CN102886230A - 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 active principle is high in low, the synthesis gas, operating cost is low and environmental friendliness.China comes producing synthesis gas in the bed pulverized coal gasification technology that in succession introduced more than ten cover shell the beginning of this century.Waste heat boiler is adopted in the cooling of crude synthesis gas in this technology, and CO butt volume content is up to more than 60% in the crude synthesis gas of generation, and the steam volume content is less than 20% simultaneously, and crude synthesis gas has the distinguishing features such as the low and CO content height of water vapour content.The Shell Coal Gasification technology is used for just facing when gas making comes the device such as supporting synthetic ammonia, hydrogen manufacturing, synthesizing methanol a high concentration CO converter technique difficult problem.So in the time of the 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. the mole strong exothermal reaction, generate carbon dioxide and hydrogen.For the crude synthesis gas that different Coal Gasification Technology generates, the chemical reaction process of downstream transforms operation all is identical, but shift process need to design targetedly according to the characteristics of crude synthesis gas.Crude synthesis gas for the Technology of Shell Coal Gasification generation, when shift conversion step carries out the CO transformationreation, the Focal point and difficult point of shift process design is bed temperature how effectively to control the CO transformationreation, prolongs service life, the equipment investment of minimizing conversion sum of series, the Pressure Drop that reduces shift conversion step and saving middle pressure steam and the power consumption of transformation catalyst.
At present domesticly generally adopt adiabatic change furnace in the design of high concentration CO shift process, transformationreation is strong exothermic process in view of CO, and existing conversion process process organization all adopts the 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 easy overtemperature of change furnace, the series of problems such as catalyst life is short and energy consumption 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 the furnace wall, causes the equipment wall thickness large, and equipment investment is high; The first change furnace catalyst is under the higher temperature and moves, and running environment is harsh, and catalyst life is shorter, changes the frequent operation expense high; Adiabatic change furnace temperature control is difficulty, overtemperatute easily occurs, and safe operation causes adverse effect to shift conversion step, has potential safety hazard.Simultaneously, complicated to the catalyst vulcanization process when shift conversion step is driven because adiabatic reaction progression is many, 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 string constant-temperature oven CO conversion process, with the series of problems such as solve high WGR CO conversion process long flow path in the prior art, 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 the technical scheme that adopts: this saturator string constant-temperature oven CO conversion process is characterized in that comprising the steps:
The raw gas of being sent here by coal gasification workshop section is at first sent into gas-liquid separator and is carried out liquid phase and separate, and sends into the impurity of removing in the detoxification groove in the raw gas after isolating liquid phase, sends into subsequently in the saturator;
Raw gas is sent into saturator by the bottom of saturator, after the process recycled water heat exchange to 180 of sending from hot-water tower bottom～200 ℃, enters saturator by the top of saturator, and the countercurrent heat-transfer mass transfer is carried out in two bursts of logistics in saturator.The process recycled water of sending bottom saturator is back to hot-water tower after the pressurization of saturator column bottoms pump;
Raw gas is humidified temperature raising in saturator after, sent by the saturator top, after middle pressure superheated steam humidification by mixing of gas temperature raising from pipe network, send into the isothermal change furnace and carry out depth conversion reaction, control enters that the water of the raw gas of isothermal change furnace/dry gas mol ratio is 1.0～1.2,250 ℃ of temperature; The air speed of control isothermal change furnace inner catalyst is 1000～3000, and the temperature rise of isothermal change furnace is 10 ℃～20 ℃; The conversion gas temperature that goes out the isothermal change furnace is 250 ℃～270 ℃, and CO butt volume content is 1%～2%;
Go out the conversion gaseous mixture of isothermal change furnace after heat exchange is cooled to 180～200 ℃, send into hot-water tower by the hot-water tower bottom, carrying out countercurrent mass transfer with the process recycled water that enters from the hot-water tower middle part conducts heat, 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, carrying out countercurrent mass transfer conducts heat, conversion gaseous mixture after the hot-water tower top obtains lowering the temperature obtains process recycled water in the hot-water tower bottom.
The above-mentioned consumption that enters the process recycled water of hot-water tower from the hot-water tower middle part is 4.0～6.0 with the mol ratio that enters the butt raw gas of gas-liquid separator.
Employed isothermal change furnace can use any one isothermal change furnace of the prior art in the above-mentioned technique.Preferably, described isothermal change furnace comprises body of heater, be provided with the heat-exchanging tube bundle that is formed by many heat exchanger tubes in the described body of heater, 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 coolant 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 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 that removably connects, the cylindrical shell that is provided with tubular structure in the described second segment body of heater consists of the gas distributor of reacting furnace, the upper/lower terminal of this cylindrical shell is connected on upper perforated plate and the 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 the described cylindrical shell, and the two ends of each described heat exchanger tube are separately fixed on the described upper and lower tube sheet and are communicated with respectively the cavity that is made 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 cavity that described low head is positioned at low head and described bottom of furnace body formation is passed in the lower end of gas collector; Described upper cover is provided with coolant outlet, and this coolant outlet connects described coolant outlet by outlet pipe, and described outlet pipe comprises the two parts that are detachably connected; Described low head is provided with the cooling water inlet, and this coolant outlet connects described cooling water inlet by water inlet pipe, and described water inlet pipe comprises the two parts that are detachably connected; Be provided with evenly and at intervals a plurality of pores on the described gas distributor.
Preferably, can connect by flange between first paragraph body of heater and the second segment body of heater, body of heater can be bearing in vertical placement on the skirt.
In order to make things convenient for the filling of catalyst, described gas distributor can comprise a plurality of segmentations that are detachably connected, and each segmentation is removably connected by two semicircular cylinders again and consists of.
Further, distributing homogeneity when guaranteeing that gas enters beds, each described segmentation includes outer cylinder body and is set in the interior inner barrel of described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected and forms the inner core be set in the described urceolus, and described outer cylinder body and described inner barrel interval are gapped.Inner barrel plays the effect of quadratic distribution to reaction gas.
Preferably, the density of the pore described in the such scheme on the inner core is greater than described urceolus, and the aperture of the pore on the described endoporus is less than or equal to 3mm.
Consider the settlement issues of catalyst in the production process, described gas distributor is not offered pore near described upper perforated plate 100mm with interior position, refluxes and short circuit to prevent the reaction gas that catalyst sedimentation causes.
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, is separated with the space of flowing out for synthesis gas between the periphery of described baffle plate and described gas collector lower end port.The Diffusion of gas stream that this structure can be used gas collector flows, avoided air-flow directly to impact the impact injury that the body of heater low head causes body of heater, and can use short stay in the cavity of gas between low head and body of heater of gas collector, guaranteed the inside and outside pressure balance of low head, and can make the inside and outside environment temperature of body of heater and cylindrical shell and low head relative even, can not produce stress and concentrate.
Can be welded to connect by bearing rib between baffle plate and the gas collector, and strengthen by gusset.Preferably, the collecting pipe top is near not perforate in the upper perforated plate 100mm, refluxes and short circuit to prevent the catalyst sedimentation gas that induces reaction.
Consider the thermal expansion of gas collector, can be provided with adapter sleeve at the lower surface of described upper perforated plate, 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, but this gap supplied gas collector thermal expansion.
Consider the thermal expansion of reacting furnace inside, can expansion joint be set at described outlet pipe, 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 be provided with locating ring at the perisporium of described body of heater, 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 the described groove, and is provided with sealing ring between projection and the groove.
The internal perisporium of described body of heater is provided with many group location-plates, every group of location-plate comprises left location-plate and the right location-plate that left and right interval arranges, accordingly, the sidewall of described upper perforated plate is provided with the polylith locating piece, and each described locating piece is contained between the corresponding upper location-plate and lower location-plate.
Preferably, be welded with 4 locating pieces on the upper perforated plate, cooperate radial location with 4 groups of location-plates on being welded on inboard wall of furnace body, with being sealed and matched of the Fast Installation that guarantees inner tube bank and described tongue and groove.
Isothermal change furnace in the such scheme adopts overall diameter to the Z-type structure on the whole, the reaction gas upper entering and lower leaving, it is beds between heat exchanger tube, walk recirculated cooling water in the pipe, cooling water absorbs conversion heat, according to the requirement of strength that reaction heat shifts out, the cooling water circulation process can be that Natural Circulation also can be forced circulation, and the recirculated cooling water downstream can arrange drum byproduct steam recovery waste heat.Keep 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 the isothermal change furnace to substitute at least adiabatic change furnace of two-stage, reduced the change furnace number of units, saved equipment investment and catalyst costs.
3, isothermal change furnace operating temperature is low, and catalyst running environment is gentle, the catalyst long service life, and shift conversion step is easily realized long-period stable operation.
4, the self-produced steam of shift conversion step overheated through the methanation operation after, all for the transformationreation of self, saved part sect heat-exchanger and energy recovery equipment, simplified technological process, further saved equipment investment.
5, reach and shift out fast the high concentration CO reaction heat by the cooling water circuit, its process can be also forced circulation of Natural Circulation, reach the purpose of control change reaction temperature by the controlled circulation water yield, coolant outlet can arrange the drum byproduct steam, recovery waste heat, structure of reactor is simple, small investment, and controllability is strong.
6, utilize overall diameter to the little characteristics of gas reactor pressure drop, inner reaction system is adopted the equipment self-weight sealing, the cooling water inlet/outlet pipe is connected with body of heater and is adopted flange to connect, the internal-response system can wholely be extracted out, and the demountable structure that adds gas distributor is that the quick loading and unloading of catalyst and the checking maintenance of post facility facilitate.
7, the setting of internal-response systemic circulation coolant outlet expansion joint and gas-collecting pipe top cover cylinder gap location, take into full account the 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.
8, the isothermal change furnace adopts overall diameter to 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 the reaction gas quadratic distribution, make distribution of gas more even, be conducive to improve conversion ratio, simultaneously, take into full account the catalyst sedimentation problem, all be 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 the 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.
Description of drawings
Fig. 1 is the floor map of assembly structure in the embodiment of the invention;
Fig. 2 is upper perforated plate location schematic diagram in the embodiment of the invention;
Fig. 3 is lower perforated plate location schematic diagram in the embodiment of the invention;
Fig. 4 is gas distributor structural representation in the embodiment of the invention;
Fig. 5 be along A-A among Fig. 4 to cutaway view.
Fig. 6 is gas collector structural representation in the embodiment of the invention;
Fig. 7 is the process flow diagram of the embodiment of the invention.
The specific 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 ton/years of urea of 300,000 ton/years of synthetic ammonia, the present invention being described in further detail.
To shown in Figure 6, employed isothermal change furnace comprises in the present embodiment such as Fig. 1:
Body of heater 51, comprise main body 511, upper cover 515 and low head 512, be provided with changeover portion 518 between main body 511 and the upper cover 515, the employing flange removably connects between main body 511 and the changeover portion 518, is between main body 511 and low head 512, upper cover 515 and the changeover portion 518 to 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, the low head bottom is provided with cooling water inlet 519 and conversion gas outlet 5110, body of heater 51 bottoms are seated on the skirt 56, and skirt 56 is the base for supporting of this isothermal change furnace.
The internal-response system mainly is comprised 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 that is connected with above-mentioned circulating cooling water out 514, and the outlet pipe vertically middle part of part is provided with expansion joint, and the effect of expansion joint is to eliminate the stress that the 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 that communicates with above-mentioned bottom inspection manhole 513 and the recirculated cooling water import pipeline section that is connected with above-mentioned cooling water inlet 519 flanges.The 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 the upper perforated plate and the four groups of location-plates 5212 that are welded on the equipment barrel to cooperate radial locations, guarantees axial displacement.Every group of location-plate comprises that between left and right every the left location-plate and the right location-plate that arrange, locating piece is between the left and right location-plate of correspondence.Be welded with locating ring 5215 on the internal perisporium of main body 511, 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 the locating ring 5215, to strengthen the load-bearing of locating ring; Eight jackscrews 5214 also are set on the locating ring, make things convenient for the dismounting of reaction system.Lower perforated plate 5210 is provided with the annular lug suitable with groove, and projection is contained in the groove, and is provided with sealing ring 5217 between projection and the groove.Also be welded with four locating cones 5216 between the inwall of the upper surface of locating ring and main body 511, locating cone inclination at 45 °; The effect of locating cone mainly is for lower perforated plate is located.Be equipped with the pore that plugs for each heat exchanger tube 528 on the upper and lower tube sheet, the two ends of each heat exchanger tube are plugged in respectively and form heat-exchanging tube bundle in the corresponding pore, be filled with catalyst in each heat exchanger tube gap, the middle part of heat-exchanging tube bundle is provided with a plurality of support members 529 for supporting 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 steam of being sent here by coal gasification workshop section, pressure 3.7Mpa, with pipeline raw gas is being delivered to the process of conversion section because thermal loss from gasification workshop section, a small amount of steam in raw gas generation condensate liquid that can be condensed, the coexistence in pipe-line system of raw gas and lime set can cause corrosion and the vibrations of pipeline and equipment, so raw gas at first needs lime set is wherein separated.
Therefore the present embodiment is sent into raw gas first gas-liquid separator 1, and liquid flows out from the outlet at bottom of gas-liquid separator 1.Out the raw gas through behind the separatory is sent into detoxification groove 2 and is removed the impurity such as ash content the raw gas and heavy metal from gas-liquid separator 1 top, then enters the bottom of saturator 3.
Raw gas carries out heat and mass with the process recycled water counter current contacting that from hot-water tower 8 temperature is 180 ℃～185 ℃ in saturator 3, go out the process recycled water of saturator 3 bottoms after 4 pressurizations of saturator column bottoms pump, send again Heating Cyclic use of hot-water tower 8 back to, extract simultaneously 3%～8% of process cycles water inventory out and go to rear system to carry out stripping, prevent that harmful substance from accumulating in the process cycles water system.
Crude synthesis gas is humidified temperature raising in saturator 3, temperature reaches 175 ℃～180 ℃, and water dry gas mol ratio is 0.44～0.48.Replenish the 4.0Mpa from methanation and steam pipe system, press superheated steam in 400 ℃, water/the dry gas mol ratio is 1.0～1.1 to regulate crude synthesis gas, and temperature is 250 ℃, sends into and carries out depth conversion in the isothermal change furnace 5.
The conversion gas temperature that goes out isothermal change furnace 5 is 250 ℃～270 ℃, and CO butt volume content is about 1.0%～2.0%, and this conversion gas is cooled to 185 ℃ through conversion gas cooler 7 and process recycled water heat exchange, then sends into hot-water tower 8 bottoms.
The conversion gaseous mixture reclaims Lowlevel thermal energy in hot-water tower 8 and from the process recycled water of saturator 3 with from the process condensate of rear system and additional medium-pressure boiler feedwater countercurrent heat-transfer mass transfer.The process cycles coolant-temperature gage of being sent by hot-water tower 8 bottoms is about 171 ℃, after 7 temperature raisings of conversion gas cooler, sends into saturator 3.Be about 160 ℃ by hot-water tower 8 tops conversion gas temperature out, send into downstream section and reclaim low temperature exhaust heat.
Comparative Examples
For adopting Shell Coal Gasification gas making to produce the typical chemical fertilizer plant of 520,000 ton/years of urea of 300,000 ton/years of synthetic ammonia, enter effective gas (H of conversion section
2+ CO) be approximately 85000Nm
3/ h compares 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 and sees Table 1.
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, the system pressure drop I with remarkable reduction after the work done during compression consumption of system, both all can play the purpose of saving operating cost.
Claims (10)
1. a saturator string constant-temperature oven CO conversion process is characterized in that comprising the steps:
The raw gas of being sent here by coal gasification workshop section is at first sent into gas-liquid separator and is carried out liquid phase and separate, and sends into the impurity of removing in the detoxification groove in the raw gas after isolating liquid phase, sends into subsequently in the saturator;
Raw gas is sent into saturator by the bottom of saturator, after the process recycled water heat exchange to 180 of sending from hot-water tower bottom～200 ℃, enters saturator by the top of saturator, and the countercurrent heat-transfer mass transfer is carried out in two bursts of logistics in saturator.The process recycled water of sending bottom saturator is back to hot-water tower after the pressurization of saturator column bottoms pump;
Raw gas is humidified temperature raising in saturator after, sent by the saturator top, after middle pressure superheated steam humidification by mixing of gas temperature raising from pipe network, send into the isothermal change furnace and carry out depth conversion reaction, control enters that the water of the raw gas of isothermal change furnace/dry gas mol ratio is 1.0～1.2,250 ℃ of temperature; The air speed of control isothermal change furnace inner catalyst is 1000～3000, and the temperature rise of isothermal change furnace is 10 ℃～20 ℃; The conversion gas temperature that goes out the isothermal change furnace is 250 ℃～270 ℃, and CO butt volume content is 1%～2%;
Go out the conversion gaseous mixture of isothermal change furnace after heat exchange is cooled to 180～200 ℃, send into hot-water tower by the hot-water tower bottom, carrying out countercurrent mass transfer with the process recycled water that enters from the hot-water tower middle part conducts heat, 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, carrying out countercurrent mass transfer conducts heat, conversion gaseous mixture after the hot-water tower top obtains lowering the temperature obtains process recycled water in the hot-water tower bottom.
The above-mentioned consumption that enters the process recycled water of hot-water tower from the 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 string constant-temperature oven CO conversion process according to claim 1, it is characterized in that described isothermal change furnace body of heater, be provided with the heat-exchanging tube bundle that is formed by many heat exchanger tubes in the described body of heater, 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 coolant 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 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 that removably connects, be provided with gas distributor in the described second segment body of heater, the upper/lower terminal of this gas distributor is connected on upper perforated plate and the 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 the described gas distributor, and the two ends of each described heat exchanger tube are separately fixed on the described upper and lower tube sheet and are communicated with respectively the cavity that is made 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 cavity that described low head is positioned at low head and described bottom of furnace body formation is passed in the lower end of gas collector; Described upper cover is provided with coolant outlet, and this coolant outlet connects described coolant outlet by outlet pipe, and described outlet pipe comprises the two parts that are detachably connected; Described low head is provided with the cooling water inlet, and this coolant outlet connects described cooling water inlet by water inlet pipe, and described water inlet pipe comprises the two parts that are detachably connected.
3. CO overall diameter according to claim 2 is characterized in that to the isothermal change furnace described gas distributor comprises a plurality of segmentations that are detachably connected, and each segmentation is removably connected by two semicircular cylinders again and consists of.
4. CO overall diameter according to claim 3 is to the isothermal change furnace, it is characterized in that each described segmentation includes outer cylinder body and is set in the interior inner barrel of described outer cylinder body, each described outer cylinder body formation urceolus that is detachably connected, each described inner barrel is detachably connected and forms the inner core be set in the described urceolus, and described outer cylinder body and described inner barrel interval are gapped.
5. CO overall diameter according to claim 4 is to the isothermal change furnace, and the density that it is characterized in that the pore on the described inner core is greater than described urceolus, and the aperture of the pore on the described endoporus is less than or equal to 3mm.
6. CO overall diameter according to claim 5 is to the isothermal change furnace, it is characterized in that described gas distributor and gas collector all do not offering pore near described upper perforated plate 100mm with interior position.
According to claim 2 to the described CO overall diameter of 6 arbitrary claims to the isothermal change furnace, 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, is separated with the space of flowing out for synthesis gas between the periphery of described baffle plate and described gas collector lower end port.
8. CO overall diameter according to claim 7 is characterized in that to the isothermal change furnace 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. CO overall diameter according to claim 8 is characterized in that to the isothermal change furnace described outlet pipe is provided with expansion joint.
10. CO overall diameter according to claim 9 is characterized in that to the isothermal change furnace 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 the described groove, and is provided with sealing ring between projection and the groove; The internal perisporium of described body of heater is provided with many group location-plates, every group of location-plate comprises upper location-plate and the lower location-plate that upper and lower interval arranges, accordingly, the sidewall of described upper perforated plate is provided with the polylith locating piece, and each described locating piece is contained between the corresponding upper location-plate and lower location-plate.
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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 |
| CN103879961A (en) * | 2014-03-24 | 2014-06-25 | 中石化宁波工程有限公司 | Saturation tower split-circulation CO transformation process |
| CN104152187A (en) * | 2014-08-06 | 2014-11-19 | 中石化宁波工程有限公司 | CO conversion process capable of prolonging service life of catalysts |
| 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 |
| CN104818065A (en) * | 2015-01-30 | 2015-08-05 | 成都高科达科技有限公司 | Adiabatic cooling type methanation synthesis method for methane |
| CN104818065B (en) * | 2015-01-30 | 2017-03-15 | 成都高科达科技有限公司 | A kind of adiabatic cooling type methanation synthesizing methane method |
| 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 |
| CN109385293A (en) * | 2017-08-02 | 2019-02-26 | 中国石油化工股份有限公司 | Hydrocarbon steam conversion acid water recycle device and method |
| 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 |
| CN108772026A (en) * | 2018-06-24 | 2018-11-09 | 唐山三友硅业有限责任公司 | The gas distributor of tower reactor is catalyzed for gas-solid body |
| 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 |
| CN109052319A (en) * | 2018-09-30 | 2018-12-21 | 中石化宁波工程有限公司 | The high CO conversion process of mating methanol-fueled CLC |
| 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 |
| CN110550602A (en) * | 2019-08-08 | 2019-12-10 | 中石化宁波工程有限公司 | controllable semi-isothermal conversion process for high-concentration carbon monoxide for oxo synthesis |
| 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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