1 It is a schematic diagram of the structure of an adsorption tower in a desorption gas purification device of a boiler flue gas carbon dioxide co-production nitrogen device in one embodiment of the present invention; Figure 2 This is a schematic structural diagram of an analytical gas purification device for a boiler flue gas carbon dioxide capture and nitrogen co-production device in an embodiment of the invention.

[0029] The present invention provides a boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device, the process of the device is described as follows: the main components of the tail gas of the boiler flue gas after the carbon dioxide capture device are nitrogen (89%), oxygen (8%), carbon dioxide (3%) and a small amount of impurities; first, after cooling and physical filtration by a three-stage filter, the impurities in the tail gas are removed and then enter the pressure swing adsorption purification device; then, the oxygen and carbon dioxide in the gas source can be separated by the pressure swing adsorption purification device, and high-purity 99.9% nitrogen can be obtained. The present invention adopts the method of cooling + physical filtration to remove large particle impurities with a particle size of 1-3 microns, meeting the working conditions of the pressure swing adsorption nitrogen purification equipment.

[0030] However, the above process also has certain technical problems: after 1-2 years of long-term operation of the pressure swing adsorption nitrogen purification equipment, it was found that the gas production and purity of the 99.9% pure nitrogen product gas were attenuated, and the attenuation rate was much higher than the normal attenuation rate of 3-5% / year. Among many devices, the highest attenuation rate was as high as 21%, and the rest were 17-20%, and the energy consumption would also increase by 20-23%.

[0031] After facing the above problems, we conducted a problem investigation. After repeated inspections, we found that the pressure swing adsorption nitrogen purification device itself did not have any electrical or mechanical faults. We further analyzed whether the poisoning of filler 3 was caused by abnormal gas source components. After multiple routine on-site air bag sampling, testing, and analysis, we found that the gas source did not contain conventional gas components that cause filler 3 poisoning (such as chlorine, oil, etc.). We continued to take samples to detect whether the gas source contained sulfides, nitrogen oxides, etc. After testing, we found that it contained sulfides below 0.1ppm and nitrogen oxides below 0.1ppm. This content was not enough to cause short-term poisoning of the separation filler. We took samples again to detect whether the gas source contained organic compounds such as methane, propane and n-butane. The content was all below 0.1ppm, which was not the main factor causing the poisoning.

[0032] After opening the pressure swing adsorption nitrogen purification device, the packing was sampled and separated, and no obvious changes were found in appearance. After elemental analysis, new elements were found. After sampling different bed heights and different working cycles to separate raw materials for analysis, it was found that all the tested packings had new elements. After comparison and summary, it was found that the amount of elements added in packing 3 changed regularly: the amount of elements gradually decreased from the bottom to the top layer, and the amount of elements gradually decreased from long to short working cycles. After many analyses and discussions, it was concluded that the source of the new elements was the gas source, and the gas source contained the morphological compounds of the new elements.

[0033] Through a self-made absorption test device, pure water or other absorbents are used in the test device. A stable flow of gas source is passed through the test device to detect the substances added in the absorbent. The mass content is calculated based on the gas source flow rate and absorption time. The following impurities are determined in the gas source:

[0034]

[0035] A magnet was used to conduct an attraction comparison experiment on the sampled and new fillers. The new fillers had no magnetism, while all the sampled fillers were magnetic, and the strength of the magnetism changed in a regular pattern: the magnetism gradually decreased from the bottom to the top layer, and the magnetism gradually decreased from a long to a short working cycle.

[0036] After the problem was identified, the solutions attempted were as follows: After testing, it was found that the impurities contained in the gas source had an impact on the performance and service life of the separation filler, and such impurities were filtered and removed. On the basis of the original cooling and multi-stage filtration, the cooling device was improved to further cool the temperature from the original cooling temperature of 35°C to 25°C. After monitoring the operation for one week, it was found that there was no increase in the above-mentioned impurities in the sewage after cooling. The temperature was further reduced from 25°C to 8°C, and no increase in impurities was found in the sewage after cooling after monitoring the operation for one week. This cooling temperature has reached the limit value of conventional cooling and pressure swing adsorption, and no further cooling attempts can be made. The possibility of separation and precipitation at low temperatures is ruled out.

[0037] On the basis of the existing equipment, two levels of filtration are added, and the filtration accuracy is increased to 0.01 micron and 0.003 micron. It is used in conjunction with the cooling temperature 8℃ process. After one week of monitoring and operation, it is found that there is no increase in impurity components in the sewage of the filter. Add a self-made activated carbon adsorption tower 1 of the first level company, and fill the tank with columnar granular activated carbon with an iodine value of more than 1000 for adsorption and filtration. After one week of monitoring and operation, it is found that there is no increase in impurity components in the sewage of each level of filter and activated carbon adsorption tower 1. A self-made strong magnetic filter is installed at the outlet of the 5-micron filter to try to remove divalent and trivalent iron from impurities. After four weeks of operation, the cover of the strong magnetic filter is opened, and no visible residues are found around the strong magnet. The strong magnetic filter is placed at the outlet of the self-made activated carbon adsorption tower 1. After four weeks of operation, the cover of the strong magnetic filter is opened, and no visible residues are found around the strong magnet. Summary: Impurities do not have pure magnetism and cannot be directly attracted by magnets; impurities cannot be filtered out by physical filters with a filtration accuracy of 0.003 microns, and the impurity particle size is less than 0.003 microns.

[0038] Based on the experience gained from many attempts, it is estimated that the particle size of impurities is less than 0.003 microns. Combined with the characteristics of the gas source components, nitrogen (89%), oxygen (8%), and carbon dioxide (3%), try to use a conventional adsorption dryer. Add a 180Nm 3 / min processing capacity, pressure dew point -40℃ micro-heat regeneration adsorption dryer, installed after cooling device and 0.01 micron filter, before commissioning, the adsorption dryer packing 3 is sampled and sealed. After commissioning and stable operation, the dew point is maintained at -62℃, and the dew point fluctuates slightly to -60℃ when the double towers are switched. The monitoring operation was carried out for one, two and four weeks, and the sewage outlets of filters at all levels, cooling device sewage outlets, and activated carbon adsorption tower 1 sewage outlets were recorded respectively. No impurities were found in the above sewage, and there was no visible residue around the strong magnetic field of the strong magnetic filter. The adsorption dryer operated stably, the dew point curve was stable, and it operated normally without any faults. After three months of continuous monitoring, the equipment still operated stably, the dew point curve was stable, and it was operating normally without any faults. After the machine was started and operated for a total of six months, it operated stably during the period with a stable dew point. After the machine was shut down, the filling and unloading ports were opened to take the top and bottom filler 3 samples 1 and 2 respectively, and compared with the sealed sample 3 for analysis. It was found that although the amount of some elements in samples 1, 2 and sample 3 increased, the increase ratio was low, and the increase ratio was less than 0.5%, and the difference between sample 1 and sample 2 was less than 0.1%. It can be concluded that: 1. Impurities cannot be adsorbed by the filler 3 of the conventional adsorption dryer, and 2. After being adsorbed, they cannot be precipitated after being purged and cleaned by high-temperature pressure reduction. Because the adsorption dryer has two working processes of adsorption and analysis when working, the above two conclusions cannot be accurately judged, so the dryer is adjusted as follows: the dryer only performs low-temperature adsorption and does not perform high-temperature regeneration and analysis, and the dew point of the air source treated by the dryer is no longer monitored. After four months of operation, samples 4 and 5 were taken from the top and bottom fillers 3 for testing. After comparing the test reports of samples 1 and 2, the element increase ratio of sample 4 / 5 was also less than 0.5% compared with sample 1 / 2, and the difference between sample 4 and sample 5 was less than 0.1%. It can be determined that impurities cannot be adsorbed by the filler 3 of the conventional adsorption dryer.

[0039] It took one year from the discovery of the attenuation to the last technical transformation attempt mentioned above. During this period, the equipment was in a state of continuous attenuation, and the average attenuation rate calculated over the cumulative time was 17.4% / year.

[0040] Summary and analysis of the stage: The characteristics of the separation packing adsorption of the pressure swing adsorption purification device are that the separation packing preferentially adsorbs oxygen and carbon dioxide, and nitrogen passes through the separation packing to achieve the separation of oxygen, carbon dioxide, and nitrogen, and the target gas nitrogen is concentrated to more than 99.9%. The equipment's finished gas volume and purity attenuation rate is as high as 20%, which is much higher than the normal production attenuation rate of 3-5% / year, and the energy consumption increases by 20-23%. The main reason is that impurities or impurity compounds enter the pressure swing adsorption purification device with the gas source and adhere to the surface of the separation packing. With repeated pressure increase adsorption and pressure reduction analysis, they enter the micropores of the packing and cause pore blockage, and cannot be discharged through the normal analysis step, causing the separation packing to be blocked and poisoned, destroying the polarity of the separation packing, and rapidly reducing the separation efficiency of oxygen, nitrogen, and carbon dioxide (annual attenuation rate is as high as 17-20%), so that the final finished nitrogen flow and purity do not meet the standards, and greatly increase the energy consumption of the equipment (energy consumption increases by 20-23%). The poisoned filler cannot be analyzed through conventional process steps, and the performance of the filler can be improved through factory activation technology. Samples were taken from one of the 3# machines with the largest attenuation, with a sample quantity of 730kg (sample 6) sent to the company, and 330kg of them were randomly loaded into the experimental device. Air was used as the raw gas to separate oxygen and nitrogen, and the separation efficiency and gas consumption were recorded; a mixture of 92% pure nitrogen and 8% pure oxygen produced by the gas generation platform was used as the raw gas to separate oxygen and nitrogen, and the separation efficiency and gas consumption were recorded. After the quantity was confirmed to be correct, 330kg of filler in the experimental device was taken out and mixed into the remaining sample 6, and evenly divided into two batches of samples, 360kg each for sample 7 and sample 8, and the remaining 10kg was sample 9, which were activated and regenerated under different processes. The activation and regeneration conditions of sample 7 are: activation temperature 350℃, activation time 3 hours, activation environment nitrogen replacement slightly positive pressure; the activation and regeneration conditions of sample 8 are: activation temperature 500℃, activation time 3 hours, activation environment nitrogen replacement slightly positive pressure; the activation and regeneration conditions of sample 9 are: activation temperature 500℃, activation time 5 hours, activation environment vacuum negative pressure -50kPa (gauge pressure). The loss rates after activation are 5%, 5.3%, and 5.8% respectively. After activation, air and mixed gas separation tests were performed on sample 7 and sample 8 after filling, and static adsorption was performed on sample 9. The performance indicators before activation were compared as follows:

[0041]

[0042]

[0043] The performance growth rate is negative, which means that the separation efficiency is further reduced; the gas consumption reduction rate is positive, which means that the energy consumption is further increased. The performance of the three samples after activation is further reduced, which is contrary to the activation and regeneration effect of similar fillers, and the difference is large. In other similar projects, similar separation fillers can be improved to 75-85% of the performance of new fillers after activation and regeneration (activation and regeneration conditions are the same as sample 7). The basic principle of activation and regeneration is to vaporize the pollutants attached to the surface of the filler or in the micropores at high temperature, and then use inert gas to purge and replace the precipitated pollutants (or use vacuum negative pressure). It is a direct and effective technical means for general pollutants. However, for samples 7 / 8 / 9, not only did the efficiency not improve but decreased. It is inferred that the pollutants reacted with the filler at high temperature, further aggravating the pore blocking and poisoning phenomenon, and there is no need to perform element detection on the activated filler.

[0044] Interim summary: After activation regeneration, cooling, multi-stage filtration, and technical transformation experiments of conventional adsorption dryers, there was no effect. Combined with the recorded experimental results, it was inferred that the particle size of the impurity pollutants is less than 5 nanometers, and it is easy to react chemically with the filler at high temperature. Even when using the blocking method for regeneration, heating and decomposition regeneration cannot be used.

[0045] Through the above-mentioned multiple stages of problem processing and analysis, the present invention intends to use a newly designed multi-tower adsorption equipment for gas source purification. The equipment name is a boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device. The design idea is: using a combination of large, medium and small pore size fillers for adsorption purification and analytical regeneration. The analysis does not use heating analytical regeneration, but uses normal temperature analytical regeneration; the fillers are isolated between the multiple filler layers. If it is found that the analytical regeneration cannot be completed after adsorption purification, the impurities can be blocked from entering the next level of pressure swing adsorption purification system by regularly replacing this part of the filler; when designing analytical regeneration, the gas source after analysis is considered to enter the next level of adsorption tower 1 for use, and cannot be directly emptied, wasting a large amount of tower gas and purge gas, which is defined as zero gas consumption. If zero gas consumption adsorption purification cannot be achieved, micro gas consumption adsorption purification can be used. After adsorption, the gas in the tower is discharged in small amounts, and the analytical regeneration gas is directly discharged into the atmosphere. The discharge amount can be adjusted, which is defined as micro gas consumption, and the gas consumption does not exceed 3%. The feasibility of switching between the two adsorption purification processes and the mixed application of the two adsorption purification processes must be comprehensively considered during the design; the pore size, strength, and adsorption of the filler to the gas source and impurities are comprehensively considered, and the structural design is used to maximize the adsorption capacity. An innovative three-tower adsorption structure is planned to ensure simultaneous adsorption purification in two towers and analysis and regeneration in one tower; a reasonable structure inside the tower, a large gas source volume, and high pressure require a reasonable airflow distribution to control the empty tower flow rate and increase the service life of the filler. It is planned to use a bottom airflow diffuser and a top airflow collector for 6-point uniform diffusion and collection. The finite element simulation analysis structure has been used. The bottom airflow diffuser is evenly filled with inert alumina to avoid direct contact with the filler and cause a large impact on the filler; when switching between multiple towers, it is necessary to consider pressure drop and reversal, reduce the number of airflow reversals in the tower, and reduce the pressure drop after airflow reversal. It is planned to use equal pressure reversal or reversal after equal pressure; manual sampling and venting ports are set on the tower body and pipelines.

[0046] The present invention provides a desorption gas purification device for a boiler flue gas carbon dioxide capture and nitrogen co-production device, comprising an adsorption tower 1, the adsorption tower 1 is a tank structure (a metal tank structure is adopted), a first gas port is arranged at one end of the adsorption tower 1 along the length direction of the adsorption tower 1 (it can also be understood as along the gas flow path inside the adsorption tower 1), and a second gas port is arranged at the other end of the adsorption tower 1, and the first gas port and the second gas port are respectively used for air intake and air discharge.

[0047] The structure of the adsorption tower 1 is as follows: the adsorption tower 1 is filled with filler 3, which is used to adsorb and purify impurities in the raw gas. There are multiple adsorption towers 1, and all the adsorption towers 1 are arranged in parallel. Among all the adsorption towers 1, at least one adsorption tower 1 is in a decomposition working state, and at least two adsorption towers 1 are in an adsorption working state. Specifically, a first gas port is arranged at one end of the adsorption tower 1, and two parallel branches are arranged on the first gas port, namely the first branch and the second branch. A second gas port is arranged at the other end of the adsorption tower 1, and two parallel branches are arranged on the second gas port, namely the third branch and the fourth branch. Among them, in all the adsorption towers 1 shown, the first branch is connected through an adsorption outlet pipeline, the third branch is connected through an adsorption inlet pipeline 5, the second branch is connected through a decomposition inlet pipeline 6, and the fourth branch is connected through a decomposition outlet pipeline.

[0048] The present invention is also provided with a raw gas delivery pipe 4, which is connected to the adsorption air intake pipeline 5 and the desorption air intake pipeline 6, and can independently deliver air to the adsorption air intake pipeline 5 or the desorption air intake pipeline 6 by controlling the valve. In order to realize the control of the air path, the present invention is provided with individually controllable valves on each branch. Furthermore, the valve provided on the third branch is a proportional regulating valve 7, and the other valves are all switch valves.

[0049] In the adsorption tower 1 and along the gas flow path, the adsorption tower 1 is filled with multiple packing layers, and the packing 3 in each packing layer can be replaced separately; a sealing separation component 2 is provided between each packing layer to separate and pack each packing layer; and the particle size and pore size of the packing 3 in each packing layer are different. At the same time, airflow diffusers are provided in the adsorption tower 1 and near both ends of the adsorption tower 1.

[0050] In the above structural design, the raw gas enters the adsorption tower 1 from the bottom, then passes through each packing layer in turn (from bottom to top), and finally is discharged from the top, thereby achieving adsorption purification of the raw gas. In the analysis process, the raw gas enters the adsorption tower 1 from the top as a purge gas, then passes through each packing layer in turn (from top to bottom), thereby achieving analysis and recovery of each packing layer.

[0051] As for the specific structure of the adsorption tower 1, the present invention is provided with a sealing separation component 2 in the tower body of the adsorption tower 1, and a plurality of sealing separation components 2 are provided, and all of the sealing separation components 2 are provided in the adsorption tower 1. In the adsorption tower 1 and along the gas flow path, the sealing separation component 2 divides the internal space of the adsorption tower 1 into a plurality of cavity structures. The present invention is provided with a filler 3 in the adsorption tower 1, and the fillers 3 include a plurality of types according to the adsorption sequence, the pore size of the filler 3, the adsorption strength, and the analytical conditions, and are respectively filled in different cavity structures.

[0052] A bracket structure is provided inside the tower body of the adsorption tower 1, and the sealing separation component 2 adopts a metal keel plus a metal mesh structure, and the mesh of the metal mesh is smaller than the particle size of the filler 3 of this layer, so that the smooth passage of the raw gas can be ensured, and the filler 3 can be stably supported. Of course, the sealing separation component 2 can be a cage-type structure, so that the filler 3 of this layer can be completely filled into the sealing separation component 2, which is convenient for the replacement of the filler 3. It should be noted that the sealing separation component 2 and the inner wall of the tower body are in a completely airtight contact structure to prevent the escape of the raw gas.

[0053] In the present invention, in the adsorption tower 1 and along the gas flow path, the filler 3 filled in the first cavity structure forms a first filler layer, and the first filler layer is a large-pore spherical adsorption filler with a diameter of 3-5 mm, a strength of 150 N, and a bulk density of 750 kg / m 3 The pore size is 5 nanometers, which is used to adsorb water and carbon dioxide in the mixed gas source. After adsorption by this filler layer, the dew point can be reduced to -60°C and the carbon dioxide concentration can be reduced to 2.8%.

[0054] In the present invention, in the adsorption tower 1 and along the gas flow path, the filler 3 filled in the second cavity structure forms a second filler layer, and the second filler layer is a medium-pore spherical adsorption filler with a diameter of 3-5 mm, a strength of 80 N, and a bulk density of 720 kg / m 3 The pore size is 0.4-0.5 nanometers, which is used to improve the adsorption of impurities and compounds. The total content of impurities and compounds in the gas after adsorption by the second filler layer is less than 10μg / m 3 .

[0055] In the present invention, in the adsorption tower 1 and along the gas flow path, the filler 3 filled in the third cavity structure forms a third filler layer, and the third filler layer is a small-pore particle adsorption filler with a diameter of 1.0-1.3 mm, a strength of 65 N, and a bulk density of 700 kg / m 3 , pore size is 0.3-0.4 nanometers, used to adsorb residual 10μg / m 3 impurities and compounds.

[0056] Specifically, each packing layer filled in the adsorption tower 1 can be analyzed and replaced individually.

[0057] As can be seen from the above, there are multiple adsorption towers 1, and all the adsorption towers 1 are arranged in parallel. Among them, there are at least three adsorption towers 1, and among all the adsorption towers 1 shown, at least one adsorption tower 1 is in the analysis working state, and at least two adsorption towers 1 are in the adsorption working state. Further, among all the adsorption towers 1, the number of adsorption towers 1 in the adsorption working state is at least twice the number of adsorption towers 1 in the analysis working state. At the same time, all the adsorption towers 1 in the present invention include two working modes, namely zero gas consumption mode and micro gas consumption mode, wherein the zero gas consumption mode does not empty the raw gas, and the micro gas consumption mode emptying the raw gas, and the emptying volume of the raw gas is 3%, that is, 3% gas loss. Furthermore, the boiler flue gas capture carbon dioxide co-production nitrogen device analysis gas purification device adopts a zero gas consumption plus micro gas consumption mixed working mode, wherein the zero gas consumption mode works for 3-4 hours, the micro gas consumption mode works for 1-2 hours, and the total switching time is 4-6 hours. The working process can be appropriately increased or shortened according to the working state;

[0058] If the mixed process is not applicable, the zero gas consumption or low gas consumption process shall be used alone.

[0059] By summarizing the above experience, the present invention proposes a new solution as follows:

[0060] 1. Improvement of composite filler layer:

[0061] The fillers 3 are divided into three different fillers according to the adsorption order, pore size, adsorption strength and analytical conditions. The three fillers are mixed and loaded in the adsorption tower 1 (mixed loading specifically means that each layer is filled with the same filler, and then each layer is loaded into the tower body of the adsorption tower 1), and the filler layers are isolated. The first filler layer is a large-pore spherical adsorption filler 3 with a diameter of 3-5mm, a strength of 150N, and a bulk density of 750kg / m 3 The pore size is 5 nanometers, with strong impact resistance. Its main function is to adsorb a small amount of water and trace carbon dioxide in the mixed gas source. After adsorption by this filler layer, the dew point can be reduced to -60°C and the carbon dioxide concentration can be reduced to 2.8%. The second filler layer is a medium-pore spherical adsorption filler 3 with a diameter of 3-5mm, a strength of 80N, and a bulk density of 720kg / m 3 The pore size is 0.4-0.5 nanometers. The adsorption filler 3 under this pore size has a strong adsorption capacity for impurities and compounds and can be regenerated. The total content of impurities and compounds after adsorption by the second filler layer is less than 10μg / m 3 The third filler layer is a small-pore particle adsorption filler 3 with a diameter of 1.0-1.3 mm, a strength of 65 N, and a bulk density of 700 kg / m 3 The pore size is 0.3-0.4 nanometers, and its main function is to adsorb residual 10μg / m 3The total content of impurities and compounds after passing through three layers of packing is less than 4μg / m 3 . Note: The above data are derived from multiple tests and are theoretical calculation values.

[0062] Through the above structural design, the present invention has the following advantages:

[0063] 1. The packing 3 is easy to replace.

[0064] A sealing layer is used for filling, and a dedicated sealing separation component 2 is used between the filling layers to ensure that the fillings 3 are not mixed, and replacement of a certain layer of fillings 3 is simple and quick; in actual use, if one of the fillings 3 cannot be analyzed and regenerated after adsorption, it can be considered to replace this type of filling 3 alone, and other fillings 3 can continue to be used.

[0065] 2. Diversified processes.

[0066] The work process is diversified, and the main work processes are: zero gas consumption and micro gas consumption. It is planned to use the two processes in combination during work. If the process monitoring data deviates greatly from the design data, the work process can be adjusted at any time. For the zero gas consumption mode, the zero gas consumption three-tower process, the main steps are tower 3 analysis, tower 1 adsorption, tower 2 adsorption; tower 1 analysis, tower 2 adsorption, tower 3 adsorption; tower 2 analysis, tower 3 adsorption, tower 1 adsorption. During adsorption, ensure that the two towers adsorb at the same time and one tower regenerates. Compared with one tower adsorption and one tower regeneration, the adsorption capacity is doubled, which is equivalent to doubling the processing gas volume. The analysis and regeneration tower has zero emissions and does not consume any raw gas. For the micro gas consumption mode, the micro gas consumption three-tower process, the main steps are tower 1 adsorption, tower 2 adsorption, tower 3 analysis; tower 2 adsorption, tower 3 adsorption, tower 1 analysis; tower 3 adsorption, tower 1 adsorption, tower 2 analysis. During double tower adsorption, the third tower is analyzed and regenerated, and the analyzed gas is vented. The venting volume can be adjusted, and the designed venting volume is 3%, that is, 3% gas loss. During adsorption, it is ensured that the two towers adsorb at the same time, and one tower regenerates. Compared with one tower adsorption and one tower regeneration, the adsorption capacity is doubled, which is equivalent to doubling the gas processing volume.

[0067] Design the workflow, zero gas consumption + low gas consumption mixed work, zero gas consumption process working time 3-4 hours, low gas consumption process 1-2 hours, total switching process 4-6 hours, according to the working status can be appropriately extended or shortened workflow. If the mixed process is not applicable, can use zero gas consumption or low gas consumption process alone.

[0068] 3. Actual effect.

[0069] After the equipment was put into use, it was continuously operated and monitored for 12 months using a mixed process. The sampling time was from the 26th to the 28th of each month. The monitoring points were the bottom sewage discharge of adsorption tower 1 and the outlet of finished gas. The inspection device used a self-made absorption inspection device. The test results showed that the total content of impurities and compounds was 4-8μg / m3 ; After the pressure swing adsorption purification device filler 3 was put into operation for 11 months, the sampling and testing showed that the increase ratio of elements was significantly reduced compared with that before the adsorption purification device was used, and the increase ratio was less than 2%; the one-year attenuation rate of the pressure swing adsorption purification device was 5.2%, slightly higher than the average attenuation rate of 3-5% / year. According to various data, the boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device has obvious effects and is an effective product.

[0070] It is known from common technical knowledge that the present invention can be implemented by other embodiments that do not deviate from its spirit or essential features. Therefore, the above disclosed embodiments are only illustrative in all respects and are not exclusive. All changes within the scope of the present invention or within the scope equivalent to the present invention are included in the present invention.

Claims

1. A boiler flue gas capture carbon dioxide co-production nitrogen device analytical gas purification device, characterized in that: include: An adsorption tower, wherein the adsorption tower is a tank structure, a first gas port is provided at one end of the adsorption tower, and a second gas port is provided at the other end of the adsorption tower, wherein the first gas port and the second gas port are used for air intake and air discharge, respectively; A sealing separation component, wherein a plurality of the sealing separation components are provided, and all of the sealing separation components are provided in the adsorption tower, and in the adsorption tower and along the gas flow path, the sealing separation components divide the internal space of the adsorption tower into a plurality of cavity structures; The filler includes various types according to the adsorption order, filler pore size, adsorption strength, and analytical conditions, and is respectively filled in different cavity structures.

2. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to claim 1 is characterized in that: In the adsorption tower and along the gas flow path, the filler filled in the first cavity structure forms a first filler layer, and the first filler layer is a large-pore spherical adsorption filler with a diameter of 3-5 mm, a strength of 150 N, and a bulk density of 750 kg / m 3 The pore size is 5 nanometers, which is used to adsorb water and carbon dioxide in the mixed gas source. After adsorption by this filler layer, the dew point can be reduced to -60°C and the carbon dioxide concentration can be reduced to 2.8%.

3. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to claim 2 is characterized in that: In the adsorption tower and along the gas flow path, the filler filled in the second cavity structure forms a second filler layer, and the second filler layer is a medium-pore spherical adsorption filler with a diameter of 3-5 mm, a strength of 80 N, and a bulk density of 720 kg / m 3 The pore size is 0.4-0.5 nanometers, which is used to improve the adsorption of impurities and compounds. The total content of impurities and compounds in the gas after adsorption by the second filler layer is less than 10μg / m3.

4. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to claim 3 is characterized in that: In the adsorption tower and along the gas flow path, the filler filled in the third cavity structure forms a third filler layer, and the third filler layer is a small-pore particle adsorption filler with a diameter of 1.0-1.3 mm, a strength of 65 N, and a bulk density of 700 kg / m 3 , pore size is 0.3-0.4 nanometers, used to adsorb residual impurities and compounds of 10μg / m3.

5. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to claim 4, characterized in that: Each packing layer filled in the adsorption tower can be analyzed and replaced individually.

6. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to any one of claims 1 to 5, characterized in that: A plurality of adsorption towers are provided, and all of the adsorption towers are arranged in parallel.

7. The analytical gas purification device for capturing carbon dioxide and producing nitrogen from boiler flue gas according to claim 6, characterized in that: At least three adsorption towers are provided. Among all the adsorption towers, at least one adsorption tower is in a decomposition working state, and at least two adsorption towers are in an adsorption working state.

8. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to claim 7, characterized in that: Among all the adsorption towers, the number of adsorption towers in the adsorption working state is at least twice the number of adsorption towers in the desorption working state.

9. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to claim 8, characterized in that: All of the adsorption towers include two working modes, namely zero gas consumption mode and micro gas consumption mode. The zero gas consumption mode does not evacuate the raw gas, and the micro gas consumption mode evacuates the raw gas. The venting volume of the raw gas is 3%, i.e., 3% gas loss.

10. The analytical gas purification device for capturing carbon dioxide and co-producing nitrogen from boiler flue gas according to claim 9, characterized in that: The analytical gas purification device of the boiler flue gas capture carbon dioxide co-production nitrogen device adopts a zero gas consumption plus micro gas consumption mixed working mode, wherein the zero gas consumption mode works for 3-4 hours, the micro gas consumption mode works for 1-2 hours, and the total switching time is 4-6 hours. The work process can be appropriately extended or shortened according to the working state; If the mixed process is not applicable, the zero gas consumption or low gas consumption process shall be used alone.

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