Energy-saving deacidification and ammonia distillation process and device

Abstract

The present invention relates to the technical field of industrial wastewater treatment, and in particular to an energy-saving deacidification and ammonia distillation process and device. The residual ammonia water from coking is cooled by a residual ammonia water cooler and then enters the top of the upper tower section of the deacidification and ammonia distillation tower for ammonia distillation operation; the vapor phase discharge part of the top of the deacidification and ammonia distillation tower is sent to the pre-desulfurization coal gas pipeline or ammonium sulfate saturator; the concentrated ammonia vapor is extracted from the side line in the middle of the deacidification and ammonia distillation tower and enters the vapor-liquid separator to remove the tiny droplets that may be entrained, and the liquid phase after vapor-liquid separation is discharged into the middle of the deacidification and ammonia distillation tower through the pipeline liquid seal; the vapor phase after vapor-liquid separation enters the ammonia condenser for condensation and cooling to become clean concentrated ammonia water; the wastewater at the bottom of the deacidification and ammonia distillation tower is pumped by a wastewater pump into a heat exchanger for heat exchange with circulating hot water, and then enters the wastewater cooler for cooling, and then is sent to the phenol-cyanide wastewater treatment device. It can not only greatly reduce the energy consumption and operating cost of coking ammonia distillation, but also has low equipment investment, low operating cost and simple process flow.

Description

Technical Field

[0001] The invention relates to the technical field of industrial wastewater treatment, and in particular to an energy-saving deacidification and ammonia distillation process and device. Background Art

[0002] The composition of residual ammonia water from coking is complex, and the impurity ammonia exists in three forms: free NH3, volatile ammonium salts and fixed ammonium salts. Volatile ammonium salts are mainly ammonium carbonate, ammonium sulfide, ammonium cyanide, etc. Volatile ammonium salts are easily decomposed into ammonia, hydrogen sulfide, carbon dioxide, hydrogen cyanide and other gases when heated, but fixed ammonium salts require the addition of alkali to decompose.

[0003] At present, the residual ammonia water in coking is mostly deaminated by steam stripping, and the evaporated ammonia vapor is sent to the gas pipeline or saturator before the desulfurization unit, or made into concentrated ammonia water for sale. The steam stripping deammoniation process is mature and widely used, but this method has high steam consumption and high operating costs, and the general coking ammonia evaporation process is a pure energy input, and no product profit can be obtained.

[0004] At present, the commonly used residual ammonia distillation processes in the coking industry generally include conventional atmospheric pressure ammonia distillation process and heat pump ammonia distillation process; the conventional atmospheric pressure ammonia distillation process is mature in technology and stable in operation, but this process consumes a large amount of steam, about 170 to 200 kg of low-pressure steam is consumed for each ton of residual ammonia water treated, which consumes a lot of energy and has a high operating cost. In order to reduce the energy consumption of ammonia distillation, the heat pump ammonia distillation process uses the second type of absorption heat pump to recover the latent heat of ammonia vapor at the top of the ammonia distillation tower to heat the wastewater at the bottom of the tower, providing part of the heat source and saving the energy consumption of ammonia distillation. This process can reduce the operating cost of ammonia distillation by 34%, but this process adds more equipment, the fixed equipment investment is large, and the ammonia distillation operation becomes more complicated. Summary of the invention

[0005] In order to overcome the deficiencies of the prior art, the present invention provides an energy-saving deacidification ammonia evaporation process and device, which can not only significantly reduce the energy consumption and operating costs of coking ammonia evaporation, but also require less equipment investment, low operating costs and simple process flow.

[0006] In order to achieve the above object, the present invention adopts the following technical solutions:

[0007] An energy-saving deacidification and ammonia distillation process specifically comprises the following steps:

[0008] 1) The residual ammonia water from coking is cooled in the residual ammonia water cooler and then enters the top of the upper tower section of the deacidification ammonia distillation tower for ammonia distillation operation; the vapor phase discharge from the top of the deacidification ammonia distillation tower is sent to the pre-desulfurization coal gas pipeline or ammonium sulfate saturator;

[0009] 2) The concentrated ammonia vapor is extracted from the side line in the middle of the deacidification ammonia still tower and enters the vapor-liquid separator to remove the tiny droplets that may be entrained. The liquid phase after vapor-liquid separation is discharged into the middle of the deacidification ammonia still tower through the pipeline liquid seal;

[0010] 3) After the vapor-liquid separation, the vapor phase enters the ammonia condenser for condensation and cooling to become clean concentrated ammonia water;

[0011] 4) The wastewater at the bottom of the deacidification and ammonia distillation tower is pumped into the heat exchanger through the wastewater pump to exchange heat with the circulating hot water, and then enters the wastewater cooler for cooling before being sent to the phenol-cyanide wastewater treatment device.

[0012] Furthermore, in step 1), the temperature of the residual ammonia water entering the top of the upper tower section of the deacidification ammonia distillation tower is 60°C to 66°C; the pressure at the top of the deacidification ammonia distillation tower is 20kPag to 50kPag; and the temperature of the ammonia-containing vapor coming out of the top of the deacidification ammonia distillation tower is 85°C to 102°C.

[0013] Furthermore, in step 2), the temperature of concentrated ammonia vapor extracted from the middle side line of the deacidification ammonia distillation tower is 102°C to 110°C.

[0014] Furthermore, in step 2), the mass fraction of ammonia in the concentrated ammonia vapor extracted from the middle side line of the deacidification ammonia distillation tower is 15% to 25%.

[0015] Furthermore, in step 4), the temperature of the wastewater at the bottom of the deacidification and ammonia distillation tower is 110°C to 120°C.

[0016] Furthermore, in step 4), the temperature of the waste water at the bottom of the deacidification and ammonia distillation tower after heat exchange with the circulating hot water is 70°C.

[0017] Furthermore, in step 4), the wastewater at the bottom of the deacidification and ammonia distillation tower is pumped into a heat exchanger through a wastewater pump to exchange heat with circulating hot water at 63°C to 73°C, and then enters a wastewater cooler to be cooled to 40±2°C.

[0018] An energy-saving deacidification and ammonia distillation device comprises a deacidification and ammonia distillation tower, a reboiler, a residual ammonia water cooler, a No. 1 waste hot water heat exchanger, a waste water cooler, a vapor-liquid separator, a No. 2 waste hot water heat exchanger and an ammonia condenser; the bottom of the deacidification and ammonia distillation tower, the No. 1 waste hot water heat exchanger, the waste water cooler and a phenol-cyanide waste water treatment device are connected in sequence by pipelines; the residual ammonia water pipeline, the residual ammonia water cooler and the top of the deacidification and ammonia distillation tower are connected in sequence by pipelines; the top of the deacidification and ammonia distillation tower is connected to a pre-desulfurization coal gas pipeline or an ammonium sulfate saturator pipeline of an ammonium sulfate process; the middle of the deacidification and ammonia distillation tower, a vapor-liquid separator, a No. 2 waste hot water heat exchanger and an ammonia condenser are connected in sequence by pipelines; the waste water pipeline at the bottom of the deacidification and ammonia distillation tower is connected to a reboiler pipeline, and the reboiler outlet is connected to a vapor phase space pipeline at the bottom of the deacidification and ammonia distillation tower.

[0019] Furthermore, it also includes a wastewater pump, the bottom of the deacidification and ammonia distillation tower is connected to the wastewater pump inlet pipeline; the wastewater pump outlet is connected to the 1# waste hot water heat exchanger pipeline.

[0020] Furthermore, the liquid phase interface end of the vapor-liquid separator is connected to the middle pipeline of the deacidification and ammonia distillation tower; the gas phase interface end of the vapor-liquid separator is connected to the ammonia vapor inlet pipeline of the 2# waste hot water heat exchanger.

[0021] Compared with the prior art, the present invention has the following beneficial effects:

[0022] 1. In terms of energy saving, the process of the invention only consumes 135kg steam / ton of residual ammonia water, compared with the traditional ammonia evaporation process which consumes 170kg-200kg steam / ton of residual ammonia water, saving about 32% of steam consumption; in terms of circulating water consumption, compared with the traditional coking ammonia evaporation process which consumes about 8t-9t of circulating water / ton of residual ammonia water, the circulating water consumption is low, only 3.3t of circulating water / ton of residual ammonia water, saving 63% of circulating water consumption.

[0023] 2. In terms of waste heat recovery, unlike the existing ammonia evaporation technology, this process can recover 5.8t of circulating hot water per ton of residual ammonia water. The circulating hot water recovered from the waste heat of ammonia evaporation can be used to provide heat source for the coking plant's refrigeration machine in summer or heating in winter, or as a heat source for the vacuum potassium carbonate desulfurization regeneration tower, which greatly improves the energy utilization rate of the coking plant itself and reduces the operating costs of the production enterprise.

[0024] 3. In terms of equipment investment, compared with the conventional atmospheric pressure ammonia distillation process, the process of this invention uses the cooled residual ammonia water as the top cold reflux liquid, and directly transfers mass and heat with the rising stripping steam in the tower. There is no need to set up an additional top expander of the ammonia distillation tower, which reduces the use of titanium materials for the expander. The residual ammonia water cooler can be made of carbon steel. This process reduces equipment investment.

[0025] 4. In terms of equipment layout, unlike the existing ammonia evaporation technology in which the ammonia splitter is set on the top of the ammonia evaporation tower, the residual ammonia water cooler of this process can be set on the ground, which not only further reduces the strength requirements of the ammonia evaporation tower, but also reduces the requirements for operators to operate on the top of the tower.

[0026] According to the present invention, after the remaining ammonia water is cooled, all of the ammonia water enters the top of the deacidification ammonia distillation tower, and clean ammonia vapor is extracted from the side line in the middle of the deacidification ammonia distillation tower to prepare relatively clean concentrated ammonia water. The waste heat of the ammonia vapor extracted from the side line and the waste heat of the waste water at the bottom of the deacidification ammonia distillation tower can be used to prepare hot water at 63-73°C for heat recovery and utilization, which can provide a heat source for the refrigeration machine in the coking plant in summer or heating in winter, thereby improving the utilization rate of the coking waste heat. The invention is an ammonia distillation process with low equipment investment, low operating cost and simple process flow. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 It is a schematic diagram of the structure and process principle of the present invention.

[0028] In the figure: 1-deacidification ammonia distillation tower, 2-reboiler, 3-wastewater pump, 4-residual ammonia water cooler, 5-1# waste hot water heat exchanger, 6-wastewater cooler, 7-gas-liquid separator, 8-2# waste hot water heat exchanger, 9-ammonia condenser. DETAILED DESCRIPTION

[0029] The present invention discloses an energy-saving deacidification and ammonia distillation process. Those skilled in the art can refer to the content of this article and appropriately improve the process parameters to achieve it. It is particularly important to point out that all similar substitutions and modifications are obvious to those skilled in the art, and they are all considered to be included in the present invention. The method and application of the present invention have been described through preferred embodiments, and relevant personnel can obviously modify or appropriately change and combine the methods and applications described herein without departing from the content, spirit and scope of the present invention to implement and apply the technology of the present invention.

[0030] The specific implementation of the present invention will be further described below in conjunction with the accompanying drawings:

[0031] like Figure 1 As shown, an energy-saving deacidification and ammonia distillation device includes a deacidification and ammonia distillation tower 1, a reboiler 2, a wastewater pump 3, a residual ammonia water cooler 4, a 1# waste hot water heat exchanger 5, a wastewater cooler 6, a vapor-liquid separator 7, a 2# waste hot water heat exchanger 8, and an ammonia condenser 9.

[0032] The bottom of the deacidification and ammonia distillation tower 1 is connected to the inlet pipe of the wastewater pump 3, and the outlet of the wastewater pump 3 is connected to the pipe of the 1# waste hot water heat exchanger 5; the outlet of the 1# waste hot water heat exchanger 5 is connected to the inlet pipe of the wastewater cooler 6; the wastewater outlet of the wastewater cooler 6 is connected to the pipe of the phenol-cyanide wastewater treatment device.

[0033] The residual ammonia water pipeline is connected to the ammonia water inlet pipeline of the residual ammonia water cooler 4; the ammonia water outlet of the residual ammonia water cooler 4 is connected to the top pipeline of the deacidification ammonia distillation tower 1; the top of the deacidification ammonia distillation tower 1 is connected to the pre-desulfurization coal gas pipeline or the ammonium sulfate saturator pipeline of the ammonium sulfate process.

[0034] The middle part of the deacidification ammonia distillation tower 1 is connected to the pipeline of the vapor-liquid separator 7; the liquid phase interface end of the vapor-liquid separator 7 is connected to the middle part of the pipeline of the deacidification ammonia distillation tower 1; the gas phase interface end of the vapor-liquid separator 7 is connected to the ammonia vapor inlet pipeline of the 2# waste hot water heat exchanger 8; the ammonia vapor outlet of the 2# waste hot water heat exchanger 8 is connected to the pipeline of the ammonia condenser 9.

[0035] The waste water pipeline at the bottom of the deacidification and ammonia distillation tower 1 is connected to the pipeline of the reboiler 2; the outlet of the reboiler 2 is connected to the vapor phase space pipeline at the bottom of the deacidification and ammonia distillation tower 1.

[0036] An energy-saving deacidification and ammonia distillation process specifically comprises the following steps:

[0037] 1. The residual ammonia water from coking is cooled by the residual ammonia water cooler 4 and then enters the top of the upper tower section of the deacidification ammonia distillation tower 1 for ammonia distillation operation; the vapor phase discharge from the top of the deacidification ammonia distillation tower 1 is sent to the pre-desulfurization coal gas pipeline or the ammonium sulfate saturator.

[0038] The temperature of the residual ammonia water entering the top of the upper tower section of the deacidification ammonia distillation tower 1 is 60°C to 66°C; the pressure at the top of the deacidification ammonia distillation tower 1 is 20kPag to 50kPag; the temperature of the ammonia-containing vapor coming out of the top of the deacidification ammonia distillation tower 1 is 85°C to 102°C.

[0039] 2. The concentrated ammonia vapor is extracted from the side line in the middle of the deacidification ammonia distillation tower 1 and enters the vapor-liquid separator 7 to remove the tiny droplets that may be entrained. The liquid phase after vapor-liquid separation is discharged into the middle of the deacidification ammonia distillation tower 1 through the pipeline liquid seal.

[0040] The temperature of concentrated ammonia vapor produced from the middle side line of the deacidification ammonia still 1 is 102° C. to 110° C.; the mass fraction of ammonia in the concentrated ammonia vapor produced from the middle side line of the deacidification ammonia still 1 is 15% to 25%.

[0041] 3. After the vapor-liquid separation, the vapor phase enters the ammonia condenser 9 for condensation and cooling to become clean concentrated ammonia water.

[0042] 4. The waste water at the bottom of the deacidification and ammonia distillation tower 1 is pumped into the circulating hot water (63°C-73°C) by the waste water pump 3, and then enters the waste water cooler 6 to be cooled to about 40°C, and then sent to the phenol-cyanide waste water treatment device.

[0043] The temperature of the waste water at the bottom of the deacidification ammonia distillation tower 1 is 110°C to 120°C; the temperature of the waste water at the bottom of the deacidification ammonia distillation tower 1 after heat exchange with circulating hot water is 70°C.

[0044] [Example]

[0045] In this embodiment, the treatment of 100 tons / hour of coking residual ammonia water is taken as an example, in which the impurities contain: volatile NH3: 2.5g / L, fixed NH3: 2.5g / L, H2S: 0.3g / L, CO2: 2g / L, HCN: 0.2g / L.

[0046] The residual ammonia water is cooled to 63°C by the residual ammonia water cooler and enters the top of the deacidification ammonia distillation. The top temperature of the deacidification ammonia distillation is 98°C and the pressure is 50kPag.

[0047] The ammonia mass concentration of ammonia vapor produced from the middle side line of deacidification and ammonia distillation is 20%, and the total amount of other acidic impurities in the ammonia vapor is less than 0.1%. The steam temperature is 107°C and the pressure is 57kPag. After gas-liquid separation, it enters the 2# waste hot water heat exchanger and exchanges heat with circulating hot water at 63°C to 73°C to 70°C, and then enters the ammonia condenser for further cooling to about 40°C.

[0048] The wastewater at the bottom of the deacidification and ammonia distillation tower is heat exchanged with 63℃~73℃ circulating hot water in the 1# waste hot water heat exchanger to 70℃, and then enters the wastewater cooler to be cooled to 40℃ and discharged to the phenol-cyanide wastewater treatment device.

[0049] In the above embodiment, the total ammonia content in the wastewater at the bottom of the deacidification ammonia distillation tower is less than 50 mg / L.

[0050] In the above embodiment, the steam consumption is 135 kg / ton of residual ammonia water, which saves 20.6% of low-pressure steam compared with the low-pressure steam consumption of 170 kg / ton of residual ammonia water in the traditional coking ammonia evaporation process; the circulating water consumption is 3.3 t / ton of residual ammonia water, which saves 63% of circulating water compared with the circulating water consumption of 9 t / ton of residual ammonia water in the traditional coking ammonia evaporation process;

[0051] Economic benefit analysis of the process of the present invention: Taking the treatment of 100t / h of residual ammonia water, the ammonia content of the ammonia evaporation wastewater being controlled below 100mg / L, and the wastewater being cooled to 40°C and then discharged to biochemical treatment as an example, the energy consumption comparison of the four ammonia evaporation processes is shown in Table 1.

[0052] Table 1 Comparison of energy consumption and benefits of four ammonia distillation processes

[0053]

[0054] As can be seen from the above table, the operating costs of the four ammonia distillation processes are as follows: conventional atmospheric pressure ammonia distillation process > conventional deacidification ammonia distillation process > heat pump atmospheric pressure ammonia distillation process > energy-saving deacidification ammonia distillation process of the present invention. The energy-saving ammonia distillation process of the present invention reduces the total operating cost by 58.5% compared with the currently widely used conventional atmospheric pressure ammonia distillation process, which can greatly reduce the energy consumption of ammonia distillation in coking and other enterprises, and fundamentally solve the problems of high steam consumption and poor economic benefits of ammonia distillation units.

[0055] In terms of energy saving, the process of the invention only consumes 135kg of steam per ton of residual ammonia water, compared with the traditional ammonia evaporation process which consumes 170kg to 200kg of steam per ton of residual ammonia water, saving about 32% of steam consumption; in terms of circulating water consumption, compared with the traditional coking ammonia evaporation process which consumes about 8t to 9t of circulating water per ton of residual ammonia water, the circulating water consumption is low, only 3.3t of circulating water per ton of residual ammonia water, saving 63% of circulating water consumption.

[0056] In terms of waste heat recovery, unlike the existing ammonia evaporation technology, this process can recover 5.8t of circulating hot water per ton of residual ammonia water. The circulating hot water recovered from the waste heat of ammonia evaporation can be used to provide heat source for the coking plant's summer refrigeration machine or winter heating, or as a heat source for the vacuum potassium carbonate desulfurization regeneration tower, which greatly improves the energy utilization rate of the coking plant itself and reduces the operating costs of the production enterprise.

[0057] In terms of equipment investment, compared with the conventional atmospheric pressure ammonia distillation process, the process of the present invention utilizes the cooled residual ammonia water as the cold reflux liquid at the top of the tower, and directly transfers mass and heat with the rising stripping steam in the tower. There is no need to additionally set up a fractionator at the top of the ammonia distillation tower, which reduces the use of titanium materials for the fractionator. The residual ammonia water cooler can be made of carbon steel. This process reduces equipment investment.

[0058] In terms of equipment layout, unlike the existing ammonia evaporation technology in which the ammonia fractionator is set on the top of the ammonia evaporation tower, the residual ammonia water cooler in this process can be set on the ground, which not only further reduces the strength requirements of the ammonia evaporation tower, but also reduces the requirements for operators to operate on the top of the tower.

[0059] The present invention cools the remaining ammonia water and then all of the ammonia water enters the top of the deacidification ammonia distillation tower 1. The clean ammonia vapor is extracted from the side line in the middle of the deacidification ammonia distillation tower 1 to prepare relatively clean concentrated ammonia water. The waste heat of the ammonia vapor extracted from the side line and the waste heat of the waste water at the bottom of the deacidification ammonia distillation tower can be used to prepare hot water at 63-73° C. for heat recovery and utilization, which can provide a heat source for the refrigeration machine in the coking plant in summer or heating in winter, thereby improving the utilization rate of the coking waste heat. The invention is an ammonia distillation process with low equipment investment, low operating cost and simple process flow.

[0060] The above description is only a preferred specific implementation manner of the present invention, but the protection scope of the present invention is not limited thereto. Any technician familiar with the technical field can make equivalent replacements or changes according to the technical scheme and inventive concept of the present invention within the technical scope disclosed by the present invention, which should be covered by the protection scope of the present invention.

Claims

1. An energy-saving deacidification and ammonia distillation process, characterized in that: The specific steps include: 1) The residual ammonia water from coking is cooled in the residual ammonia water cooler and then enters the top of the upper tower section of the deacidification ammonia distillation tower for ammonia distillation operation; the vapor phase discharge from the top of the deacidification ammonia distillation tower is sent to the pre-desulfurization coal gas pipeline or ammonium sulfate saturator; The temperature of the residual ammonia water entering the top of the upper tower section of the deacidification ammonia distillation tower is 60℃~66℃; the pressure at the top of the deacidification ammonia distillation tower is 20kPag~50kPag; the temperature of the ammonia-containing vapor coming out of the top of the deacidification ammonia distillation tower is 85℃~102℃; 2) The concentrated ammonia vapor is extracted from the side line in the middle of the deacidification ammonia still tower and enters the vapor-liquid separator to remove the tiny droplets that may be entrained. After gas-liquid separation, it enters the 2# waste hot water heat exchanger and exchanges heat with circulating hot water at 63℃~73℃ to 70℃, and then enters the ammonia condenser for further cooling; the liquid phase after vapor-liquid separation is discharged into the middle of the deacidification ammonia still tower through the pipeline liquid seal; The temperature of concentrated ammonia vapor produced from the side line in the middle of the deacidification ammonia distillation tower is 102℃~110℃; 3) After the vapor-liquid separation, the vapor phase enters the ammonia condenser for condensation and cooling to become clean concentrated ammonia water; 4) The wastewater at the bottom of the deacidification and ammonia distillation tower is pumped into a heat exchanger through a wastewater pump to exchange heat with circulating hot water, then enters a wastewater cooler for cooling, and is then sent to a phenol-cyanide wastewater treatment device; The wastewater temperature at the bottom of the deacidification and ammonia distillation tower is 110℃~120℃; The temperature of the wastewater at the bottom of the deacidification and ammonia distillation tower after heat exchange with circulating hot water is 70°C; The wastewater at the bottom of the deacidification and ammonia distillation tower is pumped into the heat exchanger by the wastewater pump to exchange heat with circulating hot water at 63℃~73℃, and then enters the wastewater cooler to be cooled to 40±2℃.

2. The energy-saving deacidification and ammonia distillation process according to claim 1, characterized in that: In the step 2), the mass fraction of ammonia in the concentrated ammonia vapor extracted from the middle side line of the deacidification ammonia distillation tower is 15% to 25%.

3. An energy-saving deacidification and ammonia distillation process device according to claim 1, characterized in that: It includes a deacidification ammonia distillation tower, a reboiler, a residual ammonia water cooler, a 1# waste hot water heat exchanger, a waste water cooler, a vapor-liquid separator, a 2# waste hot water heat exchanger and an ammonia condenser; the bottom of the deacidification ammonia distillation tower, the 1# waste hot water heat exchanger, the waste water cooler and the phenol-cyanide wastewater treatment device are connected in sequence by pipelines; the residual ammonia water pipeline, the residual ammonia water cooler and the top of the deacidification ammonia distillation tower are connected in sequence by pipelines; the top of the deacidification ammonia distillation tower is connected to the pre-desulfurization coal gas pipeline or the ammonium sulfate saturator pipeline of the ammonium sulfate process; the middle part of the deacidification ammonia distillation tower, the vapor-liquid separator, the 2# waste hot water heat exchanger and the ammonia condenser are connected in sequence by pipelines; the waste water pipeline at the bottom of the deacidification ammonia distillation tower is connected to the reboiler pipeline, and the reboiler outlet is connected to the vapor phase space pipeline at the bottom of the deacidification ammonia distillation tower.

4. The energy-saving deacidification and ammonia distillation device according to claim 3, characterized in that: It also includes a wastewater pump, the bottom of the deacidification and ammonia distillation tower is connected to the wastewater pump inlet pipe; the wastewater pump outlet is connected to the 1# waste hot water heat exchanger pipe.

5. The energy-saving deacidification and ammonia distillation device according to claim 3, characterized in that: The liquid phase interface end of the vapor-liquid separator is connected to the middle pipeline of the deacidification and ammonia distillation tower; the gas phase interface end of the vapor-liquid separator is connected to the ammonia vapor inlet pipeline of the 2# waste hot water heat exchanger.

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