CN218145930U - High-pressure black water flash evaporation system for coal water slurry gasification process - Google Patents
High-pressure black water flash evaporation system for coal water slurry gasification process Download PDFInfo
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- CN218145930U CN218145930U CN202222004327.9U CN202222004327U CN218145930U CN 218145930 U CN218145930 U CN 218145930U CN 202222004327 U CN202222004327 U CN 202222004327U CN 218145930 U CN218145930 U CN 218145930U
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Abstract
The utility model discloses a coal slurry gasification flow high pressure black water flash distillation system, including branch pipe, flow mixing line, five notches have been seted up to the inside of branch pipe, and the flange board has been cup jointed to the outside of branch pipe bottom is fixed, and the bottom fixed mounting of branch pipe has the inclined plane pipe, and the bottom fixed mounting of inclined plane pipe has the end ring, and flow mixing line's bottom is provided with the Z11 valve. Through the branch pipe, the recovery technology solves the problems of high flash steam temperature rise and pressure exceeding after the heat exchange effect of the high-pressure flash evaporation condenser is reduced, eliminates the influence of flash steam torch discharge on the environment, and ensures the safe and stable long-period operation of the device.
Description
Technical Field
The utility model belongs to the technical field of the high-pressure black water flash distillation, concretely relates to coal slurry gasification flow high pressure black water flash distillation system.
Background
The high-pressure black water is subjected to reduced pressure flash evaporation to establish new gas-liquid balance and release certain heat, and a heat exchanger is adopted in the process design to recover the heat. The technological process of the coal water slurry gasification process flash evaporation system generally adopts three modes of secondary flash evaporation (high-pressure flash evaporation and vacuum flash evaporation), tertiary flash evaporation (high-pressure flash evaporation, low-pressure flash evaporation and vacuum flash evaporation) and four-stage flash evaporation (high-pressure 1 flash evaporation, high-pressure 2 flash evaporation, low-pressure flash evaporation and vacuum flash evaporation). Through different flash evaporation stage flow designs, the purposes of reducing the temperature of the black water, concentrating the solid content of the black water, resolving acid gas in the black water and recovering waste heat are achieved. In order to recover the heat of the high flash steam, a high-pressure flash condenser is arranged in the high-pressure flash steam phase flow, heat exchange is carried out between high-pressure grey water and the high flash steam in the system, waste heat recovery is carried out, and the temperature of the high flash steam is still about 173 ℃ after the high flash steam passes through the high-pressure flash steam condenser. In the actual operation of the device, because of the particularity of the process medium, the high-pressure flash condenser is easy to reduce the heat exchange effect due to ash scaling, the temperature of high flash steam discharged from the high-pressure flash condenser rises, and the pressure of a flash system exceeds the standard. In order to keep the device continuously running, a large amount of flash steam is forced to be discharged through a torch, the high flash steam cannot be effectively recovered, the surrounding environment is affected, and the device is shut down in severe cases.
Companies and design units with the same type of devices further reduce the high flash steam temperature, and a circulating water cooler is additionally arranged behind the high-pressure flash evaporation condenser, so that a large amount of circulating water is used for further reducing the high flash steam temperature. Although the design achieves the purposes of reducing the temperature and controlling the high flash pressure, the design has the following defects: 1. most of heat of high flash steam is taken away by circulating water, so that the heat cannot be effectively utilized, and the heat loss of the high flash steam is more; 2. increase the circulating water consumption of the device; 3. the energy consumption of the device is increased; 4. for a production device in operation, if no enough space exists on site, the improvement of the process is difficult to realize, the high-pressure black water flash evaporation is a key process for continuous operation of a coal gasification device, the heat exchange effect of a system is reduced to cause continuous deterioration of the whole coal gasification process, the device is shut down in a whole line in severe cases, and the problems of over-temperature and over-pressure caused by the reduction of the heat exchange effect of the high-pressure flash evaporation steam condenser in the conventional high-pressure black water flash evaporation process are solved.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a coal slurry gasification flow high pressure black water flash distillation system, has solved current high pressure black water flash distillation flow, the problem of the super temperature that brings after high pressure flash distillation vapour condenser heat transfer effect reduces, superpressure problem to the not enough of prior art existence.
In order to achieve the above object, the utility model provides a following technical scheme: coal slurry gasification process high pressure black water flash distillation system, including branch pipe, flow mixing line, five notches have been seted up to the inside of branch pipe, the fixed flange board that has cup jointed in the outside of branch pipe bottom, the bottom fixed mounting of branch pipe has the inclined plane pipe, the bottom fixed mounting of inclined plane pipe has the end ring, the bottom of flow mixing line is provided with the Z11 valve.
Preferably, five notches are uniformly distributed in the inner part of the branch pipe in a linear staggered mode.
By adopting the technical scheme, the device has the advantages that the device is uniformly injected into the high-pressure flash evaporation pipeline and is directly mixed with high-pressure flash evaporation steam.
Preferably, the opening angles of five of the notches are all 120 °.
Through adopting above-mentioned technical scheme, the advantage lies in inserting current pipeline in, sets up the angle and is convenient for circulate.
Preferably, the length of the branch pipe is 15CM, and the specification size of the branch pipe is matched with that of the flow mixing pipeline.
By adopting the technical scheme, the flow mixing pipeline has the advantage of being convenient to insert into the flow mixing pipeline.
Preferably, five of said notches are located at the top end of the manifold at intervals of 7 CM.
Through adopting above-mentioned technical scheme, the advantage lies in this district's section and makes the notch be located the inside of flow mixing pipeline, is convenient for carry out the operation.
Preferably, the branch pipe movably penetrates through the Z11 valve and extends to the interior of the process mixing pipeline.
By adopting the technical scheme, the novel LED lamp has the advantages of being convenient to install and use and convenient to implement the technical scheme.
Preferably, the specification size of the branch pipe and the flange plate is matched with the specification size of the Z11 valve.
Through adopting above-mentioned technical scheme, the advantage lies in when inserting Z11 valve and flow mixing pipeline inside, carries on spacingly and fixedly through the flange board.
Compared with the prior art, the beneficial effects of the utility model are that:
1. through the branch pipe that sets up, this waste heat recovery technique does not receive the restriction of place, pipeline arrangement in the device, only needs a carbon steel material pipeline to realize, convenient practicality, and can accomplish a series of constructions at the device operation in-process.
2. Through the arranged branch pipes, the flow of the recovery technology does not increase the equipment investment cost and is small in change compared with the flow improvement of additionally arranging a circulating water cooler, and only hundreds of yuan is spent on completing the flow improvement.
3. Through the branch pipe, the circulating water consumption is not increased in the recovery technology, the low-pressure grey water in the system is utilized for mixing heat exchange, and finally the low-pressure grey water returns to the deaerator and then is supplied to the device again for use, so that the cyclic utilization of the low-pressure grey water is realized, compared with the process of increasing a water cooler, the circulating water is saved by about 20t/h by a single-series device.
4. Through the branch pipe, the recovery technology solves the problems of high flash steam temperature rise and pressure exceeding after the heat exchange effect of the high-pressure flash evaporation condenser is reduced, eliminates the influence of flash steam torch discharge on the environment, and ensures the safe and stable long-period operation of the device.
5. Through the branch pipe that sets up, this recovery technology has improved the temperature of the lime set in the high pressure flash separation jar. The heat of the condensed liquid can meet the requirements of other medium process parameters in the deaerator, so that the use amount of 0.45MPa steam in the deaerator is reduced by 3.5t/h, the purposes of saving energy and reducing consumption of the device are achieved, and the production cost of the device is also reduced.
Drawings
FIG. 1 is a schematic view of a front perspective structure of the present invention;
FIG. 2 is a front sectional view of the mixing pipeline and branch pipe of the present invention;
fig. 3 is a flow chart of the improved waste heat recovery process after the branch pipe is inserted into the flow mixing pipeline.
In the figure: 1. a branch pipe; 2. a notch; 3. a flange plate; 4. a bottom ring; 5. an inclined tube; 6. a process mixing line; 7. a Z11 valve.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts all belong to the protection scope of the present invention.
As shown in fig. 1-3, the coal water slurry gasification process high-pressure black water flash evaporation system comprises a branch pipe 1 and a process mixing pipeline 6, wherein five notches 2 are formed in the branch pipe 1, a flange plate 3 is fixedly sleeved on the outer side of the bottom of the branch pipe 1, an inclined plane pipe 5 is fixedly installed at the bottom of the branch pipe 1, a bottom ring 4 is fixedly installed at the bottom of the inclined plane pipe 5, and a Z11 valve 7 is arranged at the bottom of the process mixing pipeline 6.
The working principle of the technical scheme is as follows:
the method comprises the steps of dividing low-pressure grey water from a grey water tank into two parts, feeding one part of the low-pressure grey water into a deaerator according to the original flow to serve as water supplement, uniformly injecting the other part of low-pressure grey water pipeline (provided with two stop valves 1# and 2# valves) into a high-pressure flash pipeline through Z111, directly mixing the low-pressure grey water with high-pressure flash steam, forming atomized steam by the low-pressure grey water at high temperature and high pressure to take away heat in the flash steam, feeding the atomized steam into a high-pressure flash separation tank through a Z112 (high-flash steam regulation outlet stop valve), condensing the atomized steam into condensate at the bottom of the separation tank, and feeding the condensate into the deaerator through a separation tank outlet regulating valve to achieve the purposes of reducing the temperature and the pressure of process flash steam and recovering waste heat.
In another embodiment, as shown in fig. 1 and 2, five notches 2 are uniformly distributed in the interior of the branch pipe 1 in a linear staggered manner.
The high-pressure flash steam is uniformly injected into the high-pressure flash pipeline through the branch pipe 1 and is directly mixed with the high-pressure flash steam.
In another embodiment, as shown in fig. 1 and 2, the opening angles of the five notches 2 are all 120 °.
All structures of the branch pipe 1 are added at the Z11 valve 7: a15 cm straight pipe is welded on a flange, five cuts with 120-degree angles are formed in a 7cm section, and the cut is inserted into an existing pipeline and is provided with an angle for facilitating circulation.
In another embodiment, as shown in FIGS. 1 and 2, the length of branch 1 is 15CM, and the size of branch 1 is adapted to the size of process mixing line 6.
The length of the branch pipe 1 is matched with the size of the process mixing pipeline 6 and the Z11 valve 7, so that the branch pipe can be conveniently inserted into the process mixing pipeline 6.
In another embodiment, as shown in fig. 1 and 2, five notches 2 are located at the top end 7CM of the branch pipe 1.
The notch 2 is formed such that the notch 2 is positioned inside the process mixing line 6 when the branch pipe 1 is inserted into the process mixing line 6, thereby facilitating the work.
In another embodiment, shown in FIGS. 2 and 3, branch 1 is movable through Z11 valve 7 and extends into the interior of process mixing line 6.
The diagram of the improved waste heat recovery process flow chart is as follows: black water from a chilling chamber of the gasification furnace and black water from a tower kettle of a washing tower are decompressed to 0.9MPa (G) and then enter a high-pressure flash tank (1130V 101/201/301), and flash evaporation is carried out in the high flash tank to reduce the temperature, concentrate the solid content, resolve purge gas and effectively recover heat.
And a second module: the water vapor flashed off from the high-pressure flash tank and most of the dissolved acid gas components are cooled to 173 ℃ by a high-pressure flash condenser (1130E 101/201/301),
and a third module: the cooled flash gas is separated by a high-pressure flash separation tank (1130V 102/202/302), the gas phase is sent to a sulfur-tolerant shift unit for further treatment,
and a fourth module: and after the cooled flash gas is separated by a high-pressure flash separation tank (1130V 102/202/302), the liquid phase recovered heat condensate is conveyed to a deaerator (1130V 002) and conveyed back to a system for utilization by a pump.
In another embodiment, shown in fig. 1 and 2, the dimensions of the manifold 1 and the flange plate 3 are adapted to the dimensions of the Z11 valve 7.
When branch pipe 1 and flange plate 3 insert Z11 valve 7 and flow hybrid pipeline 6 inside, carry on spacingly and fixed through flange plate 3 to carry out the operation through inclined plane pipe 5 and end ring 4 connecting line, the stable structure of being convenient for avoids becoming flexible.
The utility model discloses a theory of operation and use flow: dividing low-pressure grey water from a grey water tank into two parts, wherein one part enters a deaerator as a deaerator to replenish water according to the original flow, the other part of low-pressure grey water pipeline (two stop valves 1# and 2# are arranged on the pipeline) is uniformly injected into a high-pressure flash pipeline through Z111 (all structures of a branch pipe 1 are added at the position of Z111, namely a 15cm straight pipe is welded through a flange, five cuts with an angle of 120 degrees are formed at a section of 7cm, the cut is inserted into the existing pipeline), the high-pressure flash steam is directly mixed with the low-pressure grey water, atomized steam is formed by the low-pressure grey water under high temperature and high pressure, heat in the flash steam is taken away, the atomized steam enters a high-pressure flash separation tank through Z112 (a high-flash steam regulation outlet stop valve), the condensed liquid is condensed at the bottom of the separation tank, and then the low-pressure grey water is sent into the deaerator through a separation tank outlet regulating valve, the purposes of reducing the temperature and the pressure of the flash steam and recovering waste heat, and the operation attention of the using process is paid: the method comprises the steps of firstly, fully opening a stop valve No. 1, leading low-pressure grey water to a valve No. 2, secondly, fully opening a guide shower valve of a Z111 high-flash steam pipeline, thirdly, slowly controlling the amount of the sprayed low-pressure grey water through the valve No. 2, fourthly, preventing water hammer, adjusting according to the temperature of a pipeline behind a high-flash heat exchanger and the change trend of the temperature of a gas phase pipeline of a high-flash separation tank, adding a pipeline and an auxiliary valve in a graph 3, improving the flow, increasing equipment and pipelines, and improving the process flow of a high-pressure black water flash evaporation system of the existing coal water slurry gasification device, so that the problem of over-temperature and over-pressure in the operation process of the device is solved, the recovery and utilization of process waste heat are realized, the coal gasification device is half a year from the implementation, the consumption and efficiency reducing effects are obvious, steam is saved by about 1.5 tons, and the production cost is reduced by more than 180 ten thousand yuan.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (7)
1. Coal slurry gasification process high pressure black water flash system, including branch pipe (1), flow mixing line (6), its characterized in that: five notches (2) have been seted up to the inside of branch pipe (1), flange plate (3) have been fixed to have cup jointed in the outside of branch pipe (1) bottom, the bottom fixed mounting of branch pipe (1) has inclined plane pipe (5), the bottom fixed mounting of inclined plane pipe (5) has end ring (4), the bottom of flow mixing line (6) is provided with Z11 valve (7).
2. The coal water slurry gasification process high-pressure black water flash evaporation system of claim 1, wherein: five notches (2) are linearly and uniformly distributed in the branch pipe (1) in a staggered manner.
3. The coal water slurry gasification process high-pressure black water flash evaporation system of claim 1, wherein: the opening angles of the five notches (2) are all 120 degrees.
4. The coal water slurry gasification process high-pressure black water flash evaporation system of claim 1, which is characterized in that: the length of the branch pipe (1) is 15CM, and the specification and the size of the branch pipe (1) are matched with those of the process mixing pipeline (6).
5. The coal water slurry gasification process high-pressure black water flash evaporation system of claim 1, wherein: five notches (2) are positioned at the interval of 7CM at the top end of the branch pipe (1).
6. The coal water slurry gasification process high-pressure black water flash evaporation system of claim 1, wherein: the branch pipe (1) movably penetrates through the Z11 valve (7) and extends to the interior of the flow mixing pipeline (6).
7. The coal water slurry gasification process high-pressure black water flash evaporation system of claim 1, wherein: and the specification and the size of the branch pipe (1) and the flange plate (3) are matched with those of the Z11 valve (7).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222004327.9U CN218145930U (en) | 2022-08-01 | 2022-08-01 | High-pressure black water flash evaporation system for coal water slurry gasification process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222004327.9U CN218145930U (en) | 2022-08-01 | 2022-08-01 | High-pressure black water flash evaporation system for coal water slurry gasification process |
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| CN218145930U true CN218145930U (en) | 2022-12-27 |
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| CN202222004327.9U Active CN218145930U (en) | 2022-08-01 | 2022-08-01 | High-pressure black water flash evaporation system for coal water slurry gasification process |
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- 2022-08-01 CN CN202222004327.9U patent/CN218145930U/en active Active
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