CN209866059U - Tubular reaction component, device and tubular heating furnace for pyrolysis reaction - Google Patents
Tubular reaction component, device and tubular heating furnace for pyrolysis reaction Download PDFInfo
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Abstract
The utility model belongs to the technical field of the organic matter pyrolysis, concretely relates to tubular reaction subassembly, device and tubular heating furnace for pyrolytic reaction. The utility model discloses a pyrolytic reaction device is including the tubular reaction subassembly and the heating element that are used for pyrolytic reaction, the tubular reaction subassembly that is used for pyrolytic reaction includes along the transition district, reaction zone and the pyrolysis gas transport area that carrier gas flow direction communicates in order, wherein, the reaction zone include spherical reaction chamber and rather than the communicating straight tube reaction zone in both sides, the internal diameter D in spherical reaction chamber compares 8-20 with the internal diameter D in straight tube reaction zone: 1; the residence time of the substances to be pyrolyzed in the reaction area can be prolonged, the control is accurate, the uniform mixing degree of the carrier gas and the substances to be pyrolyzed is increased, and the influence on the final organic matter pyrolysis path analysis caused by inaccurate factors of a reaction system is reduced.
Description
Technical Field
The utility model belongs to the technical field of the organic matter pyrolysis, concretely relates to tubular reaction subassembly, device and tubular heating furnace for pyrolytic reaction.
Background
With the development of science and technology and the progress of society, organic chemicals are increasingly kept away from clothes and eating residents in the life of people, and most of the organic chemicals belong to organic matters. When the living goods are discarded and enter the garbage, the garbage can bring potential harm to the environment along with the further treatment of the garbage. The incineration method is a main method for treating domestic garbage, and wastes containing the organic matters possibly release a lot of toxic and harmful substances in the combustion process, thereby causing secondary pollution to the environment. Many scholars establish corresponding device under the laboratory condition to research the high temperature degradation mechanism of these organic matters, and in this in-process, factors such as temperature, dwell time, oxygen concentration all can produce the influence to the degradation mechanism, therefore how accurate control these factors, have become the main bottleneck whether can accurately resolve out the chemical degradation route. The research on the pyrolysis path of the pollutants is usually carried out under pure gas phase conditions, and the interference of other factors such as surface reaction, catalytic reaction and the like is avoided as much as possible, so that a strict pyrolysis device needs to be established, and all influencing factors in the pyrolysis process are required to be accurate as much as possible. The common pyrolysis device is a tubular reactor, and during an experiment, the temperature of the heating furnace is adjusted to realize the regulation of the pyrolysis temperature of the organic matters. For example, chinese patent CN104267140B discloses a tobacco pyrolysis combustion reactor, an analysis system and a method, wherein the tobacco pyrolysis combustion reactor comprises a quartz glass tube, a heating source, a thermocouple and a temperature control system. The device comprises a quartz glass tube, a thermocouple, a temperature control system and a control system, wherein the two ends of the quartz glass tube are provided with openings and are used for containing tobacco samples, the heating source can heat the tobacco samples in the quartz glass tube, the thermocouple is in contact with the quartz glass tube and is connected with the temperature control system, and the temperature control system can control the temperature of the tobacco samples in the quartz glass tube and the temperature keeping time; the system provides an experimental platform for the research on the mechanism of generation of main smoke components in the tobacco pyrolysis combustion process. However, this type of reactor has at least two problems: on one hand, the temperature constant area of the heating furnace is limited, the temperature correction curves of the heating furnaces of various types produced by various manufacturers are not necessarily the same, but no matter the heating furnace is a one-section type heating furnace or a multi-section type heating furnace, after the heating furnace is heated to a certain temperature and is stable, a temperature transition area with different lengths exists between the two ends of the heating furnace and the external environment (room temperature is 25 ℃), the organic matter is difficult to be pyrolyzed under the condition of constant temperature, and the interference is brought to the pyrolysis path of the analyzed organic matter. On the other hand, most of the conventional pyrolysis reactors are straight tubes made of glass, ceramic or quartz, and can be directly placed into a tubular heating furnace. When organic matters enter the reaction tube along with the carrier gas, the organic matters pass through a long transition area, and the retention time in the transition area is too long, so that side reactions occur in the area, and the final analysis of the pyrolysis path of the organic matters is influenced.
SUMMERY OF THE UTILITY MODEL
Therefore, the to-be-solved technical problem of the utility model lies in overcoming the pyrolysis device transition zone proportion among the prior art high, and actual pyrolysis reaction time is inaccurate, to the analytic defect that influences greatly of organic matter pyrolysis route to a tubular reaction subassembly, device and tubular heating furnace for pyrolytic reaction are provided.
Therefore, the utility model discloses technical scheme as follows:
a tubular reaction component for pyrolysis reaction comprises a transition zone, a reaction zone and a pyrolysis gas conveying zone which are sequentially communicated along the flowing direction of carrier gas, wherein,
the reaction zone comprises a spherical reaction chamber and a straight tube reaction zone communicated with the two sides of the spherical reaction chamber, and the ratio of the inner diameter D of the spherical reaction chamber to the inner diameter D of the straight tube reaction zone is 8-20: 1;
the transition region and the pyrolysis gas conveying region are both of straight pipe structures and are respectively connected with the straight pipe reaction regions on two sides of the spherical reaction cavity;
the volume ratio of the reaction zone to the transition zone is greater than 10: 1;
one end of the transition area, which is close to the carrier gas input, is connected with a sample placing area, and one end of the pyrolysis gas conveying area, which is far away from the carrier gas input, is connected with an adsorbing material placing area.
Further, the inner diameter of the straight tube reaction zone is not less than the inner diameter of the transition zone.
Further, the inner diameters of the straight tube reaction zone, the transition zone and the pyrolysis gas conveying zone are consistent.
The utility model also provides a pyrolytic reaction device, be used for pyrolytic reaction's tubular reaction subassembly and cladding in its outside heating element including the aforesaid.
Further, the heating component is a tubular heating furnace.
Furthermore, the transition area of the tubular reaction component for the pyrolysis reaction is also connected with an air inlet pipeline, and the pyrolysis gas conveying area is also connected with a tail gas discharge pipeline.
Further, the heating assembly at least covers the sample placing area, the transition area, the reaction area, the pyrolysis gas conveying area and the adsorbing material placing area of the tubular reaction assembly for pyrolysis reaction.
The utility model also provides a tubular heating furnace, be used for pyrolytic reaction's tubular reaction subassembly or including above-mentioned pyrolytic reaction device including the aforesaid.
The pyrolysis method of the pyrolysis reaction device comprises the following steps:
1) acquiring a temperature correction curve of a pyrolysis reaction device at a pyrolysis temperature;
2) placing organic matters to be pyrolyzed in the sample placing area, and placing an adsorbing material in the adsorbing material placing area;
3) the heating assembly is started and carrier gas is introduced.
Further, the temperature of the sample placement area is at 100-150 ℃; the temperature of the adsorbing material placing area is 150-200 ℃.
Further, the volatilization rate of the organic matters to be pyrolyzed is 0.001-0.1 mol/min.
Further, the organic matter to be pyrolyzed is one of polychlorinated biphenyl, polycyclic aromatic hydrocarbon and dioxin.
Further, the adsorption material is one of XAD-2, XAD-4, XAD-7, XAD-8 and activated carbon.
Further, the organic matter to be pyrolyzed is fixed in the sample placing area by quartz wool.
Further, an adsorbing material is fixed in the adsorbing material placing area by quartz wool.
Further, the carrier gas is a mixed gas of air and an inert gas.
The utility model discloses technical scheme has following advantage:
1. the utility model provides a tubular reaction subassembly for pyrolytic reaction, include transition district, reaction zone and pyrolysis gas transport area that communicate in order along carrier gas flow direction, wherein, the reaction zone includes spherical reaction chamber and rather than the communicating straight tube reaction zone in both sides, and the reaction zone adopts spherical reaction chamber accurate control gas dwell time to be experimental actual pyrolysis reaction time promptly to spherical form is optimum for reactant and carrier gas misce bene, makes the homogeneous that reactant gas concentration is the most possible. In terms of dynamics, the spherical shape (perfect circle) is easier to uniformly mix the gas; therefore, the utility model discloses select spherical reaction chamber as the mode that increases gas path and accurate control gas dwell time. The ratio of the inner diameter D of the spherical reaction cavity to the inner diameter D of the straight pipe reaction area is 8-20: 1, in the proportion range, the residence time in the reaction zone can be ensured to be increased, and the phenomenon that the longer the time required for the target reactant and the carrier gas to be uniformly mixed and reach stable concentration due to overlarge airflow disturbance when the carrier enters the spherical reaction cavity from the straight tube reaction zone can be avoided. The volume ratio of the reaction zone to the transition zone is greater than 10: 1, the residence time of the target reactant in the reaction zone with the carrier gas can be increased to a greater extent closer to the theoretical residence time.
2. The utility model provides a pyrolytic reaction device can increase the organic matter along with the dwell time of carrier gas in the reaction zone, and the theoretical dwell time that is close of bigger degree reduces the influence of other regions to the reaction, reduces the influence of inaccurate factor because of reaction system brings to the utmost to final organic matter pyrolysis route analytic.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic structural view of a tubular reaction assembly for pyrolysis reaction according to the present invention;
FIG. 2 is a schematic structural view of the pyrolysis reaction apparatus of the present invention;
FIG. 3 is a schematic structural view of a tube-type heating furnace provided by the present invention;
FIG. 4 is a temperature correction curve of the pyrolysis reaction apparatus in example 2;
FIG. 5 is a graph of the concentration of pyrolysis products generated in different reactors as a function of temperature.
Description of reference numerals:
1-transition zone, 2-spherical reaction chamber, 3-pyrolysis gas conveying zone, 4-straight tube reaction zone, 5-sample placing zone, 6-adsorbing material placing zone, 7-heating component, 8-air inlet pipeline, 9 tail gas discharge pipeline and 10-heating furnace body.
Detailed Description
The technical solution of the present invention will be described clearly and completely with reference to the accompanying drawings, and obviously, the described embodiments are some, but not all embodiments of the present invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Furthermore, the technical features mentioned in the different embodiments of the invention described below can be combined with each other as long as they do not conflict with each other.
Example 1
As shown in fig. 1, a tubular reaction module for pyrolysis reaction includes a transition zone 1, a reaction zone and a pyrolysis gas delivery zone 3, which are sequentially communicated in a flow direction of a carrier gas, wherein,
the reaction zone comprises a spherical reaction chamber 2 and a straight tube reaction zone 4 communicated with two sides of the spherical reaction chamber 2, wherein the ratio of the inner diameter D of the spherical reaction chamber 2 to the inner diameter D of the straight tube reaction zone 4 is 8-20: 1;
the transition region 1 and the pyrolysis gas conveying region 3 are both of straight pipe structures and are respectively connected with the straight pipe reaction regions 4 on two sides of the spherical reaction cavity 2;
the volume ratio of the reaction zone to the transition zone 1 is greater than 10: 1;
one end of the transition region 1, which is close to the carrier gas input, is connected with a sample placing region 5, and one end of the pyrolysis gas conveying region 3, which is far from the carrier gas input, is connected with an adsorbing material placing region 6.
The spherical reaction cavity 2 is used as a pyrolysis reactor, so that the temperature and time can be accurately controlled in the reaction process, the retention time of the organic matter to be pyrolyzed in the reaction area along with the carrier gas is closer to a theoretical value, and the actual retention time in the transition area 1 and the reaction area can be accurately judged according to the inner diameters of the spherical reaction cavity 2, the straight pipe reaction area 4 and the transition area. In addition, the spherical shape is most suitable for uniformly mixing the reactant and the carrier gas, so that the concentration of the reactant gas is uniform to the greatest extent possible, and the analysis of the pyrolysis path of the organic matters is facilitated. The transition area 1 is an area where organic matters to be pyrolyzed enter the reaction area along with the volatilization of carrier gas, and basically no chemical reaction occurs in the transition area 1; the reaction zone is a zone where reaction of the organic matter to be pyrolyzed occurs, and more than 99% of the reaction occurs in the zone; the pyrolysis gas delivery zone 3 is the zone where the reacted substances flow with the carrier gas until they are adsorbed by the adsorbent material.
The ratio of the inner diameter D of the spherical reaction cavity 2 to the inner diameter D of the straight tube reaction zone 4 is 8-20: 1. controlling the inner diameter ratio of the spherical reaction cavity 2 and the straight tube reaction zone 4, on one hand, in order to accurately calculate the retention time of the organic matter in different areas along with the carrier gas, the larger the inner diameter ratio is, the longer the retention time in the spherical reaction cavity 2 is, the better the uniform mixing degree of the carrier gas and the reactant is; on the other hand, the larger the inner diameter ratio, the better, both the actual situation and the gas flow condition of the gas at the connecting part of the straight tube reaction zone 4 and the spherical reaction chamber 2 are considered, the larger the ratio is, the larger the disturbance of the gas flow when the carrier gas enters the spherical reaction chamber 2 from the straight tube reaction zone 4 is, and the longer the time required for the target reactant and the carrier gas to be uniformly mixed in the spherical reaction chamber 2 to reach the stable concentration is. The volume ratio of the reaction zone to the transition zone 1 is greater than 10: 1; the residence time of the target reactant in the reaction zone with the carrier gas can be increased to a greater extent closer to the theoretical residence time.
The inner diameter of the straight tube reaction zone 4 is not less than that of the transition zone 1. Preferably, the straight tube reaction zone 4, the transition zone 1 and the pyrolysis gas delivery zone 3 have the same inner diameter. When the flow rate of the carrier gas is constant, the inner diameter of the straight pipe reaction zone 4 is not less than that of the transition zone 1, so that the retention time in the transition zone 1 can be reduced; the straight tube reaction zone 4 the transition zone 1 with the internal diameter of pyrolysis gas conveying zone 3 is unanimous, then can guarantee that most reactions take place in spherical reaction chamber 2, and the degree of mixing of carrier gas and reactant is far better than straight tube reaction zone 4 in spherical reaction chamber 2, can make the reaction process more accurate, is close to theoretical condition.
As shown in fig. 2, a pyrolysis reaction apparatus includes the tubular reaction module for pyrolysis reaction and a heating module 7 coated outside the tubular reaction module. Preferably, the heating assembly 7 at least covers the sample placement area 5, the transition area 1, the reaction area, the pyrolysis gas delivery area 3 and the adsorbing material placement area 5 of the tubular reaction assembly for pyrolysis reaction. The transition area 1 of the tubular reaction component for the pyrolysis reaction is also connected with an air inlet pipeline 8, and the pyrolysis gas conveying area 3 is also connected with a tail gas discharge pipeline 9. The operating principle of the pyrolysis reaction device is that the organic matter to be pyrolyzed volatilizes at high temperature, then flows along with the carrier gas the tubular reaction assembly for pyrolysis reaction, reaches the pyrolysis temperature when entering the reaction zone to take place most pyrolysis reaction in spherical reaction chamber 2, the pyrolysis product continues to flow along with the carrier gas and places the district 5 and be adsorbed by the adsorption material to the adsorption material, and the carrier that is not adsorbed then gets into exhaust emission pipeline 9. If the heating member 7 does not cover the tubular reaction member for pyrolysis reaction, non-uniform heating occurs, resulting in an increase in pyrolysis by-products.
As shown in FIG. 3, for the utility model provides a tubular heating furnace, including the above-mentioned tubular reaction subassembly that is used for pyrolytic reaction, and heating furnace body 10.
The utility model provides a pyrolysis method of pyrolysis device, including following step:
1) acquiring a temperature correction curve of a pyrolysis reaction device at a pyrolysis temperature;
2) placing organic matters to be pyrolyzed in the sample placing area, and placing an adsorbing material in the adsorbing material placing area;
3) the heating element 7 is activated and a carrier gas is introduced.
After the heating component 7 is started, the pyrolysis reaction device is close to the end parts of the carrier gas input and output, a temperature increasing or decreasing area is generated due to the external temperature difference, the temperature increasing area is a temperature increasing area along the flow direction of the carrier gas, and the temperature decreasing area is a temperature decreasing area; the temperature of the middle part of the pyrolysis device is constant, and is a set target temperature, namely a constant temperature area; the purpose of obtaining the temperature correction curve of the pyrolysis reaction device at the pyrolysis temperature is to determine a temperature increasing area, a constant temperature area and a temperature decreasing area of the pyrolysis reaction device. The reaction area of the tubular reaction assembly for the pyrolysis reaction is located in a constant temperature area, the transition area 1 and the sample placing area 5 are located in a temperature increasing area, and the pyrolysis gas conveying area 3 and the adsorbing material placing area 6 are located in a temperature decreasing area. The temperature correction curve of the pyrolysis reaction device can be adjusted by increasing the sealing degree of the end position of the pyrolysis reaction device close to the carrier gas input and output, so as to ensure the corresponding relation between the sample placing area 5 and the transition area 1, between the reaction area, between the pyrolysis gas conveying area 3 and the adsorbing material placing area 5 and between the temperature increasing area, the constant temperature area and the temperature decreasing area of the pyrolysis reaction device.
The temperature of the sample placing area 5 is 100-150 ℃; the temperature of the adsorbing material placing area 6 is 150-200 ℃. The volatilization rate of the organic matters to be pyrolyzed is 0.001-0.1 mol/min. The volatilization rate of the organic matters to be pyrolyzed can be changed along with the flow rate and the temperature of the carrier gas, the temperature of the sample placing area 5 is controlled to be 150-. When the temperature is too low, the organic matter to be pyrolyzed cannot volatilize, or the volatilization rate is too slow, at the moment, the volatilization rate cannot be controlled by only increasing the flow rate of the carrier gas, and the difficulty in fixing the organic matter to be pyrolyzed is increased by too high the flow rate of the carrier gas. Too high temperature, too fast volatilization, non-uniform mixing of carrier gas and reactants, influence the reaction accuracy. In addition, when the heating element 7 is started and the temperature rises to be stable, the organic matter to be pyrolyzed enters the reaction area along with the carrier gas at a relatively stable volatilization rate after the carrier gas is opened to perform pyrolysis reaction. If the organic matter to be pyrolyzed is directly placed in the reaction zone, in the process that the temperature of the heating assembly 7 is raised to be stable, even if the carrier gas is closed, the reactant undergoes the whole process that the temperature is increased from low to high, and because the temperature of the reaction zone is far higher than that of the transition zone 1, the reactant can be completely volatilized in a few seconds, the pyrolysis reaction is generated, and the corresponding generated product can also seriously influence the experimental result.
The organic matter to be pyrolyzed is one of polychlorinated biphenyl, polycyclic aromatic hydrocarbon and dioxin. The adsorption material is one of XAD-2, XAD-4, XAD-7, XAD-8 and active carbon. And fixing the organic matter to be pyrolyzed in the sample placing area by using quartz cotton. And (3) fixing an adsorbing material in the adsorbing material placing area by using quartz wool. The carrier gas is a mixed gas of air and inert gas.
Example 2
4-chlorobiphenyl (4-CB) as a target substance, a pyrolysis reaction was carried out by using the pyrolysis reaction apparatus of example 1, wherein the heating unit 7 was a tubular heating furnace body 10 having a furnace length of 50cm, an inner diameter D of the spherical reaction chamber 2 of 80mm, the same inner diameters D of the straight tube reaction zone 4 and the transition zone 1 of 5mm, and a reaction residence time t was setRThe pyrolysis temperature is 700 ℃ for 5s, the carrier gas is a mixed gas of air and nitrogen, and the oxygen concentration is 8%.
1) Acquiring a temperature correction curve of a pyrolysis reaction device, namely a heating furnace, at 700 ℃;
2) placing organic matters to be pyrolyzed in the sample placing area 5, and placing an adsorbing material in the adsorbing material placing area 6;
3) the heating element 7 is activated and a carrier gas is introduced.
The temperature of the sample placement area 5 is 140 ℃; the temperature of the adsorbing material placing area 6 is 200 ℃; the volatilization rate of the organic matters to be pyrolyzed is 0.001 mol/min; the adsorbing material is XAD-2. The quartz wool fixes the organic matter to be pyrolyzed in the sample placing area 5. The adsorbing material is fixed in the adsorbing material placing area 6 by quartz wool.
Fig. 4 is a temperature correction curve, and the temperature increasing region, the constant temperature region and the temperature decreasing region of the pyrolysis reaction device correspond to the sample placing region 5, the transition region 1, the reaction region, the pyrolysis gas conveying region 3 and the adsorbing material placing region 6 of the tubular reaction assembly for pyrolysis reaction. It can be seen that the length of the temperature increasing zone is 14cm, the transition zone 1 and the sample placement zone 5 are located in the temperature increasing zone, the length of the transition zone 1 is 8cm, and the volume of the transition zone 1 is 1570mm3(3.14＊2.5＊2.5＊80 ═ 1570); the length of the constant temperature area is 22cm, the length of the reaction area is consistent with that of the constant temperature area, the inner diameter of the spherical reaction cavity 2 is 8cm, and the total length of the straight tube reaction area 4 is 14cm, so that the volume of the reaction area is 270694.17mm3(4/3 x 3.14 x 40+3.14 x 2.5 x 140 x 270694.167); the reactant enters a pyrolysis gas conveying area 3 along with carrier gas after reacting in the reaction area; the pyrolysis gas conveying area 3 and the adsorbing material placing area 6 are positioned in a temperature decreasing area, and the length of the temperature decreasing area is 14 cm; wherein the pyrolysis gas transfer zone 3 located before the sorption material has a length of 12 cm. From the above data, it is calculated that the volume of the organic matter to be pyrolyzed is about 0.58% of the volume of the reaction zone in the transition zone 1 along with the carrier gas. That is, when the reaction residence time is set to 5s, the organic matter to be pyrolyzed stays only for less than 0.03s in the transition zone 1 along with the carrier gas and stays for 4.97s in the reaction zone.
Comparative example 1
4-chlorobiphenyl (4-CB) is used as a target substance, a tubular heating furnace is adopted for carrying out pyrolysis reaction, the furnace body 10 of the tubular heating furnace is consistent with that of the embodiment 2, and a pyrolysis reactor is a high-purity quartz straight pipe; the furnace length is 50cm, the inner diameter of the quartz straight pipe is 2.5mm, and the reaction residence time t is setRThe pyrolysis temperature is 700 ℃ for 5s, the carrier gas is a mixed gas of air and nitrogen, and the oxygen concentration is 8%.
1) Acquiring a temperature correction curve of the tubular heating furnace at the pyrolysis temperature;
2) placing the organic matter to be pyrolyzed at the left end of the tube furnace and fixing the organic matter by high-temperature-resistant high-purity quartz cotton;
3) the adsorbing material is arranged at the right end of the tube furnace and is fixed by high-temperature-resistant high-purity quartz cotton;
4) the heating system is started and carrier gas is introduced.
The volatilization rate of the organic matters to be pyrolyzed is 0.001 mol/min; the adsorbing material is XAD-2. Since the same heating element 7 was used as in example 2, both temperature correction curves were identical and are shown in FIG. 4. The lengths of the temperature increasing area, the constant temperature area and the temperature decreasing area are 14cm, 22cm and 14cm respectively. Because the pyrolysis reactor is a straight pipe, the residence time in the temperature increasing zone, the constant temperature zone and the temperature decreasing zone is 3.18s, 5s and 3.18s, respectively. The relative residence time in the constant temperature region is short, so that there may occur a problem that side reactions occur in the temperature increasing region and the temperature decreasing region, the reaction is incomplete in the constant temperature region,
since the temperature of the transition zones on the left and right sides is high, side reactions are completely likely to occur in the zones, and the reaction residence time on the left and right sides is t1+t25.42s, or even more than the reaction residence time t of the intermediate constant-temperature zoneR(5s), once side reactions occur on the left side and the right side, the generated products have great influence on the result of 4-CB pyrolysis at 700 ℃, and the judgment result of the product generated by 4-CB pyrolysis at the temperature is seriously influenced.
Experimental example 1
4-chlorobiphenyl was pyrolyzed according to the pyrolysis apparatus and the pyrolysis method of example 2 and comparative example 1, the variation of the pyrolysis product in the two pyrolysis apparatuses is shown in fig. 5, and in the case of the same heating assembly 7, it can be seen that the generation concentration of the pyrolysis product Naphthalene is higher in the straight tube reactor in the temperature range of 300-. The maximum value of the concentration of naphthalene in the straight-tube reactor is again 700 ℃ and in the tubular reaction module for pyrolysis reactions of the present invention is 675 ℃ to the maximum value. The analysis reason, 700 ℃ the time, the temperature range of straight tube reactor temperature increase district is just suitable for the temperature that the naphthalene generated, and therefore the naphthalene that generates in the temperature increase district is great to the total amount influence of naphthalene, consequently causes 700 ℃ the time, and the naphthalene in the straight tube reactor generates the concentration and is far higher than the utility model discloses a condition that generates the concentration in the tubular reaction subassembly for pyrolytic reaction.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications can be made without departing from the scope of the invention.
Claims (8)
1. A tubular reaction component for pyrolysis reaction is characterized by comprising a transition zone, a reaction zone and a pyrolysis gas conveying zone which are sequentially communicated along the flowing direction of carrier gas, wherein,
the reaction zone comprises a spherical reaction chamber and a straight tube reaction zone communicated with the two sides of the spherical reaction chamber, and the ratio of the inner diameter D of the spherical reaction chamber to the inner diameter D of the straight tube reaction zone is 8-20: 1;
the transition region and the pyrolysis gas conveying region are both of straight pipe structures and are respectively connected with the straight pipe reaction regions on two sides of the spherical reaction cavity;
the volume ratio of the reaction zone to the transition zone is greater than 10: 1;
one end of the transition area, which is close to the carrier gas input, is connected with a sample placing area, and one end of the pyrolysis gas conveying area, which is far away from the carrier gas input, is connected with an adsorbing material placing area.
2. The tubular reaction assembly for pyrolysis reaction of claim 1 wherein an inner diameter of the straight tube reaction zone is not less than an inner diameter of the transition zone.
3. The tubular reaction assembly for pyrolysis reactions of claim 1 wherein the straight tube reaction zone, the transition zone, and the pyrolysis gas delivery zone have uniform inside diameters.
4. A pyrolysis reaction apparatus comprising the tubular reaction module for pyrolysis reaction according to claim 1 or 2 and a heating module wrapped outside thereof.
5. The pyrolysis reaction device of claim 4, wherein the transition zone of the tubular reaction component for pyrolysis reaction is further connected with an air inlet pipeline, and the pyrolysis gas conveying zone is further connected with a tail gas discharge pipeline.
6. The pyrolytic reaction device according to claim 4, wherein the heating component covers at least the sample placement area, the transition area, the reaction area, the pyrolysis gas delivery area and the adsorbing material placement area of the tubular reaction component for pyrolytic reaction.
7. A pyrolytic reaction device in accordance with any one of claims 4-6 wherein the heating element is a tubular furnace.
8. A tubular heating furnace comprising the tubular reaction module for pyrolysis reaction of any one of claims 1 to 3 or comprising the pyrolysis reaction apparatus of any one of claims 4 to 6.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109647317A (en) * | 2018-12-10 | 2019-04-19 | 中国环境科学研究院 | A kind of pyrolytic reaction device and its method for pyrolysis |
| WO2022012612A1 (en) * | 2020-07-15 | 2022-01-20 | 上海博箭实业有限公司 | Improved electro-pyrolytic furnace |
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2018
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109647317A (en) * | 2018-12-10 | 2019-04-19 | 中国环境科学研究院 | A kind of pyrolytic reaction device and its method for pyrolysis |
| CN109647317B (en) * | 2018-12-10 | 2024-01-26 | 中国环境科学研究院 | Pyrolysis reaction device and pyrolysis method thereof |
| WO2022012612A1 (en) * | 2020-07-15 | 2022-01-20 | 上海博箭实业有限公司 | Improved electro-pyrolytic furnace |
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