Carbon dioxide emission reduction and utilization process and device based on dry quenching process

Abstract

The application discloses a kind of carbon dioxide emission reduction utilization process and device based on dry quenching process, belong to coking and carbon emission reduction technical field.The device includes coke receiving tank, reduction reactor, dry quenching furnace, high-temperature dust collector, waste heat boiler, steam turbine, cyclone separator, CO separation device;The application sets reduction reactor, utilizes red coke heat, and CO2 reduction reaction is converted into CO, and is converted into fuel oil or methanol or olefin etc. High-value chemicals by synthesis gas conversion device with H2, realizes that coking CO2 is efficiently controllable conversion and utilization;It is provided with gas collecting hood and nitrogen replacement process, ensures that air does not permeate reduction reactor and reaction product CO in the process of loading coke, eliminates coke burning loss, eliminates explosion risk, realizes the safe and stable operation of whole process.

Description

TECHNICAL FIELD

[0001] The present application relates to a carbon dioxide emission reduction and utilization process and device based on a dry quenching process, in particular to a dry quenching process and device with a reduction reactor using CO2 as a reaction gas and a heat carrier, belonging to the technical field of coking and carbon emission reduction. BACKGROUND

[0002] China's coking industry has huge production capacity, with an annual output of over 400 million tons. Although the carbon emission intensity of the coking industry is relatively low, the total carbon emission is still very large due to the huge production of coke. In 2023, the national coke production reached 492 million tons, and the carbon dioxide emission was nearly 200 million tons. In addition, compared with the power, steel and other key industries for emission reduction, the coking industry has unclear emission reduction path, lacks emission reduction technology, and has low carbon emission concentration, all of which directly lead to the unclear prospect of emission reduction in the coking industry.

[0003] In the coking industry, in addition to the flue gas of the coke oven combustion chamber, the dry quenching process also emits a large amount of carbon dioxide. Due to the particularity of the coke oven out-of-furnace method, the current dry quenching device can only use intermittent coke feeding. However, when the coke is fed into the dry quenching oven, there is no replacement of the oven, no sealing or air extraction around the dry quenching oven hopper, or other operations. Air will enter the dry quenching oven along with the hot red coke. When the air stays in the dry quenching oven pre-storage section, it will undergo semi-oxidation or combustion reaction with the red coke, not only burning the coke, but also producing carbon dioxide and carbon monoxide. Carbon monoxide will gradually accumulate in the dry quenching oven and the circulating gas, causing the risk of explosion or deflagration.

[0004] Chinese patent CN 114790396 A discloses "a high-efficiency emission reduction dry quenching method and a system for producing carbon monoxide". The patent uses carbon dioxide gas and carbon dioxide-rich gas as the inlet gas of the dry quenching circulating gas flow. While the dry quenching circulating gas flow exchanges heat with the red coke, the carbon dioxide reacts with the high-temperature red coke to produce carbon monoxide. The main unit devices include a dry quenching oven, a coke feeding device, a coke discharging device, a primary dust collector, a waste heat boiler, a secondary dust collector, a circulating gas flow fan, a waste heat boiler feedwater preheater, and an optional coke powder gasification unit. The coke feeding device of the patent is directly connected to the dry quenching oven, and the coke feeding method is still intermittent. In addition, CO2 is used as the circulating gas, and air may enter the dry quenching oven during the coke feeding process. The oxygen in the air will undergo incomplete oxidation with the red coke to produce carbon monoxide, which will accumulate in the space above the dry quenching oven. In the presence of red coke flames, deflagration and explosion are likely to occur. In addition, if air is mixed into the circulating gas, combustion or explosion may occur in the dry quenching oven or the pipeline.

[0005] Chinese patent CN118978927 A discloses a system and method for reducing coke burn loss in dry quenching coke oven, which includes dry quenching coke oven, primary dust collector, waste heat boiler, secondary dust collector and circulating fan. The method reduces the carbon dioxide content of the inlet gas of the dry quenching coke oven to reduce the carbon dissolution reaction between carbon dioxide and coke in the cooling section, effectively reducing the coke burn loss rate and pollution. The main reason for the occurrence of coke dissolution loss reaction is that air enters the dry quenching coke oven with coke during charging, producing CO through incomplete oxidation or producing CO2 through combustion. This method still cannot change the production mode of intermittent addition of red coke, so it cannot eliminate the air brought in during charging, and therefore cannot truly and substantially reduce carbon dissolution loss.

[0006] The above prior art cannot avoid air leakage during intermittent charging of dry quenching coke, O2 in the air mixes with the circulating gas, and coke burn loss or semi-oxidation of CO occurs, which gradually accumulates CO and O2 in the space above the hopper or in the dry quenching oven, causing explosion or combustion risk and other problems. SUMMARY

[0007] To achieve CO2 emission reduction and utilization in coking, solve the coke burn loss caused by air leakage during intermittent charging of dry quenching coke, and the resulting explosion risk, the present application provides a CO2 emission reduction and utilization process and device based on the dry quenching process, in particular a dry quenching and CO2 utilization process using CO2 as reaction gas and heat carrier and containing a reduction reactor.

[0008] Due to the intermittent operation characteristics of the coking process, dry quenching coke is added intermittently, but air easily leaks into the dry quenching oven during coke charging. Although the dry quenching oven is divided into a pre-storage section and a cooling section, which are relatively separated, air may not enter the cooling section. However, since the temperature of red coke is relatively high (900-1050℃) at this time, air quickly reacts with red coke through oxidation or semi-oxidation to generate CO and CO2. If CO gradually accumulates in the circulating cooling gas and the concentration reaches the explosion limit, there is a risk of deflagration or explosion. Based on the technical goal of eliminating the risk of CO production and utilizing high-temperature red coke to convert CO2 under the condition of intermittent coke charging in dry quenching, the present application separately provides a reduction reactor, so that high-temperature red coke and CO2 react in the reduction reactor to generate CO, and CO is separated from the circulating gas, realizing controllable synthesis of CO and conversion and utilization of CO2. In addition, inert gas replacement is provided before and during coke charging, completely avoiding air infiltration. In addition, when the temperature of coke in the reduction reactor is reduced to below 700℃, CO2 is used for cooling in the dry quenching oven. Since the temperature is below 700℃, CO2 does not react with coke, thus eliminating the risk of CO production and explosion.

[0009] The application provides a carbon dioxide emission reduction and utilization process based on a dry quenching process, comprising the following steps:

[0010] (1) 1000-1050℃ red-hot red coke transported by a coke oven car is loaded into a coke receiving tank, and the coke receiving tank loaded with the red coke is hoisted above a reduction reactor; nitrogen is introduced from below a reduction reactor hopper for 0.5 hours, and then the nitrogen is continuously introduced, the top gate valve of the reduction reactor, the bottom valve of the coke receiving tank and the A valve of the top outlet of the dry quenching furnace are opened in sequence, the red coke falls into the reduction reactor under the action of gravity, and the CO2 valve at the bottom of the dry quenching furnace is opened, CO2 is introduced into the dry quenching furnace, the air in the dry quenching furnace is replaced, the exhaust pump is opened, and the air in the dry quenching furnace and the dust and air above the reduction reactor hopper and the exhaust gas are introduced out through a gas hood, are dusted through a cyclone separator A, and then the gas is discharged to an exhaust gas treatment system for further treatment.

[0011] (2) after all the red coke is loaded into the reduction reactor, the nitrogen introduction from below the reduction reactor hopper is stopped, the top gate valve of the reduction reactor is closed, the A valve is opened, the C valve and the D valve of the CO separation device inlet and outlet are opened, the circulating CO2 and the supplementary CO2 are introduced into a CO2 preheater through a pipeline, are heat-exchanged with high-temperature gas after dust removal through a high-temperature dust remover, are introduced into the reduction reactor from the bottom of the reduction reactor, and are reacted with the red coke to generate CO, the reaction gas is introduced into the high-temperature dust remover through the A valve pipeline from the top outlet of the reduction reactor, is dusted at high temperature, is preheated after mixing with CO2, and is sent to a waste heat boiler to recover heat and drive a steam turbine to generate power.

[0012] (3) the cooled reaction gas (140-180℃) from the waste heat boiler is dusted through a cyclone separator B, is sent to a CO separation device, and the separated CO is sent to a gas tank for storage; the separated circulating CO2 and supplementary CO2 of the CO separation device are heated through a CO2 preheater and are sent into the reduction reactor for reaction; the temperature of the coke after reaction in the reduction reactor is reduced to 800℃, the A valve, the C valve and the D valve are closed, the B valve is opened, the bottom valve of the reduction reactor is opened, the 800℃ coke falls into the dry quenching furnace, CO2 is introduced from the bottom of the dry quenching furnace, is heat-exchanged with the coke in the furnace in a reverse direction, the heat-exchanged hot CO2 is introduced into the high-temperature dust remover from the top outlet of the dry quenching furnace, is dusted at high temperature, is sent to the waste heat boiler to recover heat and drive the steam turbine to generate power, and the cold CO2 (140-180℃) cooled through the waste heat boiler is sent into the cyclone separator B for secondary dust removal and is returned to the bottom of the dry quenching furnace to continue cooling the coke; the coke is cooled to below 200℃, the bottom valve of the dry quenching furnace is opened, the coke is discharged and is transported to a coke storage.

[0013] Further, the CO2 volume space velocity at the bottom of the reduction reactor is 40-200 / h, and the supplementary CO2 is obtained from CO2 with a purity higher than 99% separated from coke oven flue gas.

[0014] Further, the CO separation device is a pressure swing adsorption device or an organic amine solution absorption device. The unreacted CO2 after gas separation or the recycled CO2 has a purity higher than 99%.

[0015] Further, the CO sent to the gas tank in step (3) is mixed with H2 produced by the hydrogen production device in a certain proportion, and then sent to the syngas conversion device to produce fuel oil, olefin or methanol. Further, the volume ratio of CO / H2 is 1:1.5~1:3.

[0016] Further, in step (1), the nitrogen gas volume space velocity during displacement is 1.5~2 / h.

[0017] Further, in step (2), the volume ratio of recycled CO2 to supplementary CO2 is 1:25~3:1.

[0018] Further, in step (3), the CO2 volume space velocity introduced from the bottom of the dry quenching furnace is 1200~1350 / h.

[0019] The application provides a carbon dioxide emission reduction and utilization device based on a dry quenching process, which comprises a coke receiving tank, a reduction reactor, a dry quenching furnace, a high-temperature dust remover, a waste heat boiler, a steam turbine, a cyclone separator and a CO separation device.

[0020] The top and bottom of the focusing tank are provided with gate valves, the reduction reactor is arranged between the focusing tank and the dry quenching furnace, a nitrogen inlet is arranged below the hopper of the reduction reactor, a gas collecting hood is arranged above the hopper, and the gas collecting hood is used for collecting dust and air / waste gas above the hopper; the top of the reduction reactor is provided with a gate valve and a gas outlet, the bottom is provided with a gas distributor and a CO2 inlet, the CO2 inlet is connected with the pipe passage outlet of the CO2 preheater, the pipe passage inlet of the CO2 preheater is connected with the CO2 outlet of the CO separation device; the shell passage inlet and outlet of the CO2 preheater are connected with the high-temperature dust remover and the waste heat boiler respectively, and are used for preheating CO2 in the pipe passage; the steam outlet of the waste heat boiler is connected with the steam turbine, the gas outlet is connected with the cyclone separator B, the gas outlet of the cyclone separator B is connected with the inlet of the circulating gas pump and the inlet of the CO separation device respectively; a B valve is arranged on the connecting pipeline between the cyclone separator B and the circulating gas pump, and a C valve is arranged on the connecting pipeline between the cyclone separator B and the CO separation device; the CO separation device is provided with a CO outlet at the top, and the CO outlet is connected with a gas tank for storing CO; the CO2 outlet arranged at the bottom of the CO separation device is connected with the inlet of the CO2 preheater; a D valve is arranged on the connecting pipeline between the CO separation device and the CO2 preheater, the pipeline between the outlet of the D valve and the inlet of the CO2 preheater is combined with a supplementary CO2 pipeline, and the CO2 preheater is connected; a valve is arranged at the connecting position between the dry quenching furnace and the bottom of the reduction reactor, the top of the dry quenching furnace is provided with a gas outlet connected with the gas inlet of the high-temperature dust remover; the outlet pipeline of the dry quenching furnace and the outlet pipeline of the reduction reactor are connected with the exhaust pump and the cyclone separator A; the bottom of the dry quenching furnace is provided with a coke discharge port, a gas distributor and a CO2 gas inlet, and the CO2 gas inlet is connected with the outlet of the circulating gas pump.

[0021] Further, the A valve and the connecting pipeline are arranged between the outlet pipeline of the dry quenching furnace and the outlet pipeline of the reduction reactor; when the replacement gas is used, the exhaust pump and the A valve are opened, and the gas in the dry quenching furnace is discharged by the exhaust pump; when the reaction is carried out, the exhaust pump is closed, and the A valve is opened, and the gas after the reaction is led to the high-temperature dust remover.

[0022] Further, the above-mentioned carbon dioxide emission reduction and utilization device based on the dry quenching process further comprises a synthesis gas conversion device and a hydrogen extraction device, the CO outlet arranged at the top of the CO separation device is connected with the inlet of the synthesis gas conversion device, and the connecting pipeline is connected with the H2 outlet of the hydrogen extraction device.

[0023] Further, the hydrogen extraction device is a photovoltaic water electrolysis hydrogen device or a coke oven gas hydrogen extraction device, and the synthesis gas conversion device is a fixed bed / slurry bed Fischer-Tropsch synthesis device, a fixed bed methanol synthesis device or a fixed bed olefin synthesis device.

[0024] The beneficial effects of the present application are as follows:

[0025] The application is provided with a reduction reactor, CO2 is converted into CO by reduction reaction using red coke heat, and is converted into fuel oil or methanol or olefin and other high-value chemicals by a synthesis gas conversion device with H2, realizing efficient and controllable conversion and utilization of coking CO2; the gas collecting hood and nitrogen replacement process are provided to ensure that air does not penetrate into the reduction reactor and reaction product CO during the coke loading process, eliminate coke burning loss, eliminate explosion risk, and realize safe and stable operation of the whole process. BRIEF DESCRIPTION OF DRAWINGS

[0026] Figure 1 is a process flow diagram of the carbon dioxide emission reduction and utilization process based on the dry quenching process of the application;

[0027] In the figure: 1-coke receiving tank; 2-reduction reactor; 3-dry quenching furnace; 4-gas distributor; 5-exhaust pump; 6-cyclone separator A; 7-high-temperature dust collector; 8-waste heat boiler; 9-turbine; 10-steam turbine; 11-cyclone separator B; 12-CO separation device; 13-circulating gas pump; 14-synthesis gas conversion device; 15-CO2 preheater; 16-hydrogen extraction device. DETAILED DESCRIPTION

[0028] The application will be further illustrated by the following examples, but is not limited to the following examples.

[0029] As shown in Figure 1 A carbon dioxide emission reduction and utilization device based on the dry quenching process, including a coke receiving tank 1, a reduction reactor 2, a dry quenching furnace 3, a high-temperature dust collector 7, a waste heat boiler 8, a steam turbine 10, a cyclone separator, a CO separation device 12;

[0030] The top and bottom of the focusing tank are provided with gate valves, the reduction reactor 2 is arranged between the focusing tank 1 and the dry quenching furnace 3, a nitrogen inlet is arranged below the hopper of the reduction reactor 2, and a gas collecting hood is arranged above the hopper, which is used to collect dust and air or waste gas above the hopper; the top of the reduction reactor 2 is provided with a gate valve and a gas outlet, and the bottom is provided with a gas distributor and a CO2 inlet, the CO2 inlet is connected with the pipe passage outlet of the CO2 preheater 15, the pipe passage inlet of the CO2 preheater 15 is connected with the CO2 outlet of the CO separation device 12; the shell passage inlet and outlet of the CO2 preheater 15 are connected with the high-temperature dust collector 7 and the waste heat boiler 8 respectively, which are used to preheat CO2 in the pipe passage; the steam outlet of the waste heat boiler is connected with the steam turbine 10, and the gas outlet is connected with the cyclone separator B11, the gas outlet of the cyclone separator B11 is connected with the inlet of the circulating gas pump 13 and the inlet of the CO separation device 12 respectively; a B valve is arranged on the connecting pipeline between the cyclone separator B11 and the circulating gas pump 13, and a C valve is arranged on the connecting pipeline between the cyclone separator B11 and the CO separation device 12; the top of the CO separation device 12 is provided with a CO outlet connected with a gas tank, which is used to store CO; the CO2 outlet arranged at the bottom of the CO separation device 12 is connected with the inlet of the CO2 preheater 15; a D valve is arranged on the connecting pipeline between the CO separation device 12 and the CO2 preheater 15, the pipeline between the outlet of the D valve and the inlet of the CO2 preheater 15 is combined with a supplementary CO2 pipeline, and the two pipelines are connected with the CO2 preheater 15 together; a valve is arranged at the connection between the dry quenching furnace 3 and the bottom of the reduction reactor 2, the top of the dry quenching furnace 3 is provided with a gas outlet connected with the gas inlet of the high-temperature dust collector 7; the outlet pipeline of the dry quenching furnace 3 and the outlet pipeline of the reduction reactor 2 are connected with the exhaust pump 5 and the cyclone separator A6; the bottom of the dry quenching furnace 3 is provided with a coke discharge port, a gas distributor 4 and a CO2 gas inlet, and the CO2 gas inlet is connected with the outlet of the circulating gas pump 13.

[0031] Further, an A valve and a connecting pipeline are arranged between the outlet pipeline of the dry quenching furnace 3 and the outlet pipeline of the reduction reactor 2; when the displacement gas is used, the exhaust pump 5 and the A valve are opened to discharge the gas in the dry quenching furnace 3; when the reaction is carried out, the exhaust pump 5 is closed and the A valve is opened to pass the reaction gas in the reduction reactor 2 to the high-temperature dust collector 7.

[0032] Further, the above-mentioned carbon dioxide emission reduction and utilization device based on the dry quenching process further comprises a synthesis gas conversion device 14 and a hydrogen extraction device 16, the CO outlet arranged at the top of the CO separation device 12 is connected with the inlet of the synthesis gas conversion device 14 (see the dashed part in Figure 1 Fig. 2), and the connecting pipeline between the two is connected with the H2 outlet of the hydrogen extraction device 16.

[0033] Further, the hydrogen extraction device 16 is a photovoltaic electrolysis water hydrogen production device or a coke oven gas hydrogen extraction device, and the synthesis gas conversion device 14 is one of a fixed bed / slurry bed Fischer-Tropsch synthesis device, a fixed bed methanol synthesis device or a fixed bed olefin synthesis device. Example 1

[0034] 13 tons (10 cubic meters) of 1000℃~1050℃ incandescent red-hot coke, loaded into coke receiving tank 1, is transported by coke oven discharge car to the side of dry quenching furnace 3. Coke receiving tank 1, filled with red-hot coke, is then hoisted above reduction reactor 2. Nitrogen gas is introduced from below the hopper of reduction reactor 2 at a flow rate of 20 m³ / h. 3 At a rate of / h, purging is performed for 0.5 hours, followed by continued nitrogen flow. The top gate valve of reduction reactor 2, the bottom valve of coke inlet 1, and valve A are opened sequentially. Under gravity, the red-hot coke falls into reduction reactor 2. Simultaneously, the bottom CO2 valve of dry quenching furnace 3 is opened, allowing CO2 to be introduced into dry quenching furnace 3 at a flow rate of 50 m³ / h. 3 At / h, the air inside the furnace is replaced, and exhaust pump 5 is turned on. The air inside the dry quenching furnace 3, as well as the dust, air, and exhaust gas above the hopper of reduction reactor 2, are collected through the gas collection hood, led out by exhaust pump 5, and then discharged after dust removal by cyclone separator A 6 and sent for exhaust gas treatment. After all the red coke is loaded into reduction reactor 2, nitrogen is stopped flowing under the hopper of reduction reactor, the top gate valve of reduction reactor 2 is closed, valve A is opened, and valves C and D are opened to circulate CO2 and replenish CO2. (Total flow rate is 700m³) 3 / h, the circulation / replenishment volume ratio is 215:485, and the CO2 / coke volume hourly space velocity is 70h. -1 The gas enters the CO2 preheater 15, where it exchanges heat with the high-temperature gas that has been dusted by the high-temperature dust collector 7. It then enters the reduction reactor 2 from the bottom, where it undergoes a thermal reduction reaction with the red-hot coke to generate CO. The gas after the reaction exits from the top outlet of the reduction reactor 2, passes through the high-temperature dust collector 7, is preheated, and recycled CO2 is replenished before being sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity. After being cooled by the waste heat boiler 8, the gas passes through the cyclone separator B 11 for dust removal before going to the CO separation device (pressure swing adsorption device) 12, where CO is separated (flow rate 485 m³ / s). 3 The CO2 (with a CO2 conversion rate of 69.2%) is fed into the gas tank. The separated recycled CO2 (purity greater than 99%) and supplementary CO2 (purity greater than 99%) are heated by the CO2 preheater 15 and then fed into the bottom of the reduction reactor 2 for reaction. After the coke temperature drops to 800℃ in the reduction reactor 2, valves A, C, and D are closed, valve B is opened, and the bottom valve of the reduction reactor 2 is opened. The 800℃ coke falls into the dry quenching furnace 3, and CO2 (flow rate 13300 m³ / h) is released. 3The CO2 is introduced from the bottom of the dry quenching furnace 3 and exchanges heat with the coke in a counter-current manner inside the furnace. The hot CO2 after heat exchange is sent from the top outlet of the dry quenching furnace 3 through the high-temperature dust collector 7 to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity. After being cooled by the waste heat boiler 8, the cold CO2 is removed by the cyclone separator B 11 and then returned to the bottom of the dry quenching furnace 3 to continue cooling the coke. The coke (12.7 tons, with a melting loss rate of 2%) is cooled to below 200°C, and the bottom valve of the dry quenching furnace 3 is opened to discharge the coke and transport it to the coke warehouse. Example 2

[0035] 13 tons (10 cubic meters) of 1000℃~1050℃ incandescent red-hot coke, loaded into coke receiving tank 1, is transported by coke oven discharge car to the side of dry quenching furnace 3. Coke receiving tank 1, filled with red-hot coke, is then hoisted above reduction reactor 2. Nitrogen gas is introduced from below the hopper of reduction reactor 2 at a flow rate of 20 m³ / h. 3 At a rate of / h, purging is performed for 0.5 hours, followed by continued nitrogen flow. The top gate valve of reduction reactor 2, the bottom valve of coke inlet 1, and valve A are opened sequentially. Under gravity, the red-hot coke falls into reduction reactor 2. Simultaneously, the bottom CO2 valve of dry quenching furnace 3 is opened, allowing CO2 to be introduced into dry quenching furnace 3 at a flow rate of 50 m³ / h. 3 At / h, the air inside the furnace is replaced, and exhaust pump 5 is turned on. The air inside the dry quenching furnace 3, as well as the dust, air, and exhaust gas above the hopper of reduction reactor 2, are collected through the gas collection hood, led out by exhaust pump 5, and then discharged after dust removal by cyclone separator A 6 and sent for exhaust gas treatment. After all the red coke is loaded into reduction reactor 2, nitrogen is stopped flowing under the hopper of reduction reactor, the top gate valve of reduction reactor 2 is closed, valve A is opened, and valves C and D are opened to circulate CO2 and replenish CO2. (Total flow rate is 400m³) 3 / h, the circulation / replenishment volume ratio is 16:384, and the CO2 / coke volume hourly space velocity is 40h. -1 The gas enters the CO2 preheater 15, where it exchanges heat with the high-temperature gas that has been dusted by the high-temperature dust collector 7. Then, it is introduced into the reduction reactor 2 from the bottom, where it undergoes a thermal reduction reaction with the red-hot coke to generate CO. The gas after the reaction exits from the top outlet of the reduction reactor 2, passes through the high-temperature dust collector 7, is preheated with recycled CO2 and supplemented with CO2, and is then sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity. After being cooled by the waste heat boiler 8, the gas after the reaction is dusted by the cyclone separator B 11 and then goes to the CO separation device (pressure swing adsorption device) 12, where CO is separated (flow rate 384 m³ / s). 3 / h, CO2 conversion rate 96%) into the gas tank, the separated recycled CO2 (purity greater than 99%) and the supplementary CO2 (purity greater than 99%) are heated by the CO2 preheater 15 and then fed into the bottom of the reduction reactor 2 for reaction; the temperature of the coke after reaction in the reduction reactor 2 is reduced to 800°C, the A valve, the C valve and the D valve are closed, the B valve is opened, the valve at the bottom of the reduction reactor 2 is opened, and the 800°C coke falls into the dry quenching furnace 3, the CO2 (flow rate 13300 m 3 / h) is introduced from the bottom of the dry quenching furnace 3 and exchanges heat with the coke in the furnace, the hot CO2 after heat exchange is discharged from the top of the dry quenching furnace 3, passes through the high-temperature dust collector 7, and then is sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity, after that, the cold CO2 after cooling in the waste heat boiler 8 is dusted by the cyclone separator B 11 and then is returned to the bottom of the dry quenching furnace 3 to continue cooling the coke; the coke (12.79 tons, dissolution loss rate 1.6%) is cooled to below 200°C, the valve at the bottom of the dry quenching furnace 3 is opened, and the coke is discharged and transported to the coke storage. Example 3

[0036] The 13 tons (10 cubic meters) of 1000°C~1050°C red-hot coke charged into the coke receiving tank 1 is transported to the side of the dry quenching furnace 3 by the coke oven pusher, and the coke receiving tank 1 charged with the red coke is hoisted above the reduction reactor 2; nitrogen is introduced from below the hopper of the reduction reactor 2, and the flow rate is 20 m 3 / h, and the nitrogen continues to be introduced, the top gate valve of the reduction reactor 2, the bottom valve of the coke receiving tank 1 and the A valve are opened in turn, the red coke falls into the reduction reactor 2 under the action of gravity, and the CO2 valve at the bottom of the dry quenching furnace 3 is opened, CO2 is introduced into the dry quenching furnace 3, and the flow rate is 50 m 3 / h, the air in the furnace is started to be replaced, the exhaust pump 5 is opened, the air in the dry quenching furnace 3 and the dust and air above the hopper of the reduction reactor 2 and the exhaust gas are collected by the gas hood, introduced by the exhaust pump 5, and then dusted by the cyclone separator A 6 before being discharged and sent to the exhaust gas treatment; after all the red coke is charged into the reduction reactor 2, the nitrogen introduction below the hopper of the reduction reactor is stopped, the top gate valve of the reduction reactor 2 is closed, the A valve is opened, the C valve and the D valve are opened, and the recycled CO2 and the supplementary CO2 (total flow rate 2000 m 3 / h, recycled / supplementary volume ratio 1400:600, CO2 / coke volume space velocity 200 h -1), into the CO2 preheater 15, and after heat exchange with the high-temperature gas that has been dedusted by the high-temperature dust collector 7, the CO2 is fed into the reduction reactor 2 from the bottom of the reduction reactor 2 to generate CO by thermal reduction reaction with the red coke, and after the reaction, the gas is discharged from the top of the reduction reactor 2, and after passing through the high-temperature dust collector 7, the preheated circulating CO2 and the supplementary CO2 are fed into the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity, and then the reaction gas after cooling in the waste heat boiler 8 is dedusted by the cyclone separator B 11, and then sent to the CO separation device (organic amine solution absorption device) 12, and the CO (flow rate 600 m 3 / h, CO2 conversion rate 30%) is separated out and sent to the gas tank, and the separated circulating CO2 (purity greater than 99%) and the supplementary CO2 (purity greater than 99%) are heated by the CO2 preheater 15 and then fed into the reduction reactor 2 for reaction; the temperature of the coke after reaction in the reduction reactor 2 is reduced to 800°C, the A valve, the C valve and the D valve are closed, the B valve is opened, and the valve at the bottom of the reduction reactor 2 is opened, and the 800°C coke falls into the dry quenching furnace 3, and the CO2 (flow rate 13300 m 3 / h) is fed from the bottom of the dry quenching furnace 3 to exchange heat with the coke in the furnace, the hot CO2 after heat exchange is discharged from the top of the dry quenching furnace 3, and after passing through the high-temperature dust collector 7, the CO2 is fed into the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity, and then the cold CO2 after cooling in the waste heat boiler 8 is dedusted by the cyclone separator B 11 and then returned to the bottom of the dry quenching furnace 3 to continue cooling the coke; the coke (12.68 tons, dissolution loss rate 2.47%) is cooled to below 200°C, the valve at the bottom of the dry quenching furnace 3 is opened, and the coke is discharged and transported to the coke storage. Example 4

[0037] The 13 tons (10 cubic meters) of 1000°C~1050°C red-hot coke charged into the coke receiving tank 1 is transported to the side of the dry quenching furnace 3 by the coke oven coke discharge car, and the coke receiving tank 1 charged with red coke is hoisted to the top of the reduction reactor 2; nitrogen is fed from below the hopper of the reduction reactor 2 at a flow rate of 15 m 3 / h, and the replacement is continued for 0.5 hours, and then the nitrogen is continuously fed, the top gate valve of the reduction reactor 2, the bottom valve of the coke receiving tank 1 and the A valve are opened in sequence, and the red coke falls into the reduction reactor 2 under the action of gravity, and at the same time, the CO2 valve at the bottom of the dry quenching furnace 3 is opened, and CO2 is fed into the dry quenching furnace 3 at a flow rate of 30 m 3 / h, the replacement of air in the furnace is started, the exhaust pump 5 is opened, and the air in the dry quenching furnace 3, the dust and air above the hopper of the reduction reactor 2 and the exhaust gas are collected by the gas collecting hood, and then discharged by the exhaust pump 5, and then dedusted by the cyclone separator A 6 before being discharged for exhaust gas treatment; after all the red coke is charged into the reduction reactor 2, the nitrogen feeding below the hopper of the reduction reactor is stopped, the top gate valve of the reduction reactor 2 is closed, the A valve is opened, the C valve and the D valve are opened, and the circulating CO2 and the supplementary CO2 (total flow rate 2000 m 3 / h, CO2 / carbon volume space velocity 200 h -1 ), into the CO2 preheater 15, and after heat exchange with the high-temperature gas that has been dedusted by the high-temperature dust collector 7, the CO2 is introduced into the reduction reactor 2 from the bottom of the reduction reactor 2 to have a thermal reduction reaction with the red coke to generate CO. After the reaction, the gas is discharged from the top of the reduction reactor 2, and after passing through the high-temperature dust collector 7, the preheated circulating CO2 and the supplementary CO2 are sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity. After the reaction gas is cooled by the waste heat boiler 8, the cooled reaction gas is dedusted by the cyclone separator B 11, and then sent to the CO separation device (pressure swing adsorption device) 12. The separated CO (flow rate 570 m 3 / h) is sent to the gas tank, and the separated circulating CO2 (purity greater than 99%) and the supplementary CO2 (purity greater than 99%) are heated by the CO2 preheater 15 and then sent to the bottom of the reduction reactor 2 for reaction. The temperature of the coke after the reaction in the reduction reactor 2 is reduced to 800°C, the A valve, the C valve and the D valve are closed, the B valve is opened, and the valve at the bottom of the reduction reactor 2 is opened. The 800°C coke falls into the dry quenching furnace 3, and the CO2 (flow rate 12000 m 3 / h) is introduced from the bottom of the dry quenching furnace 3 to have a reverse heat exchange with the coke in the furnace. The heated CO2 after the heat exchange is discharged from the top of the dry quenching furnace 3, and after passing through the high-temperature dust collector 7, the CO2 is sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity. After the cooled CO2 is cooled by the waste heat boiler 8, the cooled CO2 is dedusted by the cyclone separator B 11 and then returned to the bottom of the dry quenching furnace 3 to continue cooling the coke. The coke (12.60 tons, with a dissolution loss rate of 3.08%) is cooled to below 200°C, the valve at the bottom of the dry quenching furnace 3 is opened, and the coke is discharged and transported to the coke storage. Example 5

[0038] The 13 tons (10 cubic meters) of 1000°C~1050°C red-hot coke charged into the coke receiving tank 1 is transported by a coke oven car to the side of the dry quenching furnace 3, and the coke receiving tank 1 charged with the red coke is hoisted to the top of the reduction reactor 2. Nitrogen is introduced from below the hopper of the reduction reactor 2 at a flow rate of 15 m 3 / h for 0.5 hours, and the nitrogen is continuously introduced. The top gate valve of the reduction reactor 2, the bottom valve of the coke receiving tank 1 and the A valve are opened in sequence. The red coke falls into the reduction reactor 2 under the action of gravity, and at the same time, the CO2 valve at the bottom of the dry quenching furnace 3 is opened. The CO2 is introduced into the dry quenching furnace 3 at a flow rate of 30 m 3 / h, the exhaust pump 5 is started, and the air in the dry quenching furnace 3, as well as the dust and air above the hopper of the reduction reactor 2 and the exhaust gas are collected by the gas collecting hood, introduced out by the exhaust pump 5, and then dedusted by the cyclone separator A 6 before being discharged and sent to the exhaust gas treatment. After all the red coke is charged into the reduction reactor 2, the nitrogen introduction from below the hopper of the reduction reactor 2 is stopped, the top gate valve of the reduction reactor 2 is closed, the A valve is opened, the C valve and the D valve are opened, and the circulating CO2 and the supplementary CO2 (total flow 2000 m 3 / h, recycle / make-up volume ratio 1430:570, CO2 / coke volume space velocity 200 h -1 ), enters the CO2 preheater 15, exchanges heat with the high-temperature gas that has been dedusted by the high-temperature dust collector 7, and is then introduced into the reduction reactor 2 from the bottom of the reduction reactor 2 to have a thermal reduction reaction with the red coke to generate CO. After the reaction, the gas is discharged from the top of the reduction reactor 2, is dedusted by the high-temperature dust collector 7, is preheated with recycled CO2 and make-up CO2, is sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity, and then, after being cooled by the waste heat boiler 8, is dedusted by the cyclone B 11 and is sent to the CO separation device (pressure swing adsorption device) 12 to separate CO (flow 570 m 3 / h, CO2 conversion rate 28.5%). The separated recycled CO2 (purity greater than 99%) and make-up CO2 (purity greater than 99%) are heated by the CO2 preheater 15 and are then introduced into the reduction reactor 2 to have a reaction. The temperature of the coke after the reaction in the reduction reactor 2 is reduced to 800°C, the A valve, the C valve and the D valve are closed, the B valve is opened, the bottom valve of the reduction reactor 2 is opened, and the 800°C coke falls into the dry quenching furnace 3. CO2 (flow 12000 m 3 / h) is introduced from the bottom of the dry quenching furnace 3 to exchange heat with the coke in the furnace in a reverse direction. The heated CO2 after the heat exchange is discharged from the top of the dry quenching furnace 3, is dedusted by the high-temperature dust collector 7, is sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity, and then, after being cooled by the waste heat boiler 8, is dedusted by the cyclone B 11 and is returned to the bottom of the dry quenching furnace 3 to continue to cool the coke. The coke (12.60 tons, dissolution loss rate 3.08%) is cooled to below 200°C, the bottom valve of the dry quenching furnace 3 is opened, and the coke is discharged to be transported to a coke storage. Example 6

[0039] The 13 tons (10 cubic meters) of red coke at 1000°C-1050°C in the coke receiving tank 1 is transported by a coke oven car to the side of the dry quenching furnace 3, the coke receiving tank 1 loaded with the red coke is hoisted to the top of the reduction reactor 2, nitrogen is introduced from below the hopper of the reduction reactor 2, the flow is 15 m 3 / h, the nitrogen is continuously introduced, the top gate valve of the reduction reactor 2, the bottom valve of the coke receiving tank 1 and the A valve are opened in sequence, the red coke falls into the reduction reactor 2 under the action of gravity, the CO2 valve at the bottom of the dry quenching furnace 3 is opened, and CO2 is introduced into the dry quenching furnace 3, the flow is 30 m 3 / h, start to replace the air in the furnace, open the exhaust pump 5, dry quenching furnace 3 air and reducing reactor 2 hopper above the dust and air, exhaust gas through the hood collection, by the exhaust pump 5 out, then after cyclone A 6 dust removal, exhaust gas treatment; all the red coke into the reducing reactor 2, reducing reactor hopper below stop into nitrogen, close the top gate valve of the reducing reactor 2, open A valve, open C valve and D valve, circulating CO2 and supplement CO2 (total flow 2000 m 3 / h, circulating / supplement volume ratio 1430:570, CO2 / coke volume space velocity 200 h -1 ), into the CO2 preheater 15, heat exchange with high temperature gas after high temperature dust removal device 7, from the bottom of the reducing reactor 2 into the reducing reactor 2, and red coke hot reduction reaction to generate CO, after the reaction gas from the top of the reducing reactor 2 outlet after high temperature dust removal device 7, preheating circulating CO2 and supplementary CO2, send waste heat boiler 8 to recover heat, drive steam turbine 10 power generation, after the reaction gas cooled by waste heat boiler 8 after cyclone B 11 dust removal, to CO separation device (pressure swing adsorption device) 12, separate out CO (flow 570 m 3 / h, CO2 conversion rate 28.5%), CO after compression, mixed with H2 generated by photovoltaic electrolysis water hydrogen device according to the volume ratio of 1:2, converted into methanol by fixed bed methanol synthesis device 14; separated circulating CO2 (purity greater than 99%) and supplementary CO2 (purity greater than 99%) after heating by CO2 preheater 15, into the bottom of the reducing reactor 2 for reaction; the temperature of the coke after reaction in the reducing reactor is reduced to 800℃, close A valve, C valve and D valve, open B valve, open the bottom valve of the reducing reactor, 800℃ coke falls into the dry quenching furnace 3, CO2 (flow 12000 m 3 / h) from the bottom of the dry quenching furnace 3 into the furnace and contact heat exchange with coke in reverse, after heat exchange, hot CO2 from the top of the dry quenching furnace 3 outlet after high temperature dust removal device 7, send waste heat boiler 8 to recover heat, drive steam turbine 10 power generation, after the cold CO2 cooled by waste heat boiler 8 after cyclone B 11 dust removal, return to the bottom of the dry quenching furnace 3 to continue to cool the coke; the coke (12.60 tons, loss on ignition rate 3.08%) is cooled to below 200℃, open the bottom valve of the dry quenching furnace 3, discharge the coke to the coke storage. Example 7

[0040] 13 tons (10 cubic meters) of 1000℃~1050℃ red hot coke are loaded into the coke receiving tank 1, which is transported to the side of the dry quenching furnace 3 by the coke oven car, and the coke receiving tank 1 loaded with red coke is hoisted above the reducing reactor 2; nitrogen is introduced from below the reducing reactor 2 hopper at a flow rate of 15 m 3 / h, the nitrogen flow was continued, the top gate valve of the reduction reactor 2, the bottom valve of the coke collection tank 1 and the A valve were opened in sequence, the red coke fell into the reduction reactor 2 under the action of gravity, the CO2 valve at the bottom of the dry quenching furnace 3 was opened, CO2 was introduced into the dry quenching furnace 3, and the flow rate was 30 m 3 / h, the air in the furnace was replaced, the exhaust pump 5 was opened, the air in the dry quenching furnace 3 and the dust and air above the hopper of the reduction reactor 2 were collected by the exhaust hood, were introduced out by the exhaust pump 5, were then dedusted by the cyclone separator A 6, and were discharged to waste gas treatment; after all the red coke was loaded into the reduction reactor 2, the nitrogen flow below the hopper of the reduction reactor was stopped, the top gate valve of the reduction reactor 2 was closed, the A valve was opened, the C valve and the D valve were opened, and the circulating CO2 and the supplementary CO2 were introduced (h, the total flow rate was 2000 m 3 / h, the circulating / supplementary volume ratio was 1430:570, and the CO2 / coke volume space velocity was 200 h -1 ), was introduced into the reduction reactor 2 from the bottom of the reduction reactor 2 after heat exchange with high-temperature gas dedusted by the high-temperature dust collector 7, and reacted with the red coke to generate CO, the reaction gas was introduced out of the top of the reduction reactor 2 after the high-temperature dust collector 7, was preheated to circulate CO2 and supplement CO2, was sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity, and then was dedusted by the cyclone separator B 11 after being cooled by the waste heat boiler 8, was sent to the CO separation device (pressure swing adsorption device) 12, and CO (flow rate 570 m 3 / h) was separated out, the CO was mixed with H2 generated by the coke oven gas hydrogen extraction device according to a volume ratio of 1:3, was converted into ethylene or propylene by the fixed-bed olefin synthesis device 14, the separated circulating CO2 (purity greater than 99%) and the supplementary CO2 (purity greater than 99%) were heated by the CO2 preheater 15 and were introduced into the bottom of the reduction reactor 2 to react, the temperature of the coke in the reduction reactor 2 was reduced to 800 DEG C, the A valve, the C valve and the D valve were closed, the B valve was opened, the bottom valve of the reduction reactor 2 was opened, and the 800 DEG C coke fell into the dry quenching furnace 3, CO2 (flow rate 12000 m 3 / h) was introduced from the bottom of the dry quenching furnace 3 to exchange heat with the coke in the furnace in a reverse direction, the hot CO2 after heat exchange was introduced out of the top of the dry quenching furnace 3 after the high-temperature dust collector 7, was sent to the waste heat boiler 8 to recover heat and drive the steam turbine 10 to generate electricity, and then was dedusted by the cyclone separator B 11 after being cooled by the waste heat boiler 8, and was returned to the bottom of the dry quenching furnace 3 to continue to cool the coke; the coke (12.60 tons, dissolution loss rate 3.08%) was cooled to below 200 DEG C, the bottom valve of the dry quenching furnace 3 was opened, and the coke was discharged to a coke storage.

Claims

1. A carbon dioxide emission reduction and utilization process based on dry quenching, characterized in that... Includes the following steps: (1) 1000℃~1050℃ hot coke transported from the coke oven car is loaded into the coke receiving tank. The coke receiving tank containing the hot coke is hoisted above the reduction reactor. Nitrogen gas is introduced from below the hopper of the reduction reactor and replaced for 0.5 hours. Nitrogen gas is continued to be introduced. The top gate valve of the reduction reactor, the bottom valve of the coke receiving tank and the A valve at the top outlet of the dry quenching furnace are opened in sequence. Under the action of gravity, the hot coke falls into the reduction reactor. At the same time, the CO2 valve at the bottom of the dry quenching furnace is opened and CO2 is introduced into the dry quenching furnace to start replacing the air in the furnace. The exhaust pump is turned on. The air in the dry quenching furnace and the dust and air above the hopper of the reduction reactor are drawn out through the gas collection hood, dusted by the cyclone separator A, and then the discharged gas is sent to the waste gas treatment system for further treatment. (2) After all the red coke is loaded into the reduction reactor, nitrogen gas is stopped flowing into the bottom of the hopper of the reduction reactor. The top gate valve of the reduction reactor is closed, valve A is opened, and valves C and D of the inlet and outlet of the CO separation device are opened. The circulating CO2 and the supplementary CO2 enter the CO2 preheater through the pipeline. After exchanging heat with the high-temperature gas that has been dusted by the high-temperature dust collector, it is introduced into the reduction reactor from the bottom of the reduction reactor. It reacts with the red coke to generate CO. After the reaction, the gas enters the high-temperature dust collector through the A valve pipeline from the top outlet of the reduction reactor. After high-temperature dust removal, the preheated mixed CO2 is sent to the waste heat boiler to recover heat and drive the steam turbine to generate electricity. (3) The reaction gas cooled to 140-180°C from the waste heat boiler is removed by the cyclone separator B and then sent to the CO separation device to separate CO and send it to the gas tank for storage. The circulating CO2 separated by the CO separation device and the supplementary CO2 are heated by the CO2 preheater and sent to the reduction reactor for reaction. After the coke temperature is reduced to 800°C in the reduction reactor, valves A, C and D are closed and valve B is opened. The bottom valve of the reduction reactor is opened and the 800°C coke falls into the dry quenching furnace. CO2 is introduced from the bottom of the dry quenching furnace and exchanges heat with the coke in the opposite direction in the furnace. The hot CO2 after heat exchange enters the high temperature dust collector from the top outlet of the dry quenching furnace. After high temperature dust removal, it is sent to the waste heat boiler to recover heat and drive the steam turbine to generate electricity. After being cooled by the waste heat boiler, the 140~180℃ cold CO2 enters the cyclone separator B for secondary dust removal, and then returns to the bottom of the dry quenching furnace to continue cooling the coke; when the coke is cooled to below 200℃, the bottom valve of the dry quenching furnace is opened, and the coke is discharged and transported to the coke warehouse. The carbon dioxide emission reduction and utilization process based on dry quenching employs a carbon dioxide emission reduction and utilization device based on the dry quenching process, including a coke receiving tank, a reduction reactor, a dry quenching furnace, a high-temperature dust collector, a waste heat boiler, a steam turbine, a cyclone separator, and a CO separation device. The coke receiving tank is equipped with gate valves at both the top and bottom. The reduction reactor is located between the coke receiving tank and the dry quenching furnace. A nitrogen inlet is located below the hopper of the reduction reactor, and a gas collecting hood is located above the hopper to collect dust, air, and waste gas above the hopper. The reduction reactor has a gate valve and a gas outlet at the top, and a gas distribution hood at the bottom. The CO2 inlet is connected to the tube-side outlet of the CO2 preheater, and the tube-side inlet of the CO2 preheater is connected to the CO2 outlet of the CO separation unit. The shell-side inlet and outlet of the CO2 preheater are respectively connected to the high-temperature dust collector and the waste heat boiler for preheating the CO2 in the tube side. The steam outlet of the waste heat boiler is connected to the steam turbine, and the gas outlet is connected to cyclone separator B. The gas outlet of cyclone separator B is respectively connected to the inlet of the circulating gas pump and the inlet of the CO separation unit. A valve B is installed on the connection line between cyclone separator B and the circulating gas pump, and a valve C is installed on the connection line between cyclone separator B and the CO separation unit. The CO separation unit is equipped with a CO outlet connected to a gas tank at the top for storing CO. The CO2 outlet at the bottom of the CO separation unit is connected to the inlet of the CO2 preheater. A D valve is installed on the connecting pipeline between the CO separation unit and the CO2 preheater. The pipeline between the outlet of the D valve and the inlet of the CO2 preheater merges with the supplementary CO2 pipeline, connecting to the CO2 preheater. A valve is installed at the bottom connection between the dry quenching furnace and the reduction reactor. A gas outlet is located at the top of the dry quenching furnace, connecting to the gas inlet of the high-temperature dust collector. Both the dry quenching furnace outlet pipeline and the reduction reactor outlet pipeline are connected to the exhaust pump and cyclone separator A. The bottom of the dry quenching furnace has a coke discharge port, a gas distributor, and a CO2 gas inlet, which is connected to the outlet of the circulating gas pump. A valve A and a connecting pipeline are installed between the dry quenching furnace outlet pipeline and the reduction reactor outlet pipeline. During gas replacement, the exhaust pump and valve A are opened to discharge the gas from the dry quenching furnace. During the reaction, the exhaust pump is closed, valve A is opened, and the reacted gas is directed to the high-temperature dust collector.

2. The carbon dioxide emission reduction and utilization process based on dry quenching as described in claim 1, characterized in that: The CO2 volume hourly space velocity at the bottom of the reduction reactor is 40~200 / h, and the supplementary CO2 comes from CO2 with a purity higher than 99% after purification and separation from coke oven flue gas.

3. The carbon dioxide emission reduction and utilization process based on dry quenching as described in claim 1, characterized in that: In step (1), the nitrogen volume hourly space velocity during the displacement is 1.5~2 / h.

4. The carbon dioxide emission reduction and utilization process based on dry quenching as described in claim 1, characterized in that: In step (2), the volume ratio of recycled CO2 to supplemented CO2 is 1:25~3:

1.

5. The carbon dioxide emission reduction and utilization process based on dry quenching as described in claim 1, characterized in that: In step (3), the volumetric space velocity of CO2 introduced from the bottom of the dry quenching furnace is 1200~1350 / h.

6. The carbon dioxide emission reduction and utilization process based on dry quenching as described in claim 1, characterized in that: In step (3), the CO sent to the gas tank is mixed with the H2 generated by the hydrogen extraction unit in a certain proportion and then processed by the syngas conversion unit to produce fuel oil, olefins or methanol; the volume ratio of CO / H2 is 1:1.5~1:3.

Images