CN107998689B - Removing CO in the medium-to-variable gas acidic condensate2And O2Heat integrated rectification process - Google Patents
Removing CO in the medium-to-variable gas acidic condensate2And O2Heat integrated rectification process Download PDFInfo
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- CN107998689B CN107998689B CN201711262168.XA CN201711262168A CN107998689B CN 107998689 B CN107998689 B CN 107998689B CN 201711262168 A CN201711262168 A CN 201711262168A CN 107998689 B CN107998689 B CN 107998689B
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- 238000000034 method Methods 0.000 title claims abstract description 79
- 230000002378 acidificating effect Effects 0.000 title claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 145
- 239000007789 gas Substances 0.000 claims abstract description 140
- 230000010354 integration Effects 0.000 claims abstract description 17
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 15
- 239000002737 fuel gas Substances 0.000 claims abstract description 15
- 239000001257 hydrogen Substances 0.000 claims abstract description 15
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 15
- 238000000746 purification Methods 0.000 claims abstract description 6
- 239000002253 acid Substances 0.000 claims abstract description 5
- 238000009833 condensation Methods 0.000 claims description 30
- 230000005494 condensation Effects 0.000 claims description 30
- 239000007791 liquid phase Substances 0.000 claims description 22
- 239000012071 phase Substances 0.000 claims description 19
- 239000008213 purified water Substances 0.000 claims description 16
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 5
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 5
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 239000002918 waste heat Substances 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000005329 float glass Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0068—General arrangements, e.g. flowsheets
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0073—Degasification of liquids by a method not covered by groups B01D19/0005 - B01D19/0042
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention belongs to the technical field of petrochemical hydrogen production devices, and relates to a method for removing CO in acid condensate of medium transformer gas2And O2The heat integration rectification process. The invention removes CO from the medium-temperature gas condensate2and O2Is stripped by steamChanging the process or the self-flashing process into a rectifying process, and carrying out heat integration on the feeding of a heat flow strand and a rectifying tower reboiler; the device used in the process comprises a first middle variable gas condensing tank, a second middle variable gas condensing tank, a third middle variable gas condensing tank, a deaerator, a deaerating water heater, a desalted water preheater, a heat medium water generator, a heat medium water preheater, a circulating water cooler, a fuel gas preheater, a stripping tower, a water purification pump and a stripping tower reboiler. Compared with the prior conventional process, the method has the advantages of CO2And O2The removal is thorough, the boiler feed water standard is achieved, the boiler feed water can be directly mixed with the deoxygenated water without a deoxygenator, and the load of the deoxygenator is reduced; the low-temperature waste heat is fully recovered, the energy consumption of cold and hot public works is saved, and the equipment investment and the operation cost are low.
Description
Technical Field
The invention belongs to the field of petrochemical hydrogen production devices, and relates to a method for removing CO in acid condensate of medium transformer gas2And O2The heat integration rectification process. Specifically, two strands of acid condensate with different temperature levels are generated after the moisture of the medium shift gas is divided, the high-temperature condensate provides a heat source for a reboiler at the bottom of a stripping tower, then the high-temperature condensate and the low-temperature condensate respectively enter the stripping tower, and CO is removed through steam stripping or self-flashing2And O2。
Background
Hydrogen is the main industrial feedstock and is also of paramount importanceIndustrial gases and special gases are generally used as raw materials for ammonia synthesis, methanol synthesis and hydrochloric acid synthesis, reducing agents for metallurgy, hydrogen desulfurization agents in petroleum refining, and the like. The hydrogen has wide application in the fields of petrochemical industry, electronic industry, metallurgical industry, food processing, float glass, fine organic synthesis, aerospace and the like. The main method for industrial hydrogen production is mostly water gas hydrogen production or dry gas hydrogen production, and the patent mainly aims at the medium-temperature conversion section of a dry gas hydrogen production device. In the traditional medium temperature conversion section, condensate generated by medium gas conversion multistage condensation enters a stripping tower, and steam is used for stripping to remove CO2And O2Then enters an oxygen removing groove to further remove O2For generating steam; the CO is removed by flash evaporation directly depending on the heat of condensate without steam stripping in some working sections2And O2. Wherein, the steam stripping efficiency is lower, the energy consumption is larger, and the condensate liquid removes CO by self-flash evaporation2The effect of (A) is not thorough enough, and the corrosion of subsequent equipment, especially a deoxidizing tank, is easy to cause leakage accidents. In addition, the traditional medium temperature conversion section uses a circulating water cooler and an air cooler to cool medium temperature gas, so that large low temperature heat loss is caused, and the energy consumption of cold public works is increased.
Disclosure of Invention
Aiming at the actual conditions, the invention provides a method for efficiently removing the middle-variable gas acidic condensate CO with low energy consumption2And O2The process of (1) removing CO from the medium-to-variable gas condensate2And O2The process of (1) is changed from a steam stripping process or a self-flashing process into a rectifying process, and heat integration is carried out on a hot flow strand feeding and a rectifying tower reboiler. The system comprises a medium-shift gas first-stage condensing tank, a medium-shift gas second-stage condensing tank, a medium-shift gas third-stage condensing tank, a deaerator water heater, a desalted water preheater, a heating medium water generator, a heating medium water preheater, a circulating water cooler, two standby water coolers, a fuel gas preheater, an acid water stripping tower and a purification water pump. The medium gas enters a heat medium water generator and then enters a medium gas first-stage condensation tank. After gas-liquid separation, the gas phase enters a deaerating water heater and then enters a secondary condensing tank of medium-to-variable gas. After gas-liquid separation, the produced liquid phase is produced in the same middle-changed gas first condensation tankMixing raw liquid phases, passing through a fuel gas preheater and a reboiler at the bottom of a stripping tower, and then entering the stripping tower from the middle part; the generated gas phase passes through a heat medium water preheater, a desalted water preheater and a circulating water cooler and then enters a third condensate tank of the medium-to-variable gas, the gas phase after gas-liquid separation enters a pressure swing adsorption part, and the liquid phase enters a stripping tower from the top of the tower. And the preheated desalted water enters a deaerator. Stripping to obtain purified water, CO2The content is reduced to 10ppb, O2The content reaches the deaerated water standard, therefore, the purified water can be directly mixed with the deaerated water to enter a subsequent steam generating device without entering a deaerator, thereby reducing the energy consumption of the deaerator.
In addition, the main function of the coagulation tank is to separate water and dissolve CO in the water2As little as possible. At high temperature segregation, the amount of water condensed is small, and at this time CO2The solubility in water is low, and CO in condensate2The content is low; at low temperature, the amount of water condensed is large, and at this time, CO is condensed2The solubility in water is high, and CO in condensate2The content is higher. The temperatures associated with the first and last tanks are determined by the upstream process and cold utilities, respectively, for efficient separation of condensate and CO2It is necessary to balance the phase equilibrium relationship of water and CO2Determining the operating temperature and the number of the intermediate partial condensation tanks according to the dissolution equilibrium relationship in water, thereby formulating a reasonable heat extraction separation strategy. The specific method is that according to the condensation curve of the medium-temperature gas and CO under the operation pressure2For the change trend of the solubility curve of water, a gel separation tank is respectively arranged at the temperature corresponding to the inflection point of the two curves. Under the working condition, the temperatures corresponding to the inflection points of the two curves are close, so that a partial condensation tank is arranged between the two inflection points in consideration of equipment cost and separation effect, and the total flow of three tanks is most reasonable.
The technical scheme of the invention is as follows:
CO in removing middle-aged gas acidic condensate2And O2The heat integration rectification process removes CO from the medium-to-variable gas condensate2And O2the process of (A) is changed from a steam stripping process or a self-flashing process into a rectifying process and the heat flow is subjected toCarrying out heat integration on the strand feeding material and a rectifying tower reboiler;
The device used in the process comprises a medium-variable gas first condensate tank 1, a medium-variable gas second condensate tank 2, a medium-variable gas third condensate tank 3, a heat medium water generator 4, a deaerating water heater 5, a heat medium water preheater 6, a desalted water preheater 7, a circulating water cooler 8, a fuel gas preheater 9, a stripping tower 10, a deaerator 11, a purified water pump 12 and a stripping tower reboiler 13; the medium transformer gas feeding pipeline is connected with a heat medium water generator 4 tube pass inlet, and a heat medium water generator 4 tube pass outlet is connected with a medium transformer gas first condensation tank 1 inlet; a gas phase outlet of the medium-to-medium gas first separation tank 1 is connected with a tube pass inlet of a deoxygenated water heater 5, and a liquid phase outlet is connected with a tube pass inlet of a fuel gas preheater 9; the tube pass outlet of the deaerated water heater 5 is connected with the medium gas changing second condensing tank 2; a gas phase outlet of the second medium-to-gas condensing tank 2 is connected with a tube pass inlet of a heat medium water preheater 6, and a liquid phase outlet is connected with a tube pass inlet of a fuel gas preheater 9; a pipe pass outlet of the desalted water preheater 7 is connected with a pipe pass inlet of the circulating water cooler 8, and a pipe pass outlet of the circulating water cooler 8 is connected with the middle transformer gas third condensate tank 3; a gas phase outlet of the third partial condensation tank 3 of the medium-modified gas is connected with a pressure swing adsorption working section, and a liquid phase outlet is connected with a feed inlet at the top of the stripping tower 10; a tube pass outlet of the fuel gas preheater 9 is connected with a shell pass inlet of a reboiler 13 of the stripping tower, and a shell pass outlet of the reboiler 13 of the stripping tower is connected with a middle feed inlet of the stripping tower 10; the top of the stripping tower 10 is connected with the atmosphere, the bottom of the stripping tower is connected with the inlet of a purified water pump 12, and the outlet of the purified water pump 12 is connected with the outlet pipeline of a deaerator 11; an outlet of a shell pass of the desalted water preheater 7 is connected with an inlet of a deaerator 11, and an outlet of the deaerator 11 is connected with a subsequent steam generating device;
The specific process comprises the following steps:
The medium-to-medium gas is heated by a heating medium water generator 4 and then enters a medium-to-medium gas first condensation tank 1, and the generated gas phase enters a medium-to-medium gas second condensation tank 2 after passing through a deaerated water heater 5; after liquid phases generated by the first intermediate transformer gas condensate tank 1 and the second intermediate transformer gas condensate tank 2 are collected, the liquid phases are heated by a fuel gas preheater 9 and a stripping tower reboiler 13 and then enter a stripping tower 10 from the middle part; the gas phase generated by the second secondary condensate tank 2 of the medium-to-variable gas is sequentially cooled to 35 ℃ through a heat medium water preheater 6, a desalted water preheater 7 and a circulating water cooler 8, then enters the third secondary condensate tank 3 of the medium-to-variable gas, the gas phase directly enters a subsequent pressure swing adsorption working section, and the liquid phase enters a stripping tower 10 from the top; the desalted water enters a deaerator 11 after being preheated to generate deaerated water; purified water is extracted from the bottom of the stripping tower 10, mixed with deoxygenated water by a purified water pump 12 and then enters a steam generation section;
The technological parameters of the heat medium water generator are as follows: the temperature of the hot medium water is 100 ℃, the increment of the hot medium water is used as a free end, and the heat load of the heat exchanger is controlled by adjusting the hot medium water, so that the temperature of the variable gas in the outlet is controlled to be 155-160 ℃.
The process parameters of the middle variable gas first condensate tank 1 are as follows: the feeding temperature is 155-160 ℃; the operating pressure is 2.32-2.30 MPag.
The process parameters of the middle transformer gas second condensation tank 2 are as follows: the feeding temperature is 145-150 ℃; the operating pressure is 2.30-2.27 MPag.
The technological parameters of the middle variable gas third partial condensation tank 3 are as follows: the feeding temperature is 35-40 ℃; the operating pressure is 2.27-2.25 MPag.
The stripping tower 10 has the following technological parameters: the liquid phase of the middle transformer gas third condensate tank 3 enters from the top of a stripping tower 10, the mixed condensate of the middle transformer gas first condensate tank 1 and the middle transformer gas second condensate tank 2 is heated and then enters from 2 nd to 3 rd theoretical plates of the stripping tower 10, the operating pressure is micro-positive pressure, the temperature at the top of the tower is 45-55 ℃, the temperature at the bottom of the tower is 100-110 ℃, and the number of the theoretical plates is 4-6; the load of the stripping tower reboiler 13 is provided by the mixed condensate of the medium-pressure gas first condensate tank 1 and the medium-pressure gas second condensate tank 2; CO purification of water after steam stripping2The content is 10ppb, O2The content is lower than 15ppb, and the standard of boiler feed water is achieved.
the volume fraction of hydrogen in the medium-grade gas is 40-50%; the volume fraction of the carbon dioxide is 10-15 percent; the volume fraction of the water vapor is 40-45%; the volume fraction of methane is 2-4%; the volume fraction of the carbon monoxide is 1 to 2 percent; the volume fraction of the remaining gas is less than 1%.
The invention has the beneficial effects that: the invention adopts low energy consumption to efficiently remove the middle gas shift acidic condensate CO2And O2The process of (1) removing CO from the medium-to-variable gas condensate2And O2The process of (1) is changed from a steam stripping process or a self-flashing process into a rectifying process, and heat integration is carried out on a hot flow strand feeding and a rectifying tower reboiler. Compared with the prior conventional process, CO2And O2The removal is thorough, the boiler feed water standard is achieved, the boiler feed water can be directly mixed with the deoxygenated water without a deoxygenator, and the load of the deoxygenator is reduced; the low-temperature waste heat is fully recovered, and the energy consumption of cold and hot public works is saved. In addition, the traditional process is technically improved into the process, so that the equipment investment and the operation cost are low.
Drawings
FIG. 1 is a schematic process diagram of a middle gas shift section.
in the figure: 1, a first variable gas condensation tank; 2, a secondary condensing tank for the medium transformer gas; 3, changing gas to a third partial condensation tank; 4, a heating medium water generator; 5 a deaerated water heater; 6, a heating medium water preheater; 7 a desalted water preheater; 8, a circulating water cooler; 9 a fuel gas preheater; 10 stripping tower; 11 a deaerator; 12 purifying the water pump; 13 stripper reboiler.
Detailed Description
The following detailed description of the embodiments of the invention is provided in connection with the accompanying drawings.
The medium transformer gas firstly enters a heat medium water generator 4, the medium transformer gas enters a first condensation tank 1 after heat is taken, and the generated gas phase enters a second condensation tank 2 after passing through a deaerating water heater 5. After the liquid phases generated by the two tanks are converged, the heat is extracted by a fuel gas preheater 9 and a reboiler 13 at the bottom of the stripping tower, and then the liquid phases enter the stripping tower 10 from the middle part. The gas phase generated by the second secondary condensate tank 2 of the medium-to-variable gas is cooled to 35 ℃ through a heat medium water preheater 6, a desalted water preheater 7 and a circulating water cooler 8, then enters the third secondary condensate tank 3 of the medium-to-variable gas, the gas phase directly enters a subsequent pressure swing adsorption working section, and the liquid phase enters a stripping tower 10 from the top. The desalted water enters the deaerator 11 after being preheated, and deaerated water is generated. The purified water is extracted from the bottom of the stripping tower, mixed with the deoxygenated water by the purified water pump 12 and then enters the steam generation section.
Example (b):
25000Nm for a petrochemical company3System of hA hydrogen device, wherein the volume fraction of hydrogen in the medium-grade gas is 44.6 percent; the volume fraction of carbon dioxide is 10.9%; the volume fraction of water vapor is 40.3%; the volume fraction of methane was 2.6%; the volume fraction of carbon monoxide is 1.1%; the volume fraction of the remaining gas was 0.7%. After being separated by the device and the method provided by the invention, CO in the purified water2The content is 10ppb, O2The content is lower than 15ppb, and the standard of boiler feed water is achieved.
Technological parameters of the heat medium water generator are as follows: the temperature of the hot medium water is 100 ℃, the increment of the hot medium water is used as a free end, and the heat load of the heat exchanger is controlled by adjusting the hot medium water, so that the temperature of the variable gas in the outlet is controlled to be 156 ℃.
The process parameters of the first secondary condensing tank of the medium-grade transformer gas are as follows: the feed temperature was 156 ℃; the operating pressure was 2.30 MPag.
the process parameters of the secondary condensate tank of the medium-grade transformer gas are as follows: the feeding temperature is 147.4 ℃; the operating pressure was 2.28 MPag.
the process parameters of the medium-to-variable gas third partial condensation tank are as follows: the feeding temperature is 35 ℃; the operating pressure was 2.25 MPag.
Stripping tower process parameters: the liquid phase of the third middle shift gas condensate tank enters from the top of the stripping tower, the temperature of the mixed condensate of the first middle shift gas condensate tank and the second middle shift gas condensate tank is 154.4 ℃, the temperature is 115 ℃ after heat extraction, the mixed condensate enters from the 3 rd actual plate of the stripping tower, the operating pressure is micro-positive pressure, the temperature at the top of the stripping tower is 49.2 ℃, the temperature at the bottom of the stripping tower is 105 ℃, and the actual number of tower plates is 6; the load of a reboiler at the bottom of the tower is 423kW and is provided by mixed condensate of a first condensate tank and a second condensate tank of the medium pressure gas. CO purification of water after steam stripping2The content is 10ppb, O2The content is lower than 15ppb, and the water reaches the boiler water supply standard, so that the purified water can be directly mixed with the deoxygenated water at the outlet of the deoxygenator without entering the deoxygenator, and the energy consumption of the deoxygenator is reduced.
The invention provides a method for efficiently removing middle-variable gas acidic condensate CO with low energy consumption2And O2The process of (1) removing CO from the medium-to-variable gas condensate2And O2The process of (1) is changed into a rectification process from a steam stripping process and a self-flashing process, and heat integration is carried out on a heat flow strand feeding material and a rectification tower reboiler. Compared with the prior conventional process, CO2And O2The removal is thorough, the boiler feed water standard is achieved, the boiler feed water can be directly mixed with the deoxygenated water without a deoxygenator, and the load of the deoxygenator is reduced; the low-temperature waste heat is fully recovered, and the energy consumption of cold and hot public works is saved. In addition, the traditional process is technically improved into the process, so that the equipment investment and the operation cost are low.
Claims (8)
1. CO in removing middle-aged gas acidic condensate2And O2the heat integration rectification process is characterized in that the medium-to-medium gas condensate is subjected to CO removal2And O2The process of (2) is changed from a steam stripping process or a self-flashing process into a rectifying process, and heat integration is carried out on the feeding of a heat flow strand and a reboiler of a rectifying tower;
The device used in the process comprises a medium-variable gas first condensation tank (1), a medium-variable gas second condensation tank (2), a medium-variable gas third condensation tank (3), a hot medium water generator (4), a deaerating water heater (5), a hot medium water preheater (6), a desalted water preheater (7), a circulating water cooler (8), a fuel gas preheater (9), a stripping tower (10), a deaerator (11), a purified water pump (12) and a stripping tower reboiler (13); the medium variable gas feed pipeline is connected with a tube pass inlet of a heat medium water generator (4), an outlet of a tube pass of the heat medium water generator (4) is connected with an inlet of a first condensate tank (1) of the medium variable gas, and another outlet of the tube pass of the heat medium water generator (4) is connected with a tube pass inlet of a desalted water preheater (6); a gas phase outlet of the medium-to-medium gas first separation tank (1) is connected with a tube pass inlet of the deoxygenated water heater (5), and a liquid phase outlet is connected with a tube pass inlet of the fuel gas preheater (9); the tube pass outlet of the deaerated water heater (5) is connected with the second medium-to-medium gas condensing tank (2); a gas phase outlet of the second medium-to-medium gas condensing tank (2) is connected with a tube pass inlet of the heat medium water preheater (6), and a liquid phase outlet is connected with a tube pass inlet of the fuel gas preheater (9); a tube pass outlet of the desalted water preheater (7) is connected with a tube pass inlet of the circulating water cooler (8), and a tube pass outlet of the circulating water cooler (8) is connected with a middle condensing tank (3); a gas phase outlet of the medium-modified gas third condensate tank (3) is connected with a pressure swing adsorption working section, and a liquid phase outlet is connected with a feed inlet at the top of the stripping tower (10); a tube pass outlet of the fuel gas preheater (9) is connected with a shell pass inlet of a stripping tower reboiler (13), and a shell pass outlet of the stripping tower reboiler (13) is connected with a middle feed inlet of the stripping tower (10); the top of the stripping tower (10) is connected with the atmosphere, the bottom of the stripping tower is connected with the inlet of a purified water pump (12), and the outlet of the purified water pump (12) is connected with the outlet pipeline of a deaerator (11); the shell pass outlet of the desalted water preheater (7) is connected with the inlet of a deaerator (11), and the outlet of the deaerator (11) is connected with a subsequent steam generating device;
The specific process comprises the following steps:
The medium-to-medium gas is heated by a heating medium water generator (4) and then enters a medium-to-medium gas first condensation tank (1), and the generated gas phase enters a medium-to-medium gas second condensation tank (2) after passing through a deaerating water heater (5); after liquid phases generated by the first middle shift gas condensate tank (1) and the second middle shift gas condensate tank (2) are converged, the liquid phases are heated by a fuel gas preheater (9) and a stripping tower reboiler (13) and then enter a stripping tower (10) from the middle part; the gas phase generated by the second condensate tank (2) of the medium-to-variable gas is sequentially cooled to 35 ℃ through a heat medium water preheater (6), a desalted water preheater (7) and a circulating water cooler (8), then enters the third condensate tank (3) of the medium-to-variable gas, the gas phase directly enters a subsequent pressure swing adsorption working section, and the liquid phase enters a stripping tower (10) from the top; the desalted water enters a deaerator (11) after being preheated to generate deaerated water; purified water is extracted from the bottom of the stripping tower (10), mixed with deoxygenated water by a purified water pump (12) and then enters a steam generation section.
2. The method for removing CO from the middle gas shift acidic condensate according to claim 12And O2The heat integration rectification process is characterized in that the process parameters of the heat medium water generator (4) are as follows: the temperature of the hot medium water is 100 ℃, the increment of the hot medium water is used as a free end, and the heat load of the heat exchanger is controlled by adjusting the hot medium water, so that the temperature of the variable gas in the outlet is controlled to be 155-160 ℃.
3. The method for removing CO from the middle gas shift acidic condensate according to claim 1 or 22And O2The heat integration rectification process is characterized in that the process parameters of the medium-variable gas first condensation separation tank (1) are as follows: the feeding temperature is 155-160 ℃; the operating pressure is 2.32-2.30 MPag;
The process parameters of the middle variable gas condensing second condenser (2) are as follows: the feeding temperature is 145-150 ℃; the operating pressure is 2.30-2.27 MPag;
The medium-to-medium gas third partial condensation tank (3) has the following process parameters: the feeding temperature is 35-40 ℃; the operating pressure is 2.27-2.25 MPag.
4. The method for removing CO from the middle gas shift acidic condensate according to claim 1 or 22and O2The heat integration rectification process is characterized in that the stripping tower (10) has the following process parameters: the liquid phase of the medium-to-medium gas change third partial condensation tank (3) enters from the top of a stripping tower (10), the mixed condensate of the medium-to-medium gas change first partial condensation tank (1) and the medium-to-medium gas change second partial condensation tank (2) is heated and then enters from 2 nd to 3 rd theoretical plates of the stripping tower (10), the operating pressure is micro-positive pressure, the temperature at the top of the tower is 45-55 ℃, the temperature at the bottom of the tower is 100-110 ℃, and the number of theoretical plates is 4-6; the load of the stripping tower reboiler (13) is provided by the mixed condensate of the medium-variable gas first condensate tank (1) and the medium-variable gas second condensate tank (2); CO purification of water after steam stripping2The content is 10ppb, O2The content is lower than 15ppb, and the standard of boiler feed water is achieved.
5. The method for removing CO from the middle gas shift acidic condensate according to claim 32And O2The heat integration rectification process is characterized in that the stripping tower (10) has the following process parameters: the liquid phase of the medium-to-medium gas change third partial condensation tank (3) enters from the top of a stripping tower (10), the mixed condensate of the medium-to-medium gas change first partial condensation tank (1) and the medium-to-medium gas change second partial condensation tank (2) is heated and then enters from 2 nd to 3 rd theoretical plates of the stripping tower (10), the operating pressure is micro-positive pressure, the temperature at the top of the tower is 45-55 ℃, the temperature at the bottom of the tower is 100-110 ℃, and the number of theoretical plates is 4-6; the load of the stripping tower reboiler (13) is provided by the mixed condensate of the medium-variable gas first condensate tank (1) and the medium-variable gas second condensate tank (2); CO purification of water after steam stripping2The content is 10ppb, O2The content is lower than 15ppb, and the standard of boiler feed water is achieved.
6. A method according to claim 1, 2 or 5 for removing CO from a medium gas shift acid condensate2And O2The heat integration rectification process is characterized in that hydrogen in the medium-pressure gasThe volume fraction of (A) is 40-50%; the volume fraction of the carbon dioxide is 10-15 percent; the volume fraction of the water vapor is 40-45%; the volume fraction of methane is 2-4%; the volume fraction of the carbon monoxide is 1 to 2 percent; the volume fraction of the remaining gas is less than 1%.
7. The method for removing CO from the middle gas shift acidic condensate according to claim 32And O2the heat integration rectification process is characterized in that the volume fraction of hydrogen in the medium-pressure shift gas is 40-50%; the volume fraction of the carbon dioxide is 10-15 percent; the volume fraction of the water vapor is 40-45%; the volume fraction of methane is 2-4%; the volume fraction of the carbon monoxide is 1 to 2 percent; the volume fraction of the remaining gas is less than 1%.
8. The method for removing CO from the middle gas shift acidic condensate according to claim 42And O2The heat integration rectification process is characterized in that the volume fraction of hydrogen in the medium-pressure shift gas is 40-50%; the volume fraction of the carbon dioxide is 10-15 percent; the volume fraction of the water vapor is 40-45%; the volume fraction of methane is 2-4%; the volume fraction of the carbon monoxide is 1 to 2 percent; the volume fraction of the remaining gas is less than 1%.
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