CN220485624U - System for improving operation elasticity of fuel gas and steam system of oil refinery - Google Patents
System for improving operation elasticity of fuel gas and steam system of oil refinery Download PDFInfo
- Publication number
- CN220485624U CN220485624U CN202322142918.7U CN202322142918U CN220485624U CN 220485624 U CN220485624 U CN 220485624U CN 202322142918 U CN202322142918 U CN 202322142918U CN 220485624 U CN220485624 U CN 220485624U
- Authority
- CN
- China
- Prior art keywords
- naphtha
- heat exchanger
- tower
- fractionating tower
- refined
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002737 fuel gas Substances 0.000 title claims abstract description 32
- 230000001105 regulatory effect Effects 0.000 claims abstract description 28
- 238000004523 catalytic cracking Methods 0.000 claims abstract description 24
- 239000000463 material Substances 0.000 claims abstract description 18
- 238000004519 manufacturing process Methods 0.000 claims abstract description 13
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000001257 hydrogen Substances 0.000 claims abstract description 9
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 9
- 239000002283 diesel fuel Substances 0.000 claims description 22
- 238000002407 reforming Methods 0.000 claims description 15
- 238000005984 hydrogenation reaction Methods 0.000 claims description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 238000000034 method Methods 0.000 claims description 8
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000005855 radiation Effects 0.000 claims description 3
- 238000004804 winding Methods 0.000 claims description 3
- 239000003921 oil Substances 0.000 abstract description 14
- 239000010779 crude oil Substances 0.000 abstract description 2
- 239000000047 product Substances 0.000 description 10
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 8
- 230000008901 benefit Effects 0.000 description 4
- 239000001294 propane Substances 0.000 description 4
- 239000007789 gas Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical class C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000037351 starvation Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model discloses a system for improving the operation elasticity of a fuel gas and steam system of an oil refinery, wherein materials at the bottom of a naphtha fractionating tower enter a high-efficiency heat exchanger through a first gate valve and a pipeline to be heated, then return into the tower from the lower part of the naphtha fractionating tower through a second gate valve and the pipeline, refined naphtha at the bottom of the naphtha fractionating tower passes through a refined naphtha pump and a refined naphtha pipeline to a downstream device, a heat source of the high-efficiency heat exchanger is derived from refined diesel, and after the heat exchange of the refined diesel is carried out through a refined diesel/cold low-split oil heat exchanger, the refined diesel enters the high-efficiency heat exchanger through a third gate valve to exchange heat, and then enters a reboiler of a catalytic cracking depropanizer through a sixth regulating valve. The system can improve the operation elasticity of the fuel gas system and the steam system, is suitable for different crude oil processing loads, is suitable for the shutdown or operation of the hydrogen production device, and is suitable for the working conditions of winter and summer.
Description
Technical Field
The utility model relates to the technical field of refinery processes, in particular to a system for improving the operation elasticity of a fuel gas and steam system of a refinery, which is suitable for a typical refinery with continuous reforming, diesel hydro-upgrading, catalytic cracking and hydrogen production devices.
Background
Fuel gas is an important byproduct of a refinery, part of the fuel gas is used for preparing hydrogen raw materials, and the rest of the fuel gas is used as heating furnace fuel of each device, so that the fuel gas is one of main energy consumption of the refinery. However, refineries are generally faced with fuel gas starvation situations, requiring high added value propane or domestic liquefied gas to balance the fuel gas system. The comprehensive commodity rate of the oil refinery can be reduced, and propane with high added value is fed into a fuel gas system, so that the oil refinery belongs to high quality and low use, and the economic benefit is influenced. Meanwhile, the oil refinery is provided with a plurality of back pressure turbines, medium pressure steam is consumed, a large amount of low pressure steam is produced by back pressure, the low pressure steam is mainly used as a heat source of a heat exchanger and heat tracing, the consumption difference between the heat tracing season and the non-heat tracing season is large, and meanwhile, the balance of fuel gas and steam is a great difficulty facing the oil refinery due to the change of processing load and raw material properties. Or the low-pressure steam is excessively emptied, so that the resource waste is caused; the fuel gas is insufficient to supplement propane with high added value, or the fuel gas is excessive and discharged into a torch to burn when the hydrogen production device is stopped according to the production adjustment requirement, so that the energy is extremely wasted, and the economic benefit is influenced by high quality and low use, and the current energy-saving low-carbon situation is seriously contrary.
Disclosure of Invention
The utility model aims at overcoming the defects of the prior art and provides a system for improving the operation flexibility of a fuel gas and steam system of an oil refinery.
The technical proposal is as follows: a system for improving the operation elasticity of a fuel gas and steam system of a refinery comprises a reforming pre-hydrogenation stripping tower, a stripping tower reboiling furnace pump, a stripping tower reboiling furnace, a naphtha fractionating tower bottom pump, a diesel hydrogenation modified product fractionating tower, a refined diesel pump, a refined diesel/product fractionating tower feeding heat exchanger, a refined diesel/cold low-pressure oil heat exchanger, a refined diesel steam generator, a catalytic cracking depropanizer reboiler, a refined diesel/catalytic cracking heating medium water heat exchanger, a refined diesel/catalytic cracking desalted water heat exchanger, an air cooler and a naphtha fractionating tower; the pre-hydrogenated naphtha pipeline enters the middle part of a reforming pre-hydrogenation stripping tower, the bottom material flow of the reforming pre-hydrogenation stripping tower enters a convection chamber of a stripping tower reboiling furnace through a stripping tower reboiling furnace pump and a first regulating valve, and after being heated, enters the lower part of the reforming pre-hydrogenation stripping tower from an outlet of the stripping tower reboiling furnace; the stripped pre-hydrogenated naphtha pipeline enters the middle part of a naphtha fractionating tower, and the bottom material flow of the naphtha fractionating tower enters a radiation chamber of a reboiler of the naphtha fractionating tower through a naphtha fractionating tower bottom pump and a second regulating valve, and enters the lower part of the naphtha fractionating tower from an outlet of the reboiler of the naphtha fractionating tower after being heated; the bottom oil pipeline of the diesel hydro-upgrading stripping tower enters the tower from the middle part of the diesel hydro-upgrading product fractionating tower, the refined diesel oil in the bottom material flow of the diesel hydro-upgrading product fractionating tower passes through a refined diesel oil pump, a third regulating valve, a refined diesel oil/product fractionating tower feeding heat exchanger, a fourth regulating valve, a refined diesel oil/cold low-pressure oil heat exchanger, a fifth regulating valve, a refined diesel oil steam generator, a catalytic cracking depropanizer reboiler, a refined diesel oil/catalytic cracking heat medium water heat exchanger and a refined diesel oil/catalytic cracking desalted water heat exchanger, and finally is cooled by an air cooler to be discharged from the device. The bottom pipeline of the naphtha fractionating tower is added with two paths of process pipelines, the bottom material of the naphtha fractionating tower enters a cold medium inlet of a high-efficiency heat exchanger through a first gate valve and a pipeline, after being heated, the bottom refined naphtha of the naphtha fractionating tower returns to the tower from the lower part of the naphtha fractionating tower through a second gate valve and the pipeline, the refined naphtha passes through another pipeline, a refined naphtha pump and a refined naphtha pipeline which are added to a downstream device, the heat source of the high-efficiency heat exchanger is from refined diesel, the refined diesel enters a heat medium inlet of the high-efficiency heat exchanger through a third gate valve and the pipeline after being subjected to heat exchange, and enters a catalytic cracking depropanizer reboiler through a sixth regulating valve after being subjected to heat exchange, a fourth gate valve is added to an outlet of the refined diesel steam generator, and a fifth gate valve is added to the pipeline between an outlet of a naphtha reboiling furnace and the naphtha fractionating tower.
Further, the fourth gate valve, the fifth gate valve, the second regulating valve and the fifth regulating valve are in a closed state in normal operation of the system.
Further, the efficient heat exchanger is a winding type heat exchanger and is vertically arranged.
Further, the stripper reboiler and the naphtha fractionator reboiler are two-in-one heater structures sharing a convection chamber.
Further, the naphtha fractionating tower reboiler is reserved when the system is running in normal production, is mutually standby with the efficient heat exchanger and is switched at any time; according to the production regulation requirement, the hydrogen production device is stopped or the processing load is regulated, and when the fuel gas is excessive, the process is switched back to the reboiling furnace flow.
Compared with the prior art, the utility model has the following advantages:
1. the high-efficiency heat exchanger adopted in the utility model can meet the requirement of small site position, and can meet the requirement of high heat transfer efficiency under the condition of small temperature difference between refined diesel and the tower bottom material of the naphtha fractionating tower. Meanwhile, the high-efficiency heat exchanger is vertically placed, so that the heat exchange area can be guaranteed, the height of the heat exchanger is reduced, and the pressure loss is reduced.
2. In the utility model, the refined diesel oil is used as the heat source of the efficient heat exchanger, and steam is not used as the heat source, so that the problem of continuous reforming catalyst failure caused by water content of refined naphtha when the heat exchanger fails and leaks is avoided.
3. In the patent of the utility model, the reboiler of the original naphtha fractionating tower is reserved, and the reboiler and the high-efficiency heat exchanger are mutually standby and switched at any time. According to the production adjustment requirement, the hydrogen production device is stopped or the processing load is adjusted, and when the fuel gas is excessive, the process can be switched back to the reboiling furnace flow, so that the elastic adjustment of the fuel gas system can be realized.
4. By the system in the patent of the utility model, the fuel gas consumption is reduced by 850Nm 3 And (h) saving propane and civil gas; 3.5-6.5 t/h low-pressure steam can be produced at a small amount, and excessive emptying of the low-pressure steam is avoided; when the heat supplied to catalytic cracking is insufficient after the heat exchange of the diesel hydro-upgrading refined diesel, surplus 1.0MPa steam can be used, which is an important technology for solving the balance of steam and gas; the continuous reforming device stops 10000V/250KW big pump, and increases small pump, which can save electricity by 60%. Through the system in this patent, improved fuel gas system and steam system operation elasticity, can adapt to different crude oil processing loads, be suitable for hydrogen plant and shut down or operate, adapt to winter and summer operating mode. Namely: under various working conditions, dynamic economical balance of the whole-plant fuel gas system and the steam system is realized through linkage and switching of fuel gas and steam.
Drawings
FIG. 1 is a schematic diagram of an embodiment of the present utility model.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present utility model more apparent, the technical solutions in the embodiments of the present utility model will be clearly and completely described in the following in conjunction with the embodiments of the present utility model, and it is apparent that the described embodiments are some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Referring to fig. 1, a system for improving the operation flexibility of a refinery fuel gas and steam system comprises a reforming pre-hydrogenation stripper 2, a stripper reboiler 3, a stripper reboiler 5, a naphtha fractionating tower reboiler 6, a naphtha fractionating tower bottom pump 8, a diesel hydro-upgrading product fractionating tower 20, a refined diesel pump 21, a refined diesel/product fractionating tower feed heat exchanger 23, a refined diesel/cold low-pressure oil heat exchanger 25, a refined diesel steam generator 27, a catalytic cracking depropanizer reboiler 28, a refined diesel/catalytic cracking heat medium water heat exchanger 29, a refined diesel/catalytic cracking demineralized water heat exchanger 30, an air cooler 31, and a naphtha fractionating tower 33; the pre-hydrogenated naphtha pipeline 1 enters the middle part of the reforming pre-hydrogenation stripping tower 2, the bottom material flow of the reforming pre-hydrogenation stripping tower 2 enters a convection chamber of a stripping tower reboiling furnace 5 through a stripping tower reboiling furnace pump 3 and a first regulating valve 4, and after being heated, enters the lower part of the reforming pre-hydrogenation stripping tower 2 from an outlet of the stripping tower reboiling furnace 5; the stripped pre-hydrogenated naphtha line 7 enters the middle part of a naphtha fractionating tower 33, and the bottom material flow of the naphtha fractionating tower 33 enters a radiation chamber of a naphtha fractionating tower reboiler 6 through a naphtha fractionating tower bottom pump 8 and a second regulating valve 9, and after being heated, enters the lower part of the naphtha fractionating tower 33 from an outlet of the naphtha fractionating tower reboiler 6; the bottom oil pipeline 19 of the diesel hydro-upgrading stripping tower enters the tower from the middle part of the diesel hydro-upgrading product fractionating tower 20, refined diesel oil in the bottom material flow of the diesel hydro-upgrading product fractionating tower 20 passes through a refined diesel oil pump 21, a third regulating valve 22, a refined diesel oil/product fractionating tower feeding heat exchanger 23, a fourth regulating valve 24, a refined diesel oil/cold low-pressure oil heat exchanger 25, a fifth regulating valve 26, a refined diesel oil steam generator 27, a catalytic cracking depropanizer reboiler 28, a refined diesel oil/catalytic cracking heat medium water heat exchanger 29 and a refined diesel oil/catalytic cracking desalting water heat exchanger 30, and finally is cooled by an air cooler 31 and then discharged. The bottom pipeline of the naphtha fractionating tower 33 is added with two paths of process pipelines, the bottom material of the naphtha fractionating tower 33 enters a cold medium inlet of a high-efficiency heat exchanger through a pipeline which is added, after being heated, the material enters a cold medium inlet of the high-efficiency heat exchanger through a first gate valve 11 and the pipeline, the heated material returns into the tower from the lower part of the naphtha fractionating tower 33 through a second gate valve 13 and the pipeline, refined naphtha at the bottom of the naphtha fractionating tower 33 enters a downstream device through another pipeline which is added, a refined naphtha pump 16 and a refined naphtha pipeline 17, a heat source of the high-efficiency heat exchanger 12 is from refined diesel, the refined diesel enters a hot medium inlet of the high-efficiency heat exchanger 12 through a third gate valve 14 and the pipeline after being subjected to heat exchange, the material enters a catalytic cracking depropanizing tower reboiler 28 through a sixth regulating valve 15, a fourth gate valve 18 is added at an outlet of the refined diesel steam generator 27, and a fifth gate valve 10 is added on the pipeline between an outlet of the naphtha fractionating tower reboiler 6 and the naphtha fractionating tower 33. The fourth gate valve 18, the fifth gate valve 10, the second regulating valve 9, and the fifth regulating valve 26 are in a closed state during normal operation of the system. The efficient heat exchanger 12 is a winding type heat exchanger and is vertically arranged. The stripping tower reboiling furnace 5 and the naphtha fractionating tower reboiling furnace 6 are two-in-one heating furnace structures and share one convection chamber. The naphtha fractionating tower reboiler 6 is reserved when the system is running in normal yield, is mutually standby with the high-efficiency heat exchanger 12 and is switched at any time; according to the production regulation requirement, the hydrogen production device is stopped or the processing load is regulated, and when the fuel gas is excessive, the process is switched back to the reboiling furnace flow.
The above embodiments are only for illustrating the technical solution of the present utility model, and are not limiting; although the utility model has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit and scope of the technical solutions of the embodiments of the present utility model.
Claims (5)
1. A system for improving the operation flexibility of a fuel gas and steam system of a refinery, which comprises a reforming pre-hydrogenation stripping tower (2), a stripping tower reboiler (3), a stripping tower reboiler (5), a naphtha fractionating tower reboiler (6), a naphtha fractionating tower bottom pump (8), a diesel hydro-upgrading product fractionating tower (20), a refined diesel pump (21), a refined diesel/product fractionating tower feeding heat exchanger (23), a refined diesel/cold low-pressure oil heat exchanger (25), a refined diesel steam generator (27), a catalytic cracking depropanizer reboiler (28), a refined diesel/catalytic cracking heat medium water heat exchanger (29), a refined diesel/catalytic cracking demineralized water heat exchanger (30), an air cooler (31) and a naphtha fractionating tower (33); the pre-hydrogenation naphtha pipeline (1) enters the middle part of a reforming pre-hydrogenation stripping tower (2), a bottom material flow of the reforming pre-hydrogenation stripping tower (2) enters a convection chamber of a stripping tower reboiling furnace (5) through a stripping tower reboiling furnace pump (3) and a first regulating valve (4), and after being heated, enters the lower part of the reforming pre-hydrogenation stripping tower (2) from an outlet of the stripping tower reboiling furnace (5); the stripped pre-hydrogenated naphtha pipeline (7) enters the middle part of a naphtha fractionating tower (33), a bottom material flow of the naphtha fractionating tower (33) enters a radiation chamber of a naphtha fractionating tower reboiling furnace (6) through a naphtha fractionating tower bottom pump (8) and a second regulating valve (9), and after being heated, enters the lower part of the naphtha fractionating tower (33) from an outlet of the naphtha fractionating tower reboiling furnace (6); the bottom oil pipeline (19) of the diesel hydro-upgrading stripping tower enters the tower from the middle part of the diesel hydro-upgrading product fractionating tower (20), refined diesel oil in the bottom material flow of the diesel hydro-upgrading product fractionating tower (20) passes through a refined diesel oil pump (21), a third regulating valve (22), a refined diesel oil/product fractionating tower feeding heat exchanger (23), a fourth regulating valve (24), a refined diesel oil/cold low-pressure oil heat exchanger (25), a fifth regulating valve (26), a refined diesel oil steam generator (27), a catalytic cracking depropanizer reboiler (28), a refined diesel oil/catalytic cracking heat medium water heat exchanger (29) and a refined diesel oil/catalytic cracking demineralized water heat exchanger (30), and finally is cooled by an air cooler (31) and then is discharged from the device, and the device is characterized in that: the bottom pipeline of the naphtha fractionating tower (33) is added with two paths of process pipelines, the bottom material of the naphtha fractionating tower (33) enters a cold medium inlet of a high-efficiency heat exchanger through a first gate valve (11) and a pipeline, after being heated, the material returns into the tower from the lower part of the naphtha fractionating tower (33) through a second gate valve (13) and the pipeline, refined naphtha at the bottom of the naphtha fractionating tower (33) enters a downstream device through another pipeline added, a refined naphtha pump (16) and a refined naphtha pipeline (17), a heat source of the high-efficiency heat exchanger (12) is from refined diesel, the refined diesel enters a heat medium inlet of the high-efficiency heat exchanger (12) through a third gate valve (14) and the pipeline after being subjected to heat exchange, and enters a catalytic cracking depropanizer (28) through a sixth regulating valve (15), a fourth gate valve (18) is added at the outlet of a refined diesel steam generator (27), and a fifth gate valve (10) is added between the outlet of the naphtha reboiling tower (6) and the naphtha fractionating tower (33).
2. A system for increasing operational flexibility of a refinery fuel gas and steam system according to claim 1, wherein: the fourth gate valve (18), the fifth gate valve (10), the second regulating valve (9) and the fifth regulating valve (26) are in a closed state in normal operation of the system.
3. A system for increasing operational flexibility of a refinery fuel gas and steam system according to claim 1, wherein: the efficient heat exchanger (12) is a winding type heat exchanger and is vertically arranged.
4. A system for increasing operational flexibility of a refinery fuel gas and steam system according to claim 1, wherein: the stripping tower reboiling furnace (5) and the naphtha fractionating tower reboiling furnace (6) are two-in-one heating furnace structures and share a convection chamber.
5. A system for increasing operational flexibility of a refinery fuel gas and steam system according to claim 1, wherein: the naphtha fractionating tower reboiler (6) is reserved when the system is running in normal yield, is mutually standby with the high-efficiency heat exchanger (12) and is switched at any time; according to the production regulation requirement, the hydrogen production device is stopped or the processing load is regulated, and when the fuel gas is excessive, the process is switched back to the reboiling furnace flow.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322142918.7U CN220485624U (en) | 2023-08-10 | 2023-08-10 | System for improving operation elasticity of fuel gas and steam system of oil refinery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322142918.7U CN220485624U (en) | 2023-08-10 | 2023-08-10 | System for improving operation elasticity of fuel gas and steam system of oil refinery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220485624U true CN220485624U (en) | 2024-02-13 |
Family
ID=89829076
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202322142918.7U Active CN220485624U (en) | 2023-08-10 | 2023-08-10 | System for improving operation elasticity of fuel gas and steam system of oil refinery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN220485624U (en) |
-
2023
- 2023-08-10 CN CN202322142918.7U patent/CN220485624U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN111706411A (en) | Thermodynamic system for transforming back pressure unit into extraction condensing unit and working method | |
| CN211814285U (en) | Heat exchange system of diesel hydrogenation device | |
| CN116006282A (en) | Energy storage system based on machine stove decoupling | |
| CN220485624U (en) | System for improving operation elasticity of fuel gas and steam system of oil refinery | |
| CN102559490B (en) | Device and method for producing biogas by supplying boiler tail gas as heat source to anaerobic tank | |
| CN209026792U (en) | A kind of hot energy-accumulating power station cogeneration system having single tank regenerative apparatus for hot side | |
| CN115234328B (en) | Molten salt heat storage depth peak regulation system of generator set and working method thereof | |
| CN115264563A (en) | Heat storage peak regulation and energy-saving steam supply thermodynamic system | |
| CN202492520U (en) | Device for generating biogas by feeding boiler tail gas as heat source to anaerobic tank | |
| CN214808522U (en) | Methanol rectification unit waste heat cascade utilization coproduction heating system | |
| CN213924805U (en) | Efficient heat recycling system for coupling biogas engineering and biogas slurry thermal hydrolysis engineering | |
| CN210373373U (en) | Double-tank fused salt coupling electric steam boiler and gas steam boiler heat supply system | |
| CN210800708U (en) | Liquid chlorine vaporization system | |
| CN111911253A (en) | Deaerator combined cold recirculation system and method for improving steam supply capacity of boiler | |
| CN207538941U (en) | Internal combustion engine high-temperature residual heat recovery system applied to leather industry | |
| CN212457965U (en) | High-temperature waste heat utilization device | |
| CN215288655U (en) | Diesel oil upgrading device feeding hydrogen preheating energy recovery system | |
| CN101289631A (en) | Optimizing hydrogenation and heat-exchange system | |
| CN220249958U (en) | Parallel external steam supply device for electric boiler and reheat steam | |
| CN205576042U (en) | A heater that goes into operation for SNG device and heating system goes into operation thereof | |
| CN215984152U (en) | Hot water heat energy recovery comprehensive utilization device | |
| CN219159037U (en) | Energy storage system based on machine stove decoupling | |
| CN217816968U (en) | Heat storage peak regulation and energy-saving steam supply thermodynamic system | |
| CN212417031U (en) | System for reducing energy consumption of carbon nine separation tower | |
| CN215718995U (en) | Single-bypass control steam extraction type mixed heat exchange frequency modulation device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |