Isothermal transformation system suitable for high-concentration carbon monoxide

Abstract

The utility model belongs to the technical field of carbon monoxide isothermal conversion, and discloses an isothermal conversion system suitable for high-concentration carbon monoxide, outlet purified gas of a feed gas purification furnace is divided into two paths, one path is connected with an inlet of an isothermal conversion reaction furnace, and the other path is connected with an inlet at the upper end of an adiabatic conversion reaction furnace after passing through a first flow control valve; an outlet of the isothermal shift reaction furnace is connected with an inlet at the upper end of the adiabatic shift reaction furnace, an outlet at the lower end of the adiabatic shift reaction furnace is connected with an inlet of the first gas-liquid condenser, and an outlet of the first gas-liquid condenser is connected with an inlet of the second gas-liquid condenser; a steam pocket is arranged above the isothermal shift reaction furnace, lower hanging type water jackets are uniformly mounted in the isothermal shift reaction furnace, and inlets and outlets of the lower hanging type water jackets are communicated with the steam pocket. The device is suitable for one or more mixed gases of coal gas containing high-concentration carbon monoxide, calcium carbide furnace tail gas, iron alloy tail gas or methanol purge gas, and the service life of a catalyst is prolonged.

Description

TECHNICAL FIELD

[0001] The utility model belongs to carbon monoxide isothermal transformation technical field, concretely relates to a kind of isothermal transformation system of high concentration carbon monoxide suitable for. BACKGROUND

[0002] CO transformation unit is the important component of subsequent purification stage in pulverized coal gasification process, and is used to treat the raw gas generated by pulverized coal gasification device. At present, most of the equipment adopts advanced and mature medium transformation and low transformation sulfur transformation process, and the process is to convert CO and steam generated in the gasification process into H2 and CO2 by transformation catalyst.

[0003] CO transformation is an important section after coal chemical industry gasification, and its process scheme is mature, and currently most of them adopt isothermal transformation and adiabatic transformation two technologies.

[0004] U.S. Patent No. 6,033,634 discloses a plate-type high-temperature converter with a transformation reaction cavity filled with high-temperature transformation catalyst, a cooling cavity with packing to promote heat transfer, cooling gas introduced into the cooling cavity, and a partition separating the transformation reaction cavity and the cooling cavity. The transformation reaction cavity has a hydrogen cavity separated by a plate-type partition composed of a porous plate and a hydrogen-permeable palladium membrane. Therefore, only hydrogen generated in the transformation reaction cavity can pass through the hydrogen-permeable membrane into the hydrogen cavity.

[0005] Chinese Patent CN1461730A discloses a carbon monoxide transformation process and reactor. The process steps include: introducing raw gas into the reactor tube of the reaction unit, the reactor tube has a fixed bed of transformation catalyst in the reaction zone; contacting the raw gas with the catalyst under transformation reaction conditions that can effectively react carbon monoxide with steam to generate hydrogen; the cooling medium has a descending mode along the outer shell of the reactor tube, the reaction is cooled by non-direct heat exchange with the cooling medium, and the heated cooling medium is removed from the descending mode, the hydrogen generated by the transformation reaction reaches the permeation zone through the hydrogen-selective mode; hydrogen is extracted from the permeation zone and carbon monoxide-depleted raw gas is discharged from the reaction zone.

[0006] Coal gas, calcium carbide furnace tail gas, iron alloy tail gas, methanol purge gas and other gases contain CO, H2, CH4 and other effective fuel components, accounting for about 80% of the gas volume, mainly CO, with a calorific value of 2100-2400 kcal / m. Carbon monoxide, especially high-concentration carbon monoxide, releases a large amount of heat during the transformation reaction, resulting in high hot spot temperature of the catalyst bed, thereby reducing the service life of the catalyst and failing to meet normal production requirements. UTILITY MODEL CONTENTS

[0007] The utility model aims to provide a kind of isothermal transformation system of high concentration carbon monoxide suitable for, to solve the above problems existing in prior art.

[0008] In order to achieve the above object, the utility model adopts the following technical scheme:

[0009] A kind of high concentration carbon monoxide isothermal transformation system, including raw material gas purifier, isothermal transformation reaction furnace, adiabatic transformation reaction furnace, steam drum, first gas-liquid condenser and second gas-liquid condenser, raw material gas purifier inside is provided with from top to bottom sequentially filled desulfurization catalyst, dechlorination catalyst, arsenic removal catalyst and deoxygenation catalyst, and raw material gas purifier outlet purified gas is divided into two ways, one way is connected with the inlet of isothermal transformation reaction furnace, another way is connected with the inlet of adiabatic transformation reaction furnace upper end after passing through first flow control valve;The isothermal transformation reaction furnace is radially isothermal fixed bed with isothermal transformation catalyst inside, the inlet of adiabatic transformation reaction furnace upper end is connected with the outlet of isothermal transformation reaction furnace, and the adiabatic transformation reaction furnace is axially adiabatic fixed bed with copper series transformation catalyst inside, the inlet of first gas-liquid condenser is connected with the outlet of adiabatic transformation reaction furnace lower end, and the inlet of second gas-liquid condenser is connected with the outlet of first gas-liquid condenser;Steam drum is provided above the isothermal transformation reaction furnace, and the lower hanging type water jacket pipe with circulating water inside is uniformly installed in the isothermal transformation reaction furnace, and the inlet and outlet of lower hanging type water jacket pipe are communicated with steam drum.

[0010] As a preferred technical scheme in the utility model, the isothermal transformation reaction furnace is provided with annular gas inlet cavity close to its outer wall inside, the isothermal transformation reaction furnace is provided with middle gas outlet pipe in its middle part, the lower end of annular gas inlet cavity is communicated with the inlet of isothermal transformation reaction furnace, the lower end of middle gas outlet pipe is communicated with the outlet of isothermal transformation reaction furnace, and a plurality of gas holes are arranged on annular gas inlet cavity and middle gas outlet pipe.

[0011] As a preferred technical scheme in the utility model, the upper portion of isothermal transformation reaction furnace and the upper portion of adiabatic transformation reaction furnace are provided with water vapor gas inlet, and the second flow control valve is arranged in front of water vapor gas inlet of adiabatic transformation reaction furnace.

[0012] As a preferred technical scheme in the utility model, the concentration of sulfide in the purified gas of raw material gas purifier outlet is less than or equal to 0.05ppm, the content of oxygen is less than or equal to 0.02Vol%, the concentration of chloride is less than or equal to 0.01ppm, and the concentration of arsenide is less than or equal to 0.005ppm.

[0013] As a preferred technical scheme in the utility model, the volume space velocity of isothermal transformation reaction furnace is 1000-2000h -1 , the inlet temperature is 200-210 DEG C, and the outlet temperature is 220-250 DEG C.

[0014] As a preferred technical scheme in the utility model, the volume space velocity of adiabatic transformation reaction furnace is 1000-2000h-1 Inlet temperature 190-200℃, outlet temperature 210-240℃.

[0015] As a preferred technical scheme in the utility model, the bottom of the raw material gas purification furnace, the first gas-liquid condenser and the second gas-liquid condenser is provided with a condensate outlet.

[0016] As a preferred technical scheme in the utility model, the opening range of the first flow control valve is 0-20%.

[0017] Beneficial effects: the utility model adopts two different reaction furnace conversion series-parallel form, can satisfy high concentration carbon monoxide raw material gas shift reaction requirement, can effectively guarantee carbon monoxide shift effect, is applicable to one or more mixed gas of containing high concentration carbon monoxide coal gas, calcium carbide furnace tail gas, iron alloy tail gas or methanol release gas, solves the technical problem that many enterprises face that contain high concentration carbon monoxide and gas composition is complex. Among them, high-efficiency purification reaction furnace is used, can effectively control the content of sulfide, chloride, arsenide and oxygen of shift raw material gas, widens the source range of raw material gas. Radial isothermal fixed bed reactor is used, can effectively remove the heat generated by reaction, and the catalyst is in a reasonable temperature range for shift reaction, while by-product medium-pressure steam is produced. The adiabatic fixed bed reactor can be used as a refining reactor, effectively ensuring the shift effect of carbon monoxide, controlling the gas flow entering each shift reaction furnace through the first flow control valve, reasonably adjusting the reaction progress, ensuring that the catalyst will not be sintered at high temperature, prolonging the service life of the catalyst. BRIEF DESCRIPTION OF DRAWINGS

[0018] Figure 1 It is a structural schematic view of the utility model.

[0019] In the figure: 1-raw material gas purification furnace;2-isothermal shift reaction furnace;3-adiabatic shift reaction furnace;4-steam drum;5-first gas-liquid condenser;6-second gas-liquid condenser;7-first flow control valve;8-second flow control valve. DETAILED DESCRIPTION

[0020] In order to more clearly illustrate the technical scheme in the embodiment of the utility model or prior art, the utility model will be briefly introduced in combination with the drawings and the description of the embodiment or prior art, obviously, the following description of the structure of the drawings is only some embodiments of the utility model, and for those skilled in the art, other drawings can be obtained without creative labor according to these drawings. It needs to be explained that the description of these embodiment modes is used to help understanding the utility model, but does not constitute the limitation of the utility model.

[0021] Embodiment:

[0022] As Figure 1 shown, the present embodiment provides a high-concentration carbon monoxide isothermal shift conversion system, which comprises a raw gas purifier 1, an isothermal shift conversion reactor 2, an adiabatic shift conversion reactor 3, a steam drum 4, a first gas-liquid condenser 5 and a second gas-liquid condenser 6. The raw gas source of the raw gas purifier 1 can be one or more mixed gases containing high-concentration carbon monoxide, such as coal gas, calcium carbide furnace tail gas, ferroalloy tail gas or methanol purge gas. The raw gas purifier 1 is internally provided with desulfurization catalyst, dechlorination catalyst, dearsenization catalyst and deoxygenation catalyst filled in sequence from top to bottom. Through the treatment of the desulfurization catalyst, dechlorination catalyst, dearsenization catalyst and deoxygenation catalyst, combined with temperature control, the content of sulfides in the purified gas at the outlet of the raw gas purifier 1 is less than or equal to 0.05 ppm, the content of oxygen is less than or equal to 0.02 Vol%, the content of chlorides is less than or equal to 0.01 ppm, and the content of arsenides is less than or equal to 0.005 ppm. The high-efficiency purification reactor can effectively control the content of sulfides, chlorides, arsenides and oxygen in the shift raw gas, broaden the source range of the raw gas, and the purified gas at the outlet of the raw gas purifier 1 is divided into two routes, one of which is connected to the inlet of the isothermal shift conversion reactor 2, and the other is connected to the inlet of the upper end of the adiabatic shift conversion reactor 3 after passing through the first flow control valve 7. The opening range of the first flow control valve 7 is 0-20%, and the gas flow into the isothermal shift conversion reactor 2 and the adiabatic shift conversion reactor 3 can be controlled through the first flow control valve 7, so as to reasonably adjust the reaction progress and ensure that the catalyst will not be sintered at high temperature, thereby prolonging the service life of the catalyst. The isothermal shift conversion reactor 2 is a radial isothermal fixed bed filled with isothermal shift conversion catalyst, the outlet of the isothermal shift conversion reactor 2 is connected to the inlet of the upper end of the adiabatic shift conversion reactor 3, and the radial isothermal fixed bed reactor can effectively remove the heat generated during the reaction, so that the catalyst can perform shift conversion within a reasonable temperature range and simultaneously produce medium-pressure steam. The adiabatic shift conversion reactor 3 is an axial adiabatic fixed bed installed with copper-based shift catalyst, which can be used as a refining reactor to effectively ensure the shift conversion effect of carbon monoxide. The outlet at the lower end of the adiabatic shift conversion reactor 3 is connected to the inlet of the first gas-liquid condenser 5, and the outlet of the first gas-liquid condenser 5 is connected to the inlet of the second gas-liquid condenser 6, so as to finally obtain a crude shift product gas. The steam drum 4 is arranged above the isothermal shift conversion reactor 2, and the isothermal shift conversion reactor 2 is uniformly provided with a lower-hung water jacket pipe internally provided with circulating water. The inlet and outlet of the lower-hung water jacket pipe are both communicated with the steam drum 4, so that the water flow direction is upward.

[0023] As a preferred embodiment in the present embodiment, it needs to be further explained that the inside of the isothermal shift reactor 2 is provided with an annular gas inlet cavity close to the outer wall thereof, the inside of the isothermal shift reactor 2 is provided with a middle gas outlet pipe in the middle part thereof, the lower end of the annular gas inlet cavity is communicated with the inlet of the isothermal shift reactor 2, the lower end of the middle gas outlet pipe is communicated with the outlet of the isothermal shift reactor 2, and a plurality of gas holes are arranged on the annular gas inlet cavity and the middle gas outlet pipe, so that the purified gas entering the isothermal shift reactor 2 is fully contacted with the isothermal shift catalyst, then enters the middle gas outlet pipe, and then enters the adiabatic shift reactor 3 from the outlet of the isothermal shift reactor 2.

[0024] As a preferred embodiment in the present embodiment, it needs to be further explained that the upper part of the isothermal shift reactor 2 and the upper part of the adiabatic shift reactor 3 are both provided with a water vapor inlet, and the water vapor inlet of the adiabatic shift reactor 3 is provided with a second flow control valve 8 in front of the water vapor inlet, so that the depth of the shift reaction can be controlled by adjusting the amount of water vapor entering.

[0025] As a preferred embodiment in the present embodiment, it needs to be further explained that the volume space velocity of the isothermal shift reactor 2 is 1000-2000h -1 , the inlet temperature is 200-210℃, and the outlet temperature is 220-250℃, the volume space velocity of the adiabatic shift reactor 3 is 1000-2000h -1 , the inlet temperature is 190-200℃, and the outlet temperature is 210-240℃, the gas flow entering each shift reactor can be controlled by the volume flow combined with the regulating valve, the reaction progress can be reasonably allocated, the catalyst will not be sintered at high temperature, the service life of the catalyst is prolonged, the control of the temperature range can effectively ensure the shift effect of carbon monoxide, and the system design requirements are met.

[0026] As a preferred embodiment in the present embodiment, it needs to be further explained that the bottom of the raw gas purification furnace 1, the first gas-liquid condenser 5 and the second gas-liquid condenser 6 are all provided with a condensate outlet, so as to facilitate the discharge of the generated process condensate.

[0027] Experimental Example 1:

[0028] The raw material gas is derived from calcium carbide furnace tail gas, and the composition of the purified gas is: H2 4.4%, CO 77.8%, CO2 6.2%, N2 11.9%, CH4 0.025%, sulfide 0.02ppm, chloride 0.003ppm, arsenide 0ppm, and O2 0.001ppm.

[0029] The volume space velocity of the isothermal shift reactor 2 is 1500h -1 , the inlet temperature is 200℃, and the outlet temperature is 225℃;

[0030] The volume space velocity of the adiabatic shift reactor 3 was 1500 h -1 , the inlet temperature was 190°C, and the outlet temperature was 215°C.

[0031] The opening of the flow control valve 7 was 5%.

[0032] The gas composition of the crude product gas was H2 69.52%, CO 1.5%, CO2 17.7%, N2 11.25%, and CH4 0.028%.

[0033] The total carbon monoxide conversion rate was 96.62%.

[0034] Experimental Example 2

[0035] The raw material gas was derived from a mixture of an electric furnace tail gas of ferroalloy and a coal gas, and the gas composition of the purified gas was H2 11.5%, CO 64.1%, CO2 5.3%, N2 13.6%, CH4 1.4%, sulfide 0.015 ppm, chloride 0.002 ppm, arsenide 0 ppm, and O2 0.005 ppm.

[0036] The volume space velocity of the isothermal shift reactor 2 was 1500 h -1 , the inlet temperature was 205°C, and the outlet temperature was 225°C.

[0037] The volume space velocity of the adiabatic shift reactor 3 was 1500 h -1 , the inlet temperature was 190°C, and the outlet temperature was 215°C.

[0038] The opening of the flow control valve 7 was 0%.

[0039] The gas composition of the crude product gas was H2 72.25%, CO 1.5%, CO2 12.4%, N2 11.9%, and CH4 1.25%.

[0040] The total carbon monoxide conversion rate was 96.22%.

[0041] Experimental Example 3

[0042] The raw material gas was derived from a mixture of an electric furnace tail gas of ferroalloy and a coal gas, and the gas composition of the purified gas was H2 11.5%, CO 64.1%, CO2 5.3%, N2 13.6%, CH4 1.4%, sulfide 0.015 ppm, chloride 0.002 ppm, arsenide 0 ppm, and O2 0.005 ppm.

[0043] The volume space velocity of the isothermal shift reactor 2 was 2000 h -1 , the inlet temperature was 205°C, and the outlet temperature was 230°C.

[0044] The volume space velocity of the adiabatic shift reaction furnace 3 was 2100 h -1 , the inlet temperature was 195°C, and the outlet temperature was 215°C.

[0045] The opening of the flow control valve 7 was 10%.

[0046] The gas composition of the crude product gas was H2 72.25%, CO 1.52%, CO2 12.4%, N2 11.9%, and CH4 1.25%.

[0047] The total carbon monoxide conversion rate was 96.17%.

[0048] Experimental Example 4:

[0049] The raw material gas was derived from coal gas, and the gas composition of the purified gas was H2 12.0%, CO 32.1%, CO2 5.3%, N2 47.4%, CH4 3.1%, sulfide 0.02 ppm, chloride 0.004 ppm, arsenide 0 ppm, and O2 0.001 ppm.

[0050] The volume space velocity of the isothermal shift reaction furnace 2 was 1500 h -1 , the inlet temperature was 205°C, and the outlet temperature was 230°C.

[0051] The volume space velocity of the adiabatic shift reaction furnace 3 was 1500 h -1 , the inlet temperature was 195°C, and the outlet temperature was 235°C.

[0052] The opening of the flow control valve 7 was 0%.

[0053] The gas composition of the crude product gas was H2 37.45%, CO 1.1%, CO2 12.9%, N2 45.5%, and CH4 2.85%.

[0054] The total carbon monoxide conversion rate was 96.11%.

[0055] Experimental Example 5:

[0056] The raw material gas was derived from a mixture of iron alloy electric furnace tail gas and coal gas, and the gas composition of the purified gas was H2 11.5%, CO 64.1%, CO2 5.3%, N2 13.6%, CH4 1.4%, sulfide 0.015 ppm, chloride 0.002 ppm, arsenide 0 ppm, and O2 0.005 ppm.

[0057] The volume space velocity of the isothermal shift reaction furnace 2 was 1500 h -1 , the inlet temperature was 205°C, and the outlet temperature was 230°C.

[0058] The volume space velocity of the adiabatic shift reaction furnace 3 was 2000 h -1Inlet temperature 195℃, outlet temperature 215℃

[0059] Flow control valve 7 opening degree is 20%.

[0060] The gas composition of the crude product gas is: H2 72.25%, CO 1.62%, CO2 12.4%, N2 11.9%, CH4 1.25%.

[0061] The total carbon monoxide conversion rate is 95.95%.

[0062] The utility model discloses a two different reaction furnace conversion series-parallel connection form, can satisfy the raw material gas shift reaction requirement of high concentration carbon monoxide, can effectively guarantee the shift effect of carbon monoxide, is applicable to one or more mixed gas of coal gas, calcium carbide furnace tail gas, iron alloy tail gas or methanol release gas containing high concentration carbon monoxide, solves the technical problem of many enterprises facing containing high concentration carbon monoxide and complex gas composition.

[0063] Finally, it should be noted that: the above only for the preferred embodiment of the utility model, and is not used to limit the protection scope of the utility model. Any modification, equivalent replacement, improvement etc. that is made within the spirit and principles of the utility model, should be included in the protection scope of the utility model.

Claims

1. An isothermal shift conversion system for high concentrations of carbon monoxide, characterized by, The application relates to a raw gas purification furnace (1), an isothermal shift reaction furnace (2), an adiabatic shift reaction furnace (3), a steam drum (4), a first gas-liquid condenser (5) and a second gas-liquid condenser (6), the raw gas purification furnace (1) is internally provided with desulfurization catalysts, dechlorination catalysts, dearsenic catalysts and deoxygenation catalysts filled from top to bottom, and the outlet purified gas of the raw gas purification furnace (1) is divided into two paths, one path is connected with the inlet of the isothermal shift reaction furnace (2), and the other path is connected with the inlet of the upper end of the adiabatic shift reaction furnace (3) after passing through a first flow control valve (7); the isothermal shift reaction furnace (2) is a radial isothermal fixed bed internally filled with isothermal shift catalysts, the outlet of the isothermal shift reaction furnace (2) is connected with the inlet of the upper end of the adiabatic shift reaction furnace (3), the adiabatic shift reaction furnace (3) is an axial adiabatic fixed bed internally installed with copper series shift catalysts, the outlet of the lower end of the adiabatic shift reaction furnace (3) is connected with the inlet of the first gas-liquid condenser (5), and the outlet of the first gas-liquid condenser (5) is connected with the inlet of the second gas-liquid condenser (6); the isothermal shift reaction furnace (2) is provided with the steam drum (4) above, and is uniformly installed with a lower hanging type water jacket pipe internally provided with circulating water, and the inlet and outlet of the lower hanging type water jacket pipe are both communicated with the steam drum (4).

2. The high concentration carbon monoxide isothermal shift system according to claim 1, wherein, The isothermal shift reaction furnace (2) is internally provided with an annular gas inlet cavity close to the outer wall, the isothermal shift reaction furnace (2) is internally provided with a middle gas outlet pipe located in the middle part, the lower end of the annular gas inlet cavity is communicated with the inlet of the isothermal shift reaction furnace (2), the lower end of the middle gas outlet pipe is communicated with the outlet of the isothermal shift reaction furnace (2), and a plurality of gas holes are arranged on the annular gas inlet cavity and the middle gas outlet pipe.

3. A high concentration carbon monoxide isothermal shift system according to claim 1 or 2, wherein The upper part of the isothermal shift reaction furnace (2) and the upper part of the adiabatic shift reaction furnace (3) are both provided with water vapor inlets, and the water vapor inlet of the adiabatic shift reaction furnace (3) is provided with a second flow control valve (8) in front.

4. The high concentration carbon monoxide isothermal shift system according to claim 1 or 2, characterized in that, The bottom of the raw gas purification furnace (1), the first gas-liquid condenser (5) and the second gas-liquid condenser (6) is provided with a condensate outlet.

5. A high concentration carbon monoxide isothermal shift system according to claim 1 or 2, wherein The opening range of the first flow control valve (7) is 0-20%.

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