Petroleum coke calcination flue gas waste heat utilization and denitration integrated equipment

Abstract

The utility model belongs to the field of waste heat utilization and purification of petroleum coke calcination flue gas in the aluminum carbon industry, and particularly relates to petroleum coke calcination flue gas waste heat utilization and denitration integrated equipment which comprises a steam generator, an SCR (Selective Catalytic Reduction) reactor, an economizer, a deaerator and a steam pocket, the steam generator is communicated with the SCR reactor through a 1 # communication flue, the SCR reactor is communicated with the economizer through a 2 # communication flue, the steam pocket is respectively communicated with the deaerator and the steam generator through pipelines, the deaerator is communicated with a liquid inlet of the economizer through a pipeline, and a liquid outlet of the economizer is communicated with a liquid inlet of the steam pocket through a pipeline; the steam pocket provides saturated steam and saturated water for the flue gas to enable the flue gas to be cooled for the second time, the cooled flue gas and ammonia gas are denitrated in the SCR reactor, then the flue gas enters the economizer, the flue gas is cooled through deoxygenated hot water provided in the deaerator, and finally the flue gas is discharged. Waste heat utilization and denitration of flue gas are integrated on one device, and the site space is efficiently utilized.

Description

TECHNICAL FIELD

[0001] The utility model belongs to the petroleum coke calcination flue gas's waste heat utilization and purification field of carbon industry for aluminum, specifically relates to a kind of petroleum coke calcination flue gas waste heat utilization and denitration integrated equipment. BACKGROUND

[0002] Petroleum coke calcined is the main raw material of aluminum anode, in our country, tank type calcining furnace is the preferred equipment of petroleum coke calcination.In recent years, the emission index requirement of kiln flue gas pollutants in various industries is strict, and the demand for high-temperature flue gas waste heat utilization is also increasing, and so is the petroleum coke calcination furnace flue gas.

[0003] Petroleum coke is calcined in tank type calcining furnace, and the high-temperature flue gas discharged after calcination is generally about 900℃, and the flue gas contains NOx, dust and SO2 and other atmospheric pollutants, among which the concentration of NOx is about 200mg / Nm 3 At present, the conventional waste heat utilization and denitration scheme of calcination flue gas is to set up a waste heat boiler system and an SCR denitration system.

[0004] Because the conventional waste heat utilization and denitration are independent systems, there are many equipment, the connection between equipment is complex, and many other factors, which leads to inefficient use of space, high cost of land use and engineering construction.In addition, the SCR reactor, the core equipment of the SCR denitration system, has special requirements for flue gas temperature, which generally requires the flue gas temperature to be controlled between 320℃ and 400℃.Once the temperature exceeds the control, the denitration efficiency will decrease sharply, and the environmental emission will exceed the standard, so the arrangement position of the SCR reactor needs to be closely matched with the waste heat boiler, which is also a technical difficulty. INVENTION CONTENTS

[0005] In view of the above technical difficulties, the utility model aims to provide a kind of petroleum coke calcination flue gas waste heat utilization and denitration integrated equipment, which integrates the waste heat utilization and denitration of flue gas in one equipment, so that the structure is simple, the efficiency is higher, and the technical economy of calcination flue gas waste heat utilization and denitration is better.

[0006] To achieve the above purpose, the utility model provides a kind of petroleum coke calcination flue gas waste heat utilization and denitration integrated equipment, which comprises a steam generator, a 1# communication flue, an SCR reactor, a 2# communication flue, a coal economizer, a deaerator and a steam drum.

[0007] The steam generator is connected with the SCR reactor through the 1# communication flue, the SCR reactor is connected with the coal economizer through the 2# communication flue, the steam drum is connected with the deaerator and the steam generator through pipelines, the deaerator is connected with an external water supply device, the deaerator is connected with the inlet of the coal economizer through a pipeline, and the outlet of the coal economizer is connected with the inlet of the steam drum through a pipeline.

[0008] The flow path of the high-temperature saturated water in the steam drum is: steam drum→steam generator→steam drum; and the state change of the high-temperature saturated water in the steam drum is: high-temperature saturated water→saturated steam.

[0009] The flow path of a part of the saturated steam in the steam drum is: steam drum→steam generator→discharge for external supply; and the state change of the part of the saturated steam in the steam drum is: saturated steam→high-temperature steam.

[0010] The flow path of another part of the saturated steam in the steam drum is: steam drum→deaerator→economizer→steam drum; and the state change of the another part of the saturated steam in the steam drum is: saturated steam→deoxygenated hot water→high-temperature water.

[0011] The flow path of the flue gas is: high-temperature flue gas→steam generator→1# connecting flue→SCR reactor→2# connecting flue→economizer→discharge.

[0012] The steam generator comprises a steam generator shell, a superheater heat exchange coil and an evaporator heat exchange coil, and the superheater heat exchange coil and the evaporator heat exchange coil are embedded in the steam generator shell.

[0013] The steam drum comprises a steam outlet I and a steam outlet II, the steam outlet II of the steam drum is connected with the deaerator through a pipeline, the steam outlet I of the steam drum is connected with the superheater heat exchange coil through a pipeline, a liquid outlet of the steam drum is connected with the evaporator heat exchange coil through a pipeline, and a gas outlet of the evaporator heat exchange coil is connected with a steam inlet of the steam drum through a pipeline.

[0014] The flow path of the high-temperature saturated water in the steam drum is: steam drum→evaporator heat exchange coil→steam drum; and the state change of the high-temperature saturated water in the steam drum is: high-temperature saturated water→saturated steam.

[0015] The flow path of a part of the saturated steam in the steam drum is: steam drum→superheater heat exchange coil→discharge for external supply, and the state change of the part of the saturated steam in the steam drum is: saturated steam→high-temperature steam.

[0016] The flow path of another part of the saturated steam in the steam drum is: steam drum→deaerator; and the state change of the another part of the saturated steam in the steam drum is: saturated steam→deoxygenated hot water.

[0017] The flow path of the flue gas is: high-temperature flue gas→superheater heat exchange coil→evaporator heat exchange coil→cooled flue gas.

[0018] The steam generator shell comprises, from outside to inside, a steel plate, a calcium silicate plate and refractory castable.

[0019] The temperature of the cooled flue gas in the steam generator is 320-400℃.

[0020] An ammonia gas nozzle is arranged on the 1# connecting flue.

[0021] The SCR reactor comprises an SCR reactor shell, an SCR catalyst, the SCR catalyst is arranged in the SCR reactor shell, and the SCR catalyst is a finished honeycomb catalyst module arranged in three layers.

[0022] The economizer comprises an economizer shell and an economizer heat exchange coil embedded in the economizer shell; the outlet of the deaerator communicates with the inlet of the economizer heat exchange coil through a pipeline, and a feed water pump is arranged on the pipeline; the outlet of the economizer heat exchange coil communicates with the inlet of the steam drum through a pipeline; the flow path of the deaerated hot water is: deaerator→economizer heat exchange coil→steam drum; and the state of the deaerated hot water changes from deaerated hot water to high-temperature water.

[0023] The flow path of the flue gas is: flue gas after the steam generator is cooled→1# communication flue→SCR reactor→2# communication flue→economizer heat exchange coil→discharge.

[0024] The steam drum and the deaerator are fixed on the top of the steel structure frame, and the feed water pump is located at the bottom of the steel structure frame.

[0025] The 1# communication flue and the 2# communication flue are steel pipes.

[0026] The bottom of the steam generator, the SCR reactor and the economizer is provided with a dust discharge port, and the particle dust is discharged from the dust discharge port.

[0027] Compared with the conventional technology, the utility model has the advantages that:

[0028] 1、The utility model discloses a compact structure, and the steam generator, SCR reactor, economizer, deaerator, steam drum, feed water pump and other dispersed equipment are gathered together, so that the site space is efficiently utilized, and the land utilization cost and engineering construction cost are remarkably reduced.

[0029] 2、The utility model provides the suitable flue gas temperature for the SCR reactor through scientific thermal analysis and calculation, and reasonably matches the flue gas temperature in each equipment, so that the denitration efficiency is maximized.

[0030] 3、The utility model adopts modular design, and the corresponding type of waste heat utilization and denitration integrated equipment is matched according to the production capacity of the tank type calcining furnace, so that the engineering construction period can be shortened, and higher time efficiency is obtained. BRIEF DESCRIPTION OF DRAWINGS

[0031] Figure 1 It is the structural schematic diagram of the utility model patent embodiment;

[0032] In the drawing, 1 is a steam generator, 2 is a 1# communication flue, 3 is an SCR reactor, 4 is a 2# communication flue, 5 is an economizer, 6 is a deaerator, 7 is a steam drum, 8 is a feed water pump, and 9 is a steel structure frame.

[0033] In the figure, 1.1, steam generator shell; 1.2, superheater heat exchange coil; 1.3, evaporator heat exchange coil;

[0034] In the figure, 3.1, SCR reactor shell; 3.2, SCR catalyst;

[0035] In the figure, 5.1, economizer shell; 5.2, economizer heat exchange coil;

[0036] In the figure, A, flue gas inlet; B, flue gas outlet; C, ash outlet. DETAILED DESCRIPTION

[0037] The utility model patent is further explained below in combination with the drawings and examples.

[0038] As Figure 1 shown, a petroleum coke calcination flue gas waste heat utilization and denitration integrated equipment, including steam generator 1, 1# communication flue 2, SCR reactor 3, 2# communication flue 4, economizer 5, deaerator 6, steam drum 7, steam generator 1 is communicated SCR reactor 3 through 1# communication flue 2, SCR reactor 3 is communicated economizer 5 through 2# communication flue 4, steam drum 7 is communicated with deaerator 6 and steam generator 1 through pipeline respectively, deaerator 6 is connected with external water supply device, deaerator 6 is communicated with the liquid inlet of economizer 5 through pipeline, and the liquid outlet of economizer 5 is communicated with the liquid inlet of steam drum 7 through pipeline;

[0039] The flow path of high-temperature saturated water in steam drum 7 is: steam drum 7→steam generator 1→steam drum 7;The state change of high-temperature saturated water in steam drum 7 is: high-temperature saturated water→saturated steam;

[0040] The flow path of a part of saturated steam in steam drum 7 is: steam drum 7→steam generator 1→discharge outside supply;The state change of a part of saturated steam in steam drum 7 is: saturated steam→high-temperature steam;

[0041] The flow path of another part of saturated steam in steam drum 7 is: steam drum 7→deaerator 6→economizer 5→steam drum 7;The state change of another part of saturated steam in steam drum 7 is: saturated steam→deoxygenated hot water→high-temperature water;

[0042] The flow path of flue gas is: high-temperature flue gas→steam generator 1→1# communication flue 2→SCR reactor 3→2# communication flue 4→economizer 5→discharge.

[0043] The specific heat exchange and denitration process is as follows: the upper part of the steam drum 7 is saturated steam, and the lower part is high-temperature saturated water. The high-temperature saturated water and part of the saturated steam in the steam drum 7 enter the steam generator 1, and are indirectly counter-flow exchanged with the high-temperature flue gas entering from the flue gas inlet A, so that the high-temperature flue gas is cooled, the saturated steam after heat exchange becomes high-temperature steam and is discharged for external supply, and the high-temperature saturated water after heat exchange becomes saturated steam and enters the steam drum 7; part of the saturated steam in the steam drum 7 enters the deaerator 6 and is mixed with the deaerated water supplied into the deaerator 6 by the external water supply device, so that the deaerated hot water is formed in the deaerator 6; the flue gas after heat exchange and cooling in the steam generator 1 enters the SCR reactor 3 through the 1# connecting flue 2, in the process, the ammonia gas channel on the 1# connecting flue 2 is connected to the ammonia gas, the ammonia gas and the NOx in the flue gas react in the SCR reactor 3, the flue gas after reaction enters the economizer 5 through the 2# connecting flue 4, the deaerated hot water in the deaerator 6 enters the economizer 5 through the liquid inlet of the economizer 5 and is indirectly counter-flow exchanged with the flue gas after reaction, the flue gas after heat exchange is discharged from the flue gas outlet B, and the deaerated hot water after heat exchange becomes high-temperature water and enters the steam drum 7 through the liquid outlet of the economizer 5 and the liquid inlet of the steam drum 7; the bottom of the steam generator 1, the SCR reactor 3 and the economizer 5 are respectively provided with the ash discharge port C, and the particles and dust carried by the flue gas are respectively discharged from the ash discharge ports C at the bottom of the steam generator 1, the SCR reactor 3 and the economizer 5.

[0044] After the high-temperature flue gas enters the steam generator 1, the saturated steam and the high-temperature saturated water provided by the steam drum 7 are used to cool the flue gas twice, so that the flue gas reaches the suitable temperature for denitration reaction, at the same time, the saturated steam is heated to become high-temperature steam for external supply, and the high-temperature saturated water becomes saturated steam and returns to the steam drum 7, so that the steam is supplemented; the flue gas after cooling in the steam generator 1 enters the SCR reactor 3 through the 1# connecting flue 2, the ammonia gas channel is arranged on the 1# connecting flue 2, the ammonia gas is mixed with the flue gas in the 1# connecting flue 2, so that they are fully contacted, and the reaction is carried out under the action of the catalyst in the SCR reactor 3, so that the denitration is carried out, then the flue gas enters the economizer 5, the deaerated hot water is provided for the economizer 5 by the deaerator 6, the deaerated hot water cools the flue gas, the flue gas after cooling is discharged, the deaerated hot water becomes high-temperature water and enters the steam drum 7, so that the water is recycled.

[0045] The steam generator 1 comprises a steam generator shell 1.1, a superheater heat exchange coil 1.2 and an evaporator heat exchange coil 1.3, the superheater heat exchange coil 1.2 and the evaporator heat exchange coil 1.3 are embedded in the steam generator shell 1.1, the steam generator shell 1.1 comprises, from outside to inside, a steel plate, a calcium silicate plate and a refractory castable, the upper part of the steam drum 7 is saturated steam, and the lower part is high-temperature saturated water, the saturated water enters the evaporator heat exchange coil 1.3 to recover the waste heat of flue gas, and then changes into saturated steam to return to the steam drum 7, the saturated steam drawn out of the steam drum 7 enters the superheater heat exchange coil 1.2 and the deaerator 6 respectively, the saturated steam enters the superheater heat exchange coil 1.2 to recover the waste heat of flue gas, and the superheater heat exchange coil 1.2 is used for heating the saturated steam in the pipe into hot steam, and the evaporator heat exchange coil is used for heating the saturated water in the pipe into saturated steam.

[0046] The steam drum 7 comprises a steam outlet I and a steam outlet II, the steam outlet II of the steam drum 7 is connected with the deaerator 6 through a pipeline, the steam outlet I of the steam drum 7 is connected with the superheater heat exchange coil 1.2 through a pipeline, and the liquid outlet of the steam drum 7 is connected with the evaporator heat exchange coil 1.3 through a pipeline, and the gas outlet of the evaporator heat exchange coil 1.3 is connected with the steam inlet of the steam drum 7 through a pipeline.

[0047] The flow path of the high-temperature saturated water in the steam drum 7 is: the steam drum 7→the evaporator heat exchange coil 1.3→the steam drum 7, and the state change of the high-temperature saturated water in the steam drum 7 is: high-temperature saturated water→saturated steam.

[0048] The flow path of a part of the saturated steam in the steam drum 7 is: the steam drum 7→the superheater heat exchange coil 1.2→being discharged for external supply, and the state change of the part of the saturated steam in the steam drum 7 is: saturated steam→high-temperature steam.

[0049] The flow path of another part of the saturated steam in the steam drum 7 is: the steam drum 7→the deaerator 6, and the state change of the another part of the saturated steam in the steam drum 7 is: saturated steam→deaerated hot water.

[0050] The flow path of the flue gas is: high-temperature flue gas→the superheater heat exchange coil 1.2→the evaporator heat exchange coil 1.3→the flue gas after being cooled.

[0051] The specific heat exchange process is as follows: a part of the saturated steam in the steam drum 7 enters the superheater heat exchange coil 1.2 through the steam outlet I to perform the first indirect counterflow heat exchange in the steam generator 1, the high-temperature steam after the first indirect counterflow heat exchange is externally supplied; the high-temperature saturated water in the steam drum 7 enters the evaporator heat exchange coil 1.3 through the liquid outlet to perform the second indirect counterflow heat exchange in the steam generator 1, the saturated steam after the second indirect counterflow heat exchange enters the steam drum 7 through the steam inlet, and the temperature of the flue gas after the second indirect counterflow heat exchange in the steam generator 1 is 320-400 ℃.

[0052] The SCR reactor 3 comprises an SCR reactor shell 3.1, and an SCR catalyst 3.2 arranged in the SCR reactor shell 3.1, wherein the SCR reactor shell 3.1 is a carbon steel shell, and the SCR catalyst 3.2 is a finished honeycomb catalyst module arranged in three layers; the 1# communicating flue is provided with an ammonia gas nozzle, ammonia gas is introduced into the ammonia gas nozzle in the 1# communicating flue 2, and the ammonia gas and the flue gas are fully mixed in the 1# communicating flue 2; the flue gas after being cooled in the steam generator 1 flows downward through the SCR catalyst 3.2, and the ammonia gas reacts with the NOx in the flue gas under the catalysis of the SCR catalyst 3.2, so that most of the NOx is removed, and the NOx in the flue gas meets the environmental protection emission standard.

[0053] The economizer 5 comprises an economizer shell 5.1 and an economizer heat exchange coil 5.2, wherein the economizer shell 5.1 is a carbon steel shell, and the economizer heat exchange coil 5.2 is embedded in the economizer shell 5.1; the economizer heat exchange coil 5.2 is used for recovering flue gas waste heat, and the deaerated hot water in the pipe is changed into high-temperature water and recovered into the steam drum 7; the outlet of the deaerator 6 is communicated with the inlet of the economizer heat exchange coil 5.2 through a pipeline, and a feed water pump 8 is arranged on the pipeline; the feed water pump 8 is a high-temperature resistant centrifugal pump; the outlet of the economizer heat exchange coil 5.2 is communicated with the inlet of the steam drum 7 through a pipeline; the flow path of the deaerated hot water is: the deaerator 6→the economizer heat exchange coil 5.2→the steam drum 7; the state of the deaerated hot water changes from deaerated hot water to high-temperature water; and the flow path of the flue gas is: the flue gas after being cooled in the steam generator 1→the 1# communicating flue 2→the SCR reactor 3→the 2# communicating flue 4→the economizer heat exchange coil 5.2→discharge.

[0054] The deaerated water at about 40℃ in the external water supplement device is supplemented into the deaerator 6, part of the saturated steam in the steam drum 7 is mixed with the deaerated water in the deaerator 6 to form deaerated hot water at 104℃; the deaerated hot water is pressurized by the feed water pump 8 and then enters the economizer heat exchange coil 5.2 of the economizer 5; the deaerated hot water in the deaerator 6 is indirectly countercurrently exchanged with the flue gas in the economizer shell 5.1; the exchanged flue gas is discharged from the flue gas outlet B of the economizer 5; and the exchanged deaerated hot water changes into high-temperature water and enters the steam drum 7.

[0055] The steam drum 7 and the deaerator 6 are fixed on the top of the steel structure frame 9, and the feed water pump 8 is located at the bottom of the steel structure frame 9.

[0056] In the embodiment, the 1# communicating flue 2 and the 2# communicating flue 4 are steel pipes welded by steel plates.

[0057] The process flow of the utility model discloses: high-temperature calcination flue gas enters steam generator 1, and in turn flows through heat exchanger heat coil 1.2 and evaporator heat coil 1.3 to recover flue gas waste heat, and the flue gas after cooling is mixed with ammonia gas in 1# communication flue 2, then enters SCR reactor 3, and the denitration reaction is completed under the catalysis of SCR catalyst, and the flue gas after denitration enters economizer 5 through 2# communication flue 4, and is discharged after further recovering flue gas waste heat;Low-temperature deoxidized water and saturated steam are mixed and heated to deoxidize in deoxidizer 6, then are pressurized by feed water pump 8 and sent into economizer 5, and after heat exchange and heating, enter steam drum 7, and the saturated water in the lower part of steam drum 7 enters evaporator heat coil 1.3 to recover flue gas waste heat and change into saturated steam returning to steam drum 7, and the saturated steam in the upper part of steam drum 7 enters superheater heat coil 1.2 to recover flue gas waste heat and upgrade to superheated steam for external supply.

[0058] The working principle of the utility model "a petroleum coke calcination flue gas waste heat utilization and denitration integrated equipment" is as follows:

[0059] Flue gas system: high-temperature flue gas (900 DEG C) discharged from the tank-type calcining furnace enters steam generator 1 from flue gas inlet A, and in steam generator 1, flue gas flows through heat exchanger heat coil 1.2 and evaporator heat coil 1.3 in turn, and carries out countercurrent indirect heat exchange with saturated steam and high-temperature saturated water in the coil respectively, then the flue gas temperature is reduced to about 350 DEG C, and then the flue gas flows through 1# communication flue 2 and mixes with external ammonia gas, then enters SCR reactor 3, and under the catalysis of SCR catalyst 3.2, ammonia gas and NOx in flue gas fully react, and most of NOx is removed, so that the NOx in flue gas meets the environmental protection emission standard, then the flue gas reaches economizer 5 through 2# communication flue 4, and the flue gas and economizer heat exchange coil 5.2 further carry out countercurrent indirect heat exchange, and the flue gas temperature is reduced to about 180 DEG C, and then the flue gas is discharged from flue gas outlet B;Large-particle dust in the flue gas deposits at the bottom of steam generator 1, SCR reactor 3 and economizer 5, and is discharged from dust outlet C.

[0060] Water-steam system: 40 DEG C or so deoxidized water is supplemented into deoxidizer 6, and a part of saturated steam discharged from steam drum 7 is mixed and deoxidized in deoxidizer 6, and is made into 104 DEG C deoxidized hot water, then is pressurized by feed water pump 8 and enters economizer 5, carries out countercurrent indirect heat exchange with flue gas through economizer heat exchange coil 5.2, enters steam drum 7 after temperature rising, the upper part of steam drum 7 is saturated steam, and the lower part is high-temperature saturated water, then saturated water enters evaporator heat coil 1.3 and carries out countercurrent indirect heat exchange with flue gas, and changes into saturated steam returning to steam drum 7, and the saturated steam led out from steam drum 7 enters superheater heat coil 1.2 and carries out countercurrent indirect heat exchange with flue gas and changes into superheated steam for external supply.

Claims

1. A petroleum coke calcination flue gas waste heat utilization and denitration integrated device, characterized in that, The steam generator, the 1# communication flue, the SCR reactor, the 2# communication flue, the coal economizer, the deaerator and the steam drum are included. The steam generator is connected with the SCR reactor through the 1# communication flue, the SCR reactor is connected with the coal economizer through the 2# communication flue, the steam drum is connected with the deaerator and the steam generator through pipelines, the deaerator is connected with the external water supply device, the deaerator is connected with the liquid inlet of the coal economizer through a pipeline, and the liquid outlet of the coal economizer is connected with the liquid inlet of the steam drum through a pipeline. The circulation path of the high-temperature saturated water in the steam drum is steam drum→steam generator→steam drum, and the state change of the high-temperature saturated water in the steam drum is high-temperature saturated water→saturated steam. The circulation path of a part of the saturated steam in the steam drum is steam drum→steam generator→discharge, and the state change of the saturated steam in the steam drum is saturated steam→high-temperature steam. The circulation path of another part of the saturated steam in the steam drum is steam drum→deaerator→coal economizer→steam drum, and the state change of the saturated steam in the steam drum is saturated steam→deoxygenated hot water→high-temperature water. The circulation path of the flue gas is high-temperature flue gas→steam generator→1# communication flue→SCR reactor→2# communication flue→coal economizer→discharge.

2. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 1, characterized in that, The steam generator comprises a steam generator shell, a superheater heat exchange coil and an evaporator heat exchange coil, and the superheater heat exchange coil and the evaporator heat exchange coil are embedded in the steam generator shell. The steam drum comprises a steam outlet I and a steam outlet II, the steam outlet II of the steam drum is connected with the deaerator through a pipeline, the steam outlet I of the steam drum is connected with the superheater heat exchange coil through a pipeline, the liquid outlet of the steam drum is connected with the evaporator heat exchange coil through a pipeline, and the gas outlet of the evaporator heat exchange coil is connected with the steam inlet of the steam drum through a pipeline. The circulation path of the high-temperature saturated water in the steam drum is steam drum→evaporator heat exchange coil→steam drum, and the state change of the high-temperature saturated water in the steam drum is high-temperature saturated water→saturated steam. The circulation path of a part of the saturated steam in the steam drum is steam drum→superheater heat exchange coil→discharge, and the state change of the saturated steam in the steam drum is saturated steam→high-temperature steam. The circulation path of another part of the saturated steam in the steam drum is steam drum→deaerator, and the state change of the saturated steam in the steam drum is saturated steam→deoxygenated hot water. The circulation path of the flue gas is high-temperature flue gas→superheater heat exchange coil→evaporator heat exchange coil→cooled flue gas.

3. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 2, characterized in that, The steam generator shell comprises a steel plate, a calcium silicate plate and refractory castable from outside to inside.

4. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 2, characterized in that, The temperature of the cooled flue gas in the steam generator is 320-400 DEG C.

5. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 1, characterized in that, An ammonia nozzle is arranged on the 1# communication flue.

6. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 1, characterized in that, The SCR reactor comprises an SCR reactor shell and an SCR catalyst, the SCR catalyst is arranged in the SCR reactor shell, the SCR catalyst is a finished honeycomb catalyst module, and the SCR catalyst is arranged in three layers.

7. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 1, characterized in that, The coal economizer comprises a coal economizer shell and a coal economizer heat exchange coil, the coal economizer heat exchange coil is embedded in the coal economizer shell, the liquid outlet of the deaerator is connected with the liquid inlet of the coal economizer heat exchange coil through a pipeline, a feed water pump is arranged on the pipeline, and the liquid outlet of the coal economizer heat exchange coil is connected with the liquid inlet of the steam drum through a pipeline. The flow path of the deoxygenated hot water is: deoxygenator→ coal economizer heat exchange coil→ steam drum; the state of the deoxygenated hot water changes as: deoxygenated hot water→ high-temperature water; The flow path of the flue gas is: flue gas after steam generator cooling→ 1# connecting flue→ SCR reactor→ 2# connecting flue→ coal economizer heat exchange coil→ discharge.

8. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 7, characterized in that, The steam drum and the deoxygenator are fixed on the top of the steel structure frame, and the feed water pump is located at the bottom of the steel structure frame.

9. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 1, characterized in that, The 1# connecting flue and the 2# connecting flue are steel pipes.

10. The petroleum coke calcination flue gas waste heat utilization and denitration integrated device according to claim 1, characterized in that, The bottom of the steam generator, the SCR reactor and the coal economizer is provided with an ash discharge port, and the granular dust is discharged from the ash discharge port.

Images