CN210140501U - System for handle coal gasification buck - Google Patents
System for handle coal gasification buck Download PDFInfo
- Publication number
- CN210140501U CN210140501U CN201920790814.8U CN201920790814U CN210140501U CN 210140501 U CN210140501 U CN 210140501U CN 201920790814 U CN201920790814 U CN 201920790814U CN 210140501 U CN210140501 U CN 210140501U
- Authority
- CN
- China
- Prior art keywords
- pressure
- water
- temperature high
- liquid separation
- inlet
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model provides a system for handle coal gasification buck mainly solves among the prior art flash distillation process equipment bulky, the civil engineering is with high costs, the high problem of energy consumption to and handle the cyclic utilization scheduling problem of coal gasification grey water in-process solid-liquid separation's precision, energy under the highly compressed operating mode of high temperature. The utility model discloses system for handle coal gasification buck, including pretreatment zone, solid-liquid separation district, indirect cooling district and the cyclic utilization district that communicates in proper order. The pretreatment area is used for flocculating the grey water, so that the difficulty of solid-liquid separation is reduced; the solid-liquid separation zone adopts a series solid-liquid separation combination mode of a hydrocyclone and a high-pressure cross flow filter, so that the solid-liquid separation precision is improved; the indirect cooling area adopts a combined cooling mode of a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler, so that the heat consumption is reduced; the recycling area is used for recycling energy. Adopt the utility model discloses a system treatment buck can reduce the energy consumption, and scientific environmental protection is economical feasible again.
Description
Technical Field
The utility model relates to a coal gasification technical field, concretely relates to system for handle coal gasification buck.
Background
Clean and efficient utilization of coal has been a major issue for energy and environmental protection, and the main approach for coal conversion is coal gasification. After the implementation of the new environmental protection method, energy conservation and environmental protection cannot be ignored while pursuing economic benefits, so how to treat the grey water generated by coal gasification is the most important of the coal chemical industry.
At present, most of common grey water treatment systems adopt a multi-stage flash evaporation process and a sedimentation process, and the common grey water treatment systems have the advantages of rapid and efficient cooling, serious washing and ash entrainment, large equipment volume of flash tanks and sedimentation tanks, large floor area, high civil engineering cost and high energy consumption.
Compared with the prior art, the indirect heat exchange cooling process has the advantages of short flow, less equipment, less investment and low energy consumption, but the coal chemical industry enterprises rarely adopt the indirect cooling technology of the heat exchanger, and the main reason is the problems of scaling and blockage of the heat exchanger. In the grey water cooling process, ash carried by the grey water, generated dirt and separated salt can scale a pipe box and a heat exchange pipe of the heat exchanger, so that the heat resistance of the heat exchange pipe is increased, the heat exchange efficiency is reduced, the heat exchanger can be blocked in serious conditions, the heat exchanger is invalid, and finally the system is stopped. Therefore, the indirect heat exchange cooling process has high requirements on the precision of the solid-liquid separation of the grey water.
Chinese patent publication No. CN106630307A describes a system for treating coal gasification grey water. The system mainly solves the problems of hardness, turbidity and suspended matters in the coal gasification grey water, and thoroughly solves the system scaling problem caused by high hardness in the coal gasification grey water. The invention takes an electrochemical method as a main working principle, and calcium ions and magnesium ions form precipitate substances to be separated out by adjusting the pH value and the alkalinity. Under the action of the electric field, solid particles contained in the grey water and newly formed fine particles of the calcium-magnesium compound are separated. However, the following disadvantages are still present in this patent: 1. the system adopts an electrochemical method to remove hardness and separate particles, and is difficult to apply to the working conditions of high temperature and high pressure due to the electrode plates, the power supply device and the like involved in the electrochemical method; 2. because the dust removal and hardness removal system cannot work at high temperature and high pressure, the grey water from the washing tower is gradually cooled and depressurized, and is subjected to dust removal and then is pressurized to the pressure of the washing tower by using a high-speed pump for recycling, so that the equipment and power consumption are increased; 3. the device can not remove dust at high temperature, so the heat exchanger can not be used for heat exchange and cooling in the cooling process, and the device can only adopt a flash evaporation method for cooling and pressure reduction, thereby greatly increasing the equipment investment, the occupied area and the civil engineering cost.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a system for handle coal gasification buck reduces area, equipment investment, reduces the energy consumption, solves solid-liquid separation's precision problem to carry out cyclic utilization to the resource.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a system for treating coal gasification grey water comprises a pretreatment zone, a solid-liquid separation zone, an indirect cooling zone and a recycling zone which are sequentially communicated; wherein the content of the first and second substances,
the pretreatment area is used for flocculating the grey water and outputting mixed water;
the solid-liquid separation zone is used for carrying out solid-liquid separation on the mixed water and outputting clear liquid at the permeation side;
the indirect cooling area is used for carrying out indirect heat exchange cooling on the clear liquid at the permeation side and comprises a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler; the inlet of the high-temperature high-pressure cooler is communicated with a fresh water inlet and a clear liquid outlet at the permeation side of the solid-liquid separation zone, and the outlet of the high-temperature high-pressure cooler is communicated with the recycling zone; the inlet of the medium-temperature high-pressure cooler is communicated with a cooling water inlet and the outlet of the high-temperature high-pressure cooler, and the outlet of the medium-temperature high-pressure cooler is communicated with a recycling area; the clear liquid at the permeation side output by the solid-liquid separation zone passes through a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler for indirect heat exchange and cooling, and low-temperature high-pressure water is output;
the recycling area is used for recycling the water obtained by the high-temperature high-pressure cooler and the medium-temperature high-pressure cooler.
Furthermore, the pretreatment area is provided with three inlets which are respectively a black water inlet, an ash water inlet and a flocculating agent inlet, and the black water and the ash water are uniformly mixed and then flocculated to output mixed water.
Further, the solid-liquid separation zone comprises a hydrocyclone and a high-pressure cross-flow filter, and the hydrocyclone and the high-pressure cross-flow filter are connected in series;
the inlet of the hydrocyclone separator is communicated with the mixed water outlet of the pretreatment area, and the outlet of the hydrocyclone separator is communicated with the inlet of the high-pressure cross flow filter; the mixed water output from the pretreatment area enters a hydrocyclone separator, a high-speed rotating flow field is formed in the hydrocyclone separator, solid particles in the mixed water are primarily separated by using centrifugal force, and overflow clear liquid is output;
the inlet of the high-pressure cross-flow filter is communicated with the outlet of the hydrocyclone, the outlet of the high-pressure cross-flow filter is communicated with the indirect cooling area, the overflow clear liquid enters the high-pressure cross-flow filter from the hydrocyclone for cross-flow filtration, and the solid particles in the overflow clear liquid are separated to output clear liquid at the permeation side.
Further, the hydrocyclone separator comprises a plurality of cyclones, and the cyclones are arranged in parallel in a circumferential mode; and the mixed water enters the hydrocyclone separator and then respectively enters the inlets of the cyclones, hydrocyclone separation is carried out in each cyclone, and then the mixed water is collected and the overflow clear liquid is output.
Furthermore, the high-pressure cross flow filter is composed of a plurality of tubular membranes, each tubular membrane is connected with the end sockets at two ends, and micropores for intercepting fine dust are arranged on the tubular membranes; and the overflow clear liquid enters the end sockets of the high-pressure cross flow filter from the hydrocyclone separator and then enters each tubular membrane, and water in the tubular membranes permeates the micropores of the tubular membranes under the driving of pressure difference, is seeped out and collected, and is output as clear liquid at the permeation side.
Further, the high-temperature high-pressure cooler is also provided with a low-pressure steam outlet; and the permeate side clear liquid is subjected to indirect heat exchange with fresh water for cooling, and the fresh water is heated into low-pressure saturated steam and recycled through the low-pressure steam outlet.
Further, the recycling area comprises a gas-liquid separation device and a grey water circulation device, and the gas-liquid separation device and the grey water circulation device are connected in parallel;
an inlet of the gas-liquid separation equipment is communicated with the indirect cooling area to introduce low-temperature high-pressure water, and the low-temperature high-pressure water enters the gas-liquid separation equipment from the indirect cooling area to obtain low-temperature circulating water;
the inlet of the grey water circulating equipment is communicated with the indirect cooling area so as to introduce medium-temperature high-pressure water, and the medium-temperature high-pressure water enters the grey water circulating equipment from the indirect cooling area and returns to the washing tower to be recycled as washing water.
Further, the system also comprises a pressure reducing device, and the medium-temperature high-pressure cooler is sequentially connected with the pressure reducing device and the gas-liquid separation device.
Further, the pressure reducing device is a hydraulic turbine.
The utility model has the advantages as follows:
the utility model provides a system for processing coal gasification grey water, which replaces a multi-stage flash evaporation process in a way of cooling by combining a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler, reduces the volume and the occupied area of equipment, and saves about 60 percent of heat consumption; in addition, the pretreatment of mixed flocculation is carried out on the grey water before solid-liquid separation, so that solid particles are increased to more than 5 microns, and the precision problem of solid-liquid separation is solved by a serial solid-liquid separation combination mode of a hydrocyclone and a high-pressure cross flow filter, so that the problems of scaling and blockage of a heat exchanger in the indirect heat exchange cooling process do not exist; and simultaneously, the utility model discloses a system has still realized the cyclic utilization to the energy, can provide the circulation power about 4Mpa, has improved the value and the utilization taste of the energy.
Drawings
FIG. 1 is a flow chart of a process for treating coal gasification grey water as disclosed in the present invention
FIG. 2 is a schematic view of a system for treating coal gasification grey water according to the present invention
FIG. 3a is a front view of a hydrocyclone
FIG. 3b is a top view of a hydrocyclone
FIG. 4 is a schematic view of a high pressure cross-flow filter
FIG. 5 is a schematic view of a high-temperature high-pressure cooler
FIG. 6 is a schematic diagram of the structure of the intermediate temperature and high pressure cooler
Reference numerals:
1-black water inlet; 2-ash water inlet; 3-flocculant solution inlet; 4-mixed water outlet; 5-underflow thick slurry outlet; 6-overflow clear liquid outlet; 7-dense slurry outlet on the retentate side; 8-permeate side clear outlet; 9-medium temperature high pressure water outlet; 10-high pressure circulating water inlet; 11-medium temperature high pressure water inlet; 12-a low temperature and high pressure water outlet; 13-low temperature normal pressure water outlet; 14-a low-temperature circulating water outlet; 15-noncondensable gas outlet; 16-fresh water inlet; 17-a low-pressure saturated steam outlet; 18-cooling water inlet; 19-cooling return water outlet; 20-overflow clear liquid inlet; 21-mixed water inlet; 22-a central tube; 23-a cyclone; 24-permeate side clear liquid inlet
Detailed Description
Various aspects and features of the present application are described herein with reference to the drawings.
It will be understood that various modifications may be made to the embodiments of the present application. Accordingly, the foregoing description should not be construed as limiting, but merely as exemplifications of embodiments. Those skilled in the art will envision other modifications within the scope and spirit of the application.
The accompanying drawings, which are incorporated in and constitute a part of the specification, illustrate embodiments of the application and, together with a general description of the application given above and the detailed description of the embodiments given below, serve to explain the principles of the application.
These and other characteristics of the present application will become apparent from the following description of preferred forms of embodiment, given as non-limiting examples, with reference to the attached drawings.
It should also be understood that, although the present application has been described with reference to some specific examples, a person of skill in the art shall certainly be able to achieve many other equivalent forms of application, having the characteristics as set forth in the claims and hence all coming within the field of protection defined thereby.
The above and other aspects, features and advantages of the present application will become more apparent in view of the following detailed description when taken in conjunction with the accompanying drawings.
Specific embodiments of the present application are described hereinafter with reference to the accompanying drawings; however, it is to be understood that the disclosed embodiments are merely exemplary of the application, which can be embodied in various forms. Well-known and/or repeated functions and constructions are not described in detail to avoid obscuring the application of unnecessary or unnecessary detail. Therefore, specific structural and functional details disclosed herein are not to be interpreted as limiting, but merely as a basis for the claims and as a representative basis for teaching one skilled in the art to variously employ the present application in virtually any appropriately detailed structure.
FIG. 1 is a flow diagram of a process for treating coal gasification grey water as disclosed in the present invention, and as shown in FIG. 1, the present invention discloses a system for treating coal gasification grey water, comprising a pretreatment zone, a solid-liquid separation zone, an indirect cooling zone and a recycling zone, which are connected in sequence; wherein the content of the first and second substances,
the pretreatment area is used for flocculating the grey water and outputting mixed water;
the solid-liquid separation zone is used for carrying out solid-liquid separation on the mixed water and outputting clear liquid at the permeation side;
the indirect cooling area is used for carrying out indirect heat exchange cooling on the clear liquid at the permeation side and comprises a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler; the inlet of the high-temperature high-pressure cooler is communicated with a fresh water inlet and a clear liquid outlet at the permeation side of the solid-liquid separation zone, and the outlet of the high-temperature high-pressure cooler is communicated with the recycling zone; the inlet of the medium-temperature high-pressure cooler is communicated with a cooling water inlet and the outlet of the high-temperature high-pressure cooler, and the outlet of the medium-temperature high-pressure cooler is communicated with a recycling area; the clear liquid at the permeation side output by the solid-liquid separation zone flows through a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler for indirect heat exchange and cooling to obtain low-temperature high-pressure water;
the recycling area is used for recycling the water obtained by the high-temperature high-pressure cooler and the medium-temperature high-pressure cooler.
With reference to the system diagram of fig. 2, the pretreatment zone is further provided with three inlets, namely a black water inlet 1, a grey water inlet 2 and a flocculant solution inlet 3, and an outlet, namely a mixed water outlet 4, which is communicated with the inlet of the hydrocyclone of the solid-liquid separation zone. Black water from a chilling chamber of the gasification furnace and grey water at the bottom of the synthetic gas washing tower respectively enter a pretreatment region to be mixed and flocculated with a flocculating agent solution, so that fine ash particles are increased to more than 5 mu m, and mixed water is output.
Further, the solid-liquid separation zone comprises a hydrocyclone separator and a high-pressure cross-flow filter, and the hydrocyclone separator and the high-pressure cross-flow filter are connected in series;
the hydrocyclone has an inlet and two outlets. The inlet is a mixed water inlet and is communicated with the outlet of the pretreatment area; the top outlet is an overflow clear liquid outlet 6 which is communicated with the inlet of the high-pressure cross-flow filter; the bottom outlet is an underflow thick slurry outlet 5. And (3) the mixed water from the pretreatment area enters a hydrocyclone separator, a high-speed rotating flow field is formed in the hydrocyclone separator, the solid particles in the mixed water are primarily separated by using centrifugal force, and overflow clear liquid is output.
The high pressure cross-flow filter has an inlet and two outlets. The inlet is an overflow clear liquid inlet and is communicated with the outlet of the hydrocyclone separator; the two outlets are respectively a clear liquid outlet 8 at the permeation side and a thick slurry outlet 7 at the retentate side, and the clear liquid outlet 8 at the permeation side is communicated with the inlet of the high-temperature high-pressure cooler. And the overflow clear liquid from the hydrocyclone enters a high-pressure cross-flow filter for cross-flow filtration, and the clear liquid at the permeation side is output by separating solid particles in the overflow clear liquid.
Preferably, as shown in figures 3a and 3b, the hydrocyclone comprises a plurality of cyclones 23 arranged in circumferential parallel. Mixed water enters a central pipe 22 of the hydrocyclone from a mixed water inlet 21 and then flows into inlets of the cyclones, hydrocyclone separation is carried out in the cyclones and then the mixed water is collected to obtain overflow clear liquid which is output through an overflow clear liquid outlet 6, and separated thick slurry is discharged through an underflow thick slurry outlet 5. According to simulation and test results, the hydrocyclone adopting a plurality of cyclones arranged in parallel at the circumference is particularly suitable for solid-liquid separation of high-temperature and high-pressure grey water, the separation efficiency of solid particles larger than 5 mu m can reach 95%, the amount of fine ash entering a high-pressure cross-flow filter is reduced, and the processing capacity of the cross-flow filter is improved.
Preferably, as shown in fig. 4, the high pressure cross-flow filter is comprised of a plurality of ceramic tubular membranes. The inner diameter of each ceramic membrane is 10mm, the length of each ceramic membrane is 1-2 meters, the ceramic membranes are arranged in a triangular or square mode, the ceramic membranes are connected with the end sockets at two ends, and the tubular membranes are provided with micropores used for intercepting fine ash. The overflow clear liquid enters the end socket of the high-pressure cross flow filter from the overflow clear liquid inlet 20 and then enters each ceramic tubular membrane, water in the tubular membranes permeates the micropores of the tubular membranes under the driving of pressure difference and is seeped out and collected to obtain a permeate side clear liquid, and the permeate side clear liquid is output through a permeate side clear liquid outlet 8; the fine ash intercepted by the tubular membrane enables the solid concentration in the liquid to rise to form thick slurry, and the thick slurry is collected at the other end head of the filter and is discharged through a thick slurry outlet 7 at the retentate side. During back flushing, the overflow clear liquid inlet 20 is closed, the back flushing liquid enters from the clear liquid outlet 8 on the permeation side, the back flushing liquid seeps into the membrane from the outside of the tubular membrane under the action of reverse pressure difference to achieve the effect of flushing filter cakes, and the flushed thick slurry is discharged from the thick slurry outlet 7 on the permeation side.
With reference to fig. 2, further, the indirect cooling zone includes a high temperature high pressure cooler and a medium temperature high pressure cooler. The high temperature and high pressure cooler has two inlets and one outlet. The inlets of the high-temperature high-pressure cooler are respectively a clear liquid inlet at the permeation side and a fresh water inlet 16, wherein the clear liquid inlet at the permeation side is communicated with a clear liquid outlet 8 at the permeation side of the solid-liquid separation zone; the outlet of the high-temperature high-pressure cooler is a medium-temperature high-pressure water outlet 9. The clear liquid at the permeation side from the solid-liquid separation zone enters a high-temperature high-pressure cooler to be indirectly subjected to heat exchange with fresh water for cooling, and medium-temperature high-pressure water is output.
The medium-temperature high-pressure cooler is provided with two inlets and two outlets. The inlets of the medium-temperature high-pressure cooler are respectively an inlet 11 for medium-temperature high-pressure water and an inlet 18 for cooling water, wherein the inlet 11 for medium-temperature high-pressure water is communicated with the outlet 9 for medium-temperature high-pressure water of the high-temperature high-pressure cooler; the outlets of the medium-temperature high-pressure cooler are respectively a low-temperature high-pressure water outlet 12 and a cooling water return outlet 19. The medium temperature high pressure water from the high temperature high pressure cooler is further indirectly cooled by heat exchange with cooling water, and the low temperature high pressure water is output.
Preferably, the high temperature and high pressure cooler is further provided with a low pressure saturated steam outlet 17, the permeate side clear liquid is cooled by indirect heat exchange with fresh water, and the fresh water is heated into low pressure saturated steam and recycled through the low pressure saturated steam outlet.
Preferably, as shown in fig. 5, the high temperature and high pressure cooler is a kettle reboiler and the tube side is a U-tube design. The permeate side clear liquid enters the heat exchanger tube side from the permeate side clear liquid inlet 24 of the end socket, and the fresh water enters the heat exchanger shell side from the fresh water inlet 16 of the shell side. The clear liquid at the permeation side and fresh water are subjected to indirect heat exchange and cooling to obtain medium-temperature high-pressure water, and the medium-temperature high-pressure water is output through a medium-temperature high-pressure water outlet 9 of the tube pass; the fresh water is heated to generate phase change, and low-pressure saturated steam is obtained and recycled through a low-pressure saturated steam outlet 17 of the shell side.
Preferably, as shown in fig. 6, the medium-temperature high-pressure cooler is a single-pass shell-and-tube heat exchanger. Wherein the medium temperature high pressure water inlet 11 and the low temperature high pressure water outlet 12 are tube pass inlets and outlets and are respectively connected with end sockets at two ends of the heat exchanger; the cooling water inlet 18 and the cooling return water outlet 19 are shell pass inlets and outlets and are respectively connected with the shell pass of the heat exchanger. The medium temperature high pressure water from the high temperature high pressure cooler enters the heat exchanger tube pass through the medium temperature high pressure water inlet 11, and the cooling water enters the heat exchanger shell pass through the cooling water inlet 18. The medium temperature high pressure water and the cooling water are subjected to indirect heat exchange and cooling to obtain low temperature high pressure water which is output through a low temperature high pressure water outlet 12 of the tube pass; the cooling water is heated to obtain cooling return water, and the cooling return water is discharged through a cooling return water outlet 19 of the shell pass.
With continued reference to FIG. 2, further, the recycling area includes a gas-liquid separation device and a grey water recycling device. The gas-liquid separation device is provided with an inlet and two outlets, namely a low-temperature high-pressure water inlet, a non-condensable gas outlet 15 and a low-temperature circulating water outlet 14, wherein the low-temperature high-pressure water inlet is communicated with the outlet of the medium-temperature high-pressure cooler. And the low-temperature high-pressure water from the medium-temperature high-pressure cooler passes through a gas-liquid separation device to remove acid gas and non-condensable gas dissolved in the water, and low-temperature circulating water is obtained.
The grey water circulating equipment has an inlet and an outlet, which are a high pressure circulating water inlet 10 and a scrubber water outlet, respectively. Wherein, the high-pressure circulating water inlet 10 is communicated with the medium-temperature high-pressure water 9 outlet of the high-temperature high-pressure cooler. The medium-temperature high-pressure water from the high-temperature high-pressure cooler passes through grey water circulating equipment and then returns to the washing tower to be used as washing water for recycling.
Preferably, a pressure reducing device can be arranged in front of the gas-liquid separation device, the pressure reducing device is provided with an inlet and an outlet, the low-temperature high-pressure water inlet is communicated with the low-temperature high-pressure water outlet 12 of the medium-temperature high-pressure cooler, and the low-temperature normal-pressure water outlet 13 is communicated with the inlet of the gas-liquid separation device. And the low-temperature high-pressure water from the medium-temperature high-pressure cooler is decompressed through a decompression device so as to facilitate the escape of acid gas and non-condensable gas.
Preferably, the pressure reduction device is a hydraulic turbine, and excess pressure in the high-pressure low-temperature water is recovered by using the hydraulic turbine.
The system of the embodiment of the present invention will be described in detail with reference to the working flow of the system of the present invention and the corresponding advantageous effects,
the utility model discloses the flow of specific operation as follows:
the flow rate of black water from a chilling chamber of the gasification furnace is 154.8t/h, the flow rate of black water with the solid content of 3.65t/h and the flow rate of grey water from the bottom of a synthetic gas washing tower are 18.27t/h, and the grey water with the solid content of 1.76t/h respectively enter a pretreatment region to be mixed and flocculated with a flocculant solution, so that fine ash particles are increased to be more than 5 mu m, and mixed water is output.
The mixed water from the pretreatment area enters a hydrocyclone separator for preliminary separation, the flow rate after separation is 0.9t/h, and underflow concentrated slurry with the solid content of 5.15t/h is discharged; the top overflow clear liquid with the flow rate of 172.1t/h and the solid content of 0.25t/h enters a high-pressure cross-flow filter.
After the top overflow clear liquid is further filtered in a cross flow manner by the high-pressure cross flow filter, the flow rate is 11.4t/h, and the thick slurry on the retentate side with the solid content of 0.25t/h is discharged; the clear liquid on the permeate side with the flow rate of 160.7t/h enters a high-temperature high-pressure cooler for cooling.
The permeate side clear liquid with the high temperature and the high pressure of about 220 ℃ entering the high temperature and high pressure cooler is cooled by indirect heat exchange with fresh water with the flow rate of 18t/h and the temperature of about 30 ℃ to obtain medium temperature and high pressure water with the temperature of about 150 ℃, and the fresh water is heated into low pressure saturated steam with the temperature of about 160 ℃ to be used in a plant area. The cooled medium-temperature high-pressure water with the flow rate of 145t/h passes through grey water circulating equipment and then returns to the washing tower to be used as washing water for recycling; the medium temperature and high pressure water with the flow rate of 15.7t/h enters the medium temperature and high pressure cooler.
The medium-temperature high-pressure water entering the medium-temperature high-pressure cooler is further subjected to indirect heat exchange and cooling with cooling water with the flow rate of 10t/h to be cooled to about 58 ℃ to obtain low-temperature high-pressure water.
And then, decompressing the low-temperature high-pressure water to 0.1MPa through a decompression device, and then, introducing the water into a gas-liquid separation device to remove acid gas and non-condensable gas to be used as low-temperature circulating water.
The above embodiments are only exemplary embodiments of the present invention, and are not intended to limit the present invention, and the protection scope of the present invention is defined by the claims. Various modifications and equivalents of the invention can be made by those skilled in the art within the spirit and scope of the invention, and such modifications and equivalents should also be considered as falling within the scope of the invention.
Claims (9)
1. A system for treating coal gasification grey water is characterized by comprising a pretreatment zone, a solid-liquid separation zone, an indirect cooling zone and a recycling zone which are sequentially communicated; wherein the content of the first and second substances,
the pretreatment area is used for flocculating the grey water and outputting mixed water;
the solid-liquid separation zone is used for carrying out solid-liquid separation on the mixed water and outputting clear liquid at the permeation side;
the indirect cooling area is used for carrying out indirect heat exchange cooling on the clear liquid at the permeation side and comprises a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler; the inlet of the high-temperature high-pressure cooler is communicated with a fresh water inlet and a clear liquid outlet at the permeation side of the solid-liquid separation zone, and the outlet of the high-temperature high-pressure cooler is communicated with the recycling zone; the inlet of the medium-temperature high-pressure cooler is communicated with a cooling water inlet and the outlet of the high-temperature high-pressure cooler, and the outlet of the medium-temperature high-pressure cooler is communicated with a recycling area; the clear liquid at the permeation side output by the solid-liquid separation zone passes through a high-temperature high-pressure cooler and a medium-temperature high-pressure cooler for indirect heat exchange and cooling, and low-temperature high-pressure water is output;
the recycling area is used for recycling the water obtained by the high-temperature high-pressure cooler and the medium-temperature high-pressure cooler.
2. The system of claim 1, wherein the pretreatment zone has three inlets, namely a black water inlet, a grey water inlet and a flocculating agent inlet, and the black water and the grey water are uniformly mixed and flocculated to output mixed water.
3. The system of claim 1 wherein the solid liquid displacement zone comprises a hydrocyclone and a high pressure cross-flow filter, the hydrocyclone and the high pressure cross-flow filter being connected in series;
the inlet of the hydrocyclone separator is communicated with the mixed water outlet of the pretreatment area, and the outlet of the hydrocyclone separator is communicated with the inlet of the high-pressure cross flow filter; the mixed water output from the pretreatment area enters a hydrocyclone separator, a high-speed rotating flow field is formed in the hydrocyclone separator, solid particles in the mixed water are primarily separated by using centrifugal force, and overflow clear liquid is output;
the inlet of the high-pressure cross-flow filter is communicated with the outlet of the hydrocyclone, the outlet of the high-pressure cross-flow filter is communicated with the indirect cooling area, the overflow clear liquid enters the high-pressure cross-flow filter from the hydrocyclone for cross-flow filtration, and the fine solid particles in the overflow clear liquid are separated to output clear liquid at the permeation side.
4. The system of claim 3, wherein the hydrocyclone comprises a plurality of cyclones, each arranged in circumferential parallel;
and the mixed water enters the hydrocyclone separator and then respectively enters the inlets of the cyclones, hydrocyclone separation is carried out in each cyclone, and then the mixed water is collected and the overflow clear liquid is output.
5. The system of claim 3, wherein the high-pressure cross-flow filter is composed of a plurality of tubular membranes, each tubular membrane is connected with the end sockets at two ends, and the tubular membranes are provided with micropores for intercepting fine ash; and the overflow clear liquid enters the end sockets of the high-pressure cross flow filter from the hydrocyclone separator and then enters each tubular membrane, and water in the tubular membranes permeates the micropores of the tubular membranes under the driving of pressure difference, is seeped out and collected, and is output as clear liquid at the permeation side.
6. The system of claim 1, wherein the high temperature and high pressure cooler is further provided with a low pressure steam outlet; and the permeate side clear liquid is subjected to indirect heat exchange with fresh water for cooling, and the fresh water is heated into low-pressure saturated steam and recycled through the low-pressure steam outlet.
7. The system of claim 1, wherein the recycling zone comprises a gas-liquid separation device and a grey water recycling device, the gas-liquid separation device and the grey water recycling device being connected in parallel;
an inlet of the gas-liquid separation equipment is communicated with the indirect cooling area to introduce low-temperature high-pressure water, and the low-temperature high-pressure water enters the gas-liquid separation equipment from the indirect cooling area to obtain low-temperature circulating water;
the inlet of the grey water circulating equipment is communicated with the indirect cooling area so as to introduce medium-temperature high-pressure water, and the medium-temperature high-pressure water enters the grey water circulating equipment from the indirect cooling area and returns to the washing tower to be recycled as washing water.
8. The system of claim 7, further comprising a pressure reduction device, wherein the medium temperature and high pressure cooler is connected to the pressure reduction device and the gas-liquid separation device in sequence.
9. The system of claim 8, wherein the pressure reducing device is a hydraulic turbine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920790814.8U CN210140501U (en) | 2019-05-29 | 2019-05-29 | System for handle coal gasification buck |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920790814.8U CN210140501U (en) | 2019-05-29 | 2019-05-29 | System for handle coal gasification buck |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210140501U true CN210140501U (en) | 2020-03-13 |
Family
ID=69734837
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920790814.8U Active CN210140501U (en) | 2019-05-29 | 2019-05-29 | System for handle coal gasification buck |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210140501U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113461186A (en) * | 2020-03-30 | 2021-10-01 | 石家庄波特无机膜分离设备有限公司 | Coal gasification black ash water energy recovery and fly ash recycling system and method |
| CN114273098A (en) * | 2021-12-29 | 2022-04-05 | 上海赛科石油化工有限责任公司 | System and method for separating polymer in acrylonitrile production process |
-
2019
- 2019-05-29 CN CN201920790814.8U patent/CN210140501U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113461186A (en) * | 2020-03-30 | 2021-10-01 | 石家庄波特无机膜分离设备有限公司 | Coal gasification black ash water energy recovery and fly ash recycling system and method |
| CN114273098A (en) * | 2021-12-29 | 2022-04-05 | 上海赛科石油化工有限责任公司 | System and method for separating polymer in acrylonitrile production process |
| CN114273098B (en) * | 2021-12-29 | 2024-04-26 | 上海赛科石油化工有限责任公司 | System and method for separating polymer in acrylonitrile production flow |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN210140501U (en) | System for handle coal gasification buck | |
| CN204569599U (en) | A kind of novel no pollution sewage effluent total system | |
| CN210001701U (en) | system for treating mine water with high suspended matter and high mineralization degree | |
| CN205360735U (en) | A full -automatic continuous demineralizer for production of furan phenol | |
| CN107352727B (en) | Method for realizing zero discharge of coal chemical industry wastewater | |
| CN114380441A (en) | Method and device for recovering bromine and sodium from PTA tail gas treatment waste liquid | |
| CN107311381A (en) | A kind of reverse osmosis concentrated seawater comprehensive utilizing method and system | |
| CN204417276U (en) | A kind of Coal Chemical Industry strong brine evaporative crystallization divides salt device | |
| CN105859005A (en) | Method and system for treating stainless steel cold-rolling and pickling waste acid | |
| CN112624448A (en) | Method for treating wastewater generated in white carbon black production process by precipitation process | |
| CN110436585B (en) | Method for removing and recycling water-soluble salt in secondary aluminum ash | |
| CN106746129B (en) | Landfill leachate evaporation crystallization system | |
| CN105461596A (en) | Clean production process for converting camphor ammonium sulfonate into camphorsulfonic acid | |
| JP2014015639A (en) | Method and apparatus for treating salt waste water | |
| KR101778021B1 (en) | Eco-friendly desalination system using forward osmosis and reverse osmosis | |
| CN112010450A (en) | System and method for treating coal gasification grey water | |
| CN104609596B (en) | A kind of photovoltaic acidity washing waste water recycling technique | |
| CN106746046A (en) | Process unit and method that ionic membrane realizes desulfurization waste liquor zero-emission are driven based on electricity | |
| CN107459021B (en) | Apparatus and method for decomposing nitrate solution | |
| CN206219367U (en) | A kind of processing unit of yarn-dyed fabric yarn dyeing waste water | |
| CN207405051U (en) | A kind of system that calcium and aluminium are recycled in the sludge from Aluminum | |
| CN208632266U (en) | A kind of industrial circulating cooling water Zero discharging system | |
| CN208829472U (en) | A kind of processing heavy metal wastewater thereby device | |
| CN205953752U (en) | System for implement regeneration processing method of dense salt waste water of coal industry | |
| CN221217512U (en) | Mine water advanced treatment equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |