CN110986649A - Synthetic gas heat recovery system - Google Patents
Synthetic gas heat recovery system Download PDFInfo
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- CN110986649A CN110986649A CN201911322636.7A CN201911322636A CN110986649A CN 110986649 A CN110986649 A CN 110986649A CN 201911322636 A CN201911322636 A CN 201911322636A CN 110986649 A CN110986649 A CN 110986649A
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- Prior art keywords
- heat
- heat exchanger
- synthesis gas
- heat exchange
- integrated
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
A system for recovering heat from a hydrogen-containing synthesis gas stream is disclosed. Syngas (major components of CO and H) produced by steam Hydrocarbon reforming (SMR) Process2) The temperature is high, and the heat contained in the waste heat is recycled to save energy and improve the production efficiency. The invention discloses a plurality of heat exchange devices and gas-liquid separators which are arranged in a heat exchange sequence, and the adopted heat exchangers all integrate more than one heat exchange medium to exchange heat with synthesis gas flow in the same shell. Specifically, heat exchange means integrating the feed gas stream with boiler feed water and heat exchange means integrating demineralized water with cooling water, optionally further integrated with a gas-liquid separator. The invention can achieve the technical effects of saving the space occupied by the heat exchange equipment and increasing the heat exchange efficiency through the integrated design.
Description
Technical Field
The invention belongs to the field of synthesis gas technology, in particular to the field of synthesis gas heat recovery.
Background
Steam hydrocarbon conversion (SMR) processes involve reacting a hydrocarbon feedstock (such as natural gas, refinery gas, or naphtha) with steam at high temperature (up to about 900 ℃) and high pressure (20 to 35 bar) and in the presence of a catalyst to produce a gas mixture consisting primarily of hydrogen and carbon monoxide, commonly referred to as synthesis gas. The use of syngas to produce hydrogen is a major commercial application of SMR processes. This application typically integrates several processes: i) feed gas pretreatment, ii) reforming and heat recovery (including steam generation), iii) carbon monoxide reforming (water gas shift reaction) and iv) hydrogen purification (typically, hydrogen PSA). In the united states alone, steam methane reforming accounts for about 95% of the hydrogen produced from light hydrocarbon feedstocks.
Considerable research has focused on reducing equipment investment and operating costs in SMR processes. Since steam methane reforming is a strong endothermic reaction, the generated synthesis gas has a high temperature of 800-. Even relatively minor improvements to such a system can have a large impact on the cost and efficiency of the overall process. For example, for the economy of the process, the thermal energy of the endothermic reforming reaction is used as much as possible to heat the hydrocarbon-containing feed gas and generate steam.
CN102650501B discloses a heat exchanger suitable for a synthesis gas heat exchange system, which comprises at least four separated fluid circuits to reduce energy consumption and improve cooling efficiency of hydrogen-containing synthesis gas.
The prior art discloses devices involving only a single heat exchanger and no means for improving the overall heat exchange system from a system, global perspective.
Disclosure of Invention
Prior art systems for recovering heat from a synthesis gas stream typically include a plurality of separate and distinct heat exchangers that indirectly exchange heat from the synthesis gas stream with a single heat exchange medium, such as a feed gas stream, boiler feed water, demineralized water, cooling water, etc., to cool the synthesis gas stream to a desired temperature. The large number of heat exchangers increases cost and space.
In order to solve the above technical problems in the prior art, the present invention provides a system for recovering energy from a hydrogen-containing synthesis gas stream, comprising the following devices arranged in sequence:
a. a heat exchanger I for indirect heat exchange between the synthesis gas flow and the raw gas flow,
b. a heat exchanger II for indirect heat exchange between the synthesis gas flow and boiler feed water,
c. a deoxidation tank III for indirectly exchanging heat between the synthesis gas stream and the demineralized water and deoxidizing the demineralized water,
d. alternatively, an air cooler IV for cooling the syngas stream with ambient air,
e. a heat exchanger V for indirect heat exchange of the synthesis gas stream with demineralised water,
f. a heat exchanger VI for indirect heat exchange of the synthesis gas stream with cooling water,
g. a gas-liquid separator VII separating a condensed portion of the cooled syngas stream;
wherein at least two devices are integrated in such a way that heat exchangers I and II are integrated, and/or heat exchangers V and VI are integrated, and/or heat exchanger V, VI is integrated with gas-liquid separator VII.
In the above system, the heat exchanger comprises a plate-fin heat exchanger and/or a shell-and-tube heat exchanger and/or a spiral coil heat exchanger.
Further, when the heat exchanger V, VI is integrated with the gas-liquid separator VII to form a gas cooler, the heat exchangers V and VI are arranged horizontally or vertically in parallel in the upper space of the gas cooler, and the condensed portion of the syngas stream produced after passing through the heat exchangers V and VI is collected in the bottom space of the gas cooler.
Integrated means that at least two devices share one external housing; or further, the heat exchange devices sharing one outer shell have a uniform heat exchange structure.
Compared with the prior art, the technical scheme provided by the invention has the following advantages:
1. the integrated heat exchanger reduces the number and space occupied.
2. The modularization of the whole synthesis gas production device is more convenient.
3. In the process of integrating the heat exchanger, the cost can be reduced through proper design, and the heat exchange efficiency is improved.
Drawings
The advantages and spirit of the present invention can be further understood by the following detailed description of the invention and the accompanying drawings.
FIG. 1 is a schematic flow diagram of the prior art process for recovering heat from a hydrogen-containing synthesis gas stream;
FIG. 2 is a schematic flow diagram of the heat recovery from a hydrogen-containing synthesis gas stream provided by the present invention.
The same numbers and letters in the two figures correspond to the same streams and/or equipment.
Detailed Description
The following detailed description of embodiments of the invention refers to the accompanying drawings. However, the present invention should be understood not to be limited to such an embodiment described below, and the technical idea of the present invention may be implemented in combination with other known techniques or other techniques having the same functions as those of the known techniques.
In the following description of the embodiments, for purposes of clearly illustrating the structure and operation of the present invention, directional terms are used, but the terms "front", "rear", "left", "right", "outer", "inner", "outward", "inward", "axial", "radial", and the like are to be construed as words of convenience and are not to be construed as limiting terms.
In the following description of the specific embodiments, it is to be understood that the terms "length," "width," "upper," "lower," "front," "rear," "left," "right," "vertical," "horizontal," "top," "bottom," "inner," "outer," and the like are used in an orientation or positional relationship indicated in the drawings for convenience in describing the invention and to simplify the description, but are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are not to be construed as limiting the invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically stated otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly through intervening media, either internally or in any other suitable relationship. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Unless clearly indicated to the contrary, each aspect or embodiment defined herein may be combined with any other aspect or embodiments. In particular, any feature indicated as being preferred or advantageous may be combined with any other feature indicated as being preferred or advantageous.
Steam reforming reactions of hydrocarbons, particularly methane, are typically carried out in a reformer, sometimes referred to as a reformer. A plurality of rows of catalyst tubes, sometimes referred to as reformer tubes, filled with a nickel-based reforming catalyst are disposed in an insulated housing, and a pre-reformed feed stream containing methane and steam is passed into the catalyst tubes for reforming reactions. For example, natural gas needs to be desulfurized and heated to about 450 ℃ - & gt, 500 ℃ and then sent to the pre-reformer. In the pre-converter, the preheated natural gas is converted into H2And CO2And heated to about 650 c. Steam is obtained by heating boiler feed water. The two feed streams react to obtain the main components of CO and H with the temperature of about 800-900 DEG C2The heat contained in the synthesis gas is first exchanged with the hydrocarbon-containing feed gas stream and boiler feed water to produce a preheated synthesis gasThe raw gas flow, the steam and the residual heat can be respectively used for deoxidizing softened water to obtain boiler feed water, the boiler feed water exchanges heat with heat exchange media such as air flow, softened water, cooling water or a solvent, and finally the synthesis gas flow with the temperature close to the ambient temperature is obtained and is supplied to the next process.
The heat exchanger in the invention can be selected from one or a combination of a plurality of plate-fin heat exchangers, shell-and-tube heat exchangers and/or spiral coil heat exchangers according to requirements. "integrating" multiple heat exchangers means placing multiple heat exchangers in the same housing and redesigning some parameters of the multiple heat exchangers in the process, including optionally: unifying the heat exchange structures of a plurality of heat exchangers, for example, all the heat exchange structures are of a plate-fin type or all the heat exchange structures are of a shell-and-tube type; a plurality of separated heat exchange areas are arranged in the same shell, and the heat exchange areas are horizontally arranged in parallel or in a stacked mode; arranging a plurality of separated fluid circuits in the same shell, and enabling the fluid circuits of the synthesis gas flow to be contacted with the circuits of other heat exchange media in a parallel or sequential mode; and any combination of the above. The redesigned and integrated heat exchangers can be further integrated with other devices in the system, such as a gas-liquid separator, thereby achieving the technical effects of saving space and improving efficiency.
FIG. 1 is a schematic flow diagram depicting a prior art syngas stream heat recovery system. As shown in fig. 1, after heat exchange of a synthesis gas stream 10 by a plurality of heat exchangers, a cooled synthesis gas stream 10' and condensed water 11 are obtained in a gas-liquid separator. The synthesis gas stream 10 passes sequentially through a heat exchanger I which heats an incoming feed gas stream 12 to an outgoing feed gas stream 13; a heat exchanger II that heats boiler feed water 14 to a steam stream 15; and a deoxygenation tank III that causes the demineralized water to be heated by the syngas stream for deoxygenation, the deoxygenated demineralized water being pumped by pump 30 to a suitable pressure and then being incorporated into boiler feed water stream 14 entering heat exchanger II. The syngas stream is then further cooled in air cooler IV by ambient air and then enters heat exchanger V for heat exchange with a softened water stream 16, which heated softened water stream 17 passes to deoxygenation tank III. The synthesis gas stream leaving exchanger V is further cooled in exchanger VI by a cooling water stream 18 which is correspondingly warmed to stream 19. In the last step of this heat recovery system the synthesis gas stream enters a gas-liquid separator VII, where condensed water 11 is removed from the bottom of the gas-liquid separator, mixed with a heated demineralized water stream 17 and passed to a deoxygenator tank III, and a dried cooled synthesis gas stream 10' exits from the top of the gas-liquid separator VII, where the temperature is about 50-65 ℃, suitable for further process steps such as water gas shift or hydrogen purification.
FIG. 2 depicts an exemplary embodiment of the present invention in which the synthesis gas stream 10 is subjected to a heat exchange step substantially the same as that of FIG. 1, with the primary difference being focused on the heat exchanger. In FIG. 2, the original heat exchangers I and II are integrated, and the feed gas stream 12 is heat exchanged with the synthesis gas stream in this integrated heat exchanger simultaneously with the boiler feed water 14; the original heat exchangers V and VI and the gas-liquid separator VII are integrated into a new device, namely a gas cooler, and the original heat exchangers V and VI are arranged at the upper part of the gas-liquid separation part, and can be arranged in parallel in the horizontal direction or can be arranged in a vertically stacked manner. The synthesis gas flow is respectively subjected to heat exchange with softened water and cooling water in a gas cooler, and then enters a gas-liquid separation part, wherein condensed water 11 is discharged from the bottom of the equipment, is mixed with heated softened water flow 17 and then is introduced into a deoxidation tank III, and a dried and cooled synthesis gas flow 10' leaves from the upper part of the equipment. The integration may be performed in the manner described above. Alternatively to the flow scheme shown in fig. 2, only the heat exchangers V and VI may be integrated, and the cooled synthesis gas stream may be fed to a separately provided gas-liquid separator for gas-liquid separation.
The terms "first" and "second" as used herein do not denote any order, quantity, or importance, but rather are used to distinguish one element from another, unless otherwise specified. Similarly, the appearances of the phrases "a" or "an" in various places herein are not necessarily all referring to the same quantity, but rather to the same quantity, and are intended to cover all technical features not previously described. Similarly, modifiers similar to "about", "approximately" or "approximately" that occur before a numerical term herein typically include the same number, and their specific meaning should be read in conjunction with the context. Similarly, unless a specific number of a claim recitation is intended to cover both the singular and the plural, and embodiments may include a single feature or a plurality of features.
The embodiments described in the specification are only preferred embodiments of the present invention, and the above embodiments are only used to illustrate the technical solutions of the present invention and not to limit the present invention. Those skilled in the art can obtain technical solutions through logical analysis, reasoning or limited experiments according to the concepts of the present invention, and all such technical solutions are within the scope of the present invention.
Claims (6)
1. A system for recovering heat from a hydrogen-containing synthesis gas stream comprising the following apparatus arranged in series:
a. a heat exchanger I for indirect heat exchange between the synthesis gas flow and the raw gas flow,
b. a heat exchanger II for indirect heat exchange between the synthesis gas flow and boiler feed water,
c. a deoxidation tank III for indirectly exchanging heat between the synthesis gas stream and the demineralized water and deoxidizing the demineralized water,
d. alternatively, an air cooler IV for cooling the syngas stream with ambient air,
e. a heat exchanger V for indirect heat exchange of the synthesis gas stream with demineralised water,
f. a heat exchanger VI for indirect heat exchange of the synthesis gas stream with cooling water,
g. a gas-liquid separator VII separating a condensed portion of the cooled syngas stream;
wherein at least two devices are integrated in such a way that heat exchangers I and II are integrated, and/or heat exchangers V and VI are integrated, and/or heat exchanger V, VI is integrated with gas-liquid separator VII.
2. The system of claim 1, wherein the heat exchanger comprises a plate fin heat exchanger and/or a shell and tube heat exchanger and/or a spiral coil heat exchanger.
3. A system according to claim 2, wherein the heat exchanger V, VI is integrated with the gas-liquid separator VII to form a gas cooler, the heat exchangers V and VI being arranged horizontally or vertically in parallel in the upper space of the gas cooler, and the condensed portion of the synthesis gas stream after passing through the heat exchangers V and VI is collected in the bottom space of the gas cooler.
4. A system as claimed in any one of claims 1 to 3, wherein integration means that at least two devices share an external housing.
5. A system as claimed in any one of claims 1 to 3 wherein integration means that at least two devices share an external housing and the devices have a uniform heat exchange configuration.
6. A system for recovering energy from a hydrogen-containing synthesis gas stream comprising the following apparatus arranged in series:
a. a heat exchanger I for indirect heat exchange between the synthesis gas flow and the raw gas flow,
b. a heat exchanger II for indirect heat exchange between the synthesis gas flow and boiler feed water,
c. a deoxidation tank III for indirectly exchanging heat between the synthesis gas stream and the demineralized water and deoxidizing the demineralized water,
d. alternatively, an air cooler IV for cooling the syngas stream with ambient air,
e. a heat exchanger V for indirect heat exchange of the synthesis gas stream with demineralised water,
f. a heat exchanger VI for indirect heat exchange of the synthesis gas stream with cooling water,
g. a gas-liquid separator VII separating a condensed portion of the cooled syngas stream;
wherein at least two devices are integrated in such a way that heat exchangers I and II are integrated and heat exchanger V, VI is integrated with gas-liquid separator VII.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911322636.7A CN110986649A (en) | 2019-12-20 | 2019-12-20 | Synthetic gas heat recovery system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201911322636.7A CN110986649A (en) | 2019-12-20 | 2019-12-20 | Synthetic gas heat recovery system |
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| CN110986649A true CN110986649A (en) | 2020-04-10 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113267075A (en) * | 2021-04-30 | 2021-08-17 | 镇海石化建安工程有限公司 | Heat exchange system and heat exchange process for hydrogenation process |
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Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| US6349566B1 (en) * | 2000-09-15 | 2002-02-26 | Air Products And Chemicals, Inc. | Dephlegmator system and process |
| US7553476B2 (en) * | 2003-09-29 | 2009-06-30 | Praxair Technology, Inc. | Process stream condensate recycle method for a steam reformer |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113267075A (en) * | 2021-04-30 | 2021-08-17 | 镇海石化建安工程有限公司 | Heat exchange system and heat exchange process for hydrogenation process |
| CN113267075B (en) * | 2021-04-30 | 2023-09-01 | 镇海石化建安工程股份有限公司 | Heat exchange system and heat exchange process for hydrogenation process |
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