CN104031692A - Device and method for preparing process heat medium water by directly quenching coking raw coke oven gas at high temperature - Google Patents

Abstract

A device and method for directly quenching raw coking gas at high temperature to produce process heat medium water, the device includes a gas collecting pipe, a mechanized clarification tank A, a mechanized clarification tank B, an oil-water separator, a tar storage tank, a residual ammonia water tank, and an ammonia distillation tower , Ammonia distillation tower feed heat exchanger, gas precooler, hot water lithium bromide refrigeration unit, two-stage horizontal tube primary cooler. During production, by adding ammonia distilled waste water circulation and tar circulation, using tar-water mixture to perform high-temperature quenching operation on raw coal gas in the gas collection, changing the direct quenching effect of raw coal gas, increasing the gas temperature at the outlet of the gas collection pipe, and configuring coal gas pre-cooling Under the premise of ensuring the same cooling effect (heat transfer effect) and decoking effect (mass transfer effect) of raw gas, the waste heat of raw gas is recovered to produce 82-85°C process heat medium water, which is used for hot water lithium bromide refrigeration The heat source of the unit generator; in addition, due to the recovery of the waste heat of the raw gas before the primary cooler, compared with the existing process, the consumption of the primary cooler cooling utilities is greatly reduced.

Description

A device and method for producing process heat medium water by directly quenching coking raw gas at high temperature

technical field

The invention belongs to the field of coal chemical coking, and relates to a device for directly quenching coking raw coal gas at high temperature to produce process heat medium water. Specifically, on the basis of the existing raw gas quenching process, by adding ammonia distilled wastewater circulation and tar circulation, the tar-water mixture is used to perform high-temperature quenching operation on the raw gas in the gas collection pipe, so as to increase the gas temperature at the outlet of the gas collection pipe and configure the gas The pre-cooler, under the premise of ensuring the cooling effect (heat transfer effect) and decoking effect (mass transfer effect) of the raw gas, further recovers the waste heat of the raw gas, and produces process heat medium water at about 85°C, which is used for subsequent heating Matching process heat sink. In addition, due to the recovery of the waste heat of raw gas before the primary cooler, compared with the existing process, the consumption of cold utilities for the primary cooler is greatly reduced. the

Background technique

During the coking process, the temperature of the raw coal gas escaping from the coke oven coking chamber through the riser is 650-750°C. At this time, the gas contains tar vapor, benzene group hydrocarbons, water vapor, ammonia, hydrogen sulfide, hydrogen cyanide, naphthalene and other compounds, and contains about one-third of the heat in the coking process. Raw coal gas needs to be cooled and purified to obtain qualified coal gas. The primary cooling of raw gas is the basis of gas purification, and its operating effect not only affects the subsequent unit operation of gas purification, but also affects the processing of chemical products and the operation of coke ovens. The primary cooling of raw gas is carried out in two steps: the first step is direct quenching with a large amount of circulating ammonia water in the gas collecting pipe; the second step is indirect cooling with circulating water and low-temperature water in the primary gas cooler. the

At present, in the coal coking industry, raw coal gas is directly quenched in the form of spraying by 0.15 to 0.2 MPa (gauge pressure) and 5% mass concentration of circulating ammonia water in the bridge pipe and gas collecting pipe. When the mist-like ammonia water is in full contact with the gas, because the temperature of the gas is high and the saturation of water vapor is low, the temperature of the ammonia water is low, so the raw coal gas is instantly cooled by the ammonia water, and the heavy components are continuously condensed and precipitated, releasing a large amount of heat. Ammonia water is vaporized in a large amount when heated by the raw gas, absorbing the heat in the raw gas, thereby reducing the temperature of the entire system and achieving a rapid cooling effect. It can be seen that the instantaneous quenching process undergoes intense heat and mass transfer processes. Through the above-mentioned rapid cooling process, the gas temperature drops from 650 to 700°C to 82 to 86°C, and at the same time about 60% of the tar vapor is condensed. In actual production, the gas temperature can be cooled to 1-3°C higher than the corresponding dew point temperature of its quenched composition. Raw coal gas at 82°C enters the primary cooler and is cooled to about 23°C by circulating water and low-temperature water before entering the subsequent purification section. the

Although the existing raw gas quenching process can cool the gas from 650-700°C to 82-86°C, reduce the cooling load of the primary cooler, and cool down about 60% of the tar vapor to alleviate the coking phenomenon of the primary cooler, but due to The mass concentration of sprayed ammonia water is 5%, and its bubble point temperature is about 82°C, resulting in the temperature of the raw gas at the outlet of the gas collecting pipe at 82-86°C, and the temperature of the recovered waste heat is too low to be further effectively utilized in the subsequent recovery section. In addition, since the heat of raw gas cannot be recovered before the primary cooler, the heat is eventually lost in circulating water (55°C) and low temperature water (23°C), which not only causes waste of heat, but also increases the consumption of cooling capacity. the

At the same time, there are a large number of medium and low temperature potential heat sinks in the chemical production recovery section, such as the heat source of the hot water lithium bromide refrigerator generator (85°C), the heat source of the bottom reboiler of the vacuum potassium carbonate desulfurization process (55°C), and the negative pressure ammonia steam The heat source of the reboiler at the bottom of the tower (80°C), etc. In addition, a large amount of heat needs to be supplied to the system to realize the functions of pipeline heat tracing and tank area heat maintenance. In the existing technology, the above-mentioned low-temperature heat trap generally uses low-pressure steam (0.3MPa) for heating, and the temperature of the 0.3MPa steam is generally above 130°C, which will result in high heat and low utilization, resulting in energy waste. From the perspective of energy recovery, the energy bottleneck lies in the fact that the large amount of waste heat contained in raw gas cannot be recovered in the high temperature section, and the recovered low temperature heat cannot be reasonably matched with the low temperature heat sink. Therefore, efforts should be made to increase the recovery temperature of waste heat from raw coal gas (≥85°C). the

China Metallurgical Jiaonai Engineering Technology Co., Ltd. has applied for the development of a waste heat recovery method for desulfurization-rich liquid in the vacuum potassium carbonate desulfurization process by using the waste heat of raw gas. Energy consumption, but still use the heat below 82 ℃ of raw coal gas, the grade of recovered heat is low. The patent number is: CN200710086480.8. the

Northeastern University has developed a waste heat recovery technology that uses heat transfer oil to recover the heat of raw gas and use it in heating chemical production-related processes, but it needs to add a closed heat transfer oil system, and the heat transfer oil heat exchanger is easy to coke. The patent number is changed to: CN201110437813.3. the

Shanghai Baosteel Energy Conservation Technology Co., Ltd. has applied for the development of a coke oven raw gas waste heat power generation device. A superheater is installed in the riser tube, and an evaporator is installed in the bridge tube. The liquid working fluid passes through the heat extraction subsystem to form superheated steam, which will generate electricity. The working fluid inside is heated and drives the power generator set in the power generation sub-system to generate electricity. However, heat extraction equipment exposed to raw gas is prone to coking, resulting in a decrease in heat transfer effect, and frequent coke cleaning is required. The patent number is: CN201210318033.1. the

Contents of the invention

Aiming at the above actual situation, the present invention provides a device for directly quenching coking raw coal gas at high temperature to produce process heat medium water. By adding ammonia distillation waste water circulation and tar circulation, a tar-water mixture is used to heat the raw coal gas at high temperature in the gas collection pipe. Quenching operation, raising the gas temperature at the outlet of the gas collecting pipe, and configuring a gas pre-cooler, under the premise of ensuring the same cooling effect (heat transfer effect) and decoking effect (mass transfer effect) of the raw gas, the waste heat of the raw gas is recovered to produce 85 ℃ process heat medium water, used to meet the subsequent matching process heat sink. In addition, since the waste heat of raw gas is recovered before the primary cooler, compared with the existing process, the consumption of cold utilities for the primary cooler is greatly reduced. the

In the waste heat recovery process of raw gas, the temperature of the raw gas in the direct quenching process of the gas collector has the largest change, and the heat and mass transfer phenomena of the system are the most severe. Therefore, it is necessary to try to increase the temperature of the raw gas at the outlet of the gas collector to improve the recovery of waste heat from the raw gas. temperature. The temperature of the raw gas at the outlet of the gas collection pipe is determined by the bubble point temperature of the sprayed tar-water mixture, so the bubble point temperature can be increased by adjusting the composition of the tar-water mixture, thereby increasing the temperature of waste heat recovery; at the same time, in order to ensure the removal of raw gas The coke effect is the same, the influence of the composition of the circulating tar-water mixture on the dew point temperature of the volatile tar-water-raw gas mixture should be considered. The higher the dew point temperature, the better the decoking effect in the same temperature range. the

The tar-water mixture is used for spraying, and the spraying amount needs to be further optimized. First, the amount of spraying should meet the heat transfer requirement, that is, the amount of tar water sprayed should be enough to cool the raw gas at 680-700°C to the target temperature according to the heat balance; According to calculations, the sprayed tar water is enough to take 60% of the tar out of the gas phase; finally, the sprayed amount of tar-water should be able to maintain the temperature of the mechanized clarifier, so that the temperature of the sprayed tar-water is close to its bubble point temperature, and its It is advisable for the temperature difference to be less than or equal to 3°C. the

On the basis of completing the optimization of tar-water composition, temperature and flow rate, relevant processes should also be adjusted appropriately. If tar-water is directly quenched, the related equipment of circulating ammonia water (circulating ammonia water tank and its pipelines, etc.) will be cancelled, and a mechanized clarifier tank A will be added for the oil-water separation and slag removal of the condensate in the gas collecting pipe. The oil phase is divided into two strands, one is used as circulating tar, pumped back to the gas collection pipe for spraying, and the other enters the oil-water separator for treatment; the separated water phase is sent to the residual ammonia water tank together with the water phase of the mechanized clarifier B , and carry out separation operation in the ammonia distillation tower. The gas phase at the top of the tower is condensed by the shrinker and then sent to the sulfur ammonia section to supplement the ammonia source. The ammonia distillation wastewater at the bottom of the tower is discharged after recovering heat in one way according to the material balance of the system water, and the other way is discharged. It is directly pumped back to the gas collecting pipe, mixed with circulating tar at the top, sprayed and quenched to maintain the spray composition, temperature and flow rate of the tar-water mixture. In addition, if two-stage indirect primary coolers are used in the primary gas cooling process, a gas pre-cooler should be installed between the gas collector and the two-stage primary coolers to cool the raw gas at around 90°C to 85°C and simultaneously produce 85 The process heat medium water above ℃; if the gas primary cooling process adopts three-stage indirect primary cooler, the temperature of the produced hot water can be raised to 85°C by adjusting the flow rate of the hot water in the hot water section. The subsequent initial cooling process of raw gas at 85°C can maintain the original process. Since the dew point of the volatile tar-water-raw gas mixture system is basically unchanged, the coking degree of the primary cooler is basically unchanged, and there is no need to spray more tar-ammonia water ; In the current process, the raw gas heat is taken out by the pre-cooler (two-stage primary cooler process) or the hot water section (three-stage primary cooler process), the cooling load of the primary cooler will be reduced, and the amount of circulating water and low-temperature water will be corresponding reduce. the

Technical scheme of the present invention is as follows:

A device for directly quenching raw coking gas at high temperature to produce process heat medium water, including a gas collecting pipe, a mechanized clarification tank A, a mechanized clarification tank B, an oil-water separator, a tar storage tank, a residual ammonia water tank, an ammonia distillation tower, and an ammonia distillation tower Feed heat exchanger, gas precooler, hot water lithium bromide refrigeration unit, two-stage horizontal tube primary cooler. The condensate discharge of the gas collecting pipe is connected to the mechanized clarifier A, the water phase discharge of the mechanized clarifier A is connected to the remaining ammonia water tank, and the oil phase discharge of the mechanized clarifier A is connected in two ways: (1) The oil phase discharge of the mechanized clarifier A (2) The other way of the mechanized clarification tank A oil phase outlet is connected to the inlet of the oil-water separator; the outlet of the remaining ammonia water tank is connected to the inlet of the shell side of the feed heat exchanger of the ammonia distillation tower; The shell-side outlet of the feed heat exchanger of the ammonia tower is connected to the feed port of the ammonia distillation tower; the gas phase at the top of the ammonia distillation tower is condensed by a shrinker and then desulfurized ammonia section; the ammonia distillation waste water at the bottom of the ammonia distillation tower is connected in two ways: (1) One way of the ammonia distillation wastewater is connected to the gas collection pipe; (2) the other way of the ammonia distillation wastewater is connected to the inlet of the tube side of the feed heat exchanger of the ammonia distillation tower; the outlet material of the tube side of the feed heat exchanger of the ammonia distillation tower is sent to biochemical treatment; The gas phase discharge is connected to the shell side inlet of the gas precooler; the gas precooler condensate outlet is connected to the mechanized clarifier B inlet; the gas precooler shell side outlet is connected to the shell side inlet of the two-stage horizontal tube primary cooler ; The shell-side discharge of the two-stage horizontal tube primary cooler is sent to the subsequent gas purification section; (2) The other outlet of the condensate of the two-stage horizontal tube primary cooler is connected to the inlet of mechanized clarification tank B; the hot water outlet of the hot water lithium bromide refrigeration unit is connected to the gas precooler tube The hot water inlet of the hot water lithium bromide refrigeration unit is connected with the gas precooler tube outlet; the cold water outlet of the hot water lithium bromide refrigeration unit is connected with the cold water inlet of the two-section horizontal tube primary cooler; the hot water lithium bromide refrigeration unit The cold water inlet is connected to the cold water outlet of the two-stage horizontal tube primary cooler; the oil phase outlet of the mechanized clarification tank B is connected to the inlet of the oil-water separator; the outlet of the oil phase of the oil-water separator is connected to the inlet of the tar storage tank. the

The process is as follows:

(1) The 650-700°C raw coal gas from the coke oven is quenched by mixed spraying of circulating tar and circulating ammonia distillation wastewater in the gas collector. The temperature of the condensate in the gas collecting pipe is 88～92℃, the condensate is pumped into the mechanized clarification tank A, the water phase of the mechanized clarification tank A is pumped to the residual ammonia water tank, and the oil phase is divided into two according to the ratio of 35～40:1. Road: the former is sent to the air collecting pipe and mixed with ammonia distilled waste water for spraying and quenching; the latter is sent to the oil-water separator to remove water or sent to the tar storage tank. After quenching, the raw gas temperature is 88-92°C, and enters the gas pre-cooler for further cooling. the

(2) The 88-92°C raw gas from the gas collecting pipe enters the shell side from the bottom of the gas pre-cooler, and the 72-78°C circulating hot water is fed into the top tube side of the gas pre-cooler, and the raw gas and the circulating hot water are exchanged countercurrently Heat, the raw gas is exchanged to 82-85°C, and then enters the two-stage horizontal tube primary cooler through the outlet of the top tube side of the gas pre-cooler; the circulating hot water is heated to 82-85°C, which has reached the process heat Medium water requirements, it can be sent to the process heat sink for heating. In this process, it is sent to the hot water type lithium bromide refrigeration unit as the heat source of the generator of the hot water type lithium bromide refrigeration unit. After heating, the 72-78 ℃ hot water is pumped back to the gas The pre-cooler circulates heat to produce process heat medium water; the condensate of the gas pre-cooler is pumped from the bottom condensate outlet to the mechanized clarification tank B. the

(3) The 82-85°C raw gas from the raw gas precooler enters the shell side from the top of the two-stage horizontal tube primary cooler, and the upper and lower sections of the two-stage horizontal tube primary cooler are respectively fed by 35°C circulating water Cool with 16°C low-temperature water, and finally cool to 22-25°C and send it to the subsequent gas purification section; the 16°C low-temperature water used for cooling in the lower section is supplied by a hot-water lithium bromide refrigeration unit, and the 23°C low-temperature water is returned to the hot-water type after heat exchange Lithium bromide refrigeration unit; the condensate is pumped into the mechanical clarification tank B from the condensate outlet at the bottom of the two-stage horizontal tube primary cooler. the

(4) The condensate collected by the gas precooler and the two-stage horizontal tube primary cooler is clarified and divided into three layers in the mechanized clarification tank B, the upper layer is ammonia water, the middle layer is tar, and the lower layer is tar residue. The ammonia water in the upper layer is pumped to the residual ammonia water tank, and then the ammonia distillation operation is carried out in the ammonia distillation tower. After the gas-phase output from the top of the ammonia distillation tower is cooled by the shrinker, the ammonia gas is sent to the ammonium sulfate section saturator to supplement the amount of ammonia. The ammonia distillation waste water at the bottom of the ammonia distillation tower is divided into two streams, and the distribution ratio is 1:6-8: The former exchanges heat with the feedstock of the ammonia distillation tower and sends it to biochemical treatment. The flow of the waste water from ammonia distillation should be equal to the water volume of the raw coke oven gas, which is determined by the water volume brought into the system by the raw gas; the latter is pumped to the collector The top of the trachea is mixed with circulating tar and sprayed to ensure that the oil-to-water mass ratio of tar to water spray is 1.2 to 2:1, and the mixed spray temperature is 88 to 92 °C. Part of the oil phase in the mechanized clarification tank B enters the oil-water separator, and after oil-water separation, the oil phase enters the tar storage tank. the

Compared with the existing process, the present invention adds ammonia distilling waste water circulation and tar circulation, uses tar-water mixture to perform high-temperature quenching operation on raw coal gas in gas collection, changes the direct quenching effect of raw coal gas, and increases the gas temperature at the outlet of the gas collecting pipe. And equipped with a gas pre-cooler, under the premise of ensuring the same raw gas cooling effect (heat transfer effect) and decoking effect (mass transfer effect), the waste heat of the raw gas is recovered to produce 82-85 °C process heat medium water for use in Hot water type lithium bromide refrigeration unit generator heat source; in addition, due to the recovery of waste heat from raw gas before the primary cooler, compared with the existing process, the consumption of cold utilities for the primary cooler is greatly reduced. the

Description of drawings

The accompanying drawing is a schematic diagram of the device and equipment structure for producing process heat medium water by directly quenching raw gas at high temperature. the

Detailed ways

The specific implementation manner of the present invention will be described in detail below in combination with the technical scheme and accompanying drawings. the

As shown in the figure, the condensate discharge of the gas collection pipe is connected to the mechanized clarifier A, the water phase discharge of the mechanized clarifier is connected to the remaining ammonia water tank, and the oil phase discharge of the mechanized clarifier is connected in two ways: (1) Mechanized clarifier oil One way of the phase discharge is connected to the gas collecting pipe; (2) The other way of the oil phase discharge of the mechanized clarification tank is connected to the inlet of the oil-water separator; the outlet of the remaining ammonia water tank is connected to the inlet of the shell side of the feed heat exchanger of the ammonia distillation tower; The shell side outlet of the feed heat exchanger of the ammonia distillation tower is connected to the feed port of the ammonia distillation tower; the gas phase at the top of the ammonia distillation tower is condensed by a shrinker and then desulfurized ammonia section; the ammonia distillation waste water at the bottom of the ammonia distillation tower is connected in two ways: (1 ) one way of ammonia distillation wastewater is connected to the gas collecting pipe; (2) the other way of ammonia distillation wastewater is connected to the inlet of the feed heat exchanger tube side of the ammonia distillation tower; the outlet material of the feed heat exchanger tube side of the ammonia distillation tower is sent to biochemical treatment; The gas phase discharge of the gas pipe is connected to the shell side inlet of the gas precooler; the condensate outlet of the gas precooler is connected to the feed port of the mechanical clarification tank B; the shell side outlet of the gas precooler is connected to the shell side inlet of the two-stage horizontal tube primary cooler The two-stage horizontal tube primary cooler shell-side discharge is sent to the subsequent gas purification section; the two-stage horizontal tube primary cooler condensate is connected in two ways: (1) The two-stage horizontal tube primary cooler condensate one way (2) The other outlet of the condensate of the two-stage horizontal tube primary cooler is connected to the inlet of the mechanized clarification tank; the hot water outlet of the hot water lithium bromide refrigeration unit is connected to the gas precooler tube The hot water inlet of the hot water lithium bromide refrigeration unit is connected with the gas precooler tube outlet; the cold water outlet of the hot water lithium bromide refrigeration unit is connected with the cold water inlet of the two-section horizontal tube primary cooler; the hot water lithium bromide refrigeration unit The cold water inlet is connected to the cold water outlet of the two-stage horizontal tube primary cooler; the oil phase outlet of the mechanized clarification tank is connected to the inlet of the oil-water separator; the outlet of the oil phase of the oil-water separator is connected to the inlet of the tar storage tank. the

The specific process is:

(1) As shown in the figure, the raw coal gas with a treatment capacity of 320kg/h is quenched by mixed spraying of circulating tar and circulating ammonia distillation wastewater in the gas collector C101. The spraying rate is 1900kg/h, and the mixed spraying temperature is 90°C , pump the condensate from gas collecting pipe C101 into mechanized clarification tank A, and pump the water phase from mechanized clarifying tank B to the remaining ammonia water tank B101. Quenching; the other way is sent to oil-water separator B105 to remove water or sent to tar storage tank B106. After quenching, the raw gas temperature is 90°C, and enters the gas pre-cooler C102 for further cooling. the

(2) The 90°C raw coal gas from the gas collecting pipe C101, with a flow rate of 530kg/h, enters the shell side from the bottom of the gas precooler C102, and the 75°C circulating hot water flows into the top tube side of C102, and the raw coal gas and the circulating hot water flow countercurrently Heat exchange, the heat exchange of raw coal gas to 85°C is sent from the outlet of the top tube side of C102 to the two-stage horizontal tube primary cooler C103 for cooling; the circulating hot water is heated to 85°C, which has reached the requirements of the process heat medium water, and can be Send it to the process heat sink for heat supply. In this process, it is sent to the hot water type lithium bromide refrigeration unit as the heat source of the generator of the lithium bromide refrigeration unit. After heating, the 75°C hot water is pumped back to C102 to circulate heat and produce process heat medium water. ; The C102 condensate is pumped from the bottom condensate outlet to the mechanized clarification tank B104. the

(3) The 85°C raw gas from the raw gas pre-cooler C102 enters the shell side from the top of the two-stage horizontal tube primary cooler C103, and is cooled by 35°C circulating water and 16°C low-temperature water in the upper and lower sections of C103, respectively. Finally, it is cooled to 22-25°C and sent to the subsequent gas purification section; the 16°C low-temperature water used for cooling in the lower section is supplied by the hot-water lithium bromide refrigeration unit, and the 23°C low-temperature water is returned to the hot-water lithium bromide refrigeration unit after heat exchange; the condensate is supplied by The condensate outlet at the bottom of C103 is pumped into the mechanized clarification tank B104. the

(4) The condensate collected by the gas precooler C102 and the two-stage horizontal tube primary cooler C103 is clarified in the mechanized clarification tank B104 and divided into three layers, the upper layer is ammonia water, the middle layer is tar, and the lower layer is tar residue. The ammonia water in the upper layer is pumped to the residual ammonia water tank B101, and then the ammonia distillation operation is carried out in the ammonia distillation tower. After the gas-phase output from the top of the ammonia distillation tower is cooled by the shrinker, the ammonia gas is sent to the saturator in the ammonium sulfate section to supplement the amount of ammonia. After heating, it is sent to biochemical treatment. The flow rate of this ammonia distillation waste water should be equal to the water volume of coke oven raw gas, which is determined by the water volume brought into the system by raw gas; the other stream is 700kg/h, pumped to the collection The top of the air pipe C101 is mixed with circulating tar and sprayed to ensure that the oil-water ratio (mass fraction) of tar to water spray is 1.2 to 2:1, and the mixed spray temperature is 90°C. Part of the oil phase in the mechanized clarification tank B104 enters the oil-water separator B105, and after oil-water separation, the oil phase enters the tar storage tank B106. the

Compared with the existing process, the present invention adds ammonia distilling waste water circulation and tar circulation, uses tar-water mixture to perform high-temperature quenching operation on raw coal gas in gas collection, changes the direct quenching effect of raw coal gas, and increases the gas temperature at the outlet of the gas collecting pipe. And equipped with a gas pre-cooler, under the premise of ensuring the same raw gas cooling effect (heat transfer effect) and decoking effect (mass transfer effect), the waste heat of the raw gas is recovered to produce 82-85 °C process heat medium water for use in Hot water type lithium bromide refrigeration unit generator heat source; in addition, due to the recovery of waste heat from raw gas before the primary cooler, compared with the existing process, the consumption of cold utilities for the primary cooler is greatly reduced. the

Claims (2)

1. A device for producing process heat medium water by direct rapid cooling of coking raw gas at high temperature, including gas collecting pipe, mechanized clarification tank A, mechanized clarification tank B, oil-water separator, tar storage tank, residual ammonia water tank, ammonia distillation tower, distillation Ammonia tower feed heat exchanger, gas precooler, hot water lithium bromide refrigeration unit and two-stage horizontal tube primary cooler; The condensate discharge of the gas collection pipe is connected to the mechanized clarifier A, the water phase discharge of the mechanized clarifier A is connected to the remaining ammonia water tank, and the oil phase discharge of the mechanized clarifier A is connected in two ways: (1) The oil phase of the mechanized clarifier A (2) The other outlet of the oil phase of the mechanized clarification tank A is connected to the inlet of the oil-water separator; the outlet of the residual ammonia water tank is connected to the inlet of the shell side of the feed heat exchanger of the ammonia distillation tower; The shell-side outlet of the feed heat exchanger of the ammonia distillation tower is connected to the feed port of the ammonia distillation tower; the gas phase at the top of the ammonia distillation tower is condensed by a shrinker and then desulfurized ammonia section; the ammonia distillation waste water at the bottom of the ammonia distillation tower is connected in two ways: (1 ) one way of ammonia distillation wastewater is connected to the gas collecting pipe; (2) the other way of ammonia distillation wastewater is connected to the inlet of the feed heat exchanger tube side of the ammonia distillation tower; the outlet material of the feed heat exchanger tube side of the ammonia distillation tower is sent to biochemical treatment; The gas phase discharge of the gas pipe is connected to the shell side inlet of the gas precooler; the condensate outlet of the gas precooler is connected to the feed port of the mechanical clarification tank B; the shell side outlet of the gas precooler is connected to the shell side inlet of the two-stage horizontal tube primary cooler Connected; two-stage horizontal tube primary cooler shell-side output is sent to the subsequent gas purification section; two-stage horizontal tube primary cooler condensate is connected in two ways: (1) two-stage horizontal tube primary cooler condensate one Return to the low-temperature water section for circulating spraying; (2) The other outlet of the condensate of the two-stage horizontal tube primary cooler is connected to the inlet of mechanized clarification tank B; the hot water outlet of the hot water lithium bromide refrigeration unit is connected to the gas precooler The inlet of the tube side is connected; the hot water inlet of the hot water type lithium bromide refrigeration unit is connected with the outlet of the gas precooler; the cold water outlet of the hot water type lithium bromide refrigeration unit is connected with the cold water inlet of the two-section horizontal tube primary cooler; The cold water inlet of the unit is connected to the cold water outlet of the two-stage horizontal tube primary cooler; the oil phase outlet of the mechanized clarification tank B is connected to the inlet of the oil-water separator; the outlet of the oil phase of the oil-water separator is connected to the inlet of the tar storage tank. 2. utilize the method for the said device of claim 1 to produce process heat medium water, it is characterized in that comprising the following steps: (1) The 650-700°C raw coal gas from the coke oven is quenched by mixed spraying of circulating tar and circulating ammonia distillation wastewater in the gas collector. The temperature of the condensate in the gas collecting pipe is 88～92℃, the condensate is pumped into the mechanized clarification tank A, the water phase of the mechanized clarification tank A is pumped to the residual ammonia water tank, and the oil phase is divided into two according to the ratio of 35～40:1. Road: The former is sent to the gas collection pipe and mixed with ammonia distillation wastewater to spray and quench; the latter is sent to the oil-water separator to remove water or sent to the tar storage tank; after quenching, the raw gas temperature is 88-92°C, and it enters the gas pre-cooler for further cool down; (2) The 88-92°C raw gas from the gas collecting pipe enters the shell side from the bottom of the gas pre-cooler, and the 72-78°C circulating hot water is fed into the top tube side of the gas pre-cooler, and the raw gas and the circulating hot water are exchanged countercurrently Heat, raw coal gas heat exchange to 82 ~ 85 ℃, and then enter the two-section horizontal tube primary cooler through the top tube outlet of the gas precooler to cool; the circulating hot water is heated to 82 ~ 85 ℃, and sent to the hot water type lithium bromide The refrigerating unit is used as the heat source of the lithium bromide refrigerating unit generator; the 72-78 ℃ hot water after heating is pumped back to the gas pre-cooler to circulate heat to produce process heat medium water; the condensate of the gas pre-cooler is pumped from the bottom condensate outlet Mechanized clarifier B; (3) The 82-85°C raw gas from the raw gas precooler enters the shell side from the top of the two-stage horizontal tube primary cooler, and the upper and lower sections of the two-stage horizontal tube primary cooler are respectively fed by 35°C circulating water Cool with 16°C low-temperature water, and finally cool to 22-25°C and send it to the subsequent gas purification section; the 16°C low-temperature water used for cooling in the lower section is supplied by a hot-water lithium bromide refrigeration unit, and the 23°C low-temperature water is returned to the hot-water type after heat exchange Lithium bromide refrigeration unit; the condensate is pumped into the mechanical clarification tank B from the condensate outlet at the bottom of the two-stage horizontal tube primary cooler; (4) The condensate collected by the gas precooler and the two-stage horizontal tube primary cooler is clarified and divided into three layers in the mechanized clarification tank B, the upper layer is ammonia water, the middle layer is tar, and the lower layer is tar residue; the upper layer ammonia water pump to the remaining ammonia water tank, and then carry out ammonia distillation operation in the ammonia distillation tower; after the gas phase discharge from the top of the ammonia distillation tower is cooled by the shrinker, the ammonia gas is sent to the ammonium sulfate section saturator to supplement the amount of ammonia, and the ammonia distillation wastewater at the bottom of the ammonia distillation tower There are two streams of output, and the distribution ratio is 1:6~8: the former is sent to biochemical treatment after exchanging heat with the feed of the ammonia distillation tower. The flow rate of this ammonia distillation waste water should be equal to the water volume of the coke oven raw gas, which is determined by The amount of water brought into the system by raw coal gas is determined; the latter is pumped to the top of the gas collecting pipe and mixed with circulating tar to ensure that the mass ratio of tar to water spray is 1.2 to 2:1, and the mixed spray temperature is 88 to 92 °C ; Part of the oil phase in the mechanized settling tank B enters the oil-water separator, and after oil-water separation, the oil phase enters the tar storage tank.