CN211311372U - Device for doing work by utilizing waste heat of coke oven crude gas - Google Patents
Device for doing work by utilizing waste heat of coke oven crude gas Download PDFInfo
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- CN211311372U CN211311372U CN201922008708.2U CN201922008708U CN211311372U CN 211311372 U CN211311372 U CN 211311372U CN 201922008708 U CN201922008708 U CN 201922008708U CN 211311372 U CN211311372 U CN 211311372U
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- 239000000571 coke Substances 0.000 title claims abstract description 40
- 239000007789 gas Substances 0.000 title claims abstract description 40
- 239000002918 waste heat Substances 0.000 title claims abstract description 21
- 230000001174 ascending effect Effects 0.000 claims abstract description 78
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 60
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 58
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 29
- 238000004821 distillation Methods 0.000 claims abstract description 17
- 239000000203 mixture Substances 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims description 31
- 238000010438 heat treatment Methods 0.000 claims description 26
- 238000000034 method Methods 0.000 claims description 21
- 230000008569 process Effects 0.000 claims description 14
- 238000001704 evaporation Methods 0.000 claims description 12
- 230000008020 evaporation Effects 0.000 claims description 12
- 238000012824 chemical production Methods 0.000 claims description 10
- 230000000630 rising effect Effects 0.000 claims description 9
- 239000003245 coal Substances 0.000 claims description 7
- 229920006395 saturated elastomer Polymers 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000002912 waste gas Substances 0.000 abstract description 2
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 53
- 239000002609 medium Substances 0.000 description 25
- 230000006872 improvement Effects 0.000 description 13
- 238000005406 washing Methods 0.000 description 11
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 7
- 235000011114 ammonium hydroxide Nutrition 0.000 description 7
- 239000003034 coal gas Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000005086 pumping Methods 0.000 description 4
- 239000012736 aqueous medium Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000009413 insulation Methods 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000001133 acceleration Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000009841 combustion method Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
Abstract
The utility model provides a device for applying work by utilizing waste heat of coke oven crude gas, which comprises a riser heat exchanger, a heat exchange device and a circulating pump, wherein the riser heat exchanger, the heat exchange device and the circulating pump are respectively and independently arranged on the top of the coke oven and are connected into a ring to form a heat exchange cycle, and water, heat conduction oil or other heat mediums are adopted as heat exchange mediums in the heat exchange cycle; the heat exchange medium is driven by the circulating pump to absorb heat through the ascending pipe heat exchanger to become a steam-water mixture or a high-temperature heat medium, then the steam-water mixture or the high-temperature heat medium passes through the heat exchange device to be cooled, and then the steam-water mixture or the high-temperature heat medium enters the circulating pump again to complete a cycle. The device replaces a debenzolization tubular furnace and an ammonia distillation tubular furnace which burn coke oven gas in the conventional production process, improves the thermal efficiency of a coke oven production process system, and reduces the emission point of waste gas pollution.
Description
Technical Field
The utility model belongs to the technical field of boiler equipment, in particular to adopt and utilize coke oven crude gas waste heat acting device.
Background
The coke oven can perform high-temperature dry distillation treatment on coal, and efficiently convert the coal into products such as coke, coke oven gas, coal tar, crude benzene and the like, thereby being an efficient energy conversion kiln. In the coke oven waste heat, the heat brought out by the crude gas at 650-700 ℃ accounts for about 36%, and the method has extremely high recycling value. The produced raw gas contains benzene, tar and other substances, and a series of treatment links are carried out after the temperature is reduced, so that the industrial application can be realized, wherein one link is benzene removal. The common process is as follows: after being finally cooled to about 25 ℃, the raw gas firstly enters the bottom of the first benzene washing tower, is led out from the top of the tower and then sequentially passes through the benzene washing towers. The benzene content of the gas from the top of the last benzene washing tower is required to be lower than 2g/Nm3. The lean oil from the lean oil tank is sprayed from the top of the last benzene washing tower and closely contacts with the coal gas in a reverse direction to absorb the benzene in the coal gas. And (3) leading out the rich oil containing about 2.5 percent of benzene from the bottom of the first benzene washing tower, pumping the rich oil to a benzene removal process by using a rich oil pump, and feeding the benzene-removed lean oil back to a lean oil tank for recycling. The lean oil becomes rich after absorbing the benzene.
The bottom of each benzene washing tower is provided with a washing oil receiving groove which is separated from the coal gas by a steel plate. The washing oil from the top of the tower flows into the tank through the U-shaped pipe, and the oil level in the tank is kept stable. The mist catching layer is arranged on the spray head of the last benzene washing tower to catch oil drops carried by the coal gas, so that the loss of washing oil is reduced, and the washing oil is prevented from entering the coal gas. When the recovered crude gas heat in the ascending pipe is used for heating lean oil and rich oil, but in the traditional chemical production process, a tubular furnace is usually adopted for burning coke oven gas, wherein the exhaust gas temperature is as high as 350 ℃, and the thermal efficiency is about 60 percent. Therefore, how to reduce the exhaust gas pollution emission in the chemical production process more possibly, and improving the thermal efficiency has been the focus of attention in this industry. The heat of the high-temperature raw gas is recovered by adopting the ascending tube heat exchanger to heat rich oil, lean oil, water for ammonia distillation, superheated steam and the like, so that the tubular furnace is replaced, the heat efficiency is improved by more than 35 percent, and the exhaust emission point of the tubular furnace is reduced. Therefore, the economic and environmental benefits of coking are greatly improved.
In addition, the coke oven in production is generally not in production all the year round, but after the ascending tube heat exchanger is installed, if emergency situations or emergencies such as natural power failure, motor faults and the like occur, the pump driving water or heat medium stops running, the water or heat medium flowing through the ascending tube heat exchanger is cut off, a dry burning state in the ascending tube heat exchanger is generated, the damage to parts in the ascending tube heat exchanger is large in the dry burning state, and the service life of the ascending tube heat exchanger is greatly shortened.
SUMMERY OF THE UTILITY MODEL
The technical problem is as follows: in order to solve the defects in the prior art, the application provides a device for doing work by utilizing waste heat of raw gas of a coke oven.
The technical scheme is as follows: in order to solve the defects of the prior art, the utility model provides an utilize coke oven crude gas waste heat to do work device which characterized in that: the device comprises a riser heat exchanger, a heat exchange device and a circulating pump, wherein the riser heat exchanger, the heat exchange device and the circulating pump are respectively and independently arranged on the top of the coke oven and are connected in a ring to form a heat exchange cycle, and water, heat conducting oil or other heat media are adopted as heat exchange media in the heat exchange cycle; the ascending pipe heat exchanger is used for recovering heat of high-temperature raw gas in the ascending pipe, water is changed into saturated steam or low-temperature heating medium is changed into high-temperature heating medium, and the heat exchange device is used for transferring the recovered heat to water for rich oil, lean oil or ammonia distillation in a coal chemical production process; the heat exchange medium is driven by the circulating pump to absorb heat through the ascending pipe heat exchanger to become a steam-water mixture or a high-temperature heat medium, then the steam-water mixture or the high-temperature heat medium passes through the heat exchange device to be cooled, and then the steam-water mixture or the high-temperature heat medium enters the circulating pump again to complete a cycle.
As an improvement, the heat exchange device is at least one of a steam drum, a water heater for ammonia distillation, a rich oil heater, a heat transfer oil evaporator and a lean oil heater.
As another improvement, the device also comprises a rising pipe superheater which is independently arranged on the top of the coke oven; and introducing steam into the riser superheater, wherein the steam absorbs heat in the riser superheater and becomes superheated steam which is sent to the coal chemical production process.
As another improvement, when water is used as a heat exchange medium, the ascending tube heat exchanger is the ascending tube evaporator.
As a further improvement, the outlet end of the heat exchange medium of the ascending tube evaporator is connected with one inlet end of the steam drum, one outlet end of the steam drum is communicated with the inlet end of the circulating pump, the outlet end of the circulating pump is communicated with the inlet end of the ammonia evaporation water heater, and the outlet end of the ammonia evaporation water heater is communicated with the inlet end of the heat exchange medium of the ascending tube evaporator to complete a cycle.
As a further improvement, the outlet end of the heat exchange medium of the ascending tube evaporator is connected with one inlet end of a steam drum, one outlet end of the steam drum is communicated with the inlet end of a circulating pump, the outlet end of the circulating pump is communicated with the inlet end of a rich oil heater, the outlet end of the rich oil heater is communicated with the inlet end of a water heater for ammonia distillation, and the outlet end of the water heater for ammonia distillation is communicated with the inlet end of the heat exchange medium of the ascending tube evaporator, so that one cycle is completed.
As a further improvement, the outlet end of the heat exchange medium of the ascending tube evaporator is connected with one inlet end of the steam drum, one outlet end of the steam drum is communicated with the inlet end of the circulating pump, and the outlet end of the circulating pump is communicated with the inlet end of the heat exchange medium of the ascending tube evaporator to complete a cycle.
As a further improvement, a rich oil channel or a lean oil channel is arranged in the steam pocket, the rich oil channel or the lean oil channel exchanges heat with steam in the steam pocket to heat the rich oil or the lean oil in the rich oil channel or the lean oil channel, when the heat exchange area of the rich oil or the lean oil heated by the steam is large, the heat exchange device can be arranged above the steam pocket, the heat exchange device is communicated with the steam pocket through a rising communicating pipe and a falling communicating pipe, the steam upwards enters the heat exchange device through the rising communicating pipe, and condensed water enters the steam pocket through the falling communicating pipe.
As a further improvement, a saturated steam outlet in the steam drum is connected with a steam inlet of the ascending pipe superheater, and the steam is heated continuously by the ascending pipe superheater to form superheated steam.
As another improvement, the outlet end of a heat exchange medium, such as heat conducting oil, of the ascending tube heat exchanger is connected with the inlet end of the rich oil heater, the outlet end of the rich oil heater is communicated with the inlet end of the ammonia evaporation water heater, the outlet end of the ammonia evaporation water heater is communicated with the inlet end of the heat conducting oil evaporator, the outlet end of the heat conducting oil evaporator is connected with the inlet end of the circulating pump, and the outlet end of the circulating pump is communicated with the inlet end of the ascending tube heat exchanger.
As another improvement, the outlet end of a heat exchange medium (heat conduction oil) of the ascending tube heat exchanger is connected with the inlet end of a lean oil heater, the outlet end of the lean oil heater is connected with the inlet end of a heat conduction oil evaporator, the outlet end of the heat conduction oil evaporator is connected with the inlet end of a circulating pump, and the outlet end of the circulating pump is communicated with the inlet end of the ascending tube heat exchanger to complete a cycle.
As a further improvement, the ascending tube heat exchanger comprises an inner tube, a heat exchange tube, a natural cooling tube, a tube cap and a heat conduction layer, wherein the heat exchange tube and the natural cooling tube are buried in the heat conduction layer; the outer wall of the inner cylinder is alternately and spirally wound with heat exchange tubes and natural cooling tubes; the natural cooling pipe is composed of a plurality of groups of sections, each group of sections is provided with a group of inlet ends and outlet ends which are communicated with the outside air, and the pipe caps are fixedly arranged at the inlet ends.
As a further improvement, the aerodynamic force inside each natural cooling air pipe should satisfy the following conditions:
delta H is more than or equal to Delta P, wherein the Delta H is airflow power, and the Delta P is airflow resistance;
Δ H is Δ ρ gh, Δ ρ is the density difference of the air inlet and outlet, g is the gravity acceleration, and H is the height difference of the inlet and outlet;
ΔP＝(λL/d+Σξ)ρu 22, lambda is the on-way resistance coefficient, L is the length of the pipe, d is the inner diameter of the cooling air pipe, and sigma ξ is the sum of the local resistance coefficients;
the flow speed under the working condition is u-G/(rho pi d)2/4)；
G is the mass flow rate of air, and ρ is the average temperature correspondence of airThe average temperature is t ═ t (t)1+t2)/2，t1Is the inlet temperature, t2Is the outlet temperature;
the heat exchange quantity of the natural cooling air pipe is Q, which is equal to the heat absorption quantity of air, and Q is GCp (t)2-t1) And Cp is the specific heat corresponding to the average temperature of air.
As a further improvement, when a water pump or a heat medium pump for supplying the ascending pipe heat exchanger does not operate in case of power failure, the pipe cap is in an open state; when the water pump or the heat medium pump which is supplied to the heat exchanger of the ascending pipe is electrified and operated after being electrified, the pipe cap is in a closed state.
Has the advantages that: the utility model provides a do work device by utilizing waste heat of coke oven crude gas, which has the industrial application of multiple purposes, according to the heat recovery of an ascending tube heat exchanger and the heat required by heating rich oil, ammonia water, lean oil, superheated steam and the like in the coal chemical production process, the quantity of the ascending tube heat exchanger and the ascending tube superheater in the device are reasonably arranged, the benzene removal tube furnace and the ammonia distillation tube furnace which adopt coke oven gas combustion in the conventional process are replaced, the adverse effects of the two heating modes that the smoke exhaust temperature is up to 350 ℃ and the thermal efficiency is lower than about 60 percent are eliminated, the device specifically comprises the heating of the rich oil by steam heating or the hot water after the pump to heat the rich oil, the steam to heat the lean oil, the hot water after the pump to heat the ammonia water, the high-temperature heat conduction oil to heat the rich oil and the ammonia water, the types of lean oil and the like, the industrial application and the structure, the thermal efficiency of the coke oven production process, and the emission point of waste gas pollution is reduced, energy is saved, emission is reduced, and the significance of environmental protection is great.
And simultaneously, the utility model discloses the middle needle is to the dry combustion method phenomenon that tedge heat exchanger easily takes place when the outage, from the physics mechanics angle, is provided with the pipe cap at natural cooling tube entrance point, has reached the cooling purpose to other parts in the tedge heat exchanger when dry combustion method effectively, plays the effect of protection tedge heat exchanger. In addition, the pipe orifice at the hot air outlet is in a slope shape, so that rainwater can be prevented from entering the natural cooling pipe.
Drawings
Fig. 1 is a schematic structural diagram of a first embodiment of the heating device of the present invention.
Fig. 2 is a schematic structural diagram of a second embodiment of the heating device of the present invention.
Fig. 3 is a schematic structural diagram of a third embodiment of the heating device of the present invention.
Fig. 4 is a schematic structural diagram of a fourth embodiment of the heating device of the present invention.
Fig. 5 is a schematic structural view of a fifth embodiment of the heating device of the present invention.
Fig. 6 is a schematic structural view of the riser heat exchanger of the present invention.
In the drawings: 1. a riser evaporator; 2. a steam drum; 3. a circulation pump; 4. a water heater for ammonia distillation; 5. a riser superheater; 6. a rich oil heater; 7. a riser heat exchanger; 71. an inner barrel; 72. a heat exchange pipe; 73. naturally cooling the tube; 74. A pipe cap; 75. a heat conductive layer; 76. a heat-insulating layer; 77. an outer cylinder; 8. a heat transfer oil evaporator; 9. a lean oil heater.
Detailed Description
The drawings of the present invention will be described in detail with reference to the embodiments.
The device for recovering, heating and utilizing the waste heat of the crude gas in the ascending pipe of the coke oven by using the high-temperature sensible heat, recovering the heat sensible heat of the crude gas in the ascending pipe of the coke oven, combining with a chemical production process, and using the recovered heat for heating a chemical production process medium. The device for applying work by using the waste heat of the raw gas of the coke oven is different according to different heat medium adopted for recovering the sensible heat of the raw gas: when the heat of the raw coke oven gas is absorbed by using the forced circulation of water to generate steam, the steam heats rich oil, or hot water after pumping heats rich oil, hot water after pumping heats water for ammonia distillation, and the like; when the heat of the raw coke oven gas is absorbed by utilizing the forced circulation of the heat conducting oil to be changed into high-temperature heat conducting oil, the equipment comprises equipment of heating rich oil by the high-temperature heat conducting oil or heating lean oil by the high-temperature heat conducting oil. One part of the ascending pipes of the coke oven recovers the heat of the raw gas by adopting the two methods, the other part of the coke oven introduces saturated steam into the ascending pipe heat exchanger, the saturated steam absorbs the heat of the raw gas and becomes high-temperature superheated steam, and the high-temperature superheated steam is sent to a chemical production process to replace the conventional tubular furnace. The implementation mode of the specific structure of the device for doing work by using the waste heat of the raw gas of the coke oven is shown in the processes in figures 1-5:
the first implementation mode is as follows:
comprises an ascending pipe superheater 5, an ascending pipe evaporator 1, a steam drum 2, a first circulating pump 3 and an ammonia distillation water heater 4; the ascending tube superheater 5 is communicated with the ascending tube evaporator 1, the outlet end of the ascending tube evaporator 1 is connected with one inlet end of the steam drum 2, one outlet end of the steam drum 2 is communicated with the inlet end of the circulating pump 3, the outlet end of the circulating pump 3 is communicated with the inlet end of the ammonia water heater 4, and the outlet end of the ammonia water heater 4 is communicated with the inlet end of the ascending tube evaporator 1; the steam drum 2 is internally provided with an oil-rich channel, the steam drum 2 is provided with an oil-rich inlet port and an oil-rich outlet port, and the oil-rich channel is used for carrying out heat exchange and heating treatment on the internal oil-rich; the circulation pump 3 may be internally provided as an aqueous medium. The method can replace a tubular furnace for rich oil debenzolization.
The second embodiment is as follows:
comprises an ascending pipe superheater 5, an ascending pipe evaporator 1, a steam drum 2, a circulating pump 3, an ammonia distillation water heater 4 and an oil-rich heater 6; the outlet end of the ascending tube evaporator 1 is connected with one inlet end of the steam drum 2, one outlet end of the steam drum 2 is communicated with the inlet end of the circulating pump 3, the outlet end of the circulating pump 3 is communicated with the inlet end of the rich oil heater 6, the outlet end of the rich oil heater 6 is communicated with the inlet end of the ammonia water heater 4, and the outlet end of the ammonia water heater 4 is communicated with the inlet end of the ascending tube evaporator 1; wherein the interior of the steam drum 2 and the interior of the circulation pump 3 can be provided as aqueous media. The method can replace a tubular furnace for rich oil debenzolization.
The inside rich oil passageway that is provided with of steam drum 2, the rich oil passageway carries out heat treatment with the steam heat transfer in the steam drum to the rich oil in the rich oil passageway, and when the heat transfer area of steam heating rich oil was great, the heat-transfer surface can set up in the top of steam drum, by rising, decline communicating pipe UNICOM between heat-transfer surface and the steam drum, steam upwards gets into the heat-transfer surface through rising communicating pipe, and the comdenstion water gets into in the steam drum through descending communicating pipe.
The saturated steam outlet in the steam drum 2 can be not connected with the steam inlet of the ascending pipe superheater 5, or can be connected with the steam inlet of the ascending pipe superheater 5, and the steam is continuously heated by the ascending pipe superheater 5 to form superheated steam.
The third embodiment is as follows:
comprises a rising pipe evaporator 1, a steam drum 2 and a circulating pump 3; the outlet end of the ascending tube evaporator 1 is connected with one inlet end of the steam drum 2, one outlet end of the steam drum 2 is communicated with the inlet end of the circulating pump 3, and the outlet end of the circulating pump 3 is communicated with the inlet end of the ascending tube evaporator 1; wherein the interior of the steam drum 2 and the interior of the circulation pump 3 can be provided as aqueous media.
The steam pocket 2 is internally provided with a lean oil passage, the lean oil passage exchanges heat with steam in the steam pocket to heat lean oil in the lean oil passage, when the heat exchange area of the steam heating lean oil is large, a heat exchange surface can be arranged above the steam pocket, the heat exchange surface is communicated with the steam pocket through a rising communicating pipe and a falling communicating pipe, the steam upwards enters the heat exchange surface through the rising communicating pipe, and condensed water enters the steam pocket through the falling communicating pipe. The method can replace a tubular furnace for removing benzene from lean oil.
The fourth embodiment is as follows:
the device comprises an ascending pipe superheater 5, an ascending pipe heat exchanger 7, a rich oil heater 6, an ammonia evaporation water heater 4, a heat conduction oil evaporator 8 and a circulating pump 3, wherein the outlet end of the ascending pipe heat exchanger 7 is connected with the inlet end of the rich oil heater 6, the outlet end of the rich oil heater 6 is connected with the inlet end of the ammonia evaporation water heater 4, the outlet end of the ammonia evaporation water heater 4 is connected with the inlet end of the heat conduction oil evaporator 8, the outlet end of the heat conduction oil evaporator 8 is connected with the inlet end of the circulating pump 3, and the outlet end of the circulating pump 3 is; the circulating pump 3 is internally provided with a heat conducting oil medium. The method can replace a tubular furnace for rich oil debenzolization.
The fifth embodiment is:
the device comprises a riser heat exchanger 7, wherein the outlet end of the riser heat exchanger 7 is connected with the inlet end of a lean oil heater 9, the outlet end of the lean oil heater 9 is connected with the inlet end of a heat-conducting oil evaporator 8, the outlet end of the heat-conducting oil evaporator 8 is connected with the inlet end of a circulating pump 3, and the outlet end of the circulating pump 3 is communicated with the inlet end of the riser heat exchanger 7; the circulating pump 3 is internally provided with a heat conducting oil medium. The method can replace a tubular furnace for removing benzene from lean oil.
In the first embodiment, rich oil is heated by steam, and water for ammonia evaporation is heated by hot water after pumping to replace a rich oil tubular furnace; in the second embodiment, the pump-back hot water is adopted to heat the rich oil and the water for ammonia distillation, so that the conventional rich oil tube furnace is replaced. In the third embodiment, steam is adopted to heat the lean oil, and the conventional lean oil tube furnace is replaced. In the fourth embodiment, high-temperature heat conduction oil is adopted to heat rich oil and water for ammonia distillation, and the conventional rich oil tubular furnace is replaced. In the fifth embodiment, high-temperature heat conduction oil is adopted to heat the lean oil, so that a conventional lean oil tubular furnace is replaced.
Meanwhile, the ascending pipe heat exchanger 7 of the present invention includes an inner cylinder 71, a heat exchange pipe 72, a natural cooling pipe 73, a pipe cap 74, and a heat conduction layer 75, wherein the heat exchange pipe 72 and the natural cooling pipe 73 are buried in the heat conduction layer 75; heat exchange tubes 72 and natural cooling tubes 73 are alternately and spirally wound on the outer wall of the inner barrel 71; the natural cooling pipe 73 is composed of a plurality of sections, each section is provided with a set of inlet end and outlet end communicated with the outside air, and a pipe cap 74 is fixedly installed at the inlet end. An insulating layer 76 is disposed on the outer layer of the heat conducting layer 75 for heat preservation and heat dissipation reduction. The heat insulation structure further comprises an outer cylinder 77, wherein the outer cylinder 77 is arranged on the outer side surface of the heat insulation layer 76 and used for fixing the heat insulation layer 76 and an internal structure.
The number of segments of the natural cooling tubes 73 can be calculated according to physical mechanics to ensure that the buoyancy force applied to the air in each segment is sufficient to overcome the flow resistance to determine how many groups of natural cooling tubes should be arranged.
In order to overcome the flow resistance and ensure the air circulation speed, the aerodynamic force inside each natural cooling air pipe should satisfy:
delta H is more than or equal to Delta P, wherein the Delta H is flow power, and the Delta P is flow resistance;
Δ H is Δ ρ gh, Δ ρ is the density difference of the air inlet and outlet, g is the gravity acceleration, and H is the height difference of the inlet and outlet;
ΔP＝(λL/d+Σξ)ρu22, lambda is the on-way resistance coefficient, L is the length of the pipe, d is the inner diameter of the cooling air pipe, and sigma ξ is the sum of the local resistance coefficients;
the flow speed under the working condition is u-G/(rho pi d)2/4)；
G is the mass flow of air, and ρ is the average of the airDensity corresponding to temperature, average temperature t ═ t (t)1+t2)/2，t1Is the inlet temperature, t2Is the outlet temperature;
the heat exchange quantity of the natural cooling air pipe is Q, which is equal to the heat absorption quantity of air, and Q is GCp (t)2-t1) And Cp is the specific heat corresponding to the average temperature of air.
The cap 74 of the inlet of the natural cooling pipe 73 is closed and not opened when the riser heat exchanger is in normal operation, and the cap 74 is opened when the power failure pump of the riser heat exchanger 7 is not operated. When power is cut off, the pump driving water or heat medium stops running, the water or heat medium flowing through the heat exchange pipe is cut off, and the ascending pipe heat exchanger is in a dry burning state. At this time, the pipe cap 74 at the inlet of the natural cooling pipe can be quickly screwed off, because the outlet of the natural cooling pipe is positioned relatively above, the cold air in the external environment enters the natural cooling pipe, absorbs the heat accumulated by each component in the ascending pipe heat exchanger and turns into the hot air, because the density of the hot air is smaller than that of the cold air, the hot air can flow upwards along the spiral line in the natural cooling pipe under the buoyancy effect generated by the density difference and is discharged to the atmosphere from the outlet, the aim of cooling other components in the ascending pipe heat exchanger during dry burning is achieved, and the function of protecting the ascending pipe heat exchanger is achieved. Simultaneously the utility model discloses in set up the mouth of pipe in hot-blast exit and be the slope shape, can prevent that the rainwater from getting into the natural cooling pipe.
The above-mentioned embodiments only represent some embodiments of the present invention, and the description thereof is specific and detailed, but not to be construed as limiting the scope of the present invention. It should be noted that, for those skilled in the art, without departing from the spirit of the present invention, several variations and modifications can be made, which are within the scope of the present invention. Therefore, the protection scope of the present invention should be subject to the appended claims.
Claims (10)
1. A device for utilizing waste heat of coke oven crude gas to do work is characterized in that: the device comprises a riser heat exchanger (7) which is respectively and independently arranged on the top of the coke oven, a heat exchange device and a circulating pump (3), wherein the riser heat exchanger (7), the heat exchange device and the circulating pump (3) are connected in a ring to form a heat exchange cycle, and water, heat conduction oil or other heat media are adopted as heat exchange media in the heat exchange cycle; the ascending pipe heat exchanger (7) is used for recovering heat of high-temperature raw gas in the ascending pipe, water is changed into saturated steam or low-temperature heating medium is changed into high-temperature heating medium, and the heat exchange device is used for transferring the recovered heat to water for rich oil, lean oil or ammonia distillation in the coal chemical production process; the heat exchange medium is driven by the circulating pump to absorb heat through the ascending pipe heat exchanger (7) to become a steam-water mixture or a high-temperature heating medium, then the steam-water mixture or the high-temperature heating medium passes through the heat exchange device to be cooled, and then the steam-water mixture or the high-temperature heating medium enters the circulating pump again to complete a cycle; when water is used as a heat exchange medium, the ascending tube heat exchanger (7) is the ascending tube evaporator (1).
2. The device for applying work by using the waste heat of the coke oven crude gas as claimed in claim 1, wherein: the heat exchange device is at least one of a steam drum (2), a water heater (4) for ammonia distillation, an oil-rich heater (6), a heat-conducting oil evaporator (8) and a lean oil heater (9).
3. The device for applying work by using the waste heat of the coke oven crude gas as claimed in claim 1, wherein: the device also comprises a rising pipe superheater (5) which is independently arranged on the top of the coke oven; and steam is introduced into the riser superheater (5), and the steam absorbs heat in the riser superheater (5) and becomes superheated steam which is sent to the coal chemical production process.
4. The device for utilizing the waste heat of the coke oven crude gas to do work according to claim 3, characterized in that: the outlet end of the heat exchange medium of the ascending tube evaporator (1) is connected with one inlet end of the steam drum (2), one outlet end of the steam drum (2) is communicated with the inlet end of the circulating pump (3), the outlet end of the circulating pump (3) is communicated with the inlet end of the ammonia distillation water heater (4), and the outlet end of the ammonia distillation water heater (4) is communicated with the inlet end of the heat exchange medium of the ascending tube evaporator (1), so that one cycle is completed.
5. The device for utilizing the waste heat of the coke oven crude gas to do work according to claim 3, characterized in that: the outlet end of the heat exchange medium of the ascending tube evaporator (1) is connected with one inlet end of the steam drum (2), one outlet end of the steam drum (2) is communicated with the inlet end of the circulating pump (3), the outlet end of the circulating pump (3) is communicated with the inlet end of the rich oil heater (6), the outlet end of the rich oil heater (6) is communicated with the inlet end of the ammonia evaporation water heater (4), and the outlet end of the ammonia evaporation water heater (4) is communicated with the inlet end of the heat exchange medium of the ascending tube evaporator (1), so that a cycle is completed.
6. The device for utilizing the waste heat of the coke oven crude gas to do work according to claim 3, characterized in that: the outlet end of the heat exchange medium of the ascending tube evaporator (1) is connected with one inlet end of the steam drum (2), one outlet end of the steam drum (2) is communicated with the inlet end of the circulating pump (3), and the outlet end of the circulating pump (3) is communicated with the inlet end of the heat exchange medium of the ascending tube evaporator (1) to complete a cycle.
7. The device for utilizing the waste heat of the coke oven crude gas to do work according to claim 4, which is characterized in that: the steam pocket (2) is internally provided with an oil-rich or oil-poor channel, the oil-rich or oil-poor channel exchanges heat with steam in the steam pocket to heat the oil-rich or oil-poor in the oil-rich or oil-poor channel, when the heat exchange area of the steam heating the oil-rich or oil-poor is large, the heat exchange device can be arranged above the steam pocket (2), the heat exchange device is communicated with the steam pocket (2) through ascending and descending communicating pipes, the steam upwards enters the heat exchange device through the ascending communicating pipes, and condensed water enters the steam pocket through the descending communicating pipes; and a saturated steam outlet in the steam drum (2) is connected with a steam inlet of the ascending pipe superheater (5), and the steam is continuously heated by the ascending pipe superheater (5) to form superheated steam.
8. The device for applying work by using the waste heat of the coke oven crude gas as claimed in claim 1, wherein: the outlet end of a heat exchange medium of the ascending tube heat exchanger (7) is connected with the inlet end of the rich oil heater (6), the outlet end of the rich oil heater (6) is communicated with the inlet end of the ammonia evaporation water heater (4), the outlet end of the ammonia evaporation water heater (4) is communicated with the inlet end of the heat-conducting oil evaporator (8), the outlet end of the heat-conducting oil evaporator (8) is connected with the inlet end of the circulating pump (3), and the outlet end of the circulating pump (3) is communicated with the inlet end of the ascending tube heat exchanger (7) to complete a cycle.
9. The device for applying work by using the waste heat of the coke oven crude gas as claimed in claim 1, wherein: the outlet end of a heat exchange medium of the ascending tube heat exchanger (7) is connected with the inlet end of a lean oil heater (9), the outlet end of the lean oil heater (9) is connected with the inlet end of a heat-conducting oil evaporator (8), the outlet end of the heat-conducting oil evaporator (8) is connected with the inlet end of a circulating pump (3), and the outlet end of the circulating pump (3) is communicated with the inlet end of the ascending tube heat exchanger (7) to complete a cycle.
10. The device for utilizing the waste heat of the raw gas of the coke oven to do work according to any one of claims 1 to 9, which is characterized in that: the ascending tube heat exchanger (7) comprises an inner tube (71), a heat exchange tube (72), a natural cooling tube (73), a tube cap (74) and a heat conduction layer (75), wherein the heat exchange tube (72) and the natural cooling tube (73) are buried in the heat conduction layer (75); heat exchange tubes (72) and natural cooling tubes (73) are alternately and spirally wound on the outer wall of the inner cylinder (71); the natural cooling pipe (73) is composed of a plurality of groups of sections, each group of sections is provided with a group of inlet ends and outlet ends which are communicated with the outside air, and the pipe cap (74) is fixedly arranged at the inlet end.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201922008708.2U CN211311372U (en) | 2019-11-19 | 2019-11-19 | Device for doing work by utilizing waste heat of coke oven crude gas |
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| CN201922008708.2U CN211311372U (en) | 2019-11-19 | 2019-11-19 | Device for doing work by utilizing waste heat of coke oven crude gas |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114705064A (en) * | 2022-03-30 | 2022-07-05 | 南京华电节能环保股份有限公司 | Raw coke oven gas waste heat recycling device for coke oven ascension pipe |
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2019
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114705064A (en) * | 2022-03-30 | 2022-07-05 | 南京华电节能环保股份有限公司 | Raw coke oven gas waste heat recycling device for coke oven ascension pipe |
| CN114705064B (en) * | 2022-03-30 | 2023-06-13 | 南京华电节能环保股份有限公司 | Raw gas waste heat recycling device for coke oven rising pipe |
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