CN217464376U - System for removing benzene by using waste heat of raw gas to replace tubular furnace ammonia distillation - Google Patents
System for removing benzene by using waste heat of raw gas to replace tubular furnace ammonia distillation Download PDFInfo
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- CN217464376U CN217464376U CN202221251576.1U CN202221251576U CN217464376U CN 217464376 U CN217464376 U CN 217464376U CN 202221251576 U CN202221251576 U CN 202221251576U CN 217464376 U CN217464376 U CN 217464376U
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Abstract
A raw gas waste heat is used for replacing a tubular furnace ammonia distillation debenzolization system, and comprises a deaerator, an ascending tube steam generator group, a steam splitting cylinder, an oil-rich heater and a flash evaporation type indirect ammonia water heater; the outlet of the deaerator is connected with the inlet of the ascending pipe steam generator group through a pipeline, the outlet of the ascending pipe steam generator group is connected with the inlet of the steam-distributing cylinder through a pipeline, the first outlet of the steam-distributing cylinder is connected with the first inlet of the rich oil heater through a pipeline, the first outlet of the rich oil heater is connected with the first inlet of the flash evaporation type indirect ammonia water heater through a pipeline, the rich oil heater is used for benzene removal, the first outlet of the flash evaporation type indirect ammonia water heater is connected with the inlet of the deaerator through a pipeline, and the flash evaporation type indirect ammonia water heater is used for ammonia evaporation. The sensible heat of crude gas in the riser pipe in the operation process of the coke oven of the coke plant is utilized, the riser pipe is adopted to convert the heat into steam, and the generated steam is used for heating rich oil and ammonia-containing wastewater. Eliminates the hidden trouble of the operation of the prior tubular furnace system, saves coal gas and reduces the consumption of washing oil.
Description
Technical Field
The utility model belongs to the technical field of coking industry coke oven raw gas waste heat utilization, in particular to raw gas waste heat is used for replacing tubular furnace ammonia distillation debenzolization system.
Background
At present, crude and sensible heat coal gas of an ascending pipe of a coke plant is mostly not recovered, a benzene removal process of a crude benzene section of a chemical production workshop adopts a tubular furnace to heat rich oil, and a large amount of coal gas is used as a heat source in the production process. Under the force of promoting energy conservation and emission reduction and increasingly strict environmental protection management in China, the existing production mode is contrary to the current energy policy and environmental protection policy.
The problems of the original tubular furnace crude benzene process flow are found through long-term production practice, the tubular furnace of the process flow has a plurality of problems, and the safe production and the circulating wash oil consumption of a crude benzene working section are seriously influenced.
(1) The tubular furnace has great potential safety hazard and seriously influences the safe production of the crude benzene workshop section.
a) The hearth oil-rich pipeline of the tube furnace has potential safety hazard. After long-term heating, the rich oil pipeline in the hearth can be gradually aged, the pipe wall becomes thinner, rich oil leakage can occur after a certain age, the rich oil leaked in the hearth of the tubular furnace can be in fire when meeting open fire, the production stop of a crude benzene working section is caused, and the production is influenced and safety accidents are caused; and local high temperature condition exists, and the rich oil forms carbonization slagging.
b) The gas heating system of the tube furnace has potential safety hazard. The coke oven gas for the tubular furnace is used as a heat source to heat the rich oil, the coke oven gas is difficult to be interrupted in the production process, and the tubular furnace is easy to be tempered and explode if the coke oven gas cannot be processed in time. Such accidents occur occasionally during coking, production losses are immeasurable, and even casualties.
(2) The high temperature of the tube furnace accelerates the deterioration speed of the washing oil, which causes the consumption of the washing oil to be increased. The temperature in the hearth of the tubular furnace is above 700 ℃, rich oil runs at the temperature for a long time, and the local temperature of the rich oil at the part in contact with the tube wall is higher, so that the speed of gathering reaction of unsaturated compounds in the rich oil at high temperature is increased, the quality of circulating wash oil is deteriorated, the benzene washing effect is influenced, and the consumption of the wash oil is increased.
(3) The tube furnace consumes coke oven gas, the exhaust gas temperature is about 400 ℃, resources are extremely wasted, and the method is not economical; generating waste gas polluting the environment.
The original coke oven operation process and the benzene removal process have the problems of the tubular furnace, and simultaneously, a large amount of heat energy is wasted by the raw coke oven gas, so that the method does not conform to the energy utilization guidelines of clean production, energy conservation and emission reduction.
Disclosure of Invention
An object of the utility model is to provide a raw coke oven gas waste heat is used for replacing tubular furnace ammonia distillation debenzolization system to solve above-mentioned problem.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a raw gas waste heat is used for replacing a tubular furnace ammonia distillation debenzolization system, and comprises a deaerator, an ascending tube steam generator group, a steam splitting cylinder, an oil-rich heater and a flash evaporation type indirect ammonia water heater; the outlet of the deaerator is connected with the inlet of the ascending pipe steam generator group through a pipeline, the outlet of the ascending pipe steam generator group is connected with the inlet of the steam-distributing cylinder through a pipeline, the first outlet of the steam-distributing cylinder is connected with the first inlet of the rich oil heater through a pipeline, the first outlet of the rich oil heater is connected with the first inlet of the flash evaporation type indirect ammonia water heater through a pipeline, the rich oil heater is used for benzene removal, the first outlet of the flash evaporation type indirect ammonia water heater is connected with the inlet of the deaerator through a pipeline, and the flash evaporation type indirect ammonia water heater is used for ammonia evaporation.
Furthermore, the ascending pipe steam generator group is composed of a plurality of steam generators connected in parallel, and the inlets and outlets of all the steam generators are converged on one pipeline.
Furthermore, a second outlet of the air distributing cylinder is connected with a water draining device, and the water draining device is connected with an inlet of the deaerator through a pipeline.
Further, a third outlet of the steam distributing cylinder is connected with a flash evaporation type indirect ammonia water heater through a pipeline.
Furthermore, a second inlet of the rich oil heater is connected with the rich oil tank, and a second outlet of the rich oil heater is connected with the debenzolization device; and a second outlet of the rich oil heater is a drain hole.
Furthermore, a second inlet of the flash evaporation type indirect ammonia water heater is connected with ammonia-containing wastewater, a second outlet of the flash evaporation type indirect ammonia water heater is connected with an ammonia still, and a second outlet of the flash evaporation type indirect ammonia water heater is a drain port.
Furthermore, a condensate pump is arranged between the flash evaporation type indirect ammonia water heater and the deaerator.
Furthermore, a plunger type water feeding pump is arranged between the deaerator and the ascending pipe steam generator set.
Compared with the prior art, the utility model discloses there is following technological effect:
the utility model discloses utilize coke oven plant coke oven operation in-process tedge raw gas's sensible heat, adopt the tedge to change the heat into steam, the steam of production is used for rich oil heating and contains the heating of ammonia waste water. The raw gas sensible heat recovery system of the coke oven ascending pipe recovers a large amount of energy to generate steam, replaces a tubular furnace to heat to generate steam, eliminates the hidden trouble of the existing tubular furnace system in operation, saves coal gas and reduces oil washing consumption.
Drawings
FIG. 1 is a schematic flow chart of the present invention;
wherein: 1. a deaerator; 2. a plunger-type feed pump; 3. a riser steam generator water inlet; 4. a riser steam generator; 5. a steam outlet of the riser steam generator; 6. a main steam pipe; 7. a cylinder is divided; 8. A water-repelling device; 9. a benzene removal device; 10. a rich oil heater; 11. an oil rich tank; 12. a drain port of the rich oil heater; 13. an ammonia still; 14. a drain port of a flash evaporation type indirect ammonia water heater; 15. a flash evaporation type indirect ammonia water heater; 16. a condensate pump.
Detailed Description
The present invention will be further explained with reference to the accompanying drawings:
a coke oven ascending pipe crude gas waste heat is used for replacing a tubular furnace ammonia distillation debenzolization device, and mainly comprises a coke oven ascending pipe steam generator 4, a steam distribution cylinder 7, an oil-rich heater 10, a flash evaporation type indirect ammonia water evaporation heater 15, a deaerator and the like 1; the coke oven ascending pipe steam generator 4 is arranged at the position of an original ascending pipe on the top of the coke oven, deoxygenated water enters from a water inlet of the ascending pipe steam generator, sensible heat in raw coke oven gas is absorbed, the raw coke oven gas is further heated and evaporated, and finally generated steam is discharged from a steam outlet 5 of the steam generator; in order to utilize the heat of the produced steam more, the utility model adopts a mode of energy gradient utilization, the produced steam with higher pressure firstly enters a rich oil heater 10 with higher heating temperature to heat rich oil, and the steam is condensed into condensed water under the same pressure after the rich oil is heated and flows out through a drain port 12 of the rich oil heater; the high-pressure condensed water from the rich oil heater 10 enters a flash evaporation type indirect ammonia-containing wastewater heater 15 with the constant pressure being lower pressure to heat the ammonia-containing wastewater with relatively lower temperature, the generated steam and the ammonia-containing wastewater are subjected to condensation heat exchange due to pressure reduction and vaporization at the moment of entering the flash evaporation type indirect ammonia-containing wastewater heater 15, and the steam is condensed into low-pressure condensed water and flows out from a drain opening 14 of the flash evaporation type indirect ammonia-containing wastewater heater; the low-pressure condensed water is sent into the deaerator 1 through the condensed water pump 16 for recycling.
Specifically, the method comprises the following steps: the device comprises a deaerator 1, an ascending pipe steam generator 4, a steam distributing cylinder 7, a rich oil heater 10, a flash evaporation type indirect ammonia water heater 15 and the like; the outlet of the deaerator 1 is connected with a riser steam generator 4, deaerated water is pumped into a plurality of riser steam generators 4 connected in parallel through a plunger type water feeding pump 2, is heated and evaporated in the steam generators 4, and is finally changed into saturated steam which is discharged from a steam outlet 5 of the riser steam generator; the ascending tube steam generator 4 adopts a coil tube type structure, and can improve the steam pressure which can reach 4.0 MPa. The flow of the deoxygenated water entering the riser evaporator 4 is obtained through calculation, and the plunger type water feeding pump 2 is selected to accurately control the water inlet flow, so that the high water content of outlet steam or overheating of steam caused by overlarge water feeding error is avoided.
Saturated steam from the steam outlet 5 of the rising pipe steam generator is collected and then sent to the steam distributing cylinder 7 through the steam main pipe 6, and then is distributed to each steam consuming device through each outlet of the steam distributing cylinder 7; the lower part of the steam distributing cylinder 7 is provided with a drainage device 8, water in steam is separated out in time, and the water separated out by the drainage device 8 enters the deaerator 1 through a condensed water pipe for cyclic utilization.
Leading out steam with higher pressure from the steam distributing cylinder 7 to the rich oil heater 10, condensing and exchanging heat in the rich oil heater 10, condensing the steam into saturated water with the same pressure after heat exchange, and flowing out through a drain port 12 of the rich oil heater; the low-temperature rich oil from the rich oil tank 11 is heated to a required temperature and then sent to a debenzolization device 9 for rich oil debenzolization. The rich oil heater 10 adopts a condensing heat exchanger, so that the heat exchange efficiency is high, and the materials and the occupied area are saved.
The drain port 12 of the rich oil heater is connected with the flash evaporation type indirect ammonia water heater 15, high-pressure drain water from the rich oil heater 10 enters the flash evaporation type indirect ammonia water heater 15 with lower constant pressure, the high-pressure drain water is vaporized into steam due to pressure drop at the moment of entering the ammonia water heater, the generated steam and ammonia-containing wastewater are subjected to condensation heat exchange, and the heat exchange efficiency is improved; the branch cylinder is divided into a path of steam to be introduced into the flash evaporation type indirect ammonia water heater, insufficient heat for heating ammonia-containing wastewater is provided by the steam, indirect heat exchange is adopted for heat exchange between the steam and the ammonia-containing wastewater, steam is condensed into water after heat exchange and is discharged from a drain port 14 of the flash evaporation type indirect ammonia water heater, the discharged water is pumped into the deaerator 1 through the condensate pump 16 to be recycled, and water resource waste is avoided; the heated ammonia-containing wastewater enters an ammonia still 13 to be evaporated with ammonia.
The utility model discloses utilize distinctive tedge steam generator 4 to arrange in coke oven top tedge position, inhale and produce steam from coke oven exhaust raw coke oven gas sensible heat, the steam that produces at first gets into rich oil heater 10 heating rich oil through gas-distributing cylinder 7, and the condensate water that comes out from rich oil heater 10 reenters flash evaporation formula indirect ammonia water heater 15, and the heat transfer is condensed again in flash evaporation formula indirect ammonia water heater 15 flash evaporation, realizes that the heat step utilizes. The water condensed by the flash evaporation type indirect ammonia water heater 15 is pumped into the deaerator 1 through the condensed water pump 16 for cyclic utilization, the process does not consume extra energy, waste heat utilization is realized, the enterprise burden is greatly reduced, the core policy of enterprise sustainable development is followed, the aims of national energy conservation and emission reduction are actively responded, the clean production of the coke oven is met, and the purposes of energy conservation and consumption reduction are achieved.
Claims (8)
1. A system for removing benzene by using raw gas waste heat to replace a tubular furnace for ammonia distillation is characterized by comprising a deaerator (1), a rising pipe steam generator set, a steam distributing cylinder (7), a rich oil heater (10) and a flash evaporation type indirect ammonia water heater (15); the outlet of the deaerator (1) is connected with the inlet of the ascending pipe steam generator group through a pipeline, the outlet of the ascending pipe steam generator group is connected with the inlet of the branch cylinder (7) through a pipeline, the first outlet of the branch cylinder (7) is connected with the first inlet of the rich oil heater (10) through a pipeline, the first outlet of the rich oil heater (10) is connected with the first inlet of the flash evaporation type indirect ammonia water heater (15) through a pipeline, the rich oil heater (10) is used for debenzolization, the first outlet of the flash evaporation type indirect ammonia water heater (15) is connected with the inlet of the deaerator (1) through a pipeline, and the flash evaporation type indirect ammonia water heater (15) is used for ammonia distillation.
2. The system for removing benzene by ammonia distillation of raw gas as claimed in claim 1, wherein the ascending tube steam generator group comprises a plurality of steam generators (4) connected in parallel, and the inlet and outlet of all the steam generators (4) are collected on a pipeline.
3. The system for removing benzene by ammonia distillation of the tubular furnace by using the waste heat of the raw gas as claimed in claim 1, wherein the second outlet of the gas-distributing cylinder (7) is connected with a water draining device (8), and the water draining device (8) is connected with the inlet of the deaerator (1) through a pipeline.
4. The system for removing benzene by ammonia distillation of the raw gas instead of the tube furnace according to the claim 1, characterized in that the third outlet of the gas-distributing cylinder (7) is connected with a flash evaporation type indirect ammonia water heater (15) through a pipeline.
5. The system for removing the benzene by the ammonia distillation of the tubular furnace by using the waste heat of the raw gas as the claim 1, wherein a second inlet of the rich oil heater (10) is connected with the rich oil tank (11), and a second outlet of the rich oil heater (10) is connected with the benzene removal device (9); and a second outlet of the rich oil heater (10) is a drain hole.
6. The system for removing benzene by ammonia distillation of the tubular furnace by using the raw gas waste heat according to claim 1, wherein a second inlet of the flash evaporation type indirect ammonia water heater (15) is connected with ammonia-containing wastewater, a second outlet of the flash evaporation type indirect ammonia water heater (15) is connected with the ammonia distillation tower (13), and a second outlet of the flash evaporation type indirect ammonia water heater (15) is a drain port.
7. The system for removing benzene by ammonia distillation of the raw gas instead of the tube furnace according to the claim 1, characterized in that a condensate pump (16) is arranged between the flash evaporation type indirect ammonia water heater (15) and the deaerator (1).
8. The system for removing benzene by ammonia distillation of the tubular furnace by using the waste heat of the raw gas as the raw gas according to claim 1, wherein a plunger type water feeding pump (2) is arranged between the deaerator (1) and the riser steam generator set.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221251576.1U CN217464376U (en) | 2022-05-23 | 2022-05-23 | System for removing benzene by using waste heat of raw gas to replace tubular furnace ammonia distillation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202221251576.1U CN217464376U (en) | 2022-05-23 | 2022-05-23 | System for removing benzene by using waste heat of raw gas to replace tubular furnace ammonia distillation |
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| Publication Number | Publication Date |
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| CN217464376U true CN217464376U (en) | 2022-09-20 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202221251576.1U Active CN217464376U (en) | 2022-05-23 | 2022-05-23 | System for removing benzene by using waste heat of raw gas to replace tubular furnace ammonia distillation |
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| CN (1) | CN217464376U (en) |
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2022
- 2022-05-23 CN CN202221251576.1U patent/CN217464376U/en active Active
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