CN102888252B - Saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology - Google Patents
Saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology Download PDFInfo
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Abstract
The invention relates to saturation tower/isothermal furnace series/heat isolation furnace CO transformation technology, which comprises the following steps: feeding gas-liquid-separated crude gas into a saturation tower after removing impurity from the crude gas; completing the saturation tower with medium-pressure overheat steam from a pipe network after increasing humidity and temperature of the interior of the saturation tower; increasing the temperature and the humidity again; dividing into two strands, namely a first strand and a second strand, wherein the volume of the first strand is equal to 20-40% of the total volume; feeding the first strand into an isothermal transformation furnace so as to process depth transformation reaction; mixing transformed mixing gas of the isothermal transformation furnace with the second strand of the crude gas so as to feed into a gas-liquid mixer; after increasing the humidity of the medium-pressure boiler water from a boundary area so as to feed into a first heat isolating transformation furnace, and continuously processing the transformation reaction. Compared with the prior art, saturation tower series/isothermal furnace CO transformation technology solves a series of problems of long saturation hot water tower high moisture rate CO transformation technology procedure, too many heat isolation reaction grade, large system pressure drop, high equipment investment, easy over-temperature transformation furnace, short catalyst service life and the like.
Description
Technical field
The present invention relates to a kind of CO conversion process, specifically refer to a kind of saturator constant-temperature oven string heat insulation furnace CO conversion process.
Background technology
China has successively introduced the large-scale coal chemical engineering equipment that more than ten covers adopt Shell Coal Gasification techniques the beginning of this century, and this technology requires to ature of coal that in low, synthetic gas, active principle is high, working cost is low and environmental friendliness.The crude synthesis gas that Shell Coal Gasification generates adopts waste heat boiler cooling, and in crude synthesis gas, CO butt volume content is up to more than 60%, and water vapour volume content is less than 20% simultaneously, and crude synthesis gas has the low and high distinguishing feature of CO content of water vapour content.
China is when introducing Shell Coal Gasification technology, and this technology commercial operation only limits to use the crude synthesis gas gas combustion-gas vapor combined cycle device after purifying, and does not need to arrange CO shift conversion step.But when being carried out to the devices such as supporting synthetic ammonia, hydrogen manufacturing, synthesizing methanol for gas making, Shell Coal Gasification technology just faces a high concentration CO converter technique difficult problem.So the introduction of Shell Coal Gasification technology, has also promoted the development and progress of China's high concentration CO converter technique simultaneously greatly.
CO conversion be water vapour and CO etc. mole strong exothermal reaction, generate carbonic acid gas and hydrogen.The crude synthesis gas generating for different Coal Gasification Technology, the chemical reaction process of shift conversion step is all identical, but shift process need to design targetedly according to the feature of crude synthesis gas.The crude synthesis gas generating for Technology of Shell Coal Gasification, when shift conversion step carries out CO transformationreation, the Focal point and difficult point of shift process design is the bed temperature of effectively controlling CO transformationreation, extends the work-ing life of transformation catalyst.
At present domesticly in the design of high concentration CO shift process, generally adopt adiabatic shift converter, in view of CO, transformationreation is strong exothermic process, and existing conversion process process organization all adopts multistage insulation shift converter to react, the intersegmental heat of reaction of removing.The series of problems such as therefore, cause that existing high concentration CO converter technique shift converter is many, calorific loss is large, the easy overtemperature of the first shift converter, catalyst life are short.
As the application number mono-kind high water-gas ratio saturated hot-water tower share split CO conversion process > > of the disclosed < < of Chinese invention patent application that is 201110260539.7, this high water-gas ratio saturated hot-water tower share split CO conversion process all adopts adiabatic shift converter, reaction order is more, system pressure drop is large, and the rear system energy consumption that compression consumes to conversion gas is high; Especially the first shift converter adopts adiabatic shift converter, and the conversion gas of High Temperature High Pressure will be born in furnace wall, causes equipment wall thickness large, and facility investment is high; And the first shift converter catalyzer moves for a long time under comparatively high temps, running environment is harsh, and catalyst life is shorter, changes frequently, and process cost is high; Meanwhile, the first shift converter adopts heat insulation furnace, and temperature is controlled more difficult, easily occurs overtemperatute, and to shift conversion step, safe operation causes disadvantageous effect, has potential safety hazard.Because adiabatic reaction progression is many, complicated to catalyst vulcanization process when shift conversion step is driven, drive length consuming time, expense of shift conversion step is high.
Summary of the invention
Technical problem to be solved by this invention is that the present situation for prior art provides a kind of saturator constant-temperature oven string heat insulation furnace CO conversion process, solving existing saturated hot-water tower height water-gas ratio CO conversion process long flow path, adiabatic reaction progression is more, system pressure drop is large, the series of problems such as facility investment is high, the easy overtemperature of shift converter, catalyst life are short.
The present invention solves the problems of the technologies described above adopted technical scheme: this saturator constant-temperature oven string heat insulation furnace CO conversion process, is characterized in that comprising the steps:
First the raw gas of being sent here by coal gasification workshop section is sent into gas-liquid separator and is carried out liquid phase separation;
By gas-liquid separator top raw gas out, send into detoxification groove and remove after the impurity in raw gas, send in saturator;
Raw gas is sent into saturator by the bottom of saturator, and the process recycled water of sending from hot-water tower bottom is through behind heat exchange to 190～210 ℃, by the top of saturator, enters saturator, and countercurrent heat-transfer mass transfer is carried out in two bursts of logistics in saturator; The process recycled water of being sent by saturator bottom, after the pressurization of saturator column bottoms pump, is back to hot-water tower;
Raw gas is humidified after temperature raising in saturator, by saturator top, sent, after heat exchange temperature raising, fully mixed with the middle pressure superheated vapour from pipe network again, temperature raising humidification, is divided into two strands subsequently again, first strand and second strand, the volume of first strand is that 20～40%, first strand of cumulative volume sent into isothermal shift converter and carried out depth conversion reaction, and water/dry gas mol ratio of controlling the raw gas that enters isothermal shift converter is 0.9～1.2,250～280 ℃ of temperature;
After the conversion gas mixture that goes out isothermal shift converter mixes with second strand of raw gas, enter in gas liquid mixer, after medium pressure boiler water humidification by mixing of gas from battery limit (BL), send into the first adiabatic shift converter and continue transformationreation, control the mixing air water/dry gas mol ratio that enters the first adiabatic shift converter and be 0.55～0.65,230～250 ℃ of temperature;
A change gas mixture that goes out the first adiabatic shift converter is cooled to after 200～220 ℃ through heat exchange, sends into the second adiabatic shift converter and proceeds transformationreation;
The two change gas mixtures that go out the second adiabatic shift converter are cooled to after 180～200 ℃ through heat exchange, by hot-water tower bottom, sent in hot-water tower, carry out countercurrent mass transfer heat transfer with the process recycled water entering from hot-water tower middle part, on the top of hot-water tower, spray into purification process phlegma and medium pressure boiler water, the mol ratio of process recycled water and purification and condensation liquid and medium pressure boiler water is 7.0～10.0, carry out countercurrent mass transfer heat transfer, conversion gas mixture after hot-water tower top is lowered the temperature, obtains process recycled water in hot-water tower bottom.
The consumption of the above-mentioned process recycled water entering from hot-water tower middle part is 4.0～6.0 with the mol ratio that enters the butt raw gas of gas-liquid separator.
The isothermal shift converter using in above-mentioned technique can be used any one isothermal shift converter of the prior art.Preferably, described isothermal shift converter comprises body of heater, in described body of heater, be provided with the heat-exchanging tube bundle being formed by many heat transfer tubes, described body of heater top is provided with reaction gas entrance and inspection manhole, the upper portion side wall of body of heater is provided with cooling water outlet, bottom of furnace body is provided with conversion gas outlet and cooling water inlet, and the center of described body of heater is provided with gas trap; It is characterized in that described body of heater comprises top first paragraph body of heater and the bottom second segment body of heater removably connecting, the cylindrical shell that is provided with tubular structure in described second segment body of heater forms the gas distributor of Reaktionsofen, the upper/lower terminal of this cylindrical shell is connected on upper tubesheet and lower tubesheet, the inwall interval of described upper tubesheet and described body of heater is gapped, the be tightly connected internal perisporium of described body of heater of the periphery of described lower tubesheet; The top of described upper tubesheet is provided with upper cover, the below of described lower tubesheet is provided with lower cover, described heat-exchanging tube bundle is arranged in described cylindrical shell, and described in each, two ends of heat transfer tube are separately fixed on described upper and lower tube sheet and are communicated with respectively the cavity consisting of upper cover and upper tubesheet, lower cover and lower tubesheet; The upper end of described gas trap connects described upper tubesheet, and the lower end of gas trap is positioned at the cavity of lower cover and described bottom of furnace body formation through described lower cover; Described upper cover is provided with cooling water outlet, and this cooling water outlet connects described cooling water outlet by rising pipe, and described rising pipe comprises the two portions that are detachably connected; Described lower cover is provided with cooling water inlet, and this cooling water outlet connects described cooling water inlet by water inlet pipe, and described water inlet pipe comprises the two portions that are detachably connected; On described gas distributor, be provided with evenly and at intervals a plurality of pores.
Preferably, between first paragraph body of heater and second segment body of heater, can connect by flange, body of heater can be supported on vertical placement on skirt.
In order to facilitate the filling of catalyzer, described gas distributor can comprise a plurality of segmentations that are detachably connected, and each segmentation is removably connected and formed by two semicircular cylinders again.
Further, distributing homogeneity when guaranteeing that gas enters beds, described in each, segmentation includes outer cylinder body and is set in the inner barrel in described outer cylinder body, the outer cylinder body formation urceolus that is detachably connected described in each, described in each, inner barrel is detachably connected to form and is set in the inner core in described urceolus, and described outer cylinder body and described inner barrel interval gapped.Inner barrel plays the effect of quadratic distribution to reaction gas.
Preferably, the density of the pore described in such scheme on inner core is greater than described urceolus, and the aperture of the pore on described endoporus is less than or equal to 3mm.
Consider the settlement issues of catalyzer in production process, described gas distributor is not offered pore near described upper tubesheet 100mm with interior position, to prevent that the reaction gas that catalyst sedimentation causes from refluxing and short circuit.
In above-mentioned each scheme, the part that described gas trap exposes to described lower cover is horn-like, and the middle part of described gas trap lower end port is provided with baffle plate, between the periphery of described baffle plate and described gas trap lower end port, be separated with the space of flowing out for synthetic gas.The Diffusion of gas stream that this structure can be used gas trap flows, avoided air-flow directly to impact the impact injury that body of heater lower cover causes body of heater, and short stay in the cavity of the gas that can use gas trap between lower cover and body of heater, guaranteed the inside and outside pressure equilibrium of lower cover, and can make body of heater relative even with the envrionment temperature inside and outside cylindrical shell and lower cover, can not produce stress concentration.
Between baffle plate and gas trap, can be welded to connect by bearing rib, and strengthen by gusset.Preferably, collection tube top is near not perforate in upper tubesheet 100mm, to prevent that the catalyst sedimentation gas that induces reaction from refluxing and short circuit.
Consider the thermal expansion of gas trap, can on the lower surface of described upper tubesheet, be provided with adapter sleeve, it is interior and gapped with described upper tubesheet interval that the upper end of described gas trap is positioned at this adapter sleeve, and this gap can the thermal expansion of supplied gas collector.
Consider the thermal expansion of Reaktionsofen inside, can on described rising pipe, expansion joint be set, to solve internal-response entire system thermal expansion problem.
The mode of connection of lower tubesheet and body of heater can have multiple, preferably, can on the perisporium of described body of heater, be provided with retaining ring, and the upper surface of this retaining ring is provided with annular recesses; Described lower tubesheet is provided with the annular lug suitable with described groove, and described projection is contained in described groove, and is provided with sealing-ring between projection and groove.
The internal perisporium of described body of heater is provided with many group strongbacks, every group of strongback comprises left and right spaced left strongback and right strongback, accordingly, the sidewall of described upper tubesheet is provided with polylith preset pieces, and described in each, preset pieces is contained between corresponding left strongback and right strongback.
Preferably, on upper tubesheet, be welded with 4 preset piecess, coordinate radial location with 4 groups of strongbacks that are welded on inboard wall of furnace body, to guarantee the Fast Installation of inner tube bank and being sealed and matched of described tongue and groove.
Isothermal shift converter in such scheme adopts overall diameter to Z-type structure on the whole, reaction gas upper entering and lower leaving, it between heat transfer tube, is beds, in pipe, walk recirculated cooling water, water coolant absorbs conversion heat, the requirement of strength shifting out according to reaction heat, cooling water circulation process can be that natural circulation can be also pump circulation, recirculated cooling water downstream can arrange drum byproduct steam recovery waste heat.By the controlled circulation water yield, maintain the constant of transformationreation temperature.
Compared with prior art, the invention has the advantages that:
1, depth conversion adopts constant-temperature oven, and system pressure drop is little, and after saving, the compression work of system, has reduced energy consumption.
2, isothermal shift converter service temperature is low, and catalyzer running environment is gentle, catalyzer long service life, and shift conversion step is easily realized long-period stable operation.
3, the self-produced steam of shift conversion step, after heat insulation furnace is overheated, all for the transformationreation of self, has saved part sect heat-exchanger and energy recovery equipment, has simplified technical process, has saved facility investment.
4, the isothermal shift converter using in preferred version, utilize overall diameter to the little feature of gas reactor pressure drop, inner reactive system is adopted to equipment self-weight sealing, and water coolant inlet/outlet pipe all adopts flange to be connected with body of heater, internal-response system can wholely be extracted out, and the quick handling that the demountable structure of gas distributor is catalyzer in addition and the checking maintenance of post facility facilitate.
5, the setting of internal-response systemic circulation cooling water outlet expansion joint and location, gas-collecting pipe top cover cylinder gap, take into full account high temperature stress operating mode, solved the overall thermal expansion of internal-response system and the differential expansion of gas-collecting pipe, be conducive to stable equipment operation and increase the service life.
6, isothermal shift converter adopts full radial structure, and circulation area is large, and bed resistance is little, and pressure drop is little.Gas distributor adopts inside and outside barrel structure, to reaction gas quadratic distribution, make gas distribution more even, be conducive to improve transformation efficiency, simultaneously, take into full account catalyst sedimentation problem, at gas distributor and collection tube top, be all reserved with not aperture area of 100mm, can prevent backflow, the short circuit of conversion gas.
7, the present invention adopts shell and tube-type reactor, and between catalyst loading heat transfer tube, reaction bed temperature is stable, and the life-span is long, and can increase CO conversion gas treatment capacity by increasing gas distributor hop count mode, is conducive to the maximization of device.
Accompanying drawing explanation
Fig. 1 is the floor map of isothermal shift converter assembly structure in the embodiment of the present invention;
Fig. 2 is upper tubesheet location schematic diagram in the embodiment of the present invention;
Fig. 3 is lower tubesheet location schematic diagram in the embodiment of the present invention;
Fig. 4 is gas distributor structural representation in the embodiment of the present invention;
Fig. 5 be along A-A in Fig. 4 to sectional view.
Fig. 6 is gas trap structural representation in the embodiment of the present invention;
Fig. 7 is the process flow diagram of the embodiment of the present invention.
Embodiment
Following accompanying drawing embodiment is in conjunction with adopting Shell Coal Gasification gas making to produce the typical chemical fertilizer plant of 520,000 tons/year of urea of 300,000 tons/year of synthetic ammonia, the present invention being described in further detail.
As shown in Figures 1 to 6, the isothermal shift converter 5 using in the present embodiment comprises:
Body of heater 51, comprise main body 511, upper cover 515 and lower cover 512, between main body 511 and upper cover 515, be provided with transition section 518, between main body 511 and transition section 518, adopt flange to removably connect, between main body 511 and lower cover 512, upper cover 515 and transition section 518, be and be welded to connect.Upper cover 515 tops are provided with reaction gas entrance 516 and top inspection manhole 517, transition section 518 sidewalls are provided with circulating cooling water out 514, main body 511 lower end sidewalls are provided with bottom inspection manhole 513, lower cover bottom is provided with cooling water inlet 519 and conversion gas outlet 5110, body of heater 51 bottoms are seated on skirt 56, and skirt 56 is the base for supporting of this isothermal shift converter.
Internal-response system, is mainly comprised of parts such as heat-exchanging tube bundle 52, gas distributor 53, gas-collecting pipe 54, oval upper cover 526 and spherical lower covers 522.Upper cover 526 tops are provided with the cooling water outlet pipe 525 being connected with above-mentioned circulating cooling water out 514, and the middle part of rising pipe vertical portion is provided with expansion joint, and the effect of expansion joint is to eliminate the stress that rising pipe thermal expansion produces; The horizontal component of rising pipe is divided into two sections, and these two sections are detachably connected by flange.Circular lower cover 522 is provided with the internal overhaul manhole 521 communicating with above-mentioned bottom inspection manhole 513 and the recirculated cooling water import pipeline section being connected with above-mentioned cooling water inlet 519 flanges.Internal-response system also comprises upper tubesheet 527 and lower tubesheet 5210, and upper tubesheet 527 relies on four preset piecess 5211 that are welded on upper tubesheet and is welded on four groups of strongbacks, the 5212 cooperation radial locations in equipment barrel, guarantees axial displacement.Every group of strongback comprises the spaced left strongback in left and right and right strongback, and preset pieces is between the left and right strongback of correspondence.On the internal perisporium of main body 511, be welded with retaining ring 5215, the upper surface of this retaining ring is provided with annular recesses; The bottom of retaining ring is provided with 16 uniform bearing ribs 5213, and these bearing ribs are welded on main body 511 and retaining ring 5215, to strengthen the load-bearing of retaining ring; Eight jackscrews 5214 are also set on retaining ring, facilitate the dismounting of reactive system.Lower tubesheet 5210 is provided with the annular lug suitable with groove, and projection is contained in groove, and is provided with sealing-ring 5217 between projection and groove.Between the inwall of the upper surface of retaining ring and main body 511, be also welded with four locating cones 5216, locating cone inclination at 45 °; The effect of locating cone is mainly used for lower tubesheet to locate.On upper and lower tube sheet, be equipped with the pore plugging for each heat transfer tube 528, the two ends of each heat transfer tube are plugged in respectively formation heat-exchanging tube bundle in corresponding pore, between each heat transfer tube, in gap, be filled with catalyzer, the middle part of heat-exchanging tube bundle is provided with a plurality of for supporting the strut member 529 of heat-exchanging tube bundle.
As shown in Figure 7, the CO conversion process of the present embodiment is as follows:
160 ℃ of the raw gas temperature of the saturated water vapour of being sent here by coal gasification workshop section, pressure 3.7Mpa, with pipeline by raw gas from gasification workshop section delivers to the process of conversion section due to calorific loss, a small amount of water vapour in raw gas generation phlegma that can be condensed, raw gas and lime set coexist and can cause corrosion and the vibrations of pipeline and equipment in tubing system, so first raw gas needs lime set wherein to separate.
Therefore the present embodiment is first sent into raw gas gas-liquid separator 1, and liquid flows out from the outlet at bottom of gas-liquid separator 1.From the gas-liquid separator 1 top raw gas after separatory out, send into detoxification groove 2 and remove the impurity such as ash content in raw gas and heavy metal, then enter the bottom of saturator 3.
Raw gas carries out heat and mass with the process recycled water counter current contact that is 190 ℃～200 ℃ from hot-water tower 13 temperature in saturator 3, go out the process recycled water of saturator 3 bottoms through 4 pressurizations of saturator column bottoms pump, send hot-water tower 13 heating cycle use again back to, extract 3%～8% of technological cycle water inventory simultaneously out and go rear system to carry out stripping, prevent that objectionable impurities from accumulating in technological cycle water system.Crude synthesis gas is humidified temperature raising in saturator 3, temperature reaches 185 ℃～190 ℃, water/dry gas mol ratio is 0.58～0.62, through crude synthesis gas well heater 9, lift temperature to 205 ℃～210 ℃, sneak into the 4.0Mpa from methanation and steam pipe system, in 400 ℃, press superheated vapour, regulate that crude synthesis gas water/dry gas mol ratio is 0.9～1.1, temperature is to be divided into two strands after 250 ℃, first strand and second strand, the volumetric flow rate of first strand is 30%, the first strand of total flux and enters and isothermal shift converter 5, carry out deep reaction from isothermal shift converter entrance 516.Water coolant in the heat transfer tube 528 that reaction liberated heat is arranged in reactor absorbs, after the heat absorption of part water coolant, become vapour phase, gas-liquid two-phase returns in drum 6 by circulating cooling water out 514, in drum 6, carry out liquid phase separation, it is overheated that isolated gas phase middle pressure steam demethanization operation is carried out, isolated liquid phase relies on gravity to flow out together with the medium pressure boiler water filling into from drum 6 bottoms, by cooling water inlet 519, reenters the interior absorption transformationreation of isothermal shift converter heat transfer tube 528 institute liberated heat.Interior the produced gas-liquid two-phase fluid of isothermal shift converter heat transfer tube 528 and the water coolant reentering complete circulation by thermal siphon, have saved power consumption.
From the conversion gas outlet 5110 isothermal conversion gas temperature that go out isothermal shift converter 5, be about 260 ℃, CO butt volume content is about 2.0%～3.0%, isothermal conversion gas mixes with another strand of crude synthesis gas, enter in gas liquid mixer 7, fully mix with the 4.0Mpa from battery limit (BL), 130 ℃ of medium pressure boiler feedwater, carry out Quench humidification, regulate mixture temperature to 230 ℃, water/dry gas mol ratio is 0.58～0.60, enters the adiabatic shift converter 8 of 1# and continues transformationreation.
A change mixture temperature that goes out the adiabatic shift converter 8 of 1# is about 350 ℃～355 ℃, and CO butt volume content is about 5.0%～5.5%.One change gas mixture enters crude synthesis gas well heater 9 successively, conversion gas water cooler 10 is cooled to 200 ℃ with crude synthesis gas, process recycled water heat exchange, enters the adiabatic shift converter 11 of 2# and proceeds transformationreation.
The two change mixture temperatures that go out the adiabatic shift converter 11 of 2# are about 230 ℃～235 ℃, CO butt volume content is about 1.0%～1.5%, two change gas mixtures enter conversion gas aftercooler 12 and are cooled to 185 ℃ with the process recycled water heat exchange from hot-water tower 13, enter hot-water tower 13 bottoms.
Two become gas mixtures at hot-water tower 13 middle parts and process recycled water countercurrent heat-transfer mass transfer from saturator 3, at hot-water tower 13 tops and process condensate from rear system and supplementary medium pressure boiler feedwater countercurrent heat-transfer mass transfer.The technological cycle water temp of being sent by hot-water tower 13 bottoms is 167 ℃, through 14 pressurizations of hot-water tower column bottoms pump, lifts temperature to 195 ℃ successively through conversion gas aftercooler 12 and conversion gas water cooler 10, sends into saturator 3 tops.The conversion gas temperature of being sent by hot-water tower 13 tops is about 160 ℃, sends into downstream section and reclaims low temperature exhaust heat.
Isothermal shift converter 5 is removed reaction heat by oiler feed mode, while by-product pressure 4.0Mpa, the middle pressure saturation steam that temperature is 251 ℃, the middle pressure saturation steam of by-product enters the separated liquid phase of drum 6, the middle pressure saturation steam demethanization operation that drum 6 tops are sent is superheated to 400 ℃, then become in advance in gas mixture with the supplementary steam injection as transformationreation together with the middle pressure superheated vapour of pipe network, the liquid phase of drum 6 bottoms is entered in isothermal shift converter 5 and is recycled by thermal siphon mode, by battery limit (BL), to the interior supplementary medium pressure boiler of drum 6, fed water simultaneously, to maintain the stable of liquid level of steam drum.
comparative example
For adopting Shell Coal Gasification gas making to produce the typical chemical fertilizer plant of 520,000 tons/year of urea of 300,000 tons/year of synthetic ammonia, enter effective gas (H of conversion section
2+ CO) be approximately 85000Nm
3/ h contrasts in Table 1 a kind of high water-gas ratio saturated hot-water tower share split CO conversion process and a kind of saturator isothermal string heat insulation furnace CO conversion process significant parameter under this benchmark.
Table 1
As can be seen from Table 1, in the saturator string constant-temperature oven CO conversion process that the present embodiment provides, shift converter quantity is few, and loaded catalyst is little, hot(test)-spot temperature is low and system pressure drop is less.Can reduce equipment and the catalyzer investment cost of shift conversion step.The low effectively extending catalyst of hot(test)-spot temperature work-ing life, system pressure drop I is significantly to reduce the compression work consumption of rear system, and both all can play the object of saving process cost.
Claims (10)
1. a saturator constant-temperature oven string heat insulation furnace CO conversion process, is characterized in that comprising the steps:
First the raw gas of being sent here by coal gasification workshop section is sent into gas-liquid separator and is carried out liquid phase separation;
By gas-liquid separator top raw gas out, send into detoxification groove and remove after the impurity in raw gas, send in saturator;
Raw gas is sent into saturator by the bottom of saturator, and the process recycled water of sending from hot-water tower bottom is through behind heat exchange to 190～210 ℃, by the top of saturator, enters saturator, and countercurrent heat-transfer mass transfer is carried out in two bursts of logistics in saturator; The process recycled water of being sent by saturator bottom, after the pressurization of saturator column bottoms pump, is back to hot-water tower;
Raw gas is humidified after temperature raising in saturator, by saturator top, sent, after heat exchange temperature raising, fully mixed with the middle pressure superheated vapour from pipe network again, temperature raising humidification, is divided into two strands subsequently again, first strand and second strand, the volume of first strand is that 20～40%, first strand of cumulative volume sent into isothermal shift converter and carried out depth conversion reaction, and water/dry gas mol ratio of controlling the raw gas that enters isothermal shift converter is 0.9～1.2,250～280 ℃ of temperature;
After the conversion gas mixture that goes out isothermal shift converter mixes with second strand of raw gas, enter in gas liquid mixer, after medium pressure boiler water humidification by mixing of gas from battery limit (BL), send into the first adiabatic shift converter and continue transformationreation, control the mixing air water/dry gas mol ratio that enters the first adiabatic shift converter and be 0.55～0.65,230～250 ℃ of temperature;
A change gas mixture that goes out the first adiabatic shift converter is cooled to after 200～220 ℃ through heat exchange, sends into the second adiabatic shift converter and proceeds transformationreation;
The two change gas mixtures that go out the second adiabatic shift converter are cooled to after 180～200 ℃ through heat exchange, by hot-water tower bottom, sent in hot-water tower, carry out countercurrent mass transfer heat transfer with the process recycled water entering from hot-water tower middle part, on the top of hot-water tower, spray into purification process phlegma and medium pressure boiler water, the mol ratio of process recycled water and purification and condensation liquid and medium pressure boiler water is 7.0～10.0, carry out countercurrent mass transfer heat transfer, conversion gas mixture after hot-water tower top is lowered the temperature, obtains process recycled water in hot-water tower bottom;
The consumption of the above-mentioned process recycled water entering from hot-water tower middle part is 4.0～6.0 with the mol ratio that enters the butt raw gas of gas-liquid separator.
2. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 1, it is characterized in that described isothermal shift converter comprises body of heater, in described body of heater, be provided with the heat-exchanging tube bundle being formed by many heat transfer tubes, described body of heater top is provided with reaction gas entrance and inspection manhole, the upper portion side wall of body of heater is provided with cooling water outlet, bottom of furnace body is provided with conversion gas outlet and cooling water inlet, and the center of described body of heater is provided with gas trap; It is characterized in that described body of heater comprises top first paragraph body of heater and the bottom second segment body of heater removably connecting, in described second segment body of heater, be provided with gas distributor, the upper/lower terminal of this gas distributor is connected on upper tubesheet and lower tubesheet, gapped between described upper tubesheet and the inwall of described body of heater, the be tightly connected internal perisporium of described body of heater of the periphery of described lower tubesheet; The top of described upper tubesheet is provided with upper cover, the below of described lower tubesheet is provided with lower cover, described heat-exchanging tube bundle is arranged in described gas distributor, and described in each, two ends of heat transfer tube are separately fixed on described upper and lower tube sheet and are communicated with respectively the cavity consisting of upper cover and upper tubesheet, lower cover and lower tubesheet; The upper end of described gas trap connects described upper tubesheet, and the lower end of gas trap is positioned at the cavity of lower cover and described bottom of furnace body formation through described lower cover; Described upper cover is provided with cooling water outlet, and this cooling water outlet connects the cooling water outlet in the described upper portion side wall that is located at body of heater by rising pipe, and described rising pipe comprises the two portions that are detachably connected; Described lower cover is provided with cooling water inlet, and this cooling water outlet connects the described cooling water inlet that is located at bottom of furnace body by water inlet pipe, and described water inlet pipe comprises the two portions that are detachably connected.
3. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 2, it is characterized in that described gas distributor comprises a plurality of segmentations that are detachably connected, and each segmentation is removably connected and is formed again by two semicircular cylinders.
4. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 3, it is characterized in that segmentation includes outer cylinder body and is set in the inner barrel in described outer cylinder body described in each, the outer cylinder body formation urceolus that is detachably connected described in each, described in each, inner barrel is detachably connected to form and is set in the inner core in described urceolus, and gapped between described outer cylinder body and described inner barrel.
5. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 4, the density that it is characterized in that the pore on described inner core is greater than described urceolus, and the aperture of the pore on described endoporus is less than or equal to 3mm.
6. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 5, is characterized in that described gas distributor and gas trap all do not offering pore near described upper tubesheet 100mm with interior position.
7. according to the saturator constant-temperature oven string heat insulation furnace CO conversion process described in the arbitrary claim of claim 2 to 6, it is characterized in that the part that described gas trap exposes to described lower cover is horn-like, and the middle part of described gas trap lower end port is provided with baffle plate, between the periphery of described baffle plate and described gas trap lower end port, be separated with the space of flowing out for synthetic gas.
8. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 7, is characterized in that the lower surface of described upper tubesheet is provided with adapter sleeve, the upper end of described gas trap be positioned in this adapter sleeve and and described upper tubesheet between gapped.
9. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 8, is characterized in that described rising pipe is provided with expansion joint.
10. saturator constant-temperature oven string heat insulation furnace CO conversion process according to claim 9, is characterized in that the perisporium of described body of heater is provided with retaining ring, and the upper surface of this retaining ring is provided with annular recesses; Described lower tubesheet is provided with the annular lug suitable with described groove, and described projection is contained in described groove, and is provided with sealing-ring between projection and groove; The internal perisporium of described body of heater is provided with many group strongbacks, every group of strongback comprises upper and lower spaced upper strongback and lower strongback, accordingly, the sidewall of described upper tubesheet is provided with polylith preset pieces, and described in each, preset pieces is contained between corresponding upper strongback and lower strongback.
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