CN107557040B - System and method for recovering heat of high-temperature pyrolysis gas - Google Patents
System and method for recovering heat of high-temperature pyrolysis gas Download PDFInfo
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- CN107557040B CN107557040B CN201710936270.7A CN201710936270A CN107557040B CN 107557040 B CN107557040 B CN 107557040B CN 201710936270 A CN201710936270 A CN 201710936270A CN 107557040 B CN107557040 B CN 107557040B
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Abstract
The invention provides a system and a method for recovering heat of high-temperature pyrolysis gas. The system comprises a fast pyrolysis furnace, an atomization chiller, a dust removing device, a fractional condensation type heat exchanger, a gas-liquid separator, an oil-water separator and an atomization booster pump. The atomization chiller is respectively connected with the fast pyrolysis furnace and the dust collector, the fractional condensation type heat exchanger is respectively connected with the dust collector and the gas-liquid separator, the oil-water separator is respectively connected with the gas-liquid separator and the atomization booster pump, and the atomization booster pump is also respectively connected with the atomization chiller and the fractional condensation type heat exchanger. The invention has high efficiency, energy conservation and environmental protection, can solve the problems of heat recovery operation stability and safety of pyrolysis gas, and can also reduce the cost of the pyrolysis gas purification system.
Description
Technical Field
The invention belongs to the technical field of coal chemical industry, and particularly relates to a system and a method for recovering heat of high-temperature pyrolysis gas.
Background
The coal pyrolysis upgrading technology can be classified into low-temperature (500-600 ℃) pyrolysis and medium-temperature (600-800 ℃) pyrolysis according to pyrolysis temperature; according to different heat supply mediums, the pyrolysis quality improvement technology can be divided into a gas phase heat carrier pyrolysis technology, a solid phase heat carrier pyrolysis technology and a special heat accumulating pyrolysis technology. In the pyrolysis process, the temperature of the gas outlet reaches 850 ℃ or even higher, and a small amount of tar, a large amount of dust and a large amount of heat are carried, so that higher difficulty is brought to subsequent gas purification and tar recovery. The heat of a large amount of high-temperature gas is recovered, so that on one hand, the difficulty of gas dust removal is reduced, and on the other hand, the economic benefit of the system is improved; therefore, reasonable and efficient utilization is a key in the implementation process.
At present, two methods are mainly used for cooling high-temperature coal gas, namely, a gasification coal gas chilling process is similar, and water is directly sprayed to the high-temperature coal gas for cooling; and secondly, the gas is subjected to heat exchange through a waste heat boiler to produce steam.
Wherein, the representative of the gas chilling process is Texaco gasified gas chilling technology; the gas cooling process is mainly performed in a chilling chamber. The chilling chamber mainly comprises a chilling ring, a down pipe and a rising pipe. The quench water is injected into the quench chamber through small holes in the quench ring distribution chamber. The chilled water flows out through the lower annular slot of the chilled ring chamber, forms a uniform liquid film on the inner surface of the downcomer, and is contacted with the high-temperature gasified coal gas in parallel flow, so that the heat mass is generated, and the coal gas is cooled in the process of transferring. The technology has the defects of energy saving and energy waste, no recovery of heat in the coal gas, and serious environmental pollution caused by the fact that the washing water and the coal gas are in direct contact to generate washing sewage and difficult to treat. And the pyrolysis temperature of lignite is lower than the gasification temperature, so that the quantity of tar carried in the coal gas is higher than that of the lignite by the gasification technology, the subsequent oil-water-dust separation difficulty is higher, the problem of blockage is more likely to occur, and the operation period of the system is influenced.
The other method is to add a waste heat boiler on a gas outlet pipeline to indirectly exchange heat with raw gas in a heat exchanger, and flash evaporation of heated water in a steam drum produces low-pressure saturated steam, so that sensible heat of the raw gas can be recovered to 35%, but under the influence of tar and dust in the gas, the problem of rapid reduction of heat exchange efficiency exists, and the operation safety of a subsequent system is reduced.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a high-efficiency, energy-saving and environment-friendly technology for recovering the heat of high-temperature pyrolysis gas, which can solve the problems of stability and safety in the recovery operation of the heat of the high-temperature pyrolysis gas and can also reduce the cost of a high-temperature pyrolysis gas purification system.
The invention provides a system for recovering heat of high-temperature pyrolysis gas, which comprises:
the rapid pyrolysis furnace is provided with a pyrolysis material inlet, a pyrolysis gas outlet and a semicoke outlet;
the atomization chiller is provided with a high-temperature pyrolysis gas inlet, a chilled water inlet and a pyrolysis gas outlet, and the high-temperature pyrolysis gas inlet is connected with the high-temperature pyrolysis gas outlet of the rapid pyrolysis furnace; along the direction of gas flow, the atomization chiller is sequentially provided with an activation reaction zone, a chilling dust suppression zone and a chilling temperature control zone, the activation reaction zone, the chilling dust suppression zone and the chilling temperature control zone are provided with spray heads, and the chilling water inlet is arranged on the spray heads;
the dust removing device is provided with a pyrolysis gas inlet, a dust removing gas outlet and a dust outlet, and the pyrolysis gas inlet is connected with the pyrolysis gas outlet of the atomization chiller;
the fractional condensation type heat exchanger is provided with a dedusting gas inlet, a soft water inlet, a flushing water inlet, a gas-liquid mixture outlet, a steam outlet and a sewage outlet, wherein the dedusting gas inlet is connected with a dedusting gas outlet of the dedusting device; the fractional condensation type heat exchanger is sequentially provided with a high temperature section, a medium temperature section and a low temperature section along the gas flowing direction, wherein the high temperature section, the medium temperature section and the low temperature section are respectively provided with a gas inlet and a gas outlet, and the soft water inlet is arranged on the low temperature section;
the gas-liquid separator is provided with a gas-liquid mixture inlet, an oil-water mixture outlet and a gas outlet, and the gas-liquid mixture inlet is connected with the gas-liquid mixture outlet of the fractional condensation heat exchanger;
the oil-water separator is provided with an oil-water mixture inlet, a tar outlet and a condensed water outlet, and the oil-water mixture inlet is connected with the oil-water mixture outlet of the gas-liquid separator;
the atomization booster pump is provided with a condensate inlet and a pressurized water outlet, the condensate inlet is connected with the condensate outlet of the oil-water separator, and the pressurized water outlet is respectively connected with the chilling water inlet of the atomization chiller and the flushing water inlet of the fractional condensation heat exchanger.
In some embodiments of the invention, the spray heads of the activation reaction zone are annularly arranged around the conduit.
In some embodiments of the invention, the spray heads of the chilled dust suppression zone are arranged in the range of 110-130 degrees at the upper part of the pipeline, and 3-5 groups are arranged.
In some embodiments of the invention, the spray head of the chilled temperature controlled zone is disposed inside a pipe.
In some embodiments of the invention, the system further comprises a refrigeration device and a cryogenic device;
the refrigerating device is provided with a steam inlet and a refrigerating water outlet, and the steam inlet is connected with the steam inlet of the fractional condensation heat exchanger;
the cryogenic device is provided with a refrigeration water inlet, a gas inlet and a low-temperature gas outlet, the refrigeration water inlet is connected with the refrigeration water outlet of the refrigeration device, and the gas inlet is connected with the gas outlet of the gas-liquid separator.
The method for recycling the heat of the high-temperature pyrolysis gas by utilizing the system provided by the invention comprises the following steps:
the pyrolysis material is sent into the fast pyrolysis furnace for pyrolysis, and high-temperature pyrolysis gas and semicoke are obtained;
sending the pyrolysis gas into the atomization chiller for cooling to obtain pyrolysis gas with the temperature of 250-550 ℃;
feeding the pyrolysis gas into the dust removing device to remove dust, so as to obtain dust removing gas;
feeding the dedusting gas into the fractional condensation type heat exchanger to exchange heat with soft water, condensing water vapor and tar in the dedusting gas, and heating the soft water to obtain a gas-liquid mixture and vapor;
sending the gas-liquid mixture into the gas-liquid separator for separation to obtain an oil-water mixture and coal gas;
sending the oil-water mixture into the oil-water separator for separation to obtain oil and condensed water;
and after being pressurized by the atomization booster pump, the condensed water is respectively sent into the atomization chiller as chilling water and is sent into the fractional condensation heat exchanger as flushing water.
In some embodiments of the invention, the steam is used as a heat source for supplying heat, and the obtained refrigeration water is used for further reducing the temperature of the coal gas.
In some embodiments of the invention, the temperature of the activation reaction zone of the atomizing chiller is controlled from 750 ℃ to 830 ℃.
In some embodiments of the invention, the amount of chilled water injected into the activation reaction zone of the atomization chiller is 1/5-1/4 of the total chilled water amount, the amount of chilled water injected into the chilled dust suppression zone is 1/2-3/5 of the total chilled water amount, and the amount of chilled water injected into the chilled temperature control zone is 1/5-1/4 of the total chilled water amount.
In some embodiments of the invention, the temperature of the gas inlet of the temperature section in the fractional condensation heat exchanger is 320 ℃ to 360 ℃ and the temperature of the gas inlet of the low temperature section is 120 ℃ to 180 ℃.
The invention avoids the potential safety hazard of post system overtemperature caused by the influence of dust tar and the like possibly caused by the conventional heat recovery technology, thereby solving the problem of stability and safety of heat recovery operation of pyrolysis gas.
The invention recovers sensible heat and latent heat, has high heat utilization efficiency and small water circulation, only needs to supplement part of chilling water in the initial stage, and generates water by pyrolysis in the normal operation process, thereby having high efficiency, energy conservation and environmental protection.
In addition, the volume of the increase of the steam quantity generated by the water sprayed by the atomization chiller is lower than the reduction of the working condition volume caused by the reduction of the temperature, so that the treatment capacity of the dust removing equipment can be reduced, and the material selection grade of the dust removing equipment is reduced due to the reduction of the temperature, so that the running cost of the system is low.
Additional aspects and advantages of the invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention.
Drawings
Fig. 1 is a schematic structural diagram of a system for recovering heat of pyrolysis gas according to an embodiment of the present invention.
FIG. 2 is a schematic illustration of an atomizing quench in accordance with an embodiment of the present disclosure; wherein A is a schematic diagram of the whole structure, B is a schematic diagram of the longitudinal section of the activation reaction zone a, C is a schematic diagram of the longitudinal section of the chilling dust suppression zone B, and D is a schematic diagram of the longitudinal section of the chilling temperature control zone C.
Fig. 3 is a schematic structural diagram of a heat recovery device according to an embodiment of the present invention.
FIG. 4 is a process flow diagram of recovering heat from a pyrolysis gas according to one embodiment of the present invention.
Detailed Description
The following detailed description of specific embodiments of the invention is provided in connection with the accompanying drawings and examples in order to provide a better understanding of the aspects of the invention and advantages thereof. However, the following description of specific embodiments and examples is for illustrative purposes only and is not intended to be limiting of the invention.
It should be noted that the directions or positional relationships indicated by the terms "upper", "lower", "left", "right" and the like in the present invention are directions or positional relationships based on those shown in the drawings, and are merely for convenience of description of the present invention, and do not require that the present invention must be constructed and operated in a specific direction, and thus should not be construed as limiting the present invention.
Fig. 1 shows a system for recovering heat of high-temperature pyrolysis gas, which is a system for recovering heat of high-temperature pyrolysis gas and comprises a feed storage bin 1, a fast pyrolysis furnace 2, an atomization chiller 3, a dust removal device 4, a fractional condensation heat exchanger 5, a gas-liquid separator 6, an oil-water separator 7, an atomization booster pump 8, a refrigeration device 9 and a deep cooling device 10.
The feed bin 1 is provided with a raw material inlet 101, a raw material outlet 102.
The fast pyrolysis furnace 2 is provided with a pyrolysis material inlet 201, a pyrolysis gas outlet 202 and a semicoke outlet 203, wherein the pyrolysis material inlet 201 is connected with the raw material outlet 102 of the feeding bin 1.
The atomizing chiller 3 is provided with a pyrolysis gas inlet 301, a chilled water inlet 302, and a pyrolysis gas outlet 303, the pyrolysis gas inlet 301 being connected to the pyrolysis gas outlet 202 of the fast pyrolysis furnace 2.
The dust removing device 4 is provided with a pyrolysis gas inlet 401, a dust removing gas outlet 402 and a dust outlet 403, and the pyrolysis gas inlet 401 is connected with the pyrolysis gas outlet 303 of the atomizing chiller 3.
The fractional condensation heat exchanger 5 is provided with a dedusting gas inlet 501, a soft water inlet 502, a flushing water inlet 503, a steam outlet 504 and a gas-liquid mixture outlet 505, the dedusting gas inlet 501 being connected to the dedusting gas outlet 402 of the dedusting apparatus 4.
The gas-liquid separator 6 is provided with a gas-liquid mixture inlet 601, an oil-water mixture outlet 602 and a gas outlet 603, and the gas-liquid mixture inlet 601 is connected with the gas-liquid mixture outlet 505 of the fractional condensation heat exchanger 5.
The oil-water separator 7 is provided with an oil-water mixture inlet 701, a tar outlet 702 and a condensate outlet 703, and the oil-water mixture inlet 701 is connected with the oil-water mixture outlet 602 of the gas-liquid separator 6.
The atomizing booster pump 8 is provided with a condensate inlet 801 and a pressurized water outlet 802, the condensate inlet 801 is connected with the condensate outlet 703 of the oil-water separator 7, and the pressurized water outlet 802 is connected with the chilled water inlet 302 of the atomizing chiller 3 and the rinse water inlet 503 of the fractional condensation heat exchanger 5, respectively.
The refrigerating device 9 is provided with a steam inlet 901 and a refrigerating water outlet 902, the steam inlet 901 being connected to the steam outlet 504 of the fractional condensation heat exchanger 5.
The cryogenic device 10 is provided with a chilled water inlet 1001, a gas inlet 1002 and a low temperature gas outlet 1003, the chilled water inlet 1001 being connected to the chilled water outlet 902 of the chiller 9, the gas inlet 1002 being connected to the gas outlet 603 of the gas-liquid separator 6.
It should be noted that the feed bin 1, the refrigerating device 9 and the cryogenic device 10 are not necessary for achieving the object of the present invention, and may be increased or decreased according to actual needs.
The atomizing chiller 3 and the fractional condensation heat exchanger 5 are core devices of the present invention, the structures of which are shown in fig. 2 and 3, and other devices of the present invention are common devices in the art, and the structures thereof are not described herein.
As shown in fig. 2A, along the direction of the gas flow (i.e. the direction of the transverse arrow in the figure, 305 in fig. 2A is the main gas pipeline), the atomization chiller 3 is sequentially provided with an activation reaction zone a, a chilling dust suppression zone b and a chilling temperature control zone c, the activation reaction zone a, the chilling dust suppression zone b and the chilling temperature control zone c are provided with spray heads 304, and a chilling water inlet 302 is arranged on the spray heads 304.
In order to disrupt the flow field of the gas stream in the tube by the injected chilled water, which increases the heat transfer effect and rapidly gasifies, in the preferred embodiment of the present invention, the injected chilled water is perpendicular to the direction of gas flow, i.e., the spray heads 304 of the activation reaction zone a are annularly arranged around the tube as shown in FIG. 2B (the arrows in the figure indicate the direction of chilled water injection).
The sprayed quenching water is pressurized water, the pressurized water is changed into water mist after being sprayed by the spray head 304, the partial pressure of water vapor in pyrolysis gas is increased, the activity of dust carried in the pyrolysis gas is higher, a certain degree of water gas reaction can be carried out, carbon of the dust can be further converted into the pyrolysis gas, and the content of effective gas is increased.
The chilling dust suppression zone b is mainly used for cooling the pyrolysis gas, and in the preferred embodiment of the invention, the spray heads 304 of the chilling dust suppression zone b are arranged in the range of 110-130 degrees at the upper part of the pipeline, and 3-5 groups are arranged. At this time, the injected chilled water is concentrated at the upper half part of the pipeline (as shown in fig. 2C, the arrow in the drawing shows the direction of injecting the chilled water), and part of dust is settled under the action of self gravity along with the change of the volume flow of gas in the cooling process, so that a certain dust suppression effect is achieved.
The chilling temperature control zone c is mainly used for controlling the temperature of the output pyrolysis gas and ensuring the safe and stable use of the follow-up dust removing equipment. In the preferred embodiment of the present invention, the spray head 304 of the quench temperature zone c is disposed within the tube and sprays in the direction of the gas flow (as shown in FIG. 2D, the arrows in the figure indicate the direction of chilled water spray).
The volume of the increase of the steam quantity generated by spraying water into the atomization chiller is lower than the reduction of the working condition volume caused by the reduction of the temperature, so that the treatment capacity of the dust removing equipment can be reduced, and the material selection grade of the dust removing equipment is reduced due to the reduction of the temperature, so that the operation cost of the system is low.
Through the addition of circulation chilling water, chilling cooling is carried out in stages, on one hand, part of pyrolysis gas heat is used for water gas reaction heat absorption of dust, on the other hand, part of raw gas heat is used for a small amount of methane conversion reaction heat absorption, and most of pyrolysis gas sensible heat is absorbed through steam latent heat, so that the water content in the pyrolysis gas is increased, and the oil-water ratio in condensate in the heat recovery process is reduced.
The fractional condensation heat exchanger 5 is a heat recovery device, as shown in fig. 3, and the fractional condensation heat exchanger 5 is provided with a high temperature section d, a medium temperature section e and a low temperature section f in this order along the direction of gas flow (from top to bottom, not shown in the drawing), the high temperature section d, the medium temperature section e and the low temperature section f are respectively provided with a gas inlet and a gas outlet (not shown in the drawing), and the soft water inlet 502 is provided on the low temperature section f. The dust removing gas inlet 501 and the steam outlet 504 are provided above the high temperature section d, and the washing water inlet 503 and the gas-liquid mixture outlet 505 are provided below the low temperature section f, wherein the gas-liquid mixture outlet 505 is provided at the bottommost end of the fractional condensation heat exchanger 5.
Has a certain CH in the pyrolysis gas 4 The content of the catalyst is high, a large amount of dust is carried, and through the washing water sprayed in a grading way, certain methane steam conversion reaction and water gas reaction can occur in a high-temperature section d, so that the effective component H in pyrolysis gas is improved 2 The CO content while also consuming part of the pyrolysis water that has been produced. By adding a certain amount of flushing water, the partial pressure of tar steam in pyrolysis gas is reduced, which is beneficial to reducing secondary reaction of tar.
As shown in fig. 4, the method for recovering heat of high-temperature pyrolysis gas provided by the invention comprises the following steps:
and (3) delivering the pyrolysis material into a fast pyrolysis furnace 2 for pyrolysis to obtain high-temperature pyrolysis gas and semicoke. The carbocoal was collected and used for other purposes.
And sending the pyrolysis gas into an atomization chiller 3 for cooling to obtain the pyrolysis gas with the temperature of 250-550 ℃.
The pyrolysis gas is sent into a dust removing device 4 to remove dust, and dust removing gas is obtained.
The dedusting gas is sent into a fractional condensation type heat exchanger 5 to exchange heat with soft water, water vapor and tar in the dedusting gas are condensed, and the soft water is heated to obtain a gas-liquid mixture and vapor.
The gas-liquid mixture is sent into a gas-liquid separator 6 for separation, and an oil-water mixture and coal gas are obtained.
The oil-water mixture is sent into an oil-water separator 7 for separation, and tar and condensed water are obtained. The tar obtained is used as a product to enter a post-processing section, and the specific process is not described in detail here.
After being pressurized by an atomization booster pump 8, the condensed water is respectively sent into an atomization chiller 3 as chilled water and into a fractional condensation heat exchanger 5 as flushing water. If the residual water is left, the residual water is sent to a sewage treatment unit for treatment, and the specific process is not repeated here.
As described above, in the case where the refrigerating apparatus 9 and the refrigerating apparatus 10 are provided, heat can be supplied by using steam as a heat source, and the obtained refrigerating water can be used to further lower the temperature of the gas. Of course, it can be used as other heat sources.
In the preferred embodiment of the invention, the temperature of the activation reaction zone a of the atomization chiller 3 is controlled at 750-830 ℃, which is favorable for the rapid gasification of the sprayed chilled water, thereby improving the partial pressure of water vapor in the pyrolysis gas and generating a certain degree of water gas reaction.
In order to ensure the use of the subsequent dust removing device 4, the temperature of the pyrolysis gas at the outlet of the chilling temperature control zone c of the atomizing chiller 3 is preferably controlled to be 250-350 ℃ or 460-550 ℃.
In the preferred embodiment of the invention, the quenching water quantity sprayed by the activation reaction zone a of the atomization chiller 3 is 1/5-1/4 of the total quenching water quantity, the quenching water quantity sprayed by the quenching dust suppression zone b is 1/2-3/5 of the total quenching water quantity, and the quenching water quantity sprayed by the quenching temperature control zone c is 1/5-1/4 of the total quenching water quantity. The temperature of pyrolysis gas in different areas is controlled by controlling the injection amount of the quenching water so as to achieve corresponding effects.
In a preferred embodiment of the invention, the gas inlet temperature of the intermediate temperature section e of the fractional condensation heat exchanger 5 is 320 ℃ to 360 ℃ and the gas inlet temperature of the low temperature section f is 120 ℃ to 180 ℃. In the low-temperature section f, the pyrolysis gas exchanges heat with reverse soft water, a large amount of water vapor is condensed, and meanwhile, tar condensed in the medium-temperature section e is flushed by matching with flushing water and mixed to flow to a discharge port. The pyrolysis gas in the medium temperature section e exchanges heat with the steam-water mixture at 100-150 ℃ generated in the low temperature section f, the temperature is reduced to be below the dew point of tar, but because the temperature of each medium is higher, the mobility of the tar is better, and the tar easily flows into the lower section along the pipe wall due to the adoption of the downstream direction of the heat exchange pipe. The high temperature section d generates steam to further overheat the middle temperature section e in a radiation heat transfer mode.
The invention will now be described with reference to specific examples. The values of the process conditions taken in the examples below are exemplary and can be obtained in the ranges indicated in the foregoing summary, and for process parameters not specifically identified, reference may be made to conventional techniques. The detection methods used in the examples below are all conventional in the industry.
Example 1
This embodiment uses the system shown in fig. 1 to recover the heat of the pyrolysis gas. Wherein, the spray heads 304 of the activation reaction zone a are annularly arranged around the pipeline, the spray heads 304 of the chilling dust suppression zone b are arranged in the range of 110 DEG at the upper part of the pipeline, 3 groups of spray heads 304 of the chilling temperature control zone c are arranged inside the pipeline.
The pulverized coal enters the fast pyrolysis furnace 2 from the feeding storage bin 1 to be pyrolyzed in a downlink pyrolysis mode, and the grain size of the raw materials is smaller than 6mm. The temperature of pyrolysis gas generated after pyrolysis in the fast pyrolysis furnace 2 is 850 ℃, the dust content is 50-150g/Nm < 3 >, and the tar content is 20-50g/Nm < 3 >.
And sending the pyrolysis gas into an atomization chiller 3 for cooling to obtain the pyrolysis gas with the temperature of 480-550 ℃. The temperature of the activation reaction zone a of the atomization chiller 3 is controlled between 750 ℃ and 830 ℃. The quenching water quantity sprayed by the activation reaction zone a is 1/5 of the total quenching water quantity, the quenching water quantity sprayed by the quenching dust suppression zone b is 3/5 of the total quenching water quantity, and the quenching water quantity sprayed by the quenching temperature control zone c is 1/5 of the total quenching water quantity.
The pyrolysis gas is sent into a dust removing device 4 to remove dust, and dust removing gas is obtained. Dust content of the dedusting gas is less than 50mg/Nm 3 。
The dedusting gas is sent into a fractional condensation type heat exchanger 5 to exchange heat with soft water, water vapor and tar in the dedusting gas are condensed, and the soft water is heated to obtain a gas-liquid mixture and vapor. The gas inlet temperature of the middle temperature section e is 320-360 ℃, and the gas inlet temperature of the low temperature section f is 120-180 ℃. The pressure of the generated steam is 3.8Mpa and the temperature is 450 ℃; the temperature of the gas-liquid mixture is 70-82 ℃.
The gas-liquid mixture is sent into a gas-liquid separator 6 for separation, and an oil-water mixture and coal gas are obtained.
The oil-water mixture is sent into an oil-water separator 7 for separation, and tar and condensed water are obtained.
After being pressurized by the atomizing booster pump 8, the condensed water is respectively sent into an atomizing chiller as chilling water and into a fractional condensation heat exchanger as flushing water.
Example 2
This embodiment uses the system shown in fig. 1 to recover the heat of the pyrolysis gas. Wherein, the spray heads 304 of the activation reaction zone a are annularly arranged around the pipeline, the spray heads 304 of the chilling dust suppression zone b are arranged within the range of 130 DEG at the upper part of the pipeline, 5 groups of spray heads 304 of the chilling temperature control zone c are arranged inside the pipeline.
The pulverized coal enters the fast pyrolysis furnace 2 from the feeding storage bin 1 to be pyrolyzed in a downlink pyrolysis mode, and the grain size of the raw materials is smaller than 3mm. The temperature of pyrolysis gas generated after pyrolysis in the fast pyrolysis furnace 2 is 900 ℃, the dust content is 100-180g/Nm < 3 >, and the tar content is 1-5g/Nm < 3 >.
And sending the pyrolysis gas into an atomization chiller 3 for cooling to obtain the pyrolysis gas with the temperature of 280-350 ℃. The temperature of the activation reaction zone a of the atomization chiller 3 is controlled between 750 ℃ and 830 ℃. The quenching water quantity sprayed by the activation reaction zone a is 1/4 of the total quenching water quantity, the quenching water quantity sprayed by the quenching dust suppression zone b is 1/2 of the total quenching water quantity, and the quenching water quantity sprayed by the quenching temperature control zone c is 1/4 of the total quenching water quantity.
The pyrolysis gas is sent into a dust removing device 4 to remove dust, and dust removing gas is obtained. Dust content of the dedusting gas is less than 50mg/Nm 3 。
The dedusting gas is sent into a fractional condensation type heat exchanger 5 to exchange heat with soft water, water vapor and tar in the dedusting gas are condensed, and the soft water is heated to obtain a gas-liquid mixture and vapor. The gas inlet temperature of the middle temperature section e is 320-360 ℃, and the gas inlet temperature of the low temperature section f is 120-180 ℃. The pressure of the generated steam is 1.6Mpa, and the temperature is 201 ℃; the temperature of the gas-liquid mixture is 60-70 ℃.
The gas-liquid mixture is sent into a gas-liquid separator 6 for separation, and an oil-water mixture and coal gas are obtained.
The oil-water mixture is sent into an oil-water separator 7 for separation, and tar and condensed water are obtained.
After being pressurized by the atomizing booster pump 8, the condensed water is respectively sent into an atomizing chiller as chilling water and into a fractional condensation heat exchanger as flushing water.
The steam is fed as a heat source into the refrigerating device 9 for heating, and the obtained refrigerating water is fed into the cryogenic device 10 for further lowering the temperature of the gas.
According to the embodiment, the potential safety hazard of post-system overtemperature caused by the influence of dust tar and the like possibly caused by the conventional heat recovery technology is avoided, so that the stability and the safety of the heat recovery operation of the pyrolysis gas can be solved.
The invention recovers sensible heat and latent heat, has high heat utilization efficiency and small water circulation, only needs to supplement part of chilling water in the initial stage, and generates water by pyrolysis in the normal operation process, thereby having high efficiency, energy conservation and environmental protection.
It is apparent that the above examples are only illustrative of the present invention and are not limiting of the embodiments. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present invention.
Claims (10)
1. A system for recovering heat from a high temperature pyrolysis gas, comprising:
the rapid pyrolysis furnace is provided with a pyrolysis material inlet, a pyrolysis gas outlet and a semicoke outlet;
the atomization chiller is provided with a high-temperature pyrolysis gas inlet, a chilled water inlet and a pyrolysis gas outlet, and the high-temperature pyrolysis gas inlet is connected with the high-temperature pyrolysis gas outlet of the rapid pyrolysis furnace; along the direction of gas flow, the atomization chiller is sequentially provided with an activation reaction zone, a chilling dust suppression zone and a chilling temperature control zone, the activation reaction zone, the chilling dust suppression zone and the chilling temperature control zone are provided with spray heads, and the chilling water inlet is arranged on the spray heads;
the dust removing device is provided with a pyrolysis gas inlet, a dust removing gas outlet and a dust outlet, and the pyrolysis gas inlet is connected with the pyrolysis gas outlet of the atomization chiller;
the fractional condensation type heat exchanger is provided with a dedusting gas inlet, a soft water inlet, a flushing water inlet, a gas-liquid mixture outlet, a steam outlet and a sewage outlet, wherein the dedusting gas inlet is connected with a dedusting gas outlet of the dedusting device; the fractional condensation type heat exchanger is sequentially provided with a high temperature section, a medium temperature section and a low temperature section along the gas flowing direction, wherein the high temperature section, the medium temperature section and the low temperature section are respectively provided with a gas inlet and a gas outlet, and the soft water inlet is arranged on the low temperature section;
the gas-liquid separator is provided with a gas-liquid mixture inlet, an oil-water mixture outlet and a gas outlet, and the gas-liquid mixture inlet is connected with the gas-liquid mixture outlet of the fractional condensation heat exchanger;
the oil-water separator is provided with an oil-water mixture inlet, a tar outlet and a condensed water outlet, and the oil-water mixture inlet is connected with the oil-water mixture outlet of the gas-liquid separator;
the atomization booster pump is provided with a condensate inlet and a pressurized water outlet, the condensate inlet is connected with the condensate outlet of the oil-water separator, and the pressurized water outlet is respectively connected with the chilling water inlet of the atomization chiller and the flushing water inlet of the fractional condensation heat exchanger.
2. The system of claim 1, wherein the spray heads of the activation reaction zone are annularly disposed about the conduit.
3. The system of claim 1, wherein the spray heads of the chilled dust suppression zone are arranged in the range of 110 ° -130 ° above the pipe, with 3-5 groups being arranged.
4. The system of claim 1, wherein the spray head of the quench temperature zone is disposed inside a pipe.
5. The system of claim 1, further comprising a refrigeration device and a cryogenic device;
the refrigerating device is provided with a steam inlet and a refrigerating water outlet, and the steam inlet is connected with the steam inlet of the fractional condensation heat exchanger;
the cryogenic device is provided with a refrigeration water inlet, a gas inlet and a low-temperature gas outlet, the refrigeration water inlet is connected with the refrigeration water outlet of the refrigeration device, and the gas inlet is connected with the gas outlet of the gas-liquid separator.
6. A method of recovering heat from pyrolysis gas using the system of any one of claims 1-5, comprising the steps of:
the pyrolysis material is sent into the fast pyrolysis furnace for pyrolysis, and high-temperature pyrolysis gas and semicoke are obtained;
sending the pyrolysis gas into the atomization chiller for cooling to obtain pyrolysis gas with the temperature of 250-550 ℃;
feeding the pyrolysis gas into the dust removing device to remove dust, so as to obtain dust removing gas;
feeding the dedusting gas into the fractional condensation type heat exchanger to exchange heat with soft water, condensing water vapor and tar in the dedusting gas, and heating the soft water to obtain a gas-liquid mixture and vapor;
sending the gas-liquid mixture into the gas-liquid separator for separation to obtain an oil-water mixture and coal gas;
sending the oil-water mixture into the oil-water separator for separation to obtain tar and condensed water;
and after being pressurized by the atomization booster pump, the condensed water is respectively sent into the atomization chiller as chilling water and is sent into the fractional condensation heat exchanger as flushing water.
7. The method according to claim 6, wherein the steam is used as a heat source for supplying heat, and the obtained chilled water is used for further lowering the temperature of the gas.
8. The method of claim 6, wherein the temperature of the activation reaction zone of the atomizing chiller is controlled between 750 ℃ and 830 ℃.
9. The method according to claim 6, wherein the amount of the chilled water injected into the activation reaction zone of the atomization chiller is 1/5-1/4 of the total chilled water amount, the amount of the chilled water injected into the chilled dust suppression zone is 1/2-3/5 of the total chilled water amount, and the amount of the chilled water injected into the chilled temperature control zone is 1/5-1/4 of the total chilled water amount.
10. The method of claim 6, wherein the temperature of the gas inlet of the warm section of the fractional condensation heat exchanger is 320 ℃ to 360 ℃ and the temperature of the gas inlet of the low temperature section is 120 ℃ to 180 ℃.
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