Coal-to-liquid purification semi-physical simulation device

Abstract

The utility model belongs to the field of process skill training and examination, and particularly relates to a coal-to-liquid purification semi-physical simulation device. Comprising a simulation transformation section, a simulation low-temperature methanol washing section and a simulation material; the simulation conversion section comprises a raw material gas separator, a conversion gas quenching device, a gas-gas heat exchanger, a protection bed, a first conversion furnace, a second conversion furnace, a low-pressure steam waste boiler, a boiler feed water preheater, a desalted water preheater, a conversion gas water cooler and a conversion gas separator; the simulated low-temperature methanol washing section comprises a raw material gas synthesis gas heat exchanger, a shift gas / tail gas heat exchanger, a raw material gas chiller, a raw material gas deep freezer, an ammonia washing tower, an absorption tower, a carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler, a carbon dioxide rich methanol intercooler, a hydrogen sulfide rich methanol cooler and the like; the typical coal-to-liquid purification process flow in industrial practice can be well reflected, so that students can know the typical process flow, the production principle, the structure and the application performance of main equipment and the like of the transformation and low-temperature methanol washing process.

Description

Technical Field

[0001] The utility model belongs to the field of process skill training and assessment, and specifically relates to a semi-physical simulation device for coal-to-oil purification. Background Art

[0002] The conversion reaction is to produce hydrogen and carbon dioxide by the conversion reaction of carbon monoxide and water vapor under certain pressure and temperature conditions and under the action of catalyst. According to different catalysts and process conditions, the carbon monoxide content in coal gas can be reduced to 2-4% or 0.2-0.4%. Low-temperature methanol washing is to use methanol to remove acidic gases from raw gas. This technology of low-temperature methanol washing has been widely used.

[0003] The conversion and low-temperature methanol washing process requires schools, training centers and enterprises to conduct practical training assessments and skill practical assessment ratings for operators. However, there is currently a lack of effective training and assessment physical devices, and there is an urgent need for physical devices that integrate training and assessment.

[0004] In the existing training and assessment of the conversion and low-temperature methanol washing process, people adopt a pure simulation form, without any materials, and use only simulated instruments and valves. In addition, the process flow and control logic scheme are incomplete and overly simplified. The training focuses on theoretical training, has a single function, and the training content is empty. There is a lack of control over safety accidents. The appearance and installation form of the equipment, the types and styles of instruments, the DCS control system, etc. are very different from those of industrial production. They have little practical guidance significance for industrial production site operations and cannot effectively improve the pulverized coal gasification process skills of school students and practitioners. Utility Model Content

[0005] An object of the present invention is to solve at least the above problems and to provide at least the advantages which will be described below.

[0006] The utility model provides the following technical solutions: a semi-physical simulation device for coal-to-liquid purification, comprising a simulated conversion section, a simulated low-temperature methanol washing section and simulated materials, wherein the simulated materials flow in the simulated conversion section and the simulated low-temperature methanol washing section;

[0007] The simulated conversion section includes a raw gas separator, a conversion gas quencher, a gas-to-gas heat exchanger, a guard bed, a first conversion furnace, a second conversion furnace, a low-pressure steam waste boiler, a boiler feed water preheater, a desalted water preheater, a conversion gas water cooler, and a conversion gas separator;

[0008] The tube-side inlet of the gas-gas heat exchanger is connected to the raw gas separator through a pipeline, the tube-side outlet of the gas-gas heat exchanger is connected to the top inlet of the protection bed through a pipeline, the shell-side inlet of the gas-gas heat exchanger is connected to the bottom outlet of the first conversion furnace through a pipeline, and the shell-side outlet of the gas-gas heat exchanger is connected to the top inlet of the conversion gas quench cooler through a pipeline; the top inlet of the first conversion furnace is connected to the bottom outlet of the protection bed through a pipeline; the conversion gas quench cooler, the second conversion furnace, the low-pressure steam waste boiler, the boiler feed water preheater, the desalted water preheater, the conversion gas water cooler, and the conversion gas separator are connected in sequence through pipelines; the outlet of the conversion gas separator is connected to the simulated low-temperature methanol washing section through a pipeline;

[0009] The simulated low-temperature methanol washing section includes the raw gas synthesis gas heat exchanger, the shift gas / tail gas heat exchanger, the raw gas quencher, the raw gas deep cooler, the ammonia washing tower, the absorption tower, the carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler, the carbon dioxide rich methanol intercooler, the hydrogen sulfide rich methanol cooler, the hydrogen sulfide absorption feed cooler, the synthesis gas heater, and the fine desulfurization tower;

[0010] The pipeline from the shift gas separator is divided into two branches. The first branch is connected to the raw gas synthesis gas heat exchanger and the raw gas quencher in sequence, and the second branch is connected to the shift gas / tail gas heat exchanger. The first branch and the second branch merge at the entrance of the ammonia scrubbing tower; the ammonia scrubbing tower, the raw gas deep cooler, and the absorption tower are connected in sequence through pipelines;

[0011] The absorption tower is divided into a pre-wash section, an H2S washing section, a CO2 cooling section and a CO2 absorption section; the pre-wash section is connected to the hydrogen sulfide absorption feed cooler through pipelines; the H2S washing section is connected to the hydrogen sulfide rich methanol cooler and the hydrogen sulfide absorption feed cooler through pipelines respectively; the CO2 cooling section is connected to the hydrogen sulfide absorption feed cooler and the carbon dioxide rich methanol intercooler through pipelines; the CO2 absorption section is connected to the carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler through pipelines;

[0012] The synthesis gas heater is connected to the raw gas synthesis gas heat exchanger through a pipeline; the fine desulfurization tower is connected to the synthesis gas heater through a pipeline.

[0013] Furthermore, a flow meter is provided on the pipeline connecting the raw gas synthesis gas heat exchanger to the synthesis gas heater; and a flow meter is provided on the pipeline connecting the hydrogen sulfide absorption feed cooler to the absorption tower.

[0014] Furthermore, pressure sensors are provided on the outlet pipeline of the conversion gas separator, on the pipeline connecting the ammonia washing tower to the raw gas cryogenic cooler, on the top outlet pipeline of the absorption tower and on the bottom outlet pipeline of the fine desulfurization tower.

[0015] Furthermore, liquid level gauges are provided in the raw gas separator, the conversion gas quench cooler, the low-pressure steam waste boiler, the conversion gas separator, the ammonia washing tower, the raw gas quench cooler, the carbon dioxide-rich methanol intercooler, and the absorption tower.

[0016] Furthermore, the guard bed, the first conversion furnace and the second conversion furnace are all provided with temperature gauges.

[0017] Furthermore, a gas composition analyzer is provided on the top outlet pipeline of the conversion gas separator.

[0018] Furthermore, the simulated material includes water and air.

[0019] Compared with the prior art, the advantages of the present invention are:

[0020] The utility model provides a semi-physical simulation device for coal-to-oil purification, including a conversion section, a low-temperature methanol washing section and simulated materials, which can better reflect the typical coal-to-oil purification process in industrial practice and enable students to understand the typical process flow, production principle, structure and use performance of the main equipment of the conversion and low-temperature methanol washing processes.

[0021] Simulated material water and air operation is adopted to ensure safety. The operating materials are safe, environmentally friendly, recyclable and have low operating costs. Training and assessment of coal-to-oil purification semi-physical simulation equipment are carried out, multiple skill training carriers are realized, and basic capacity building for conversion process and low-temperature methanol washing process skill training is supported. BRIEF DESCRIPTION OF THE DRAWINGS

[0022] Figure 1 It is a schematic diagram of the transformation section;

[0023] Figure 2 This is a schematic diagram of the low-temperature methanol washing section.

[0024] In the figure: V201-raw gas separator; V202-conversion gas quencher; E201-gas-gas heat exchanger; R203-guard bed; R201-first conversion furnace; R202-second conversion furnace; E202-low-pressure steam waste boiler; E203-boiler feed water preheater; E204-desalt water preheater; E205-conversion gas water cooler; V203-conversion gas separator; E301-raw gas synthesis gas heat exchanger; E3 02-conversion gas / tail gas heat exchanger; E303-raw gas quencher; E304-raw gas deep cooler; T301-ammonia washing tower; T302-absorption tower; E305-carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler; E306-carbon dioxide rich methanol intercooler; E309-hydrogen sulfide rich methanol cooler; E307-hydrogen sulfide absorption feed cooler; E308-synthesis gas heater; R301-fine desulfurization tower. DETAILED DESCRIPTION

[0025] In order to more clearly illustrate the embodiments of the utility model or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the utility model. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0026] like Figure 1 , Figure 2 As shown: a semi-physical simulation device for coal-to-oil purification includes a simulated conversion section, a simulated low-temperature methanol washing section and simulated materials, and the simulated materials flow in the simulated conversion section and the simulated low-temperature methanol washing section; the simulated materials include water and air, and the operating materials are safe, environmentally friendly, and recyclable, with low operating costs.

[0027] The simulated conversion section includes raw gas separator V201, conversion gas quencher V202, gas-to-gas heat exchanger E201, guard bed R203, first conversion furnace R201, second conversion furnace R202, low-pressure steam waste boiler E202, boiler feed water preheater E203, desalted water preheater E204, conversion gas water cooler E205, and conversion gas separator V203.

[0028] The tube-side inlet of the gas-to-gas heat exchanger E201 is connected to the raw gas separator V201 through a pipeline, the tube-side outlet of the gas-to-gas heat exchanger E201 is connected to the top inlet of the guard bed R203 through a pipeline, the shell-side inlet of the gas-to-gas heat exchanger E201 is connected to the bottom outlet of the first conversion furnace R201 through a pipeline, and the shell-side outlet of the gas-to-gas heat exchanger E201 is connected to the top inlet of the conversion gas quench cooler V202 through a pipeline; the top inlet of the first conversion furnace R201 is connected to the bottom outlet of the guard bed R203 through a pipeline; the conversion gas quench cooler V202, the second conversion furnace R202, the low-pressure steam waste boiler E202, the boiler feed water preheater E203, the desalted water preheater E204, the conversion gas water cooler E205, and the conversion gas separator V203 are connected in sequence through pipelines; the outlet pipeline of the conversion gas separator V203 is connected to the simulated low-temperature methanol washing section.

[0029] Transformation Process

[0030] The raw coal gas (temperature 165°C, pressure 4.0MPa) first passes through the raw gas separator V201 to separate the cooling water. The raw coal gas exiting the raw gas separator V201 enters the gas-to-gas heat exchanger E201 for heat exchange with the conversion gas from the outlet of the first conversion furnace R201. After the heat exchange, the temperature of the raw coal gas rises to 210-250°C and then enters the guard bed R203 to remove impurities such as Cl-, As, and dust in the raw coal gas. The raw coal gas after impurity removal enters the first conversion furnace R201 for conversion reaction to form conversion gas. The hot spot temperature of the first conversion furnace R201 is less than 450°C, and the volume dry content of CO at the outlet of the first conversion furnace is 36-42%. The conversion gas from the first conversion furnace R201 is heat exchanged with the raw coal gas in the gas-to-gas heat exchanger E201, and the temperature of the conversion gas is 340-370°C. Then the conversion gas enters the conversion gas quencher V202. At the inlet of the conversion gas quencher V202, the conversion gas is cooled and humidified by adding boiler water and a small amount of steam to achieve the water / gas ratio required by the second conversion furnace R202. The temperature of the conversion gas is controlled to 210-240°C, and then it enters the second conversion furnace R202 to continue the conversion reaction. The volume dry content of CO in the conversion gas from the second conversion furnace R202 is 20-25%, and the simulated temperature is 340-370°C. Then it enters the low-pressure steam waste boiler E202. The conversion gas from the low-pressure steam waste boiler E202 is further recovered through the boiler feed water preheater E203, the desalted water preheater E204, the conversion gas water cooler E205 and the conversion gas separator V203 to recover heat. After the process condensed water along the way is separated by the conversion gas separator V203, the conversion gas (temperature 40°C, pressure 3.6MPa) is sent to the downstream low-temperature methanol washing section.

[0031] The simulated low-temperature methanol washing section includes the raw gas synthesis gas heat exchanger E301, the conversion gas / tail gas heat exchanger E302, the raw gas quencher E303, the raw gas deep cooler E304, the ammonia washing tower T301, the absorption tower T302, the carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler E305, the carbon dioxide rich methanol intercooler E306, the hydrogen sulfide rich methanol cooler E309, the hydrogen sulfide absorption feed cooler E307, the synthesis gas heater E308, and the fine desulfurization tower R301.

[0032] The pipeline from the conversion gas separator V203 is divided into two branches. The first branch is connected to the raw gas synthesis gas heat exchanger E301 and the raw gas quencher E303 in sequence, and the second branch is connected to the conversion gas / tail gas heat exchanger E302. The first branch and the second branch merge at the entrance of the ammonia washing tower T301; the ammonia washing tower T301, the raw gas deep cooler E304, and the absorption tower T302 are connected in sequence through pipelines.

[0033] Absorption tower T302 is divided into a pre-wash section, an H2S washing section, a CO2 cooling section and a CO2 absorption section; the pre-wash section is connected to the hydrogen sulfide absorption feed cooler E307 through a pipeline; the H2S washing section is connected to the hydrogen sulfide rich methanol cooler E309 and the hydrogen sulfide absorption feed cooler E307 through pipelines respectively; the CO2 cooling section is connected to the hydrogen sulfide absorption feed cooler E307 and the carbon dioxide rich methanol intercooler E306 through a pipeline; the CO2 absorption section is connected to the carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler E305 through a pipeline.

[0034] The synthesis gas heater E308 is connected to the raw gas synthesis gas heat exchanger E301 through a pipeline; the fine desulfurization tower R301 is connected to the synthesis gas heater E308 through a pipeline.

[0035] Low temperature methanol washing process

[0036] (1) Cooling of raw gas (conversion gas)

[0037] The raw gas entering this unit is divided into two streams. The first stream is cooled to a temperature of about 10°C after passing through the raw gas / purified gas heat exchanger E301 and the raw gas quencher E303. The other stream of raw gas is cooled to a temperature of about 12°C in the raw gas / exhaust gas heat exchanger E302. Then the two streams of raw gas are mixed again and enter the ammonia washing tower T301 to remove most of the ammonia. The raw gas leaving the ammonia washing tower T301 is first mixed with a small stream of methanol to prevent water from freezing at low temperatures. Finally, the mixed raw gas is cooled by heat exchange with the purified synthesis gas, CO2 product gas and exhaust gas in the raw gas deep freezer E304.

[0038] (2) Mixed raw gas H2S / CO2 absorption

[0039] The pre-wash section of the absorption tower T302 is connected to the hydrogen sulfide absorption feed cooler E307 through a pipeline, and a small amount of impurities in the raw gas, such as NH3 and HCN, are absorbed by a small stream of supercooled CO2-rich methanol from the CO2 cooling section of the absorption tower T302; the H2S washing section is connected to the hydrogen sulfide rich methanol cooler E309 and the hydrogen sulfide absorption feed cooler E307 through pipelines, and H2S and COS are washed and removed by the CO2-rich methanol from the CO2 cooling section of the absorption tower T302; the CO2 cooling section is connected to the hydrogen sulfide absorption feed cooler E307 and the carbon dioxide rich methanol intercooler E306 through a pipeline, and the gas is washed by cooled CO2-rich methanol; the CO2 absorption section is connected to the carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler E305 through a pipeline, and the mixed raw gas is washed by methanol from the CO2 flash tower and cold hot regenerated methanol.

[0040] A flow meter is provided on the pipeline connecting the raw gas synthesis gas heat exchanger E301 to the synthesis gas heater E308; a flow meter is provided on the pipeline connecting the hydrogen sulfide absorption feed cooler E307 to the absorption tower T302.

[0041] Pressure sensors are provided on the outlet pipeline of the conversion gas separator V203, on the pipeline connecting the ammonia washing tower T301 to the raw gas deep cooler E304, on the top outlet pipeline of the absorption tower T302, and on the bottom outlet pipeline of the fine desulfurization tower R301.

[0042] Liquid level meters are installed in the raw gas separator V201, conversion gas quencher V202, low-pressure steam waste boiler E202, conversion gas separator V203, ammonia washing tower T301, raw gas quencher E303, carbon dioxide rich methanol intercooler E306 and absorption tower T302.

[0043] The guard bed R203, the first conversion furnace R201 and the second conversion furnace R202 are all equipped with temperature meters.

[0044] A gas composition analyzer is provided on the top outlet pipeline of the conversion gas separator V203.

[0045] This utility model is designed and developed for the research and teaching needs of schools of engineering majors such as chemical safety engineering, chemical engineering and technology, applied chemistry, and electrical engineering, and for the production safety skills training, assessment and certification needs of training centers and chemical companies. It combines the actual situation of the coal chemical industry and uses simulation to conduct practical training and examination of coal gasification purification process skills. It integrates the pulverized coal gasification purification process training for school students, enterprise operators and managers, and job personnel skills training, forming a complete, scientific, effective, and distinctive new system for practical assessment of coal-to-liquid purification semi-physical simulation devices. This device can better reflect the typical pulverized coal gasification purification process in industrial practice. The on-site device is reduced in proportion to the typical equipment in the pulverized coal chemical process, so that students can understand the typical process flow, production principle, structure and use performance of the main equipment in the pulverized coal gasification purification industry.

[0046] The above description of the disclosed embodiments enables those skilled in the art to implement or use the present invention. Various modifications to these embodiments will be apparent to those skilled in the art, and the general principles defined herein may be implemented in other embodiments without departing from the spirit or scope of the present invention. Therefore, the present invention will not be limited to the embodiments shown herein, but will conform to the widest scope consistent with the principles and novel features disclosed herein.

Claims

1. A semi-physical simulation device for coal-to-liquid purification, characterized in that: It includes a simulated conversion section, a simulated low-temperature methanol washing section and simulated materials, and the simulated materials flow in the simulated conversion section and the simulated low-temperature methanol washing section; The simulated conversion section includes a raw gas separator (V201), a conversion gas quencher (V202), a gas-to-gas heat exchanger (E201), a guard bed (R203), a first conversion furnace (R201), a second conversion furnace (R202), a low-pressure steam waste boiler (E202), a boiler feed water preheater (E203), a desalted water preheater (E204), a conversion gas water cooler (E205), and a conversion gas separator (V203); The tube-side inlet of the gas-gas heat exchanger (E201) is connected to the raw gas separator (V201) through a pipeline, the tube-side outlet of the gas-gas heat exchanger (E201) is connected to the top inlet of the guard bed (R203) through a pipeline, the shell-side inlet of the gas-gas heat exchanger (E201) is connected to the bottom outlet of the first conversion furnace (R201) through a pipeline, and the shell-side outlet of the gas-gas heat exchanger (E201) is connected to the top inlet of the conversion gas quencher (V202) through a pipeline; the first conversion furnace ( The top inlet of R201 is connected to the bottom outlet of the guard bed (R203) through a pipeline; the conversion gas quencher (V202), the second conversion furnace (R202), the low-pressure steam waste boiler (E202), the boiler feed water preheater (E203), the desalted water preheater (E204), the conversion gas water cooler (E205), and the conversion gas separator (V203) are connected in sequence through pipelines; the outlet pipeline of the conversion gas separator (V203) is connected to the simulated low-temperature methanol washing section; The simulated low-temperature methanol washing section includes the raw gas synthesis gas heat exchanger (E301), the shift gas / tail gas heat exchanger (E302), the raw gas quencher (E303), the raw gas deep cooler (E304), the ammonia washing tower (T301), the absorption tower (T302), the carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler (E305), the carbon dioxide rich methanol intercooler (E306), the hydrogen sulfide rich methanol cooler (E309), the hydrogen sulfide absorption feed cooler (E307), the synthesis gas heater (E308), and the fine desulfurization tower (R301); The pipeline from the shift gas separator (V203) is divided into two branches, the first branch is connected to the raw gas synthesis gas heat exchanger (E301) and the raw gas quencher (E303) in sequence, and the second branch is connected to the shift gas / tail gas heat exchanger (E302). The first branch and the second branch merge at the entrance of the ammonia washing tower (T301); the ammonia washing tower (T301), the raw gas deep cooler (E304), and the absorption tower (T302) are connected in sequence through pipelines; The absorption tower (T302) is divided into a pre-washing section, an H2S washing section, a CO2 cooling section and a CO2 absorption section; the pre-washing section is connected to the hydrogen sulfide absorption feed cooler (E307) through a pipeline; the H2S washing section is connected to the hydrogen sulfide rich methanol cooler (E309) and the hydrogen sulfide absorption feed cooler (E307) through pipelines; the CO2 cooling section is connected to the hydrogen sulfide absorption feed cooler (E307) and the carbon dioxide rich methanol intercooler (E306) through a pipeline; the CO2 absorption section is connected to the carbon dioxide rich methanol / hydrogen sulfide rich methanol cooler (E305) through a pipeline; The synthesis gas heater (E308) is connected to the raw gas synthesis gas heat exchanger (E301) through a pipeline; the fine desulfurization tower (R301) is connected to the synthesis gas heater (E308) through a pipeline.

2. A semi-physical simulation device for coal-to-liquid purification according to claim 1, characterized in that: A flow meter is provided on the pipeline connecting the raw gas synthesis gas heat exchanger (E301) to the synthesis gas heater (E308); a flow meter is provided on the pipeline connecting the hydrogen sulfide absorption feed cooler (E307) to the absorption tower (T302).

3. A semi-physical simulation device for coal-to-liquid purification according to claim 1, characterized in that: Pressure sensors are provided on the outlet pipeline of the conversion gas separator (V203), on the pipeline connecting the ammonia washing tower (T301) to the raw gas deep cooler (E304), on the top outlet pipeline of the absorption tower (T302) and on the bottom outlet pipeline of the fine desulfurization tower (R301).

4. A semi-physical simulation device for coal-to-liquid purification according to claim 1, characterized in that: The raw gas separator (V201), conversion gas quencher (V202), low-pressure steam waste boiler (E202), conversion gas separator (V203), ammonia washing tower (T301), raw gas quencher (E303), carbon dioxide rich methanol intercooler (E306), and absorption tower (T302) are all equipped with liquid level meters.

5. A semi-physical simulation device for coal-to-liquid purification according to claim 1, characterized in that: The guard bed (R203), the first conversion furnace (R201) and the second conversion furnace (R202) are all provided with temperature gauges.

6. A semi-physical simulation device for coal-to-liquid purification according to claim 1, characterized in that: A gas composition analyzer is provided on the top outlet pipeline of the conversion gas separator (V203).

7. A semi-physical simulation device for coal-to-liquid purification according to any one of claims 1 to 6, characterized in that: The simulated materials include water and air.

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