CN102886230B - CO (carbon monoxide) conversion process adopting tandem isothermal furnaces of saturation tower - Google Patents
CO (carbon monoxide) conversion process adopting tandem isothermal furnaces of saturation tower Download PDFInfo
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Abstract
The invention relates to a CO (carbon monoxide) conversion process adopting the tandem isothermal furnaces of a saturation tower, which is characterized by comprising the following steps of: feeding the raw gas obtained by gas-liquid separation in the saturation tower after impurity removal, feeding the raw gas in an isothermal conversion furnace to perform a deep conversion reaction after humidifying and heating in the saturation tower, and feeding the conversion mixed gas output from the isothermal conversion furnace to a hot-water tower to perform heat exchange with process cooling water after heat exchange and cooling. In the preferable scheme, the structure of the isothermal conversion furnace used in the process is provided. Compared with the prior art, via the CO conversion process for the tandem isothermal furnaces of the saturation tower provided by the invention, a series of problems of long flow, multiple reaction orders, large system pressure drop, high equipment investment, easily-caused conversion furnace overtemperature, short catalyst life and the like of a CO conversion process with a high water-air ratio in the prior art are solved.
Description
Technical field
The present invention relates to a kind of CO conversion process, specifically refer to a kind of saturator string constant-temperature oven CO conversion process.
Background technology
Technology of Shell Coal Gasification requires to ature of coal that in low, synthesis gas, active principle is high, operating cost is low and environmental friendliness.China carrys out producing synthesis gas in the bed pulverized coal gasification technology that in succession introduced more than ten cover shell the beginning of this century.The cooling employing waste heat boiler of crude synthesis gas in this technology, in the crude synthesis gas of generation, CO butt volume content is up to more than 60%, and simultaneously steam volume content is less than 20%, and crude synthesis gas has the distinguishing features such as the low and CO content height of water vapour content.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 when Shell Coal Gasification technology transfer, also promoted greatly the development and progress of China's high concentration CO converter technique.
Shift conversion step be steam and CO etc. mole strong exothermal reaction, generate carbon dioxide and hydrogen.The crude synthesis gas generating for different Coal Gasification Technology, the chemical reaction process of downstream transforms operation 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, in the time that shift conversion step carries out CO transformationreation, the Focal point and difficult point of shift process design is bed temperature how effectively to control CO transformationreation, and service life, the minimizing that extends transformation catalyst converts sum of series equipment investment, reduce the Pressure Drop of shift conversion step and save middle pressure steam and power consumption.
At present domesticly in the design of high concentration CO shift process, generally adopt adiabatic change furnace, in view of CO, transformationreation is strong exothermic process, and existing conversion process process organization all adopts multistage insulation change furnace to react, the intersegmental heat of reaction of removing.Therefore, cause that the technological process of existing high concentration CO converter technique is long, system pressure drop is large, thermal loss is many, equipment investment is high, the series of problems such as the short and energy consumption of the easy overtemperature of change furnace, catalyst life is high.
Application number is that 201110260537.8 Chinese invention patent application discloses " a kind of saturated hot-water tower height WGR CO conversion process ", this saturated hot-water tower height WGR CO conversion process all adopts adiabatic change furnace, the order of reaction is more, system pressure drop is large, and the rear system energy consumption that compression consumes to conversion gas is high; Its change furnace all adopts adiabatic change furnace, and especially the first change furnace and the second change furnace adopt adiabatic change furnace, and the conversion gas of HTHP will be born in furnace wall, causes equipment wall thickness large, and equipment investment is high; The first change furnace catalyst moves under higher temperature, running environment harshness, and catalyst life is shorter, changes frequent operation expense high; The control of adiabatic change furnace temperature is more difficult, easily occurs overtemperatute, and to shift conversion step, safe operation causes adverse effect, has potential safety hazard.Meanwhile, because adiabatic reaction progression is many, when shift conversion step is driven, to catalyst vulcanization process complexity, drive length consuming time, expense of shift conversion step is high.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of saturator string constant-temperature oven CO conversion process for the present situation of prior art, solving high WGR CO conversion process long flow path in prior art, the series of problems such as the order of reaction is many, system pressure drop is large, equipment investment is high, the easy overtemperature of change furnace, catalyst life are short.
The present invention solves the problems of the technologies described above adopted technical scheme: this saturator string constant-temperature oven 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, isolates after liquid phase and sends in detoxification groove and remove the impurity in raw gas, sends into subsequently in saturator;
Raw gas is sent into saturator by the bottom of saturator, process recycled water heat exchange to 180～200 of sending DEG C, enters saturator by the top of saturator from hot-water tower bottom, 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, sent by saturator top, after middle pressure superheated steam humidification by mixing of gas temperature raising from pipe network, send into isothermal change furnace and carry out depth conversion reaction, control the water/dry gas mol ratio of raw gas that enters isothermal change furnace and be 1.0～1.2,250 DEG C of temperature; The air speed of controlling isothermal change furnace inner catalyst is 1000～3000, and the temperature rise of isothermal change furnace is 10 DEG C～20 DEG C; The conversion gas temperature that goes out isothermal change furnace is 250 DEG C～270 DEG C, and CO butt volume content is 1%～2%;
The conversion gaseous mixture that goes out isothermal change furnace is cooled to after 180～200 DEG C through heat exchange, send into hot-water tower by hot-water tower bottom, carry out countercurrent mass transfer heat transfer with the process recycled water entering from hot-water tower middle part, spray into process for purifying condensate liquid and medium-pressure boiler water on the top of hot-water tower, the mol ratio of described process recycled water and purification and condensation liquid sum and described medium-pressure boiler water is 7.0～10.0, carry out countercurrent mass transfer heat transfer, obtain the conversion gaseous mixture after cooling at hot-water tower top, obtain process recycled water in hot-water tower bottom.
The consumption of the above-mentioned process recycled water that enters hot-water tower from hot-water tower middle part is 4.0～6.0 with the mol ratio of the butt raw gas that enters gas-liquid separator.
The isothermal change furnace using in above-mentioned technique can use any one isothermal change furnace of the prior art.Preferably, described isothermal change furnace comprises body of heater, in described body of heater, be provided with the heat-exchanging tube bundle being formed by many heat exchanger 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 circulating cooling water out, bottom of furnace body is provided with conversion gas outlet and the first cooling water inlet, and the center of described body of heater is provided with gas collector; 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 reacting furnace, the upper/lower terminal of this cylindrical shell is connected on upper perforated plate and lower perforated plate, the inwall interval of described upper perforated plate and described body of heater is gapped, the be tightly connected internal perisporium of described body of heater of the periphery of described lower perforated plate; The top of described upper perforated plate is provided with upper cover, the below of described lower perforated plate is provided with low head, described heat-exchanging tube bundle is arranged in described cylindrical shell, and the two ends of each described heat exchanger tube are separately fixed on described upper and lower tube sheet and are communicated with respectively the cavity being made up of upper cover and upper perforated plate, low head and lower perforated plate; The upper end of described gas collector connects described upper perforated plate, and the lower end of gas collector is positioned at the cavity of low head and described bottom of furnace body formation through described low head; Described upper cover is provided with coolant outlet, and this coolant outlet connects described circulating cooling water out by outlet pipe, and described outlet pipe comprises the two parts that are detachably connected; Described low head is provided with the second cooling water inlet, and this second cooling water inlet connects the first described cooling water inlet by water inlet pipe, and described water inlet pipe comprises the two parts that are detachably connected; On described gas distributor, be provided with evenly and at intervals multiple pores.
Preferably, between first paragraph body of heater and second segment body of heater, can connect by flange, body of heater can be bearing in vertical placement on skirt.
In order to facilitate the filling of catalyst, described gas distributor can comprise the multiple segmentations that are detachably connected, and each segmentation is removably connected and formed by two semicircular cylinders again.
Further, distributing homogeneity when ensureing that gas enters beds, each described segmentation includes outer cylinder body and is set in the inner barrel in described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected to form and is set in 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 pore on described endoporus is less than or equal to 3mm.
Consider the settlement issues of catalyst in production process, described gas distributor is not offered pore near described upper perforated plate 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 collector exposes to described low head is horn-like, and the middle part of described gas collector lower end port is provided with baffle plate, between the periphery of described baffle plate and described gas collector lower end port, be separated with the space of flowing out for synthesis gas.The Diffusion of gas stream that this structure can be used gas collector flows, avoid air-flow directly to impact the impact injury that body of heater low head causes body of heater, and short stay in the cavity of the gas that can use gas collector between low head and body of heater, ensure the inside and outside pressure balance of low head, and can make body of heater relative even with the environment temperature inside and outside cylindrical shell and low head, can not produce stress and concentrate.
Between baffle plate and gas collector, can be welded to connect by bearing rib, and strengthen by gusset.Preferably, collecting pipe top is near not perforate in upper perforated plate 100mm, to prevent that the catalyst sedimentation gas that induces reaction from refluxing and short circuit.
Consider the thermal expansion of gas collector, can on the lower surface of described upper perforated plate, be provided with adapter sleeve, it is interior and gapped with described upper perforated plate interval that the upper end of described gas collector is positioned at this adapter sleeve, and this gap can the thermal expansion of supplied gas collector.
Consider the thermal expansion of reacting furnace inside, can on described outlet pipe, expansion joint be set, to solve internal-response entire system thermal expansion problem.
The connected mode of lower perforated plate and body of heater can have multiple, preferably, can on the perisporium of described body of heater, be provided with locating ring, and the upper surface of this locating ring is provided with annular groove; Described lower perforated plate 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 location-plates, every group of location-plate comprises left and right spaced left location-plate and right location-plate, accordingly, the sidewall of described upper perforated plate is provided with polylith locating piece, and each described locating piece is contained between corresponding upper location-plate and lower location-plate.
Preferably, on upper perforated plate, be welded with 4 locating pieces, coordinate radial location with 4 groups of location-plates that are welded on inboard wall of furnace body, to ensure the Fast Installation of inner tube bank and being sealed and matched of described tongue and groove.
Isothermal change furnace in such scheme adopts overall diameter to Z-type structure on the whole, reaction gas upper entering and lower leaving, it between heat exchanger tube, is beds, in pipe, walk recirculated cooling water, cooling water 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 forced circulation, recirculated cooling water downstream can arrange drum byproduct steam recovery waste heat.Maintain the constant of transformationreation temperature by the controlled circulation water yield.
One, compare with existing saturated hot-water tower height WGR CO conversion process, the invention has the advantages that:
1, shift process is short, and SR is little, has saved the work done during compression of next procedure, has reduced energy consumption.
2, use isothermal change furnace to substitute at least adiabatic change furnace of two-stage, reduced change furnace number of units, saved equipment investment and catalyst costs.
3, isothermal change furnace operating temperature is low, catalyst running environment gentleness, and catalyst long service life, shift conversion step is easily realized long-period stable operation.
4, the self-produced steam of shift conversion step, after methanation operation is overheated, all for the transformationreation of self, has saved part sect heat-exchanger and energy recovery equipment, has simplified technological process, has further saved equipment investment.
5, reach and shift out fast high concentration CO reaction heat by the circulation of cooling water, its process can be also forced circulation of Natural Circulation, reach the object of control change reaction temperature by the controlled circulation water yield, coolant outlet can arrange drum byproduct steam, recovery waste heat, structure of reactor is simple, small investment, and controllability is strong.
6, utilize overall diameter to the little feature of gas reactor pressure drop, inner reaction system is adopted to equipment self-weight sealing, cooling water inlet/outlet pipe all adopts flange to be connected with body of heater, internal-response system can entirety be extracted out, and the quick handling that the demountable structure that adds gas distributor is catalyst and the checking maintenance of post facility facilitate.
7, the setting of internal-response systemic circulation coolant outlet expansion joint and location, gas-collecting pipe top cover cylinder gap, take into full account high temperature stress operating mode, solve 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.
8, isothermal change furnace 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 distribution of gas more even, be conducive to improve conversion ratio, simultaneously, take into full account catalyst sedimentation problem, be all reserved with not aperture area of 100mm at gas distributor and collecting pipe top, can prevent backflow, the short circuit of conversion gas.
9, the present invention adopts shell-and-tube reactor, between Catalyst packing heat exchanger tube, and reaction bed temperature, stable, the life-span is long, and can increase CO conversion gas treating capacity by increasing gas distributor hop count mode, is conducive to the maximization of device.
Brief description of the drawings
Fig. 1 is the floor map of assembly structure in the embodiment of the present invention;
Fig. 2 is upper perforated plate location schematic diagram in the embodiment of the present invention;
Fig. 3 is lower perforated plate 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 cutaway view.
Fig. 6 is gas collector structural representation in the embodiment of the present invention;
Fig. 7 is the process flow diagram of the embodiment of the present invention.
Detailed description of the invention
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 change furnace using in the present embodiment comprises:
Body of heater 51, comprise main body 511, upper cover 515 and low head 512, between main body 511 and upper cover 515, be provided with changeover portion 518, between main body 511 and changeover portion 518, adopt flange to removably connect, between main body 511 and low head 512, upper cover 515 and changeover portion 518, be and be welded to connect.Upper cover 515 tops are provided with reaction gas entrance 516 and top inspection manhole 517, changeover portion 518 sidewalls are provided with circulating cooling water out 514, main body 511 lower end sidewalls are provided with bottom inspection manhole 513, low head bottom is provided with the first 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 change furnace.
Internal-response system, is mainly made up of parts such as heat-exchanging tube bundle 52, gas distributor 53, gas-collecting pipe 54, oval upper cover 526 and spherical low heads 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 outlet pipe vertical portion is provided with expansion joint, and the effect of expansion joint is to eliminate the stress that outlet pipe thermal expansion produces; The horizontal component of outlet pipe is divided into two sections, and these two sections are detachably connected by flange.Circular low head 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 the first cooling water inlet 519 flanges.Internal-response system also comprises upper perforated plate 527 and lower perforated plate 5210, and upper perforated plate 527 relies on four locating pieces 5211 that are welded on upper perforated plate and four groups of location-plates 5212 that are welded in equipment barrel to coordinate radial location, ensures axial displacement.Every group of location-plate comprises the spaced left location-plate in left and right and right location-plate, and locating piece is between the left and right location-plate of correspondence.On the internal perisporium of main body 511, be welded with locating ring 5215, the upper surface of this locating ring is provided with annular groove; The bottom of locating ring is provided with 16 uniform bearing ribs 5213, and these bearing ribs are welded on main body 511 and locating ring 5215, to strengthen the load-bearing of locating ring; Eight jackscrews 5214 are also set on locating ring, facilitate the dismounting of reaction system.Lower perforated plate 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 locating 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 perforated plate to locate.On upper and lower tube sheet, be equipped with the pore plugging for each heat exchanger tube 528, the two ends of each heat exchanger tube are plugged in respectively formation heat-exchanging tube bundle in corresponding pore, between each heat exchanger tube, in gap, be filled with catalyst, the middle part of heat-exchanging tube bundle is provided with multiple for supporting the support member 529 of heat-exchanging tube bundle.
Gas distributor 53, gas distributor pipe nipple bolt by several sections of same structures connects to form, every section of distributor includes inner barrel 535 and the outer cylinder body 534 that length is 500mm, and inside and outside cylindrical shell forms by two semicircular cylinders, semicircular cylinder end is welded with two groups of vertical connecting plates 533, and two semicircular cylindrical shell bolts are formed to columniform cylindrical shell together; After each section of inner barrel connects, form inner core, after each section of outer cylinder body connects, form sheathed urceolus outer tube.On inner barrel 535 and outer cylinder body 534, be evenly equipped with respectively circular pore as reactant gas passage; Inner core is as gas quadratic distribution device, and its perforate density is greater than urceolus and aperture is not more than 3mm, and meanwhile, inside and outside cylinder is apart from not offering pore within upper perforated plate 100mm height and position to prevent the catalyst sedimentation road of breathing hard that induces reaction.The top of inner core and urceolus and bottom are equipped with two and half ring flat-plates 531, half ring flat-plate split position is consistent with inner core and urceolus, and weld together with vertical connecting plate 533, half ring flat-plate 531 ends are provided with eight journal stirrups 532, for bolt and location between upper-lower section gas distributor, the upper end of epimere cylindrical shell relies on the locating ring location of welding with upper perforated plate 527, and the lower end of hypomere cylindrical shell is put into 5210 cannelures of opening on lower perforated plate and located.The segmentation bolt releasable connection of gas distributor designs, and can effectively improve the efficiency of loading and unloading of catalyst.
Gas collector 54, comprises collecting pipe 543, has the strip gas collection hole that width is less than 3mm on it, same, stays highly not perforate of 100mm, with the reaction gas short circuit that prevents from causing because of catalyst sedimentation at collecting pipe top near upper perforated plate 527.Collecting pipe welded top has circular cover 542, circular cover outside is provided with the collecting pipe abutment sleeve 541 that is welded on upper perforated plate 527, between sleeve and described cover plate 542, stay 2mm gap, between cover plate and upper perforated plate 527, be provided with 30mm gap to solve gas-collecting pipe 54 thermal expansion problems.The spherical low head 522 of collecting pipe 543 lower ends and internal-response system is welded to connect.Described collecting pipe bottom is provided with expander section 545, and expander outlet at bottom is provided with central circular baffle plate 547, makes gas be diffusion type and flows, and center baffle and expander section are welded to connect by bearing rib 546, and strengthen by welding 54 bearing ribs 544.
As shown in Figure 7, the CO conversion process of the present embodiment is as follows:
160 DEG C of the raw gas temperature of the saturated steam 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 thermal loss, a small amount of steam in raw gas generation condensate liquid that can be condensed, raw gas and lime set coexist and can cause corrosion and the vibrations of pipeline and equipment in pipe-line 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.Send into detoxification groove 2 from the gas-liquid separator 1 top raw gas after separatory out and remove the impurity such as ash content and heavy metal in raw gas, then enter the bottom of saturator 3.
Raw gas carries out heat and mass with the process recycled water counter current contacting that is 180 DEG C～185 DEG C from hot-water tower 8 temperature in saturator 3, go out the process recycled water of saturator 3 bottoms after 4 pressurizations of saturator column bottoms pump, send hot-water tower 8 Heating Cyclic use again back to, extract 3%～8% of process cycles water inventory simultaneously out and go rear system to carry out stripping, prevent that harmful substance from accumulating in process cycles water system.
Crude synthesis gas is humidified temperature raising in saturator 3, and temperature reaches 175 DEG C～180 DEG C, and water dry gas mol ratio is 0.44～0.48.Supplement from the 4.0Mpa of methanation and steam pipe system, press superheated steam in 400 DEG C, regulating crude synthesis gas water/dry gas mol ratio is 1.0～1.1, and temperature is 250 DEG C, sends into and in isothermal change furnace 5, carries out depth conversion.
The conversion gas temperature that goes out isothermal change furnace 5 is 250 DEG C～270 DEG C, and CO butt volume content is about 1.0%～2.0%, and this conversion gas is cooled to 185 DEG C through conversion gas cooler 7 and process recycled water heat exchange, then sends into hot-water tower 8 bottoms.
Conversion gaseous mixture, in hot-water tower 8 and from the process recycled water of saturator 3 with from the process condensate of rear system and supplementary medium-pressure boiler feedwater countercurrent heat-transfer mass transfer, reclaims Lowlevel thermal energy.The process cycles coolant-temperature gage of being sent by hot-water tower 8 bottoms is about 171 DEG C, after 7 temperature raisings of conversion gas cooler, sends into saturator 3.Be about 160 DEG C by hot-water tower 8 tops conversion gas temperature out, send into downstream section and reclaim low temperature exhaust heat.
Isothermal change furnace 5 is removed reaction heat by boiler feedwater mode, by-product pressure 4.0Mpa simultaneously, the middle pressure saturated vapor that temperature is 251 DEG C, the middle pressure saturated vapor of by-product enters drum 6 and separates liquid phase, the middle pressure saturated vapor demethanization operation that drum 6 tops are sent is superheated to 400 DEG C, then with the supplementary steam as transformationreation together with the middle pressure superheated steam of pipe network, inject from saturator 3 tops raw gas out, the liquid phase of drum 6 bottoms is entered in isothermal change furnace 5 and is recycled by self-circulation mode, fed water to the interior supplementary medium-pressure boiler of drum 6 by battery limit (BL) 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 saturated hot-water tower height WGR CO conversion process and a kind of saturator string constant-temperature oven CO conversion process major 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, change furnace quantity is few, and loaded catalyst is little, hot(test)-spot temperature is low and system pressure drop is little.Can reduce equipment and the catalyst investment cost of shift conversion step.The low effectively extending catalyst of hot(test)-spot temperature service life, system pressure drop I is significantly to reduce the work done during compression consumption of rear system, and both all can play the object of saving operating cost.
Claims (10)
1. a saturator string constant-temperature oven 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, isolates after liquid phase and sends in detoxification groove and remove the impurity in raw gas, sends into subsequently in saturator;
Raw gas is sent into saturator by the bottom of saturator, process recycled water heat exchange to 180～200 of sending from hot-water tower bottom DEG C, top by saturator enters saturator, 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, sent by saturator top, after middle pressure superheated steam humidification by mixing of gas temperature raising from pipe network, send into isothermal change furnace and carry out depth conversion reaction, control the water/dry gas mol ratio of raw gas that enters isothermal change furnace and be 1.0～1.2,250 DEG C of temperature; The air speed of controlling isothermal change furnace inner catalyst is 1000～3000, and the temperature rise of isothermal change furnace is 10 DEG C～20 DEG C; The conversion gas temperature that goes out isothermal change furnace is 250 DEG C～270 DEG C, and CO butt volume content is 1%～2%;
The conversion gaseous mixture that goes out isothermal change furnace is cooled to after 180～200 DEG C through heat exchange, send into hot-water tower by hot-water tower bottom, carry out countercurrent mass transfer heat transfer with the process recycled water entering from hot-water tower middle part, spray into process for purifying condensate liquid and medium-pressure boiler water on the top of hot-water tower, the mol ratio of described process recycled water and purification and condensation liquid sum and described medium-pressure boiler water is 7.0～10.0, carry out countercurrent mass transfer heat transfer, obtain the conversion gaseous mixture after cooling at hot-water tower top, obtain process recycled water in hot-water tower bottom;
The consumption of the above-mentioned process recycled water that enters hot-water tower from hot-water tower middle part is 4.0～6.0 with the mol ratio of the butt raw gas that enters gas-liquid separator.
2. saturator string constant-temperature oven CO conversion process according to claim 1, in the body of heater of the isothermal change furnace described in it is characterized in that, be provided with the heat-exchanging tube bundle being formed by many heat exchanger 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 circulating cooling water out, bottom of furnace body is provided with conversion gas outlet and the first cooling water inlet, and the center of described body of heater is provided with gas collector; 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 perforated plate and lower perforated plate, the inwall interval of described upper perforated plate and described body of heater is gapped, the be tightly connected internal perisporium of described body of heater of the periphery of described lower perforated plate; The top of described upper perforated plate is provided with upper cover, the below of described lower perforated plate is provided with low head, described heat-exchanging tube bundle is arranged in described gas distributor, and the two ends of each described heat exchanger tube are separately fixed on described upper and lower tube sheet and are communicated with respectively the cavity being made up of upper cover and upper perforated plate, low head and lower perforated plate; The upper end of described gas collector connects described upper perforated plate, and the lower end of gas collector is positioned at the cavity of low head and described bottom of furnace body formation through described low head; Described upper cover is provided with coolant outlet, and this coolant outlet connects described circulating cooling water out by outlet pipe, and described outlet pipe comprises the two parts that are detachably connected; Described low head is provided with the second cooling water inlet, and this second cooling water inlet connects the first described cooling water inlet by water inlet pipe, and described water inlet pipe comprises the two parts that are detachably connected.
3. saturator string constant-temperature oven CO conversion process according to claim 2, it is characterized in that described gas distributor comprises the multiple segmentations that are detachably connected, and each segmentation is removably connected and is formed again by two semicircular cylinders.
4. saturator string constant-temperature oven CO conversion process according to claim 3, it is characterized in that each described segmentation includes outer cylinder body and is set in the inner barrel in described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected to form and is set in inner core in described urceolus, and described outer cylinder body and described inner barrel interval gapped.
5. saturator string constant-temperature oven 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 pore on described endoporus is less than or equal to 3mm.
6. saturator string constant-temperature oven CO conversion process according to claim 5, is characterized in that described gas distributor and gas collector be not all offering pore near the position in described upper perforated plate 100mm.
7. according to the saturator string constant-temperature oven CO conversion process described in the arbitrary claim of claim 2 to 6, it is characterized in that the part that described gas collector exposes to described low head is horn-like, and the middle part of described gas collector lower end port is provided with baffle plate, between the periphery of described baffle plate and described gas collector lower end port, be separated with the space of flowing out for synthesis gas.
8. saturator string constant-temperature oven CO conversion process according to claim 7, is characterized in that the lower surface of described upper perforated plate is provided with adapter sleeve, and it is interior and gapped with described upper perforated plate interval that the upper end of described gas collector is positioned at this adapter sleeve.
9. saturator string constant-temperature oven CO conversion process according to claim 8, is characterized in that described outlet pipe is provided with expansion joint.
10. saturator string constant-temperature oven CO conversion process according to claim 9, is characterized in that the perisporium of described body of heater is provided with locating ring, and the upper surface of this locating ring is provided with annular groove; Described lower perforated plate 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 location-plates, every group of location-plate comprises upper and lower spaced upper location-plate and lower location-plate, accordingly, the sidewall of described upper perforated plate is provided with polylith locating piece, and each described locating piece is contained between corresponding upper location-plate and lower location-plate.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210378009.7A CN102886230B (en) | 2012-10-08 | 2012-10-08 | CO (carbon monoxide) conversion process adopting tandem isothermal furnaces of saturation tower |
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| CN104748662A (en) * | 2013-12-30 | 2015-07-01 | 中核武汉核电运行技术股份有限公司 | Measuring method for scale deposit thickness on external wall of heat transferring pipe based on eddy current testing signals |
| CN104748666A (en) * | 2013-12-30 | 2015-07-01 | 中核武汉核电运行技术股份有限公司 | Deep defect quantifying method based on eddy rotating probe signal |
| CN103879961B (en) * | 2014-03-24 | 2015-07-29 | 中石化宁波工程有限公司 | A kind of saturator share split circulation CO conversion process |
| CN104152187B (en) * | 2014-08-06 | 2016-02-17 | 中石化宁波工程有限公司 | A kind of can the CO conversion process in extending catalyst work-ing life |
| CN204589113U (en) * | 2015-01-30 | 2015-08-26 | 成都高科达科技有限公司 | A kind of methanation synthesizing methane system not with circulation gas |
| CN107164007A (en) * | 2017-05-15 | 2017-09-15 | 中石化南京工程有限公司 | A kind of method of non-stoichiometric isothermal synthetic natural gas |
| CN109385293B (en) * | 2017-08-02 | 2020-12-08 | 中国石油化工股份有限公司 | Hydrocarbon steam conversion acidic water recycling device and method |
| CN108772026B (en) * | 2018-06-24 | 2024-04-26 | 唐山三友硅业股份有限公司 | Gas distributor for gas-solid catalytic tower reactor |
| CN109052319B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | High CO conversion process matched with methanol synthesis |
| CN109438181A (en) * | 2018-11-08 | 2019-03-08 | 鄂尔多斯市瀚博科技有限公司 | A method of methanol is produced using silicomanganese furnace exhaust gas |
| CN110550602B (en) * | 2019-08-08 | 2022-08-12 | 中石化宁波工程有限公司 | Controllable semi-isothermal conversion process for high-concentration carbon monoxide for oxo synthesis |
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