CN203582821U - Movable coal-made synthesis gas methanation catalyst test platform - Google Patents
Movable coal-made synthesis gas methanation catalyst test platform Download PDFInfo
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- CN203582821U CN203582821U CN201320520280.XU CN201320520280U CN203582821U CN 203582821 U CN203582821 U CN 203582821U CN 201320520280 U CN201320520280 U CN 201320520280U CN 203582821 U CN203582821 U CN 203582821U
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Abstract
The utility model discloses a movable coal-made synthesis gas methanation catalyst test platform, which comprises a gas component transformation and purification part and a gas methanation part which can be transported in a container, wherein the gas component transformation and purification part comprises a sulfur-resistant water gas transformation device, a medium-temperature zinc oxide desulphurization device, a gas-water separation device and an NaOH and 5A molecular sieve column decarbonization device; the gas methanation part is a three-segment methanation reactor device. The work flow of the test platform is that 1, the sulfur-resistant water gas transformation device turns the ratio of hydrogen to carbon monoxide in coal gas to a proper value; 2, the medium-temperature zinc oxide desulphurization device lowers the sulfur content below 0.2 ppm; 3, the gas-water separation device separate moisture out of the coal gas; 4, the NaOH and 5A molecular sieve column decarbonization device decarbonizes below 20 ppm; 5, the three-segment methanation reactor device undergoes a coal gas methanation reaction. The platform is used for testing the optimal methanation reaction conditions of various gas source states, is suitable for testing different feed gas components, different operation conditions and different catalysts, and can be used for evaluating a methanation process, operation parameters and catalyst performance.
Description
Technical field
The utility model relates to coal preparing natural gas technical field, is specifically related to a kind of packaged type producing synthesis gas from coal methanation catalyst test platform.
Background technology
China's energy structure is " many coals, few oil, have gas ", and hydrocarbon resources is not enough, and coal resources are relatively abundant.Coal discharges a large amount of oxysulfides, oxynitride and dust pollution in combustion processes, can cause the weather such as acid rain, photo-chemical smog and pollute, and dust particularly PM2.5 can cause human respiratory disease.China is in the industrialization middle and later periods, and demand for energy is large, and pollutant emission also grows in intensity thereupon, causes environment event to take place frequently.So must focus on environment protection, advocate energy-saving and emission-reduction, coal be carried out to the conversion of high-efficiency cleaning, to meet the clean utilization of coal and the requirement of Sustainable development.
With respect to technology such as coal methyl alcohol processed, coal derived DME, DCL/Direct coal liquefaction, ICL for Indirect Coal Liquefaction, coal synthetic natural gas processed (SNG) has the calorific value investment of total efficiency of utilization high (more than 50%), unit, cost is low, and CO transformation efficiency high (approaching 100%), used heat utilization ratio high (attached product high temperature and high pressure steam), waste water are easily processed the advantage of (need not process and can be used as oiler feed or recirculated water).
Compare with coal, Sweet natural gas is a kind of high-grade energy of high-efficiency cleaning, China's natural gas market development is in recent years very fast, within 2012, China's natural gas apparent consumption amount has reached 1471 billion cubic meters, and domestic gas production only has 1077 billion cubic meters the same period, annual from marine import from Australia, Indonesia, Malaysia and Iranian a large amount of natural gas liquids (LNG), from the second west to east gas pipeline project import from Kazakhstan, a large amount of pipe natural gas of Turkmenistan import, and plan build from the pipeline of Russian Far East inlet natural gas.
At present, the external interdependency of China's natural gas has reached 27%, also will continue in a short time to improve, in order to strengthen Chinese energy safety, improve domestic gas production, the relatively abundant coal of utilization is produced Sweet natural gas, becomes and alleviates Sweet natural gas supply anxiety and the external high feasible means of interdependency.This also meets the clean utilization of coal, the scientific development thinking of environmental emission reduction simultaneously.
In the coal resources of China, having is the brown coal of low-quality greatly, and directly utilising efficiency is low, pollution is large.Brown coal are transformed as raw material, produce high-grade energy Sweet natural gas, for the utilization of China's inferior coal provides a kind of new means.Simultaneously, the side area such as Xinjiang of China, Inner Mongol coal resource is very abundant, but be subject to the restriction of Rail Highway system transport power and great number transportation cost, develop difficulty larger, how can effectively utilize these regional coal resources significant for the energy safeguard of China.The coal resource of encouraging energetically Xinjiang, Inner Mongolia of national strategy is converted into high-quality Sweet natural gas on the spot in recent years, by the natural gas line in existing or planning construction, carry, alleviate the load of Rail Highway system, drive side area expanding economy.
At present, built the Datang Inner Mongol 4,000,000,000 side/years of Keshiketeng Banner, 4,000,000,000 side/years of Fuxin, Datang Liaoning of China, celebrate magnificent 5,500,000,000 side/years of Yining, remittance energy 1,600,000,000 side/year of Ordos, inner Mongolia four projects.In April, 2013 Committee of Development and Reform again ratify area of Tong coal corporation in Shanxi and 4,000,000,000 side/years of CNOOC Datong District, middle electricity is thrown 6,000,000,000 side/years of Huocheng, Xinjiang, newly cover Ordos, inner Mongolia 4,000,000,000 sides/Nian Heguo electricity Inner Mongol 4,000,000,000 sides of Hinggan League/Nian Sige new projects puts into operation.Gas maked coal enters fast-developing period again.
The committed step of coal synthetic natural gas technique processed is the synthetic gas COx component full methanation reaction after gasification.In the synthetic gas that gasification produces, mainly comprise CO, CO
2, H
2, CH
4and N
2deng composition, after the techniques such as conversion and purification, by methanation reaction, make CO, the CO in synthetic gas
2and H
2be converted under certain conditions CH
4, finally by techniques such as decarburization and enrichments, obtain CH
4content surpasses 90% synthetic natural gas (SNG).
The chemical equation of methanation reaction is:
CO+3H
2→CH
4+H
2O ΔH=-206kJ/mol
CO
2+4H
2→CH
4+2H
2O ΔH=-165kJ/mol
Visible, methanation is the reaction that a gas molecula number reduces, and high pressure will be conducive to CH
4generation, simultaneously synthetic gas methanation is the process of a strong heat release, by the violent temperature rise of the system of inducing reaction.Therefore, can be under High Temperature High Pressure long-time steady operation the methanation catalyst with high catalytic activity are one of key factors of technique.
The main Shi You of the commercialization synthetic gas full methanation catalyzer Britain of at present external comparative maturity wears dimension process technology (Davy Process Technology) company and the research and development of Denmark Top rope (Haldor Topsoe A/S) company.The CRG methanation catalyst of Dai Wei company (US Patent No. 4455391) is nickel catalyzator, and nickel content more than 50%, needs pre-desulfurization, during use, needn't regulate in advance the n (H in unstripped gas
2)/n (CO), lives for 250 ℃, 300～600 ℃ of optimal working temps, 700 ℃ of above inactivations.What big plain in u.s.a factory was used at present is exactly the methanation catalyst that Dai Wei company produces.The catalyzer of the Ye Shidaiwei company that Datang Keshiketeng Banner and Fuxin project are used.The MCR-2X methanation catalyst (English Patent GB2077613A) of rope company of Top is also nickel catalyzator, also needs pre-desulfurization, and need to adjust in advance n (H while using
2)/n (CO), Active components distribution, on ceramic monolith, still has higher activity above at 700 ℃.What energy He Qinghua Yining, Erdos project of converging was used is the catalyzer of rope company of Top.
It is domestic that what carry out synthetic gas full methanation catalyst research comparative maturity is Dalian Inst of Chemicophysics, Chinese Academy of Sciences and subordinate's thereof Dalian Pratt Chemical Technology Co., Ltd.They mainly comprise M348(Chinese patent CN88105142.X by the commercialized catalyst of exploitation) and M349(Chinese patent CN200810001419.3) two kinds of models.The main active component of two kinds of catalyzer is Ni, and carrier is Al
2o
3or TiO
2, auxiliary agent comprises Mn, Zr, Cr and RE etc.But the catalyzer of domestic-developed does not also have the report of industrial applications.All things considered, the most of realization production domesticization of core technology that the Production Flow Chart of coal preparing natural gas is related, only has the current domestic industrialized precedent that do not have of methanation technology.In order to realize as early as possible the production domesticization of gas maked coal whole process production technique, domestic Duo Jia unit is all actively developing the work of this respect.
Although the research about methanation process has had recent two decades both at home and abroad, there is part to have the use experience of large-scale industry project or pilot project, still have a lot of problems to need further research.First, because gaseous constituent difference after different process gasification is very large, as the 4th generation lurgi gasifier to produce crude synthesis gas component be CO:56%, H
2: 28%, CO
2: 4%, CH
4composition is generally higher 8%; It is CO:59% that Shell vapourizing furnace produces crude synthesis gas component, H
2: 28%, CO
2: 3.4%, CH
4: 0.9%; It is CO:45% that Texaco gasifier produces crude synthesis gas component, H
2: 33%, CO
2: 20%, CH
4: 0.2%, be applicable to the methanation process flow process of each gasification technology and its catalyzer used because the difference of gaseous constituent and load need to be done corresponding adjustment.Moreover, the full methanation catalyzer majority of research and development is in the laboratory study stage at present, need from now on to do a large amount of industrialization pilot scales than selecting optimization of catalysts and definite optimal processing parameter, and in general only have the catalyzer through steady running in thousands of hours just can enter the stage of large industrialized.Therefore, in order to provide one to be applicable to the thick synthesizer component of different gasification technologies, conveniently moving and can to reuse, and can assess the test set of efficiency and the energy consumption of different catalysts, therefore need to design a kind of portable producing synthesis gas from coal methanation catalyst converter test platform.
Utility model content
The problem existing in order to solve above-mentioned prior art, the purpose of this utility model is to provide a kind of packaged type producing synthesis gas from coal methanation catalyst test platform, can adapt to the test of different material gas composition, different operating condition, different catalysts; By this test platform can test and assess methanation process, operating parameters and catalyst performance.
For reaching above object, the utility model adopts following technical scheme:
A kind of packaged type producing synthesis gas from coal methanation catalyst test platform, comprise and can be placed on the gaseous fraction conversion of transportation in a freight container and purify the gentle body methanation of part part, described gaseous fraction conversion and purification portion are divided and are comprised sulfur resistant water gas changing device, middle temperature zinc oxide desulfurization device, gas and water separator and NaOH and 5A molecular sieve column decarbonization device, and described gas methanation is partly syllogic methanation reaction apparatus;
Described sulfur resistant water gas changing device comprises the electrical heating preheater A X101 being connected with gas surge tank V101, electrical heating preheater A X101 is connected with shift converter B T102 with the shift converter A T101 being in series after being connected with water vapor pipeline again, also comprises the gaseous media interchanger E101 being connected between electrical heating preheater X101 and middle temperature zinc oxide desulfurization device;
Described middle temperature zinc oxide desulfurization device comprises two thionizer A T103 that are in parallel and the thionizer B T104 being connected with shift converter B T102, wherein any one in thionizer A T103 and thionizer B T104 is standby thionizer, in thionizer A T103 and thionizer B T104, all places zinc oxide post;
Described gas and water separator comprises water medium interchanger E102 and the air water separator V102 being connected successively with gaseous media interchanger E101;
Described NaOH and 5A molecular sieve column decarbonization device comprise two molecular sieve tower A T105 that are in parallel and the molecular sieve tower B T106 being connected with air water separator V102, wherein any one in molecular sieve tower A T105 and molecular sieve tower B T106 is standby molecular sieve tower, in molecular sieve tower A T105 and molecular sieve tower B T106, all places NaOH and 5A molecular sieve column;
Described syllogic methanation reaction apparatus comprises interchanger A E103, the a mouth of described interchanger A E103 and molecular sieve tower A T105 are connected with the outlet after molecular sieve tower B T106 parallel connection, the d mouth of interchanger A E103 successively with electrical heating preheater B X102, methanator A R101 is connected with de-salted water interchanger B E104, the output terminal of de-salted water interchanger B E104 is connected with the c mouth of interchanger A E103, the b mouth of interchanger A E103 successively with methanator B R102, de-salted water interchanger C E105, methanator C R103 is connected with de-salted water interchanger D E106.
The parameter of described sulfur resistant water gas changing device arranges as follows: gas flow 0.8～4Nm
3/ h, quantitative watering steam and coal gas volume ratio are 0.2～0.7:1, shift converter A T101 and shift converter B T102 design height are 1.2 meters, aspect ratio is 4:1, material selection 304L, transformation catalyst loadings 100ml, catalyzer model is selected Co-Mo sulfur-tolerant catalyzer, and the operation air speed of shift converter A T101 and shift converter B T102 is 8000～40000h
-1, working temperature is 190～500 ℃, and design top temperature is 600 ℃, and operating pressure is 0.1～4Mpa, and design top pressure is 5Mpa.
The parameter of described middle temperature zinc oxide desulfurization device arranges as follows: gas flow is 0.8～4Nm
3/ h, zinc oxide column material adopts 304L, and working temperature is 100～500 ℃, design top temperature is 600 ℃, and operating pressure is 0.1～4Mpa, and design top pressure is 5Mpa, zinc oxide post loadings is 5L, selects middle temperature Zinc oxide desulfurizer, and operation air speed is 160～800h
-1, warm dry desulfurization during desulfurization adopts, by zinc oxide desulfurization, is down to total sulfur below 0.2ppm.
Water medium interchanger E102 in described gas and water separator adopts plate-type heat exchanger, and heat interchanging area is 0.8m
2, the volume of air water separator V102 is 200L.
The parameter of described NaOH and 5A molecular sieve column decarbonization device arranges as follows: in molecular sieve tower A T105 and molecular sieve tower B T106, gas flow is 0.8～4Nm
3/ h, NaOH and 5A molecular sieve column material selection 304L, working temperature is 35～100 ℃, and operating pressure is 0.1～4.5Mpa, and design top pressure is 5Mpa, and NaOH loadings is 2.5L, and 5A molecular sieve loadings is 2.5L, and operation air speed is 160～800h
-1.
The parameter of described syllogic methanation reaction apparatus arranges as follows: gas flow is 0.8～4Nm
3/ h, the material selection 304L of methanator A R101, methanator B R102 and methanator C R103, working temperature is 300～700 ℃, design top temperature is 800 ℃, operating pressure is 0.1～3Mpa, design top pressure is 5Mpa, and loaded catalyst is 100ml, and operation air speed is 8000～40000h
-1methanator A R101, methanator B R102 and methanator C R103 aspect ratio are selected between 6～3:1, interchanger A E103, de-salted water interchanger B E104, de-salted water interchanger C E105 and de-salted water interchanger D E106 select plate-type heat exchanger, heat interchanging area 1.5m
2.
Described test platform is applicable to lurgi gasifier, Texaco stove, Shell stove or coke-oven gas.
The testing method of a kind of packaged type producing synthesis gas from coal methanation catalyst test platform described above, by unstripped gas by analysis, metering is sent into gas buffer tank V101 after regulating, then after being heated to 200 ℃ of vapor mixing that make up water, electrical heating preheater A X101 enters shift converter A T101 and shift converter B T102, water vapor is 0.2～0.7:1 with feed gas volume ratio, converts the CO in gas to H
2and CO
2, adjust H
2: CO volume ratio is 2.9～3.1, then enter thionizer A T103 or thionizer B T104, desulfurization is to 0.2ppm, working off one's feeling vent one's spleen with the inlet gas of shift converter A T103 by gaseous media interchanger E101 heat exchange, with enter the separated moisture of air water separator V102 by water medium interchanger E102 heat exchange cooling after desulfurization, enter afterwards molecular sieve tower A T105 or molecular sieve tower B T106,5A molecular sieve adsorption CO
2to 20ppm, after reaching methanation reaction temperature requirement, be sent to methanator, pretreated gas after interchanger AE103 inner casing again through electrical heating preheater BX102, at 300 ℃, enter methanator A R101, in methanator A R101, most of carbon monoxide and hydrogen reaction generate methane and water, and emit large calorimetric, Outlet Gas Temperature is controlled in 600 ℃, by de-salted water interchanger B E104 cooling heat exchange, and then through interchanger A E103 cooling heat exchange, gas temperature enters methanator B R102 after reducing, the carbon monoxide of small part and hydrogen further react and generate methane and water, and heat release, after exit gas and de-salted water interchanger C E105 heat exchange, enter methanator C R103, the outlet synthetic gas of methanator C R103 obtains synthetic methane gas product after de-salted water interchanger D E106 is cooling, gaseous fraction directly draws after measuring that the torch district of getting back to factory lights or direct high row.
Compared to the prior art, tool has the following advantages the utility model:
1, the utility model platform suitability is strong, can be applicable to different sources of the gas, and to existing lurgi gasifier, Texaco stove, Shell stove, even coke-oven gas is all suitable for.This platform, for testing the best methanation reaction condition of various source of the gas situations, can adapt to the test of different material gas composition, different operating condition, different catalysts.By installing can test and assess methanation process, operating parameters and catalyst performance.
2, rational in infrastructure, the compact in design of platform design, device can be placed in a freight container, convenient transportation.
3, platform is provided with CO shift conversion step, without external pure H
2distribution.
4, testing method is selected and is different from the low-temperature rectisol technology that large scale industry gasifying device is conventional, has saved Multi-stage heat-exchanging device, refrigeration plant and cyclic regeneration device, is easy to the miniaturization of platform.And the desulfurization of selecting, dehydration and decarbonization method all do not need main equipment and complicated technology, can both in a device, complete, and be designed to the using and the reserved, be convenient to change assurance operation continuously.
5, advanced line translation moderate temperature desulphurization again, utilizes transformationreation liberated heat to reach the required temperature of ZnO moderate temperature desulphurization.
6, utilize the preheating of transformationreation liberated heat to enter the thick gas before conversion, utilize the preheating of methanation reaction liberated heat to enter the air-flow before methanation, except utilizing torch heating and when temperature declines concurrent heating when driving, all utilize system response self heat maintain each section temperature required.
7, methanator design adopts and forces to move hot mode the amount of heat of emitting after reaction is removed, and controls subsequent reactor bed temperature, prevents temperature runaway.
8, utilize the pressure of unstripped gas that motivating force is provided, without optional equipment supercharger.
9, sulfur resistant water gas changing device; Middle temperature zinc oxide desulfurization device; Gas and water separator; NaOH and 5A molecular sieve column decarbonization device can flexible operatings, according to field condition, can select to close and by-pass water gas reforming device, desulfurizer or decarbonization device.
Accompanying drawing explanation
Fig. 1 is the utility model test platform architecture schematic diagram.
Fig. 2 is the utility model testing method schema.
Embodiment
Below in conjunction with drawings and the specific embodiments, the utility model is described in further detail.
As shown in Figure 1, a kind of packaged type producing synthesis gas from coal of the utility model methanation catalyst test platform, comprise and can be placed on the gaseous fraction conversion of transportation in a freight container and purify the gentle body methanation of part part, described gaseous fraction conversion and purification portion are divided and are comprised sulfur resistant water gas changing device, middle temperature zinc oxide desulfurization device, gas and water separator and NaOH and 5A molecular sieve column decarbonization device, and described gas methanation is partly syllogic methanation reaction apparatus, described sulfur resistant water gas changing device comprises the electrical heating preheater A X101 being connected with gas surge tank V101, electrical heating preheater A X101 is connected with shift converter B T102 with the shift converter A T101 being in series after being connected with water vapor pipeline again, also comprises the gaseous media interchanger E101 being connected between electrical heating preheater X101 and middle temperature zinc oxide desulfurization device, described middle temperature zinc oxide desulfurization device comprises two thionizer A T103 that are in parallel and the thionizer B T104 being connected with shift converter B T102, wherein any one in thionizer A T103 and thionizer B T104 is standby thionizer, in thionizer A T103 and thionizer B T104, all places zinc oxide post, described gas and water separator comprises water medium interchanger E102 and the air water separator V102 being connected successively with gaseous media interchanger E101, described NaOH and 5A molecular sieve column decarbonization device comprise two molecular sieve tower A T105 that are in parallel and the molecular sieve tower B T106 being connected with air water separator V102, wherein any one in molecular sieve tower A T105 and molecular sieve tower B T106 is standby molecular sieve tower, in molecular sieve tower A T105 and molecular sieve tower B T106, all places NaOH and 5A molecular sieve column, described syllogic methanation reaction apparatus comprises interchanger A E103, the a mouth of described interchanger A E103 and molecular sieve tower A T105 are connected with the outlet after molecular sieve tower B T106 parallel connection, the d mouth of interchanger AE103 successively with electrical heating preheater B X102, methanator A R101 is connected with de-salted water interchanger B E104, the output terminal of de-salted water interchanger B E104 is connected with the c mouth of interchanger A E103, the b mouth of interchanger A E103 successively with methanator B R102, de-salted water interchanger C E105, methanator C R103 is connected with de-salted water interchanger D E106.
As preferred implementation of the present utility model, the parameter of described sulfur resistant water gas changing device arranges as follows: gas flow is 0.8～4Nm
3/ h, more preferably gas flow is 2～3Nm
3/ h, quantitative watering steam and coal gas volume ratio are 0.2～0.7:1, shift converter A T101 and shift converter B T102 design height are 1.2 meters, aspect ratio is 4:1, material selection 304L, transformation catalyst loadings 100ml, catalyzer is selected Co-Mo sulfur-tolerant shift catalyst, and the operation air speed of shift converter A T101 and shift converter B T102 is 8000～40000h
-1, working temperature is 190～500 ℃, and design top temperature is 600 ℃, and operating pressure is 0.1～4Mpa, and design top pressure is 5Mpa.More preferably operating air speed is 20000～30000h
-1, working temperature is 200～400 ℃, operating pressure is 1～2Mpa.
As preferred implementation of the present utility model, the parameter of described middle temperature zinc oxide desulfurization device arranges as follows: gas flow is 0.8～4Nm
3/ h, zinc oxide column material adopts 304L, and working temperature is 100～500 ℃, design top temperature is 600 ℃, and operating pressure is 0.1～4Mpa, and design top pressure is 5Mpa, zinc oxide post loadings is 5L, selects general middle temperature Zinc oxide desulfurizer, and operation air speed is 160～800h
-1, what in gas, catalyzer is harmful to is mainly sulphur, warm dry desulfurization during desulfurization adopts, by zinc oxide desulfurization, can be down to total sulfur below 0.2ppm.More preferably gas flow is 2～3Nm
3/ h, zinc oxide column material is selected 304L, and working temperature is 200～400 ℃, and operating pressure is 1.0～3.0Mpa, and operation air speed is 300～600h
-1.
As preferred implementation of the present utility model, the water medium interchanger E102 in described gas and water separator adopts plate-type heat exchanger, and heat interchanging area is 0.8m
2, the volume of air water separator V102 is 200L.In order to realize full methanation, improve the degree of depth of methanation reaction and prevent that other side reactions from carrying out (as CO conversion), need to reduce moisture, admittedly adopt cooling method to realize gas-water separation.
As preferred implementation of the present utility model, the parameter of described NaOH and 5A molecular sieve column decarbonization device arranges as follows: in molecular sieve tower A T105 and molecular sieve tower B T106, gas flow is 0.8～4Nm
3/ h, NaOH and 5A molecular sieve column material selection 304L, working temperature is 35～100 ℃, and operating pressure is 0.1～4.5Mpa, and design top pressure is 5Mpa, and NaOH loadings is 2.5L, and 5A molecular sieve loadings is 2.5L, and operation air speed is 160～800h
-1.More preferably gas flow is 2～3Nm
3/ h, working temperature is 50～80 ℃, and operating pressure is 2～3Mpa, and operation air speed is 400～600h
-1.Gas flow is due to CO in methanation reaction
2the H of reaction needed
2more, in order to guarantee H
2enough CO reactions, improve catalyzer to CO transformation efficiency, need to shift to an earlier date decarburization, and this device adopts NaOH and 5A molecular sieve to mix CO absorption at normal temperatures
2, and CO, H
2and CH
4can pass through.
The parameter of described syllogic methanation reaction apparatus arranges as follows: gas flow is 0.8～4Nm
3/ h, the material selection 304L of methanator A R101, methanator B R102 and methanator C R103, working temperature is 300～700 ℃, design top temperature is 800 ℃, operating pressure is 0.1～3Mpa, design top pressure is 5Mpa, and loaded catalyst is 100ml, and operation air speed is 8000～40000h
-1methanator A R101, methanator B R102 and methanator C R103 aspect ratio are selected between 6～3:1, interchanger A E103, de-salted water interchanger B E104, de-salted water interchanger C E105 and de-salted water interchanger D E106 select plate-type heat exchanger, heat interchanging area 1.5m
2.Preferred gas flow is 1～2Nm
3/ h, working temperature is 400～500 ℃, and operating pressure is 0.5～2Mpa, and operation air speed is 10000～20000h
-1, reactor aspect ratio is at 6～5:1.
Described test platform is applicable to lurgi gasifier, Texaco stove, Shell stove or coke-oven gas.
As shown in Figure 2, a kind of testing method of packaged type producing synthesis gas from coal methanation catalyst test platform, by unstripped gas by analysis, metering is sent into gas buffer tank V101 after regulating, then after being heated to 200 ℃ of vapor mixing that make up water, electrical heating preheater A X101 enters shift converter A T101 and shift converter B T102, water vapor is 0.2～0.7:1 with feed gas volume ratio, converts the CO in gas to H
2and CO
2, adjust H
2: CO volume ratio is 2.9～3.1, then enter thionizer A T103 or thionizer B T104, desulfurization is to 0.2ppm, working off one's feeling vent one's spleen with the inlet gas of shift converter A T101 by gaseous media interchanger E101 heat exchange, with enter the separated moisture of air water separator V102 by water medium interchanger E102 heat exchange cooling after desulfurization, enter afterwards molecular sieve tower A T105 or molecular sieve tower B T106,5A molecular sieve adsorption CO
2to 20ppm, after reaching methanation reaction temperature requirement, be sent to methanator, pretreated gas after interchanger AE103 inner casing again through electrical heating preheater B X102, at 300 ℃, enter methanator A R101, in methanator A R101, most of carbon monoxide and hydrogen reaction generate methane and water, and emit large calorimetric, Outlet Gas Temperature is controlled in 600 ℃, by de-salted water interchanger B E104 cooling heat exchange, and then through interchanger A E103 cooling heat exchange, gas temperature enters methanator B R102 after reducing, the carbon monoxide of small part and hydrogen further react and generate methane and water, and heat release, after exit gas and de-salted water interchanger C E105 heat exchange, enter methanator C R103, the outlet synthetic gas of methanator C R103 obtains synthetic methane gas product after de-salted water interchanger D E106 is cooling, gaseous fraction directly draws after measuring that the torch district of getting back to factory lights or direct high row.
Specific examples
Following gaseous fraction is volume percent.
Example one
The coal gas that this example is used Shell vapourizing furnace to produce is source of the gas, and its gaseous fraction is as shown in table 1 below:
Table 1
| CO 2 | 2.98% |
| CO | 51.19% |
| H 2 | 23.15% |
| N 2 | 8.34% |
| Ar | 0.10% |
| H 2S | 0.13% |
| COS | 0.01% |
| HCN | 0.002 |
| CH 4 | 0.77% |
| NH 3 | 0.01% |
| H 2O | 13.33% |
1) sulfur resistant water gas changing device becomes desired value by hydrogen in coal gas and carbon monoxide ratio
Gas temperature is 160 ℃, and pressure is 2.8Mpa.Coal gas is with 3Nm
3first the flow of/h passes through gas buffer tank V101, takes off most of moisture.Then through electrical heating preheater A X101, be heated to 200 ℃, through indication, control the under meter FTC101 steam that makes up water, the volume ratio of water vapor and coal gas is 0.21, after mixing, enter shift converter A T101, the gas that shift converter A X101 processes is controlled the under meter FTC102 steam that makes up water through indication, the volume ratio of water vapor and coal gas is 0.24, enters shift converter B T102 after mixing, and the operation air speed of shift converter A T101 and shift converter B T102 is 30000h
-1, temperature is that 300 ℃, pressure are 1.5Mpa, the H after twice conversion in gas
2: CO is 3 than 46.65/15.50.Change processing parameter as shown in table 2 below:
Table 2
2) in, warm zinc oxide desulfurization device is brought down below 0.2ppm by sulphur content
Coal gas after water-gas shift is with 2Nm
3the flow of/h enters thionizer A T103 or thionizer BT104, and in temperature, being 200 ℃ is zinc oxide and H under 2.0Mpa with pressure
2s reaction generates ZnS desulfurization, the H of thionizer outlet
2s concentration is down to below 0.2ppm.
3) moisture in the separated coal gas of gas and water separator
Therefrom warm zinc oxide desulfurization device gas out and the inlet gas heat exchange of shift converter A T101, with enter the separated moisture of air water separator V102 by circulation tap water heat exchange cooling.
4) NaOH and the decarburization of 5A molecular sieve column decarbonization device are lower than 20ppm
Coal gas through gas-water separation enters molecular sieve tower A T105 or molecular sieve tower B T106, and the NaOH loading in tower and 5A molecular sieve dual function can active adsorption CO
2to 20ppm.
5) syllogic methanator carries out gas methanation reaction
Through the pretreated gas of last device after interchanger A E103 inner casing again through electrical heating preheater BX102, at 300 ℃, enter methanator A R101, in methanator A R101, most of carbon monoxide and hydrogen reaction generate methane and water, and emit large calorimetric, Outlet Gas Temperature is controlled in 600 ℃, by de-salted water interchanger B E104 cooling heat exchange, and then through interchanger A E103 cooling heat exchange, gas temperature enters methanator B R102 after reducing, the carbon monoxide of small part and hydrogen further react and generate methane and water, and heat release, after exit gas and the heat exchange of circulation de-salted water, enter methanator CR103, the outlet synthetic gas of methanator C R103 obtains synthetic methane gas product after circulation de-salted water is cooling.It is as shown in table 3 below that gaseous fraction is measured variation:
Table 3
Example two:
The coal gas that this example is used Lurgi gasifier to produce is source of the gas.Its gaseous fraction is as shown in table 4 below:
Table 4
| CO 2 | 2.98% |
| CO | 43.19% |
| H 2 | 22.15% |
| N 2 | 8.34% |
| Ar | 0.10% |
| H 2S | 0.13% |
| COS | 0.01% |
| HCN | 0.002 |
| CH 4 | 9.87% |
| NH3 | 0.01% |
| H 2O | 13.33% |
1) sulfur resistant water gas changing device becomes desired value by coal gas hydrogen and carbon monoxide ratio
Gas temperature is 160 ℃, and pressure is 2.8Mpa.Coal gas is with 2.5Nm
3first the flow of/h passes through gas buffer tank V101, takes off most of moisture.Then through electrical heating preheater A X101, be heated to 200 ℃, through indication, control the under meter FTC101 steam that makes up water, the volume ratio of water vapor and coal gas is 0.21, after mixing, enter shift converter A T101, the gas of shift converter A conversion is controlled the under meter FTC102 steam that makes up water through indication, the volume ratio of water vapor and coal gas is 0.24, enters shift converter B T102 after mixing, and the operation air speed of shift converter A T101 and shift converter B T102 is 25000h
-1, temperature is that 280 ℃, pressure are 1.6Mpa, the H after twice conversion in gas
2: CO is 2.96 than 45.95/15.50.Change processing parameter as shown in table 5 below:
Table 5
2) in, warm zinc oxide desulfurization device is brought down below 0.2ppm by sulphur content
Coal gas after water-gas shift is with 3Nm
3the flow of/h enters thionizer A T103 or thionizer BT104,200 ℃ with 3.0Mpa under zinc oxide and H
2s reaction generates ZnS desulfurization, the H of thionizer outlet
2s concentration is down to below 0.2ppm.
3) moisture in the separated coal gas of gas and water separator
Therefrom warm zinc oxide desulfurization device gas out and the inlet gas heat exchange of shift converter A T101, with enter the separated moisture of air water separator V102 by circulation tap water heat exchange cooling.
4) NaOH and the decarburization of 5A molecular sieve column decarbonization device are lower than 20ppm
Coal gas through steam separation enters molecular sieve tower A T105 or molecular sieve tower B T106, and the NaOH loading in tower and 5A molecular sieve dual function can active adsorption CO
2to 20ppm.
5 syllogic methanators carry out gas methanation reaction
Through the pretreated gas of last device after interchanger A E103 inner casing again through electrical heating preheater BX102, in methanator A R101, most of carbon monoxide and hydrogen reaction generate methane and water, and emit large calorimetric, Outlet Gas Temperature is controlled in 600 ℃, by de-salted water interchanger B E104 cooling heat exchange, and then through interchanger A E103 cooling heat exchange, gas temperature enters methanator B R102 after reducing, the carbon monoxide of small part and hydrogen further react and generate methane and water, and heat release, after exit gas and the heat exchange of circulation de-salted water, enter methanator C R103, the outlet synthetic gas of methanator C R103 obtains synthetic methane gas product after circulation de-salted water is cooling.It is as shown in table 6 below that gaseous fraction is measured variation:
Table 6
Example three:
This example is used the on-the-spot coal synthetic gas source of the gas having purified, and water-gas shift, desulfurization, dehydration, decarbonization device, without unlatching, are only opened methanator section.
Coal synthesis gas after interchanger A E103 inner casing again through electrical heating preheater B X102, at 300 ℃, enter methanator A R101, in methanator A R101, most of carbon monoxide and hydrogen reaction generate methane and water, and emit large calorimetric, Outlet Gas Temperature is controlled in 600 ℃, by de-salted water interchanger B E104 cooling heat exchange, and then through interchanger A E103 cooling heat exchange, gas temperature enters methanator B R102 after reducing, the carbon monoxide of small part and hydrogen further react and generate methane and water, and heat release, after exit gas and the heat exchange of circulation de-salted water, enter methanator C R103, the outlet synthetic gas of methanator C R103 obtains synthetic methane gas product after circulation de-salted water is cooling.It is as shown in table 7 below that gaseous fraction is measured variation:
Table 7
Example four:
The coal gas that this example is used Lurgi gasifier to produce is source of the gas, but does not open decarbonization device, only moves water-gas shift, desulfurization and dewatering unit.Its gaseous fraction is as shown in table 8 below:
Table 8
| CO 2 | 2.98% |
| CO | 43.19% |
| H 2 | 22.15% |
| N 2 | 8.34% |
| Ar | 0.10% |
| H 2S | 0.13% |
| COS | 0.01% |
| HCN | 0.002 |
| CH 4 | 9.87% |
| NH3 | 0.01% |
| H 2O | 13.33% |
1) sulfur resistant water gas changing device becomes desired value by coal gas hydrogen and carbon monoxide ratio
Gas temperature is 160 ℃, and pressure is 2.8Mpa.Coal gas is with 2.3Nm
3first the flow of/h passes through gas buffer tank V101, takes off most of moisture.Then through electric heater A X101, be heated to 200 ℃, through indication, control the under meter FTC101 steam that makes up water, the volume ratio of water vapor and coal gas is 0.21, after mixing, enter shift converter A T101, the gas that shift converter A X101 processes is controlled the under meter FTC102 steam that makes up water through indication, the volume ratio of water vapor and coal gas is 0.24, enters shift converter B T102 after mixing, and the operation air speed of shift converter A T101 and shift converter B T102 is 23000h
-1, temperature is that 320 ℃, pressure are 1.2Mpa, the H after twice conversion in gas
2: CO is 2.96 than 45.95/15.50.Change processing parameter as shown in table 9 below:
Table 9
In 2, warm zinc oxide desulfurization device is brought down below 0.2ppm by sulphur content
Coal gas after water-gas shift is with 3.5Nm
3the flow of/h enters thionizer A T103 or thionizer BT104, at 200 ℃ with 1.0Mpa under zinc oxide and H
2s reaction generates ZnS desulfurization, the H of thionizer outlet
2s concentration is down to below 0.2ppm.
Moisture in the separated coal gas of 3 gas and water separators
Therefrom warm zinc oxide desulfurization device gas out and the inlet gas heat exchange of shift converter A T101, with enter the separated moisture of air water separator V102 by circulation tap water heat exchange cooling.
4 syllogic methanators carry out gas methanation reaction
Through the pretreated gas of last device after interchanger A E103 inner casing again through electrical heating preheater BX102, at 300 ℃, enter methanator A R101, in methanator A R101, most of carbon monoxide and hydrogen reaction generate methane and water, and emit large calorimetric, Outlet Gas Temperature is controlled in 600 ℃, by de-salted water interchanger B E104 cooling heat exchange, and then through interchanger A E103 cooling heat exchange, gas temperature enters methanator B R102 after reducing, the carbon monoxide of small part and hydrogen further react and generate methane and water, and heat release, after exit gas and the heat exchange of circulation de-salted water, enter methanator CR103, the outlet synthetic gas of methanator C R103 obtains synthetic methane gas product after circulation de-salted water is cooling.It is as shown in table 10 below that gaseous fraction is measured variation:
Table 10
Claims (4)
1. a packaged type producing synthesis gas from coal methanation catalyst test platform, it is characterized in that: comprise and can be placed on the gaseous fraction conversion of transportation in a freight container and purify the gentle body methanation of part part, described gaseous fraction conversion and purification portion are divided and are comprised sulfur resistant water gas changing device, middle temperature zinc oxide desulfurization device, gas and water separator and NaOH and 5A molecular sieve column decarbonization device, and described gas methanation is partly syllogic methanation reaction apparatus;
Described sulfur resistant water gas changing device comprises the electrical heating preheater A(X101 being connected with gas surge tank (V101)), electrical heating preheater A(X101) be connected with water vapor pipeline after again with the shift converter A(T101 being in series) with shift converter B(T102) be connected, also comprise the gaseous media interchanger (E101) being connected between electrical heating preheater (X101) and middle temperature zinc oxide desulfurization device;
Described middle temperature zinc oxide desulfurization device comprises and shift converter B(T102) two thionizer A(T103 that are in parallel being connected) and thionizer B(T104), thionizer A(T103 wherein) and thionizer B(T104) in any one be standby thionizer, thionizer A(T103) and thionizer B(T104) in all place zinc oxide post;
Described gas and water separator comprises water medium interchanger (E102) and the air water separator (V102) being connected successively with gaseous media interchanger (E101);
Described NaOH comprises with 5A molecular sieve column decarbonization device two molecular sieve tower A(T105 that are in parallel that are connected with air water separator (V102)) and molecular sieve tower B(T106), molecular sieve tower A(T105 wherein) and molecular sieve tower B(T106) in any one be standby molecular sieve tower, molecular sieve tower A(T105) and molecular sieve tower B(T106) in all place NaOH and 5A molecular sieve column;
Described syllogic methanation reaction apparatus comprises interchanger A(E103), described interchanger A(E103) a mouth and molecular sieve tower A(T105) with molecular sieve tower B(T106) outlet after parallel connection is connected, interchanger A(E103) d mouth successively with electrical heating preheater B(X102), methanator A(R101) with de-salted water interchanger B(E104) be connected, de-salted water interchanger B(E104) output terminal and interchanger A(E103) c mouth be connected, interchanger A(E103) b mouth successively with methanator B(R102), de-salted water interchanger C(E105), methanator C(R103) with de-salted water interchanger D(E106) be connected.
2. a kind of packaged type producing synthesis gas from coal methanation catalyst test platform according to claim 1, it is characterized in that: the shift converter A(T101 of described sulfur resistant water gas changing device) and shift converter B(T102) design height is 1.2 meters, aspect ratio is 4:1.
3. a kind of packaged type producing synthesis gas from coal methanation catalyst test platform according to claim 1, is characterized in that: the water medium interchanger (E102) in described gas and water separator adopts plate-type heat exchanger, and heat interchanging area is 0.8m
2, the volume of air water separator (V102) is 200L.
4. a kind of packaged type producing synthesis gas from coal methanation catalyst test platform according to claim 1, it is characterized in that: the methanator A(R101 of described syllogic methanation reaction apparatus), methanator B(R102) and methanator C(R103) aspect ratio selects between 6～3:1, interchanger A(E103), de-salted water interchanger B(E104), de-salted water interchanger C(E105) and de-salted water interchanger D(E106) select plate-type heat exchanger, heat interchanging area 1.5m
2.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103468336A (en) * | 2013-08-23 | 2013-12-25 | 中国华能集团清洁能源技术研究院有限公司 | Movable coal synthesis gas metnanation catalyst testing platform and testing method |
| CN106794438A (en) * | 2014-10-15 | 2017-05-31 | 托普索公司 | It is used for the containment system of the device of catalyst protection with the safety interlock tripping operation in reactor or down periods |
| CN109799322A (en) * | 2019-03-12 | 2019-05-24 | 中国华能集团清洁能源技术研究院有限公司 | A kind of multifunctional coal gasification experiment test device |
-
2013
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103468336A (en) * | 2013-08-23 | 2013-12-25 | 中国华能集团清洁能源技术研究院有限公司 | Movable coal synthesis gas metnanation catalyst testing platform and testing method |
| CN103468336B (en) * | 2013-08-23 | 2014-11-19 | 中国华能集团清洁能源技术研究院有限公司 | Movable coal synthesis gas metnanation catalyst testing platform and testing method |
| CN106794438A (en) * | 2014-10-15 | 2017-05-31 | 托普索公司 | It is used for the containment system of the device of catalyst protection with the safety interlock tripping operation in reactor or down periods |
| CN106794438B (en) * | 2014-10-15 | 2020-03-17 | 托普索公司 | Container system with means for catalyst protection during safety interlock tripping or shutdown of reactor |
| CN109799322A (en) * | 2019-03-12 | 2019-05-24 | 中国华能集团清洁能源技术研究院有限公司 | A kind of multifunctional coal gasification experiment test device |
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