Saponification wastewater treatment system
By comprehensively utilizing equipment such as resin adsorption devices, pH adjustment systems, stripping towers, and hydrocyclones, the problem of removing suspended solids and organic matter from saponification wastewater has been solved, achieving efficient and energy-saving wastewater treatment and resource recovery, and ensuring that wastewater meets discharge standards.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2025-03-21
- Publication Date
- 2026-03-10
AI Technical Summary
Existing technologies are inefficient at removing suspended solids, volatile organic compounds, and residual chlorine from saponification wastewater, and they are energy-intensive, have insufficient resource recycling, and result in environmental pollution and low treatment efficiency.
The integrated treatment system consists of a resin adsorption device, a pH adjustment system, a stripping tower, a hydrocyclone, and a steam compressor. It removes suspended solids through resin adsorption, removes volatile organic compounds through the stripping tower, separates solid particles through the hydrocyclone, and improves energy utilization through the steam compressor, thereby achieving wastewater purification and resource recovery.
It achieves efficient removal of suspended solids and organic matter from saponification wastewater, adjusts pH value, reduces energy consumption, improves resource recycling rate, and ensures that wastewater meets discharge standards.
Smart Images
Figure CN223983563U_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The utility model relates to wastewater treatment technical field, concretely relates to saponification wastewater treatment system. BACKGROUND
[0002] Saponification wastewater is a kind of high-concentration organic wastewater commonly seen in chemical production, mainly derived from by-products and unreacted raw materials generated during saponification reaction. Saponification wastewater contains various pollutants such as trichloroethane, 1,1-dichloroethylene, sodium hydroxide, residual chlorine, and flocculants such as self-polymer. It has characteristics such as high salt content, high COD (chemical oxygen demand), and high suspended solids (SS). These pollutants not only cause serious pollution to the environment, but also increase the difficulty of wastewater treatment. Traditional saponification wastewater treatment methods usually include physical, chemical, and biological treatment technologies, but these methods have low efficiency, high energy consumption, and equipment prone to scaling and clogging when treating high-salt and high-COD wastewater, making it difficult to meet the requirements of modern industry for efficient, energy-saving, and environmentally friendly wastewater treatment.
[0003] Specifically, the typical water quality characteristics of saponification wastewater are: salt content between 13% and 25%, hardness ≤100 mg / l, suspended solids (SS) ≤100 mg / l, COD ≤5000 mg / l, pH value between 9 and 12, and feed temperature of 70°C. When the suspended solids content in wastewater increases, it can easily lead to system scaling and clogging, shorten the cleaning cycle, and affect the quality of salt products and evaporation efficiency. Therefore, how to effectively remove suspended solids, adjust pH value, remove residual chlorine and organic matter from wastewater, and achieve concentration and resource recovery of high-salt wastewater has become a key technical problem in saponification wastewater treatment.
[0004] Traditional saponification wastewater treatment methods mainly include physical, chemical, and biological methods. Physical methods usually remove suspended solids and oil from wastewater through sedimentation, filtration, etc.; chemical methods remove organic matter and residual chlorine in wastewater through neutralization, oxidation-reduction, etc. by adding chemical agents; biological methods use microorganisms to degrade organic pollutants in wastewater. However, these traditional methods have many shortcomings in terms of treatment efficiency, energy consumption, and resource recovery. For example, physical methods can remove some suspended solids, but have limited effect on dissolved organic matter; chemical methods can effectively remove organic matter and residual chlorine, but consume a large amount of chemicals and can cause secondary pollution; biological methods have a long treatment period and are not ideal for treating high-concentration organic wastewater.
[0005] In addition, saponification wastewater often contains volatile organic compounds (such as trichloroethane and 1,1-dichloroethylene), which are difficult to remove effectively by traditional methods and can also pollute the atmospheric environment. Therefore, how to efficiently and energy-efficiently treat saponification wastewater and achieve resource recycling has become a problem that needs to be solved in the field of wastewater treatment.
[0006] Therefore, it has important practical significance and application value to develop a saponification wastewater treatment system which can effectively remove organic matter, suspended solids and residual chlorine in wastewater, and realize resource recycling. The utility model discloses a saponification wastewater treatment system
[0007] The utility model discloses a saponification wastewater treatment system
[0008] In order to solve the above -mentioned problem, the technical scheme of the utility model is:
[0009] The saponification wastewater treatment system, comprising a saponification wastewater pipeline, a resin adsorption device, a wastewater buffer tank, an acid pipeline, a sodium bisulfite adding mechanism, a pH adjusting circulating pump, a pH adjusting circulating pipeline, a wastewater discharge pipeline, a stripping tower, a top condenser, a separation tank, a vacuum pump, a condensate water outlet, a wastewater white tank, an oil phase outlet pipeline, a wastewater discharge tank, an external discharge pipeline, an original liquid tank, a bag filter, a condensate water preheater, a non-condensable gas preheater, a heater, a separator, a first circulating pipeline, a forced circulating pump, a washing tower, a backwashing tower, a second circulating pipeline, a cyclone, a thickener, a centrifuge, a mother liquor tank, a crystal discharge pipeline, a steam compressor, a fresh steam pipeline, a steam transportation pipeline, a condensate water buffer tank, a heat exchange water inlet pipeline, a heat exchange water return pipeline, a gas transportation pipeline, a non-condensable gas preheater, a non-condensable gas liquid separation device.
[0010] The hydrophobic tank separates the condensate in the pipeline, reduces the amount of condensate in the steam entering the compressor, wherein the two pipelines connected with the steam return pipeline of the hydrophobic tank, one pipeline passes the condensate in the steam return pipeline into the hydrophobic tank, and the other pipeline passes the steam in the hydrophobic tank back to the steam compressor for secondary utilization.
[0011] The condensate enters the condensate buffer tank and is transported to the steam compressor through the condensate transportation pipeline for cooling and energy recovery. The condensate in the condensate buffer tank also enters the condensate preheater through the heat exchange water inlet pipeline for preheating the raw liquid, further improving the energy utilization rate. The non-condensable gas at the top of the condensate buffer tank enters the non-condensable gas preheater through the gas transportation pipeline, and the raw liquid is preheated by using the waste heat of the non-condensable gas. At the same time, the heater is connected with the non-condensable gas preheater through the preheating steam pipeline, further recovering heat.
[0012] The resin adsorption device is two sets of resin adsorption devices arranged side by side.
[0013] Further, the sodium bisulfite adding mechanism comprises a sodium bisulfite preparation tank, a circulating water pipeline and a solid feeding pipeline connected to the sodium bisulfite preparation tank, and the sodium bisulfite preparation tank is connected to the condensate outlet of the vacuum pump through a vacuum condensate pipeline.
[0014] The sodium bisulfite preparation tank is connected to the condensate outlet of the vacuum pump through a vacuum condensate pipeline, and the condensate of the vacuum pump is recycled and utilized to prepare a sodium bisulfite solution, realizing efficient utilization of resources.
[0015] The pH adjusting circulating pump comprises a first pH adjusting circulating pump and a second pH adjusting circulating pump arranged side by side.
[0016] Further, an index detection pipeline is arranged on the pH adjusting circulating pipeline, the other end of the index detection pipeline is connected to the wastewater buffer tank, and a pH detection system and a residual chlorine content sampling test port are arranged on the index detection pipeline. The pH detection device and the residual chlorine content sampling test port are arranged on the index detection pipeline of the wastewater buffer tank, the pH value and the residual chlorine content are monitored in real time through the index detection pipeline, and the adjustment effect is ensured. The wastewater is circulated and mixed in the buffer tank through the pH adjusting circulating pump and the pH adjusting circulating pipeline, and the pH is uniformly distributed.
[0017] Further, the mother liquid tank is connected to a mother liquid treatment system.
[0018] Further, the upper outlet of the cyclone is connected to the upper inlet of the separator through a pipeline. The liquid at the upper part of the cyclone returns to the separator for re-separation, further improving the separation effect.
[0019] Further, the outlets of the cyclone and the thickener are respectively connected to the mother liquid tank.
[0020] The material from the discharge port of the cyclone and the thickener is usually directly introduced into the mother liquor tank without passing through the centrifuge, because the solid particle concentration in the material is low or the particle size is small, and the solid particles cannot be effectively separated by the centrifuge. After being directly introduced into the mother liquor tank, the material is specially treated by the mother liquor treatment system to avoid blockage or scaling of the subsequent system.
[0021] Further, the wastewater buffer tank is connected to a tail gas recovery system at the top.
[0022] Working principle:
[0023] The working process of the saponification wastewater treatment system starts from the introduction of wastewater into the system. First, the wastewater is introduced into the resin adsorption device through the saponification wastewater pipeline, where suspended solids (SS) in the wastewater are effectively removed. The treated water enters the wastewater buffer tank. In the wastewater buffer tank, the wastewater is subjected to pH adjustment and residual chlorine removal. Acid is added through the acid pipeline to adjust the pH to the neutral range, and sodium bisulfite is added through the sodium bisulfite preparation tank to remove trace residual chlorine. The sodium bisulfite preparation tank is connected to the condensate outlet of the vacuum pump through the vacuum condensate pipeline to recover and utilize the condensate of the vacuum pump for preparing sodium bisulfite solution, achieving efficient use of resources. The wastewater buffer tank is provided with a pH detection device and a residual chlorine content sampling test port on the index detection pipeline to monitor the pH value and residual chlorine content in real time through the index detection pipeline to ensure the adjustment effect. The wastewater in the buffer tank is circulated and mixed by the pH adjustment circulating pump and the pH adjustment circulating pipeline to ensure uniform distribution of pH. The adjusted wastewater is introduced into the stripping tower through the wastewater discharge pipeline. In the stripping tower, volatile organic compounds (such as trichloroethane and 1,1-dichloroethylene) in the wastewater are evaporated by the action of water vapor, condensed in the tower top condenser, and then introduced into the separation tank. In the separation tank, the condensed liquid is divided into oil phase and water phase. The oil phase is discharged through the bottom oil phase outlet pipeline, and the water phase enters the wastewater white tank. The gas at the top of the separation tank is introduced into the near-oxygen cracking equipment for further treatment by the vacuum pump.
[0024] The wastewater at the bottom of the stripping tower enters a wastewater discharge tank, part of the wastewater is discharged through a discharge pipeline, and the other part enters a raw solution tank for subsequent treatment. The wastewater is further removed of suspended solids through a bag filter, then preheated through a condensate preheater and a non-condensable gas preheater in turn, and finally enters a heater. In the heater, the wastewater is heated to an evaporation temperature to form steam and concentrated liquid, the steam and the concentrated liquid enter a separator, the steam returns to the bottom of the heater through a first circulation pipeline and a forced circulation pump to form a circulation, and the concentrated liquid enters a cyclone through a discharge pump. In the cyclone, the concentrated liquid is separated from solid particles by centrifugal force, the liquid at the upper part of the cyclone returns to the separator for re-separation, and the concentrated liquid at the bottom enters a thickener for further concentration. The materials discharged from the discharge ports of the cyclone and the thickener are directly introduced into the mother liquor tank without passing through the centrifuge, usually because the solid particle concentration in the materials is low or the particles are small, and the materials cannot be effectively separated by the centrifuge. The materials directly introduced into the mother liquor tank are specially treated by a mother liquor treatment system to avoid the solid particles from entering the subsequent system to cause blockage or scaling. If the solid particle concentration in the materials is high, the materials enter the centrifuge for further separation into solid salt and mother liquor, the solid salt is discharged through a crystal discharge pipeline, and the mother liquor enters the mother liquor tank for further treatment by the mother liquor treatment system.
[0025] The steam compressor is the core equipment of the MVR system, which compresses the low-temperature steam in the washing tower into high-temperature and high-pressure steam. The high-temperature steam enters the heater through a steam transportation pipeline to provide heat for the evaporation of wastewater. The washing tower is connected to the steam compressor through a steam return pipeline to return the steam in the washing tower to the steam compressor for re-compression and utilization, thereby improving energy efficiency. The condensate water generated by the steam compressor is separated through a drain tank, the un-condensed steam is returned to the steam compressor through a pipeline, the condensate water enters a condensate buffer tank, and is transported to the steam compressor through a condensate transportation pipeline for cooling and energy recovery. The condensate water in the condensate buffer tank also enters a condensate preheater through a heat exchange water inlet pipeline to preheat the raw solution, thereby further improving energy utilization. The non-condensable gas at the top of the condensate buffer tank enters a non-condensable gas preheater through a gas transportation pipeline to preheat the raw solution using the waste heat of the non-condensable gas. The heater is connected to the non-condensable gas preheater through a preheated steam pipeline to further recover heat. The gas in the non-condensable gas preheater finally enters a non-condensable gas liquid separation device for separation and treatment.
[0026] The beneficial effects of the utility model are as follows:
[0027] The whole system realizes efficient utilization of energy through the steam compressor and the preheater, reduces consumption of fresh steam, realizes effective separation of organic matters and solid particles in the wastewater through the stripping tower, the cyclone, the thickener and the centrifuge, and finally realizes the goal of wastewater purification and resource recycling. The condensed water generated at the bottom of the heater returns to the condensed water buffer tank through the pipeline for recycling and energy recovery, ensuring stable operation of the system. Through the above process, the saponification wastewater treatment system realizes the treatment goal of high efficiency, energy saving and environmental protection, ensures that the wastewater meets the discharge standard, and recovers valuable resources. BRIEF DESCRIPTION OF DRAWINGS
[0028] The accompanying drawings, which are included to provide a further understanding of the present application and constitute a part of this application, illustrate embodiments of the present application and together with the description serve to explain the principles of the present application. In the drawings:
[0029] Figure 1 FIG. 1 is a structural schematic diagram of a saponification wastewater treatment system according to the present application;
[0030] In the figure: 1, saponification wastewater pipeline; 2, resin adsorption device; 3, wastewater buffer tank; 301, first pH adjustment circulating pump; 302, second pH adjustment circulating pump; 4, acid pipeline; 5, sodium bisulfite preparation tank; 501, circulating water pipeline; 502, vacuum condensed water pipeline; 503, solid feeding pipeline; 6, tail gas recovery system; 7, pH adjustment circulating pipeline; 701, index detection pipeline; 702, wastewater discharge pipeline; 8, stripping tower; 9, tower top condenser; 10, separation tank; 11, vacuum pump; 12, near-oxygen cleavage equipment; 13, saponification kettle; 14, wastewater white tank; 15, wastewater discharge tank; 16, discharge pipeline; 17, raw liquid tank; 18, bag filter; 19, heater; 20, separator; 21, forced circulation pump; 22, discharge pump; 23, cyclone; 24, thickener; 25, centrifuge; 26, mother liquor tank; 27, crystal discharge pipeline; 28, mother liquor treatment system; 29, washing tower; 30, steam compressor; 31, first circulating pipeline; 32, circulating discharge pipeline; 33, second circulating pipeline; 34, steam return pipeline; 35, steam transportation pipeline; 36, fresh steam pipeline; 37, drain tank; 38, condensed water buffer tank; 39, heat exchange water inlet pipeline; 40, condensed water transportation pipeline; 41, condensed water preheater; 42, non-condensable gas preheater; 43, gas transportation pipeline; 44, preheated steam pipeline; 45, non-condensable gas gas-liquid separation device; 46, heat exchange water return pipeline; 47, washing circulating pipeline. DETAILED DESCRIPTION
[0031] The present application can be understood by the following embodiments.
[0032] Embodiment 1
[0033] As Figure 1As shown, the saponification wastewater treatment system comprises a saponification wastewater pipeline 1, the saponification wastewater pipeline 1 is connected with a wastewater buffer tank 3 through a resin adsorption device 2, the wastewater buffer tank 3 is provided with an acid pipeline 4 and a sodium bisulfite adding mechanism, the bottom of the wastewater buffer tank 3 is connected with the top of the wastewater buffer tank 3 through a pH adjusting circulating pump and a pH adjusting circulating pipeline 7, a wastewater discharge pipeline 702 is arranged on the pH adjusting circulating pipeline 7, the wastewater discharge pipeline 702 is connected with a stripping tower 8, the top of the stripping tower 8 is connected with a separation tank 10 through a tower top condenser 9, the top of the separation tank 10 is connected with a near-oxygen cracking device 12 through a vacuum pump 11, the condensate outlet of the vacuum pump 11 is connected with a saponification kettle 13, the middle part of the separation tank 10 is connected with a wastewater white tank 14 through a pipeline, and the bottom of the separation tank 10 is provided with an oil phase outlet pipeline; the bottom of the stripping tower 8 is connected with a wastewater discharge tank 15, the wastewater discharge tank 15 is connected with a discharge pipeline 16 and a raw liquid tank 17, the raw liquid tank 17 is sequentially connected with a bottom inlet of a heater 19 through a bag filter 18, a condensate preheater 41 and a non-condensable gas preheater 42, a top outlet of the heater 19 is connected with a separator 20, a liquid outlet of the separator 20 is connected with a bottom inlet of the heater 19 through a first circulating pipeline 31 and a forced circulating pump 21, a top outlet of the separator 20 is connected with a top inlet of a washing tower 29, a bottom outlet of the washing tower 29 is connected with an upper part of the washing tower 29 through a washing circulating pipeline 47, a second circulating pipeline 33 is arranged on the washing circulating pipeline 47 and connected with an upper part of the separator 20, a top of a hydrocyclone 23 is connected with the bottom of the separator 20 through a discharge pump 22, a circulating discharge pipeline 32 is arranged on the first circulating pipeline 31 and connected with an inlet of the discharge pump 22, the hydrocyclone 23 is connected with a centrifuge 25 through a thickener 24, a liquid outlet of the centrifuge 25 is connected with a mother liquor tank 26, a solid outlet of the centrifuge 25 is connected with a crystal discharge pipeline 27, the washing tower 29 is connected with a steam compressor 30 through a steam return pipeline 34, the steam compressor 30 is connected with a fresh steam pipeline 36, the steam compressor 30 is connected with the heater 19 through a steam transportation pipeline 35, the steam compressor 30 is connected with a condensate water buffer tank 38 through a condensate water buffer tank 38, the condensate water buffer tank 38 is connected with the steam compressor 30 through a condensate water transportation pipeline 40 and connected with the condensate preheater 41 through a heat exchange water inlet pipeline 39, a water outlet of the condensate preheater 41 is connected with the condensate water buffer tank 38 through a heat exchange water return pipeline 46, a top of the condensate water buffer tank 38 is connected with the non-condensable gas preheater 42 through a gas transportation pipeline 43, the heater 19 is connected with the non-condensable gas preheater 42 through a preheated steam pipeline 44, and the non-condensable gas preheater 42 is connected with a non-condensable gas liquid separation device 45.
[0034] The condensed water enters the condensed water buffer tank 38 and is transported to the steam compressor 30 through the condensed water transportation pipeline 40 for cooling and energy recovery. The condensed water in the condensed water buffer tank 38 also enters the condensed water preheater 41 through the heat exchange water inlet pipeline 39 for preheating the raw solution, further improving the energy utilization rate. The non-condensable gas at the top of the condensed water buffer tank 38 enters the non-condensable gas preheater 42 through the gas transportation pipeline 43, and the raw solution is preheated by using the waste heat of the non-condensable gas. At the same time, the heater 19 is connected to the non-condensable gas preheater 42 through the preheated steam pipeline 44, further recovering heat.
[0035] The resin adsorption device 2 is two sets of resin adsorption devices 2 arranged in parallel.
[0036] Further, the sodium bisulfite adding mechanism comprises a sodium bisulfite preparation tank 5, the sodium bisulfite preparation tank 5 is connected with a circulating water pipeline 501 and a solid feeding pipeline 503, and the sodium bisulfite preparation tank 5 is connected with the condensed water outlet of the vacuum pump 11 through a vacuum condensed water pipeline 502.
[0037] The sodium bisulfite preparation tank 5 is connected with the condensed water outlet of the vacuum pump 11 through the vacuum condensed water pipeline 502, and the condensed water of the vacuum pump 11 is recycled and used for preparing the sodium bisulfite solution, thereby realizing efficient use of resources.
[0038] The pH adjusting circulating pump comprises a first pH adjusting circulating pump 301 and a second pH adjusting circulating pump 302 arranged in parallel.
[0039] Further, the pH adjusting circulating pipeline 7 is provided with an index detection pipeline 701, the other end of the index detection pipeline 701 is connected with the wastewater buffer tank 3, and the index detection pipeline 701 is provided with a pH detection system and a residual chlorine content sampling test port. The pH detection device and the residual chlorine content sampling test port are arranged on the index detection pipeline 701 of the wastewater buffer tank 3, the pH value and the residual chlorine content are monitored in real time through the index detection pipeline 701, and the adjustment effect is ensured. The wastewater is circulated and mixed in the buffer tank through the pH adjusting circulating pump and the pH adjusting circulating pipeline 7, and the uniform distribution of the pH is ensured.
[0040] Further, the mother liquor tank 26 is connected with a mother liquor treatment system 28.
[0041] Further, the upper outlet of the cyclone 23 is connected with the upper inlet of the separator 20 through a pipeline. The liquid at the upper part of the cyclone 23 returns to the separator 20 for re-separation, and the separation effect is further improved.
[0042] Further, the outlets of the cyclone 23 and the thickener 24 are connected with the mother liquor tank 26, respectively.
[0043] The material from the discharge outlets of the cyclone 23 and the thickener 24 is directly introduced into the mother liquor tank 26 without passing through the centrifuge 25, usually because the solid particle concentration in the material is low or the particles are small, and the solid particles cannot be effectively separated by the centrifuge 25. The material directly introduced into the mother liquor tank 26 is specially treated by the mother liquor treatment system 28 to avoid the solid particles from entering the subsequent system to cause blockage or scaling.
[0044] Further, the top of the wastewater buffer tank 3 is connected to the tail gas recovery system 6.
[0045] Working principle:
[0046] The working process of the saponification wastewater treatment system starts from the entry of wastewater into the system. First, the wastewater is introduced into the resin adsorption device 2 through the saponification wastewater pipeline 1, where the suspended solids (SS) in the wastewater are effectively removed. The treated water enters the wastewater buffer tank 3. In the wastewater buffer tank 3, the wastewater is subjected to pH adjustment and residual chlorine removal. Acid is added through the acid pipeline 4 to adjust the pH to the neutral range, and sodium bisulfite is added through the sodium bisulfite preparation tank 5 to remove trace residual chlorine. The sodium bisulfite preparation tank 5 is connected to the condensate outlet of the vacuum pump 11 through the vacuum condensate pipeline 502 to recover and utilize the condensate of the vacuum pump 11 for preparing sodium bisulfite solution, achieving efficient use of resources. The pH detection device and residual chlorine content sampling test port are provided on the index detection pipeline 701 of the wastewater buffer tank 3 to monitor the pH value and residual chlorine content in real time through the index detection pipeline 701 to ensure the adjustment effect. The wastewater in the buffer tank is circulated and mixed by the pH adjustment circulating pump and the pH adjustment circulating pipeline 7 to ensure uniform distribution of pH. The adjusted wastewater is introduced into the stripping tower 8 through the wastewater discharge pipeline 702. In the stripping tower 8, volatile organic compounds (such as trichloroethane and 1,1-dichloroethylene) in the wastewater are evaporated by the action of water vapor, condensed in the overhead condenser 9, and then introduced into the separation tank 10. In the separation tank 10, the condensed liquid is separated into oil phase and water phase. The oil phase is discharged through the bottom oil phase outlet pipeline, and the water phase enters the wastewater white tank 14. The gas at the top of the separation tank 10 is introduced into the near-oxygen cracking device 12 by the vacuum pump 11 for further treatment.
[0047] The wastewater at the bottom of the stripping column 8 enters a wastewater discharge tank 15, part of which is discharged through a discharge pipeline 16, and the other part enters a raw liquid tank 17 for subsequent treatment. The wastewater is further removed of suspended solids by a bag filter 18, and then preheated by a condensate preheater 41 and a non-condensable gas preheater 42 in turn, and finally enters a heater 19. In the heater 19, the wastewater is heated to the evaporation temperature to form steam and concentrated liquid, which enters a separator 20, the steam returns to the bottom of the heater 19 through a first circulation pipeline 31 and a forced circulation pump 21 to form a circulation, and the concentrated liquid enters a cyclone 23 through a discharge pump 22. In the cyclone 23, the concentrated liquid is separated from solid particles by centrifugal force, the liquid at the upper part of the cyclone 23 returns to the separator 20 for re-separation, and the concentrated liquid at the bottom enters a thickener 24 for further concentration. The materials discharged from the discharge ports of the cyclone 23 and the thickener 24 are directly introduced into a mother liquor tank 26 without passing through a centrifuge 25, usually because the solid particle concentration in these materials is low or the particles are small, and cannot be effectively separated by the centrifuge 25. After being directly introduced into the mother liquor tank 26, the materials are treated by a mother liquor treatment system 28 to avoid the solid particles from entering the subsequent system to cause blockage or scaling. If the solid particle concentration in the materials is high, the materials will enter the centrifuge 25 for further separation into solid salt and mother liquor, the solid salt is discharged through a crystal discharge pipeline 27, and the mother liquor enters the mother liquor tank 26 for further treatment by the mother liquor treatment system 28.
[0048] The steam compressor 30 is the core equipment of the MVR system, which compresses the low-temperature steam in the washing column 29 into high-temperature and high-pressure steam, which enters the heater 19 through a steam transportation pipeline 35 to provide heat for the evaporation of the wastewater. The washing column 29 is connected to the steam compressor 30 through a steam return pipeline 34 to return the steam in the washing column 29 to the steam compressor 30 for re-compression and utilization, thereby improving energy efficiency. The condensate water generated by the steam compressor 30 is separated by a drain tank 37, the un-condensed steam is returned to the steam compressor 30 through a pipeline, the condensate water enters a condensate buffer tank 38, and is transported to the steam compressor 30 through a condensate transportation pipeline 40 for cooling and energy recovery. The condensate water in the condensate buffer tank 38 also enters the condensate preheater 41 through a heat exchange water inlet pipeline 39 for preheating the raw liquid, thereby further improving energy utilization. The non-condensable gas at the top of the condensate buffer tank 38 enters the non-condensable gas preheater 42 through a gas transportation pipeline 43 to preheat the raw liquid by using the waste heat of the non-condensable gas, and the heater 19 is further connected to the non-condensable gas preheater 42 through a preheated steam pipeline 44 to recover heat. The gas in the non-condensable gas preheater 42 finally enters a non-condensable gas and liquid separation device 45 for separation treatment.
[0049] The various embodiments in the specification are described in a progressive manner, and the same or similar parts between the various embodiments can be mutually referred to, and each embodiment focuses on the difference from other embodiments. In particular, for the system embodiments, since they are basically similar to the method embodiments, the description is relatively simple, and the relevant parts can be referred to the part of the method embodiments.
[0050] The above only describes the embodiments of the present application and is not intended to limit the present application. The present application can be variously changed and modified by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present application shall be included in the scope of the claims of the present application.
Claims
1. A saponification wastewater treatment system characterized by, The application relates to a saponification wastewater pipeline (1) which is connected with a wastewater buffer tank (3) through a resin adsorption device (2), wherein the wastewater buffer tank (3) is provided with an acid pipeline (4) and a sodium bisulfite feeding mechanism; the bottom of the wastewater buffer tank (3) is connected with the top of the wastewater buffer tank (3) through a pH adjusting circulating pump and a pH adjusting circulating pipeline (7); a wastewater discharge pipeline (702) is arranged on the pH adjusting circulating pipeline (7); the wastewater discharge pipeline (702) is connected with a stripping tower (8); the top of the stripping tower (8) is connected with a separation tank (10) through a tower top condenser (9); the top of the separation tank (10) is connected with a near-oxygen cracking device (12) through a vacuum pump (11); the condensate outlet of the vacuum pump (11) is connected with a saponification kettle (13); the middle part of the separation tank (10) is connected with a wastewater white tank (14) through a pipeline; and the bottom of the separation tank (10) is provided with an oil phase outlet pipeline.The stripping tower (8) is connected with a wastewater discharge tank (15) at the bottom, the wastewater discharge tank (15) is connected with a discharge pipeline (16) and a raw solution tank (17), the raw solution tank (17) is connected with a heater (19) at the bottom inlet through a bag filter (18), a condensate water preheater (41) and a non-condensable gas preheater (42) in sequence, the top outlet of the heater (19) is connected with a separator (20), the liquid outlet of the separator (20) is connected with the heater (19) at the bottom inlet through a first circulating pipeline (31) and a forced circulating pump (21), the top outlet of the separator (20) is connected with a washing tower (29) at the top inlet, the bottom outlet of the washing tower (29) is connected with the upper part of the washing tower (29) through a washing circulating pipeline (47), the second circulating pipeline (33) is connected with the upper part of the separator (20) on the washing circulating pipeline (47), the bottom of the separator (20) is connected with a cyclone (23) at the top through a discharge pump (22), the first circulating pipeline (31) is provided with a circulating discharge pipeline (32), the circulating discharge pipeline (32) is connected with the inlet of the discharge pump (22), the cyclone (23) is connected with a centrifuge (25) through a thickener (24), the liquid outlet of the centrifuge (25) is connected with a mother liquor tank (26), the solid outlet of the centrifuge (25) is connected with a crystal discharge pipeline (27), the washing tower (29) is connected with a steam compressor (30) through a steam return pipeline (34), the steam compressor (30) is connected with a fresh steam pipeline (36), the steam compressor (30) is connected with the heater (19) through a steam transportation pipeline (35), the steam compressor (30) is connected with a condensate water buffer tank (38) through a condensate water transportation pipeline (40), the condensate water buffer tank (38) is connected with the steam compressor (30) through a condensate water preheater (41), the condensate water preheater (41) is connected with the condensate water buffer tank (38) through a heat exchange water return pipeline (46), the condensate water buffer tank (38) is connected with the non-condensable gas preheater (42) through a gas transportation pipeline (43), the heater (19) is connected with the non-condensable gas preheater (42) through a preheating steam pipeline (44), and the non-condensable gas preheater (42) is connected with a non-condensable gas liquid separation device (45).
2. The saponification wastewater treatment system according to claim 1, characterized by The sodium bisulfite feeding mechanism comprises a sodium bisulfite preparation tank (5), a circulating water pipeline (501) and a solid feeding pipeline (503) connected to the sodium bisulfite preparation tank (5), and the sodium bisulfite preparation tank (5) is connected to the condensate outlet of a vacuum pump (11) through a vacuum condensate pipeline (502).
3. The saponification wastewater treatment system according to claim 1, characterized by, The pH adjusting circulating pipeline (7) is provided with an index detection pipeline (701), one end of the index detection pipeline (701) is connected to the wastewater buffer tank (3), and the index detection pipeline (701) is provided with a pH detection system and a residual chlorine content sampling test port.
4. The saponification wastewater treatment system according to claim 1, characterized by The mother liquor tank (26) is connected to a mother liquor treatment system (28).
5. The saponification wastewater treatment system according to claim 1, characterized by The upper outlet of the cyclone (23) is connected to the upper inlet of the separator (20) through a pipeline.
6. The saponification wastewater treatment system according to claim 1, characterized by The outlets of the cyclone (23) and the thickener (24) are respectively connected to the mother liquor tank (26).
7. The saponification wastewater treatment system according to claim 1, characterized by The top of the wastewater buffer tank (3) is connected to a tail gas recovery system (6).