CN204689634U - For the production of the equipment of the synthetic gas of the process containing carbonic acid gas and hydrogen - Google Patents
For the production of the equipment of the synthetic gas of the process containing carbonic acid gas and hydrogen Download PDFInfo
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- CN204689634U CN204689634U CN201520116309.7U CN201520116309U CN204689634U CN 204689634 U CN204689634 U CN 204689634U CN 201520116309 U CN201520116309 U CN 201520116309U CN 204689634 U CN204689634 U CN 204689634U
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Abstract
The utility model relates to a kind of equipment of the synthetic gas for the production of the process containing carbonic acid gas and hydrogen, described equipment comprises with lower unit: (a) is at least one gasifier level of obtained crude synthesis gas stream or at least one reformer level, b CO transformationreation section that () is connected with at least one gasifier level described or reformer level fluid, described CO transformationreation section at least comprises the first shift-converter comprising transformation catalyst, described CO transformationreation section is suitable for the synthesis air-flow crude synthesis gas be under CO conversion condition circulation being turned to the process be under CO conversion condition, (c) device of synthesis air-flow for crossing from described CO transformationreation section extraction process, the feature of described equipment is, described first shift-converter comprises the sub-reactor of at least two parallel runnings, wherein said at least two sub-reactors comprise the described transformation catalyst of different volumes.This equipment is more flexible, work system is better.
Description
Technical field
The utility model relates to a kind of for run out of CO but enrichment hydrogen (H by making crude synthesis gas (synthetic gas) react with water in the presence of a catalyst to be circulated by the crude synthesis gas containing carbon monoxide (CO) to turn to according to so-called CO conversion or CO conversion reaction
2) and carbonic acid gas (CO
2) the equipment of synthesis air-flow.On the other hand, the utility model relates to the equipment that a kind of downstream being suitable for multistage reformer especially in integral type reformer apparatus or gasifier performs CO transformationreation.
One of the purpose of this utility model is the embodiment proposing to allow especially to perform under various synthetic gas load as the downstream process of multistage reformer apparatus or equipment for gasification the equipment of this reaction, and wherein different reformer levels or gasifier level may not be that all operations simultaneously and/or the flow (flow rate) of crude synthesis gas that receives from reformer level or gasifier level may change.
Background technology
CO transformationreation is inherently well-known in chemical technology field.The universal of the CO transformationreation in the situation of reformer apparatus or equipment for gasification and application can in " Gasification (gasification) " of textbook as C.Higman and M.van der Burgt 8.3 " Encyclopedia of Industrial Chemistry (industrial chemistry encyclopaedia) " (sixth versions saving " CO shift (CO conversion) " (Gulf Professional Publishing (Elsevier) 2003) or Ullmann, electronic version in 1998, keyword " Ammonia ", 4.5.1.2 " Carbon Monoxide Shift Conversion (carbon monodixe conversion conversion) " and keyword " Hydrogen " is saved, 4.1.2.2 save " Gasification of Liquid and Gaseous Hydrocarbons the gasification of hydrocarbon gas (liquid and) ") in find.CO conversion is widely used in being designed to the reformer apparatus producing ammonia synthesis gas because will ammonia synthesis be carried out, must from reform or gasifying process crude synthesis gas thoroughly remove carbon monoxide.
CO transformationreation
CO+H
2O=CO
2+H
2
The strong exothermic process of to be standard reaction enthalpy be-41.2kJ/mol.It can at much lower temperature as the additional and independent course work from gasifier or reformer to revise the H of synthetic gas
2/ CO ratio or make total hydrogen maximum production of unit.As seen from above-mentioned reaction formula, a mol of hydrogen can be obtained from every mole of CO.This reaction this as equimolar and therefore do not rely on pressure to a great extent.Favors low temperature is in the balance of hydrogen manufacturing.The typical equilibrium concentration of CO is low; Such as, for the steam gas ratio of 0.4, be 0.2vol% and at 200 DEG C for 0.12vol% at 220 DEG C.
CO transformationreation utilizes multiple catalysts between 200 DEG C to 500 DEG C with sufficient speed of reaction effect.The type of catalyzer is distinguished with quality, the especially sulphur content of the synthetic gas that will transform by their operative temperature scope.
Conventional high temperature conversion (HT conversion) uses and typically uses chromium and use the catalyzer based on ferric oxide that copper promotes recently.The sphere of action of these catalyzer is between 300 DEG C and 500 DEG C.When far above 500 DEG C, catalyzer causes the sintering of catalyst deactivation.The sulphur of the maximum about 100vol-ppm of HT transformation catalyst tolerance practical limit, but be easy to lose physical strength, particularly when the amount of sulphur changes.In reaction engineering, this reaction performs usually in some levels of series operation, carries out intermediate radiator between each catalyst bed that this reaction wherein adiabatically runs, to avoid too high catalyst temperature and to realize favourable balance.
Low temperature shift (LT conversion) operates and uses copper-zinc-Al catalysts in the temperature range of 200 DEG C to 270 DEG C.It for major part based on the ammonia equipment of steam reformation so that residual CO is reduced to about 0.3mol%, this is the requirement of downstream methanator.The catalyzer used is very responsive to sulphur, and even inputs the H of 0.1vol-ppm in gas
2s in the course of time catalyzer by poisoning.In addition, catalyzer is also responsive to water condensation.Near dew point, operation will cause capillary condensation and thus damage catalyzer.For the dew point of about 215 DEG C and the temperature rise of 25 to 30 DEG C, the error margin when the recrystallize of copper catalyst starts under the upper temperature limit of 270 DEG C is few.
In the legacy equipment concept of the CO conversion in methane steam reforming (SMR) equipment, steam is heated up and overheated used heat and the cooled gas from secondary reformation device enter the HT shift-converter being filled with iron-chrome catalysts 320 to 350 DEG C time by reclaiming.After the intensification of about 50 to 70 DEG C (depending on initial CO concentration) and when residual CO content is about 3%, gas is cooled to 200 to 210 DEG C subsequently to carry out LT conversion, and this LT converts and copper-zinc-Al catalysts in downstream reaction container performs and realizes the carbon monoxide concentration of 0.1 to 0.3vol%.
Having developed can converting under high temperature out (300 DEG C) copper-zinc-Al catalysts of improvement of effect than conventional LT, especially for waiting thermal reactor.This process is called middle temperature transformation (MT conversion).Described the application in reformer apparatus, and the application in equipment for gasification is unknown.
For expecting application crude synthesis gas being performed to CO conversion, the cobalt-molybdenum catalyzer being differently described as " acid conversion " or " dirty conversion " catalyzer can be used.This catalyzer is resistant to sulfur, because under it needs the sulphur in feed gas that it is maintained active sulfided state.It is usually shrend after-applied of crude synthesis gas, and described shrend typically will provide infiltration to have sufficient water to carry out the gas being in about 250 DEG C of transformationreation when not adding any steam further.For ammonia application, thick gas conversion is typically configured to two or three adiabatic reactors, and wherein intercooling causes the residual CO of about 1.6 or 0.8mol% respectively.The important subsidiary effect of thick gas conversion catalyzer one is the ability of its process other impurity gasification properties many.COS and other organosulfur compound major part are converted into H
2s, this task of making downstream sour gas remove (AGR) becomes easy.HCN and any unsaturated hydrocarbons are hydrogenated.Carbonyl decomposition is also precipitated as sulfide, which increases the pressure drop across bed.The selective removal of the arsenic in feed is also described in prior art.
Have highly active conventional acid transformation catalyst for transform comprise high concentration CO (such as, the about 60mol% to 70mol% when drying) crude synthesis gas application in, CO shift-converter starting and turn off between working life and there will be temperature great change.In order to tackle this situation, such as, in the arrangement that some adiabatic reactor levels are connected in series when inter-stage exists intermediate radiator, common practice the first shift-converter level is in the flowing direction divided into two sub-reactors in parallel, such as, instruct in European patent specification 0 121 928 B1.In this type of design, every sub-reactor comprises multiple, such as two catalyst beds, and described catalyst bed has the internal by-pass around the first catalyst bed in the direction of the air flow.Typically, also there is another the main bypass across two the first varitron reactors in parallel.This design schematically shows in FIG.
At the scene in practical application, carry out this device of Non-follow control often through the thick gas flow by each catalyst bed of hand control valve restricted passage regulated for respective flow path.Operator's experience is depended in the reasonable application of the method; Thus, unexpected in reactor temperature overshoot probability is higher.The another shortcoming of visible is the bilayer of reactor design due to catalyst bed, the supporting device for catalyst bed and for the large-scale segregaion valve that controls the flowing in main line and by-pass line and extra ducts and the additional investment cost needed.
Utility model content
Therefore, an object of the present utility model is to provide and a kind ofly run out of CO but enrichment hydrogen (H for being converted into by crude synthesis gas according to CO transformationreation of upstream device especially as multistage gasifier or reformer plants
2) and carbonic acid gas (CO
2) the equipment of synthesis air-flow, wherein different gasifier levels or reformer level can not all operation simultaneously and/or the flow alterable of crude synthesis gas that receive from reformer level.
Above-mentioned purpose is realized by a kind of like this equipment of the synthetic gas for the production of the process containing carbonic acid gas and hydrogen, and described equipment comprises with lower unit:
(a) at least one gasifier level of obtained crude synthesis gas stream or at least one reformer level,
B CO transformationreation section that () is connected with at least one gasifier level described or reformer level fluid, this CO transformationreation section at least comprises the first shift-converter comprising transformation catalyst, this CO transformationreation section is suitable for the synthesis air-flow crude synthesis gas be under CO conversion condition circulation being turned to the process be under CO conversion condition
(c) device of synthesis air-flow for crossing from CO transformationreation section extraction process,
The feature of described equipment is, the first shift-converter comprises the sub-reactor of at least two parallel runnings, and wherein said at least two sub-reactors comprise the transformation catalyst of different volumes.
No matter fluid between two of reformer tubes regions connects the connection being interpreted as making any region between two parties of fluid such as crude synthesis gas stream or the synthesis air-flow that processed or component can both flow to any type in another region from a region two regions.
Adiabatic reactor work is interpreted as such reactor work: it is characterized in that, except the convective heat flow entered with feed conductance, be supplied to reactor without external energy, and in addition by structural measure, such as by installing heat-proof device and reduce or the heat exchange of even total ban reactor and surrounding.
CO converts condition and is interpreted as realizing crude synthesis gas composition according to CO transformationreation formula CO+ H
2o=CO
2+ H
2the reaction conditions of at least part of conversion.Those skilled in the art is from the principle of such as above-mentioned these conversion conditions of literature.Can for relevant work requirement such as giving the component of stream or making necessary adjustment for the type of used catalyzer to these conditions based on routine test.
To CO conversion, especially sour gas converts in effective catalyzer principle is known for the skilled person and can trade buys for multiple different application.Professional selects suitable transformation catalyst according to the temperature of reaction that will adopt (HT/MT/LT conversion) with for special applications as acidity/visceral-qi body CO converts.
Device for the synthesis air-flow crossed from CO transformationreation section extraction process is interpreted as being suitable for any device of this purposes, the pipeline that especially can combine as gas blower or pump with e Foerderanlage or piping system.
Gasifier level or reformer level are interpreted as localized area or the space of generating gasification or reforming reaction.Term " level " should not be construed as and means there is any specific interconnected with other level, and such as whether described level is connected in series or in parallel.
The utility model is based on the fact of the strong heat release of CO transformationreation as above.Thus, the flow leading to the crude synthesis gas of CO shift-converter about given catalyzer total amount change---namely changes the space velocity of crude synthesis gas---and may cause high temperature fluctuation.Especially, under the situation that flow is too low for catalyst volume, molecular balance will be set up and release reaction is warm in small portion catalyst bed.The temperature overshoot caused in this catalyst bed section and focus are emerged by this, and finally cause too early catalyst deactivation due to the thermal ageing of catalyzer in this position or sintering.This effect is relevant with any reactor design in principle, but especially serious when the insulation fix bed reactor generally adopted due to its simple and cheap design in CO transformationreation.As the means alleviating this effect, use as shown in Figure 1 and the reactor design be described in the prior art, wherein the first shift-converter is divided into such as two sub-reactors in parallel, it comprises such as two catalyst beds separately, the flow wherein leading to each sub-reactor can regulate by valve, and the first catalyst bed arranged in the flowing direction can be bypassed.Operator's experience is depended in the reasonable application of the method; Therefore, the probability of unexpected in reactor temperature overshoot is higher.Visible another shortcoming is the bilayer of reactor design due to catalyst bed, the supporting device for catalyst bed, for controlling the large-scale segregaion valve of the flowing in main line and by-pass line and extra ducts and the additional investment cost needed.
In context of the present utility model, found advantageously by the first shift-converter---it is designed to independent reactor or a series of coherent first of CO shift-converter level, the reactor grade of most upstream for the downstream that to be such as arranged in multistage reformer or gasifier unit---be designed to comprise the sub-reactor of at least two parallel runnings, wherein said at least two sub-reactors comprise the transformation catalyst of different volumes.Crude synthesis gas flow such as crude synthesis gas prepare section (i.e. gasifier level in succession or reformer level) starting or close down period change time this allows greater flexibility.Larger crude synthesis gas stream can be transported to the sub-reactor of the comparatively large vol part comprising CO transformation catalyst, and less crude synthesis gas stream can be transported to the sub-reactor of the smaller size smaller part comprising CO transformation catalyst.Advantage is, in two schemes, little compared with the situation being all sent to identical catalyst volume with the deviation of the design load of optimal spatial speed and the crude synthesis gas being such as filled with large discharge or low discharge in the arrangement of the catalyzer of identical amount symmetrically at two sub-reactors.This causes less temperature overshoot and thus causes thermal stresses less in catalyzer and reactor material.
Preferred aspect of the present utility model
About according to equipment of the present utility model, find that favourable part is, if to gasify at least one gasifier to stream by making carbon containing carry out obtained crude synthesis gas stream, and crude synthesis gas stream comprises CO and the acid gas component of at least 50mol%, preferably 60 to 70mol%, then CO transformationreation section comprises sour transformation catalyst.Especially in these conditions, the thermal discharge of per unit volume catalyzer is high, and when crude synthesis gas flow rate fluctuation, the trend of temperature overshoot is high equally.If perform this reaction in adiabatic reactor, then this trend is more obvious.
According in the another preferred embodiment of equipment of the present utility model, first shift-converter is made up of the sub-reactor of two parallel runnings, and the catalyst volume wherein in these two sub-reactors exists with the ratio of 2/3rds in three/a pair second sub-reactors in a sub-reactor.This embodiment for wherein in the gasifier level and/or reformation level of multiple series connection and/or parallel running obtained crude synthesis gas stream work flow in time advantageous particularly.
According in another preferred embodiment of equipment of the present utility model, obtained crude synthesis gas stream in the gasifier level and/or reformation level of multiple series connection and/or parallel running.It is advantageous particularly when the present embodiment is in the work flow for comprising the first shift-converter, described first shift-converter is made up of the sub-reactor of two parallel runnings, and the catalyst volume wherein in these two sub-reactors exists with the ratio of 2/3rds in three/a pair second sub-reactors in a sub-reactor.Especially in the integral type synthesis gas equipment that crude synthesis gas stream is obtained in three gasifier levels and/or reformation level, the present embodiment allows the starting of such as producing at crude synthesis gas or closes down period distributes different choice from crude synthesis gas streams to two CO varitron reactors and scheme, as will be illustrated in exemplary embodiment below.
Particularly preferably being, comprising adiabatic reactor according to equipment of the present utility model, is especially the fact of adiabatic reactor about the sub-reactor of at least two in the first shift-converter.Adiabatic reactor is favourable due to their simple structures; But because they comprise heat-proof device to reduce the fact of the thermosteresis from inside reactor to environment, they are quite responsive to temperature overshoot.Thus, they are particularly suited for working in combination with according to equipment of the present utility model.
More development plans of the present utility model, advantage and possible application can also obtain from following exemplary embodiment and example and the description of the drawings.Illustrated and/or all structural feature the utility model of illustrating itself or arbitrary combination of the present utility model.
Accompanying drawing explanation
In the accompanying drawings:
Fig. 1 schematically shows the CO conversion equipment according to prior art (comparative examples),
Fig. 2 schematically shows according to CO conversion equipment of the present utility model.
Embodiment
In FIG, flow through from the not shown crude synthesis gas comprising the multistage coal gasification unit reception of three gasifier levels and be sent to heat exchanger 2 by pipeline 1, this heat exchanger is used for temperature to be adjusted to CO transformationreation temperature.After over-heat-exchanger 2, crude synthesis gas flows through and is directed into by pipeline 3 the CO transformationreation section be made up of two symmetrical sub-reactor 7a, 7b.Crude synthesis gas flows through and is controlled by valve 6a, 6b to the flowing of sub-reactor 7a, 7b by pipeline 5a, 5b.Two sub-reactors all comprise two catalyst beds, and each catalyst bed comprises the catalyst volume identical with other catalyst bed.Thus, the total catalyst volume existed about optimal spatial speed in two sub-reactors distributes with equal catalyst volume on four catalyst beds.In addition, two sub-reactors are all equipped with by-pass line 11a, 11b and valve 12a, 12b with around corresponding first catalyst bed making crude synthesis gas stream and get around in the flowing direction.
From CO transformationreation section run out of carbon monoxide about crude synthesis gas stream and the synthetic gas of the process of enrichment hydrogen and carbonic acid gas flows through and is extracted by pipeline 8a, 8b and valve 9a, 9b, concentrate in pipeline 10, and be sent to other process level optional, such as additional CO conversion stage itself is exactly known and not shown in the drawings.
By shut-off valve 4a, 4b and valve 9a, 9b open normally closed valve 13 and get around whole CO transformationreation section via pipeline 10 alternatively.
When three gasifier levels in parallel are started, at different levelsly usually in succession to start.Thus, the operating mode that gasifier unit runs with 1/3rd of its full scale production ability or 2/3rds will be there is, any one or two work wherein in three gasifier levels.The process that the CO of the crude synthesis gas stream received under these operation element patterns in downstream converts section is had any problem in the adjustment of optimal spatial speed.In 1/3rd throughput schemes, operator can select crude synthesis gas stream to be all directed to one or two catalyst bed---and two kinds of selections are suboptimums with regard to the adjustment of optimal spatial speed, or alternatively, can select to regulate by variable valve 6a, 6b the flow leading to the crude synthesis gas stream of a sub-reactor.The key that a rear method performs is experience and the technology of operator, and operator are easy to make mistakes.
Equally, in 2/3rds throughput schemes, operator can select crude synthesis gas stream to be directed to two catalyst beds, such as one complete sub-reactor, or be directed to three catalyst beds, the first such as complete sub-reactor adds the downstream bed of the second sub-reactor, and the upstream bed of the second sub-reactor is bypassed.Equally, two kinds of selections are all suboptimums with regard to the adjustment of optimal spatial speed.
Schematically showing in the Fig. 2 according to CO conversion equipment of the present utility model, the crude synthesis gas received from the not shown multistage gasifier unit comprising three gasifier levels in parallel flows through and is sent to heat exchanger 2 by pipeline 1, and this heat exchanger is used for temperature to be adjusted to CO transformationreation temperature.After over-heat-exchanger 2, crude synthesis gas flows through and is directed into by pipeline 3 the CO transformationreation section be made up of two that possess different catalysts volume reactor 7a, 7b.Two sub-reactors all respectively comprise an only catalyst bed, wherein reactor 7a about optimal spatial speed comprise total catalyst volume 2/3rds and reactor 7b comprise its 1/3rd.According in this example of the present utility model, there is not by-pass line 11a, 11b and valve 6a, 6b and 12a, 12b.
The same with the comparative examples in Fig. 1, from CO transformationreation section run out of carbon monoxide about crude synthesis gas stream and the synthetic gas of the process of enrichment hydrogen and carbonic acid gas flows through and is extracted by pipeline 8a, 8b and valve 9a, 9b, concentrate in pipeline 10, and be sent to inherently known and unshowned in the drawings other process level optional.
Equally, by shut-off valve 4a, 4b and valve 9a, 9b open normally closed valve 13 and get around whole CO transformationreation section via pipeline 10 alternatively.
The first gasifier level according to the parallel level gasifier unit of three in equipment of the present utility model in fig. 2---its correspond to above-mentioned 1/3rd throughput schemes---is during starting, and crude synthesis gas stream is completely transferred to comprise the sub-reactor 7b of 1/3rd of the whole catalyst volumes about optimal spatial speed.Thus, sub-reactor 7b automatic operation in optimal spatial speed system.
Equally, in 2/3rds throughput schemes, when two gasifier level works in three gasifier levels, crude synthesis gas stream is completely transferred to comprise the sub-reactor 7a of 2/3rds of the whole catalyst volumes about optimal spatial speed.Thus, sub-reactor 7a automatic operation in optimal spatial speed system.
Comparatively speaking, closing down the first gasifier level according to grade gasifier unit of three in equipment of the present utility model in Fig. 2 time---it corresponds to above-mentioned 2/3rds throughput schemes---, crude synthesis gas stream is completely transferred to comprise the sub-reactor 7a of 2/3rds of the whole catalyst volumes about optimal spatial speed.Closing down two gasifier levels in three grades of gasifier units time---it corresponds to above-mentioned 1/3rd throughput schemes---, crude synthesis gas stream is completely transferred to comprise the sub-reactor 7b of 1/3rd of the whole catalyst volumes about optimal spatial speed.Again, sub-reactor 7b automatic operation in optimal spatial speed system.
This starting is with to close down ultimate principle consistent with following observations: larger crude synthesis gas stream can be preferably delivered into the sub-reactor of the comparatively large vol part comprising CO transformation catalyst, and less crude synthesis gas stream can be transported to the sub-reactor of the smaller size smaller part comprising CO transformation catalyst.Advantage is, single reformer level in multistage reformer and/or gasifier device and/or gasifier level are started or the starting of closing down and closing in stop scheme in succession, and the situation being all sent to identical catalyst volume with the crude synthesis gas of deviation ratio as being filled with large discharge or low discharge in the arrangement of the catalyzer of identical amount symmetrically at two sub-reactors of the design load of optimal spatial speed is little.This causes less temperature overshoot and thus causes thermal stresses less in catalyzer and reactor material.
In the following table, different choice and the scheme of distributing crude synthesis gas stream to common two the CO varitron reactors forming a CO shift-converter is have collected according to the quantity of the gasifier level of work.Technician will be appreciated that as above 1/3rd and 2/3rds throughput schemes also realize by such as partly reducing by variable valve 4a, 4b one or two the flow led in sub-reactor in parallel.Be expressed as in table and select these selections of A1, B1 and B2 such as to may be used for wherein needing remove a reactor or make in its out-of-work situation.But, selection A2, B3 and C1 of the operator scheme that in context of the present utility model, obviously indicating underscore and correspond to wherein catalyst bed loading coefficient in preferred employing table is 0 and/or 1---namely corresponding sub-reactor reception zero flow or all flow---.
Table: two CO varitron reactors in parallel to formation the one CO shift-converter distribute the different choice of crude synthesis gas flow
Industrial usability
The utility model proposes and run out of carbon monoxide but the equipment of the synthesis air-flow of the process of enrichment hydrogen and carbonic acid gas for crude synthesis gas circulation being turned to.Compared with prior art, the equipment proposed is more flexible with regard to the transformation in upstream synthetic gas generation equipment such as multistage reformer and/or gasifier device.One CO shift-converter asymmetric two or more sub-reactors with different catalysts volume that are divided on the flow direction of crude synthesis gas stream allow in the starting of each synthetic gas generation level or the larger handiness during closing down, with the work of best or almost best space velocity system in each catalyst bed simultaneously in CO varitron reactor.
List of numerals
[1] pipeline
[2] heat exchanger
[3] pipeline
[4a, 4b] valve
[5a, 5b] pipeline
[6a, 6b] valve
[7a, 7b] CO varitron reactor
[8a, 8b] pipeline
[9a, 9b] valve
[10] pipeline
[11a, 11b] pipeline
[12a, 12b] valve
[13] valve.
Claims (7)
1., for the production of an equipment for the synthetic gas of the process containing carbonic acid gas and hydrogen, described equipment comprises with lower unit:
(a) at least one gasifier level of obtained crude synthesis gas stream or at least one reformer level,
B CO transformationreation section that () is connected with at least one gasifier level described or reformer level fluid, described CO transformationreation section at least comprises the first shift-converter comprising transformation catalyst, described CO transformationreation section is suitable for the synthesis air-flow crude synthesis gas be under CO conversion condition circulation being turned to the process be under CO conversion condition
(c) device of synthesis air-flow for crossing from described CO transformationreation section extraction process,
The feature of described equipment is, described first shift-converter comprises the sub-reactor of at least two parallel runnings, and wherein said at least two sub-reactors comprise the described transformation catalyst of different volumes.
2. equipment according to claim 1, it is characterized in that, described first shift-converter is made up of the sub-reactor of two parallel runnings, and the catalyst volume in wherein said two sub-reactors exists with the ratio of 2/3rds in three/a pair second sub-reactors in a sub-reactor.
3. equipment according to claim 2, is characterized in that, described equipment comprises the gasifier level of multiple series connection and/or parallel running.
4. equipment according to claim 3, is characterized in that, described equipment comprises three gasifier levels.
5. equipment according to claim 2, is characterized in that, described equipment comprises the reformer level of multiple series connection and/or parallel running.
6. equipment according to claim 5, is characterized in that, described equipment comprises three reformer levels.
7. equipment according to any one of claim 1 to 6, is characterized in that, described at least two the sub-reactors in described first shift-converter are adiabatic reactor.
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
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CN201520116309.7U CN204689634U (en) | 2014-03-05 | 2015-02-26 | For the production of the equipment of the synthetic gas of the process containing carbonic acid gas and hydrogen |
AU2015226629A AU2015226629B2 (en) | 2014-03-05 | 2015-03-04 | Process and plant for performing CO shift |
PCT/CN2015/073621 WO2015131818A1 (en) | 2014-03-05 | 2015-03-04 | Paint formulation and process of making thereof |
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CN2014072939 | 2014-03-05 | ||
CN201520116309.7U CN204689634U (en) | 2014-03-05 | 2015-02-26 | For the production of the equipment of the synthetic gas of the process containing carbonic acid gas and hydrogen |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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CN105084313B (en) * | 2014-03-05 | 2018-10-09 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for executing CO transformation |
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Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
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CN105084313B (en) * | 2014-03-05 | 2018-10-09 | 乔治洛德方法研究和开发液化空气有限公司 | Method and apparatus for executing CO transformation |
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AV01 | Patent right actively abandoned |
Granted publication date: 20151007 Effective date of abandoning: 20181009 |
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AV01 | Patent right actively abandoned | ||
AV01 | Patent right actively abandoned |