CN112708478A - Low water-gas ratio CO conversion device and method - Google Patents
Low water-gas ratio CO conversion device and method Download PDFInfo
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- CN112708478A CN112708478A CN202011320337.2A CN202011320337A CN112708478A CN 112708478 A CN112708478 A CN 112708478A CN 202011320337 A CN202011320337 A CN 202011320337A CN 112708478 A CN112708478 A CN 112708478A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
- C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
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- 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention belongs to the technical field of CO conversion processes of coal chemical devices, and relates to a low water-gas ratio CO conversion device and a low water-gas ratio CO conversion method. Aiming at the high CO crude synthesis gas from a coal gasification device, a flow splitting mode is adopted to reasonably split the crude coal gas into two streams, and the water-gas ratio of one stream is reduced, so that the reaction depth and the bed hot spot temperature of a No. 1 shift converter are controlled, and the over-temperature phenomenon of a reactor is avoided. And the CO concentration is greatly reduced after the other strand of the mixed gas is mixed with the gas from the shift converter 1, so that the possibility of methanation reaction of the shift converter 2 is greatly reduced. The process flow has the characteristics of strong upstream device operation wave resistance, good system energy integration effect, obvious energy saving and consumption reduction and the like.
Description
Technical Field
The invention belongs to the technical field of CO conversion processes of coal chemical devices, and relates to a low water-gas ratio CO conversion device and a low water-gas ratio CO conversion method.
Background
In the coal gasification configuration device, the carbon monoxide conversion device adjusts the hydrogen-carbon ratio of the crude gas produced by the gasification device through conversion reaction to meet the requirements of downstream products. The composition of the crude gas produced by various gasification processes has a large difference, and even aiming at the same downstream product, the conversion process technology matched with different gasification processes is different. The selection of the CO conversion process not only needs to adapt to the composition of the raw gas and meet the requirements of products, but also needs to consider the problems of safety, energy conservation and the like.
In the coal gasification process, the chilling type process is more and more concerned, and mainly comprises a GSP pulverized coal gasification process introduced abroad, a domestic independently developed 'space furnace', an SE oriental furnace powder coal gasification process and the like. Chilling type pulverized coal gasification and waste heat boiler type pulverized coal gasification (a typical process is Shell pulverized coal gasification) both generate crude synthesis gas with high-concentration CO, the water-gas ratio of the chilling type pulverized coal gasification is 0.7-1.0, the water-gas ratio of the waste heat boiler type pulverized coal gasification is about 0.2, the conversion operating pressure of the pulverized coal gasification is about 3.8MPa, the dry basis of CO of the crude coal gas is very high and reaches more than 60%, and some coal gas even reaches 70%, the driving force of the conversion reaction is large, the carbon monoxide conversion reaction belongs to a strong exothermic reaction and is a thermodynamic control process, and the hot point temperature of the reaction reaches more than 450 ℃. The reaction is very violent, and the overtemperature of the shift converter is easily caused.
At present, the carbon monoxide shift reaction in industrial production mostly adopts a multi-stage adiabatic reactor series process, thereby meeting the requirement of the conversion rate of carbon monoxide in process gas. Traditionally, a high water-to-gas ratio CO shift process is used, which completes the shift reaction by supplementing excess steam to the high water-to-gas ratio in the raw gas. The main problem of this technique is that part or all of the gas is first passed through the first reactor, and a large amount of steam is added to the population of the first reactor, usually to make the water-gas ratio reach more than 1.4: because the water-gas ratio and the CO content are high, the driving force of the reaction is large, and the reaction depth is difficult to control. In actual operation, in the initial stage of catalyst use, nitrogen dilution or water-gas ratio increase or partial catalyst removal method is sometimes used to reduce the temperature, which affects the service life of the catalyst; meanwhile, the steam consumption of the conversion section is high, the heat recovery system of the conversion gas is finally realized by arranging a plurality of heat exchangers, heating desalted water, cooling circulating water and the like, the amount of the condensate of the conversion gas is large, the load and the difficulty of downstream sewage treatment are greatly increased, and the device has high energy consumption and large investment.
Disclosure of Invention
The invention aims to provide a low water-gas ratio CO conversion process and a low water-gas ratio CO conversion device aiming at the defects in the prior art, and the whole process flow has the characteristics of good energy integration effect, obvious energy saving and consumption reduction and the like.
The purpose of the invention can be realized by the following technical scheme:
a low water-gas ratio CO conversion device comprises a low-pressure steam generator, a 1# detoxification tank, a 1# conversion furnace, a 2# detoxification tank, a 1# conversion furnace and a hydrolysis reactor; an output pipeline of the crude synthesis gas is connected with a No. 1 gas-liquid separator, and the output end of the crude synthesis gas at the top of the No. 1 gas-liquid separator is divided into two material flows;
the first material flow sequentially passes through a steam generator and a No. 2 gas-liquid separator through a pipeline, the output end of the top of the No. 2 gas-liquid separator sequentially enters a No. 1 detoxification tank, a No. 1 shift converter, a raw material gas heater and a No. 1 high-pressure steam generator after passing through a raw material gas heater, and the output end of the No. 1 high-pressure steam generator is connected with a No. 1 high-pressure boiler water supply preheater;
the second stream is connected with the output end of a 1# high-pressure boiler feed water preheater through a feed gas heater and a 2# detoxification groove and then enters a 2# conversion furnace; the output end of the 2# shift converter sequentially passes through a 1# high-pressure steam superheater, a 2# high-pressure steam generator and a 2# high-pressure boiler feed water preheater and then enters a hydrolysis reactor, and the output end of the hydrolysis reactor is sequentially connected with a desalted water heater and a 3# gas-liquid separator;
and the output end at the top of the No. 3 gas-liquid separator enters a No. 4 gas-liquid separator after passing through a gas-water changing cooler, and the output end at the top of the No. 4 gas-liquid separator is sent to an outside acid gas separating unit.
In the above apparatus: and a pipeline is led out from the input end of the 2# conversion furnace to be used as a regulating bypass and is connected with the output end of the 2# high-pressure steam generator.
In the above apparatus: the feed water from the high-pressure boiler from the outside is divided into two parts after passing through the No. 1 high-pressure boiler feed water preheater and the No. 2 high-pressure boiler feed water preheater, one part is sent to the No. 1 high-pressure steam generator, and the other part is sent to the No. 2 high-pressure steam generator.
In the above apparatus: high-pressure saturated steam by-products of the No. 1 high-pressure steam generator and the No. 2 high-pressure steam generator is superheated by the No. 1 high-pressure steam superheater and then is sent out; high-pressure saturated steam from the outside is superheated by a No. 2 high-pressure steam superheater and then is sent to the outside; and the feed water from the high-pressure boiler from the outside enters a No. 4 gas-liquid separator after passing through a feed water cooler of the high-pressure boiler.
In the above apparatus: and a start-up steam heater is arranged on an input end pipeline of the No. 1 detoxification tank.
A method for implementing a low water-to-gas ratio CO shift using the apparatus described above, the method comprising the steps of:
1) the method comprises the steps that after entering a No. 1 gas-liquid separator, a crude synthesis gas is separated into two material flows, a flow regulating valve is arranged on a first material flow pipeline and used for controlling the flow distribution proportion of the first material flow and the second material flow, the first material flow passes through a steam generator, the temperature of the crude synthesis gas is reduced and then enters a No. 2 gas-liquid separator for gas-liquid separation, a top gas phase is heated by a raw gas heater and then enters a No. 1 shift converter through a No. 1 detoxification groove to generate a carbon monoxide shift reaction, a shifted gas at an outlet of the No. 1 shift converter is cooled by the raw gas heater and then enters a No. 1 high pressure steam generator to generate a high-pressure saturated steam as a byproduct, and the shifted gas at the outlet is further cooled;
2) after the temperature of the second stream is raised by a raw material gas heater, the second stream is mixed with the conversion gas from the outlet of the 1# high-pressure boiler feed water preheater through a 2# detoxification tank and then enters a 2# conversion furnace to continue to carry out carbon monoxide conversion reaction;
3) step 2) after carbon monoxide shift reaction occurs in the No. 2 shift converter, the shift gas temperature is raised, and then the shift gas enters a No. 1 high-pressure steam superheater, a No. 2 high-pressure steam generator and a No. 2 high-pressure boiler feed water preheater in sequence and then enters a hydrolysis reactor to remove organic sulfur;
4) and 3) the transformed gas after organic sulfur removal firstly passes through a desalted water heater, a 3# gas-liquid separator and a transformed gas water cooler and then enters a 4# gas-liquid separator, and the gas coming out of the top of the 4# gas-liquid separator is sent to a downstream acid gas removal unit.
The method comprises the following steps: and cooling and separating the crude synthesis gas by a low-pressure steam generator, and controlling the water-gas ratio of the crude synthesis gas entering the 1# shift converter to be 0.2-0.3.
The method comprises the following steps: the first stream of material flow pipeline is provided with a flow regulating valve which is used for controlling the flow distribution proportion of the first stream of material flow to the second stream of material flow to be 6: 4-4: 6.
The method comprises the following steps: the inlet temperature of the 1# shift converter is controlled to be 200-260 ℃, the outlet temperature of the 1# shift converter is controlled to be 390-435 ℃, the outlet temperature of the 2# shift converter is controlled to be 400-440 ℃, and the inlet temperature of the hydrolysis reactor is controlled to be 165-185 ℃.
The technical scheme of the invention is as follows: the reaction furnace is an axial or axial radial reactor and adopts an adiabatic fixed bed structure.
The technical scheme of the invention is as follows: the internal part of the No. 1 gas-liquid separator (1) adopts a vane type or centrifugal tube bundle type high-efficiency separation structure or a wire mesh demister structure and improved forms thereof.
The invention has the beneficial effects that:
a low water-gas ratio CO shift process and apparatus are provided. The main advantages are as follows: firstly, the raw gas is reasonably divided into two streams, the water-gas ratio of one stream is reduced, low-pressure steam is produced as a byproduct, the loads of subsequent system equipment and pipelines are reduced, and the investment is reduced; secondly, feeding the raw synthesis gas into the shift converter in different strands, and controlling the reaction depth and the hot spot temperature of a bed layer by controlling the water-gas ratio of the raw synthesis gas at the inlet of the 1# shift converter, so that the overtemperature phenomenon of the 1# shift converter is avoided; and thirdly, the concentration of CO in the mixed gas entering the 2# shift converter is greatly reduced, and the possibility of methanation reaction of the 2# shift converter is greatly reduced. And fourthly, a mode of feeding the gas into the converter in different strands is adopted, the gas quantity is flexibly and conveniently adjusted, and the influence of the change of the upstream gas quantity and the fluctuation of the CO content on the operation of the shift converter is small.
Drawings
FIG. 1 is a schematic process flow diagram of the present invention.
In the figure: the system comprises a 1-1# gas-liquid separator, a 2-low pressure steam generator, a 3-2# gas-liquid separator, a 4-raw gas heater, a 5-1# detoxification tank, a 6-1# shift converter, a 7-1# high pressure steam generator, an 8-1# high pressure boiler feed water preheater, a 9-2# detoxification tank, a 10-2# shift converter, an 11-1# high pressure steam superheater, a 12-2# high pressure steam superheater, a 13-2# high pressure steam generator, a 14-2# high pressure boiler feed water preheater, a 15-hydrolysis reactor, a 16-desalted water heater, a 17-3# gas-liquid separator, an 18-shift gas water cooler, a 19-4# gas-liquid separator, a 20-high pressure boiler feed water cooler and a 21-start-up steam heater.
Detailed Description
The invention is further illustrated by the following examples, without limiting the scope of the invention:
a low water-gas ratio CO conversion device comprises a low-pressure steam generator 2, a 1# detoxification tank 5, a 1# conversion furnace 6, a 2# detoxification tank 9, a 1# conversion furnace 10 and a hydrolysis reactor 15; an output pipeline of the crude synthesis gas is connected with a No. 1 gas-liquid separator 1, and the output end of the crude synthesis gas at the top of the No. 1 gas-liquid separator 1 is divided into two material flows;
the first material flow sequentially passes through a steam generator 2 and a No. 2 gas-liquid separator 3 through a pipeline, the output end of the top of the No. 2 gas-liquid separator 3 sequentially enters a No. 1 detoxification tank 5, a No. 1 shift converter 6, a raw material gas heater 4 and a No. 1 high-pressure steam generator 7 after passing through a raw material gas heater 4, and the output end of the No. 1 high-pressure steam generator 7 is connected with a No. 1 high-pressure boiler feed water preheater 8;
the second stream is connected with the output end of a feed water preheater 8 of a 1# high-pressure boiler through a feed gas heater 4 and a 2# detoxification tank 5 and then enters a 2# shift converter 10; the output end of the No. 2 shift converter 10 sequentially passes through a No. 1 high-pressure steam superheater 11, a No. 2 high-pressure steam superheater 12, a No. 2 high-pressure steam generator 13 and a No. 2 high-pressure boiler feed water preheater 14 and then enters a hydrolysis reactor 15, and the output end of the hydrolysis reactor 15 is sequentially connected with a desalted water heater 16 and a No. 3 gas-liquid separator 17;
and the output end of the top of the 3# gas-liquid separator 17 enters a 4# gas-liquid separator 19 after passing through a gas-water changing cooler 18, and the output end of the top of the 4# gas-liquid separator 19 is sent to an outside acid gas removing unit.
And a pipeline is led out from the input end of the 2# conversion furnace 10 to be used as a regulating bypass and is connected with the output end of the 2# high-pressure steam generator 13.
The high-pressure boiler feed water from the outside is divided into two parts after passing through a No. 1 high-pressure boiler feed water preheater 8 and a No. 2 high-pressure boiler feed water preheater 14, one part is sent to a No. 1 high-pressure steam generator 7, and the other part is sent to a No. 2 high-pressure steam generator 13.
High-pressure saturated steam by-produced by the 1# high-pressure steam generator 7 and the 2# high-pressure steam generator 13 is superheated by the 1# high-pressure steam superheater 11 and then is sent out; high-pressure saturated steam from the outside is superheated by the No. 2 high-pressure steam superheater 12 and then sent to the outside; the high-pressure boiler feed water from outside enters the 4# gas-liquid separator 19 after passing through the high-pressure boiler feed water cooler 20.
And a start-up steam heater 21 is arranged on an input end pipeline of the No. 1 detoxification tank 5.
Example 1
484880kg/h of crude synthesis gas (206 ℃, 3.84MPa and the water-gas ratio of 0.91) from an upstream coal gasification device enters a No. 1 gas-liquid separator for gas-liquid separation and is divided into two material flows, a first material flow pipeline is provided with a flow regulating valve for controlling the flow distribution ratio of a first material flow and a second material flow to be 6:4, the first material flow (the flow is 290928kg/h) passes through a steam generator, a byproduct of 92503kg/h of low-pressure saturated steam (165 ℃, 0.5MPa) is obtained, the water-gas ratio of the crude synthesis gas is reduced to 0.24 and then enters a No. 2 gas-liquid separator for gas-liquid separation, the top gas phase passes through a raw material gas heater to be heated to 200 ℃, passes through a No. 1 detoxification groove and then enters a No. 1 shift converter for carbon monoxide shift reaction, the inlet temperature of the No. 1 shift converter is 200 ℃, the outlet temperature of the No. 1 shift converter is 405 ℃, the cooled gas is cooled to 353 ℃, enters a # 1 high-pressure steam generator to produce 17632kg/h high-pressure saturated steam as a byproduct, the outlet conversion gas is cooled to 250 ℃, and enters a # 1 high-pressure boiler feed water preheater to be further cooled to 195 ℃; the second stream (with the flow rate of 193952kg/h) is heated to 210 ℃ by a feed gas heater, then enters a 2# shift converter after being mixed with the shift gas from the outlet of a 1# high-pressure boiler feed water preheater through a 2# detoxification tank to continue the carbon monoxide shift reaction, the temperature of the shift gas is raised to 400 ℃, and then enters a 1# high-pressure steam superheater, a 2# high-pressure steam generator and a 2# high-pressure boiler feed water preheater in sequence, and then enters a hydrolysis reactor at the temperature of 180 ℃ to remove organic sulfur; the conversion gas after organic sulfur removal enters a desalted water heater, a 3# gas-liquid separator and a conversion gas water cooler, the temperature is reduced to 40 ℃, and then the conversion gas enters a 4# gas-liquid separator, and the conversion gas (the flow is 372042kg/h, the temperature is 40 ℃) is sent to a downstream acid gas removal unit.
Example 2
484880kg/h of crude synthesis gas (206 ℃, 3.84MPa and the water-gas ratio of 0.91) from an upstream coal gasification device enters a No. 1 gas-liquid separator for gas-liquid separation and is divided into two material flows, a first material flow pipeline is provided with a flow regulating valve for controlling the flow distribution ratio of a first material flow and a second material flow to be 5:5, the first material flow (the flow is 242440kg/h) passes through a steam generator, a byproduct of 82146kg/h of low-pressure saturated steam (165 ℃, 0.5MPa) is obtained, the water-gas ratio of the crude synthesis gas is reduced to 0.2 and then enters a No. 2 gas-liquid separator for gas-liquid separation, the top gas phase passes through a raw material gas heater to be heated to 225 ℃, passes through a No. 1 detoxification groove and then enters a No. 1 shift converter for carbon monoxide shift reaction, the inlet temperature of the No. 1 shift converter is 225 ℃, the outlet temperature of the No. 1 shift converter is 390 ℃, the cooled gas is cooled to 274 ℃, enters a No. 1 high-pressure steam generator to produce 10535kg/h high-pressure saturated steam as a byproduct, the outlet conversion gas is cooled to 221 ℃, and enters a No. 1 high-pressure boiler feed water preheater to be further cooled to 195 ℃; the second stream (with the flow rate of 242440kg/h) is heated to 240 ℃ by a feed gas heater, then enters a 2# shift converter after being mixed with the shift gas from the outlet of a 1# high-pressure boiler feed water preheater through a 2# detoxification tank, continues to perform carbon monoxide shift reaction, and enters a hydrolysis reactor at the temperature of 165 ℃ to remove organic sulfur after the temperature of the shift gas is raised to 430 ℃ and then sequentially enters a 1# high-pressure steam superheater, a 2# high-pressure steam generator and a 2# high-pressure boiler feed water preheater; the conversion gas after organic sulfur removal enters a desalted water heater, a 3# gas-liquid separator and a conversion gas water cooler, the temperature is reduced to 40 ℃, and then the conversion gas enters a 4# gas-liquid separator, and the conversion gas (the flow is 372434kg/h, the temperature is 40 ℃) is sent to a downstream acid gas removal unit.
Example 3
484880kg/h of crude synthesis gas (206 ℃, 3.84MPa and the water-gas ratio of 0.91) from an upstream coal gasification device enters a No. 1 gas-liquid separator for gas-liquid separation and is divided into two material flows, a first material flow pipeline is provided with a flow regulating valve for controlling the flow distribution ratio of a first material flow and a second material flow to be 4:6, the first material flow (the flow is 193952kg/h) passes through a steam generator and then produces 55218kg/h of low-pressure saturated steam (165 ℃, 0.5MPa), the water-gas ratio of the crude synthesis gas is reduced to 0.3 and then enters a No. 2 gas-liquid separator for gas-liquid separation, the top gas phase passes through a raw gas heater to be heated to 260 ℃, passes through a No. 1 detoxification groove and then enters a No. 1 shift converter for carbon monoxide shift reaction, the inlet temperature of the No. 1 shift converter is 260 ℃, the outlet temperature of the No. 1 shift converter is 435 ℃, and passes through a raw, the cooled gas is cooled to 300 ℃, enters a 1# high-pressure steam generator to produce 5978kg/h high-pressure saturated steam as a byproduct, the outlet conversion gas is cooled to 245 ℃, and enters a 1# high-pressure boiler feed water preheater to be further cooled to 210 ℃; the second stream (with the flow rate of 290928kg/h) is heated to 235 ℃ by a feed gas heater, is mixed with the conversion gas from the outlet of a feed water preheater of a 1# high-pressure boiler through a 2# detoxification tank, enters a 2# conversion furnace for continuous carbon monoxide conversion reaction, the temperature of the conversion gas is raised to 440 ℃, then enters a 1# high-pressure steam superheater, a 2# high-pressure steam generator and a 2# high-pressure boiler feed water preheater in sequence, and enters a hydrolysis reactor at the temperature of 185 ℃ for removing organic sulfur; the conversion gas after organic sulfur removal enters a desalted water heater, a 3# gas-liquid separator and a conversion gas water cooler, the temperature is reduced to 40 ℃, and then the conversion gas enters a 4# gas-liquid separator, and the conversion gas (the flow is 381049kg/h, the temperature is 40 ℃) is sent to a downstream acid gas removal unit.
The foregoing embodiments and description have been made only for the purpose of illustrating the principles of the present invention and are not to be construed as limiting the scope of the invention, since various changes and modifications may be made therein without departing from the spirit and scope of the invention as defined by the appended claims. The parts not involved in the present invention are the same as or can be implemented using the prior art.
Claims (9)
1. A low water-gas ratio CO conversion device is characterized in that: the device comprises a low-pressure steam generator (2), a 1# detoxification tank (5), a 1# conversion furnace (6), a 2# detoxification tank (9), a 1# conversion furnace (10) and a hydrolysis reactor (15); an output pipeline of the crude synthesis gas is connected with a No. 1 gas-liquid separator (1), and the output end of the crude synthesis gas at the top of the No. 1 gas-liquid separator (1) is divided into two material flows;
the first material flow sequentially passes through a steam generator (2) and a No. 2 gas-liquid separator (3) through a pipeline, the output end of the top of the No. 2 gas-liquid separator (3) sequentially enters a No. 1 detoxification tank (5), a No. 1 shift converter (6), a raw material gas heater (4) and a No. 1 high-pressure steam generator (7) after passing through a raw material gas heater (4), and the output end of the No. 1 high-pressure steam generator (7) is connected with a No. 1 high-pressure boiler feed water preheater (8);
the second stream is connected with the output end of a 1# high-pressure boiler feed water preheater (8) through a feed gas heater (4) and a 2# detoxification groove (5) and then enters a 2# shift converter (10); the output end of a No. 2 shift converter (10) sequentially passes through a No. 1 high-pressure steam superheater (11), a No. 2 high-pressure steam superheater (12), a No. 2 high-pressure steam generator (13) and a No. 2 high-pressure boiler feed water preheater (14) and then enters a hydrolysis reactor (15), and the output end of the hydrolysis reactor (15) is sequentially connected with a desalted water heater (16) and a No. 3 gas-liquid separator (17);
and the output end at the top of the 3# gas-liquid separator (17) enters a 4# gas-liquid separator (19) after passing through a gas-water cooler (18), and the output end at the top of the 4# gas-liquid separator (19) is sent to an outside acid gas removal unit.
2. The low water gas ratio CO shift plant of claim 1, wherein: and a pipeline is led out from the input end of the 2# shift converter (10) to be used as a regulating bypass and is connected with the output end of the 2# high-pressure steam generator (13).
3. The low water gas ratio CO shift plant of claim 1, wherein: the high-pressure boiler feed water from the outside is divided into two parts after passing through a No. 1 high-pressure boiler feed water preheater (8) and a No. 2 high-pressure boiler feed water preheater (14), one part is sent to a No. 1 high-pressure steam generator (7), and the other part is sent to a No. 2 high-pressure steam generator (13).
4. The low water gas ratio CO shift plant of claim 1, wherein: high-pressure saturated steam by-produced by the 1# high-pressure steam generator (7) and the 2# high-pressure steam generator (13) is superheated by the 1# high-pressure steam superheater (11) and then is sent out of the air; high-pressure saturated steam from the outside is superheated by a No. 2 high-pressure steam superheater (12) and then sent to the outside; the feed water from the high-pressure boiler from the outside enters a No. 4 gas-liquid separator (19) after passing through a feed water cooler (20) of the high-pressure boiler.
5. The low water gas ratio CO shift plant of claim 1, wherein: and a start-up steam heater (21) is arranged on an input end pipeline of the No. 1 detoxification groove (5).
6. A method of performing a low water-gas ratio CO shift using the apparatus of claim 1, wherein: the method comprises the following steps:
1) the method comprises the steps that after entering a No. 1 gas-liquid separator, a crude synthesis gas is separated into two material flows, a flow regulating valve is arranged on a first material flow pipeline and used for controlling the flow distribution proportion of the first material flow and the second material flow, the first material flow passes through a steam generator, the temperature of the crude synthesis gas is reduced and then enters a No. 2 gas-liquid separator for gas-liquid separation, a top gas phase is heated by a raw gas heater and then enters a No. 1 shift converter through a No. 1 detoxification groove to generate a carbon monoxide shift reaction, a shifted gas at an outlet of the No. 1 shift converter is cooled by the raw gas heater and then enters a No. 1 high pressure steam generator to generate a high-pressure saturated steam as a byproduct, and the shifted gas at the outlet is further cooled;
2) after the temperature of the second stream is raised by a raw material gas heater, the second stream is mixed with the conversion gas from the outlet of the 1# high-pressure boiler feed water preheater through a 2# detoxification tank and then enters a 2# conversion furnace to continue to carry out carbon monoxide conversion reaction;
3) step 2) after carbon monoxide shift reaction occurs in the No. 2 shift converter, the shift gas temperature is raised, and then the shift gas enters a No. 1 high-pressure steam superheater, a No. 2 high-pressure steam generator and a No. 2 high-pressure boiler feed water preheater in sequence and then enters a hydrolysis reactor to remove organic sulfur;
4) and 3) the transformed gas after organic sulfur removal firstly passes through a desalted water heater, a 3# gas-liquid separator and a transformed gas water cooler and then enters a 4# gas-liquid separator, and the gas coming out of the top of the 4# gas-liquid separator is sent to a downstream acid gas removal unit.
7. The method of claim 6, wherein: and cooling and separating the crude synthesis gas by a low-pressure steam generator, and controlling the water-gas ratio of the crude synthesis gas entering the 1# shift converter to be 0.2-0.3.
8. The method of claim 6, wherein: the first stream of material flow pipeline is provided with a flow regulating valve which is used for controlling the flow distribution proportion of the first stream of material flow to the second stream of material flow to be 6: 4-4: 6.
9. The method of claim 6, wherein: the inlet temperature of the 1# shift converter is controlled to be 200-260 ℃, the outlet temperature of the 1# shift converter is controlled to be 390-435 ℃, the outlet temperature of the 2# shift converter is controlled to be 400-440 ℃, and the inlet temperature of the hydrolysis reactor is controlled to be 165-185 ℃.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113460962A (en) * | 2021-07-06 | 2021-10-01 | 中石化宁波工程有限公司 | Long-period transformation process for adjusting water-gas ratio by one-step method for oxo synthesis |
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