CN104709875A - Isothermal conversion process of high-concentration carbon monoxide and system thereof - Google Patents
Isothermal conversion process of high-concentration carbon monoxide and system thereof Download PDFInfo
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Abstract
The invention discloses an isothermal conversion process of high-concentration carbon monoxide and a system thereof, and solves the problems of long procedure period, high system resistance and short in catalyst life in the existing conversion process. According to the adopted technical scheme, raw material gas flows through a raw material gas separator, so that water carried by the raw material gas is separated; then the raw material gas is filtered by a filter, and then is introduced into a shell side of a gas cooling conversion reactor to be preheated; the preheated raw material gas is introduced into a water cooling conversion reactor I to carry out conversion reaction; steam pocket byproduct steam is used for removing reaction heat of the conversion reaction; conversion gas out of the water cooling conversion reactor I is returned to the shell side of the gas cooling conversion reactor to preheat the raw material gas in the shell side,, so s to remove the reaction heat and continue to carry out conversion reaction; the conversion gas out of the gas cooling conversion reactor is further subjected to heat recycling, and after the condensed liquid is separated, the conversion gas is subsequently introduced into the downstream process. The isothermal conversion process of high-concentration carbon monoxide is simple in process, high in system reliability, low in methanation side reaction, short in process, low in system resistance, long in service life of catalyst, and low in equipment investment and operation cost.
Description
Technical field
The present invention relates to a kind of isothermal conversion process and system thereof, specifically a kind of high-concentration carbon monoxide isothermal conversion process and system thereof.
Background technology
China is a rich coal resources, the country that petroleum resources lack relatively, the efficiency utilization of coal resources has important strategic importance to China, since entering 21 century, the Coal Chemical Industry cause of China enters the stage of a high speed development, is that the technology such as raw material production synthetic ammonia urea, hydrogen manufacturing, synthesizing methanol, preparing ethylene glycol, synthetic natural gas obtain and greatly develop with coal.
CO Varying Process is a ring indispensable in Modern Coal-based Chemical technology, its Main Function is the ratio by carbon monoxide and hydrogen in transformationreation adjustment synthetic gas, to meet the requirement of downstream building-up reactions, along with applying of new type coal gasification technology, continuous pressure gasification technology obtains and develops fast, and representative has fine coal gasification process (SHELL, space flight stove, GSP etc.) and coal-water slurry gasification (Texaco, multi-nozzle, polynary slurry etc.).Carbon monoxide content (butt) in raw gas improves constantly on 30% originally traditional basis, and what have even reaches more than 70%.
Transformationreation is a thermopositive reaction, traditional conversion process adopts adiabatic shift-converter, the transformationreation of high-concentration carbon monoxide is too large due to reaction impellent, often causes beds overtemperature, has a strong impact on the work-ing life of catalyzer and the stability of operation.In order to solve this difficult problem, general employing high water-gas ratio technique or low water-gas ratio technique, when carbon monoxide content is all very high for the aqueous vapor of high water-gas ratio technique Raw gas, the loadings of necessary accurate calculation catalyzer, otherwise beds just there will be overtemperature, the water-gas ratio of low water-gas ratio technique Raw gas is lower, can well control temperature of reaction, but low water-gas ratio technique exists the risk of methanation side reaction by molecular balance.In addition, con-ventional insulation conversion process ubiquity long flow path, the problem such as equipment is many, systemic resistance is fallen greatly, bed hot(test)-spot temperature is high, catalyst life is short.
Summary of the invention
The object of the invention is to solve the problems of the technologies described above, providing that a kind of flow process is simple, system reliability good, methanation side reaction is little, flow process is short, systemic resistance is little, catalyzer long service life, system temperature control good, facility investment and running cost is low high-concentration carbon monoxide isothermal conversion process.
The present invention also provides a kind of high-concentration carbon monoxide isothermal transformation system for above-mentioned technique.
A kind of high-concentration carbon monoxide isothermal conversion process, it is characterized in that, the unstripped gas containing high-concentration carbon monoxide from upstream is first separated the moisture carried secretly through feed gas separator, then after unstripped gas metre filter dry linting dirt and toxic substance, gas enters the shell side preheating of air cooling shift-converter, unstripped gas after preheating enters 1# water-cooled shift-converter to carry out transformationreation and utilizes drum byproduct steam to remove the reaction heat of transformationreation, the unstripped gas that the conversion gas loopback going out 1# water-cooled shift-converter enters in the tube side of described air cooling shift-converter in preheating shell side is removed reaction heat and proceeds transformationreation, the conversion gas going out air cooling shift-converter reclaims heat further, lower procedure is entered after isolating phlegma.
Described go out air cooling shift-converter conversion gas adjustment water to steam ratio after send into adiabatic shift-converter, the conversion gas going out adiabatic shift-converter reclaims heat more further, isolate phlegma after enter lower procedure.
The conversion gas of the described 1# of going out water-cooled shift-converter first carries out transformationreation further through 2# water-cooled shift-converter and utilizes drum byproduct steam to remove the reaction heat of transformationreation, and the conversion gas loopback going out 2# water-cooled shift-converter enters the tube side of described air cooling shift-converter.
The described carbon monoxide butt volume content contained in the unstripped gas of high-concentration carbon monoxide from upstream is 40 ~ 90%, and water vapor/dry gas volume range is 0.2 ~ 1.6 pressure range is 3.0 ~ 8.7MPaG.
After the preheating of air cooling shift-converter, unstripped gas temperature range is 200 ~ 290 DEG C.
The hot(test)-spot temperature scope that described water-cooled shift-converter high temperature moves hot-zone is 180 ~ 350 DEG C, and by-product middle pressure steam pressure range is 0.5 ~ 6.0MPaG.
Described water-cooled shift-converter is floating head type water-cooled shift-converter or board-like water-cooled shift-converter.
Described floating head type water-cooled shift-converter comprises housing, is positioned at the upper tube box of housing epimere, the lower tube box of the middle cylinder in stage casing and hypomere, the heat transfer tube that many two ends are communicated with upper tube box and lower tube box is respectively provided with in described middle cylinder, transformation catalyst is filled with in described heat transfer tube, inert ceramic balls is filled with in described lower tube box, and described lower tube box and housing bottom have gap, described gap is communicated with middle cylinder; Vertical centering control space bar is provided with in described upper tube box, the raw material gas inlet of described case top communicates with the side of central dividing plate in upper tube box, the conversion gas outlet of described case top communicates with the side of central dividing plate in upper tube box, and described middle cylinder is provided with feedwater import and vapour outlet.
Described board-like water-cooled shift-converter comprises housing, is positioned at the upper tube box of housing epimere, the lower tube box of the middle cylinder in stage casing and hypomere, the axis of described middle cylinder is provided with pipe core, pipe core periphery is provided with the plate package of annular, described plate package is made up of the radial heat exchanger plates that arranges of several piece, transformation catalyst is filled with in gap between adjacent heat exchanger plates, there is between described plate package and housing gas collection annular space, described gas collection annular space successively with upper tube box and the conversion gas outlet being positioned at case top; Described pipe core tube wall arranges gas distribution holes, and the lower end of described pipe core is communicated with the raw material gas inlet of housing bottom; The lower end of described plate package and the feedwater inlet communication of housing bottom, upper end is communicated with the vapour outlet of case top.
Also there is inside clearance between described pipe core and plate package, in inside clearance, be filled with transformation catalyst.
For the high-concentration carbon monoxide isothermal transformation system of above-mentioned technique, comprise the feed gas separator, unstripped gas strainer, the shell side of air cooling shift-converter, 1# water-cooled shift-converter, the tube side of air cooling shift-converter and the cooling recovery system that connect successively; Described 1# water-cooled shift-converter is used for byproduct steam with drum.
Shell side or the tube side menopause thermal conversion reactor of described air cooling shift-converter are connected with cooling recovery system.
The shell side of described air cooling shift-converter is connected with the tube side of air cooling shift-converter through 1# water-cooled shift-converter, 2# water-cooled shift-converter successively, and described 2# water-cooled shift-converter is used for byproduct steam with drum.
Described water-cooled shift-converter is floating head type water-cooled shift-converter or board-like water-cooled shift-converter.
Described floating head type water-cooled shift-converter comprises housing, is positioned at the upper tube box of housing epimere, the lower tube box of the middle cylinder in stage casing and hypomere, the heat transfer tube that many two ends are communicated with upper tube box and lower tube box is respectively provided with in described middle cylinder, transformation catalyst is filled with in described heat transfer tube, inert ceramic balls is filled with in described lower tube box, and described lower tube box and housing bottom have gap, described gap is communicated with middle cylinder; Vertical centering control space bar is provided with in described upper tube box, the raw material gas inlet of described case top communicates with the side of central dividing plate in upper tube box, the conversion gas outlet of described case top communicates with the side of central dividing plate in upper tube box, and described middle cylinder is provided with feedwater import and vapour outlet.
Described board-like water-cooled shift-converter comprises housing, is positioned at the upper tube box of housing epimere, the lower tube box of the middle cylinder in stage casing and hypomere, the axis of described middle cylinder is provided with pipe core, pipe core periphery is provided with the plate package of annular, described plate package is made up of the radial heat exchanger plates that arranges of several piece, transformation catalyst is filled with in gap between adjacent heat exchanger plates, there is between described plate package and housing gas collection annular space, described gas collection annular space successively with upper tube box and the conversion gas outlet being positioned at case top; Described pipe core tube wall arranges gas distribution holes, and the lower end of described pipe core is communicated with the raw material gas inlet of housing bottom; The lower end of described plate package and the feedwater inlet communication of housing bottom, upper end is communicated with the vapour outlet of case top.
Also there is inside clearance between described pipe core and plate package, in inside clearance, be filled with transformation catalyst.
The Low Pressure Waste Heat Boiler that described cooling recovery system can include but not limited to connect successively, demineralized-water preheater, conversion are separated water cooler and conversion gas separator, for conversion gas cooling down, and isolate phlegma.
In the present invention, unstripped gas after preheating carries out transformationreation in water-cooled shift-converter, and reaction heat can be reclaimed by drum, byproduct steam, the conversion gas temperature gone out in water-cooled shift-converter is 260 ~ 280 degree, now, the available tube side passing into air cooling shift-converter carries out transformationreation further, and reaction heat can be used for the unstripped gas after preheating filtration, employing Two Stages is reacted, transformationreation heat energy shifts out fast, effectively reduces the risk of methanation side reaction, reduces systemic resistance.
Further, according to, described water-cooled shift-converter can use in two series connection, or an adiabatic shift-converter of connecting again after air cooling shift-converter, forms three grades of shift processes, improves conversion efficiency and system stability further.
Further, the structure of contriver to water-cooled shift-converter is improved, have employed the structure formation of floating head type water-cooled shift-converter or board-like water-cooled shift-converter, the former utilizes the floating head type of lower tube box to design, the oiler feed of shell side is made to be distributed in outside whole heat-exchanging tube bundle and lower tube box, extend the flow process of passing through of conversion gas on the one hand, improve transformationreation efficiency, ensure fully effectively heat exchange on the other hand, thus maintain transformationreation and carry out under almost isothermal or low temperature, avoid beds hot(test)-spot temperature too high.The latter utilizes the radial heat exchanger plates that arranges of several piece to shift out reaction heat, and, between pipe core and plate package, inside clearance is set, fill transformation catalyst therebetween and form adiabatic reaction district, fill transformation catalyst between heat exchanger plates and form isothermal reaction district, when unstripped gas is flowed out by the gas distribution holes of pipe core, be introduced into adiabatic reaction district carry out either shallow conversion make conversion gas temperature higher than byproduct steam temperature more than 10 DEG C, then the isothermal reaction district radially entered between heat exchanger plates carries out transformationreation, and by-product high-quality steam, finally enter gas collection annular space collect after by Base top contact, adiabatic reaction district and isothermal reaction district in this reactor also deposit, have that to move thermo-efficiency high, catalyst life is long, the stable advantage of bed temperature.Described air cooling shift-converter also can adopt tube-sheet type structure, and catalyst filling in tube side heat transfer tube, passes into conversion gas, and shell side passes into the unstripped gas treating preheating.
The present invention has following beneficial effect:
(1) suitability is good, is 40 ~ 90% to carbon monoxide butt volume content, water vapor/dry gas volume range be 0.2 ~ 1.6 unstripped gas all applicable.
(2) technical process is shorter, and number of devices is few, and control simple, systemic resistance is fallen little, saves facility investment and running cost.
(3) reactor operating condition is gentle, and temperature of reaction is easily controlled, and the problem that beds hot(test)-spot temperature is high is effectively solved, and reaction conversion ratio is high.
(4) heat recovery efficiency is high, to greatest extent the high-grade steam of by-product.
Accompanying drawing explanation
Fig. 1 is floating head type water-cooled shift-converter equipment drawing of the present invention.
Fig. 2 is the present invention's board-like water-cooled shift-converter equipment drawing.
Fig. 3 is the present invention's board-like formula water-cooled shift-converter A-A sectional view.
Fig. 4 is the process flow diagram of the embodiment of the present invention 1.
Fig. 5 is the process flow diagram of the embodiment of the present invention 2.
Fig. 6 is the process flow diagram of the embodiment of the present invention 3.
Wherein, drum, 6-adiabatic shift-converter, 7-Low Pressure Waste Heat Boiler, 8-demineralized-water preheater, 9-1# conversion gas separator, 10-conversion gas water cooler, 11-2# conversion gas separator, 12-3# conversion gas separator, 13-2# water-cooled shift-converter, 14-low-pressure drum is pressed in 1-feed gas separator, 2-unstripped gas strainer, 3-air cooling shift-converter, 4-1# water-cooled shift-converter, 5-.
In Fig. 1 floating head type water-cooled shift-converter, A11-housing, A12-upper tube box, A13-middle cylinder, A14-lower tube box, A15-heat transfer tube, A16-gap, A17-central dividing plate, A18-raw material gas inlet, the outlet of A19-conversion gas, the import of A20-feedwater, A21-vapour outlet
Fig. 2 invents in board-like water-cooled shift-converter, the outlet of B11-housing, B12-upper tube box, B13-middle cylinder, B14-lower tube box, B15-pipe core, B16-heat exchanger plates, B17-gas collection annular space, B18-conversion gas, B19-gas distribution holes, B20-raw material gas inlet, the import of B21-feedwater, B22-vapour outlet, B23-inside clearance.
Embodiment
Below in conjunction with accompanying drawing, explanation is further explained to the present invention:
See Fig. 1, the structure of described floating head type water-cooled shift-converter is as follows:
Comprise housing A11, be positioned at the upper tube box A12 of housing A11 epimere, the lower tube box A14 of the middle cylinder A13 in stage casing and hypomere, the heat transfer tube A15 that many two ends are communicated with upper tube box A12 and lower tube box A14 is respectively provided with in described middle cylinder A13, transformation catalyst is filled with in described heat transfer tube A15, be filled with in described lower tube box A14 inert ceramic balls (for support catalyst and be conducive to gas uniform distribution effect), and bottom described lower tube box A14 and housing A11, there is gap A16, described gap A16 is communicated with middle cylinder A13; Vertical central dividing plate A17 is provided with in described upper tube box A12, the raw material gas inlet A18 at described housing A11 top communicates with the side of central dividing plate A17 in upper tube box A12, the conversion gas outlet A19 at described housing A11 top communicates with the side of central dividing plate A17 in upper tube box A12, and described middle cylinder A13 is provided with feedwater import A20 and vapour outlet A21.
Principle of work: unstripped gas enters in upper tube box A12 by raw material gas inlet A18, due to the buffer action of central dividing plate A17, unstripped gas enters in the heat transfer tube A15 in left side downwards by the upper tube box A12 on the left of central dividing plate A17, transformationreation is carried out under the effect of transformation catalyst, non-interference between each heat transfer tube, the conversion gas left after the heat transfer tube A15 of left side enters in the heat transfer tube A15 on right side after entering and carrying out quadratic distribution in lower tube box A14 bottom internals again, transformationreation is proceeded under the effect of conversion gas at transformation catalyst in the heat transfer tube A15 on right side, the upper tube box A12 that the conversion gas leaving the heat transfer tube A15 on right side rises on the right side of central dividing plate A17 exports A19 by conversion gas and leaves reactor.Oiler feed enters in reactor from the boiler feedwater inlet A20 of middle cylinder A13 shell side, flowing between heat transfer tube A15 also carries out heat exchange with the conversion gas in heat transfer tube A15, remove the partial heat that transformationreation produces, carry out at low temperatures to maintain pipe inner conversion reaction, the steam of by-product leaves reactor by vapour outlet A21.
See Fig. 2, Fig. 3, the structure of described board-like water-cooled shift-converter is as follows:
Comprise housing B11, be arranged in the upper tube box B12 of housing epimere, the middle cylinder B13 in stage casing and the lower tube box B14 (lower tube box is filled with inert ceramic balls) of hypomere, the axis of described middle cylinder B13 is provided with pipe core B15, pipe core B15 periphery is provided with the plate package of annular, described plate package arranges plate package B16 by several piece is radial, is filled with transformation catalyst in the gap between adjacent heat exchanger plates B16; Between described pipe core B15 and plate package, there is inside clearance B23, transformation catalyst is filled with in inside clearance B23, have gas collection annular space B17 between described plate package and housing B11, described gas collection annular space B17 exports B18 with upper tube box B12 with the conversion gas being positioned at housing B11 top successively and is communicated with; Described pipe core B15 tube wall arranges gas distribution holes B19, and the lower end of described pipe core B15 is communicated with the raw material gas inlet B20 bottom housing B11; The lower end of described plate package is communicated with the feedwater import B21 bottom housing B11, and upper end is communicated with the vapour outlet B22 at housing B11 top.
Principle of work: unstripped gas enters in pipe core B15 by raw material gas inlet A20 bottom housing B11, inside clearance B23 between pipe core B15 and plate package and adiabatic reaction district is radially entered via the gas distribution holes B19 on pipe core B15 tube wall, in adiabatic reaction district, carry out either shallow conversion makes conversion gas temperature higher than byproduct steam temperature more than 10 DEG C, then transformationreation is carried out in the transformation catalyst between the heat exchanger plates B16 radially entering radial distribution, reacted conversion gas enters in the gas collection annular space B17 between housing B11 and plate package, export B18 through upper tube box B12 by the conversion gas at housing B11 top after conversion gas converges in gas collection annular space B17 and leave reactor.Oiler feed enters in each heat exchanger plates B16 of each heat exchange group by the boiler feedwater inlet B21 bottom housing B11 through pipeline, the outer conversion gas cross-flow heat exchange with plate in heat exchanger plates B16, remove the partial heat that transformationreation produces, carry out at low temperatures with the outer transformationreation of retaining plate, the steam of by-product leaves reactor via the vapour outlet B22 at housing B11 top.
Described transformation catalyst can be Co-Mo sulfur-tolerant shift catalyst.
Embodiment 1:
As shown in Figure 4, unstripped gas temperature from certain gasifying powder coal device (chilling process) is 208 DEG C, pressure is 3.7MpaG, carbon monoxide butt volume content is 71.2%, first unstripped gas is separated the moisture carried secretly through feed gas separator 1, then remove the harmful dust of catalyzer and toxic substance through unstripped gas strainer 2, unstripped gas after filtration enters 1# water-cooled shift-converter 4 (being floating head type water-cooled shift-converter in the present embodiment) and carries out transformationreation after entering and being preheated to 260 DEG C in the shell side of air cooling shift-converter 3, controlling temperature of reaction is 270 DEG C, medium pressure boiler feedwater enters in 1# water-cooled shift-converter 4 in bottom, in middle pressure drum 5, by by-product middle pressure steam, (pressure is 4.2MpaG, temperature is 255 DEG C) remove the reaction heat of transformationreation, the conversion gas going out 1# water-cooled shift-converter 4 enters in the tube side of air cooling shift-converter 3 and proceeds transformationreation, controlling temperature of reaction is 260 DEG C, it is enter in adiabatic shift-converter 6 after 0.23 to proceed transformationreation that the conversion gas going out air cooling shift-converter 3 fills into oiler feed adjustment water-gas ratio, controlling temperature of reaction is 220 DEG C, go out the conversion gas of adiabatic shift-converter 6 successively through Low Pressure Waste Heat Boiler 7, demineralized-water preheater 8 reclaims after heat is cooled to 80 DEG C and enters 1# conversion gas separator 9 separating and condensing liquid, the conversion gas going out 1# conversion gas separator 9 is lowered the temperature through conversion gas water cooler 10 and 2# conversion gas separator 11 successively and enters lower procedure after separating and condensing liquid, adopt the present invention can every kNm
3unstripped gas, can by-product 223kg high-quality middle pressure steam, and systemic resistance can decline 1/3, and generating cost of investment can reduce by 1/4, and the gas composition before and after present invention process conversion is as shown in Table 1 below:
The gas composition of shift conversion step is passed in and out in table 1 embodiment 1
| Each component molar mark (%) | H2 | CO | CO2 | H2O | H2S | N2 | Ar |
| Shift conversion step entrance | 10.5 | 36.1 | 3.5 | 49.3 | 0.3 | 0.2 | 0.1 |
| Shift conversion step exports | 53.1 | 1.1 | 44.9 | 0.3 | 0.3 | 0.2 | 0.1 |
Embodiment 2
As shown in Figure 5, the unstripped gas temperature from certain coal water slurry gasifying device is 215 DEG C, and pressure is 4.1MpaG, and carbon monoxide butt volume content is 47.6%.First unstripped gas is separated the moisture carried secretly through feed gas separator 1, then remove the harmful dust of catalyzer and toxic substance through unstripped gas strainer 2, enter after the shell side that unstripped gas after filtration enters air cooling shift-converter 3 is preheated to 260 DEG C in 1# water-cooled shift-converter 4 (being board-like water-cooled shift-converter in the present embodiment) and carry out transformationreation, controlling temperature of reaction is 270 DEG C, medium pressure boiler feedwater enters in 1# water-cooled shift-converter 4 in bottom, in middle pressure drum 5, by by-product middle pressure steam, (pressure is 4.2MpaG, temperature is 255 DEG C) remove the reaction heat of transformationreation, the conversion gas going out 1# water-cooled shift-converter 4 enters in air cooling shift-converter 3 and proceeds transformationreation, controlling temperature of reaction is 245 DEG C, the conversion gas going out air cooling shift-converter 3 reclaims after heat through low pressure used heat 7 boiler and enters 1# conversion gas separator 9 separating and condensing liquid, the conversion gas going out 1# conversion gas separator 9 enters after demineralized-water preheater 8 reclaims heat and enters 2# conversion gas separator 11 separating and condensing liquid, the conversion gas going out 2# conversion gas separator 11 is lowered the temperature through conversion gas water cooler 10 and 3# conversion gas separator 12 successively and enters lower procedure after separating and condensing liquid.Adopt the present invention can every kNm
3unstripped gas, can by-product 141kg high-quality middle pressure steam, and systemic resistance can decline 1/3, and generating cost of investment can reduce by 1/4, and the gas composition before and after present invention process conversion is as shown in Table 2 below:
The gas composition of shift conversion step is passed in and out in table 2 embodiment 2
| Each component molar mark (%) | H2 | CO | CO2 | H2O | H2S | N2 | Ar |
| Shift conversion step entrance | 15.1 | 22.1 | 8.8 | 53.6 | 0.1 | 0.2 | 0.1 |
| Shift conversion step exports | 54.0 | 0.8 | 44.4 | 0.3 | 0.2 | 0.2 | 0.1 |
Embodiment 3
As shown in Figure 6, the unstripped gas temperature from certain gasifying powder coal device (pot destroying process) is 170 DEG C, and pressure is 3.7MPaG, and carbon monoxide butt volume content is 64.1%.First unstripped gas is separated the moisture carried secretly through feed gas separator 1, then remove the harmful dust of catalyzer and toxic substance through unstripped gas strainer 2, enter after the shell side that unstripped gas after filtration enters air cooling shift-converter 3 is preheated to 200 DEG C in 1# water-cooled shift-converter 4 (being floating head type water-cooled shift-converter in the present embodiment) and carry out transformationreation, controlling temperature of reaction is 270 DEG C, medium pressure boiler feedwater enters in 1# water-cooled shift-converter 4 in bottom, in middle pressure drum 5, by by-product middle pressure steam, (pressure is 4.2MpaG, temperature is 255 DEG C) remove the reaction heat of transformationreation, the conversion gas going out 1# water-cooled shift-converter 4 fills into oiler feed and/or 1# floating head type (or board-like) water-cooled shift-converter institute's producing steam and part and supplies middle pressure steam adjustment water-gas ratio to be 0.43 outward.After enter in 2# water-cooled shift-converter 13 (being floating head type water-cooled shift-converter in the present embodiment) and proceed transformationreation, controlling temperature of reaction is 220 DEG C, by drum 14 by-product low-pressure steam, (pressure is 1.6MpaG, temperature is 205 DEG C) remove the reaction heat of 2# water-cooled shift-converter 13, the conversion gas going out 2# water-cooled shift-converter 13 enters in air cooling shift-converter 3 tube side and proceeds transformationreation, controlling temperature of reaction is 200 DEG C, go out the conversion gas of air cooling shift-converter 3 through Low Pressure Waste Heat Boiler 7, demineralized-water preheater 8 reclaims after heat is cooled to 80 DEG C and enters 1# conversion gas separator 9 separating and condensing liquid, the conversion gas going out 1# conversion gas separator 9 is lowered the temperature through conversion gas water cooler 10 and 2# conversion gas separator 11 successively and enters lower procedure after separating and condensing liquid.Adopt the present invention can every kNm
3unstripped gas, can by-product 116kg high-quality middle pressure steam, and systemic resistance can decline 1/3, and generating cost of investment can reduce by 1/4, and the gas composition before and after present invention process conversion is as shown in Table 3 below:
The gas composition of shift conversion step is passed in and out in table 3 embodiment 3
| Each component molar mark (%) | H2 | CO | CO2 | H2O | H2S | N2 | Ar |
| Shift conversion step entrance | 17.9 | 49.4 | 8.4 | 22.9 | 0.2 | 1.0 | 0.1 |
| Shift conversion step exports | 52.4 | 1.3 | 44.7 | 0.3 | 0.2 | 1.0 | 0.1 |
Claims (17)
1. a high-concentration carbon monoxide isothermal conversion process, it is characterized in that, the unstripped gas containing high-concentration carbon monoxide from upstream is first separated the moisture carried secretly through feed gas separator, then after unstripped gas metre filter dry linting dirt and toxic substance, gas enters the shell side preheating of air cooling shift-converter, unstripped gas after preheating enters 1# water-cooled shift-converter to carry out transformationreation and utilizes drum byproduct steam to remove the reaction heat of transformationreation, the unstripped gas that the conversion gas loopback going out 1# water-cooled shift-converter enters in the tube side of described air cooling shift-converter in preheating shell side is removed reaction heat and proceeds transformationreation, the conversion gas going out air cooling shift-converter reclaims heat further, lower procedure is entered after isolating phlegma.
2. high-concentration carbon monoxide isothermal conversion process as claimed in claim 1, it is characterized in that, described go out air cooling shift-converter conversion gas adjustment water to steam ratio after send into adiabatic shift-converter, the conversion gas going out adiabatic shift-converter reclaims heat more further, isolate phlegma after enter lower procedure.
3. high-concentration carbon monoxide isothermal conversion process as claimed in claim 1, it is characterized in that, the conversion gas of the described 1# of going out water-cooled shift-converter first carries out transformationreation further through 2# water-cooled shift-converter and utilizes drum byproduct steam to remove the reaction heat of transformationreation, and the conversion gas loopback going out 2# water-cooled shift-converter enters the tube side of described air cooling shift-converter.
4. high-concentration carbon monoxide isothermal conversion process as claimed in claim 1, it is characterized in that, the described carbon monoxide butt volume content contained in the unstripped gas of high-concentration carbon monoxide from upstream is 40 ~ 90%, and water vapor/dry gas volume range is 0.2 ~ 1.6 pressure range is 3.0 ~ 8.7MPaG.
5. high-concentration carbon monoxide isothermal conversion process as claimed in claim 1, it is characterized in that, after the preheating of air cooling shift-converter, unstripped gas temperature range is 200 ~ 290 DEG C.
6. high-concentration carbon monoxide isothermal conversion process as claimed in claim 5, it is characterized in that, the hot(test)-spot temperature scope that described water-cooled shift-converter high temperature moves hot-zone is 180 ~ 350 DEG C, and by-product middle pressure steam pressure range is 0.5 ~ 6.0MPaG.
7. the high-concentration carbon monoxide isothermal conversion process as described in any one of claim 1-6, is characterized in that, described water-cooled shift-converter is floating head type water-cooled shift-converter or board-like water-cooled shift-converter.
8. high-concentration carbon monoxide isothermal conversion process as claimed in claim 7, it is characterized in that, described floating head type water-cooled shift-converter comprises housing, is positioned at the upper tube box of housing epimere, the lower tube box of the middle cylinder in stage casing and hypomere, the heat transfer tube that many two ends are communicated with upper tube box and lower tube box is respectively provided with in described middle cylinder, transformation catalyst is filled with in described heat transfer tube, inert ceramic balls is filled with in described lower tube box, and described lower tube box and housing bottom have gap, described gap is communicated with middle cylinder; Vertical centering control space bar is provided with in described upper tube box, the raw material gas inlet of described case top communicates with the side of central dividing plate in upper tube box, the conversion gas outlet of described case top communicates with the side of central dividing plate in upper tube box, and described middle cylinder is provided with feedwater import and vapour outlet.
9. high-concentration carbon monoxide isothermal conversion process as claimed in claim 7, it is characterized in that, described board-like water-cooled shift-converter comprises housing, be positioned at the upper tube box of housing epimere, the middle cylinder in stage casing and the lower tube box of hypomere, the axis of described middle cylinder is provided with pipe core, pipe core periphery is provided with the plate package of annular, described plate package is made up of the radial heat exchanger plates that arranges of several piece, transformation catalyst is filled with in gap between adjacent heat exchanger plates, there is between described plate package and housing gas collection annular space, described gas collection annular space successively with upper tube box and the conversion gas outlet being positioned at case top, described pipe core tube wall arranges gas distribution holes, and the lower end of described pipe core is communicated with the raw material gas inlet of housing bottom, the lower end of described plate package and the feedwater inlet communication of housing bottom, upper end is communicated with the vapour outlet of case top.
10. high-concentration carbon monoxide isothermal conversion process as claimed in claim 9, is characterized in that also having inside clearance between described pipe core and plate package, be filled with transformation catalyst in inside clearance.
11. 1 kinds of high-concentration carbon monoxide isothermal transformation systems, it is characterized in that, comprise the feed gas separator, unstripped gas strainer, the shell side of air cooling shift-converter, 1# water-cooled shift-converter, the tube side of air cooling shift-converter and the cooling recovery system that connect successively; Described 1# water-cooled shift-converter is used for byproduct steam with drum.
12. high-concentration carbon monoxide isothermal transformation systems as claimed in claim 11, is characterized in that, shell side or the tube side menopause thermal conversion reactor of described air cooling shift-converter are connected with cooling recovery system.
13. high-concentration carbon monoxide isothermal transformation systems as claimed in claim 11, it is characterized in that, the shell side of described air cooling shift-converter is connected with the tube side of air cooling shift-converter through 1# water-cooled shift-converter, 2# water-cooled shift-converter successively, and described 2# water-cooled shift-converter is used for byproduct steam with drum.
14., as any one of claim 11-13 high-concentration carbon monoxide isothermal transformation system, comprise and it is characterized in that, described water-cooled shift-converter is floating head type water-cooled shift-converter or board-like water-cooled shift-converter.
15. high-concentration carbon monoxide isothermal transformation systems as claimed in claim 14, it is characterized in that, described floating head type water-cooled shift-converter comprises housing, is positioned at the upper tube box of housing epimere, the lower tube box of the middle cylinder in stage casing and hypomere, the heat transfer tube that many two ends are communicated with upper tube box and lower tube box is respectively provided with in described middle cylinder, transformation catalyst is filled with in described heat transfer tube, inert ceramic balls is filled with in described lower tube box, and described lower tube box and housing bottom have gap, described gap is communicated with middle cylinder; Vertical centering control space bar is provided with in described upper tube box, the raw material gas inlet of described case top communicates with the side of central dividing plate in upper tube box, the conversion gas outlet of described case top communicates with the side of central dividing plate in upper tube box, and described middle cylinder is provided with feedwater import and vapour outlet.
16. high-concentration carbon monoxide isothermal transformation systems as claimed in claim 14, it is characterized in that, described board-like water-cooled shift-converter comprises housing, be positioned at the upper tube box of housing epimere, the middle cylinder in stage casing and the lower tube box of hypomere, the axis of described middle cylinder is provided with pipe core, pipe core periphery is provided with the plate package of annular, described plate package is made up of the radial heat exchanger plates that arranges of several piece, transformation catalyst is filled with in gap between adjacent heat exchanger plates, there is between described plate package and housing gas collection annular space, described gas collection annular space successively with upper tube box and the conversion gas outlet being positioned at case top, described pipe core tube wall arranges gas distribution holes, and the lower end of described pipe core is communicated with the raw material gas inlet of housing bottom, the lower end of described plate package and the feedwater inlet communication of housing bottom, upper end is communicated with the vapour outlet of case top.
17. high-concentration carbon monoxide isothermal transformation systems as claimed in claim 16, is characterized in that also having inside clearance between described pipe core and plate package, be filled with transformation catalyst in inside clearance.
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105692550A (en) * | 2016-02-04 | 2016-06-22 | 中国五环工程有限公司 | Sulfur-phobic process for deeply transforming calcium carbide tail gas |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203568842U (en) * | 2013-09-13 | 2014-04-30 | 杭州林达化工技术工程有限公司 | Combined conversion device for synthesized gas CO |
| CN104150439A (en) * | 2014-07-21 | 2014-11-19 | 中国五环工程有限公司 | Carbon monoxide shifting process |
| CN204454563U (en) * | 2015-03-11 | 2015-07-08 | 中国五环工程有限公司 | High-concentration carbon monoxide isothermal transformation system |
-
2015
- 2015-03-11 CN CN201510107191.6A patent/CN104709875A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN203568842U (en) * | 2013-09-13 | 2014-04-30 | 杭州林达化工技术工程有限公司 | Combined conversion device for synthesized gas CO |
| CN104150439A (en) * | 2014-07-21 | 2014-11-19 | 中国五环工程有限公司 | Carbon monoxide shifting process |
| CN204454563U (en) * | 2015-03-11 | 2015-07-08 | 中国五环工程有限公司 | High-concentration carbon monoxide isothermal transformation system |
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