CN219580194U - System for reducing carbon emission of independent coal tar processing enterprises - Google Patents
System for reducing carbon emission of independent coal tar processing enterprises Download PDFInfo
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- CN219580194U CN219580194U CN202320684700.1U CN202320684700U CN219580194U CN 219580194 U CN219580194 U CN 219580194U CN 202320684700 U CN202320684700 U CN 202320684700U CN 219580194 U CN219580194 U CN 219580194U
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Abstract
The utility model relates to the technical field of carbon emission reduction of coal tar processing enterprises, in particular to a system for reducing carbon emission of independent coal tar processing enterprises. Comprises a flue gas collecting system, a flue gas cooling system and CO 2 An absorption and desorption system; the flue gas collecting first valve is arranged on a chimney of the heating furnace, one end of the collecting pipeline is connected with the chimney, and the other end of the collecting pipeline is connected with the flue gas cooling system; the bottom of a flue gas cooling tower of the flue gas cooling system, a cooling liquid heat exchanger and the upper part of the flue gas cooling tower are connected through pipelines in sequence, and the top of the flue gas cooling tower is connected with CO 2 The lower pipeline of the absorption tower of the absorption and desorption system is connected; CO 2 The absorption and desorption system comprises an absorption tower and a re-absorption towerTower, flue gas-liquid separator and CO 2 Separator, CO 2 The system comprises a water cooler, a lean-rich liquid heat exchanger, a lean liquid cooler and a regeneration tower reboiler. Collecting the CO-containing 2 And then cooling the flue gas of the heating furnace to remove CO in the flue gas 2 Separating out; reduce the carbon emission of independent coal tar processing enterprises and recycle CO 2 。
Description
Technical Field
The utility model relates to the technical field of carbon emission reduction of coal tar processing enterprises, in particular to a system for reducing carbon emission of independent coal tar processing enterprises.
Background
China is a large country for producing coal, and has rich coal tar resources. The high-temperature coal tar is coal tar obtained in coke production, and is one of coke oven gas clean products condensed and separated in the cooling process of raw gas. Coal tar is a complex mixture of tens of thousands of components from which 500 or more individual compounds are currently isolated and identified, accounting for about 55% of the total coal tar. The coal tar contains organic matters such as alkane, alkene, arene, phenol, polycyclic arene, heterocyclic compound and the like.
At present, the traditional mode of processing and utilizing high-temperature coal tar in China mainly comprises the steps of producing light oil, phenol oil, naphthalene oil, wash oil, anthracene oil, modified asphalt and the like, and further preparing various chemical raw materials such as benzene, toluene, xylene, phenol, cresol, xylenol, industrial naphthalene, crude anthracene and the like after deep processing.
Typical independent coal tar processing enterprises in China generally comprise devices such as tar distillation, distillate dephenolization, industrial naphthalene distillation, phenolate decomposition, refined phenol, crude anthracene, modified asphalt and asphalt molding, heat-conducting oil stations, oil reservoirs, boiler houses and the like. The tar distillation includes normal pressure distillation process, reduced pressure distillation process and atmospheric and reduced pressure distillation process. The dephenolization of the fraction adopts a continuous countercurrent counter-spraying process or a pre-pump mixing process of alkali liquor and the fraction. Industrial naphthalene distillation is carried out by single-furnace, single-tower and double-furnace, double-tower processes, and the pressure thereof is divided into atmospheric distillation and pressurized distillation. The phenolate decomposition adopts a carbon dioxide and sulfuric acid decomposition method process. The refined phenol adopts a reduced pressure distillation process, and the heat conduction oil is used as a heating source. The crude anthracene adopts a vertical partition wall cooling crystallization technology and a centrifugal separation technology. The modified asphalt adopts a kettle type heating process.
Whether a tube furnace for providing heating sources for tar distillation and industrial naphthalene distillation, a conduction oil furnace for providing heating sources for refined phenol distillation, a reaction kettle heating furnace for providing heating sources for modified asphalt, and a boiler room for providing heating sources and steam purging for a storage tank, a great amount of natural gas or coal gas needs to be continuously combusted, and CO is continuously generated 2 Flue gas.
Therefore, the carbon emission of independent coal tar processing enterprises is reduced, and the method becomes a technical problem to be solved in the system.
Disclosure of Invention
In order to overcome the defects of the prior art, the utility model provides a system for reducing carbon emission for independent coal tar processing enterprises, which collects CO 2 And then cooling the flue gas of the heating furnace to remove CO in the flue gas 2 Separating out; reduce the carbon emission of independent coal tar processing enterprises and recycle CO 2 。
In order to achieve the above purpose, the utility model is realized by adopting the following technical scheme:
a system for reducing carbon emission of independent coal tar processing enterprises comprises a flue gas collection system, a flue gas cooling system and CO 2 And an absorption and desorption system.
The flue gas collection system comprises a first valve and a collection pipeline, wherein the first valve is arranged on a heating furnace chimney, one or more heating furnaces are arranged, and a plurality of heating furnaces are connected in parallel through the pipeline. One end of the collecting pipeline is connected with a chimney in front of the first valve, and the other end of the collecting pipeline is connected with the lower part of a flue gas cooling tower of the flue gas cooling system. The collecting pipeline is provided with a second valve, and the second valve is a stop valve.
The flue gas cooling system comprises a flue gas cooling tower, a cooling circulating pump and a cooling liquid heat exchanger. The bottom of the flue gas cooling tower, the cooling circulating pump, the cooling liquid heat exchanger and the upper part of the flue gas cooling tower are connected through pipelines in sequence. The top of the flue gas cooling tower is adjacent to the inlet pipeline of the flue gas fan, and the outlet of the flue gas fan is connected with the lower pipeline of the absorption tower of the CO2 absorption and desorption system.
CO 2 The absorption and desorption system comprises an absorption tower, a regeneration tower, a flue gas-liquid separator and CO 2 Separator, CO 2 The system comprises a water cooler, a lean-rich liquid heat exchanger, a lean liquid cooler, a regeneration tower reboiler, a lean liquid pump and a rich liquid pump.
The top of the absorption tower is connected with a flue gas-liquid separator pipeline. The bottom of the absorption tower, the rich liquid pump, the lean-rich liquid heat exchanger and the upper part of the regeneration tower are connected through pipelines in sequence. The bottom of the regeneration tower, the lean-rich liquid heat exchanger, the lean liquid pump, the lean liquid cooler and the upper part of the absorption tower are connected through pipelines in sequence. The bottom of the regeneration tower, the reboiler of the regeneration tower and the lower part of the regeneration tower are connected through pipelines in turn. Top of regeneration tower, CO 2 Water cooler, CO 2 The separators are connected in turn by pipelines.
Compared with the prior art, the utility model has the beneficial effects that:
1. the utility model contains CO by improving the structures of a tubular furnace, a heat conduction oil furnace, a reaction kettle heating furnace and a boiler chimney 2 After collecting and cooling the flue gas of the heating furnace, absorbing CO from the flue gas by using an absorption liquid 2 Absorbing and separating out pure CO from the absorption liquid in a desorption tower 2 . Thereby realizing the CO in the flue gas 2 Separated out, the separated flue gas can be directly discharged into the atmosphere to separate out pure CO 2 Can be used as CO required for phenolate decomposition 2 Air source, additive for producing carbonated beverage, and CO 2 Welding shielding gas for CO 2 Supercritical extraction and CO for oil field 2 Gas injection oil recovery, CO 2 The method is used for strengthening gas recovery of coal bed gas and is used for producing chemical products: methane, methanol, dicyandiamide, salicylic acid, carbonate and the like, and dry ice and CO are prepared 2 Geological sequestration, and the like.
The utility model can be used for heating CO in the flue gas of the furnace 2 Separated out, thereby reducing CO in the flue gas 2 Is discharged and simultaneously separated CO 2 Can be used as CO required for phenolate decomposition 2 Air source, surplus CO 2 Can be used for various purposes or geological storage.
2. CO in flue gas 2 The recovery rate of (2) is more than or equal to 85 percent, and CO in the residual flue gas 2 Concentration ofMay be as low as 50PPM.
3. Recovery of CO 2 The purity is high, the concentration of the wet base after the primary recovery treatment reaches more than 98.5%, and the concentration can reach more than or equal to 99.99% after the secondary treatment.
4. The carbon emission of the production process of independent coal tar processing enterprises can be remarkably reduced.
5. The process flow is simple, the energy consumption is low, the operation is convenient, and the operation cost is low.
6. And the independent system does not influence the operation of other devices.
Drawings
FIG. 1 is a schematic structural and process schematic diagram of an embodiment of the present utility model.
In the figure: 1-1-tubular furnace body 1-2-heat conduction oil furnace 1-3-reaction kettle heating furnace 1-4-boiler 2-1-tubular furnace chimney 2-2-heat conduction oil furnace chimney 2-3-reaction kettle heating furnace chimney 2-4-boiler chimney 3-flue gas valve 4-stop valve 5-flue gas cooling tower 6-cooling circulation pump 7-cooling liquid heat exchanger 8-flue gas fan 9-absorption tower 10-flue gas liquid separator 11-lean liquid cooler 12-lean liquid pump 13-lean rich liquid heat exchanger 14-rich liquid pump 15-regeneration tower 16-CO 2 Separator 17-CO 2 Water cooler 18-regenerator reboiler
Detailed Description
Embodiments of the present utility model are described in detail below, examples of which are illustrated in the accompanying drawings, wherein like or similar reference numerals refer to like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are illustrative only and are not to be construed as limiting the utility model.
In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "axial", "radial", "circumferential", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the device or element in question must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present utility model. In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model will be understood in specific cases by those of ordinary skill in the art.
Those skilled in the art can, with the benefit of this disclosure, suitably modify the process parameters to achieve this. It is expressly noted that all such similar substitutions and modifications will be apparent to those skilled in the art, and are deemed to be included in the present utility model. While the methods and applications of this utility model have been described in terms of preferred embodiments, it will be apparent to those skilled in the relevant art that variations and modifications can be made in the methods and applications described herein, and in the practice and application of the techniques of this utility model, without departing from the spirit or scope of the utility model.
The following description of the embodiments of the utility model will be given with reference to the accompanying drawings
Examples:
as shown in FIG. 1, the independent coal tar processing enterprise is provided with four heating furnaces, namely a tubular furnace body 1-1, a heat conduction oil furnace 1-2, a reaction kettle heating furnace 1-3 and a boiler 1-4. The four heating furnaces are connected in parallel through pipelines, a tubular furnace chimney 2-1 is arranged at the top of the tubular furnace body 1-1, a heat conduction oil furnace chimney 2-2 is arranged at the top of the heat conduction oil furnace 1-2, a reaction kettle heating furnace 1-3 is provided with a reaction kettle heating furnace chimney 2-3, and a boiler chimney 2-4 is arranged at the boiler 1-4.
A system for reducing carbon emission of independent coal tar processing enterprises comprises a flue gas valve 3, a flue gas collecting system, a flue gas cooling system and CO 2 And an absorption and desorption system.
The flue gas collection system consists of a flue gas valve 3 and a collection pipeline. The flue gas valve 3 is arranged on each heating furnace chimney 2-1-2-4, the inlet of the flue gas collecting pipeline is connected to the chimney in front of the flue gas valve 3 of each heating furnace chimney 2-1-2-4, and the outlet is connected to the bottom of the flue gas cooling tower 5 of the flue gas cooling system. And a stop valve 4 is arranged on the collecting pipeline of each heating furnace.
The flue gas cooling system consists of a flue gas cooling tower 5, a cooling circulating pump 6 and a cooling liquid heat exchanger 7. And flue gas from the flue gas collection system is introduced into the lower part of the flue gas cooling tower 5 through a pipeline, and the top of the flue gas cooling tower 5 is connected with the inlet of the flue gas fan 8. The bottom of the flue gas cooling tower 5 is connected with the inlet of the cooling circulating pump 6, the outlet of the cooling circulating pump 6 is connected with the inlet of the cooling liquid heat exchanger 7, and the outlet of the cooling liquid heat exchanger 7 is connected with the upper part of the flue gas cooling tower 5.
CO 2 The absorption and desorption system comprises a flue gas fan 8, an absorption tower 9, a regeneration tower 15, a flue gas-liquid separator 10 and CO 2 Separator 16, CO 2 The water cooler 17, the rich liquid pump 14, the lean and rich liquid heat exchanger 13, the lean liquid pump 12, the lean liquid cooler 11 and the regeneration tower reboiler 18.
The top of the flue gas cooling tower 5 is connected with the inlet of the flue gas fan 8, and the outlet of the flue gas fan 8 is connected with the lower part of the absorption tower 9. The flue gas from the flue gas cooling system is led into an absorption tower 9 by a flue gas fan 8, and the top of the absorption tower 9 is connected with the middle part of a flue gas-liquid separator 10. The bottom of the absorption tower 9 is connected with an inlet of a rich liquid pump 14, an outlet of the rich liquid pump 14 is connected with an inlet of a lean-rich liquid heat exchanger 13, and an outlet of the lean-rich liquid heat exchanger 13 is connected with an upper part of a regeneration tower 15.
A stream of material at the bottom of the regeneration tower 15 is introduced into the lean liquid pump 12 through the lean-rich liquid heat exchanger 13, the bottom of the regeneration tower 15 is connected with a pipeline of the lean-rich liquid heat exchanger 13, the lean-rich liquid heat exchanger 13 is connected with an inlet pipeline of the lean liquid pump 12, an outlet of the lean liquid pump 12 is connected with an inlet of the lean liquid heat exchanger 11, and an outlet of the lean liquid heat exchanger 11 is connected with an upper pipeline of the absorption tower 9.
Another stream of material at the bottom of the regeneration tower 15 is introduced through an inlet of a regeneration tower reboiler 18, the bottom of the regeneration tower 15 is connected with an inlet pipeline of the regeneration tower reboiler 18, and an outlet of the regeneration tower reboiler 18 is connected with a lower pipeline of the regeneration tower 15. The top of the regeneration tower 15 is connected with an inlet pipeline of a CO2 water cooler 17, CO 2 Outlet of water cooler 17 and CO 2 The middle pipe of the separator 16 is connected.
The technological principle and the working process of the utility model are as follows:
1. during the ignition of the heating furnace:
and closing the stop valve 4, opening the smoke valve 3, and discharging the smoke through the chimney 2-1-2-4 and the smoke valve 3.
2. During operation:
and opening the stop valve 4, closing the smoke valve 3, and discharging the smoke through the stop valve 4, the smoke cooling tower 5, the smoke blower 8, the absorption tower 9 and the smoke gas-liquid separator 10.
3. And (3) cooling the flue gas:
the high-temperature flue gas from each heating furnace chimney 2-1 to 2-4 enters the cooling tower 5 from the lower part of the flue gas cooling tower 5, passes through the cooling tower 5 from bottom to top, is fully contacted with cooling liquid sprayed from top to bottom in a reverse direction, and is cooled in the cooling tower 5.
Cooling the flue gas with the outlet temperature of 200-250 ℃ of each heating furnace chimney 2-1-2-4 to less than or equal to 40 ℃, discharging from the cooling tower top 5, and delivering to CO by a flue gas fan 8 2 And an absorption and desorption system.
The high-temperature cooling liquid is cooled by a cooling circulation pump 6 from the bottom of the flue gas cooling tower 5 through a cooling liquid heat exchanger 7 and then is sent to the top of the flue gas cooling tower 5.
4)CO 2 Absorption:
the cooled flue gas sent from the flue gas fan 8 enters the absorption tower 9 from the lower part of the absorption tower 9, passes through the absorption tower 9 from bottom to top, is fully contacted with lean liquid of the absorption liquid sprayed from top to bottom in countercurrent, and CO in the flue gas 2 Reacts with the absorption liquid to generate a relatively stable compound, and the absorption saturated absorption liquid becomes rich liquid.
Is absorbed by CO 2 The residual flue gas after the removal of the entrained absorption liquid is directly discharged into the atmosphere after the top of the absorption tower 9 enters a flue gas-liquid separator 10, a special efficient foam remover is arranged in the flue gas-liquid separator 10, and the separated absorption liquid enters CO 2 And an absorption and desorption system.
5)CO 2 And (3) desorption:
the rich liquid is pumped from the bottom of the absorption tower 9 by a rich liquid pump 14, enters a lean-rich liquid heat exchanger 13 after being pressurized, exchanges heat with lean liquid from the bottom of the regeneration tower 15, and is sprayed into the tower through a spray head at the upper part of the regeneration tower 15.
In the regeneration tower 15, the rich solution is decomposed to release CO 2 。CO 2 Along with the entrained steam, flows out of the top of the tower, and the gas is in CO 2 The water cooler 17 exchanges heat with the circulating water, and is cooled to be less than or equal to 40 ℃ and then enters CO 2 A separator 16. In CO 2 In the separator 16, the condensate entrained by the gas is separated, and the separated CO 2 The foam is removed exclusively from the upper part of the separator 16 and sent to the following process.
CO 2 Condensate separated by separator 16 enters CO 2 And an absorption and desorption system. The rich liquid at the bottom of the regeneration tower 15 is gasified by steam and then enters the lower part of the regeneration tower 15 to provide the rich liquid for CO desorption 2 The energy required. CO is sucked out by the solution-rich dissolution 2 The solution is changed into lean solution, and the lean solution is sent by a lean solution pump 12 to be cooled by a lean solution cooler 11 and then enters an absorption tower 9 after being subjected to heat exchange with the rich solution by a lean-rich solution heat exchanger 13.
The utility model has strong expandability. The utility model classifies heating furnaces with different purposes and different types. Different independent tar processing enterprises have different scales, different device compositions and different process flows, and more than one heating furnace of a certain type or no heating furnace of a certain type can be adopted.
The utility model has strong operability. The heating furnace can deal with different working states of each heating furnace, during the ignition period of the heating furnace, the flue gas can be discharged temporarily through the original chimney, and the normal working state of the heating furnace can collect the flue gas into the system, and only the flue gas valve and the stop valve of each heating furnace are required to be switched.
The utility model improves the original heating furnace chimney by adding the valve, adds the smoke valve, and is suitable for the carbon reduction and emission reduction improvement of the existing independent tar processing enterprises. If a new tar processing enterprise is built, each heating furnace can be provided with a comprehensive large chimney at the smoke discharge port of the smoke gas-liquid separator without independently constructing a chimney according to the design of the utility model.
The utility model contains CO by improving the structures of a tube furnace chimney 2-1, a heat conduction oil furnace chimney 2-2, a reaction kettle heating furnace chimney 2-3 and a boiler chimney 2-4 2 After collecting and cooling the flue gas of the heating furnace, absorbing CO from the flue gas by using an absorption liquid 2 Absorbing and separating out pure CO from the absorption liquid in a desorption tower 2 . Thereby realizing the CO in the flue gas 2 Separated out, the separated flue gas can be directly discharged into the atmosphere to separate out pure CO 2 Can be used as CO required for phenolate decomposition 2 Air source, additive for producing carbonated beverage, and CO 2 Welding shielding gas for CO 2 Supercritical extraction and CO for oil field 2 Gas injection oil recovery, CO 2 The method is used for strengthening gas recovery of coal bed gas and is used for producing chemical products: methane, methanol, dicyandiamide, salicylic acid, carbonate and the like, and dry ice and CO are prepared 2 Geological sequestration, and the like. The utility model can be used for heating CO in the flue gas of the furnace 2 Separated out, thereby reducing CO in the flue gas 2 Is discharged and simultaneously separated CO 2 Can be used as CO required for phenolate decomposition 2 Air source, surplus CO 2 Can be used for various purposes or geological storage.
Solves the problems that independent tar processing enterprises do not have direct supply of CO which meets the requirement of phenolate decomposition 2 Air source, surplus CO 2 Can be used for various purposes or geological storage. CO in flue gas 2 The recovery rate of (2) is more than or equal to 85 percent, and CO in the residual flue gas 2 The concentration can be as low as 50PPM. Recovery of CO 2 The purity is high, the concentration of the wet base after the primary recovery treatment reaches more than 98.5%, and the concentration can reach more than or equal to 99.99% after the secondary treatment. The carbon emission of the production process of independent coal tar processing enterprises can be remarkably reduced. The process flow is simple, the energy consumption is low, the operation is convenient, and the operation cost is low. And the independent system does not influence the operation of other devices.
The foregoing is only a preferred embodiment of the present utility model, but the scope of the present utility model is not limited thereto, and any person skilled in the art, who is within the scope of the present utility model, should make equivalent substitutions or modifications according to the technical scheme of the present utility model and the inventive concept thereof, and should be covered by the scope of the present utility model.
Claims (8)
1. The utility model provides a system for independent coal tar processing enterprise reduces carbon emission which characterized in that:
comprises a flue gas collecting system, a flue gas cooling system and CO 2 An absorption and desorption system;
the flue gas collection system comprises a first valve and a collection pipeline, the first valve is arranged on a heating furnace chimney, one end of the collection pipeline is connected with the chimney in front of the first valve, and the other end of the collection pipeline is connected with the lower part of a flue gas cooling tower of the flue gas cooling system;
the flue gas cooling system comprises a flue gas cooling tower and a cooling liquid heat exchanger, wherein the bottom of the flue gas cooling tower, the cooling liquid heat exchanger and the upper part of the flue gas cooling tower are connected through pipelines in sequence, and the top of the flue gas cooling tower is connected with CO 2 The lower pipeline of the absorption tower of the absorption and desorption system is connected;
the CO 2 The absorption and desorption system comprises an absorption tower, a regeneration tower, a flue gas-liquid separator and CO 2 Separator, CO 2 A water cooler, a lean-rich liquid heat exchanger, a lean liquid cooler and a regeneration tower reboiler;
the top of the absorption tower is connected with a flue gas-liquid separator pipeline; the bottom of the absorption tower, the lean-rich liquid heat exchanger and the upper part of the regeneration tower are connected through pipelines in turn; the bottom of the regeneration tower, the lean-rich liquid heat exchanger, the lean liquid cooler and the upper part of the absorption tower are connected through pipelines in sequence; the bottom of the regeneration tower, the reboiler of the regeneration tower and the lower part of the regeneration tower are connected through pipelines in turn; top of regeneration tower, CO 2 Water cooler, CO 2 The separators are connected in turn by pipelines.
2. The system for reducing carbon emissions of an independent coal tar processing enterprise of claim 1, wherein:
at least one heating furnace and a plurality of heating furnaces are connected in parallel through pipelines.
3. The system for reducing carbon emissions of an independent coal tar processing enterprise of claim 1, wherein:
the collecting pipeline is provided with a second valve.
4. The system for reducing carbon emissions of an independent coal tar processing enterprise of claim 3, wherein:
the second valve is a stop valve.
5. The system for reducing carbon emissions of an independent coal tar processing enterprise of claim 1, wherein:
the flue gas cooling tower is characterized by further comprising a cooling circulating pump, wherein the bottom of the flue gas cooling tower is connected with an inlet pipeline of the cooling circulating pump, and an outlet of the cooling circulating pump is connected with a pipeline of the cooling liquid heat exchanger.
6. The system for reducing carbon emissions of an independent coal tar processing enterprise of claim 1, wherein: the flue gas cooling tower is characterized by further comprising a flue gas fan, the top of the flue gas cooling tower is adjacent to the inlet pipeline of the flue gas fan, and the outlet of the flue gas fan is connected with the lower pipeline of the absorption tower.
7. The system for reducing carbon emissions of an independent coal tar processing enterprise of claim 1, wherein: the lean liquid pump is connected with the lean liquid cooler pipeline.
8. The system for reducing carbon emissions of an independent coal tar processing enterprise of claim 1, wherein: the device also comprises a rich liquid pump, wherein the bottom of the absorption tower is connected with a rich liquid pump inlet, and a rich liquid pump outlet is connected with a lean rich liquid heat exchanger.
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| CN202320684700.1U CN219580194U (en) | 2023-03-31 | 2023-03-31 | System for reducing carbon emission of independent coal tar processing enterprises |
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