CN105561616A - Gasification ash water low-pressure flash heat energy utilizing device and heat energy utilizing method thereof - Google Patents
Gasification ash water low-pressure flash heat energy utilizing device and heat energy utilizing method thereof Download PDFInfo
- Publication number
- CN105561616A CN105561616A CN201610087493.6A CN201610087493A CN105561616A CN 105561616 A CN105561616 A CN 105561616A CN 201610087493 A CN201610087493 A CN 201610087493A CN 105561616 A CN105561616 A CN 105561616A
- Authority
- CN
- China
- Prior art keywords
- oxygen
- water
- steam
- eliminating device
- heat exchanger
- 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.)
- Granted
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
- B01D3/065—Multiple-effect flash distillation (more than two traps)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/10—Vacuum distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/38—Steam distillation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention belongs to a gasification ash water low-pressure flash heat energy utilizing device and a heat energy utilizing method thereof. The gasification ash water low-pressure flash heat energy utilizing device comprises a gasification furnace; a gasification furnace chilling chamber ash water drainage pipeline is connected with an inlet of a low-pressure flash tank through a first pressure reducing valve; a bottom liquid phase outlet of the low-pressure flash tank is connected with an inlet of a vacuum flash tank through a second pressure reducing valve; a bottom liquid phase outlet of the vacuum flash tank is connected with an inlet in the top of a setting tank; an ash slag discharge port is formed in the bottom of the setting tank; a liquid outlet in one side of the upper portion of the setting tank is connected with a liquid inlet in the upper portion of a gas extraction tower through the tube pass of a first pump and the tube pass of a first heat exchanger; a gas outlet in the top of the gas extraction tower is sequentially connected with the shell pass of the first heat exchanger and an inlet of a gas and liquid separator through a pipeline. The gasification ash water low-pressure flash heat energy utilizing device has the advantages that the structure is simple, design is reasonable, low-pressure flash steam has the deoxidizing, heat exchanging, vacuumizing and gas extracting effects at the same time, byproduct low-pressure steam of the whole device is reasonably and efficiently utilized, and the water quality of the whole ash water system is improved.
Description
Technical field
The invention belongs to the heat energy utilization field of gasification ash water, be specifically related to a kind of gasification ash water low pressure flash heat-energy utilizing device and heat energy utilization method thereof.
Background technology
Gasification installation many employings chilling process of Present Domestic coal chemical industry is as the wash cooling technique of gasification synthesis gas, effect utilizes water chilling high-temperature synthesis gas, after then reclaiming heat by flash system, remove the impurity in water by sedimentation, this process is called for short pulp water treatment process.In pulp water treatment process, HTHP dust-laden chilled water passes through flash distillation, more steam can be produced, it is whether reasonable that this some vapor utilizes, directly have influence on the efficiency of gasification installation, this steam utilization of current process technology ubiquity is unreasonable, need some vapor emptying, the problems such as gasification installation efficiency is low, buck water quality inferiority.
Summary of the invention
The object of the invention is to overcome defect of the prior art and provide a kind of structure simple, reasonable in design, make low pressure flash steam serve deoxygenation simultaneously, heat exchange, vacuumize and stripping effect, make the low-pressure steam of whole device by-product obtain reasonable efficiency utilization, improve a kind of gasification ash water low pressure flash heat-energy utilizing device and the heat energy utilization method thereof of whole ash water system water quality simultaneously.
The object of the present invention is achieved like this: comprise gasification furnace, gasification furnace shock chamber buck discharge line is connected with the import of low pressure flash chamber by the first pressure-reducing valve, the bottom liquid phases outlet of low pressure flash chamber is connected with the import of vacuum flasher by the second pressure-reducing valve, the bottom liquid phases outlet of vacuum flasher is connected with the import at subsider top, the bottom of described subsider is provided with grey slag outlet, the liquid outlet of side, subsider top is connected with the inlet on stripper top with the tube side of First Heat Exchanger by the first pump, the gas vent of stripper top is connected with the import of gas-liquid separator with the shell side of First Heat Exchanger successively by pipeline, the gas vent of described low pressure flash tank top respectively with the air inlet of the first oxygen-eliminating device, the shell side import of the second heat exchanger, the steam bleeding point that steam takes out lead device is connected with the air inlet of stripper bottom, the gas vent of vacuum flashing tank top takes out the steam bleeding point of lead device successively by steam, steam takes out the steam exhaust-gas mouth of lead device, the shell side of the 3rd heat exchanger is connected with the inlet on stripper top, moisturizing pipeline is by the 3rd heat exchanger tube pass, the tube side of the second heat exchanger is connected with the water inlet of the first oxygen-eliminating device, the shell-side outlet of the second heat exchanger is connected by the air inlet of pipeline with the first oxygen-eliminating device, liquid-phase outlet bottom described stripper is connected with the water inlet of the first oxygen-eliminating device by the second pump, the delivery port of described first oxygen-eliminating device is connected with shock chamber's water inlet of gasification furnace by the 3rd pump.
Described gas-liquid separator is provided with sour gas outlet and outfall, and described sour gas outlet is connected with burning torch by pipeline, and described outfall is connected with sewerage or water-coal-slurry preparation system by pipeline.
Be provided with threeway between the tube side of described second heat exchanger and the water inlet of the first oxygen-eliminating device, the 3rd end of described threeway is connected with boiler feedwater mouth by the second oxygen-eliminating device.
A heat energy utilization method for gasification ash water low pressure flash heat-energy utilizing device, the method comprises the steps:
Step one: the HTHP buck in gasification furnace shock chamber enters in low pressure flash chamber by shock chamber's buck discharge line and the first pressure-reducing valve, the pressure of described HTHP buck is: 1.0-8.7MPa, temperature is: 180-300 DEG C, and its inside is containing part coal ash and be dissolved with H
2the sour gas of S; Describedly by the pressure of buck after the first pressure-reducing valve be: 0.15-0.9MPa;
Step 2: the buck described in step one enters in low pressure flash chamber and carries out flash distillation, flash off 0.15-0.9MPa, temperature is that the low pressure steam of 120-175 DEG C enters the air inlet of the first oxygen-eliminating device respectively, the shell side import of the second heat exchanger, steam are taken out in the steam bleeding point of lead device and the air inlet of stripper bottom; The remaining solid waste water that contains carries out vacuum flash by entering in vacuum flasher after the second pressure-reducing valve decompression;
Step 3: carry out vacuum flash after entering vacuum flasher containing solid waste water in described step 2, flash off 60-80 DEG C, pressure is: the steam bleeding point that the vacuum flashing vapour of-0.08 ~-0.05MPa takes out lead device by steam enters steam and takes out in lead device, high concentration after flash distillation enters subsider sedimentation separation containing coal ash buck and goes out outside coal ash transmitting system to sell, and subsider supernatant liquor enters in stripper by the tube side of the first pump, First Heat Exchanger and the inlet on stripper top;
Step 4: low pressure steam described in step 2 enters steam by the steam bleeding point that steam takes out lead device and takes out in lead device as vacuum flasher provides vacuumizing condition, and enter in stripper by the inlet on stripper top after entering the water heat exchange in the shell side of the 3rd heat exchanger and the 3rd heat exchanger tube pass after mixing with the vacuum flashing vapour described in step 3, described with the water heat exchange in the 3rd heat exchanger tube pass after steam become the condensed water of 55-75 DEG C;
Step 5: low pressure steam described in step 2 by the air inlet of stripper bottom enter in stripper with the heat exchange described in the supernatant entered described in step 3 in stripper and step 4 after condensed water generation stripping react, generate the high-temperature-hot-water that the steam of 90-120 DEG C and temperature are 80-90 DEG C; Described temperature is that the high-temperature-hot-water of 80-90 DEG C is connected with the water inlet of the first oxygen-eliminating device;
Step 6: the steam of the 90-120 described in step 5 DEG C carries out gas-liquid separation by entering in gas-liquid separator after the shell side heat exchange of First Heat Exchanger, sour gas after gas-liquid separation enters burning torch combustion by sour gas outlet, and the sewage after gas-liquid separation enters subsequent handling by outfall sewerage or water-coal-slurry preparation system;
Step 7: after water enters the 3rd heat exchanger tube pass heat exchange by moisturizing pipeline, the low pressure steam entered in the tube side of the second heat exchanger and the shell side of the second heat exchanger carries out secondary heat exchange, in the water inlet that water after secondary heat exchange enters the first oxygen-eliminating device respectively and the second oxygen-eliminating device, described in the water entered in the second oxygen-eliminating device enter in boiler by boiler feedwater mouth;
Step 8: low pressure steam described in step 2 is entered in the shell side of the second heat exchanger with after the water heat exchange in step 7 by the shell side import of the second heat exchanger and enters the air inlet of the first oxygen-eliminating device;
Step 9: the low pressure steam described in step 2 enters in the first oxygen-eliminating device by the air inlet of the first oxygen-eliminating device; In described step 5, temperature is that the high-temperature-hot-water of 80-90 DEG C enters in the first oxygen-eliminating device by the water inlet of the first oxygen-eliminating device; Water in described step 7 after secondary heat exchange enters in the first oxygen-eliminating device by the water inlet of the first oxygen-eliminating device; Enter in the first oxygen-eliminating device by the air inlet of the first oxygen-eliminating device after low pressure steam heat exchange in described step 8; The above-mentioned material entered in the first oxygen-eliminating device is entered in the first oxygen-eliminating device and is entered in the shock chamber of gasification furnace by shock chamber's water inlet of the delivery port of the first oxygen-eliminating device, the 3rd pump and gasification furnace after deoxygenation.
Tool of the present invention has the following advantages:
1, low pressure flash vapour is as stripper stripping gas source, fully can go out H in condensate liquid by stripping
2the sour gas such as S, effectively avoid stripper to be corroded by sour gas, can also obtain the oxygen-eliminating device moisturizing source meeting water quality requirement;
2, low pressure flash vapour takes out lead device power resources as steam, can reduce the load that steam takes out lead device pump, improves steam and takes out lead device operating efficiency;
3, low pressure flash vapour is as the first oxygen-eliminating device heating source, can heat water in the first oxygen-eliminating device, and meanwhile, solubilized removes the oxygen gas component in water, and water oxygen gas is discharged with water vapour;
4, low pressure flash vapour heats moisturizing by heat exchanger, improves system water supplement temperature, boiler feed temperature is improved, and reduces boiler coal consumption, production cost is effectively reduced.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Detailed description of the invention
In order to there be understanding clearly to technical characteristic of the present invention, object and effect, now contrast accompanying drawing and the specific embodiment of the present invention is described, label identical in the various figures represents identical parts.For making simplified form, only schematically show and invent relevant part in each figure, they do not represent its practical structures as product.
As shown in Figure 1, the present invention includes gasification furnace 1, gasification furnace 1 shock chamber buck discharge line is connected with the import of low pressure flash chamber 3 by the first pressure-reducing valve 2, the bottom liquid phases outlet of low pressure flash chamber 3 is connected with the import of vacuum flasher 5 by the second pressure-reducing valve 4, the bottom liquid phases outlet of vacuum flasher 5 is connected with the import at subsider 6 top, the bottom of described subsider 6 is provided with grey slag outlet, the liquid outlet of side, subsider 6 top is connected with the inlet on stripper 9 top with the tube side of First Heat Exchanger 8 by the first pump 7, the gas vent at stripper 9 top is connected with the import of gas-liquid separator 10 with the shell side of First Heat Exchanger 8 successively by pipeline, the gas vent at described low pressure flash chamber 3 top respectively with the air inlet of the first oxygen-eliminating device 11, the shell side import of the second heat exchanger 12, the steam bleeding point that steam takes out lead device 13 is connected with the air inlet of stripper 9 bottom, the gas vent at vacuum flasher 5 top takes out the steam bleeding point of lead device 13 successively by steam, steam takes out the steam exhaust-gas mouth of lead device 13, the shell side of the 3rd heat exchanger 14 is connected with the inlet on stripper 9 top, moisturizing pipeline is by the 3rd heat exchanger 14 tube side, the tube side of the second heat exchanger 12 is connected with the water inlet of the first oxygen-eliminating device 11, the shell-side outlet of the second heat exchanger 12 is connected by the air inlet of pipeline with the first oxygen-eliminating device 11, liquid-phase outlet bottom described stripper 9 is connected with the water inlet of the first oxygen-eliminating device 11 by the second pump 15, the delivery port of described first oxygen-eliminating device 11 is connected with shock chamber's water inlet of gasification furnace 1 by the 3rd pump 16.Described gas-liquid separator 10 is provided with sour gas outlet and outfall, and described sour gas outlet is connected with burning torch 17 by pipeline, and described outfall is connected with sewerage or water-coal-slurry preparation system 18 by pipeline.Be provided with threeway between the tube side of described second heat exchanger 12 and the water inlet of the first oxygen-eliminating device 11, the 3rd end of described threeway is connected with boiler feedwater mouth 20 by the second oxygen-eliminating device 19.
A heat energy utilization method for gasification ash water low pressure flash heat-energy utilizing device, comprises the steps:
Step one: the HTHP buck in gasification furnace 1 shock chamber enters in low pressure flash chamber 3 by shock chamber's buck discharge line and the first pressure-reducing valve 2, the pressure of described HTHP buck is: 1.0-8.7MPa, temperature is: 180-300 DEG C, and its inside is containing part coal ash and be dissolved with H
2the sour gas of S; The described pressure by the rear buck of the first pressure-reducing valve 2 is: 0.15-0.9MPa;
Step 2: the buck described in step one enters in low pressure flash chamber 3 and carries out flash distillation, flash off 0.15-0.9MPa, temperature is that the low pressure steam of 120-175 DEG C enters the air inlet of the first oxygen-eliminating device 11 respectively, the shell side import of the second heat exchanger 12, steam are taken out in the steam bleeding point of lead device 13 and the air inlet of stripper 9 bottom; The remaining solid waste water that contains carries out vacuum flash by entering in vacuum flasher 5 after the second pressure-reducing valve 4 decompression;
Step 3: carry out vacuum flash after entering vacuum flasher 5 containing solid waste water in described step 2, flash off 60-80 DEG C, pressure is: the steam bleeding point that the vacuum flashing vapour of-0.08 ~-0.05MPa takes out lead device 13 by steam enters steam and takes out in lead device 13, high concentration after flash distillation enters subsider 6 sedimentation separation containing coal ash buck and goes out outside coal ash transmitting system to sell, and subsider 6 supernatant liquor enters in stripper 9 by the tube side of the first pump 7, First Heat Exchanger 8 and the inlet on stripper 9 top;
Step 4: low pressure steam described in step 2 enters steam by the steam bleeding point that steam takes out lead device 13 and takes out in lead device 13 as vacuum flasher 5 provides vacuumizing condition, and enter in stripper 9 by the inlet on stripper 9 top after entering the water heat exchange in the shell side of the 3rd heat exchanger 14 and the 3rd heat exchanger 14 tube side after mixing with the vacuum flashing vapour described in step 3, described with the water heat exchange in the 3rd heat exchanger 14 tube side after steam become the condensed water of 55-75 DEG C;
Step 5: low pressure steam described in step 2 by the air inlet of stripper 9 bottom enter in stripper 9 with enter the supernatant in stripper 9 described in step 3 and the condensed water generation stripping after the heat exchange described in step 4 reacts, generate the high-temperature-hot-water that the steam of 90-120 DEG C and temperature are 80-90 DEG C; Described temperature is that the high-temperature-hot-water of 80-90 DEG C is connected with the water inlet of the first oxygen-eliminating device 11;
Step 6: the steam of the 90-120 described in step 5 DEG C carries out gas-liquid separation by entering in gas-liquid separator 10 after the shell side heat exchange of First Heat Exchanger 8, sour gas after gas-liquid separation enters burning torch 17 combustion by sour gas outlet, and the sewage after gas-liquid separation enters subsequent handling by outfall sewerage or water-coal-slurry preparation system 18;
Step 7: after water enters the 3rd heat exchanger 14 tube side heat exchange by moisturizing pipeline, the low pressure steam entered in the tube side of the second heat exchanger 12 and the shell side of the second heat exchanger 12 carries out secondary heat exchange, in the water inlet that water after secondary heat exchange enters the first oxygen-eliminating device 11 respectively and the second oxygen-eliminating device 19, described in the water entered in the second oxygen-eliminating device 19 enter in boiler by boiler feedwater mouth 20;
Step 8: low pressure steam described in step 2 is entered in the shell side of the second heat exchanger 12 with after the water heat exchange in step 7 by the shell side import of the second heat exchanger 12 and enters the air inlet of the first oxygen-eliminating device 11;
Step 9: the low pressure steam described in step 2 enters in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11; In described step 5, temperature is that the high-temperature-hot-water of 80-90 DEG C enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Water in described step 7 after secondary heat exchange enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Enter in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11 after low pressure steam heat exchange in described step 8; The above-mentioned material entered in the first oxygen-eliminating device 11 is entered in the first oxygen-eliminating device 11 and is entered in the shock chamber of gasification furnace 1 by shock chamber's water inlet of the delivery port of the first oxygen-eliminating device 11, the 3rd pump 16 and gasification furnace 1 after deoxygenation.
In order to more detailed explanation the present invention, now the present invention is further elaborated in conjunction with the embodiments.Specific embodiment is as follows:
Embodiment one
A heat energy utilization method for gasification ash water low pressure flash heat-energy utilizing device, comprises the steps:
Step one: the HTHP buck in gasification furnace 1 shock chamber enters in low pressure flash chamber 3 by shock chamber's buck discharge line and the first pressure-reducing valve 2, the pressure of described HTHP buck is: 1.0MPa, temperature is: 180 DEG C, and it is inner containing part coal ash and the sour gas being dissolved with H2S; The described pressure by the rear buck of the first pressure-reducing valve 2 is: 0.15MPa;
Relate to rapid two: the buck described in step one enters in low pressure flash chamber 3 and carries out flash distillation, flash off 0.15MPa, temperature is that the low pressure steam of 120 DEG C enters the air inlet of the first oxygen-eliminating device 11 respectively, the shell side import of the second heat exchanger 12, steam are taken out in the steam bleeding point of lead device 13 and the air inlet of stripper 9 bottom; The remaining solid waste water that contains carries out vacuum flash by entering in vacuum flasher 5 after the second pressure-reducing valve 4 decompression;
Step 3: carry out vacuum flash after entering vacuum flasher 5 containing solid waste water in described step 2, flash off 60 DEG C, pressure is: the steam bleeding point that the vacuum flashing vapour of-0.05MPa takes out lead device 13 by steam enters steam and takes out in lead device 13, high concentration after flash distillation enters subsider 6 sedimentation separation containing coal ash buck and goes out outside coal ash transmitting system to sell, and subsider 6 supernatant liquor enters in stripper 9 by the tube side of the first pump 7, First Heat Exchanger 8 and the inlet on stripper 9 top;
Step 4: low pressure steam described in step 2 enters steam by the steam bleeding point that steam takes out lead device 13 and takes out in lead device 13 as vacuum flasher 5 provides vacuumizing condition, and enter in stripper 9 by the inlet on stripper 9 top after entering the water heat exchange in the shell side of the 3rd heat exchanger 14 and the 3rd heat exchanger 14 tube side after mixing with the vacuum flashing vapour described in step 3, described with the water heat exchange in the 3rd heat exchanger 14 tube side after steam become the condensed water of 55 DEG C;
Step 5: low pressure steam described in step 2 by the air inlet of stripper 9 bottom enter in stripper 9 with enter the supernatant in stripper 9 described in step 3 and the condensed water generation stripping after the heat exchange described in step 4 reacts, generate the high-temperature-hot-water that the steam of 90 DEG C and temperature are 80 DEG C; Described temperature is that the high-temperature-hot-water of 80 DEG C is connected with the water inlet of the first oxygen-eliminating device 11;
Step 6: the steam of 90 described in step 5 DEG C carries out gas-liquid separation by entering in gas-liquid separator 10 after the shell side heat exchange of First Heat Exchanger 8, sour gas after gas-liquid separation enters burning torch 17 combustion by sour gas outlet, and the sewage after gas-liquid separation enters subsequent handling by outfall sewerage or water-coal-slurry preparation system 18;
Step 7: after water enters the 3rd heat exchanger 14 tube side heat exchange by moisturizing pipeline, the low pressure steam entered in the tube side of the second heat exchanger 12 and the shell side of the second heat exchanger 12 carries out secondary heat exchange, in the water inlet that water after secondary heat exchange enters the first oxygen-eliminating device 11 respectively and the second oxygen-eliminating device 19, described in the water entered in the second oxygen-eliminating device 19 enter in boiler by boiler feedwater mouth 20;
Step 8: low pressure steam described in step 2 is entered in the shell side of the second heat exchanger 12 with after the water heat exchange in step 7 by the shell side import of the second heat exchanger 12 and enters the air inlet of the first oxygen-eliminating device 11;
Step 9: the low pressure steam described in step 2 enters in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11; In described step 5, temperature is that the high-temperature-hot-water of 80 DEG C enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Water in described step 7 after secondary heat exchange enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Enter in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11 after low pressure steam heat exchange in described step 8; The above-mentioned material entered in the first oxygen-eliminating device 11 is entered in the first oxygen-eliminating device 11 and is entered in the shock chamber of gasification furnace 1 by shock chamber's water inlet of the delivery port of the first oxygen-eliminating device 11, the 3rd pump 16 and gasification furnace 1 after deoxygenation.
Embodiment two
A heat energy utilization method for gasification ash water low pressure flash heat-energy utilizing device, comprises the steps:
Step one: the HTHP buck in gasification furnace 1 shock chamber enters in low pressure flash chamber 3 by shock chamber's buck discharge line and the first pressure-reducing valve 2, the pressure of described HTHP buck is: 8.7MPa, temperature is: 300 DEG C, and its inside is containing part coal ash and be dissolved with H
2the sour gas of S; The described pressure by the rear buck of the first pressure-reducing valve 2 is: 0.9MPa;
Step 2: the buck described in step one enters in low pressure flash chamber 3 and carries out flash distillation, flash off 0.9MPa, temperature is that the low pressure steam of 175 DEG C enters the air inlet of the first oxygen-eliminating device 11 respectively, the shell side import of the second heat exchanger 12, steam are taken out in the steam bleeding point of lead device 13 and the air inlet of stripper 9 bottom; The remaining solid waste water that contains carries out vacuum flash by entering in vacuum flasher 5 after the second pressure-reducing valve 4 decompression;
Step 3: carry out vacuum flash after entering vacuum flasher 5 containing solid waste water in described step 2, flash off 80 DEG C, pressure is: the steam bleeding point that the vacuum flashing vapour of-0.08MPa takes out lead device 13 by steam enters steam and takes out in lead device 13, high concentration after flash distillation enters subsider 6 sedimentation separation containing coal ash buck and goes out outside coal ash transmitting system to sell, and subsider 6 supernatant liquor enters in stripper 9 by the tube side of the first pump 7, First Heat Exchanger 8 and the inlet on stripper 9 top;
Step 4: low pressure steam described in step 2 enters steam by the steam bleeding point that steam takes out lead device 13 and takes out in lead device 13 as vacuum flasher 5 provides vacuumizing condition, and enter in stripper 9 by the inlet on stripper 9 top after entering the water heat exchange in the shell side of the 3rd heat exchanger 14 and the 3rd heat exchanger 14 tube side after mixing with the vacuum flashing vapour described in step 3, described with the water heat exchange in the 3rd heat exchanger 14 tube side after steam become the condensed water of 75 DEG C;
Step 5: low pressure steam described in step 2 by the air inlet of stripper 9 bottom enter in stripper 9 with enter the supernatant in stripper 9 described in step 3 and the condensed water generation stripping after the heat exchange described in step 4 reacts, generate the high-temperature-hot-water that the steam of 120 DEG C and temperature are 90 DEG C; Described temperature is that the high-temperature-hot-water of 90 DEG C is connected with the water inlet of the first oxygen-eliminating device 11;
Step 6: the steam of 120 described in step 5 DEG C carries out gas-liquid separation by entering in gas-liquid separator 10 after the shell side heat exchange of First Heat Exchanger 8, sour gas after gas-liquid separation enters burning torch 17 combustion by sour gas outlet, and the sewage after gas-liquid separation enters subsequent handling by outfall sewerage or water-coal-slurry preparation system 18;
Step 7: after water enters the 3rd heat exchanger 14 tube side heat exchange by moisturizing pipeline, the low pressure steam entered in the tube side of the second heat exchanger 12 and the shell side of the second heat exchanger 12 carries out secondary heat exchange, in the water inlet that water after secondary heat exchange enters the first oxygen-eliminating device 11 respectively and the second oxygen-eliminating device 19, described in the water entered in the second oxygen-eliminating device 19 enter in boiler by boiler feedwater mouth 20;
Step 8: low pressure steam described in step 2 is entered in the shell side of the second heat exchanger 12 with after the water heat exchange in step 7 by the shell side import of the second heat exchanger 12 and enters the air inlet of the first oxygen-eliminating device 11;
Step 9: the low pressure steam described in step 2 enters in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11; In described step 5, temperature is that the high-temperature-hot-water of 90 DEG C enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Water in described step 7 after secondary heat exchange enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Enter in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11 after low pressure steam heat exchange in described step 8; The above-mentioned material entered in the first oxygen-eliminating device 11 is entered in the first oxygen-eliminating device 11 and is entered in the shock chamber of gasification furnace 1 by shock chamber's water inlet of the delivery port of the first oxygen-eliminating device 11, the 3rd pump 16 and gasification furnace 1 after deoxygenation.
Embodiment three
A heat energy utilization method for gasification ash water low pressure flash heat-energy utilizing device, comprises the steps:
Step one: the HTHP buck in gasification furnace 1 shock chamber enters in low pressure flash chamber 3 by shock chamber's buck discharge line and the first pressure-reducing valve 2, the pressure of described HTHP buck is: 4.85MPa, temperature is: 240 DEG C, and its inside is containing part coal ash and be dissolved with H
2the sour gas of S; The described pressure by the rear buck of the first pressure-reducing valve 2 is: 0.525MPa;
Step 2: the buck described in step one enters in low pressure flash chamber 3 and carries out flash distillation, flash off 0.525MPa, temperature is that the low pressure steam of 147.5 DEG C enters the air inlet of the first oxygen-eliminating device 11 respectively, the shell side import of the second heat exchanger 12, steam are taken out in the steam bleeding point of lead device 13 and the air inlet of stripper 9 bottom; The remaining solid waste water that contains carries out vacuum flash by entering in vacuum flasher 5 after the second pressure-reducing valve 4 decompression;
Step 3: carry out vacuum flash after entering vacuum flasher 5 containing solid waste water in described step 2, flash off 70 DEG C, pressure is: the steam bleeding point that the vacuum flashing vapour of-0.065MPa takes out lead device 13 by steam enters steam and takes out in lead device 13, high concentration after flash distillation enters subsider 6 sedimentation separation containing coal ash buck and goes out outside coal ash transmitting system to sell, and subsider 6 supernatant liquor enters in stripper 9 by the tube side of the first pump 7, First Heat Exchanger 8 and the inlet on stripper 9 top;
Step 4: low pressure steam described in step 2 enters steam by the steam bleeding point that steam takes out lead device 13 and takes out in lead device 13 as vacuum flasher 5 provides vacuumizing condition, and enter in stripper 9 by the inlet on stripper 9 top after entering the water heat exchange in the shell side of the 3rd heat exchanger 14 and the 3rd heat exchanger 14 tube side after mixing with the vacuum flashing vapour described in step 3, described with the water heat exchange in the 3rd heat exchanger 14 tube side after steam become the condensed water of 65 DEG C;
Step 5: low pressure steam described in step 2 by the air inlet of stripper 9 bottom enter in stripper 9 with enter the supernatant in stripper 9 described in step 3 and the condensed water generation stripping after the heat exchange described in step 4 reacts, generate the high-temperature-hot-water that the steam of 105 DEG C and temperature are 85 DEG C; Described temperature is that the high-temperature-hot-water of 85 DEG C is connected with the water inlet of the first oxygen-eliminating device 11;
Step 6: the steam of 105 described in step 5 DEG C carries out gas-liquid separation by entering in gas-liquid separator 10 after the shell side heat exchange of First Heat Exchanger 8, sour gas after gas-liquid separation enters burning torch 17 combustion by sour gas outlet, and the sewage after gas-liquid separation enters subsequent handling by outfall sewerage or water-coal-slurry preparation system 18;
Step 7: after water enters the 3rd heat exchanger 14 tube side heat exchange by moisturizing pipeline, the low pressure steam entered in the tube side of the second heat exchanger 12 and the shell side of the second heat exchanger 12 carries out secondary heat exchange, in the water inlet that water after secondary heat exchange enters the first oxygen-eliminating device 11 respectively and the second oxygen-eliminating device 19, described in the water entered in the second oxygen-eliminating device 19 enter in boiler by boiler feedwater mouth 20;
Step 8: low pressure steam described in step 2 is entered in the shell side of the second heat exchanger 12 with after the water heat exchange in step 7 by the shell side import of the second heat exchanger 12 and enters the air inlet of the first oxygen-eliminating device 11;
Step 9: the low pressure steam described in step 2 enters in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11; In described step 5, temperature is that the high-temperature-hot-water of 85 DEG C enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Water in described step 7 after secondary heat exchange enters in the first oxygen-eliminating device 11 by the water inlet of the first oxygen-eliminating device 11; Enter in the first oxygen-eliminating device 11 by the air inlet of the first oxygen-eliminating device 11 after low pressure steam heat exchange in described step 8; The above-mentioned material entered in the first oxygen-eliminating device 11 is entered in the first oxygen-eliminating device 11 and is entered in the shock chamber of gasification furnace 1 by shock chamber's water inlet of the delivery port of the first oxygen-eliminating device 11, the 3rd pump 16 and gasification furnace 1 after deoxygenation.
A series of detailed description listed is above only illustrating for feasibility embodiment of the present invention; they are also not used to limit the scope of the invention, all do not depart from the skill of the present invention equivalent implementations done of spirit or change all should be included within protection scope of the present invention.It is to be noted in this article, " first ", " second " etc. only for differentiation each other, but not represent they significance level and order etc.
Claims (4)
1. a gasification ash water low pressure flash heat-energy utilizing device, comprise gasification furnace (1), it is characterized in that: gasification furnace (1) shock chamber buck discharge line is connected with the import of low pressure flash chamber (3) by the first pressure-reducing valve (2), the bottom liquid phases outlet of low pressure flash chamber (3) is connected by the import of the second pressure-reducing valve (4) with vacuum flasher (5), the bottom liquid phases outlet of vacuum flasher (5) is connected with the import at subsider (6) top, the bottom of described subsider (6) is provided with grey slag outlet, the liquid outlet of subsider (6) side, top is connected with the inlet on stripper (9) top with the tube side of First Heat Exchanger (8) by the first pump (7), the gas vent at stripper (9) top is connected with the import of gas-liquid separator (10) with the shell side of First Heat Exchanger (8) successively by pipeline, the gas vent at described low pressure flash chamber (3) top respectively with the air inlet of the first oxygen-eliminating device (11), the shell side import of the second heat exchanger (12), the steam bleeding point that steam takes out lead device (13) is connected with the air inlet of stripper (9) bottom, the gas vent at vacuum flasher (5) top takes out the steam bleeding point of lead device (13) successively by steam, steam takes out the steam exhaust-gas mouth of lead device (13), the shell side of the 3rd heat exchanger (14) is connected with the inlet on stripper (9) top, moisturizing pipeline is by the 3rd heat exchanger (14) tube side, the tube side of the second heat exchanger (12) is connected with the water inlet of the first oxygen-eliminating device (11), the shell-side outlet of the second heat exchanger (12) is connected by the air inlet of pipeline with the first oxygen-eliminating device (11), the liquid-phase outlet of described stripper (9) bottom is connected with the water inlet of the first oxygen-eliminating device (11) by the second pump (15), the delivery port of described first oxygen-eliminating device (11) is connected with shock chamber's water inlet of gasification furnace (1) by the 3rd pump (16).
2. a kind of gasification ash water low pressure flash heat-energy utilizing device according to claim 1, it is characterized in that: described gas-liquid separator (10) is provided with sour gas outlet and outfall, described sour gas outlet is connected with burning torch (17) by pipeline, and described outfall is connected with sewerage or water-coal-slurry preparation system (18) by pipeline.
3. a kind of gasification ash water low pressure flash heat-energy utilizing device according to claim 1, it is characterized in that: be provided with threeway between the tube side of described second heat exchanger (12) and the water inlet of the first oxygen-eliminating device (11), the 3rd end of described threeway is connected with boiler feedwater mouth (20) by the second oxygen-eliminating device (19).
4. the heat energy utilization method of a kind of gasification ash water low pressure flash heat-energy utilizing device according to claim 1, is characterized in that: the method comprises the steps:
Step one: the HTHP buck in gasification furnace (1) shock chamber enters in low pressure flash chamber (3) by shock chamber's buck discharge line and the first pressure-reducing valve (2), the pressure of described HTHP buck is: 1.0-8.7MPa, temperature is: 180-300 DEG C, and its inside is containing part coal ash and be dissolved with H
2the sour gas of S; The described pressure by the first pressure-reducing valve (2) buck is afterwards: 0.15-0.9MPa;
Step 2: the buck described in step one enters in low pressure flash chamber (3) and carries out flash distillation, flash off 0.15-0.9MPa, temperature is that the low pressure steam of 120-175 DEG C enters the air inlet of the first oxygen-eliminating device (11) respectively, the shell side import of the second heat exchanger (12), steam are taken out in the steam bleeding point of lead device (13) and the air inlet of stripper (9) bottom; The remaining solid waste water that contains carries out vacuum flash by entering in vacuum flasher (5) after the second pressure-reducing valve (4) decompression;
Step 3: carry out vacuum flash after entering vacuum flasher (5) containing solid waste water in described step 2, flash off 60-80 DEG C, pressure is: the steam bleeding point that the vacuum flashing vapour of-0.08 ~-0.05MPa takes out lead device (13) by steam enters steam and takes out in lead device (13), high concentration after flash distillation enters subsider (6) sedimentation separation containing coal ash buck and goes out outside coal ash transmitting system to sell, subsider (6) supernatant liquor is by the first pump (7), the tube side of First Heat Exchanger (8) and the inlet on stripper (9) top enter in stripper (9),
Step 4: low pressure steam described in step 2 enters steam by the steam bleeding point that steam takes out lead device (13) and takes out in lead device (13) and provide vacuumizing condition for vacuum flasher (5), and enter in stripper (9) by the inlet on stripper (9) top after entering the water heat exchange in the shell side of the 3rd heat exchanger (14) and the 3rd heat exchanger (14) tube side after mixing with the vacuum flashing vapour described in step 3, described with the water heat exchange in the 3rd heat exchanger (14) tube side after steam become the condensed water of 55-75 DEG C;
Step 5: low pressure steam described in step 2 by the air inlet of stripper (9) bottom enter in stripper (9) with enter the supernatant in stripper (9) described in step 3 and the condensed water generation stripping after the heat exchange described in step 4 reacts, generate the high-temperature-hot-water that the steam of 90-120 DEG C and temperature are 80-90 DEG C; Described temperature is that the high-temperature-hot-water of 80-90 DEG C is connected with the water inlet of the first oxygen-eliminating device (11);
Step 6: the steam of the 90-120 described in step 5 DEG C carries out gas-liquid separation by entering in gas-liquid separator (10) after the shell side heat exchange of First Heat Exchanger (8), sour gas after gas-liquid separation enters burning torch (17) combustion by sour gas outlet, and the sewage after gas-liquid separation enters subsequent handling by outfall sewerage or water-coal-slurry preparation system (18);
Step 7: after water enters the 3rd heat exchanger (14) tube side heat exchange by moisturizing pipeline, the low pressure steam entered in the tube side of the second heat exchanger (12) and the shell side of the second heat exchanger (12) carries out secondary heat exchange, in the water inlet that water after secondary heat exchange enters the first oxygen-eliminating device (11) respectively and the second oxygen-eliminating device (19), described in the water entered in the second oxygen-eliminating device (19) enter in boiler by boiler feedwater mouth (20);
Step 8: low pressure steam described in step 2 is entered in the shell side of the second heat exchanger (12) with after the water heat exchange in step 7 by the shell side import of the second heat exchanger (12) and enters the air inlet of the first oxygen-eliminating device (11);
Step 9: the low pressure steam described in step 2 enters in the first oxygen-eliminating device (11) by the air inlet of the first oxygen-eliminating device (11); In described step 5, temperature is that the high-temperature-hot-water of 80-90 DEG C enters in the first oxygen-eliminating device (11) by the water inlet of the first oxygen-eliminating device (11); Water in described step 7 after secondary heat exchange enters in the first oxygen-eliminating device (11) by the water inlet of the first oxygen-eliminating device (11); Enter in the first oxygen-eliminating device (11) by the air inlet of the first oxygen-eliminating device (11) after low pressure steam heat exchange in described step 8; Entered in the shock chamber of gasification furnace (1) by shock chamber's water inlet of the delivery port of the first oxygen-eliminating device (11), the 3rd pump (16) and gasification furnace (1) after the above-mentioned material entered in the first oxygen-eliminating device (11) enters the first oxygen-eliminating device (11) interior deoxygenation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610087493.6A CN105561616B (en) | 2016-02-04 | 2016-02-04 | A kind of gasification ash water low pressure flash heat-energy utilizing device and its heat energy utilization method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610087493.6A CN105561616B (en) | 2016-02-04 | 2016-02-04 | A kind of gasification ash water low pressure flash heat-energy utilizing device and its heat energy utilization method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105561616A true CN105561616A (en) | 2016-05-11 |
| CN105561616B CN105561616B (en) | 2017-11-14 |
Family
ID=55872585
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610087493.6A Active CN105561616B (en) | 2016-02-04 | 2016-02-04 | A kind of gasification ash water low pressure flash heat-energy utilizing device and its heat energy utilization method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105561616B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106492494A (en) * | 2016-12-07 | 2017-03-15 | 马宏波 | A kind of improve heat recovery rate and reduce the flash system of waste gas discharge |
| CN107541294A (en) * | 2016-06-28 | 2018-01-05 | 通用电气神华气化技术有限公司 | Hydrocarbon gasification system and internal heat integrate Application way |
| CN108167027A (en) * | 2017-12-27 | 2018-06-15 | 山西晋城无烟煤矿业集团有限责任公司 | Pressurized gasification chilling process vacuum flash vapour electricity-generating method |
| CN108911338A (en) * | 2018-08-17 | 2018-11-30 | 通用电气神华气化技术有限公司 | A kind of recovery ammonia total system and method |
| CN111426148A (en) * | 2019-12-17 | 2020-07-17 | 安徽昊源化工集团有限公司 | Method for reducing air separation energy consumption by utilizing flash evaporation low-pressure steam refrigeration of gasification furnace |
| CN112125365A (en) * | 2020-09-23 | 2020-12-25 | 中国天辰工程有限公司 | Coal gasification black water treatment system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101306899A (en) * | 2008-05-21 | 2008-11-19 | 山西丰喜肥业（集团）股份有限公司临猗分公司 | Grey water treatment technology for graded gasification furnace |
| US20100275600A1 (en) * | 2007-11-08 | 2010-11-04 | Speirs Brian C | System and method of recovering heat and water and generating power from bitumen mining operations |
| CN204434318U (en) * | 2015-01-27 | 2015-07-01 | 浙江丰登化工股份有限公司 | Gasification ash water waste-heat recovery device |
| CN105293804A (en) * | 2015-11-01 | 2016-02-03 | 张晓峰 | Coal gasification ash water treatment method |
| CN205461089U (en) * | 2016-02-04 | 2016-08-17 | 河南心连心化肥有限公司 | Gasification buck low pressure flash distillation heat utilization device |
-
2016
- 2016-02-04 CN CN201610087493.6A patent/CN105561616B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100275600A1 (en) * | 2007-11-08 | 2010-11-04 | Speirs Brian C | System and method of recovering heat and water and generating power from bitumen mining operations |
| CN101306899A (en) * | 2008-05-21 | 2008-11-19 | 山西丰喜肥业（集团）股份有限公司临猗分公司 | Grey water treatment technology for graded gasification furnace |
| CN204434318U (en) * | 2015-01-27 | 2015-07-01 | 浙江丰登化工股份有限公司 | Gasification ash water waste-heat recovery device |
| CN105293804A (en) * | 2015-11-01 | 2016-02-03 | 张晓峰 | Coal gasification ash water treatment method |
| CN205461089U (en) * | 2016-02-04 | 2016-08-17 | 河南心连心化肥有限公司 | Gasification buck low pressure flash distillation heat utilization device |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107541294A (en) * | 2016-06-28 | 2018-01-05 | 通用电气神华气化技术有限公司 | Hydrocarbon gasification system and internal heat integrate Application way |
| CN106492494A (en) * | 2016-12-07 | 2017-03-15 | 马宏波 | A kind of improve heat recovery rate and reduce the flash system of waste gas discharge |
| CN108167027A (en) * | 2017-12-27 | 2018-06-15 | 山西晋城无烟煤矿业集团有限责任公司 | Pressurized gasification chilling process vacuum flash vapour electricity-generating method |
| CN108911338A (en) * | 2018-08-17 | 2018-11-30 | 通用电气神华气化技术有限公司 | A kind of recovery ammonia total system and method |
| CN111426148A (en) * | 2019-12-17 | 2020-07-17 | 安徽昊源化工集团有限公司 | Method for reducing air separation energy consumption by utilizing flash evaporation low-pressure steam refrigeration of gasification furnace |
| CN112125365A (en) * | 2020-09-23 | 2020-12-25 | 中国天辰工程有限公司 | Coal gasification black water treatment system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105561616B (en) | 2017-11-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105561616A (en) | Gasification ash water low-pressure flash heat energy utilizing device and heat energy utilizing method thereof | |
| CN102674489B (en) | high-concentration ammonia-containing wastewater treatment method based on vapour compression | |
| CN107399870B (en) | Texaco gasifier black water heat recovery processing system | |
| CN105366751A (en) | Energy-saving environment-friendly integrated recycling and utilization method of coal chemical gasification washing black water high-temperature flashing steam | |
| CN204815724U (en) | Device is optimized to transform technology condensate strip | |
| CN103342399A (en) | Stripping system and stripping method for cleaning waste sodium hypochlorite in production of acetylene by virtue of calcium carbide method | |
| CN205461089U (en) | Gasification buck low pressure flash distillation heat utilization device | |
| CN110451596A (en) | A kind of carrier gas extraction HPE vapo(u)rization system | |
| CN202303332U (en) | Drainage waste heat recycling system | |
| CN204958641U (en) | Back processing apparatus of tower waste water is washed to coal industry carbon | |
| CN202909594U (en) | Novel steam-water separating tank for steam | |
| CN205760487U (en) | A kind of yellow phosphoric tail gas absorption plant | |
| CN211346401U (en) | Vacuum low-temperature dehydration equipment | |
| CN103848721A (en) | Aldehyde removal apparatus of pentaerythritol | |
| CN203429084U (en) | Formaldehyde production device for recycling heat energy of tail gas byproduct steam | |
| CN103467256B (en) | The formaldehyde production device of tail gas byproduct steam heat energy recycle and method | |
| CN204125192U (en) | The useless time sodium recycle device of acetylene | |
| CN211084880U (en) | Steam condensate water recycling system | |
| CN204607766U (en) | A kind of Waste water concentrating system | |
| CN203392883U (en) | Steam stripping system for waste sodium hypochlorite generated in acetylene cleaning through calcium carbide method | |
| CN210710749U (en) | S03Device for recovering waste heat of absorbing sulfuric acid | |
| CN202148269U (en) | Device for separating organic phases in hydroformylation reactions | |
| CN218106766U (en) | Energy recovery system for gasification black water four-stage flash evaporation | |
| CN215463135U (en) | Acid mist emptying pipeline of neutralization meta-hydrochloric acid solution tank | |
| CN213446257U (en) | Device for continuously discharging sewage of sulfur acid production recovery boiler |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 453731 Xinxiang Economic Development Zone, Henan Province (Xiaoji Town) Patentee after: Henan Xinlianxin Chemical Industry Group Co., Ltd. Address before: 453731 Henan Xinxiang Economic Development Zone Xiaoji Town Henan Xinlianxin Chemical Fertilizer Co., Ltd. Patentee before: Henan XInlianxin Fertiliser Limited Company |
|
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20200401 Address after: 453731 Xinxiang Economic Development Zone, Xinxiang City, Henan Province (Xiaoji Town) Co-patentee after: XINJIANG XINLIANXIN ENERGY CHEMICAL Co.,Ltd. Patentee after: Henan Xinlianxin Chemical Industry Group Co.,Ltd. Co-patentee after: Jiujiang Xinlianxin Chemical Fertilizer Co.,Ltd. Address before: 453731 Xinxiang Economic Development Zone, Henan Province (Xiaoji Town) Patentee before: Henan Xinlianxin Chemical Industry Group Co.,Ltd. |
|
| CP03 | Change of name, title or address | ||
| CP03 | Change of name, title or address |
Address after: 453731 Henan Xinxiang Economic Development Zone (Xiaoji Town) Patentee after: Henan Xinlianxin Chemical Industry Group Co.,Ltd. Patentee after: XINJIANG XINLIANXIN ENERGY CHEMICAL Co.,Ltd. Patentee after: Jiangxi xinlianxin Chemical Industry Co.,Ltd. Address before: 453731 Xinxiang Economic Development Zone, Xinxiang City, Henan Province (Xiaoji Town) Patentee before: Henan Xinlianxin Chemical Industry Group Co.,Ltd. Patentee before: XINJIANG XINLIANXIN ENERGY CHEMICAL Co.,Ltd. Patentee before: Jiujiang Xinlianxin Chemical Fertilizer Co.,Ltd. |