CN111073713A - Coke oven crude gas ammonia injection cooling system and cooling method - Google Patents

Coke oven crude gas ammonia injection cooling system and cooling method Download PDF

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CN111073713A
CN111073713A CN201911337106.XA CN201911337106A CN111073713A CN 111073713 A CN111073713 A CN 111073713A CN 201911337106 A CN201911337106 A CN 201911337106A CN 111073713 A CN111073713 A CN 111073713A
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flow
ammonia water
gas
ammonia
temperature
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CN111073713B (en
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王浩
余波
蒲春雷
桂峰
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Mcc Huatian Nanjing Engineering Technology Co Ltd
Huatian Engineering and Technology Corp MCC
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Huatian Engineering and Technology Corp MCC
MCC Huatian Anhui Energy Conservation and Environmental Protection Research Institute Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C10K1/046—Reducing the tar content
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B45/00—Other details

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  • Oil, Petroleum & Natural Gas (AREA)
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  • General Chemical & Material Sciences (AREA)
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Abstract

An ammonia injection cooling system and a cooling method for coke oven crude gas, wherein the ammonia injection cooling system comprises: the detection module comprises a thermocouple and a pressure transmitter which are arranged at a flue gas inlet of the bridge pipe, the thermocouple is used for detecting the temperature of the raw gas at the flue gas inlet of the bridge pipe, the pressure transmitter is used for detecting the pressure of the raw gas at the flue gas inlet of the bridge pipe, and the thermocouple and the pressure transmitter are connected with the control module and send the detected temperature and flow data of the raw gas to the control module; the execution module comprises an ammonia water nozzle arranged at a flue gas inlet of the bridge pipe, an ammonia water pipeline connected with the ammonia water nozzle, an adjusting valve and a variable frequency water pump, and the adjusting valve and the variable frequency water pump are connected with the control module; and the control module is used for adjusting the variable frequency water pump and the adjusting valve according to the temperature and the flow data of the crude gas in the last coking period of the coke oven, so that the flow of the ammonia water is supplied in a step descending manner, and each step keeps the flow unchanged. The invention adopts ammonia water to spray by stages, thereby reducing ammonia water amount, reducing power consumption and lowering operation cost.

Description

Coke oven crude gas ammonia injection cooling system and cooling method
Technical Field
The invention belongs to the technical field of coking, and particularly relates to a system and a method for cooling raw coke oven gas by ammonia injection.
Background
During the coking production process, a large amount of high-temperature raw coke oven gas is generated, and in order to obtain coke oven gas at the later stage, the high-temperature raw coke oven gas needs to be cooled firstly. The current technical method for cooling raw coke oven gas is generally as follows: a large amount of circulating ammonia water is sprayed at a bridge pipe of the coke oven to directly contact with the raw coke oven gas, the temperature of the raw coke oven gas is reduced to 80 ℃ by means of vaporization of excessive circulating ammonia water, and the flow of the sprayed ammonia water is always kept unchanged in the whole coking period. However, in the coking process, the temperature and the flow of the raw gas discharged from the coke oven are not constant values, but fluctuate along with the coking time, and the operation is simplified by adopting the fixed flow type ammonia water spray cooling, but the great energy waste is also caused.
The Chinese patent application with the application number of 201710601303.2 in the prior art discloses an automatic and quick anti-freezing solution energy-saving spraying linkage system and method for loading lines, which realize the automatic operation of anti-freezing solution preparation, can accurately control the concentration of anti-freezing solution preparation, and automatically adjust the spraying amount of anti-freezing solution according to the belt conveying speed and the coal quantity. Although the technology can accurately control the spraying flow of the antifreeze, the technology is only applied to spraying of the antifreeze on a rapid loading line at present, and in addition, the equipment disclosed by the invention is complex and cannot be applied to ammonia spraying and cooling of crude gas of a coke oven bridge pipe.
In the prior art, a Chinese patent with application number of 201120140348.2 discloses an ammonia water nozzle special for a coke oven, and the technology improves the uniformity of ammonia water spraying by forming a through hole at the upper end of an inner cavity in the middle of the nozzle and changing a flow deflector into an inclined hole. Although this technique can reduce the amount of sprayed ammonia water by improving the uniformity of ammonia water spraying, the effect of reducing the amount of ammonia water consumption by this method is not significant.
At present, although a series of researches on flow control and ammonia nozzle optimization are made in China, the related technology for controlling the flow of ammonia spraying of a bridge pipe of a coke oven is almost blank.
Disclosure of Invention
In order to solve the problems, the invention discloses an ammonia spraying cooling system and a cooling method for coke oven crude gas, which can greatly reduce the waste problem caused by excessive ammonia water spraying and reduce the power consumption of an ammonia water circulating pump and the workload and sewage treatment capacity of a tar separation device. The specific scheme is as follows:
a coke oven crude gas ammonia injection cooling system, crude gas enters a bridge pipe from a coke oven riser, the ammonia injection cooling system comprises:
the detection module comprises a thermocouple and a pressure transmitter which are arranged at a flue gas inlet of the bridge pipe, the thermocouple is used for detecting the temperature of the raw gas at the flue gas inlet of the bridge pipe, the pressure transmitter is used for detecting the pressure of the raw gas at the flue gas inlet of the bridge pipe, and the thermocouple and the pressure transmitter are connected with the control module and send real-time detected temperature and flow data of the raw gas to the control module;
the execution module comprises an ammonia water nozzle arranged at a flue gas inlet of the bridge pipe, an ammonia water pipeline connected with the ammonia water nozzle, an adjusting valve and a variable frequency water pump, and the adjusting valve and the variable frequency water pump are connected with the control module;
and the control module is used for adjusting the variable-frequency water pump and the adjusting valve according to the temperature and the flow data of the crude gas in the last coking period of the coke oven, so that the flow of the ammonia water in the current coking period is supplied in a step-down manner, and the flow of each step is kept unchanged.
Preferably, the coking cycle is divided into three stages according to the temperature and flow data of the raw coke oven gas, and the ammonia water flow of the coking cycle is determined according to the temperature and flow data of the raw coke oven gas of the previous coking cycle, wherein the three stages comprise:
the method comprises the following steps that at the starting stage, the temperature of raw gas gradually rises, the flow of the raw gas gradually falls, the flow of ammonia water at the starting stage of the coking cycle at this time is determined according to the average value of the temperature of the raw gas at the starting stage of the previous coking cycle and the average value of the flow of the raw gas, and the flow of the ammonia water is kept unchanged;
a fluctuation stage, namely gradually increasing the temperature of the crude gas in the fluctuation stage, enabling the flow to be in a fluctuation state, determining the flow of ammonia water in the fluctuation stage of the coking cycle according to the average value of the temperature of the crude gas in the fluctuation stage of the previous coking cycle and the average value of the flow of the crude gas, and keeping the flow of the ammonia water unchanged;
and an ending stage, wherein the temperature and the flow of the raw coke oven gas are both reduced, the stepped reduced ammonia water flow is adopted in the ending stage, and the flow is kept unchanged in each step until the ammonia water flow is reduced to 0.
Preferably, the coking cycle is started at 0-6h, the surge phase at 6-14h, and the end phase at 14-18 h.
Preferably, the control module is a PLC controller.
Preferably, the aqueous ammonia nozzle is a direct injection nozzle.
The invention also provides a coke oven crude gas ammonia injection cooling method, which adopts the coke oven crude gas ammonia injection cooling system, divides a coking cycle into three stages according to the temperature and flow data of the crude gas, and adjusts a variable frequency water pump and an adjusting valve according to the three stages of the previous coking cycle, so that the flow of ammonia water in the current coking cycle is supplied in a step-down manner, and the flow of ammonia water is kept unchanged in each step, wherein the three stages comprise:
the method comprises the following steps that at the starting stage, the temperature of raw gas gradually rises, the flow of the raw gas gradually falls, and the flow of ammonia water at the starting stage of the coking cycle is determined by using a heat balance formula according to the average value of the temperature of the raw gas at the starting stage of the previous coking cycle and the average value of the flow of the raw gas, wherein the flow of the ammonia water is kept unchanged;
a fluctuation stage, namely gradually increasing the temperature of the crude gas in the fluctuation stage, keeping the flow in a fluctuation state, and determining the flow of the ammonia water in the fluctuation stage of the coking cycle by using a heat balance formula according to the average value of the temperature of the crude gas in the fluctuation stage of the previous coking cycle and the average value of the flow of the crude gas, wherein the flow of the ammonia water is kept unchanged;
and an end stage, wherein the temperature and the flow of the crude gas in the end stage are both reduced, the ammonia water flow which is reduced in a stepped manner is adopted in the end stage, the flow of each step is kept unchanged until the ammonia water flow is reduced to 0, and the determination process of the flow of each step in the end stage is as follows:
and dividing the finishing stage into a plurality of time intervals, determining the ammonia water flow in the corresponding time interval of the coking cycle by using a heat balance formula according to the average temperature and the average flow of the raw coke gas in each time interval, and keeping the ammonia water flow unchanged until another time interval is reached.
Preferably, the heat balance formula q is adopted in all three stagesm2＝(qv1ρ1cp1Δt1)/(cp2ρ2Δt2) Calculating the ammonia water flow required by the corresponding stage in the coking cycle,
wherein q isv1Is the flow of raw gas;
ρ1is the density of the raw gas;
cp1is the specific heat capacity of the raw coke oven gas;
Δt1is the temperature variation value of the raw gas;
ρ2is the density of the ammonia;
cp2is the specific heat capacity of ammonia;
Δt2is the temperature variation value of ammonia water;
qm2is the flow rate of ammonia.
Compared with the prior art, the technical scheme provided by the invention has the following technical advantages:
1) the invention monitors the parameters in real time through the detection system, utilizes the control module to carry out on-line analysis on the data of the previous coking period, and works out a set of ammonia water staged spraying scheme which accords with the actual production condition of the coke oven of the current coking period, thereby ensuring the reliability of operation;
2) the scheme of ammonia water staged spraying is adopted, the ammonia water amount required to be provided by the circulating ammonia water pump in a coking period is reduced, the power consumption required by the circulating ammonia water pump is reduced, and the operation cost is reduced;
3) the ammonia water amount required for separating tar is reduced, and the work load and the sewage treatment capacity of the tar separator are reduced.
Drawings
The above features and technical advantages of the present invention will become more apparent and readily appreciated from the following description of the embodiments thereof taken in conjunction with the accompanying drawings.
FIG. 1 is a schematic structural diagram of a coke oven crude gas ammonia injection cooling system of the present invention;
FIG. 2 is a graph of the temperature and flow of raw coke oven gas for a coking cycle;
FIG. 3 is a flow chart of ammonia water spraying controlled by the control device of the present invention at different stages.
List of reference numerals:
1. the device comprises a coke oven ascending pipe, 2, a bridge pipe, 3, a low-pressure ammonia water nozzle, 4, a low-pressure ammonia water pipeline, 5, an electric regulating valve, 6, a variable-frequency water pump, 7, a PLC (programmable logic controller), 8, a circuit, 9, a pressure transmitter, 10 and a thermocouple.
Detailed Description
Embodiments of the coke oven raw gas ammonia injection cooling system and the cooling method according to the invention will be described below with reference to the accompanying drawings. Those of ordinary skill in the art will recognize that the described embodiments can be modified in various different ways, or combinations thereof, without departing from the spirit and scope of the present invention. Accordingly, the drawings and description are illustrative in nature and not intended to limit the scope of the claims. Furthermore, in the present description, the drawings are not to scale and like reference numerals refer to like parts.
The ammonia spraying cooling system for the coke oven crude gas comprises a detection module, a control module and an execution module, wherein the detection module is installed at a flue gas inlet of a coke oven bridge pipe and is connected with the control module through a line, and the execution module is installed on a low-pressure ammonia water pipeline and is connected with the control module through a line. The detection module can detect the temperature and the flow of crude gas at the entrance of the bridge pipe in real time, and transmits the detected data to the control module, and the control module controls the ammonia water to carry out staged spraying by controlling the execution module.
As shown in fig. 1, the detection module comprises a thermocouple 10 and a pressure transmitter 9, the raw coke oven gas enters the bridge pipe 2 from the coke oven ascension pipe 1, the thermocouple 10 is used for detecting the temperature of the raw coke oven gas at the flue gas inlet of the bridge pipe 2, the pressure transmitter 9 is used for detecting the pressure P of the raw coke oven gas at the flue gas inlet of the bridge pipe 2, and the thermocouple 10 and the pressure transmitter 9 are connected with the PLC controller 7 through a line 8. And sending the temperature and pressure data of the crude gas detected in real time to the PLC 7. The PLC 7 can obtain the flow velocity of the crude gas at the place through the Bernoulli equation
Figure BDA0002331264460000051
(ρ1Raw gas density), and the raw gas flow rate Q ═ Au (a is the cross-sectional area of the bridge pipe 2) is obtained.
The execution module comprises a low-pressure ammonia water nozzle 3, a low-pressure ammonia water pipeline 4, an electric regulating valve 5 and a variable-frequency water pump 6, and the control module comprises a PLC (programmable logic controller) 7. The electric regulating valve 5 and the variable frequency water pump 6 are connected with a PLC (programmable logic controller) 7 through a line 8. After receiving the signal of the PLC controller 7, the variable frequency water pump 6 performs step-down regulation on the flow according to different stages in a coking cycle of the coke oven, and each stage of steps keeps the flow unchanged. Meanwhile, the PLC 7 adjusts the opening degree of the electric adjusting valve 5, so that the opening degree of the electric adjusting valve is adaptive to the flow of the variable-frequency water pump 6.
In an optional embodiment, the low-pressure ammonia water nozzle is a direct injection nozzle.
In an optional embodiment, the coking cycle is divided into 3 stages, the ammonia water flow of the coking cycle is determined according to the raw gas temperature and flow data in the last coking cycle detected by the detection module in one coking cycle of the coke oven, and different flow control is adopted in the 3 stages. FIG. 2 is a temperature-flow curve diagram of the raw coke oven gas temperature and flow rate in the last coking cycle recorded by the detection module during the coking process of the 4.3m coke oven, plotted with the coking time. As can be seen from fig. 2, the raw gas temperature rises substantially linearly to the maximum temperature and then falls linearly. The flow rate of the raw gas is not completely linear, and is substantially linear in the beginning and end stages, and is in a fluctuating state in the middle stage.
The 3 phases of the coking cycle include:
1) the first stage is a starting stage, in which the temperature of the raw gas is gradually increased, but the flow rate of the raw gas is gradually decreased, so that the flow rate of ammonia water required for cooling the raw gas is basically kept unchanged. The ammonia water flow at the starting stage in the coking cycle can be determined according to the average value of the raw gas temperature and the average value of the raw gas flow in the interval in the previous coking cycle.
As shown in FIG. 2, 0-6h in the previous coking cycle is the starting stage, the average temperature of the raw gas is 725 ℃, and the average flow rate of the raw gas is 725Nm3H, using the heat balance formula qm2＝(qv1ρ1cp1Δt1)/(cp2ρ2Δt2) (subscript 1 represents raw coke oven gas parameters, and subscript 2 represents ammonia parameters) to calculate the ammonia flow required by the initial stage in the coking cycle. In order to ensure the operation safety of the equipment, the safety factor is 2, and the actual ammonia water flow at the starting stage of the coking cycle is 1038kg/h (the same applies to the required ammonia water flow calculation method below). Wherein q isv1Is the average flow, rho, of the raw gas at this stage1Is the density of the raw gas, cp1Is the specific heat capacity, Δ t, of the raw gas1Is the temperature variation value rho of the raw gas at the stage2Is the density of aqueous ammonia, cp2Is the specific heat capacity, Δ t, of aqueous ammonia2Is ammonia water at this stageValue of temperature change of qm2Is the flow rate of ammonia.
2) The second stage is a fluctuation stage, the temperature of the raw coke oven gas slowly rises in the fluctuation stage, and the flow rate is in a fluctuation state. The flow rate of the ammonia water can be determined according to the average value of the temperature of the crude gas in the interval in the previous coking cycle and the average value of the flow rate of the crude gas.
As shown in FIG. 2, 6-14h in the previous coking cycle is a fluctuation stage, the average temperature of the raw coke oven gas in the fluctuation stage is 775 ℃, and the average flow rate of the raw coke oven gas is 570Nm3Therefore, the flow rate of ammonia water adopted in the fluctuation stage in the coking cycle is 894 kg/h. The calculation method adopts the same heat balance formula as the initial stage.
3) The third stage is an end stage, the temperature and the flow of the raw gas are both rapidly reduced in the end stage, and the gradually reduced ammonia water flow is adopted in the end stage until the flow is reduced to 0. For the convenience of industrial operation, the spraying flow rate of the ammonia water in the third stage can be reduced in a step manner. The PLC controller can complete the stepped spraying of the flow of the ammonia water at the stage by controlling the opening of the electric regulating valve.
And dividing the finishing stage into a plurality of time intervals, determining the ammonia water flow in the corresponding time interval of the coking cycle by using a heat balance formula according to the average temperature and the average flow of the raw coke gas in each time interval, and keeping the ammonia water flow unchanged until another time interval is reached. For example, as shown in FIG. 2, 14-18h of the previous coking cycle are end stages, and a period of time is 14 hours to 16 hours, and a period of time is 16 hours to 18 hours, respectively. Based on the average temperature and the average flow of the crude gas from the 14 th hour to the 16 th hour, the flow of the obtained ammonia water is 790Nm & lt/EN & gt respectively according to the calculation of the heat balance formula3H and maintaining the flow rate of ammonia at 790Nm for 14 to 16 hours3The flow rates of the obtained ammonia water are respectively 474Nm and 18 Nm by calculating according to the heat balance formula on the basis of the average temperature and the average flow rate of the crude gas from 16 hours to 18 hours3H, maintaining the flow rate of ammonia water at 474Nm for 16 to 18 hours3/h。
It should be noted that the above time periods in fig. 2 are only exemplary, and the time periods of the start phase, the surge phase and the end phase in each coking cycle are not necessarily the same as those in fig. 2, but the characteristics of the phases are the same as those in fig. 2.
The invention does not change the original structure of the ascending pipe of the coke oven, thereby not influencing the production process of the coke oven. FIG. 3 is a plot of ammonia spray staging flow rate based on the data from FIG. 2. The consumption of the fixed ammonia water sprayed by the coke oven with the number of 65 chambers of 4.3m is 59.1 ten thousand tons. If the sectional type ammonia spraying cooling control module and the method for the raw coke oven gas are adopted, the ammonia water consumed in one year is 47.0 ten thousand tons, 12.1 ten thousand tons of ammonia water can be saved compared with the fixed flow type ammonia water spraying, and the electric energy consumption of an ammonia water pump, the work load of a tar separator and the sewage treatment capacity are greatly reduced.
The invention also provides a coke oven crude gas ammonia injection cooling method, which adopts the coke oven crude gas ammonia injection cooling system, divides the coking cycle into three stages according to the temperature and flow data of the crude gas, adjusts the variable frequency water pump and the adjusting valve according to the three stages of the previous coking cycle, so that the flow of ammonia water is supplied in a step descending manner, and each stage of steps keeps the flow unchanged, wherein the three stages comprise:
1) the first stage is a starting stage, in which the temperature of the raw gas is gradually increased, but the flow rate of the raw gas is gradually decreased, so that the flow rate of ammonia water required for cooling the raw gas is basically kept unchanged. The ammonia water flow at the starting stage in the coking cycle can be determined according to the average value of the raw gas temperature and the average value of the raw gas flow in the interval in the previous coking cycle.
As shown in FIG. 2, 0-6h in the previous coking cycle is the starting stage, the average temperature of the raw gas is 725 ℃, and the average flow rate of the raw gas is 725Nm3H, using the heat balance formula qm2＝(qv1ρ1cp1Δt1)/(cp2ρ2Δt2) (subscript 1 represents raw coke oven gas parameter, subscript 2 represents ammonia water parameter) to calculate ammonia water required by the initial stage of the coking cycleAnd (4) flow rate. Further, the actual ammonia flow rate at the beginning of the coking cycle is 1038kg/h (the same method is used for calculating the ammonia flow rate). Wherein q isv1Is the average flow, rho, of the raw gas at this stage1Is the density of the raw gas, cp1Is the specific heat capacity, Δ t, of the raw gas1Is the temperature variation value rho of the raw gas at the stage2Is the density of aqueous ammonia, cp2Is the specific heat capacity, Δ t, of aqueous ammonia2Is the temperature change value of ammonia water at this stage, qm2Is the flow rate of ammonia.
2) The second stage is a fluctuation stage, the temperature of the raw coke oven gas slowly rises in the fluctuation stage, and the flow rate is in a fluctuation state. The flow rate of the ammonia water can be determined according to the average value of the temperature of the crude gas in the interval in the previous coking cycle and the average value of the flow rate of the crude gas.
As shown in FIG. 2, 6-14h in the previous coking cycle is a fluctuation stage, the average temperature of the raw coke oven gas in the fluctuation stage is 775 ℃, and the average flow rate of the raw coke oven gas is 570Nm3Therefore, the flow rate of ammonia water adopted in the fluctuation stage in the coking cycle is 894 kg/h. The calculation method adopts the same heat balance formula as the initial stage.
3) The third stage is an end stage, the temperature and the flow of the raw gas are both rapidly reduced in the end stage, and the gradually reduced ammonia water flow is adopted in the end stage until the flow is reduced to 0. For the convenience of industrial operation, the spraying flow rate of the ammonia water in the third stage can be reduced in a step manner. The PLC controller can complete the stepped spraying of the flow of the ammonia water at the stage by controlling the opening of the electric regulating valve.
And dividing the finishing stage into a plurality of time intervals, determining the ammonia water flow in the corresponding time interval of the coking cycle by using a heat balance formula according to the average temperature and the average flow of the raw coke gas in each time interval, and keeping the ammonia water flow unchanged until another time interval is reached. For example, as shown in FIG. 2, 14-18h of the previous coking cycle are end stages, and a period of time is 14 hours to 16 hours, and a period of time is 16 hours to 18 hours, respectively. Based on the average temperature and the average flow of the crude gas from the 14 th hour to the 16 th hour, the heat balance formula is calculatedThe flow rates of the obtained ammonia water are 790Nm respectively3H and maintaining the flow rate of ammonia at 790Nm for 14 to 16 hours3The flow rates of the obtained ammonia water are respectively 474Nm and 18 Nm by calculating according to the heat balance formula on the basis of the average temperature and the average flow rate of the crude gas from 16 hours to 18 hours3H, maintaining the flow rate of ammonia water at 474Nm for 16 to 18 hours3/h。
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (7)

1. The utility model provides a coke oven crude gas spouts ammonia cooling system, crude gas gets into the bridge pipe from the coke oven tedge, its characterized in that spouts ammonia cooling system and contains:
the detection module comprises a thermocouple and a pressure transmitter which are arranged at a flue gas inlet of the bridge pipe, the thermocouple is used for detecting the temperature of the raw gas at the flue gas inlet of the bridge pipe, the pressure transmitter is used for detecting the pressure of the raw gas at the flue gas inlet of the bridge pipe, and the thermocouple and the pressure transmitter are connected with the control module and send real-time detected temperature and flow data of the raw gas to the control module;
the execution module comprises an ammonia water nozzle arranged at a flue gas inlet of the bridge pipe, an ammonia water pipeline connected with the ammonia water nozzle, an adjusting valve and a variable frequency water pump, and the adjusting valve and the variable frequency water pump are connected with the control module;
and the control module is used for adjusting the variable-frequency water pump and the adjusting valve according to the temperature and the flow data of the crude gas in the last coking period of the coke oven, so that the flow of the ammonia water in the current coking period is supplied in a step-down manner, and the flow of each step is kept unchanged.
2. The coke oven crude gas ammonia injection cooling system of claim 1, wherein the coking cycle is divided into three phases according to the temperature and flow data of the crude gas, and the ammonia flow of the current coking cycle is determined according to the temperature and flow data of the crude gas of the previous coking cycle, the three phases comprising:
the method comprises the following steps that at the starting stage, the temperature of raw gas gradually rises, the flow of the raw gas gradually falls, the flow of ammonia water at the starting stage of the coking cycle at this time is determined according to the average value of the temperature of the raw gas at the starting stage of the previous coking cycle and the average value of the flow of the raw gas, and the flow of the ammonia water is kept unchanged;
a fluctuation stage, namely gradually increasing the temperature of the crude gas in the fluctuation stage, enabling the flow to be in a fluctuation state, determining the flow of ammonia water in the fluctuation stage of the coking cycle according to the average value of the temperature of the crude gas in the fluctuation stage of the previous coking cycle and the average value of the flow of the crude gas, and keeping the flow of the ammonia water unchanged;
and an ending stage, wherein the temperature and the flow of the raw coke oven gas are both reduced, the stepped reduced ammonia water flow is adopted in the ending stage, and the flow is kept unchanged in each step until the ammonia water flow is reduced to 0.
3. The coke oven crude gas ammonia injection cooling system of claim 1, wherein the coking cycle is started at 0-6 hours, the coking cycle is started at 6-14 hours, and the coking cycle is ended at 14-18 hours.
4. The coke oven crude gas ammonia injection cooling system of claim 1, wherein the control module is a PLC controller.
5. The coke oven crude gas ammonia injection cooling system of claim 1,
the ammonia water nozzle is a direct injection type nozzle.
6. The method for cooling the ammonia sprayed from the coke oven raw gas is characterized in that the coke oven raw gas ammonia sprayed cooling system of claim 1 is adopted, a coking cycle is divided into three stages according to the temperature and flow data of the raw gas, and a variable frequency water pump and an adjusting valve are adjusted according to the three stages of the previous coking cycle, so that the flow of ammonia water in the current coking cycle is supplied in a step-down manner, and the flow of ammonia water is kept unchanged in each step, wherein the three stages comprise:
the method comprises the following steps that at the starting stage, the temperature of raw gas gradually rises, the flow of the raw gas gradually falls, and the flow of ammonia water at the starting stage of the coking cycle is determined by using a heat balance formula according to the average value of the temperature of the raw gas at the starting stage of the previous coking cycle and the average value of the flow of the raw gas, wherein the flow of the ammonia water is kept unchanged;
a fluctuation stage, namely gradually increasing the temperature of the crude gas in the fluctuation stage, keeping the flow in a fluctuation state, and determining the flow of the ammonia water in the fluctuation stage of the coking cycle by using a heat balance formula according to the average value of the temperature of the crude gas in the fluctuation stage of the previous coking cycle and the average value of the flow of the crude gas, wherein the flow of the ammonia water is kept unchanged;
and an end stage, wherein the temperature and the flow of the crude gas in the end stage are both reduced, the ammonia water flow which is reduced in a stepped manner is adopted in the end stage, the flow of each step is kept unchanged until the ammonia water flow is reduced to 0, and the determination process of the flow of each step in the end stage is as follows:
and dividing the finishing stage into a plurality of time intervals, determining the ammonia water flow in the corresponding time interval of the coking cycle by using a heat balance formula according to the average temperature and the average flow of the raw coke gas in each time interval, and keeping the ammonia water flow unchanged until another time interval is reached.
7. The coke oven crude gas ammonia injection cooling method as claimed in claim 6,
the heat balance formula q is adopted in the three stagesm2＝(qv1ρ1cp1Δt1)/(cp2ρ2Δt2) Calculating the ammonia water flow required by the corresponding stage in the coking cycle,
wherein q isv1Is the flow of raw gas;
ρ1is the density of the raw gas;
cp1is the specific heat capacity of the raw coke oven gas;
Δt1is the temperature variation value of the raw gas;
ρ2is the density of the ammonia;
cp2is the specific heat capacity of ammonia;
Δt2is the temperature variation value of ammonia water;
qm2is the flow rate of ammonia.
CN201911337106.XA 2019-12-23 2019-12-23 Coke oven crude gas ammonia injection cooling system and cooling method Active CN111073713B (en)

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CN201665660U (en) * 2010-01-08 2010-12-08 中钢设备有限公司 Automatic pressure adjusting device of carbonizing chamber of coke oven
JP2016098282A (en) * 2014-11-20 2016-05-30 Ｊｆｅスチール株式会社 Coke oven gas recovery method and recovery apparatus

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CN201665660U (en) * 2010-01-08 2010-12-08 中钢设备有限公司 Automatic pressure adjusting device of carbonizing chamber of coke oven
JP2016098282A (en) * 2014-11-20 2016-05-30 Ｊｆｅスチール株式会社 Coke oven gas recovery method and recovery apparatus

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