Three-stage heat exchange system for deamination treatment of semi-coke wastewater
The three-stage heat exchange system enables the cascade utilization of thermal energy in the ammonia removal treatment of semi-coke wastewater, solving the problem of insufficient thermal energy utilization in existing technologies, improving heat exchange efficiency and reducing production costs.
Patent Information
- Application Number
- CN202520135418.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-01-21
- Publication Date
- 2025-12-26
- Estimated Expiration
- 2035-01-21
AI Technical Summary
The existing process for deammoniation treatment of semi-coke wastewater does not fully utilize thermal energy, resulting in high energy consumption, complex equipment, and increased costs.
A three-stage heat exchange system is adopted, including an ammonia removal tower, a first heat exchange structure, a second heat exchange structure, and a third heat exchange structure. Through multi-stage cascade utilization of thermal energy, heat recovery of phenolic water and coal gas water and multiple heating of coal gas water are realized.
It improves heat exchange efficiency, reduces dependence on external heat sources, lowers equipment operating load and maintenance costs, and saves production costs.
Smart Images
Figure CN223726927U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model belongs to heat exchange device or equipment technical field, specifically relates to a tertiary heat exchange system for coke wastewater deamination treatment. BACKGROUND
[0002] A large amount of coke wastewater is generated during the production of coke (semi-coke), which contains harmful substances such as high-concentration ammonia nitrogen, phenols, cyanide, and polycyclic aromatic hydrocarbons. These harmful substances not only cause serious environmental pollution, but also threaten ecological balance and human health.
[0003] In the treatment process of coke wastewater, deamination is a key step. The deamination process not only removes ammonia nitrogen from wastewater, but also recovers ammonia resources, which has important environmental and economic significance. However, existing deamination technologies have some problems in treating coke wastewater, such as high energy consumption, low heat exchange efficiency, and complex equipment. Especially in the deamination process, a large amount of heat energy is generated, which will lead to energy waste and increase the operating cost of the entire treatment system if not effectively recovered and utilized.
[0004] In the deamination process, the traditional heat exchange system usually adopts a single or simple heat exchange structure, which cannot fully utilize the large amount of heat energy generated in the deamination process, resulting in low overall energy efficiency of the system. For example, coal gas water is used as the feed of the deamination tower and needs to be preheated to a certain temperature before entering the deamination tower to improve the deamination efficiency. In the traditional deamination system, the coal gas water is usually only once exchanged with the high-temperature phenol water discharged from the bottom of the deamination tower to absorb the heat released by the phenol water, thereby achieving preheating. However, this preheating process is often insufficient, and the temperature of the coal gas water may not reach the ideal deamination temperature, requiring additional steam or other heat sources for supplementary heating. SUMMARY
[0005] The technical problem to be solved by the utility model is to overcome the shortcomings of the prior art and provide a tertiary heat exchange system for coke wastewater deamination treatment.
[0006] The technical scheme adopted to solve the above technical problems is: a tertiary heat exchange system for coke wastewater deamination treatment, comprising a deamination tower, a phenol water outlet at the bottom of the deamination tower connected to an inlet A of a first heat exchange structure, an outlet A of the first heat exchange structure connected to an inlet A of a second heat exchange structure, an outlet A of the second heat exchange structure connected to a phenol water output pipe, an inlet B of the second heat exchange structure connected to a coal gas water raw material pipe, an outlet B of the second heat exchange structure connected to an inlet A of a third heat exchange structure, an outlet A of the third heat exchange structure connected to an inlet B of the first heat exchange structure, an inlet B of the third heat exchange structure connected to a deamination tower side steam pipe, an outlet B connected to a steam condensate pipe, and an outlet B of the first heat exchange structure connected to a deamination tower raw material inlet.
[0007] As a preferred technical solution, the first heat exchange structure is same as the second heat exchanger structure.
[0008] As a preferred technical solution, the first heat exchange structure is composed of heat exchanger I, heat exchanger II, heat exchanger III and heat exchanger IV in series, and a gate valve A is arranged between the liquid inlet a1 of the heat exchanger I and the liquid outlet b2 of the heat exchanger II through a pipeline, and a gate valve B is arranged between the liquid outlet d1 of the heat exchanger I and the liquid inlet c2 of the heat exchanger II through a pipeline; a gate valve C is arranged between the liquid inlet a3 of the heat exchanger III and the liquid outlet b4 of the heat exchanger IV through a pipeline, and a gate valve D is arranged between the liquid outlet d3 of the heat exchanger III and the liquid inlet c4 of the heat exchanger IV through a pipeline.
[0009] As a preferred technical solution, the third heat exchange structure is a condenser.
[0010] The beneficial effects of the present application are as follows:
[0011] The present application adopts a three-stage heat exchange structure, and through the synergistic effect of multiple heat exchange stages, the cascade utilization of heat energy is realized. The heat of high-temperature phenol water is preliminarily recovered in the first heat exchange structure and used for the third time to heat the coal gas water; the coal gas water exchanges heat with the cooled phenol water in the second heat exchange structure, and the heat of the phenol water is recovered again; the coal gas water exchanges heat with the side steam of the deamination tower in the third heat exchange structure, and the secondary heating is completed. This multi-stage heat exchange design makes the utilization of heat energy more sufficient, and significantly improves the heat exchange efficiency of the whole system.
[0012] Compared with the traditional deamination heat recovery system, the present application can fully utilize the heat energy generated in the deamination process, and reduce the dependence on external heat sources (such as steam). At the same time, the reasonable layout and efficient operation of each heat exchange structure in the system reduce the operating load and maintenance cost of the equipment, and further save the production cost. BRIEF DESCRIPTION OF DRAWINGS
[0013] Figure 1 is a structural schematic diagram of the present application.
[0014] Figure 2 is a structural schematic diagram of the first heat exchange structure of the present application.
[0015] Among them, the deamination tower 1, the first heat exchange structure 2, the third heat exchange structure 3, the second heat exchange structure 4, the heat exchanger I 21, the gate valve B 22, the heat exchanger II 23, the heat exchanger III 24, the gate valve D 25, the heat exchanger IV 26, the gate valve C 27, and the gate valve A 28. DETAILED DESCRIPTION
[0016] The utility model is further explained in detail below in combination with the drawings and embodiments, but the utility model is not limited to the following embodiments.
[0017] In Figure 1 The third heat exchange system for the ammonia removal treatment of semi-coke wastewater in the embodiment comprises a deaminization tower 1, a first heat exchange structure 2, a second heat exchange structure 4, and a third heat exchange structure 3. The phenol water outlet at the bottom of the deaminization tower 1 is connected with the inlet A of the first heat exchange structure 2. The outlet A of the first heat exchange structure 2 is connected with the inlet A of the second heat exchange structure 4. The outlet A of the second heat exchange structure 4 is connected with a phenol water output pipe. The inlet B of the second heat exchange structure 4 is connected with a coal gas water raw material pipe. The outlet B of the second heat exchange structure 4 is connected with the inlet A of the third heat exchange structure 3. The outlet A of the third heat exchange structure 3 is connected with the inlet B of the first heat exchange structure 2. The inlet B of the third heat exchange structure 3 is connected with a deaminization tower 1 side steam pipe, and the outlet B is connected with a steam condensate pipe. The outlet B of the first heat exchange structure 2 is connected with a deaminization tower 1 raw material inlet.
[0018] The first heat exchange structure 2 in the embodiment is composed of heat exchanger I 21, heat exchanger II 23, heat exchanger III 24, and heat exchanger IV 26 connected in series. A gate valve A 28 is arranged between the liquid one inlet a1 of the heat exchanger I 21 and the liquid one outlet b2 of the heat exchanger II 23 through a pipeline. A gate valve B 22 is arranged between the liquid two outlet d1 of the heat exchanger I 21 and the liquid two inlet c2 of the heat exchanger II 23 through a pipeline. A gate valve C 27 is arranged between the liquid one inlet a3 of the heat exchanger III 24 and the liquid one outlet b4 of the heat exchanger IV 26 through a pipeline. A gate valve D 25 is arranged between the liquid two outlet d3 of the heat exchanger III 24 and the liquid two inlet c4 of the heat exchanger IV 26 through a pipeline. The first heat exchange structure 2 is used for the heat exchange between high-temperature phenol water and coal gas water. The gate valve A 28, the gate valve B 22, the gate valve C 27, and the gate valve D 25 are used for adjusting the combination mode of the heat exchangers according to the needs and improving the flexibility of the system.
[0019] The second heat exchange structure 4 in the embodiment is the same as the first heat exchange structure and is used for the primary heating of coal gas water and the secondary cooling of phenol water.
[0020] The third heat exchange structure 3 in the embodiment is a partial condenser and is used for the secondary heating of coal gas water and the condensation of the deaminization tower 1 side steam.
[0021] The working principle of the embodiment is as follows:
[0022] The coal gas water raw material enters the second heat exchange structure 4 to exchange heat with the heat-exchanged phenol water, wherein the coal gas water raw material is heated for the first time, and the phenol water is outputted after being cooled for the second time through a phenol water output pipe. The coal gas water raw material enters the third heat exchange structure 3 to exchange heat with the steam outputted from the side of the deamination tower 1, the coal gas water raw material is heated for the second time, and the steam is cooled and condensed. The coal gas water raw material enters the first heat exchange structure 2 to exchange heat with the high-temperature phenol water, wherein the coal gas water raw material is heated for the third time and then enters the deamination tower 1, and the high-temperature phenol water is cooled for the first time.
Claims
1. A three-stage heat exchange system for the deamination treatment of semi-coke wastewater, comprising a deamination tower, characterized in that, The phenol water outlet at the bottom of the deamination tower is connected with the inlet A of the first heat exchange structure, the outlet A of the first heat exchange structure is connected with the inlet A of the second heat exchange structure, the outlet A of the second heat exchange structure is connected with a phenol water output pipe, the inlet B of the second heat exchange structure is connected with a coal gas water raw material pipe, the outlet B of the second heat exchange structure is connected with the inlet A of the third heat exchange structure, the outlet A of the third heat exchange structure is connected with the inlet B of the first heat exchange structure, the inlet B of the third heat exchange structure is connected with a deamination tower side steam pipe, and the outlet B is connected with a steam condensate pipe, and the outlet B of the first heat exchange structure is connected with a deamination tower raw material inlet.
2. The three-stage heat exchange system for the ammonia removal treatment of semicoke wastewater according to claim 1, characterized in that, The first heat exchange structure is the same as the second heat exchange structure.
3. The three-stage heat exchange system for the ammonia removal treatment of semicoke wastewater according to claim 1 or 2, characterized in that, The first heat exchange structure is composed of heat exchanger I, heat exchanger II, heat exchanger III and heat exchanger IV in series, a gate valve A is arranged between the liquid inlet a1 of heat exchanger I and the liquid outlet b2 of heat exchanger II through a pipeline, and a gate valve B is arranged between the liquid outlet d1 of heat exchanger I and the liquid inlet c2 of heat exchanger II through a pipeline; a gate valve C is arranged between the liquid inlet a3 of heat exchanger III and the liquid outlet b4 of heat exchanger IV through a pipeline, and a gate valve D is arranged between the liquid outlet d3 of heat exchanger III and the liquid inlet c4 of heat exchanger IV through a pipeline.
4. The three-stage heat exchange system for the ammonia removal treatment of semicoke wastewater according to claim 1, characterized in that, The third heat exchange structure is a partial condenser.