PROCESS FOR THE PRODUCTION OF HYDROGEN

Abstract

A process for the production of hydrogen, comprising a step of reforming a carbon-containing feedstock to obtain a raw hydrogen reformed stream; a step of separating the raw hydrogen reformed stream to increment the concentration of hydrogen and separate a high concentration hydrogen stream from a recovered gas stream; a step of recirculating, in which a portion of high concentration hydrogen produced in the separating step is recirculated to the reforming step together with a steam flow.

Claims

1. A process for the production of hydrogen, comprising a step of reforming a carbon-containing feedstock to obtain a raw hydrogen reformed stream; a step of separating the raw hydrogen reformed stream to increment the concentration of hydrogen and separate a high concentration hydrogen from a recovered gas stream; a step of recirculating a portion of the high concentration hydrogen produced in the separating step to the reforming step together with a steam flow; wherein a high concentration hydrogen stream produced in the separating step is recirculated to the reforming step such that the hydrogen entering into the reforming step is greater of or equal to 50 mol % with respect to the charge to be reformed.

2. A process according to claim 1, wherein the feedstock is a feedstock from renewable sources selected in the group consisting of: alcohols, for example ethanol or glycerol; vegetable oils, such as soybean oil, palm oil, etcetera; bio-oils or pyrolysis oils.

3. A process according to claim 1, wherein the feedstock is ethanol produced from biomass.

4. A process according to claim 1, wherein the reforming step is a catalytic steam reforming step, in which the feedstock is contacted with a catalyst in the presence of steam and is subjected to reforming reactions with formation of hydrogen.

5. A process according to claim 1, wherein the separating step is performed by pressure swing adsorption on a selective adsorption porous material.

6. A process according to claim 1, wherein the recirculating step is performed by means of an ejector using as a driving fluid for recirculating hydrogen a flow of steam coming from the reforming step.

7. A process according to claim 1, comprising a gas recirculating step, in which the recovered gas stream separated in the separating step is recirculated to the reforming step.

8. A process according to claim 1, wherein the reforming step is performed under thermodynamic conditions selected so as to operate, in a C—O—H ternary plot expressed in molar percentages, in a zone having H between 70 and 90%, carbon between 5 and 35%, oxygen between 10 and 40%.

9. A process according to claim 1, wherein the portion of the high concentration hydrogen from the separating step which is recirculated to the reforming step is selected so as to result in a dry fraction of hydrogen entering into the reforming step greater of or equal to 50%, preferably greater of or equal to 60%, preferably greater of or equal to 70% or more, in moles with respect to the feedstock to be reformed supplied to the reforming step.

10. A process according to claim 1, wherein when the process is in steady operation, i.e. after transitory steps of initiating and triggering the reforming reactions, the steam reforming step is performed only with the steam already present and used in the process without supplying steam from the outside; and without necessarily producing steam to be exported to the outside.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0023] Further features and advantages of the present invention will become clear from the following description of an exemplary and non-limiting embodiment thereof, with reference to the enclosed figures wherein:

[0024] FIG. 1 is a block diagram of an actuating plant of a hydrogen production process according to the invention;

[0025] FIG. 2 is a C—O—H ternary plot which illustrates some operative conditions selected for the process of the invention.

BEST MODE FOR CARRYING OUT THE INVENTION In FIG. 1, a plant for producing hydrogen by performing the process of the invention is indicated by 1.

[0026] The plant 1 comprises a reforming section 2 and a separating section 3, connected in series by a connecting line 4.

[0027] A feedstock to be treated, such as ethanol produced from biomasses, is supplied to the reforming section 2 through a supply line 5 and represents a charge to be reformed in the reforming section 5.

[0028] The treated feedstock (charge) may be, in addition to ethanol, another renewable feedstock, obtained from biomass or other; for example, in the process of the invention feedstocks can be used such as: alcohols (such as ethanol, glycerol, etcetera), vegetable oils (soybean oil, palm oil, etcetera), bio-oils (pyrolysis oil) and the like.

[0029] In alternative, the process of the invention can also employ hydro-carbon feedstocks, such as for example vacuum gas oil (VGO), light combustible oils, deasphalted oils (which however require preliminary treatments, in particular desulphurisation).

[0030] The reforming section 2 comprises at least a steam reforming reactor, provided with a catalyst for reforming reactions.

[0031] The feedstock is supplied to the reforming section 2 together with a steam flow, which in this case comes from an auxiliary supply line 6 which is inserted in the supply line 5 downstream of the reforming section 2, as further described hereinafter.

[0032] In the reforming section 2 the feedstock is placed in contact with the catalyst in presence of steam and it undergoes reforming reactions with hydrogen formation.

[0033] A raw hydrogen reformed stream is obtained from the reforming section 2 which is sent, through the connecting line 4, to the separating section 3, where the separating step is performed to increase hydrogen concentration.

[0034] The separating section 3 is, for example, of the pressure swing adsorption type (PSA) and therefore includes at least a PSA unit where the high pressure gas stream coming from the reforming section contacts a selective adsorption porous material.

[0035] The species captured at high pressure by the adsorption material are then released following a pressure reduction.

[0036] The separating section 3 separates a high concentration hydrogen stream, passing through a hydrogen outlet line 8, from a recovered gas stream (containing CO2, residual methane, etcetera) which is recirculated through a gas line 9 to the reforming step 2.

[0037] A high concentration hydrogen reaction leaving the separating section 3 is extracted from the hydrogen outlet line 8 and recirculated into the reforming section 2, by means of a recirculation line 10.

[0038] The recirculation line 10 is provided with an ejector 11 which uses as a driving fluid for recirculating hydrogen a flow of steam coming from the reforming step 2, extracted from the reforming section 2 by means of a steam line 12.

[0039] The ejector 11 thus has a hydrogen inlet, connected to the recirculation line 10, and a steam inlet, connected to the steam line 12, and uses kinetic energy of the steam flow (driving fluid) to drag the hydrogen stream (driven stream).

[0040] The ejector 11 has an outlet connected to the auxiliary supply line 6 that is inserted in the supply line 5 upstream of the reforming section 2 to provide steam to the reforming section.

[0041] According to the invention, the steam reforming step is performed under selected thermodynamic conditions.

[0042] In particular, in a C—O—H ternary plot (FIG. 2) expressed in molar percentages (i.e. on each side of the plot the molar percentages of the various components are reported), reforming is performed in a zone having H between 70 and 90%, carbon between 5 and 35%, oxygen between 10 and 40%.

[0043] For this purpose, a portion of high concentration hydrogen leaving the separating step (i.e. the separating section 3) is recirculated into the reforming step performed in the reforming section 2, resulting in a dry fraction of hydrogen entering into the reforming section 2 that is greater of or equal to 50%, preferably greater of or equal to 60%, preferably greater of or equal to 70% or more (molar percentages), with respect to the charge to be reformed (that is the feedstock supplied to the reforming section 2 for the reforming step). In other terms, a hydrogen stream, extracted from the separating step, is recirculated to the reforming step, such that the hydrogen entering the reforming section 2 is greater of or equal to 50%, preferably greater of or equal to 60%, more preferably greater of or equal to 70%, in moles with respect to the charge to be reformed.

[0044] The high amount of high concentration hydrogen which is extracted from the separating step and recirculated to the reforming step distinguishes the invention process from the prior art processes, where the possible recirculation of hydrogen is limited to relatively small amounts with the only purpose to hydrogenate potential olefins present in the charge and transform organic sulphur into H2S which will later be captured by a suitable equipment.

[0045] The present invention, if compared to the state of the art, implies a substantial modification of the reaction conditions and the high hydrogen content has a deep effect on the nature of the reactive system, both as regards reduction of the partial pressures of the other components in the mixture, and in particular as it promotes reactions removing carbon deposits that will inevitably form due to the reactive path of oxygenated components inevitably existing in predominant amounts in renewable feedstocks obtained from biomass.

[0046] Such effect has been examined both from a merely kinetic and thermodynamic perspective and from an experimental perspective, showing the efficacy of the proposed solution; in fact it was clearly noted that in standard conditions (fraction of hydrogen to the charge of around 20 mole %, as is typical in the prior art processes) a sudden formation of a carbon substance takes place (highlighted by a spectrographic and visual analysis) on the catalyst with a catastrophic deactivation within a few hours. By contrast, operating according to the conditions of the invention, no deactivation was noted within a range of 100 hours of continuous operation.

[0047] The process conditions of the reforming step are therefore significantly different from those of the typical reforming conditions of the prior art, as noted in the plot of FIG. 2 for comparison purposes). In FIG. 2 the potential working area for bio-derived charges according to the current state of the art (area C) is represented, while point B represents the operation for the aforesaid charges according to the present invention; it follows from FIG. 2 that point B is in conditions similar to the current state of the art for fossil mixtures that are free from oxygenated compounds (point A) making the operation far less critical from a thermodynamic perspective.

[0048] The process is advantageously performed without supplying steam from the outside, and without necessarily producing steam towards the outside.

[0049] In other words, once the process is at the operating speed (following possible transitory steps of initiation and triggering reforming reactions), the steam reforming step is performed in the reforming section 2 with only the steam already present and circulating into the plant 1, without adding steam from the outside.

[0050] The process is also advantageously performed without necessarily supplying supplementary fuel from outside.

[0051] It must be also understood that further changes and variants can be brought to the herein described and illustrated process without departing from the scope of the enclosed claims.