CN111420516A - Steam waste heat cascade utilization system for carbon capture absorbent regeneration system - Google Patents
Steam waste heat cascade utilization system for carbon capture absorbent regeneration systemDownload PDFInfo
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- 239000002918waste heatSubstances0.000titleclaimsabstractdescription37
- OKTJSMMVPCPJKN-UHFFFAOYSA-NCarbonChemical compound[C]OKTJSMMVPCPJKN-UHFFFAOYSA-N0.000titleclaimsabstractdescription25
- 229910052799carbonInorganic materials0.000titleclaimsabstractdescription25
- 230000008929regenerationEffects0.000titleclaimsabstractdescription21
- 238000011069regeneration methodMethods0.000titleclaimsabstractdescription21
- 230000002745absorbentEffects0.000titleclaimsabstractdescription17
- 239000002250absorbentSubstances0.000titleclaimsabstractdescription17
- XLYOFNOQVPJJNP-UHFFFAOYSA-NwaterSubstancesOXLYOFNOQVPJJNP-UHFFFAOYSA-N0.000claimsabstractdescription41
- 238000004821distillationMethods0.000claimsabstractdescription16
- 238000001704evaporationMethods0.000claimsabstractdescription16
- 230000008020evaporationEffects0.000claimsabstractdescription16
- 238000001816coolingMethods0.000claimsdescription9
- 238000007701flash-distillationMethods0.000claims4
- 239000013535sea waterSubstances0.000abstractdescription9
- UGFAIRIUMAVXCW-UHFFFAOYSA-NCarbon monoxideChemical compound[O+]#[C-]UGFAIRIUMAVXCW-UHFFFAOYSA-N0.000abstractdescription7
- 239000003546flue gasSubstances0.000abstractdescription7
- 238000004519manufacturing processMethods0.000abstractdescription2
- 239000002351wastewaterSubstances0.000abstractdescription2
- 238000000034methodMethods0.000description7
- 238000010521absorption reactionMethods0.000description5
- 238000009833condensationMethods0.000description4
- 230000005494condensationEffects0.000description4
- 230000000694effectsEffects0.000description4
- 239000007789gasSubstances0.000description4
- 230000002209hydrophobic effectEffects0.000description4
- 238000002485combustion reactionMethods0.000description3
- 238000010612desalination reactionMethods0.000description3
- 238000010438heat treatmentMethods0.000description3
- 230000010354integrationEffects0.000description3
- 238000009834vaporizationMethods0.000description3
- 230000008016vaporizationEffects0.000description3
- 238000004364calculation methodMethods0.000description2
- 238000010586diagramMethods0.000description2
- 238000010248power generationMethods0.000description2
- 238000004458analytical methodMethods0.000description1
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- 239000003245coalSubstances0.000description1
- 230000006835compressionEffects0.000description1
- 238000007906compressionMethods0.000description1
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- 238000007599dischargingMethods0.000description1
- 238000005516engineering processMethods0.000description1
- 239000000463materialSubstances0.000description1
- 238000005457optimizationMethods0.000description1
- 238000011084recoveryMethods0.000description1
- 238000003303reheatingMethods0.000description1
- 238000000926separation methodMethods0.000description1
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- 230000009466transformationEffects0.000description1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
- F01K17/02—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
- F22D1/32—Feed-water heaters, i.e. economisers or like preheaters arranged to be heated by steam, e.g. bled from turbines
- F22D1/325—Schematic arrangements or control devices therefor
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- General Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Gas Separation By Absorption (AREA)
Abstract
Description
Technical Field
The invention relates to the technical field of steam waste heat utilization, in particular to a steam waste heat cascade utilization system for a carbon capture absorbent regeneration system.
Background
Natural gas-steam combined cycle power generation combines the Brayton (Brayton) cycle of a gas turbine with the rankine (rankine) cycle of a steam turbine to form a combined cycle system. Taking a 9F-grade gas turbine of GE company in America as an example, the initial temperature of the gas is 1427 ℃, the simple cycle power under the ISO working condition is close to 300MW, and the efficiency is over 38%; the exhaust temperature of the combustion engine can reach over 600 ℃, the flow rate exceeds 2400t/h, and the design requirement of the three-pressure reheating steam-water circulation is met (the exhaust temperature of the combustion engine is higher than 560 ℃, and the flow rate is higher than 120 kg/s). The steam turbine adopts ultrahigh pressure circulation, the output of the steam turbine under the ISO working condition is about 153MW, and the power generation efficiency of the combined circulation reaches 56%.
Post combustion chemical CO absorption2The basic flow of the capture system includes: leading out original flue gas from a flue of a thermal power plant, cooling, then entering from the bottom of an absorption tower, performing countercurrent direct contact reaction with an absorbent barren solution, washing the purified flue gas with water, and then discharging the purified flue gas into the atmosphere; absorption of CO2Heating the rich solution by a lean-rich solution heat exchanger (reboiler), feeding the rich solution from the upper part of the regeneration tower, and performing countercurrent operation with steam in the tower; after the rich solution is heated and stripped for the second time, the sucked CO is desorbed2The mixed gas enters a compression liquefaction process after condensation and gas-water separation, and the desorbed barren solution enters an absorption tower again for cyclic absorption after cooling; the heat exchange steam required for the reboiler at the bottom of the regeneration tower is typically provided by the power plant steam system.
The carbon capture system and power plant steam system integration interface comprises the following 5 aspects: 1) raw flue gas enters a direct contact cooling tower of a carbon capture system; 2) extracting low-pressure steam of a steam turbine to be used as a heat source of the regeneration tower kettle type reboiler; 3) the condensed water of the reboiler is reinjected to steam-water circulation to be used as the water supply of the waste heat boiler; 4) the power plant water treatment system provides process water and cooling water for carbon capture; 5) the plant power system provides power for the carbon capture power utilization equipment. The heat exchange temperature difference of a coal economizer at the tail end of the waste heat boiler is changed, and the flue gas waste heat is not fully utilized.
Disclosure of Invention
In order to solve the problems in the prior art, the invention aims to provide a steam waste heat utilization device which has a good steam waste heat utilization effect and can effectively reduce CO2The capture system integrates a steam waste heat cascade utilization system for a carbon capture absorbent regeneration system that affects the thermal efficiency of the natural gas-steam combined cycle.
In order to achieve the purpose, the invention provides the following scheme:
the invention provides a steam waste heat cascade utilization system for a carbon capture absorbent regeneration system, which comprises a regeneration tower and a reboiler which are communicated, wherein the steam waste heat cascade utilization system comprises a temperature reduction unit, a low-pressure flash evaporation unit and a low-temperature multi-effect distillation unit, the reboiler is communicated with a low-pressure cylinder of a steam turbine through a low-pressure supersaturated steam supply pipeline, the temperature reduction unit cools and reduces the temperature of low-pressure supersaturated steam, the reboiler is communicated with the low-pressure flash evaporation unit through a condensed water supply pipeline, the low-pressure flash evaporation unit is communicated with the low-temperature multi-effect distillation unit through a low-temperature steam supply pipeline, and the condensed water in the low-pressure flash evaporation unit returns to a steam-water circulation system of a waste heat boiler at the temperature of below 70 ℃.
Preferably, the temperature reduction unit adjusts the parameters of the low-pressure supersaturated steam to be 0.4MPa and 140-160 ℃, and the temperature reduction unit is a cooling fan for cooling the low-pressure supersaturated steam supply pipeline or a variable-frequency temperature and pressure reduction device which is arranged on the low-pressure supersaturated steam supply pipeline and directly reduces the temperature and the pressure of the low-pressure supersaturated steam;
preferably, the temperature of the low pressure supersaturated steam is 150 ℃;
preferably, the parameters of the condensed water generated by the reboiler in the condensed water supply pipeline are 0.4MPa of pressure and 135-145 ℃;
preferably, the temperature of the condensed water is 140 ℃;
preferably, the low-pressure flash evaporation unit is a flash evaporator, and the temperature of steam supplied by the flash evaporator for the low-temperature multi-effect distillation unit is lower than 70 ℃.
Compared with the prior art, the invention has the following technical effects:
under the condition of carbon capture, the steam waste heat cascade utilization system for the carbon capture absorbent regeneration system utilizes the waste heat of the capture unit to desalt seawater or treat high-salinity wastewater, thereby not only realizing natural gas-steam combined cycle-CO2The cascade utilization of the unit energy is captured, the co-production is realized, the overall economy is improved, the temperature of condensed water in a steam-water circulating system returning to the waste heat boiler is reduced, and further the flue gas waste heat in the waste heat boiler system is fully utilized.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings needed to be used in the embodiments will be briefly described below, and it is obvious that the drawings in the following description are only some embodiments of the present invention, and it is obvious for those skilled in the art to obtain other drawings without inventive exercise.
FIG. 1 is a process flow diagram of a steam waste heat cascade utilization system for a carbon capture absorbent regeneration system of the present invention;
figure 2 is a process flow diagram of the low temperature multi-effect distillation unit of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
In order to make the aforementioned objects, features and advantages of the present invention comprehensible, embodiments accompanied with figures are described in further detail below.
The invention provides a steam waste heat cascade utilization system for a carbon capture absorbent regeneration system, which comprises a regeneration tower and a reboiler which are communicated, wherein the steam waste heat cascade utilization system comprises a temperature reduction unit, a low-pressure flash evaporation unit and a low-temperature multi-effect distillation unit, the reboiler is communicated with a low-pressure cylinder of a steam turbine through a low-pressure supersaturated steam supply pipeline, the temperature reduction unit cools and reduces the temperature of low-pressure supersaturated steam, the reboiler is communicated with the low-pressure flash evaporation unit through a condensed water supply pipeline, the low-pressure flash evaporation unit is communicated with the low-temperature multi-effect distillation unit through a low-temperature steam supply pipeline, and the condensed water in the low-pressure flash evaporation unit returns to a steam-water circulation system of a waste heat boiler at the temperature of below 70 ℃.
The temperature reduction unit adjusts the parameters of the low-pressure supersaturated steam to be 0.4MPa and 140-160 ℃, and is a cooling fan for cooling the low-pressure supersaturated steam supply pipeline or a variable-frequency temperature and pressure reduction device which is arranged on the low-pressure supersaturated steam supply pipeline and directly reduces the temperature and the pressure of the low-pressure supersaturated steam; further, as a preferable scheme, the temperature of the low-pressure supersaturated steam in the invention is 150 ℃;
in the invention, the parameters of the condensed water generated by the reboiler in the condensed water supply pipeline are 0.4MPa of pressure and 135-145 ℃; further, as a preferable scheme, the temperature of the condensed water in the invention is 140 ℃;
in the invention, the low-pressure flash evaporation unit is a flash evaporator, and in order to ensure the seawater desalination effect, the temperature of steam supplied by the flash evaporator to the low-temperature multi-effect distillation unit is lower than 70 ℃.
By combining the technical scheme disclosed above, the specific implementation scheme provided by the invention, which takes the GE 9F natural gas-steam combined cycle unit as an example, is as follows:
(1) thermodynamic system parameters
(2)CO2Capturing system parameters
(3) Generator set and carbon capture integrated parameters
(4) Optimization integration scheme-taking sea water desalination as example
The low-temperature Multi-effect distillation (L ow-temperature Multi-effect distillation, &lTtT transfer = L' &gTt L &lTt/T &gTt T-MED) process in the seawater desalination technology has low requirements for the temperature of a heat source, the maximum evaporation temperature is about 70 ℃, a certain amount of steam is input, and multiple times of secondary steam is obtained through multiple times of evaporation and condensation.
The design adopts 5-effect low-temperature multi-effect distillation, and the process flow is shown in figure 2.
The hydrophobic temperature of the reboiler is 140 ℃, the pressure is 4bar, the flow rate is 275t/h, and the reboiler enters a flash evaporator to generate steam. The flash tank pressure was 25kPa and the flash vapor amount was calculated by the following formula:
W·r＝F·C(ta-tb)
in the formula: w is the flash steam amount; r is the latent heat of vaporization of water; f is the drainage flow; t is taIs the hydrophobic temperature; t is tbIs the saturation temperature at the operating pressure of the flash tank.
The thermodynamic equation for a multistage flash vessel can be derived from the material and energy balance, and this example is calculated using the following equations, ignoring heat losses and condensation temperature drops:
in the formula: n is flash stage number;
the unheated evaporated seawater temperature; t is tFIs the temperature of the heated seawater; thetaIs the difference between the condensation temperature of steam in the preheater and the outlet temperature of the heated seawater, f' is a constant value and is taken as 0.238 × 10-3；ΔhmThe average value of the vaporization heat of the seawater in each flash evaporator is obtained; Δ hHThe heat of vaporization of the heating steam in the heating chamber, W is the total water yield; d is steam flow generated by the hydrophobic of the reboiler.
The flash steam flow is 37t/h, and the temperature is 65 ℃. The condensed water is used as a first-effect heat source, and the condensed water is cooled to about 65 ℃ and returns to the steam-water circulation of the waste heat boiler together with the condensed water of the flash tank. The operation temperature of 1-5 effects is respectively as follows: 60.7 ℃, 56.6 ℃, 52.8 ℃, 49 ℃ and 45.1 ℃, the hydrophobic heat of the recovery reboiler is 27.01MW, and the water quantity of the product of the low-temperature multi-effect distillation device is 155 t/h.
(5) Optimizing integrated thermal economy
Optimizing integrated system main performance parameters
Optimizing the integrated system according to the parameters
Balance calculation and thermal economic analysis of the transformation scheme to
The cost represents the economic performance of the system, and the calculation formula is as follows:
in this scenario, other estimation parameters include: the price of the power on the internet is 0.65 yuan/kW.h, and the price of the heat supply is 103.98 yuan/GJ; carbon tax 200 yuan/ton; the water selling price of the product is 4 yuan/ton. Integrates low-temperature multi-effect distillation integral body
The efficiency is improved by 0.18 percent, and the profit margin is improved by 0.2 percent. The integration scheme has certain popularization value for realizing high-efficiency energy utilization and multi-product output of the carbon capture unit.
The principle and the implementation mode of the invention are explained by applying a specific example, and the description of the embodiment is only used for helping to understand the method and the core idea of the invention; meanwhile, for a person skilled in the art, according to the idea of the present invention, the specific embodiments and the application range may be changed. In view of the above, the present disclosure should not be construed as limiting the invention.
Claims (6)
1. The utility model provides a steam waste heat cascade utilization system for absorbent regeneration system is caught to carbon, absorbent regeneration system is caught to carbon is including regenerator column and the reboiler that is linked together, its characterized in that, steam waste heat cascade utilization system includes desuperheating unit, low pressure flash distillation unit and low temperature multiple-effect distillation unit, the reboiler is linked together through the low pressure jar that supplies low pressure supersaturated steam pipeline and steam turbine, the desuperheating unit cools off the low pressure supersaturated steam, the reboiler through supplying the condensate water pipeline with the low pressure flash distillation unit is linked together, the low pressure flash distillation unit through supplying low temperature steam pipeline with low temperature multiple-effect distillation unit is linked together, the condensate water in the low pressure flash distillation unit returns waste heat boiler's steam-water circulation system below 70 ℃.
2. The steam waste heat cascade utilization system for a carbon capture absorbent regeneration system of claim 1, wherein: the temperature reduction unit adjusts the parameters of the low-pressure supersaturated steam to be 0.4MPa of pressure and 140-160 ℃, and is used for cooling a cooling fan of a low-pressure supersaturated steam pipeline or a variable-frequency temperature and pressure reduction device which is arranged on the low-pressure supersaturated steam pipeline and directly reduces the temperature and the pressure of the low-pressure supersaturated steam.
3. The steam waste heat cascade utilization system for a carbon capture absorbent regeneration system of claim 2, wherein: the temperature of the low pressure supersaturated steam was 150 ℃.
4. The steam waste heat cascade utilization system for a carbon capture absorbent regeneration system of claim 2 or 3, wherein: and the parameters of the condensed water generated by the reboiler in the condensed water supply pipeline are 0.4MPa of pressure and 135-145 ℃.
5. The steam waste heat cascade utilization system for a carbon capture absorbent regeneration system of claim 4, wherein: the temperature of the condensed water was 140 ℃.
6. The steam waste heat cascade utilization system for a carbon capture absorbent regeneration system of claim 1, wherein: the low-pressure flash evaporation unit is a flash evaporator, and the temperature of steam supplied by the flash evaporator to the low-temperature multi-effect distillation unit is lower than 70 ℃.
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| CN202010335004.0ACN111420516A (en) | 2020-04-24 | 2020-04-24 | Steam waste heat cascade utilization system for carbon capture absorbent regeneration system |
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Cited By (3)
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| CN114397922A (en)* | 2021-09-29 | 2022-04-26 | 北京百利时能源技术股份有限公司 | Temperature control system of carbon dioxide capture reboiler of coal-fired power plant |
| WO2023035492A1 (en)* | 2021-09-07 | 2023-03-16 | 中国华能集团清洁能源技术研究院有限公司 | Flue gas purification system capable of comprehensively utilizing heat, and process using same |
| CN119819085A (en)* | 2024-12-17 | 2025-04-15 | 华电电力科学研究院有限公司 | Flue gas carbon dioxide capturing and purifying system and operation method |
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| CN119819085A (en)* | 2024-12-17 | 2025-04-15 | 华电电力科学研究院有限公司 | Flue gas carbon dioxide capturing and purifying system and operation method |
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