CN2668600Y

CN2668600Y - Plate-fin type methanol vapour reforming hydrogen-making system

Info

Publication number: CN2668600Y
Application number: CNU032555253U
Authority: CN
Inventors: 陈志华; 涂善东; 王正东
Original assignee: East China University of Science and Technology
Current assignee: East China University of Science and Technology
Priority date: 2003-07-11
Filing date: 2003-07-11
Publication date: 2005-01-05
Anticipated expiration: 2013-07-11

Abstract

The utility model discloses a steam reforming hydrogen-making system, mainly comprising two plate-fin heat exchangers and a plate-fin reformer. The two plate-fin heat exchangers are mainly used for high efficiency heat transmission; wherein, the middle of one of the two plate-fin heat exchangers is provided with a connection tube which is convenient for the connection of the heat transmission passage and the heat transmission mediums of other passages. As the plate-fin reformer is mainly adopted in the utility model, and the plate-fin heat exchanger is mainly used for heat exchanging; the entire reforming system has the advantages of compact structure, convenient disassembly, and the decrease of unnecessary bulky devices such as the evaporation superheat part; besides, the occupation of space of the reforming system of the utility model and the corresponding traditional reforming system is decreased by about one-half on the condition that the amount of the produced hydrogen is unchangeable. In addition, as the plate-fin style structure is mainly adopted for the reforming system of the utility model, and the counter-flow heat exchanger (the flow direction of the heat transmission medium and the feedstock is contrary in the reforming system) is adopted; therefore, the heat-transmission efficiency is enhanced, and the heat-transmission efficiency of the entire system is higher than that of the traditional reforming system by about 2-4 times.

Description

The plate-fin hydrogen-preparing system of methanol-vapor reformation

Technical field

The present invention relates to a kind of is the novel compact plate fin reforming system of raw material reformation hydrogen production with methyl alcohol and steam.

Background technology

In order to solve problem such as the serious day by day and sustained economic development of energy shortage, environmental pollution, the exploitation of clean new and renewable sources of energy has been extremely urgent.Hydrogen Energy is as a kind of renewable energy source of cleaning, its development may bring the great change of energy structure, and it still is the low pollution of a kind of ideal or the zero automobile-used energy that pollutes at present, generally acknowledges that in the world hydrogen powered vehicle will be one of most important approach that solves urban atmospheric pollution in the near future.

The industrial hydrogen production method mainly is to be raw material with Sweet natural gas, oil and coal, at high temperature makes it with the water vapour reaction and makes, and also can carry out partial oxidation with air and make.The methanolysis steam reforming hydrogen manufacturing is the nearly twenties years hydrogen preparation techniques that grow up, and is that the hydrogen method is produced in the industry of potentialization.Compare with other hydrogen production process, have advantages such as temperature of reaction low (250 ℃-300 ℃), flow process weak point, reduced investment, energy consumption are low, non-environmental-pollution.

Methanol steam reforming method flow commonly used at present is that methyl alcohol and pure water mix and preheating, after evaporation and being heated into superheated vapour, send into reformer again, katalysis at reformer tubes internal cause catalyzer makes methyl alcohol and water vapor generation chemical reaction, produces hydrogen and carbonic acid gas and part carbon monoxide.Because the methanol recapitalization reaction is thermo-negative reaction, thermosteresis can appear in this process, reaction product is flowed through, and heat exchanger and methyl alcohol and water (raw material) carry out heat exchange and part is cooled off, this mixture sent into make water and gas delivery in the gas-liquid separator, and then with gas by the absorption of hydrogen device, with separating hydrogen gas and other product.

It is as follows that methyl alcohol and water reformation hydrogen production process mainly contain following chemical equation:

(1)

(2)

(3)

Reaction formula (1) is the steam reforming reaction of methyl alcohol, is thermo-negative reaction; The decomposition reaction of chemical equation (2) expression methyl alcohol is similarly thermo-negative reaction; Reaction formula (3) is the transformationreation of carbon monoxide, is thermopositive reaction.Above-mentioned thermo-negative reaction (1), (2) need carry out about (300 ℃) under comparatively high temps, and thermopositive reaction then can be carried out under lower temperature (about 190 ℃), and these processes all need contain the oxide compound of chromium, copper or zinc of additive as catalyzer.

Method and system about methanol steam reforming has many relevant patents, as CN1383417A, and CN1031211A etc.Relevant patent CN1239121, CN1301327 etc. are then arranged about the separation of the reaction mixture (hydrogen, water, carbonic acid gas and carbon monoxide) of reformation hydrogen production with absorbing.

Industrial, generally adopt heat exchanger to come raw material is heated, its reformer structure is comparatively complicated, causes whole reforming system structure huge, reforming reaction and thermo-efficiency, and the transfer of carbon monoxide is all not ideal enough with removal.

Summary of the invention

The utility model is for the problem that solves above-mentioned traditional structure and exist designs, and its objective is provides a kind of novel carbinol steam reformation hydrogen production system, makes whole reforming system compact construction, the heat transfer efficiencies height, and system's energy consumption reduces; And the flow velocity that can effectively utilize heat-transfer medium regulates the temperature of reformer import and export reaction product, makes that the content of carbon monoxide is controlled at lower level in the reaction product.

Novel carbinol steam reformation hydrogen production of the present utility model system mainly comprises two plate-fin heat exchangers and a plate-fin heat reformer.Two plate-fin heat exchangers are mainly used to efficient heat transfer.One of them is provided with adapter mouthful 6 heat-transfer mediums of being convenient to its heat transfer medium channels and other passage and links at the middle part.

The typical structure of plate-fin heat reformer as shown in Figure 1, reformer 104 is divided into reformation part 104a and transform portion 104b, reforming reaction passage and heat transfer medium channels are adjacent, have dividing plate 2b on the passage, channel side is provided with baffle plate 4, be provided with fin 3 in the passage, heat transfer medium channels is divided into the separate two portions in the left and right sides by dividing plate 2a, and scribbles the coating that contains catalyzer (oxide compounds such as chromium, copper or zinc) on its dividing plate 2b wall.Air flow line in the heat transfer medium channels is opposite with raw material flow direction in the reforming reaction passage, is convenient to improve heat transfer efficiency.Side 104a main generation reformation and decomposition reaction thereon because temperature is higher.Downside 104b utilizes heat-transfer medium to come regulating and controlling temperature to make it to be convenient to take place conversion reaction, to eliminate the content of carbon monoxide in the reformation part reaction product.Simultaneously can be according to the demand of actual hydrogen output, by the quantity of this structure corresponding increase reforming reaction passage and heat transfer medium channels.The typical structure of plate-fin passage as shown in Figure 2.The primary structure of plate-fin reforming heat exchanger as shown in Figure 3, its each passage is identical with the reformer structure with heat exchange mode, adopts countercurrent flow.Heat transfer medium channels middle part at interchanger 102 is provided with adapter 6, and the heat-transfer medium of being convenient to reforming reactor flows into.

Because the utility model mainly adopts plate-fin heat exchanger to carry out heat exchange, add the exploitation of plate-fin heat reformer, make whole reforming system compact construction, convenient disassembly, and reduced unnecessary bulky equipment as the evaporation superheat section, make whole reforming system of the present invention and corresponding traditional reforming system under the constant situation of hydrogen manufacturing amount, taking up an area of the space will reduce about 1/2nd.In addition, because this reforming system is based on plate-fin structure, and adopt countercurrent flow (heat-transfer medium is opposite with the flow direction of raw material in reforming system), heat transfer efficiency is improved, total system is higher 2～4 times than the heat transfer efficiency that adopts traditional reforming system.

Description of drawings

Fig. 1 is the typical structure synoptic diagram of plate-fin heat reformer.Wherein, 1-thermal insulation layer; The 2a-dividing plate; 2b-scribbles the dividing plate of catalyzer; 3-fin (position); The 4-plate washer.

Fig. 2 is the typical structure synoptic diagram of plate-fin passage.Wherein, 2b-scribbles the dividing plate of catalyzer; The 3-fin; The 4-plate washer.

Fig. 3 is the typical structure synoptic diagram of plate-fin heat exchanger.Wherein, 2b-scribbles the dividing plate of catalyzer; The 3-fin; The 4-plate washer; 6-takes over.

Fig. 4 is the embodiment schema of reforming system.

Embodiment

The specific embodiments of the utility model methanol steam reforming system is as follows:

The whole flow process of raw material in this reforming system as shown in Figure 4.Methyl alcohol and water are respectively after

pump

200 and 202 is forced into 10 normal atmosphere, enter first plate-fin heat exchanger 100 and be preheated to 140 ℃, through second interchanger 102 heating evaporation once more, make it temperature and reach superheated vapour about 300 ℃, enter the reformation part 104a of plate-fin heat reformer 104 again, under the effect of reaction channel surface catalysis agent, transform (1) and decompose (2) reaction, and with high-temperature heat-transfer medium generation heat exchange, reform and the required heat of decomposition reaction to keep it, keep the temperature of reformation part 104a constant substantially.Reaction product enters transform portion 104b and carries out transformationreation (3) then, and the carbon monoxide that decomposition reaction (2) is generated transforms, and generates hydrogen and carbonic acid gas.In this process, higher because of the reaction product temperature, add that transformationreation (3) is thermopositive reaction, so heat exchanging process is opposite with reformation part 104a, shows as high-temperature reaction product to heat transfer, the final reacting product temperature is controlled at about 190 ℃.Reaction product enters first plate-fin heat exchanger 100 and initial feed (methyl alcohol and pure water) and carries out further heat exchange with the preheating initial feed with reduce the reaction product temperature then, enter condenser 106 subsequently, with condensation moisture content wherein, enter gas-liquid separator 108 and absorbing separator 110 at last more respectively, with the water in the isolate reactant and other product, wherein the water of Sheng Chenging will be recycled, and obtain hydrogen at last.

Heat-transfer medium carries out following circulation in native system: with well heater 203 heat-transfer medium is heated to about 330 ℃, through transition pipeline and flow control valve 204 and 206, enter the reformation part 104a of plate-fin heat exchanger 102 and plate-fin heat reformer 104 respectively, carry out heat exchange at the heat-transfer medium of reformation part 104a and the methyl alcohol in the plate-fin heat exchanger 102 and pure water mixture (raw material), to supply with the required heat of reforming reaction, flow into the middle part of plate-fin heat exchanger 102 subsequently, converge with heat-transfer medium raw material is evaporated heating through flow control valve 204.Through the heat-transfer medium of flow control valve 204 then in plate-fin heat exchanger 102, from top to bottom raw material is evaporated the heat exchange of heating, and mix in the middle with through the heat-transfer medium partly of reforming, the raw material that enters plate-fin heat exchanger 102 is evaporated heating, its temperature will be reduced to about 140 ℃, enter the decomposition part 104b of reformer 104 and high-temperature reaction product generation heat exchange subsequently and be heated, enter well heater at last and further be heated to about 330 ℃, restart circulation again.

Claims

1. plate-fin hydrogen-preparing system of methanol-vapor reformation, it is characterized in that, this system mainly comprises (a) plate-fin heat reformer (104), (104a) forms with conversion (104b) two portions by reforming, the reformation hydrogen production that is used for methyl alcohol and water vapor comprises also that wherein the superheated vapour raw material decomposes and two reaction process of conversion of intermediate product are carried out Preparation of Hydrogen; (b) two plate-fin heat exchangers (100,102), one of them (100) are mainly used in by utilizing the heat transfer between high-temperature reaction product and the initial feed, and another (102) then evaporate raw material by heat-transfer medium; (c) flow control valve (204,206,208), the flow velocity of heat-transfer medium in the control carrier pipe; (d) well heater (203) is used for heating heat-transfer medium.

2. hydrogen-preparing system of methanol-vapor reformation according to claim 1 is characterized in that, reformer is a plate-fin structure, and its reforming reaction passage is adjacent with two heat transfer medium channels, has dividing plate (2b) on the passage, is provided with fin (3) in the passage; Heat transfer medium channels is divided into the separate two portions in the left and right sides by dividing plate (2a), and can increase reforming reaction passage and heat transfer medium channels according to actual needs by this structure, to increase reformation hydrogen production output.

3. hydrogen-preparing system of methanol-vapor reformation according to claim 1 is characterized in that, two interchanger (100,102) are plate-fin structure, have dividing plate (2b) on the passage, are provided with fin (3) in the passage.

4. hydrogen-preparing system of methanol-vapor reformation according to claim 1 is characterized in that, plate-fin heat reformer (104) and the size of interior each passage of interchanger (100,102) and the form of length and fin can be decided according to the actual requirements.

5. hydrogen-preparing system of methanol-vapor reformation according to claim 1 is characterized in that, is provided with adapter (6) at the middle part of second plate-fin heat exchanger (102), and the heat-transfer medium of being convenient to reformer reformation part flows into and converges.

6. hydrogen-preparing system of methanol-vapor reformation according to claim 1, it is characterized in that, wherein carrier pipe is transported to the reformation part (104a) of reformer respectively with heat-transfer medium and is used for evaporating second interchanger (102) of raw material, regulates two-part temperature respectively with flow control valve (204,206); Enter the heat-transfer medium of reformer (104), sent back to second interchanger (102) middle part after conducting heat with the reforming reaction raw material, converge with another part.

7. hydrogen-preparing system of methanol-vapor reformation according to claim 1 is characterized in that, the heat transfer of reformer transform portion (104a) is to carry out between the heat-transfer medium of pyroreaction thing and second interchanger (102) inflow; First heat transmitter (100) then is to carry out between the reaction product that initial feed and reformer conversion portion come out.

8. hydrogen-preparing system of methanol-vapor reformation according to claim 1 is characterized in that, scribbles catalyzer on the reforming reaction channel partition (2b) of its reformer (104).