CN110845304A - Method and device for co-production of methanol from melamine tail gas and application of method and device - Google Patents
Method and device for co-production of methanol from melamine tail gas and application of method and device Download PDFInfo
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- CN110845304A CN110845304A CN201911218662.5A CN201911218662A CN110845304A CN 110845304 A CN110845304 A CN 110845304A CN 201911218662 A CN201911218662 A CN 201911218662A CN 110845304 A CN110845304 A CN 110845304A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/12—Separation of ammonia from gases and vapours
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Abstract
The invention provides a method and a device for co-producing methanol from melamine tail gas and application thereof, relating to the technical field of chemical industry, wherein the method for co-producing methanol from melamine tail gas comprises the following steps: carrying out ammonia-carbon separation on the melamine tail gas to obtain carbon dioxide and liquid ammonia; the carbon dioxide reacts with hydrogen to produce methanol. The method is simple and convenient to operate, easy to realize, low in energy consumption and cost, and can fully utilize the melamine tail gas.
Description
Technical Field
The invention relates to the technical field of chemical industry, in particular to a method and a device for co-producing methanol from melamine tail gas and application of the method and the device.
Background
At present, when melamine is prepared, a large amount of carbon dioxide is contained in tail gas, the tail gas is discharged after being treated, energy waste is caused, the environment can be greatly harmed, and the rapid development of modern industry enables the emission of the carbon dioxide to be larger and larger. The existing method for treating the melamine tail gas cannot completely remove the carbon dioxide or consumes too much energy, has complex treatment procedures and higher cost, and cannot meet the requirement of treating the melamine tail gas.
In view of the above, the present invention is particularly proposed.
Disclosure of Invention
The invention aims to provide a method for co-producing methanol from melamine tail gas, which is simple and convenient to operate, easy to realize, low in energy consumption and cost and capable of fully utilizing the melamine tail gas.
The method for co-producing methanol from melamine tail gas comprises the following steps:
step a): carrying out ammonia-carbon separation on the melamine tail gas to obtain carbon dioxide and liquid ammonia;
step b): the carbon dioxide reacts with hydrogen to produce methanol.
Further, the pressure of the carbon dioxide obtained after ammonia-carbon separation is 1.5-2.5 MPa;
preferably, the temperature of the carbon dioxide obtained after ammonia-carbon separation is 60-80 ℃;
preferably, the ratio of the pressure of the carbon dioxide obtained after ammonia-carbon separation to the pressure during the reaction is 2-4;
preferably, the reaction is carried out with a molar ratio of hydrogen to carbon dioxide of from 2 to 5: 1;
preferably, the temperature of the reaction is 190-270 ℃;
preferably, the pressure of the reaction is 3-10 MPa;
preferably, the volume space velocity of the reaction is 3000-10000h-1。
Further, the reaction is carried out after preheating the mixture of carbon dioxide and hydrogen;
preferably, the temperature of the preheating is 80-130 ℃.
Further, condensing a product obtained by the reaction to obtain the methanol;
preferably, condensing the product obtained by the reaction by using the liquid ammonia;
preferably, the temperature of the liquid ammonia is 60-80 ℃, and the pressure is 1.5-2.5 MPa;
preferably, after condensing the product obtained by the reaction, the liquid ammonia is gasified into ammonia gas, and the ammonia gas is mixed with the melamine tail gas in the step a) to perform ammonia-carbon separation.
Further, after the product obtained by the reaction is condensed, gas-liquid separation and rectification are sequentially carried out to obtain the methanol;
preferably, the preheating is performed by mixing the gas obtained after the gas-liquid separation with carbon dioxide obtained after ammonia-carbon separation.
A device for co-producing methanol from melamine tail gas comprises:
the ammonia-carbon separation device comprises a melamine tail gas inlet, a liquid ammonia outlet and a carbon dioxide outlet;
the reactor comprises a raw material inlet and a product outlet, and the raw material inlet is communicated with the carbon dioxide outlet;
wherein hydrogen enters the reactor from the feed inlet and the methanol exits from the product outlet;
preferably, the reactor comprises a fixed bed reactor.
Further, still include:
the preheater comprises a carbon dioxide inlet, a hydrogen inlet and a mixed gas outlet, wherein the carbon dioxide inlet is communicated with the carbon dioxide outlet, and the mixed gas outlet is communicated with the raw material inlet.
Further, still include:
the condenser comprises a heat medium inlet, a heat medium outlet, a cold medium inlet and a cold medium outlet, the heat medium inlet is communicated with the product outlet, and the cold medium inlet is communicated with the liquid ammonia outlet;
preferably, the ammonia-carbon separation device further comprises a first inlet, and the first inlet is communicated with the cold medium outlet.
Further, still include:
the gas-liquid separator comprises a mixture inlet, a gas outlet and a liquid outlet, and the mixture inlet is communicated with the heat medium outlet;
the rectifying tower comprises a feeding hole and a discharging hole, and the feeding hole is communicated with the liquid outlet;
preferably, the preheater further comprises a second inlet in communication with the gas outlet.
Use of a device as hereinbefore described for the production of methanol.
Compared with the prior art, the invention can at least obtain the following beneficial effects:
the invention creatively utilizes the melamine tail gas to produce the methanol, and can fully utilize the carbon dioxide (CO) in the melamine tail gas2) Realizing CO in the melamine tail gas2Zero emission of CO, and2convenient source and low cost of raw materials, so that the carbon dioxide can be utilized with higher added value, and CO is utilized2The consumption of fossil resources can be reduced by producing the methanol, the sustainable utilization of carbon resources is improved, and the influence on the environment is reduced; in addition, the liquid ammonia obtained by separation can be used for producing downstream products according to requirements, and the utilization rate of ammonia in the melamine tail gas is improved. Moreover, the method of the invention has the advantages of simple and convenient operation, easy realization and lower cost.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.
FIG. 1 is a schematic structural diagram of a device for co-producing methanol from melamine off-gas in one embodiment of the present invention;
fig. 2 is a schematic structural diagram of a device for co-producing methanol from melamine off-gas in another embodiment of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
In one aspect of the present invention, the present invention provides a method for co-producing methanol from melamine tail gas, comprising:
step a): carrying out ammonia-carbon separation on the melamine tail gas to obtain carbon dioxide and liquid ammonia;
step b): the carbon dioxide reacts with hydrogen to produce methanol.
The invention creatively utilizes the melamine tail gas to produce the methanol, and can fully utilize the carbon dioxide (CO) in the melamine tail gas2) Realizing CO in the melamine tail gas2Zero emission of CO, and2convenient source and low cost of raw materials, so that the carbon dioxide can be utilized with higher added value, and CO is utilized2The consumption of fossil resources can be reduced by producing the methanol, the sustainable utilization of carbon resources is improved, and the influence on the environment is reduced; in addition, the liquid ammonia obtained by separation can be used for producing downstream products according to requirements, and the utilization rate of ammonia in the melamine tail gas is improved. Moreover, the method of the invention has the advantages of simple and convenient operation, easy realization and lower cost.
The melamine off-gas refers to off-gas generated during the production of melamine, and the off-gas contains ammonia, carbon dioxide and N2And other small amounts of impurity gases, will not be redundantly described here.
In some embodiments of the invention, the pressure of the carbon dioxide obtained after ammonia-carbon separation is 1.5 to 2.5MPa (e.g., 1.5MPa, 1.7MPa, 2MPa, 2.2MPa, 2.4MPa, or 2.5MPa, etc.). Therefore, the pressure difference between the pressure of the carbon dioxide and the pressure during reaction is favorably reduced, energy is favorably saved, and the investment is reduced.
The carbon dioxide used in the prior art for the production of methanol is generally the tail gas, CO, obtained after the combustion of fossil fuels2Under normal pressure, the compression ratio with the pressure during the reaction is large (specifically can reach 30-100), and the required methanol can be obtained only by extremely high energy consumption.
In some embodiments of the present invention, the temperature of the carbon dioxide obtained after ammonia-carbon separation is 60-80 ℃ (for example, 60 ℃, 70 ℃, or 80 ℃ may be used). Thereby facilitating the subsequent reaction.
In some embodiments of the present invention, the ratio of the pressure of the carbon dioxide obtained after ammonia-carbon separation to the pressure during the reaction is 2 to 4 (e.g., 2, 2.5, 3, 3.5, or 4). Therefore, the method is favorable for saving energy consumption and reducing investment.
In some embodiments of the invention, the reaction is carried out with a molar ratio of the hydrogen to the carbon dioxide of from 2 to 5: 1 (e.g., 2: 1, 3: 1, 4: 1, or 5: 1, etc.). When the molar ratio of the hydrogen to the carbon dioxide is too small, incomplete reaction can be caused, and the utilization rate of the carbon dioxide is low; when the molar ratio of hydrogen to carbon dioxide is too large, other side reactions may result.
In some embodiments of the invention, the reaction temperature is 190--1(for example, 3000h can be used)-1、5000h-1、7000h-1、9000h-1Or 10000h-1Etc.). Thereby, the reaction rate is increased to improve the yield of methanol.
In some embodiments of the invention, the reaction is carried out after preheating the mixture of carbon dioxide and hydrogen at a temperature of 80-130 ℃ (e.g., 80 ℃, 90 ℃, 100 ℃, 110 ℃, 120 ℃, 130 ℃, etc.). When the preheating temperature is too high, the steam energy consumption is increased, so that the cost is increased, and when the preheating temperature is too low, the carbon dioxide temperature cannot reach the required temperature, and the carbon dioxide needs to be heated again before entering the reactor, so that the energy consumption is increased.
In some embodiments of the invention, the product resulting from the reaction is condensed to provide the methanol; preferably, the product obtained from the reaction is condensed using the liquid ammonia. Therefore, the energy is fully utilized, the energy consumption is further saved, and the cost is reduced.
It will be appreciated that the liquid ammonia obtained after ammonia-carbon separation may be used partly for said condensation and partly for the production of downstream products.
In some embodiments of the invention, the liquid ammonia has a temperature of 60 to 80 ℃ and a pressure of 1.5 to 2.5 MPa. Therefore, the condensation effect is better.
In some embodiments of the invention, after condensation of the products obtained from the reaction, the liquid ammonia is gasified into ammonia gas, and the ammonia gas is mixed with the melamine off-gas in step a) to carry out the ammonia-carbon separation. Therefore, the ammonia gas and the energy are fully utilized, the energy consumption is saved, and the cost is reduced.
In some embodiments of the present invention, after the condensation, the product obtained from the reaction is subjected to gas-liquid separation and rectification sequentially to obtain the methanol. Therefore, the methanol with higher purity is favorably obtained.
In some embodiments of the present invention, the preheating is performed by mixing the gas obtained after the gas-liquid separation with carbon dioxide obtained after ammonia-carbon separation. Therefore, the method is beneficial to fully utilizing energy and reducing the emission of carbon dioxide so as to realize zero emission of the carbon dioxide.
It is understood that the gas obtained after the gas-liquid separation may contain carbon dioxide, carbon monoxide, hydrogen, and the like, which include carbon dioxide and hydrogen that do not react completely during the reaction, and may also include byproducts generated during the reaction, and the like, which are not described in detail herein.
In another aspect of the present invention, the present invention provides an apparatus for co-producing methanol from melamine off-gas, and referring to fig. 1, the apparatus comprises:
an ammonia-carbon separation device 100, wherein the ammonia-carbon separation device 100 comprises a melamine tail gas inlet 110, a liquid ammonia outlet 120 and a carbon dioxide outlet 130;
a reactor 200, said reactor 200 comprising a feedstock inlet 210 and a product outlet 220, said feedstock inlet 210 in communication with said carbon dioxide outlet 130;
wherein hydrogen enters the reactor 200 from the feedstock inlet 210 and the methanol exits from the product outlet 220.
It should be noted that all parameters and conditions in the ammonia-carbon separation apparatus correspond to the aforementioned ammonia-carbon separation, and all parameters and conditions in the reactor correspond to the aforementioned reaction.
In some embodiments of the present invention, the reactor comprises a fixed bed reactor, which may contain a catalyst used in the conventional production of methanol, and will not be described in detail herein.
In some embodiments of the invention, referring to fig. 2, the apparatus further comprises:
a preheater 300, said preheater comprising a carbon dioxide inlet 310, a hydrogen inlet 320 and a mixture outlet 330, said carbon dioxide inlet 310 being in communication with said carbon dioxide outlet 130, said mixture outlet 330 being in communication with said feedstock inlet 210. Thus, the hydrogen and the carbon dioxide can be mixed and preheated in the preheater and then jointly flow out of the mixed gas outlet and pass into the reactor.
It should be noted that all parameters and conditions in the preheater correspond to the preheating described above.
In some embodiments of the present invention, referring to fig. 2, further comprising:
a condenser 400, wherein the condenser 400 comprises a heat medium inlet 410, a heat medium outlet 420, a cold medium inlet 430 and a cold medium outlet 440, the heat medium inlet 410 is communicated with the product outlet 220, and the cold medium inlet 430 is communicated with the liquid ammonia outlet 120. Therefore, the liquid ammonia separated by the ammonia-carbon separation device can be used for condensing the products obtained by reaction, and energy is saved.
It will be appreciated that the liquid ammonia may be used partly for condensation and partly for production of downstream products, and will not be described in any greater detail here.
The heat medium refers to a medium to be cooled, and in the present invention, the heat medium refers to a product obtained in a reactor; the cold medium refers to a medium for cooling the heat medium, and in the present invention, the cold medium may be condensed water or liquid ammonia as described above.
It is to be noted that all parameters and conditions in the condenser correspond to the condensation described above.
In some preferred embodiments of the present invention, referring to fig. 2, the ammonia-carbon separation device 100 further includes a first inlet 140, and the first inlet 140 is in communication with the cooling medium outlet 440. From this, liquid ammonia exerts the condensation effect after owing to absorbed the heat and gasify for the ammonia, lets in the ammonia carbon separator with the ammonia and does benefit to and convert ammonia into liquid ammonia again, does benefit to the energy saving.
In some embodiments of the present invention, referring to fig. 2, further comprising:
a gas-liquid separator 500, the gas-liquid separator 500 including a mixture inlet 510, a gas outlet 520, and a liquid outlet 530, the mixture inlet 510 communicating with the heat medium outlet 420;
the rectifying tower 600 comprises a feeding hole 610 and a discharging hole 620, wherein the feeding hole 610 is communicated with the liquid outlet 530. Therefore, the methanol with higher purity is favorably obtained.
It should be noted that all the parameters and conditions in the gas-liquid separator correspond to the gas-liquid separation described above; all parameters and conditions in the rectification column correspond to the rectification described above.
In some preferred embodiments of the present invention, referring to fig. 2, the preheater 300 further includes a second inlet 340, and the second inlet 340 communicates with the gas outlet 520. Therefore, the gas separated from the gas-liquid separator can be re-fed into the preheater for heating, so that the raw materials are fully utilized, and the emission of carbon dioxide can be reduced.
It should be noted that the above-mentioned components may be communicated with each other through a pipe, for example, the second inlet 340 may be communicated with the gas outlet 520 through a pipe disposed between the second inlet 340 and the gas outlet 520 to communicate the second inlet 340 with the gas outlet 520.
In some embodiments of the present invention, a specific process for producing methanol by using the above apparatus for co-producing methanol from melamine off-gas may be as follows:
the melamine tail gas enters the ammonia-carbon separation device 100 through the melamine tail gas inlet 110, the melamine tail gas is separated into liquid ammonia and carbon dioxide in the ammonia-carbon separation device 100, the liquid ammonia flows out from the liquid ammonia outlet 120, one part of the liquid ammonia is used for producing downstream products, the other part of the liquid ammonia is used for subsequent condensation, and the carbon dioxide flows out from the carbon dioxide outlet 130;
carbon dioxide enters the preheater 300 through the carbon dioxide inlet 310, hydrogen enters the preheater 300 from the hydrogen inlet 320 to be mixed with the carbon dioxide for preheating, and the preheated mixed gas flows out from the mixed gas outlet 330;
the preheated mixed gas enters the reactor 200 through the raw material inlet 210, carbon dioxide and hydrogen react in the reactor 200 to generate mixed gas containing methanol, and the mixed gas containing methanol flows out through the product outlet 220;
the mixed gas containing methanol enters the condenser 400 through the heat medium inlet 410, the liquid ammonia enters the condenser 400 through the cold medium inlet 430 to condense the mixed gas containing methanol, during the condensation process, the liquid ammonia absorbs heat and is gasified into ammonia gas, the ammonia gas is discharged through the cold medium outlet 440, then enters the ammonia-carbon separation device 100 through the first inlet 140 to continuously participate in ammonia-carbon separation to obtain liquid ammonia, and the condensed mixed gas containing methanol is discharged through the heat medium outlet 420; the condensed mixed gas containing the methanol is a gas-liquid mixture, wherein the methanol is condensed into liquid and can be subjected to gas-liquid separation;
the condensed mixed gas containing methanol enters a gas-liquid separator 500 through a mixture inlet 510, the gas obtained after gas-liquid separation is discharged through a gas outlet 520 and enters a preheater 300 through a second inlet 340 to continuously participate in the subsequent reaction, the liquid containing methanol obtained after gas-liquid separation is discharged through a liquid outlet 530, and the methanol concentration in the liquid containing methanol is not particularly high, so that the liquid containing methanol can be rectified to obtain methanol with higher purity;
the liquid containing methanol enters the rectifying tower 600 through the feeding port 610, and is rectified to obtain methanol (refined methanol) with higher purity, and the methanol with higher purity is discharged through the discharging port 620.
In a further aspect of the invention, there is provided the use of an apparatus as hereinbefore described for the production of methanol.
Some embodiments of the present invention will be described in detail below with reference to specific examples. The embodiments described below and the features of the embodiments can be combined with each other without conflict.
Examples
Example 1
The method for co-producing methanol from melamine tail gas comprises the following steps:
(1) the melamine tail gas is used as a raw material and is introduced into an ammonia-carbon separation device to remove NH contained in the tail gas3And CO2Carrying out separation;
(2) the liquid ammonia separated by the ammonia-carbon separation device has the temperature of 70 ℃ and the pressure of 1.8MPa, one part of the liquid ammonia is used for producing downstream products, and the other part of the liquid ammonia enters a condenser to cool the downstream products. CO separated by ammonia-carbon separation unit2The temperature is 70 ℃ and the pressure is 1.8MPa, and the CO is added2And H2According to a molar ratio of 1: 3, then sending the mixture into a preheater to preheat to 110 ℃, and then setting the space velocity at 4000h-1And introducing into a fixed bed reactor added with a copper-based catalyst, wherein the temperature of the reactor is 250 ℃ and the pressure of the reactor is 5MPa, and fully reacting to obtain crude methanol gas. The crude methanol gas is cooled by the heat absorbed by the liquid ammonia separated by the ammonia-carbon separation device in the condenser, the liquid ammonia is gasified and then returns to the ammonia-carbon separation device for reuse, and the crude methanol gas is changed into a gas containing crude products of methanol, water and CO2CO and H2The gas-liquid mixture of (a);
(3) gas-liquid mixture passing through gas-liquidSeparating with a separator to remove unreacted CO2CO and H2And returning to the preheater for reutilization, and rectifying the crude product methanol and water in a rectifying tower to obtain refined methanol.
Example 2
The method for CO-producing methanol from melamine tail gas is the same as that in example 1, except that CO is used2And H2Directly introducing the mixture into a reactor for reaction without preheating by a preheater.
Example 3
The method for co-producing methanol from melamine tail gas is the same as that in example 1, except that the preheating temperature is 80 ℃.
Example 4
The method for co-producing methanol from melamine tail gas is the same as that in example 1, except that the preheating temperature is 130 ℃.
Example 5
The method for co-producing methanol from melamine tail gas is the same as that in example 1, except that the preheating temperature is 60 ℃.
Example 6
The method for co-producing methanol from melamine tail gas is the same as that in example 1, except that the preheating temperature is 150 ℃.
The energy consumed and the cost to produce one kilogram of methanol in examples 1-6 are given in table 1 below:
TABLE 1
| Energy consumed/W | Cost ratio | |
| Example 1 | 1626 | 1 |
| Example 2 | 4435 | 2.73 |
| Example 3 | 1831 | 1.13 |
| Example 4 | 2034 | 1.25 |
| Example 5 | 1995 | 1.23 |
| Example 6 | 2162 | 1.33 |
Note that, the cost ratio in table 1 means: the ratio of the cost of each example to the cost of example 1, it is understood that the ratio of the cost of example 1 (the cost of producing one kilogram of methanol in example 1 is 0.7 yuan) is 1.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A method for co-producing methanol from melamine tail gas is characterized by comprising the following steps:
step a): carrying out ammonia-carbon separation on the melamine tail gas to obtain carbon dioxide and liquid ammonia;
step b): the carbon dioxide reacts with hydrogen to produce methanol.
2. The method according to claim 1, wherein the pressure of the carbon dioxide obtained after ammonia-carbon separation is 1.5-2.5 MPa;
preferably, the temperature of the carbon dioxide obtained after ammonia-carbon separation is 60-80 ℃;
preferably, the ratio of the pressure of the carbon dioxide obtained after ammonia-carbon separation to the pressure during the reaction is 2-4;
preferably, the reaction is carried out with a molar ratio of hydrogen to carbon dioxide of from 2 to 5: 1;
preferably, the temperature of the reaction is 190-270 ℃;
preferably, the pressure of the reaction is 3-10 MPa;
preferably, the volume space velocity of the reaction is 3000-10000h-1。
3. The process according to claim 1 or 2, characterized in that the reaction is carried out after preheating the mixture of carbon dioxide and hydrogen;
preferably, the temperature of the preheating is 80-130 ℃.
4. The method according to claim 3, wherein the product obtained from the reaction is condensed to obtain the methanol;
preferably, condensing the product obtained by the reaction by using the liquid ammonia;
preferably, the temperature of the liquid ammonia is 60-80 ℃, and the pressure is 1.5-2.5 MPa;
preferably, after condensing the product obtained by the reaction, the liquid ammonia is gasified into ammonia gas, and the ammonia gas is mixed with the melamine tail gas in the step a) to perform ammonia-carbon separation.
5. The method according to claim 4, wherein the product obtained by the reaction is subjected to condensation, gas-liquid separation and rectification in sequence to obtain the methanol;
preferably, the preheating is performed by mixing the gas obtained after the gas-liquid separation with carbon dioxide obtained after ammonia-carbon separation.
6. The device for co-producing the methanol from the melamine tail gas is characterized by comprising the following components:
the ammonia-carbon separation device comprises a melamine tail gas inlet, a liquid ammonia outlet and a carbon dioxide outlet;
the reactor comprises a raw material inlet and a product outlet, and the raw material inlet is communicated with the carbon dioxide outlet;
wherein hydrogen enters the reactor from the feed inlet and the methanol exits from the product outlet;
preferably, the reactor comprises a fixed bed reactor.
7. The apparatus of claim 6, further comprising:
the preheater comprises a carbon dioxide inlet, a hydrogen inlet and a mixed gas outlet, wherein the carbon dioxide inlet is communicated with the carbon dioxide outlet, and the mixed gas outlet is communicated with the raw material inlet.
8. The apparatus of claim 7, further comprising:
the condenser comprises a heat medium inlet, a heat medium outlet, a cold medium inlet and a cold medium outlet, the heat medium inlet is communicated with the product outlet, and the cold medium inlet is communicated with the liquid ammonia outlet;
preferably, the ammonia-carbon separation device further comprises a first inlet, and the first inlet is communicated with the cold medium outlet.
9. The apparatus of claim 8, further comprising:
the gas-liquid separator comprises a mixture inlet, a gas outlet and a liquid outlet, and the mixture inlet is communicated with the heat medium outlet;
the rectifying tower comprises a feeding hole and a discharging hole, and the feeding hole is communicated with the liquid outlet;
preferably, the preheater further comprises a second inlet in communication with the gas outlet.
10. Use of the apparatus of any one of claims 6 to 9 in the production of methanol.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113582201A (en) * | 2021-08-20 | 2021-11-02 | 四川金象赛瑞化工股份有限公司 | Process for recycling tail gas of cyanamide process |
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