CN213823486U - Flash evaporation stripping cooling system - Google Patents
Flash evaporation stripping cooling system Download PDFInfo
- Publication number
- CN213823486U CN213823486U CN202022451015.3U CN202022451015U CN213823486U CN 213823486 U CN213823486 U CN 213823486U CN 202022451015 U CN202022451015 U CN 202022451015U CN 213823486 U CN213823486 U CN 213823486U
- Authority
- CN
- China
- Prior art keywords
- flash
- cooling tower
- stripping
- section
- stripping cooling
- 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
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a flash evaporation strip cooling system, including first flash evaporation strip cooling tower, second flash evaporation strip cooling tower, vacuum flash tank, grey basin, subsider, condenser, vacuum flash separation jar. The utility model provides a pair of flash distillation strip cooling system, equipment integrate, and the flow is simplified, and the energy consumption reduces, and heat transfer effect improves, changes low temperature buck into and cools off to realized utilizing the grade of low temperature buck, saved a large amount of circulating water, and realized the complete retrieval and utilization of sediment water.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, a flash distillation strip cooling system is related to.
Background
The raw coal gasification is an important measure for realizing the comprehensive utilization of coal resources based on the basic national situation of more coal and less oil in China. Coal gasification and coal chemical industry are important development directions for the development of chemical industry in China. Generally, raw coal is prepared into pulverized coal or coal water slurry and then gasified in a gasification furnace, and a large amount of black water is generated after generated high-temperature gas (main components such as CO, CH4, CO2 and H2) is chilled and washed. The black water contains approximately 0.01-2% of solid particles (mainly coal ash, coal slag and incompletely reflected coal), the temperature is 150-250 ℃, and the pressure is 1.8-10 MpaG. The black water at this time is almost saturated. On the one hand, gases such as CO, CO2, CH4, H2S and NH3 are also dissolved and entrained in the black water. The gases are flammable and explosive, toxic and harmful, and if not removed, the gases not only corrode equipment, but also cause harm to the whole device; on the other hand, the black water pressure generated by the washing tower and the gasification furnace is not low, but the black water cannot be used for doing work by external expansion due to the solid particles; thirdly, the temperature of the black water is not low enough to recover part of the heat energy, but the engineering problems of abrasion, blockage, scaling and the like of solid particles are overcome, so that the cost is high and the benefit is limited.
The existing engineering solutions, such as CN110228830A, CN207498194U, CN207627955U, CN207828040U, and CN209161731U, all adopt simple flash tanks to perform flash evaporation step by step, not only heat is not recycled, but also a large amount of precious water resources (mainly used as circulating cooling water) are consumed for cooling.
Texaco is one of foreign companies which enter the market of China earlier and promote the gasification of coal water slurry. CN94117093.4 discloses a multistage flash evaporation technology, and energy recovery and process water recycling are realized through subsystems such as a three-stage flash evaporation system, a sedimentation clarification system and an oxygen removal system. Black water from a gasification and synthesis gas washing system is sent to a high-pressure flash tank after passing through a pressure reducing valve, part of the black water is changed into steam through flash evaporation and enters a stripping tower to heat process water from a deoxygenation system, tail gas is sent to a sulfur recovery unit after being cooled by a heat exchanger and separated by a high flash separation tank, and condensed water separated by the high flash separation tank is sent to the deoxygenation system. And after the black water flowing out of the bottom of the high-pressure flash tank is further flashed by the low-pressure flash tank and the vacuum flash tank, the discharged water is sent to a black water settling and clarifying system. The black water is settled and clarified to become grey water, a large part of the grey water is deoxidized by an deoxidizing system and heated by a stripping tower and then sent back to a gasification and synthesis gas washing system, and the other part of the grey water is cooled by a waste water cooler and sent to a sewage treatment plant for balancing the salt dissolved in the system. And (3) conveying steam at the outlet of the low-pressure flash tank into a deoxygenation system to achieve a deoxygenation effect, cooling the steam at the outlet of the vacuum flash tank by a heat exchanger, separating by a vacuum flash separating tank, pumping by a vacuum pump, and exhausting to the atmosphere. Therefore, the technology has the advantages of more equipment, complex operation, more occupied area, and higher equipment cost and construction investment cost. The general enterprises are difficult to bear.
CN109485190A discloses a treatment method of black water produced by coal gasification, a coal gasification method and a coal gasification system, the technology is that on the basis of CN94117093.4, black water after flocculation treatment is settled, and supernatant obtained by settlement is sequentially subjected to filtration treatment and electrodialysis treatment, the number of equipment is greatly increased, and the process is more complex.
The black water flash evaporation device disclosed in CN105056560A mainly has the function of relieving steam, scouring and abrasion to equipment in the solid black water flash evaporation process. The patent technology basically has no substantial improvement on the treatment effect, the energy-saving effect and the water-saving effect of the whole slag water treatment system.
CN205948388U discloses a flash evaporation-heat exchange integrated apparatus, which comprises a tower body, wherein a partition plate of the tower body is divided into an evaporation chamber at the lower part and a hot water chamber at the upper part, a tray is arranged in the evaporation chamber, and the tray is located in a heat exchange section of the hot water chamber. The method has good effects on the aspects of flash evaporation, solid separation and the like of black water. It also has significant disadvantages: (1) the equipment only carries out single heat recovery, the temperature after primary flash evaporation is about 150-200 ℃, and the effect of heat recovery is limited; (2) the top of the tower gas phase of this equipment need set up the heat exchanger again and condense, and this heat exchanger is the floating head heat exchanger that the ABS type area colluded the circle usually, and the structure is more complicated, and the cost is comparatively expensive. (3) The gas phase condensation of the plant requires a large amount of circulating water; the coal gasification project is usually in the northwest and other places with short water resources, and is not economical and environment-friendly. (4) After the equipment is condensed, a gas-liquid separation tank needs to be arranged for separation, the equipment is complex, and the cost is increased. (5) The tray of the equipment adopts a single overflow tray, the application effect is not ideal when the liquid phase flow is large, and the conditions of flooding and the like are easy to occur. (6) The device has the phenomenon of low gas phase flow rate in the gas phase heat exchange part, and is suitable for small gasification devices.
Meanwhile, the treatment process based on the equipment also has a plurality of defects, such as CN110228830A, CN207498194U, CN207627955U, CN207828040U, CN209161731U and the like which are simple flash evaporation-separation-cooling-separation processes, and the main equipment comprises a high-pressure flash evaporation tank, a high-pressure flash evaporation primary heat exchanger, a high-pressure flash evaporation secondary heat exchanger and a high-pressure flash evaporation gas-liquid separation tank; then, a low-pressure flash process is carried out, and the equipment mainly comprises a low-pressure flash tank, a low-pressure flash condenser, a deaerator and the like; low-pressure flash process: because the first 2 times of flash separation are not thorough, a 2-stage vacuum flash device is required to be arranged. The whole slag water treatment process is complex and complicated, the equipment is huge, the number of heat exchange equipment is large, the loss of effective energy is large, the equipment efficiency is low, the occupied area is large, the manufacturing cost is large, and the like.
In addition, low temperature (relative) grey water mostly employs a series-partition heat exchange process. The grey water is subjected to primary heat exchange with steam at the top of a low-pressure flash tank by a grey water pump, then subjected to secondary heat exchange with steam at the top of a high-pressure flash tank in a heat exchanger, and finally pumped into a high-temperature and high-pressure washing tower by a pump; the second heat exchange in the two heat exchanges is limited by the driving force, so that the heat exchange is very incomplete, and a heat exchanger is connected in series behind the heat exchange. The heat exchange efficiency of the process is relatively low.
SUMMERY OF THE UTILITY MODEL
In view of the above shortcomings of the prior art, the present invention provides a flash evaporation stripping cooling system, which can utilize the system to treat black water generated in the coal gasification process, reduce the number of devices used in the treatment process, reduce the occupied area of the device, save a considerable amount of cooling water, and realize the complete recycling of slag water.
In order to achieve the above and other related objects, the present invention provides a flash stripping cooling system, which comprises a first flash stripping cooling tower, a second flash stripping cooling tower, a vacuum flash tank, a grey water tank, a settling tank, a condenser, and a vacuum flash separation tank;
the first flash steam stripping cooling tower, the second flash steam stripping cooling tower, the vacuum flash tank and the grey water tank are sequentially communicated along the black water input direction to form a black water passage; in the black water passage, the bottom of the vacuum flash tank is communicated with the grey water tank through a settling tank, and the top of the vacuum flash tank is communicated with the grey water tank through a condenser and a vacuum flash separation tank;
the ash water tank is respectively communicated with the first flash steam stripping cooling tower and the second flash steam stripping cooling tower along the ash water backflow direction to form an ash water backflow passage;
the first flash steam stripping cooling tower and the second flash steam stripping cooling tower form a condensed water loop along the flowing direction of condensed water.
Preferably, the first flash evaporation stripping cooling tower and the second flash evaporation stripping cooling tower are both flash evaporation stripping cooling towers, and the flash evaporation stripping cooling tower is sequentially provided with a flash evaporation chamber, a liquid phase retention chamber, a stripping chamber, a heat exchange chamber and a separation chamber from bottom to top; the steam stripping chamber is sequentially provided with a tower tray section, a liquid phase distributor and a gas phase distributor along the flow direction of steam, the tower tray section comprises a plurality of tower trays, the heat exchange chamber is internally provided with a heat exchanger section, and the heat exchanger section comprises a plurality of heat exchangers.
Preferably, be equipped with cone section, evaporation zone in proper order by supreme down in the flash chamber, the cone section is by supreme width grow gradually down, the bottom of cone section is equipped with the scum pipe, be equipped with the black water drain pipe on the lateral wall of cone section, be equipped with the black water inlet on the lateral wall of evaporation zone.
More preferably, the black water outlet pipe penetrates through the side wall of the cone section, one end of the black water outlet pipe is provided with a black water outlet, the black water outlet extends deep into the vertical axis position in the cone section, and the other end of the black water outlet pipe extends out of the cone section and has a downward opening.
Further preferably, the vertical distance between the black water outlet and the top of the cone section is 1/3-2/3 of the inner diameter of the top of the cone section.
More preferably, a spare black water outlet opening is formed in the side wall of the evaporation section.
Preferably, the liquid phase retention chamber is internally provided with a liquid phase retention section and a gas phase reducing section in sequence from bottom to top, and the gas phase reducing section gradually reduces in width from bottom to top.
More preferably, the bottom of the liquid phase retention section is provided with a partition plate.
Further preferably, the isolation plate is a seal head.
Further preferably, a liquid discharge pipe is arranged on the isolation plate, extends into the flash evaporation chamber and penetrates through the side wall of the flash evaporation chamber to form a liquid discharge port.
Most preferably, the liquid discharge pipe is in the form of a plurality of straight pipe sections in the flash chamber, and the bending angle between adjacent straight pipe sections is 120-145 degrees.
More preferably, a plurality of liquid inlet pipes are arranged in the liquid phase retention section, and the liquid inlet pipes penetrate through the side wall of the liquid phase retention section to form a liquid inlet.
Further preferably, the lower end of the liquid inlet pipe extends to the bottom of the liquid phase retention section.
More preferably, a liquid outlet is arranged on the side wall of the liquid phase staying section.
More preferably, a gas phase pipe is arranged in the liquid phase staying section, the gas phase pipe is vertically arranged, the lower end of the gas phase pipe penetrates through the isolation plate, and a gas cap is arranged outside the upper end of the gas phase pipe.
More preferably, the ratio of the diameter of the top surface to the diameter of the bottom surface of the gas phase reducing section is 0.1-1: 1, preferably 0.4-0.8: 1.
preferably, the trays are positioned perpendicular to the direction of vapor flow.
Preferably, the tray is a plate tray, and the tray comprises at least 2 downcomers.
Preferably, a first wire mesh demister is arranged in the gas phase distributor.
Preferably, one end of the liquid phase distributor horizontally penetrates through the stripping chamber to form an ash water inlet.
Preferably, the heat exchanger is disposed in parallel with a flow direction of the steam.
Preferably, a cooling grey water inlet and a cooling grey water outlet are arranged on the side wall of the heat exchanger section.
More preferably, the cooling grey water outlet is located above or below the cooling grey water inlet.
More preferably, the cooling grey water inlet is provided in the middle of the side wall of the heat exchanger section.
More preferably, the cooling grey water inlet is provided with an erosion shield.
Preferably, the heat exchanger is a spiral plate type or a shell and tube type heat exchanger.
More preferably, when the heat exchanger is a spiral plate type heat exchanger, a round header is arranged at the center of the heat exchanger section, and one end of the round header is communicated with the cooling grey water outlet through a pipeline.
Further preferably, the flow channel of the cooling fluid in the heat exchanger is spiral from outside to inside, and the flow channel of the steam fluid in the heat exchanger is in the gap of the spiral plate from bottom to top.
Further preferably, the gap between adjacent spiral plates in the heat exchanger is 2-28 mm.
More preferably, when the heat exchanger is a tube type heat exchanger, the diameter of a heat exchange tube in the tube type heat exchanger is 19-57 mm, the wall thickness of the heat exchange tube is 0.8-3.5 mm, the tube spacing is 25-65 mm, and the length of the heat exchange tube is 0.5-6 m.
Further preferably, the tube pass flow velocity of the heat exchange tube is 3-25 m/s.
More preferably, when the heat exchanger is a tube type heat exchanger, the number of passes of a shell pass of the heat exchange tube in the tube type heat exchanger is 1-4 passes.
More preferably, when the heat exchanger is a tube type heat exchanger, a baffle plate is arranged on the shell side of the heat exchange tube in the tube type heat exchanger, and the shape of the baffle plate is selected from one of a single-arch shape, a double-arch shape, a three-arch shape, a circular ring shape, a segment shape, a hole type baffle plate and a spiral shape.
Further preferably, the circle defect rate of the baffle plate is 10-55%; the distance between the baffle plates is 1/5-3/5 of the outer diameter of the heat exchanger section.
Further preferably, the shell-side flow velocity of the baffle plate is 1-3.5 m.
Preferably, the upper end and the lower end of the heat exchanger in the heat exchanger section are respectively detachably connected with the inner wall of the heat exchange chamber.
Preferably, a second wire mesh demister is arranged above the heat exchanger section in the heat exchange chamber.
Preferably, the top of the separation chamber is provided with an air outlet.
Preferably, the first flash steam stripping cooling tower is a high-pressure flash steam stripping cooling tower, and the pressure of the high-pressure flash steam stripping cooling tower is greater than 0.5MPaG and less than or equal to 2.0 MPaG.
Preferably, the second flash stripping cooling tower is a low-pressure flash stripping cooling tower, and the pressure of the low-pressure flash stripping cooling tower is 0.01-0.5 MPaG.
Preferably, the first flash steam stripping cooling tower is communicated with the gasification furnace and used for inputting black water from the gasification furnace.
Preferably, the gasifier is in communication with the evaporation section of the flash chamber.
Preferably, the vacuum flash tank is communicated with the black water slag removing pool through a pipeline.
Preferably, a mixer is arranged on a pipeline between the vacuum flash tank and the settling tank along the black water output direction.
Preferably, the condenser is arranged on the top of the vacuum flash tank.
Preferably, a flash vacuum pump is externally connected with the vacuum flash separation tank.
Preferably, a grey water pump unit and an air cooler are sequentially arranged on a pipeline between the grey water tank and the first flash steam stripping cooling tower along the grey water output direction, and the grey water pump unit is also communicated with the second flash steam stripping cooling tower through a pipeline.
Preferably, the ash water pump unit is selected from one of a single ash water pump and a double ash water pump.
More preferably, when the grey water pump unit is a single grey water pump, a flow regulating valve is arranged on the single grey water pump.
More preferably, when the grey water pump unit is a double-grey water pump, the double-grey water pump is a high-pressure grey water pump and a low-pressure grey water pump, the high-pressure grey water pump is arranged on a pipeline between the grey water tank and the first flash steam stripping cooling tower, and the low-pressure grey water pump is arranged on a pipeline between the grey water tank and the second flash steam stripping cooling tower.
Preferably, the ash water tank is respectively communicated with the heat exchanger sections in the heat exchange chambers of the first flash stripping cooling tower and the second flash stripping cooling tower.
Preferably, the first flash stripping cooling tower is respectively communicated with the conversion section and the synthesis gas washing tower, and is used for inputting condensed water from the conversion section and outputting the circulated condensed water to the synthesis gas washing tower.
Preferably, a stripping chamber of the first flash steam stripping cooling tower is communicated with the conversion section, a liquid phase retention chamber of the first flash steam stripping cooling tower is communicated with the syngas washing tower, a washing tower feed pump is arranged on a pipeline between the liquid phase retention chamber and the syngas washing tower, an outlet of the washing tower feed pump is communicated with the syngas washing tower, and an inlet of the washing tower feed pump is communicated with a liquid outlet of the liquid phase retention chamber of the first flash steam stripping cooling tower.
Preferably, the first flash steam stripping cooling tower is communicated with a grey water inlet of a stripping chamber in the second flash steam stripping cooling tower through a cooling grey water outlet of the heat exchange chamber, and is used for inputting condensed water flowing through the heat exchanger section in the heat exchange chamber into the second flash steam stripping cooling tower, and the second flash steam stripping cooling tower is communicated with the heat exchange chamber in the first flash steam stripping cooling tower through a liquid outlet of the liquid phase retention chamber, and is used for refluxing the condensed water input into the second flash steam stripping cooling tower to the heat exchanger section of the heat exchange chamber of the first flash steam stripping cooling tower.
Preferably, a flash stripping cooling tower feed pump is arranged on a pipeline between a liquid outlet of the liquid phase retention chamber of the second flash stripping cooling tower and the heat exchange chamber in the first flash stripping cooling tower.
Preferably, a cooling grey water inlet and a cooling grey water outlet of the second flash stripping cooling tower are externally connected with circulating cooling water to form a cooling loop.
Preferably, the first flash steam stripping cooling tower and the second flash steam stripping cooling tower are respectively communicated with a sulfur recovery device along the tail gas output direction.
As above, the utility model provides a pair of flash distillation strip cooling system forms the type of construction of high pressure flash distillation strip cooling tower and low pressure flash distillation strip cooling tower, has following beneficial effect:
(1) the utility model provides a pair of flash distillation strip cooling system, wherein, after using novel flash distillation strip cooling tower, the operating range increase is applicable to bigger large-scale gasification equipment, and it simplifies whole black water treatment process, and traditional process flow relatively has reduced the occupation of land of 2 heat exchangers, 2 flash separation jars, has reduced the equipment use quantity in the processing technology, has reduced the area of device, has reduced the operating cost of sediment water treatment process.
(2) The utility model provides a pair of flash distillation strip cooling system has formed 2 grades of cold fluid internal circulations and cover level utilization, and equipment integrates, and the flow is simplified, and the energy consumption reduces, has saved a large amount of circulating water to realize the retrieval and utilization completely of sediment water.
(3) The utility model provides a pair of flash stripping cooling system, grey water after the cooling of furthest's utilization. The high-temperature flash steam exchanges heat with the high-temperature flash steam of the cooling tower of the high-pressure flash stripping tower, and then enters the cooling tower of the low-pressure flash stripping tower for secondary heat exchange; energy is greatly saved.
(4) According to the flash evaporation stripping cooling system provided by the utility model, the cooling tower of the high-pressure flash evaporation stripping tower does not need circulating water for cooling, but uses low-temperature grey water for cooling, so that the consumption of circulating water is saved; the method has a particularly important meaning in northwest areas where water resources are scarce. The cleaner grey water is further cooled through an air cooler, so that energy is saved; when the temperature is lower in winter in the north, the air cooler can be cut out through the bypass of the air cooler, so that the operation cost is further saved.
(5) The utility model provides a pair of flash stripping cooling system uses novel flash stripping cooling tower's heat transfer effect to promote 25% at least than heat transfer device.
(6) The utility model provides a pair of flash stripping cooling system, it is integrated inside flash stripping cooling tower with the complicated, the high external heat exchanger of cost of traditional external structure to applied simple structure, heat transfer efficiency height, be applicable to the spiral plate heat exchanger that contains solid liquid. The inner heat exchanger can be segmented according to the process requirement; for example, low temperature liquid in the plant, which needs to be warmed, can be sent to the stripping cooling tower again. Low-temperature grey water is used for cooling and heat exchange in a high-pressure flash evaporation section; instead of circulating water in the traditional process, and realizes the graded utilization of the low-temperature grey water.
Drawings
Fig. 1 shows a schematic structure diagram of a flash stripping cooling tower in the present invention.
Fig. 2 is a schematic diagram of a flash stripping cooling system according to the present invention.
Reference numerals
1 flash chamber
11 conical section
111 slag discharge pipe
112 black water outlet pipe
113 black water outlet
12 evaporation stage
121 black water inlet
122 spare outlet for black water
2 liquid phase residence chamber
21 liquid phase residence section
211 division board
212 Drain pipe
213 liquid outlet
214 straight pipe section
215 liquid inlet pipe
216 liquid inlet
217 liquid outlet
218 gas phase tube
219 air cap
22 gas phase reducing section
3 stripping chamber
31 tray section
311 tray
312 downcomer
32 liquid phase distributor
321 grey water inlet
33 gas phase distributor
331 first screen demister
4 Heat exchange chamber
41 heat exchanger section
411 heat exchanger
412 cooling grey water inlet
413 cool grey water outlet
414 second wire mesh demister
5 separation chamber
51 air outlet
S1 first flash steam stripping cooling tower
S2 second flash stripping cooling tower
S3 vacuum flash tank
S4 grey water tank
S5 settling tank
S6 condenser
S7 vacuum flash separation tank
S8 gasification furnace
S9 slag fishing pool using black water
S10 mixer
S11 flash vacuum pump
S12 high-pressure ash water pump
S13 air cooler
S14 low-pressure ash water pump
S15 conversion section
S16 synthetic gas washing tower
S17 washing tower feeding pump
S18 flash stripping cooling tower feed pump
S19 sulphur recovery unit
Detailed Description
The following description is provided for illustrative purposes, and other advantages and features of the present invention will become apparent to those skilled in the art from the following detailed description.
Please refer to fig. 1-2. It should be understood that the structure, ratio, size and the like shown in the drawings attached to the present specification are only used for matching with the content disclosed in the specification, so as to be known and read by those skilled in the art, and are not used for limiting the limit conditions that the present invention can be implemented, so that the present invention has no technical essential meaning, and any structure modification, ratio relationship change or size adjustment should still fall within the scope that the technical content disclosed in the present invention can cover without affecting the function that the present invention can produce and the purpose that the present invention can achieve. Meanwhile, the terms such as "upper", "lower", "left", "right", "middle" and "one" used in the present specification are for convenience of description, and are not intended to limit the scope of the present invention, and changes or adjustments of the relative relationship thereof may be made without substantial technical changes, and the present invention is also regarded as the scope of the present invention.
The utility model provides a flash evaporation stripping cooling system, as shown in figure 2, comprising a first flash evaporation stripping cooling tower S1, a second flash evaporation stripping cooling tower S2, a vacuum flash evaporation tank S3, a grey water tank S4, a settling tank S5, a condenser S6 and a vacuum flash evaporation separation tank S7;
the first flash steam stripping cooling tower S1, the second flash steam stripping cooling tower S2, the vacuum flash tank S3 and the grey water tank S4 are sequentially communicated along the black water input direction to form a black water passage; in the black water passage, the bottom of the vacuum flash tank S3 is communicated with a grey water tank S4 through a settling tank S5, and the top of the vacuum flash tank S3 is communicated with a grey water tank S4 through a condenser S6 and a vacuum flash separation tank S7;
the grey water tank S4 is respectively communicated with the first flash stripping cooling tower S1 and the second flash stripping cooling tower S2 along the grey water reflux direction to form a grey water reflux passage;
the first flash stripping cooling tower S1 and the second flash stripping cooling tower S2 form a condensate loop in the direction of flow of condensate.
The utility model provides a flash evaporation stripping cooling system, the first flash evaporation stripping cooling tower S1 and the second flash evaporation stripping cooling tower S2 are flash evaporation stripping cooling towers, as shown in figure 1, the flash evaporation stripping cooling tower is provided with a flash evaporation chamber 1, a liquid phase retention chamber 2, a stripping chamber 3, a heat exchange chamber 4 and a separation chamber 5 from bottom to top in sequence; the stripping chamber 3 is sequentially provided with a tray section 31, a liquid phase distributor 32 and a gas phase distributor 33 along the flow direction of steam, the tray section 31 is internally provided with a plurality of trays 311, the heat exchange chamber 4 is internally provided with a heat exchanger section 41, and the heat exchanger section 41 is internally provided with a plurality of heat exchangers 411.
In the above flash evaporation stripping cooling tower, as shown in fig. 1, a cone section 11 and an evaporation section 12 are sequentially arranged in the flash evaporation chamber 1 from bottom to top, the width of the cone section 11 gradually increases from bottom to top, a slag discharge pipe 111 is arranged at the bottom of the cone section 11, a black water outlet pipe 112 is arranged on the side wall of the cone section 11, and a black water inlet 121 is arranged on the side wall of the evaporation section 12.
In a preferred embodiment, as shown in fig. 1, the black water outlet pipe 112 penetrates through the side wall of the cone segment 11, one end of the black water outlet pipe 112 is provided with a black water outlet 113, the black water outlet 113 extends to a vertical axial position in the cone segment 11, and the other end of the black water outlet pipe 112 extends out of the cone segment 11 and is opened downwards.
In a further preferred embodiment, as shown in FIG. 1, the vertical distance between the black water outlet 113 and the top of the cone segment 11 is 1/3-2/3 of the inner diameter of the top of the cone segment 11.
In a preferred embodiment, as shown in fig. 1, the side wall of the evaporation section 12 is provided with a black liquid outlet spare port 122.
In the flash stripping cooling tower, as shown in fig. 1, a liquid phase retention section 21 and a gas phase reducing section 22 are sequentially arranged in the liquid phase retention chamber 2 from bottom to top, and the width of the gas phase reducing section 22 gradually decreases from bottom to top.
In a preferred embodiment, as shown in fig. 1, the liquid phase residence section 21 is provided with a partition 211 at the bottom. The partition plate 211 is used for separating the flash chamber 1 from the liquid phase residence chamber 2.
In a further preferred embodiment, as shown in fig. 1, the isolation plate 211 is a head. Specifically, the seal head is a downward convex seal head, and the shape of the seal head is hemispherical or elliptical. The end socket can be cancelled according to the operation condition.
In a further preferred embodiment, as shown in fig. 1, the partition 211 is provided with a drain pipe 212, and the drain pipe 212 extends into the flash chamber 1 and penetrates through the side wall of the flash chamber 1 to form a drain port 213. The drain pipe 212 is used for discharging the dirty liquid in the liquid-phase retention chamber 2.
Furthermore, as shown in fig. 1, the liquid discharge pipe 212 is formed into a plurality of straight pipe sections 214 in the flash chamber 1, and the bending angle between adjacent straight pipe sections 214 is 120 to 145 °. The angle of curvature of the straight tube section 214 may prevent clogging of the drain tube 212. The straight pipe sections 214 adjacent to each other are arcuate and cannot have any corner to block the drain pipe 212.
In a preferred embodiment, as shown in fig. 1, a plurality of liquid inlet pipes 215 are disposed in the liquid phase residence section 21, and the liquid inlet pipes 215 form a liquid inlet 216 through the sidewall of the liquid phase residence section 21.
In a further preferred embodiment, as shown in fig. 1, the lower end of said liquid inlet pipe 215 extends to the bottom of the liquid phase retention section 21. Specifically, the lower end of the liquid inlet pipe 215 extends to a tangent of the partition plate 211. Is used for forming a liquid seal and preventing air leakage.
In a preferred embodiment, as shown in fig. 1, the liquid phase retention section 21 is provided with a liquid outlet 217 on the side wall. The outlet port 217 is used to deliver black water to the syngas scrubber S16 via scrubber feed pump S17.
In a preferred embodiment, as shown in fig. 1, a gas phase pipe 218 is arranged in the liquid phase retention section 21, the gas phase pipe 218 is vertically arranged, the lower end of the gas phase pipe 218 penetrates through the partition board 211, and an air cap 219 is arranged outside the upper end of the gas phase pipe 218.
In a further preferred embodiment, as shown in fig. 1, the gas cap 219 is a standard half head, and the shape of the gas cap 219 is selected from one of a cone, a square, and a circle.
In a preferred embodiment, as shown in fig. 1, the ratio of the diameter of the top surface to the diameter of the bottom surface of the gas phase reducing section 22 is 0.1 to 1: 1, preferably 0.4-0.8: 1. the gas phase reducing section 22 increases the flow velocity of the gas phase and improves the effects of gas-liquid phase heat exchange and mass transfer.
In the flash stripping cooling tower described above, the trays 311 are positioned perpendicular to the direction of vapor flow, as shown in fig. 1.
In the flash stripping cooling tower, as shown in fig. 1, the tray 311 is a plate tray, and the tray 311 includes at least 2 downcomers 312.
In a preferred embodiment, the tray is a double flooded tray. The double-overflow plate type tower tray has better heat exchange performance and operation elastic range, and reduces the occurrence of flooding.
In a further preferred embodiment, the double weir plate trays are double weir fixed valve trays. The tray 311 was made of 316L, and had a diameter of 2800mm, a plate thickness of 4mm, a plate pitch of 600mm, an opening ratio of 13%, and a bubbling region area of 47.7%.
In a preferred embodiment, the width of the top of the downcomer 312 is 600mm, the width of the bottom is 475mm, the gap at the bottom of the downcomer 312 is 70mm, the outlet weir height is 70mm, and the weir length is 2750 mm.
In the flash stripping cooling tower described above, the liquid phase distributor 32 is a conventionally used liquid phase distributor, i.e., a sparger, as shown in fig. 1.
In a preferred embodiment, the liquid phase distributor 32 types include, but are not limited to, elbow, notched, perforated calandria, multiple empty coil, distribution disk, trough distributors.
In the flash stripping cooling tower described above, the gas phase distributor 33 is a conventionally used gas phase distributor, as shown in fig. 1. In a preferred embodiment, the gas phase distributor 33 is a wire-mesh distributor or a blade distributor.
In the flash stripping cooling tower, as shown in fig. 1, a first wire mesh demister 331 is disposed in the gas phase distributor 33.
In the flash stripping cooling tower described above, as shown in fig. 1, one end of the liquid phase distributor 32 horizontally penetrates the stripping chamber 3 to form a grey water inlet 321.
In the flash stripping cooling tower, the heat exchanger 411 is arranged in parallel with the flow direction of the steam as shown in fig. 1.
In the flash stripping cooling tower, as shown in fig. 1, a cooling grey water inlet 412 and a cooling grey water outlet 413 are provided on the side wall of the heat exchanger section 41.
In a preferred embodiment, the cooling grey water outlet 413 is located above or below the cooling grey water inlet 412.
In a preferred embodiment, the cooling grey water inlet 412 is provided in the middle of the side wall of the heat exchanger section 41.
In a preferred embodiment, the cooling grey water inlet 412 is provided with an erosion shield. Specifically, the erosion preventing plate is a conventionally used erosion preventing plate, and is preferably an erosion preventing single plate or an erosion preventing ring plate.
In the flash stripping cooling tower, as shown in fig. 1, the heat exchanger 411 is a spiral plate or tube type heat exchanger, preferably a spiral plate type heat exchanger.
The spiral plate type or tube type heat exchanger has simple structure and low manufacturing cost, and can replace the prior floating head type heat exchanger with hook rings, which has high manufacturing cost and complex structure.
The heat exchange area of the heat exchanger 411 is large enough, the wall thickness is thin enough, the flow velocity ratio of the cooling medium is larger than that of the original ABS type heat exchanger, and the heat transfer coefficient can be improved by 1.25-2.5 times.
The spiral plate on the spiral plate type heat exchanger and the tube array on the tube array type heat exchanger are determined according to the heat exchange quantity and the requirement thereof.
In a preferred embodiment, when the heat exchanger 411 is a spiral plate heat exchanger, a round header is arranged at the center of the heat exchanger section 41, and one end of the round header is communicated with the cooling grey water outlet 413 through a pipeline. The heat exchanger sections 41 may be connected in series in multiple sections as appropriate.
Further, the flow channel of the cooling fluid in the heat exchanger 411 is spiral from outside to inside, and the flow channel of the steam fluid in the heat exchanger 411 is in the gap of the spiral plate from bottom to top. The flow directions of the cold fluid and the steam fluid are mutually perpendicular.
Further, the gap between adjacent spiral plates in the heat exchanger 411 is 2-28 mm, and preferably 6-18 mm.
Further, the material of the spiral plate in the heat exchanger 411 is stainless steel.
In a preferred embodiment, when the heat exchanger 411 is a tube type heat exchanger, the tube diameter of a heat exchange tube in the tube type heat exchanger is 19-57 mm, the wall thickness of the heat exchange tube is 0.8-3.5 mm, the tube spacing is 25-65 mm, and the length of the heat exchange tube is 0.5-6 m.
Further, the arrangement mode of the heat exchange tubes is selected from one of regular triangle, corner triangle, square and corner square.
Further, the heat exchange tube is made of carbon steel or stainless steel, preferably stainless steel.
Further, the tube pass flow velocity of the heat exchange tube is 3-25 m/s.
In a preferred embodiment, when the heat exchanger 411 is a tube type heat exchanger, the number of passes of a shell pass of a heat exchange tube in the tube type heat exchanger is 1-4 passes, and 1 pass is preferred.
In a preferred embodiment, when the heat exchanger 411 is a tubular heat exchanger, a baffle plate is disposed on the shell side of the heat exchange tube in the tubular heat exchanger, and the shape of the baffle plate is selected from one of a single-arch shape, a double-arch shape, a three-arch shape, a circular ring shape, a segment shape, a hole-type baffle plate and a spiral shape, and is preferably a single-arch shape. The baffle plate is used for strengthening heat exchange.
Further, the circle defect rate of the baffle plate is 10-55%, preferably 25-45%; the distance between the baffles is 1/5-3/5 of the outer diameter of the heat exchanger section 41, preferably 1/3.
Furthermore, the shell-side flow velocity of the baffle plate is 1-3.5 m, preferably 1.5-2.5 m.
In the flash evaporation stripping cooling tower, as shown in fig. 1, the upper and lower ends of the heat exchanger 411 in the heat exchanger section 41 are detachably connected with the inner wall of the heat exchange chamber 4. The detachable connection is through flange joint. Can be conveniently overhauled, disassembled, cleaned and replaced.
In the flash stripping cooling tower, as shown in fig. 1, a second wire mesh demister 414 is arranged above the heat exchanger section 41 in the heat exchange chamber 4. The second wire mesh demister 414 can more thoroughly remove liquid droplets entrained in the gas phase.
In the flash stripping cooling tower, as shown in fig. 1, the top of the separation chamber 5 is provided with a gas outlet 51.
The utility model provides a pair of flash evaporation strip cooling system, as shown in FIG. 2, first flash evaporation strip cooling tower S1 is high pressure flash evaporation strip cooling tower, high pressure flash evaporation strip cooling tower' S pressure is for being > 0.5MPaG and being less than or equal to 2.0 MPaG.
In a flash stripping cooling system provided by the present invention, as shown in fig. 2, the second flash stripping cooling tower S2 is a low-pressure flash stripping cooling tower, and the pressure of the low-pressure flash stripping cooling tower is 0.01-0.5 MPaG.
In the utility model provides a pair of flash stripping cooling system, as shown in fig. 2, first flash stripping cooling tower S1 is linked together with gasifier S8 for by gasifier S8 input black water. The gasification furnace S8 is a pulverized coal type or water coal slurry type gasification furnace.
In a preferred embodiment, as shown in fig. 2, the gasification furnace S8 is communicated with the evaporation section 12 of the flash chamber 1.
In the flash evaporation stripping cooling system provided by the utility model, as shown in fig. 2, the vacuum flash tank S3 is communicated with the slag dragging pool S9 through a pipeline and black water. The black water slag fishing pool S9 is a conventionally used black water slag fishing pool and is used for carrying out liquid-solid separation on coal slag and coal ash.
In the utility model provides a pair of flash stripping cooling system, as shown in FIG. 2, be equipped with blender S10 along black water output direction on the pipeline between vacuum flash tank S3 and settling tank S5. The mixer S10 is a conventionally used mixer, specifically, the mixer S10 is an axial flow mixer.
In a flash stripping cooling system provided by the present invention, as shown in fig. 2, the condenser S6 is disposed on the top of the vacuum flash tank S3.
In the flash stripping cooling system provided by the present invention, as shown in fig. 2, the cooling medium of the condenser S6 is circulating cooling water.
In the utility model provides a pair of flash stripping cooling system, as shown in FIG. 2, vacuum flash separation jar S7 is external to have flash vacuum pump S11. The flash vacuum pump S11 is a water ring vacuum pump.
The utility model provides a pair of in flash stripping cooling system, be equipped with grey water pump unit, air cooler S13 along grey water output direction in proper order on the pipeline between grey water groove S4 and the first flash stripping cooling tower S1, grey water pump unit still is linked together through pipeline and second flash stripping cooling tower S2.
In a preferred embodiment, the grey water pump unit is selected from one of a single grey water pump or a double grey water pump.
In a further preferred embodiment, when the grey water pump unit is a single grey water pump, a flow regulating valve is arranged on the single grey water pump. The single grey water pump performs flow distribution regulation through a flow regulating valve, and controls the proportion of the grey water flow entering the heat exchange section 41 of the first flash stripping cooling tower S1 and the stripping chamber 3 of the second flash stripping cooling tower S2.
In a further preferred embodiment, as shown in fig. 2, when the ash water pump unit is a dual ash water pump, the dual ash water pump is a high pressure ash water pump S12 and a low pressure ash water pump S14, respectively, the high pressure ash water pump S12 is disposed on the pipeline between the ash water tank S4 and the first flash stripping cooling tower S1, and the low pressure ash water pump S14 is disposed on the pipeline between the ash water tank S4 and the second flash stripping cooling tower S2.
The single ash water pump, the high-pressure ash water pump S12 and the low-pressure ash water pump S14 are centrifugal pumps. The outlet pressure of the high pressure gray water pump S12 is greater than the low pressure gray water pump S14. The air cooler S13 is a heat exchanger using air as a cooling medium.
In a preferred embodiment, as shown in fig. 2, the grey water tank S4 is in communication with the heat exchanger sections 41 in the heat exchange chamber 4 of the first flash stripping cooling tower S1 and the second flash stripping cooling tower S2, respectively.
In the flash evaporation stripping cooling system provided by the utility model, as shown in fig. 2, the first flash evaporation stripping cooling tower S1 respectively with transform workshop section S15, synthetic gas scrubbing tower S16 is communicated with the conversion section S15 for inputting condensed water and outputting the circulated condensed water to the synthesis gas scrubber S16. The conversion section S15 is a carbon monoxide conversion section which is used for producing reaction H by CO through conversion reaction2For adjusting the hydrocarbon ratio. Specifically, condensed water from the shift converter S15 in the coal gasification project is shifted, and the condensed water in the shift converter S15 is derived from entrained water in the syngas or water produced by shift reaction
The condensate contains H2S is acidic, has high corrosivity to equipment pipelines and is not easy to recycle, and the equipment can treat the waste liquid which is inconvenient to recycle due to good gas-liquid separation performance. So the overhead contains a higher concentration of H2S acid gas to the sulphur recovery unit S19.
In a preferred embodiment, as shown in fig. 2, the stripping chamber 3 of the first flash steam stripping cooling tower S1 is in communication with the shift section S15, the liquid phase retention chamber 2 of the first flash steam stripping cooling tower S1 is in communication with the syngas scrubber tower S16, a scrubber feed pump S17 is provided in the conduit between the liquid phase retention chamber 2 and the syngas scrubber tower S16, the outlet of the scrubber feed pump S17 is in communication with the syngas scrubber tower S16, and the inlet of the scrubber feed pump S17 is in communication with the liquid outlet 217 of the liquid phase retention chamber 2 of the first flash steam stripping cooling tower S1.
The scrubber feed pump S17 is a centrifugal pump and the scrubber feed pump S17 can be driven by an electric or steam driven machine, preferably an electric driven machine.
The utility model provides a pair of in flash evaporation strip cooling system, as shown in fig. 2, first flash evaporation carries cooling tower S1 to be linked together through cooling grey water export 413 of heat transfer chamber 4 and grey water import 321 of strip chamber 3 among second flash evaporation strip cooling tower S2 for with the comdenstion water input second flash evaporation strip cooling tower S2 of heat exchanger section 41 in the heat transfer chamber 4, second flash evaporation strip cooling tower S2 is linked together through liquid outlet 217 and the heat transfer chamber 4 among the first flash evaporation strip cooling tower S1 of liquid phase dwell chamber 2, is used for carrying the heat exchanger section 41 of heat exchange chamber 4 of the comdenstion water backward flow first flash evaporation strip cooling tower S1 of second flash evaporation cooling tower S2.
In a preferred embodiment, as shown in fig. 2, a flash stripping cooling tower feed pump S18 is provided on the pipeline between the liquid outlet 217 of the liquid phase residence chamber 2 of the second flash stripping cooling tower S2 and the heat exchange chamber 4 of the first flash stripping cooling tower S1.
In a preferred embodiment, as shown in fig. 2, the cooling grey water inlet 412 and the cooling grey water outlet 413 of the second flash stripping cooling tower S2 are externally connected with circulating cooling water to form a cooling loop.
The utility model provides a pair of flash evaporation strip cooling system, as shown in FIG. 2, first flash evaporation strip cooling tower S1, second flash evaporation strip cooling tower S2 are linked together with sulphur recovery unit S19 along tail gas output direction respectively. The sulfur recovery device S19 is used for recovering sulfur or treating H-containing gas at the downstream of the tower top gas2And S gas device.
The use of a flash stripping cooling system of the present invention is illustrated by the following examples.
After obtaining a flash stripping cooling system prepared as described above, as shown in fig. 1-2, black water was fed from the quench chamber of the gasifier S8 into the flash chamber 1 of the first flash stripping cooling tower S1 at a black water flow rate of 314400kg/h, a solid content of 0.02, a pressure of 4.2MpaG, and a temperature of 193 ℃. From the synthesis gas scrubber S16, the grey water was fed to the stripping chamber 3 of the first flash stripping cooling tower S1 at a flow rate of 100852.19kg/h, a solids content of 0.00845 and a temperature of 182 ℃. The black and grey water were separately depressurized to 0.7MpaG to a first flash stripping cooling tower S1. The black water is flashed in the flash chamber 1 to form first steam, and the first steam flows upwards through the liquid phase retention chamber 2 via the gas phase pipe 218, enters the stripping chamber 3 and is mixed with the grey water to perform sufficient countercurrent mass and heat transfer. The grey water may also be the stripping chamber 3 of a first flash stripping cooling tower S1, which is refluxed from a grey water tank S4, at a flow rate of 375467.56kg/h and a temperature of 125And 2 ℃. The first steam leaving the uppermost tray 311 in the stripping chamber 3 of the first flash steam stripping cooling tower S1 enters the heat exchanger section 41 of the heat exchange chamber 4 at a temperature of 125 ℃, and the heat exchange area of the heat exchanger 411 in the heat exchanger section 41 is 104.73m2The heat exchanger power was 229.72 kw. Cooling to 60 ℃ after heat exchange to obtain first tail gas, and sending the first tail gas to a sulfur recovery device S19 for sulfur recovery.
The pressure of the black water slag water after flash evaporation in the flash chamber 1 of the first flash steam stripping cooling tower S1 is 0.8MpaG, and the temperature is 180 ℃. After the pressure difference is reduced to 0.13MpaG through a pressure reduction angle valve, the flash chamber 1 of the first flash stripping cooling tower S1 is input into the flash chamber 1 of the second flash stripping cooling tower S2, and the flash steam amount of the black water slag water in the flash chamber 1 of the second flash stripping cooling tower S2 is 34492.65 kg/h. The black water is flashed in the flash chamber 1 to form a second steam, and the second steam flows upwards through the liquid phase retention chamber 2 via the gas phase pipe 218, enters the stripping chamber 3 and is mixed with the grey water to perform sufficient countercurrent mass and heat transfer. The grey water is returned from grey water tank S4 to stripping chamber 3 of second flash stripping cooling tower S2, the flow rate of the grey water is 316983.83kg/h, and the temperature is 77 ℃. The second steam leaving the uppermost tray 311 in stripping chamber 3 of the second flash stripping cooling tower S2 enters the heat exchanger section 41 of heat exchange chamber 4, and the heat exchange area of the heat exchanger 411 in the heat exchanger section 41 is 122.6m2. Cooling to 60 ℃ after heat exchange to obtain second tail gas, and sending the second tail gas to a sulfur recovery device S19 for sulfur recovery.
The flow rate of the black water slag water after flashing in the flash chamber 1 of the second flash stripping cooling tower S2 is 365900.6kg/h, the pressure is 0.13MpaG, and the temperature is 125 ℃. Reducing the pressure to-0.03 MpaG through a pressure reduction angle valve by pressure difference, and then entering a vacuum flash tank S3 for flash evaporation, wherein the flash steam amount of the black water slag water in the vacuum flash tank S3 is 26417.1 kg/h. After the black water slag water is flashed in the vacuum flash tank S3, the grey water with the flow rate of 449904.75kg/h (the pressure is-0.08 MpaG, the temperature is 82 ℃) is discharged from the bottom of the vacuum flash tank S3 and flows into the settling tank S5 through potential difference, the slag is discharged from the bottom of the settling tank S5, and the upper layer clean grey water flows into the grey water tank S4 (the pressure is normal pressure, and the temperature is 77 ℃). One part of grey water in the grey water tank S4 is sent to a second flash stripping cooling tower S2 through a low-pressure grey water pump S14, the other part of grey water is boosted through a high-pressure grey water pump S12 at the flow rate of 39587.25kg/h, is firstly cooled to 45-50 ℃ through an air cooler S13(1470.182KW), and then is sent to a heat exchanger section 41 of a first flash stripping cooling tower S1 for heat exchange (the outlet is about 50-55 ℃).
In the process, the bottom slag water in the stripping chamber 3 of the first flash steam stripping cooling tower S1 is sent to a synthesis gas washing tower S16 for washing and utilization through a washing tower feed pump S17 (the flow rate is 407249.89kg/h, and the pressure is 4.68 MpaG). The heat exchange chamber 4 of the second flash stripping cooling tower S2 is cooled by circulating water (inlet at 32 ℃ C., outlet at 40 ℃ C.) with cooling water amount of 225790.63 kg/h.
In the above process, the size of the first flash steam stripping cooling tower S1 is 1 phi 4000 x 12900 in the flash chamber, 22 phi 4000 x 10000 in the gas phase reduction section in the liquid phase retention chamber 2, and 31 phi 2800 x 5400 in the tray section of the stripping chamber 3; heat exchanger segment 41 phi 2800 x 2000, central bore 500, heat exchange area 234.8m of heat exchange chamber 42The plate interval was 0.012 m.
The size of the second flash stripping cooling tower S2 is flash chamber 1 phi 3200 x 10500, liquid phase residence chamber 2 gas phase reducing section 22 phi 3200 x 4000, stripping chamber 3 tray section 31 phi 3200 x 4800, heat exchange chamber 4 heat exchanger section 41 phi 3200 x 1800, central hole 800, heat exchange area 283.6m2The plate spacing was 0.010 m.
The treatment process and the device for black water in example 1 are compared with the existing slag water treatment process and the device thereof, and the specific data are shown in table 1. As can be seen from Table 1, the technical scheme saves the circulating water: 152.94t/h, the proportion of the circulating water needed is reduced to 8.18 percent, and the water-saving effect is very obvious; the water amount sent to the washing tower is 7.07 percent larger than that of the traditional process. The energy-saving and water-saving effects are very obvious.
TABLE 1
To sum up, the utility model provides a pair of flash distillation strip cooling system, equipment integrates, and the flow is simplified, and the energy consumption reduces, and heat transfer effect improves, changes low temperature buck into and cools off to realized utilizing the grade of low temperature buck, saved a large amount of circulating water, and realized the complete retrieval and utilization of sediment water. Therefore, the utility model effectively overcomes various defects in the prior art and has high industrial utilization value.
The above embodiments are merely illustrative of the principles and effects of the present invention, and are not to be construed as limiting the invention. Modifications and variations can be made to the above-described embodiments by those skilled in the art without departing from the spirit and scope of the present invention. Accordingly, it is intended that all equivalent modifications or changes which may be made by those skilled in the art without departing from the spirit and technical spirit of the present invention be covered by the claims of the present invention.
Claims (10)
1. A flash stripping cooling system is characterized by comprising a first flash stripping cooling tower (S1), a second flash stripping cooling tower (S2), a vacuum flash tank (S3), a grey water tank (S4), a settling tank (S5), a condenser (S6) and a vacuum flash separation tank (S7);
the first flash stripping cooling tower (S1), the second flash stripping cooling tower (S2), the vacuum flash tank (S3) and the grey water tank (S4) are sequentially communicated along the black water input direction to form a black water passage; in the black water passage, the bottom of the vacuum flash tank (S3) is communicated with a grey water tank (S4) through a settling tank (S5), and the top of the vacuum flash tank (S3) is communicated with the grey water tank (S4) through a condenser (S6) and a vacuum flash separation tank (S7);
the grey water tank (S4) is respectively communicated with the first flash stripping cooling tower (S1) and the second flash stripping cooling tower (S2) along the grey water reflux direction to form a grey water reflux passage;
the first flash stripping cooling tower (S1) and the second flash stripping cooling tower (S2) form a condensate loop in a condensate flow direction.
2. A flash stripping cooling system according to claim 1, wherein the first flash stripping cooling tower (S1) and the second flash stripping cooling tower (S2) are both flash stripping cooling towers, and the flash stripping cooling towers are sequentially provided with a flash evaporation chamber (1), a liquid phase retention chamber (2), a stripping chamber (3), a heat exchange chamber (4) and a separation chamber (5) from bottom to top; the steam stripping chamber (3) is provided with a tray section (31), a liquid phase distributor (32) and a gas phase distributor (33) in sequence along the steam flowing direction, the tray section (31) is internally provided with a plurality of trays (311), the heat exchange chamber (4) is internally provided with a heat exchanger section (41), and the heat exchanger section (41) is internally provided with a plurality of heat exchangers (411).
3. A flash evaporation stripping cooling system according to claim 2, wherein a cone section (11) and an evaporation section (12) are sequentially arranged in the flash evaporation chamber (1) from bottom to top, the width of the cone section (11) gradually increases from bottom to top, a slag discharge pipe (111) is arranged at the bottom of the cone section (11), a black water outlet pipe (112) is arranged on the side wall of the cone section (11), and a black water inlet port (121) is arranged on the side wall of the evaporation section (12).
4. A flash stripping cooling system according to claim 3, wherein the black water outlet pipe (112) penetrates through the side wall of the cone section (11), one end of the black water outlet pipe (112) is provided with a black water outlet (113), the black water outlet (113) is deep to a vertical axial position in the cone section (11), and the other end of the black water outlet pipe (112) extends out of the cone section (11) and is opened downwards; and a black effluent standby port (122) is arranged on the side wall of the evaporation section (12).
5. A flash stripping cooling system according to claim 2, characterized in that the liquid phase retention chamber (2) is provided with a liquid phase retention section (21) and a gas phase reducing section (22) from bottom to top, and the gas phase reducing section (22) is gradually reduced in width from bottom to top.
6. A flash stripping cooling system according to claim 5, characterized in that the liquid phase residence chamber (2) further comprises any one or more of the following conditions:
a1, a partition board (211) is arranged at the bottom of the liquid phase retention section (21);
a2, a plurality of liquid inlet pipes (212) are arranged in the liquid phase staying section (21), and the liquid inlet pipes (212) penetrate through the side wall of the liquid phase staying section (21) to form a liquid inlet (216);
a3, a liquid outlet (217) is arranged on the side wall of the liquid phase staying section (21);
a4, a gas phase pipe (218) is arranged in the liquid phase staying section (21), the gas phase pipe (218) is vertically arranged, the lower end of the gas phase pipe (218) penetrates through the partition board (211), and an air cap (219) is arranged outside the upper end of the gas phase pipe (218).
7. A flash stripping cooling system according to claim 2, wherein the flash stripping cooling tower further comprises any one or more of the following conditions:
b1, wherein the tray (311) is a plate tray, and the tray (311) comprises at least 2 downcomers (312);
b2, a first wire mesh demister (331) is arranged in the gas phase distributor (33);
b3 one end of the liquid phase distributor (32) horizontally penetrates the stripping chamber (3) to form a grey water inlet (321);
b4, a cooling grey water inlet (412) and a cooling grey water outlet (413) are arranged on the side wall of the heat exchanger section (41);
b5, the heat exchanger (411) is a spiral plate type or a shell and tube type heat exchanger;
b6 a second wire mesh demister (414) is arranged above the heat exchanger section (41) in the heat exchange chamber (4);
b7 the top of the separation chamber (5) is provided with an air outlet (51).
8. A flash stripping cooling system according to claim 1, wherein the first flash stripping cooling tower (S1) is a high pressure flash stripping cooling tower having a pressure > 0.5MPaG and ≤ 2.0 MPaG.
9. A flash stripping cooling system according to claim 1, wherein the second flash stripping cooling tower (S2) is a low pressure flash stripping cooling tower having a pressure of 0.01-0.5 MPaG.
10. A flash stripping cooling system according to claim 1, further comprising any one or more of the following conditions:
c1 the first flash steam stripping cooling tower (S1) is communicated with a gasification furnace (S8);
c2, the vacuum flash tank (S3) is communicated with a slag removing pool (S9) of black water through a pipeline;
c3 a mixer (S10) is arranged on a pipeline between the vacuum flash tank (S3) and the settling tank (S5) along the output direction of black water; c4 the condenser (S6) is arranged on the top of the vacuum flash tank (S3);
c5 the vacuum flash separating tank (S7) is externally connected with a flash vacuum pump (S11);
c6, an ash water pump unit and an air cooler (S13) are sequentially arranged on a pipeline between the ash water tank (S4) and the first flash stripping cooling tower (S1) along the ash water output direction, and the ash water pump unit is also communicated with the second flash stripping cooling tower (S2) through a pipeline;
c7, the first flash steam stripping cooling tower (S1) is respectively communicated with a conversion section (S15) and a synthesis gas washing tower (S16);
c8, the first flash steam stripping cooling tower (S1) is communicated with a grey water inlet (321) of a stripping chamber (3) in a second flash stripping cooling tower (S2) through a cooling grey water outlet (413) of a heat exchange chamber (4), and the second flash stripping cooling tower (S2) is communicated with the heat exchange chamber (4) in the first flash steam stripping cooling tower (S1) through a liquid outlet (217) of a liquid phase retention chamber (2); c9 the first flash steam stripping cooling tower (S1) and the second flash steam stripping cooling tower (S2) are respectively communicated with a sulfur recovery device (S19) along the tail gas output direction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022451015.3U CN213823486U (en) | 2020-10-29 | 2020-10-29 | Flash evaporation stripping cooling system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202022451015.3U CN213823486U (en) | 2020-10-29 | 2020-10-29 | Flash evaporation stripping cooling system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN213823486U true CN213823486U (en) | 2021-07-30 |
Family
ID=77012075
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202022451015.3U Active CN213823486U (en) | 2020-10-29 | 2020-10-29 | Flash evaporation stripping cooling system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN213823486U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112107875A (en) * | 2020-10-29 | 2020-12-22 | 上海华谊工程有限公司 | Flash evaporation stripping cooling system and treatment process for black water by using same |
-
2020
- 2020-10-29 CN CN202022451015.3U patent/CN213823486U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112107875A (en) * | 2020-10-29 | 2020-12-22 | 上海华谊工程有限公司 | Flash evaporation stripping cooling system and treatment process for black water by using same |
| CN112107875B (en) * | 2020-10-29 | 2023-08-15 | 上海华谊工程有限公司 | Flash evaporation steam stripping cooling system and black water treatment process using same |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107399870B (en) | Texaco gasifier black water heat recovery processing system | |
| CN103435005B (en) | A kind of synthesis gas washing treatment process | |
| CN112107875B (en) | Flash evaporation steam stripping cooling system and black water treatment process using same | |
| CN213823486U (en) | Flash evaporation stripping cooling system | |
| CN105036443A (en) | Method and device for treating phenol ammonia wastewater in single-tower stripping mode by recovering steam condensate heat | |
| CN109666508B (en) | Transformation method for improving economic operation period of hydrogenation device | |
| CN103691211A (en) | Rotational-flow purifying device for gaseous product in fluidized-bed residual oil hydrogenation reactor and method for purifying gaseous product by same | |
| CN114890560B (en) | Delayed coking wastewater fine particle removal process device | |
| CN215559637U (en) | Black water treatment system | |
| CN106362428B (en) | A kind of low temperature shifting process lime set gas stripping process | |
| CN212741038U (en) | Gasification black water treatment device | |
| CN210457560U (en) | Black water treatment equipment | |
| CN211159197U (en) | Non-condensable gas recycling device in slag water treatment system | |
| CN210438686U (en) | Steam stripping device for Fischer-Tropsch synthesis intermediate oil product | |
| CN114477369A (en) | Phenol-ammonia wastewater pretreatment device and process for degassing and light and heavy oil synchronous separation | |
| CN209848633U (en) | Methanol washing and recovering device in methanol synthesis flash evaporation gas | |
| CN111747471A (en) | Black water treatment equipment | |
| CN217556131U (en) | Heat energy recovery device of slag water system | |
| CN205773852U (en) | Phenol ammonia waste water processing and utilizing system | |
| CN110498468A (en) | Phenolic wastewater treatment extraction tower and stripping column Processes and apparatus | |
| CN215909025U (en) | Industrial steam condensate water recycle system | |
| CN216426990U (en) | Equipment for reducing ammonia nitrogen index of coal gasification water system | |
| CN215462033U (en) | Ethanol separation recovery system in konjaku flour production | |
| CN1130359A (en) | Multi-cell heating system | |
| CN113244860B (en) | Fluidized bed hydrogenation reactor and using method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |